User Guide

PRO/II 8.3 USER GUIDE

License and Copyright Information PRO/II 8.3 User Guide

The software described in this guide is furnished under a written agreement and may be used only in accordance with the terms and conditions of the license agreement under which you obtained it. The technical documentation is delivered to you AS IS and Invensys Systems, Inc. makes no warranty as to its accuracy or use. Any use of the technical documentation or the information contained therein is at the risk of the user. Documentation may include technical or other inaccuracies or typographical errors. Invensys Systems, Inc. reserves the right to make changes without prior notice.

Copyright Notice © 2009 Invensys Systems, Inc. All rights reserved. The documentation material protected by this copyright may be reproduced or utilized for the benefit and convenience of registered customers in the course of utilizing the software. Any other use or reproduction is prohibited in any form by any means, electronic or mechanical, including photocopying, recording, broadcasting, or by any information storage and retrieval system, without permission in writing from Invensys Systems, Inc.

Trademarks PRO/II and Invensys SIMSCI-ESSCOR are trademarks of Invensys plc, its subsidiaries and affiliates.

AMSIM is a trademark of DBR Schlumberger Canada Limited.

Visual Fortran is a trademark of Intel Corporation.

RATEFRAC®, BATCHFRAC®, and KOCH-GLITSCH are registered trademarks of Koch-Glitsch, LP.

Windows 98, Windows ME, Windows NT, Windows 2000, Window 2003, Windows XP, Windows Vista, and MS-DOS are trademarks of Microsoft Corporation.

Adobe, Acrobat, Exchange, and Reader are trademarks of Adobe Systems, Inc.

All other products may be trademarks of their respective companies.

U.S. GOVERNMENT RESTRICTED RIGHTS LEGEND The Software and accompanying written materials are provided with restricted rights. Use, duplication, or disclosure by the Government is subject to restrictions as set forth in subparagraph (c) (1) (ii) of the Rights in Technical Data And Computer Software clause at DFARS 252.227-7013 or in subparagraphs (c) (1) and (2) of the Commercial Computer Software-Restricted Rights clause at 48 C.F.R. 52.227-19, as applicable. The Contractor/Manufacturer is: Invensys Systems, Inc. (Invensys SIMSCI-ESSCOR) 26561 Rancho Parkway South, Suite 100, Lake Forest, CA 92630, USA. Printed in the United States of America, April 2009

Table of Contents

Chapter 1 Using PRO/II........................................................................................1 Before Starting PRO/II .....................................................................................1 Starting PRO/II..................................................................................................2 PRO/II Main Window Components.................................................................3 Using the Menus ..............................................................................................6 Using the Floating Palettes.............................................................................9 Using the Toolbar ............................................................................................9 Using the PRO/II Main Window.....................................................................14

Chapter 2 Simulation Basics ...........................................................................15 General Approach..........................................................................................15

Run the Process Simulation ........................................................................17 Analyze the Simulation Results...................................................................17

Building the Flowsheet .................................................................................17 Unit Operations............................................................................................17 Streams .......................................................................................................17

Required Data.................................................................................................18 Components ................................................................................................18 Thermodynamic Methods............................................................................18 Stream Information......................................................................................19 Unit Operations............................................................................................19

Optional Data..................................................................................................20 Miscellaneous Data .....................................................................................20 Miscellaneous Calculation Options .............................................................21 Default Data.................................................................................................23 Other Optional Data.....................................................................................23

Chapter 3 Managing Simulation Files .............................................................25 Opening a New Simulation ...........................................................................25 Opening an Existing Simulation...................................................................26 Saving the Current Simulation .....................................................................27 Closing a Simulation .....................................................................................28

Table of Contents - I

Deleting a Simulation ....................................................................................29 Copying a Simulation ....................................................................................30 Importing a PRO/II Keyword Input File ........................................................32

Keyword Features without PRO/II GUI support ..........................................33 Keyword Features Imported in “Run-Only” Mode .......................................33

Exporting Simulation Data to a File .............................................................35 Export Simulation Data to a Keyword File...................................................36 Exporting the Flowsheet Drawing to the Clipboard .....................................37 Exporting Stream or Unit Property Table Data............................................38 Exporting the PFD to an AutoCAD or PostScript File .................................39 Exporting Tag Data to a File........................................................................39

Exporting Data to Excel Using Spreadsheet Tools....................................39 Copying Property Table Data to the Clipboard...........................................40 Copying/Pasting Stream Data in an Excel Sheet........................................40

Chapter 4 Building a Flowsheet ......................................................................41 Setting Simulation Preferences....................................................................41

Setting Problem Description Global Defaults ..............................................41 Overriding the Global Default Problem Description ....................................42 Setting Units of Measure Global Defaults ...................................................43 Changing Global Units of Measure for One Simulation ..............................44 Units of Measure Library .............................................................................45 Setting Thermodynamic System Global Defaults........................................49 Changing Delete Confirmation ....................................................................50 Setting Global Flowsheet Tolerances..........................................................50

Placing a Unit on the Flowsheet...................................................................51 Drawing Streams ...........................................................................................55

Drawing a Connection .................................................................................56 Connecting Streams When One Unit is Not Visible ....................................57 Labeling a Stream .......................................................................................57 Moving Streams...........................................................................................58 Searching for a Unit or Stream....................................................................59

Changing the Flowsheet Layout ..................................................................60 Drawing Freehand Objects ...........................................................................61

Entering Text ...............................................................................................62 Drawing Lines..............................................................................................62 Drawing Shapes ..........................................................................................63 Drawing Pages ............................................................................................64

Chapter 5 Manipulating Objects ......................................................................67

II - PRO/II User Guide April 2009

Selecting Objects or Groups of Objects .....................................................67 Selecting Multiple Objects ...........................................................................67 Selecting a Group of Objects ......................................................................69

Resizing Objects............................................................................................69 Rearranging Objects or Groups of Objects ................................................71 Editing Text ....................................................................................................72

Chapter 6 Viewing Flowsheet Contents..........................................................73 Scrolling the PFD...........................................................................................73 Zooming..........................................................................................................73 Opening Multiple Viewport Windows ..........................................................75 Redrawing the Simulation.............................................................................76 Panning...........................................................................................................76 Moving the Bounding Box ............................................................................78

Chapter 7 Data Entry Windows.........................................................................79 Defining the Simulation.................................................................................79 Selecting Components..................................................................................81 Modifying Component Properties................................................................82 Selecting Thermodynamic Methods ............................................................83 Selecting Assay Data ....................................................................................84 Specifying Reaction Data..............................................................................85 Specifying Reaction Procedure Data...........................................................87 Specifying Multiple Simulations for Case Study........................................88 Setting the Problem Calculation Sequence ................................................89 Specifying Recycle Convergence ................................................................90 Data Entry Windows for Unit Operations ....................................................91

Grids and the X-Y Grid ................................................................................92

Chapter 8 Specifying Component, Thermodynamic and Stream Data........97 Component Data ............................................................................................97

Selecting Library Components ....................................................................98 Entering User-defined Components ............................................................99 Modifying Component Properties ..............................................................101 PRO/II and TDM Integration......................................................................103

Table of Contents - III

Assay Data....................................................................................................105 TBP Cut point Sets ....................................................................................107 Assay Characterization Options ................................................................108

Thermodynamic Data ..................................................................................109 Selecting Predefined Method Sets ............................................................110 User-added Thermodynamic Data ............................................................116 CAPE-OPEN Property Package................................................................116

Property Calculations..................................................................................116 Defining Transport Properties....................................................................117 Specifying Water Decant Options..............................................................118 Stream Data..................................................................................................123

Specifying Composition Defined Streams.................................................125 Specifying Stream Thermal Condition.......................................................125 Specifying Petroleum Assay Streams .......................................................126

Specifying Recycle Streams.......................................................................129 Scaling Product Streams...........................................................................131 Specifying Reference Streams..................................................................132 Copying Stream Data ................................................................................133

Refinery Inspection and User-defined Properties....................................137 Entering Refinery Inspection Properties....................................................138 User-defined Special Properties................................................................139 Entering Assay Data for Stream Special Properties .................................139 Assay Data for Refinery Inspection Properties .........................................139 Assay Data for User-defined Special Properties.......................................140

BVLE (Validating Equilibrium Data)...........................................................145

Chapter 9 Unit Operations and Utility Modules ...........................................147 Calculator .....................................................................................................148

Sample Calculator Procedures..................................................................161 CAPE-OPEN..................................................................................................166 Column, Batch..............................................................................................170 Column, Distillation .....................................................................................171

Column Algorithm......................................................................................173 Reactions...................................................................................................174 Pressure Profile .........................................................................................176 Condensers ...............................................................................................176 Reboilers ...................................................................................................178 Heaters and Coolers..................................................................................179 Flash Zones...............................................................................................179 Column Heat Leaks...................................................................................179

IV - PRO/II User Guide April 2009

Pumparounds and Vapor Bypasses..........................................................180 Initial Estimates .........................................................................................181 Homotopy Options for Convergence on Specification ..............................186 Tray Hydraulics..........................................................................................187 Column RATEFRAC® Tray Options ..........................................................187 Column RATEFRAC® Packing Options .....................................................188 RATEFRAC® Transport Calculation Methods ...........................................189 Tray Efficiencies ........................................................................................190 Side Columns ............................................................................................191 Print Options..............................................................................................191 Thermodynamic Systems..........................................................................192

Column, Liquid–Liquid Extraction .............................................................193 Column Algorithm......................................................................................194 Pressure Profile .........................................................................................195 Heaters and Coolers..................................................................................195 Initial Estimates .........................................................................................195 Performance Specifications.......................................................................196 Print Options..............................................................................................197 Thermodynamic Options ...........................................................................197

Column, Side................................................................................................199 Solution Methods.......................................................................................199

Compressor..................................................................................................203 Pressure, Work, or Head Specification .....................................................203

Controller......................................................................................................207 Crystallizer....................................................................................................211 Cyclone .........................................................................................................215 Rotary Drum Filter .......................................................................................221 Solids Dryer..................................................................................................223 Depressuring Unit........................................................................................226 Dissolver.......................................................................................................231 Excel Unit......................................................................................................232

Data Transfer Sheet ..................................................................................234 Expander.......................................................................................................238 Flash..............................................................................................................240 Flash With Solids.........................................................................................244 Flowsheet Optimizer....................................................................................246 Heat Exchanger, LNG..................................................................................252 Heat Exchanger, Air Cooled .......................................................................254

Table of Contents - V

Heat Exchanger, Rigorous..........................................................................256 Heat Exchanger, Simple..............................................................................266 Heating/Cooling Curves ..............................................................................270 Mixer..............................................................................................................274 Multivariable Controller...............................................................................276 Phase Envelope ...........................................................................................280 PIPEPHASE Unit Operation ........................................................................282 Pipe ...............................................................................................................286

Line/Fitting Data ........................................................................................288 Line Sizing Data ........................................................................................289

Polymer Reactor ..........................................................................................292 Procedure Data ............................................................................................294

Procedure Code ........................................................................................295 Pump.............................................................................................................302 Reaction Data...............................................................................................304 Reactor..........................................................................................................308 Conversion and Equilibrium Reactors ......................................................310 Continuous Stirred Tank Reactor ..............................................................310 Plug Flow Reactor .......................................................................................310 Boiling Pot Reactor .....................................................................................314 Gibbs Reactor ..............................................................................................316 Unit Reaction Definitions ............................................................................318 Reactor, Batch..............................................................................................323 Solid Separator ............................................................................................324 Splitter...........................................................................................................326 Stream Calculator ........................................................................................328 Specifications...............................................................................................332 VARY.............................................................................................................334 DEFINE..........................................................................................................336 User-added Unit Operations.......................................................................348

Customized UAS Data Entry Window .......................................................351 Modular User-Added Unit Operations .......................................................352

VI - PRO/II User Guide April 2009

Modular User-Added Utilities .....................................................................353 Detailed Information ..................................................................................353 Electrolytic Column Algorithm (ELDIST) ...................................................356

Simsci Add-on Modules ..............................................................................358 SIMSCI POLYMER CSTR Unit Operation ................................................358 SIMSCI COMPONENT PROPERTY REPORTER Unit Operation ...........359 SIMSCI BLEND Unit Operation.................................................................359 SIMSCI RESET Unit Operation.................................................................360 SIMSCI Profimatics Reactor Unit Operations ...........................................361

Valve..............................................................................................................362 Wiped Film Evaporator................................................................................364

Chapter 10 Running and Viewing a Flowsheet ............................................366 Using the Run Palette..................................................................................366 Checking the Simulation Status.................................................................368

Understanding the Unit Color Coding Cues ..............................................369 Running the Simulation ..............................................................................369

Stepping Through Simulation Execution ...................................................370 Stopping Simulation Execution..................................................................370 Using Breakpoints .....................................................................................371

Viewing Results ...........................................................................................372 Running a Case Study.................................................................................376

Viewing Case Study Results .....................................................................378 Running Files in Batch Mode .....................................................................378 Revising the File Execution Sequence Order ...........................................382

Creating an Execution File List..................................................................382 Executing the Batch List............................................................................383 Viewing Output Results .............................................................................383

Chapter 11 Printing and Plotting ....................................................................384 Defining Output Reports .............................................................................384 Generating a Report ....................................................................................392 Plotting..........................................................................................................393

Chapter 12 Customizing the PFD Workplace................................................398 Changing Unit Operation Styles.................................................................398

Changing the Unit Icon Globally................................................................399 Changing the Unit Icon for a Single Unit ...................................................400 Changing the Label Displayed for a Specific Unit .....................................401

Table of Contents - VII

Changing Stream Styles .............................................................................402 Changing the Global Stream Style ............................................................402 Display Stream Property Lists As Stream Labels .....................................404

Create Custom Stream Property Lists.......................................................405 Changing the Style of an Individual Stream .............................................408

Changing the ID Name of an Individual Stream........................................409 Toggle Stream Property List Button..........................................................410

Adding the Toggle Stream Button to the Tool Bar ....................................411 Customizing Stream ToolTips....................................................................412 Modifying Drawing Preferences.................................................................414 Specifying a Default Editor .........................................................................415 Changing the Default Font..........................................................................416

Index....................................................................................................................... i

VIII - PRO/II User Guide April 2009

Chapter 1 Using PRO/II This chapter describes how to start and exit PRO/II. In addition, it reviews some basic Windows features as they appear in PRO/II and briefly describes how to use them. Before Starting PRO/II If you have not yet installed PRO/II on your system, see the PRO/II PC/LAN Installation Guide. If you do not see a PRO/II icon in a SIMSCI group window or in your Program/SIMSCI Start menu, see the troubleshooting section in the PRO/II PC/LAN Installation Guide. Compatibility with Previous Versions This release of PRO/II can read simulation files created by previous versions of PRO/II. When you open a simulation file created by a previous version, the file is automatically converted to the current version, and a copy of the original file is saved under a different name. For example, if you open G3.prz that was created by PRO/II version 6, the converted file will be saved as “G3.prz” and a copy of the original file will be saved as “G3_v60.prz”.

Note: Some keyword input files created manually may include features that are not supported by the PRO/II graphical user interface. PRO/II issues a warning when this occurs. For flowsheet execution, all features will be preserved if you choose either the Read Only or Run Batch mode.

In all cases, if you subsequently export the problem, all un-supported features will be lost. The exported file will not include any of the unsupported features. Later import of an exported file will reveal that the unsupported features are missing. It is always prudent to make copies of your original files and to work only on the copies of the original files.

Chapter 1 Using PRO/II 1

Starting PRO/II

To start PRO/II:

Double-click the PRO/II icon, or launch from the Start menu. The PRO/II welcome window appears. This window contains information on

pening files and on the color codes used in the program. o

Click OK to close this window and open the PRO/II main window.

2 PRO/II User Guide April 2009

ain WindowFigure 1-2: The PRO/II M

ow open a new(select File/Open), or imp pter 3, Managing PFD Files, for ails.

PRO/II Main Wind

You can n simulation file (select File/New), open an existing file

rt a keyword file (select File/Import). See Chaoadditional det

ow Components

Component Description

Control Menu Box Displays a menu with commands for sizing, and closing the active window.

moving

Title Bar Identifies the application and the name of the open file; can be used to move the entire window.

Minimize Button Reduces the application window to an icon.

Maximize/Restore utton

a window to full screen or restores it to its default size BEnlarges


Component Description

Menu Bar Identifies the menus available in PRO/II: File, EdInput, Output, Tools, Draw, View, Options, Window and Help.

it,

Toolbar Provides push button access to various Edit, Input, Tools, View, Window, and Help options

PFD Main Window Provides a workspace for placing units, making stream connections, drawing objects, and adding text.

Horizontal Scroll Bar Functions as a sliding scale flowsheet to the right or left i

for moving the n the PRO/II main

window.

Vertical Scroll Bar Functions as a sliding scale for moving the flowsheet up or down in the PRO/II main window.

Status Bar Displays the active

help, information and error messages for feature or object.

Border Handles Changes window height, width, or size when the corresponding border handle is dragged to a new position.

Manipulating the PRO/II Window The PRO/II window offers mappearance, relative to the finstructions on use of the Wnumerous reference manual Changing Window The Windows interface prov s for resizing each window. Some tools automatically change a wind rs enable you to control the magnificat

/Maximize Buttons

any features that enable you to customize its ull screen and other applications. Detailed indows’ graphical user interface may be found in s available at any large bookstore.

Size ides toolow to a particular size and orientation; otheion.

Using Minimize

The minimize and maximize buttons automatically adjust the size of a window.


Using Border Handles You can use the window border to change the size of the main window. The

n grab with the cursor and drag to a new position.

tr

er handles, you can also enu to Restore, Move, Size,

pen the con at the

by pressing

Changing Window Position

orking with On-screen Color Coding Cues PRO/II provides the standard visual cue (grayed out text and icons) for menu items and toolbar buttons that are currently unavailable. In addition, PRO/II uses colored borders liberally to indicate the current status of the simulation. You may customize the color coding by accessing the Set Colors window by selecting

border works like a handle that you ca

Using the Con ol Menu

In addition to the borduse the Control mMinimize, or Maximize a window. OControl menu by clicking the PRO/II ifar left of the title bar or <Alt+Space>.

You can change the position of the main window (or any pop-up window) bydragging the title bar.

W

Options/Colors… from the menu bar.

PRO/II On-Screen Color Codes

Color Significance

Red Required data Actions or data required of the user

Green Optional or default data

Blue Data supplied by user

Yellow Questionable data. A warning that the value supplied by user is outside the normal range.

Gray Data field not available to user

Black Data entry not required


Using the Menus The names of the PRO/II main menus appear on the menu bar. Use these menus to access most PRO/II operations.

Figure 1-3: File Menu

Figure 1-4: Edit Menu


Figure 1-6: Output Menu

Figure 1-5: Input Menu

Figure 1-7: Tools Menu


Figure 1-8: Draw Menu

Figure 1-10: Options Menu

Figure 1-9: View Menu

Figure 1-12: Help Menu

Figure 1-11: Window Menu


Using the Floating Palettes There are two floating palettes. The first c it operations and streams

t a flowshe

View/Palettes from th

ontains the unneeded to construcsimulation. These pa

et. The second contains controls used to run the lettes may be displayed or hidden by selecting e menu bar.

Menu Item Description

View/Palettes/PFD Checking this option displays the PFD palette ng unit operations and streams (also known treams/Unit palette).

containias the S

View/Palettes/Run Allows running the simulation and viewing results. This button is not initially visible on the tool bar.

sing the Toolbar U

Toolbar ilable from the menus on the menu bar. Sim unction. Hovering the mouse cursor over a butt w PRO/II is fi any others are available.

s (Input, Component Selection, etc.)

n, Find Unit, Find Stream)

• Help button

Using the PFD Palette Button his button is a toggle that hides or displays the floating PFD palette.

buttons duplicate options avaply click a button to perform its fon ithout clicking displays a tool tip that identifies the button. Whenrst installed, several groups of buttons are visible. M

• New, Open, Save, and Print Show or Hide PDF Pa• lette

w button• Data Entry Windo• Navigation Aids (Pa• VLE Tool buttons • Run/Results buttons • Delete and View buttons

T

Button Menu Item Description

View/Palettes/PFD Displays or hides the PFD palette.


Using t

he D indow Buttons

Each Dat buttonwindo fo d section

ata Entry W

a Entry Windowr the selecte

provides quick access to the main data entry of input. w


Input/Problem Description

Describes the current simulation and relates it to a specific project.

Input/Units of

extracts defaults from the default Unit of Measure Set.

Measure Sets units of measure specific to this simulation. Each new simulation

Input/ComponeSelection

nt current simulation.

Specifies the components and pseudo components for the

Input/CompoProperties

nent Supplies component properties.

Input/Thermo- ic methods for the dynamic Data

Selects thermodynamcurrent simulation.

Input/Assay Characterization

ation g pseudo components

Modifies TBP cut points and characterizoptions for generatinfrom Assay streams.

Input/Reaction Data n, equilibrium, or kinetic data for

Defines reactions and provides heat of reactioreaction sets.

Input/Procedure Data

ure der to calculate kinetic reaction

Use this window to create or delete Procedblocks in orrates.

Input/Casestudy s to perform studies on a base Data

Allows usercase solution by altering parameters and rerunning.

Input/Calculation Sequence

Specifies a user-defined calculation sequence.

Convergence and aInput/Recycle Specifies user-defined recycle convergence

cceleration options.


Using Navigation Aid Buttons

o but you to jump to a se tream. PRO/II repositions pla r of the main window. The Find Stream it buttons open windows that allow direct data en w of output re or unit.

The Go T tons enable lected unit or s

the flowsheet to ce the selected unit or stream at the cente and Find Un

try and revie sults for the selected stream


View/Pan View Allows quick panning through the entire

flowsheet.

View/Unit List nt

flowsheet. By selecting a name, you can jump directly to that unit.

Displays a list of units in the curre

View/Stream List Displays a list of streams in the current

flowsheet. By selecting a name, you can jump directly to that stream.

Tools Buttons The V T ble ., flash, a stream highli PFD usi

Using VLE

LE ools buttons enaghted on the

you to perform simulation functions, e.gng the Flash Hot-key.


Tools/Flash Stream

Flashes the stream highlighted on the PFD. (Also called the Flash Hot-key)

Tools/Binary VLE Generates plots and tables of K-values

and fugacity coefficients for binary pairs of components.

Usin esults BThe Run/Results button lation floating palette. They allow you to run, stop a sim ing results and generate output reports. T Generate Output n Output menu item.

g Run/R uttons s duplicate functions on the Run Simu

ulation or permit viewhe button duplicates a



-------- Runs the simulation

-------- Stops the simulation

Output/Data

he d PFD item.

Review Window First, select any stream or unit on the PFD. Pressing this button displays tresults of the selecte

-------- View Text Results Window. First, solv

a simulation; then select any stream ounit on t

e r

he PFD. Pressing this button displays results for the selected item similar to how they would appear in the complete output text report.

Output/Generate Generates an output report for the Text Report simulation problem.

-------- Select Active report allows choosing

which pre-defined report is currently active.

-------- Generate ort suitable for s an output repviewing by using Microsoft Excel

Using e uttoPRO/I ro ton a at facilitate ed th availa le o me

DI p

lete and View Bvides a Delete but

ns nd a set of View buttons on the toolbar th

iting and viewing ofn the Edit and View

e flowsheet. These buttons duplicate itemsnus. b


Edit/Delete or <Delete>

Deletes the currently selected object(s) from the flowsheet.

Input/Toggle Stream Property List

User can select a particular stream propertytable as the toggle stream property list.

View/Zoom/Zoom Full or <Home>

Displays the entire flowsheet in the PFD window.

In, Zoom Out View/Zoom/Zoom Zooms in or out of the flowsheet.

View/ Zoom/Zoom Area

Displays the selection reca set of units, streams or

tangle used to select objects on the

flowsheet. The selected area fills the PFD.



or <Shift+Home> redraView/Zoom/Redraw Clears the PFD of any extraneous object by

wing the flowsheet. Using the Help Button The What Is? Help button displays context-sensitive help. Button Menu Item Description

What Is? Displays help for the object you point to.

Customizing the Toolbar Buttons on the toolbar may be added, removed or rearranged by using the Toolbar… item on the View menu. Over 50 buttons are available.

Figure 1-13: Toolbar Customization from View menu

All i r left to gh n the

se move items between the

tems in the “Selected Items” list box from top to bottom appear in ordet on the tool bar. Items in the “Available Items” list box do not appear ori

tool bar. U the Add, Add ALL, Delete, and Delete ALL buttons to

two list boxes as desired. To add an item to the tool bar,

Highlight an item in the “Available Items” list box.


Use the Add button to move it to the “Selected Items” list box.

o remove an item from the tool bar,

” list box. “Available Items” list box.

s” list box. uttons to change the position of

All c tely after pressing OK.

hfo

Unit operations from the PFD palette Stream connections Text Drawings Stream property tables

Use the PRO/II main window to see the contents of your simulation. You can choose to view the entire flowsheet or only a portion of it. You control the view using scroll bars, pan options, the zoom bar, or arrow keys.

Note: See Chapter 5, Manipulating Objects, for information about placing, selecting and changing the size of objects in the PFD.

T

Highlight an item in the “Selected Items Use the Delete button to move it to the

To change the order of items on the tool bar,

Highlight an item in the “Selected Itemop, and Bottom b Use the Up, Down, T

m in the list. the ite

hanges take effect immedia Using the PRO/II Main Window T e PRO/II main window (PFD) is the main drawing board. You may place the

llowing objects on the PFD:


Chapter 2 Simulation Basics In the previous chapter, you learned some of the basic window features of PRO/II. In this chapter, you will learn simulation basics; that is, how to set up simulation problems, solve them, and analyze the results.

General Approach This chapter provides a quick overview of the use of PRO/II for solving engineering problems. A suggested basic approach is given as well as helpful explanations of the information flow in PRO/II. Sample data entry windows are given to illustrate data entry for PRO/II. Step-by-step examples are available in the PRO/II Tutorial Guide. Online help is also available. You have already learned that PRO/II gives you great flexibility and numerous options when supplying simulation data. For many items of data, default values are supplied. A color code informs you when data are required, supplied by default, out of normal ranges, or missing.

Note: You must supply data for all red-bordered fields or red-linked text (including data required) before running your simulation.

Problem data may be supplied in almost any order: PRO/II warns you when required data are missing. However, it is still best to follow a logical path when supplying simulation data. For example, some options such as stream compositions are dependent upon the components selected. Some unit operations, such as the flash drum, have features that are dependent on the thermodynamic data. For some other unit operations, performance specifications based on the components in the system are the preferred way to define the operation. For these reasons, the following approach is recommended when building a simulation flowsheet. Draw the Flowsheet Select the unit operations needed for the flowsheet calculations and position them on the PRO/II PFD main window.

Chapter 2 Simulation Basics 15

Connect the Unit Operations with Streams The streams are the connectors for the process calculations, with information passed from one unit operation to another via the process streams. Define the Components in Your System It is best to order the components in volatility order, starting with the lightest component. This makes it easy to analyze the separations which occur in unit operations such as distillation. While not a necessity, for hydrocarbon/water systems, defining water as the first component is also a good idea. This makes it easy to see the break between the aqueous and non-aqueous phases. User-defined petroleum pseudo components and/or polymer components for which you supply data should be entered next. Petroleum pseudo-components generated by PRO/II from petroleum stream assay data will appear last in the component lists of the output reports. Select the Thermodynamic and Transport Property Methods For many problems, a system may be selected from the Most Commonly Used thermodynamic methods. Guidelines for thermodynamic methods are provided in the PRO/II online help, and in the PRO/II Reference Manual (both in online help and in hardcopy forms). Further assistance is available through SIMSCI – ESSCOR Technical Support. Selecting a proper thermodynamic method is a critically important step in the solution of a simulation problem. Supply Data for the Feed Streams and Recycle Streams You must supply thermal conditions, flow rates, and compositions for all external feed streams to the flowsheet. It is usually desirable, although not necessary, to provide estimated data for recycle streams to speed convergence of recycle calculations. Supply Operating Conditions for the Unit Operations Double-click the icon for each unit operation to access the data entry windows. The color codes tell you what data you must supply and what data have default values. You may also use the online help to learn more about the calculation options, data entry items, etc., for each unit operation. A quick review is also a good idea at this point. Do the thermodynamic methods support the unit operation calculations? Are transport properties required for any of the unit operations?


Run the Process Simulation PRO/II lets you know, by color code, when sufficient information has been supplied to perform the calculations. When all of the borders on the toolbar

icons have changed from red (indicating missing data) to green or blue, you are ready to run your simulation. At this point, you may click the Run (right arrow) icon on the toolbar or the Run button on the floating Run palette to begin the flowsheet calculations.

Analyze the Simulation Results Use the many convenient report and plotting features of PRO/II to analyze the simulation results. At this point, your training as an engineer should take charge. Are the results reasonable? How do the results compare with the plant data? Can differences be reconciled? Are better data for the feed stocks needed? Are the models adequate for the intended purposes? Now that we have presented an overall plan for simulating a flowsheet, let’s look at some of the individual steps in more detail. Building the Flowsheet

Unit Operations Use the floating PFD palette to begin building the flowsheet. The icons and names for the unit operations appear as buttons on the PFD palette. To add a unit operation to the flowsheet, click the unit icon on the PFD palette and click-drop it at the desired location on the flowsheet.

Streams Click the Streams button on the top of the floating PFD palette. The PFD is now in stream mode and a small “S” is attached to the cursor. You will notice that all possible exit ports for each unit operation are now marked. Required outlet ports are colored in red; green is used to mark optional ports. PRO/II adds each stream to the flowsheet in an orthogonal manner, following a rectangular grid pattern. As soon as a valid flowsheet has been built, i.e., all required inlet, outlet, and connector streams have been added for all the process units, the red border around the Streams button on the PFD palette changes to blue.


Required Data Now that the flowsheet has been built, it’s time to supply the required data for the calculations: the components and thermodynamic methods must be defined, inlet feed streams and, optionally, recycle streams must be supplied, and the operating conditions for the unit operations must be specified.

Components

To define the components, select Input/Component Selection from the menu bar or click on the benzene ring toolbar icon to open the Component Selection main window. Note that this icon has a red border, indicating that components have not yet been defined. Library components for which the library access names are known may be directly typed into this window, where they are transferred to the List of Selected Components for the problem. A convenient search procedure is also provided which may be used by clicking Select From Lists… Petroleum (PETRO) components are defined in the Petroleum Components window, which is reached by clicking Petroleum…. Non-library components can be defined in the User-defined window which is reached by clicking User-defined…. Note that petroleum pseudo-components defined by PRO/II from petroleum stream assay data do not appear in the Component Selection main window.

Thermodynamic Methods

Thermodynamic methods are defined in the Thermodynamic Data main window which is reached by selecting Input/Thermodynamic Data from the menu bar or by clicking on the phase diagram icon. Note that this icon is initially outlined in red, indicating that thermodynamic methods must be defined for the problem. For most problems, a predefined set of thermodynamic methods for calculating K-values, enthalpies, entropies, and densities may be used. PRO/II offers numerous Categories of method sets. After a category has been selected, you may select a method set within that category as a Defined System for the problem and modify it by clicking Modify… to access the Thermodynamic System-Modification window. Note that transport property calculations are not


included in the predefined method sets. If they are required for the problem, you must add them to the predefined thermodynamic method set in this window.

Stream Information The identifiers for feed streams requiring input data are marked with red borders indicating that information is missing. Stream information is supplied in the Stream Data main data entry window which is reached by double-clicking a stream identifier. The predefined stream identifier may also be changed in this window. Three types of information must be supplied in this window: the thermal condition of the stream, the flow rate for the stream, and the composition of the stream. For petroleum assay streams, the assay data are provided instead of the composition data, and PRO/II defines the stream composition for you in terms of petroleum pseudo-components. Although optional, it is good practice to provide reasonable estimates for recycle tear streams in order to accelerate convergence of problem recycle calculations.

Unit Operations Unit operation identifiers for which data entries are needed are marked with red borders. To enter information for a unit operation, double-click its icon to retrieve the Unit data entry window. Various input options and numeric values are supplied via this parent window and its child windows. Required information is always bordered in red; data entry fields for items with supplied defaults are always bordered in green. After supplying information in a data entry field, the border color changes to blue. Information you have supplied which lies outside the normal range for the field is marked with a yellow border. You may also change the default unit identifier in this window and furnish a longer, more descriptive name for the unit operation. Notice that when you return to the flowsheet, the unit identifier on the PFD has a black instead of red border, signifying that all data entry requirements are satisfied. If the border is still red, you must return to the data entry window for that unit operation and supply the missing data.


Optional Data

Miscellaneous Data All data entries in these categories are optional because PRO/II provides default values for all the options. In some cases, global values may be used to supply the defaults, as explained in Chapter 4, Building a Flowsheet. Miscellaneous data categories include problem descriptive information, the calculation sequence, recycle convergence options, flowsheet tolerances, and the scaling of product streams. Problem descriptive information is optional; however, it can be beneficial to document a simulation model for future users. This information includes a project name, problem name, user name, date, site, and problem description. This information is supplied in the Problem Descriptive Information window, which is

accessed by clicking the toolbar icon with the printed page icon or by electing Input/Problem Description from the ms enu bar.

For most problems, the calculation order determined by PRO/II is satisfactory. To

supply your own sequence, click the toolbar icon with the two connected lowsheet blocks or select the Input/Calculation Sequence from the menu bar. f Definitions of recycle loops are automatic. To define your own loops, or to use

acceleration techniques, click the toolbar icon with the flowsheet loop iconenter the Problem Recycle Convergence and Acceleration

to Options window or

elect the Input/Recycle Convergence from the menu bar.

ch reached by choosing Input/Flowsheet Tolerances from the menu bar.

for a

s Flowsheet tolerances are used for convergence of unit operation specifications and may be changed in the Default Unit Specification Tolerances window, whiis All flowsheet results may be scaled so that a desired flow is obtained product stream. To use the scaling feature, select the Output/Report Format/Miscellaneous Data. Click Product Stream Scaling… on the Miscellaneous Report Options window to access the Scale Stream Flow rate

indow.

w


Miscellaneous Calculation Options PRO/II has default settings for many global calculation settings, but in some simulations it may be desirable to employ alternative settings. The options described here correspond to entries in the General Data category of keyword input. They are more fully described in Chapter 5 of the PRO/II Keyword Input Manual. Note: Chapter 4 of this Guide describes additional settings available through the Options menu. To access these calculation settings in ProVision, navigate to Input/ Miscellaneous Data from the menu bar. This displays the Input Miscellaneous Data dialogue:

Figure 2-1: Miscellaneous Calculations Options

Include Exergy Analysis: Placing a check mark in this checkbox requests exergy calculations after the flowsheet has solved. These calculations do not affect flowsheet convergence. This corresponds to the EXERGY statement of General Data keyword input.

Component Data: Controls the component slates used in each

thermodynamic METHOD set. The default Fixed option forces all


thermodynamic sets to use the same component properties uniformly. The Variable option allows each METHOD set to use different properties for the components. This is equivalent to the CDATA option on the CALCULATION statement of General Data keyword input.

Polymer Mode Consistency Check: Set Yes by default, this generates a

report of how the phases available for polymer components agree with the phases available in the thermodynamic methods. This option takes very little time, and there is no substantial advantage for using the No option. This is equivalent to the PCONVERSION option on the PRINT statement of General Data keyword input. (It is used so rarely it no longer is documented in the Keyword Manual.)

Thermo/Phase Designation Consistency Check: This checks that the

phases declared in the thermodynamic METHOD sets are compatible with the phase designations of non-polymer components. The default Calculation Time setting performs the checks each time thermodynamic calculations are initiated. The Input Time option performs the checks only once, before flowsheet calculations begin. Performing the checks during calculations has very little impact on the elapsed solution time. This is the same as the COMPCHECK option on the CALCULATION statement of General Data keyword input.

Independent Variable Check: In equilibrium calculations where the

dependent variable (y) is relatively insensitive to the independent variable (X), the default ON setting forces relatively large changes in the independent variable. This helps ensure the solution is near the local optimum. The OFF option accepts any valid solution that is merely “within tolerance”, but may be desirable in rare situations. This is equivalent to the DVARIABLE option on the CALCULATION statement of General Data keyword input.

Flash Algorithm: PRO/II incorporates several strategies for solving flash

calculations. Each strategy has unique strengths and weaknesses. The Default setting is robust, and is appropriate for most simulations. The before Version 5.5 setting closely replicates the flash results obtained in older versions of PRO/II. The Alternate setting is recommended when the Default method fails, especially when two liquid phases are expected. For more description, refer to the FLASH option on the CALCULATION statement of General Data keyword input.

Maximum Node Calculations: This entry sets the maximum number of unit

operations and branching decisions allowed during flowsheet solution. The default number is adequate for virtually all simulations. See the MAXOPS entry on the CALCULATION statement of General Data keyword input.


Default Data To simplify data input, PRO/II supplies default options and values wherever practical. Default values supplied by PRO/II are printed in black in a data entry field with a green border, or in the case of linked text, in green. For example, the default number of iterations for a column unit operation using the IO method is supplied as 15. Entries which you must always supply are indicated with a color red because they have no default values. While it is not necessary to replace a default entry to satisfy PRO/II input requirements, default data should be inspected carefully to ascertain that they meet your requirements. After replacing a default value, the border color for the data entry field changes to blue, indicating that you have supplied this value. For linked-text strings, the color of the linked text is also changed to blue, indicating that you have replaced the default value.

Other Optional Data Optional data, which are displayed in black, are data or options not specifically necessary for the unit operations to proceed. For example, the Description entry is optional for all unit operations. A reboiler is optional for the Column unit operation, since the calculation requirements may also be satisfied by a vapor feed to the bottom tray of the column. Data options which do not apply to a particular combination of input data appear in the color gray, and are not available for data entry. For example, when the kettle reboiler option is selected for a column reboiler, the data entry fields for a thermosiphon reboiler are colored gray.


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Chapter 3 Managing Simulation Files This chapter describes how to open, save, close, delete and copy simulation files. In addition, this chapter outlines how to import a PRO/II keyword input file or export a flowsheet.

Opening a New Simulation When you start PRO/II, the program does not automatically bring up a new, untitled simulation.

Note: If you want PRO/II always to open with a new simulation, select Options/New File on Startup from the menu bar.

To open a new simulation:

Choose File/New... from the menu bar. PRO/II clears the main window for a new simulation and opens the initial viewport window, View 1.

Figure 3-1: PRO/II Main Window

Chapter 3 Managing PFD Files 25

Opening an Existing Simulation You can open any previously saved simulation for modification, viewing or printing. PRO/II opens the flowsheet file and its supporting PRO/II database files. To open an existing simulation:

Choose File/Open... from the menu bar. PRO/II displays the Open Simulation window.

Figure 3-2: Open Simulation Window

on file.

er for import of PRO/II 4.x files with dule files.

Type or select the name of the simulati Click Open or press <Enter>. PRO/II displays the simulation in the PFD

main window.

Note: PRO/II 7.x provides a file convertthe exception of Add-On Mo


Saving the Current Simulation Before you close a simulation, you should save it. You may also want to save the simulation periodically while creating it. To save the current simulation:

Choose File/Save from the menu bar. If you have not previously saved this simulation, PRO/II displays the Save As window.

Note: PRO/II 5.x automatically compresses the three PRO/II database files

(*.pr1, *.pr2, *.pr3) and the simulation flow diagram file (*.sfd) into a single *.prz file. Besides reducing the size of stored files, PRO/II file compression assures that a complete set of files for each simulation has been saved.

Figure 3-3: Save As Dialog

Type a name for this simulation. Click Save or press <Enter>.

you close or exit the

Note: The PRO/II Autosave functionality automatically creates a backup file at

ser-specified intervals from which recovery can be made. Ifusimulation without saving, this backup file is deleted. Select Options/Simulation Defaults/Autosave… from the menu bar to access the Autosave Options window.


Saving a Simulation to Another Name

es you made to the imulation since the last save are saved as part of the simulation, under its new ame.

ote: If you’ve made changes to a simulation and don’t want to alter the original e changes, use Save As.

You can save a simulation to another name. Changsn Nsimulation, but do want to keep th To save the current simulation to another file name:

Choose File/Save As... from the menu bar.

RO/II prompts you for a neP

w file name.

losing a Simulation

ou should save a simulation before closing it, although PRO/II will prompt you save changes for an existing simulation.

o close a simulation:

e menu bar.

hanges you made to the simulation since the last save.

Type a name for the simulation. Click Save or press <Enter>.

RO/II appends a .PRZ extension to the filename. P

C Yto T

Choose File/Close from th

If you close a simulation without first saving the simulation files, you lose any c


De

ou can delete any simulation except the current (active) simulation at any time.

o delete a simulation file:

leting a Simulation Y T

Choose File/Delete... from the menu bar. PRO/II displays a list of existing PRO/II simulation files.

Figure 3-4: List of Files

Type or select the name of the file you want to delete. (You may not

delete the current simulation.) Click Open or press <Enter>. PRO/II deletes all files associated with this

simulation.


Co You lation (one flowsheet and three data can copy to new or existing

e. If you copy to an existing file, PRO/II verifies if you want to overwrite the

pying a Simulation

can copy all files associated with a simubase files) to a target simulation you name. You

filexisting file. To copy a simulation file:

Choose File/Copy... from the menu bar. This opens the dialog illustrated in Figure 3-5.

Figure 3-5: Copying Files

Select the name of the file you want to copy from the file selector. (You may not copy the current sim

Enter a name for the copy (target). Click Open or press <Enter>.

II copies all files associated with

: There may be as many as 17 se e lation problem. These are describ

ulation.)

PRO/

the simulation.

Notesimu

parate files associated with a singled in Table 3-1.


Table 3-1: PRO/II Simulation Files

File Extension Description

*.pr1, *.pr2, *.pr3 PRO/II database files

*.sfd Graphics

file

*.prz Compressed files containing *.pr1, *.pr2, *.pr3 and *.sfd files

*.out Main output file

*.ot1 Component, calculation sequence, recycle loops/streams output data

*.ot3 Equipment/streams output data

*.sr1 Input source listing

*.ix3 Output index

*.hs2 Calculation history

*.inp Keyword

input file

*.plt the plot display window Plots saved in

*.txt Stream property table or plot (saved in ASCII format)

*.csv Stream property table or plot (saved in tabular format)

*.clp Graphics saved in Clipboard format

*.prc emporary procedure file created and removed by PRO/II. Only remains if

T

there is an abnormal termination.


Importing a PRO/II Keyword Input File You can import an existing PRO/II keyword input file into the PRO/II graphical user interface and then execute the simulation problem just as if you had entered he problt em using the PFD graphical main window. PRO/II automatically

l be generated, when a simulation (PFD) is saved ayout

PRO keyword input files.

converts the specified keyword input file into a flowsheet and displays it in the PFD window. Note: In the previous versions, PFD layout was retained within the *.prz file. In the current version, *.sfd file wiland exported. After the generation of *.sfd file, users can restore the PFD lusing *.inp file. To import a PRO/II keyword input file:

Choosing File/Import from the menu bar.

/II displays a list of existing

-6: List of Files Figure 3

PRO I c

e P D .

Type or select the name of the keyword file that you want to import. Click Open or press <Enter>.

/I onverts the selected keywoF main window automatically

rd input file into a flowsheet and displays it in th


Keyword Features without PRO/II GUI support The E this version feature. If a RESthe “Run Batch” feature of PRO/II may be used with these keyword input files. See running keyword

Keyword Features Imported in “Run-Only” Mode

features is detected, you will be llowed to import the keyword file, however the GUI interface will operate in the

“Run-Only” mode. Such unsupported keywords include:

BVLE Data Stream Report Writer Hydrate Unit Operation HEXTRAN Property Data Generator.

O/II program

ported features ill be automatically listed in a status window. You have the option to save or

ures,

In “

• Rev it ope e of your

• Add

D rts

d features only). • Export the flowsheet and stream property table information to other

Windows applications. • Edit the keyword file, re-import, and rerun (without leaving PRO/II).

R START feature is not supported by the graphical user interface in of PRO/II. You will not be allowed to import keyword files that contain this

TART keyword is detected upon import, you will be reminded that only

Chapter 10, Running and Viewing a Flowsheet, for information on files in “Batch” mode.

Certain keyword features are not fully supported by the graphical user interface of PRO/II. However, if one of these unsupported a

If you attempt to import a keyword input file that contains PRs not supported by the graphical user interface, the unsupfeature

wdelete the unsupported features. If you choose to save the unsupported featPRO/II will run the file in Run-Only Mode.

Run-Only” mode, you can:

iew and modify the PFD graphic image. You may move unration icons and streams around to improve the appearanc

PFD. drawing elements to the PFD.

• Add stream property tables to the PFD. • Have access to all the capabilities on the Run palette (perform all

interactive execution functions available on the Run palette for both supported/unsupported units, review the calculated results on the PFfor all streams and supported/unsupported units, generate output repofor all features, generate plots for supporte

• Use the stream flash icon.


In “ :

r stream will cause a short warning message to be displayed. • Perform any input mode functions, including changing the calculation

ccess simulation data will

you imessages dialogs appear. These describe the problems and provide options for

remedial action. The following display is typical:

Run-Only” mode, you cannot• View simulation data with the data entry windows. This includes

Component and Thermodynamic data. Double-clicking on a unit operation o

sequence. All buttons and menu options that abe disabled.

• Perform any of the following functions: adding/deleting units, adding/deleting streams, and reconnecting streams.

• Export the PRO/II keyword input file.

port a keyword file containing unsupported features, one or more Ifm

Figure 3-7: Typical Unsupported Features Warning Window

After responding to each unsupported feature dialog, the message window displays messages similar to the following:

** MESSAGE ** A single STREAM that FEEDS MORE THAN ONE UNIT operation is NOT SUPPORTED by PROVISION. Referencing streams may be used instead.

** MESSAGE ** Duplicate stream 8 feeding X1 is renamed to 8_R1 and is referenced to the first instance of 8.

Figure 3-8: Flowsheet Status Window for Unsupported Features Removin s allows PRO/II to start normallyPRO/II o

s

g all unsupported features in the dialog boxe. However, leaving even one unsupported feature present results in perating in “Run-Only” mode. The Title bar of the main PFD window

this condition, as illustrated in Figure 3-9. reveal


Figure 3-9: PRO/II in “Run-only” Mode

Click Run on the Run palette.

Oncresu

e the flowsheet solves, you may double-click a unit or stream to view the lts.

Exporting Simulation Data to a File PRO/II allows exporting the current simulation flowsheet in a variety of different formats for use in various applications. To begin the export process:

Choose File/Export… from the menu bar. PRO/II displays the Export window which lists the data export options. Refer to Figure 3-10.

Figure 3-10: Available Data Export Options


Note: In the current version, a *.sfd file is generated when the simulation (PFD) is saved and exported. After generation of the *.sfd file, users crestore the PFD layout using the (exported) *.inp file.

Choose the Simulation Data to Keywo

an

rd File option. Click OK.

re

This g the input da input file.

the destination drive and directory of choice using the Save

Thethe word files e keyword file con ics, etc.).

v6.0 and later, the "Simulation Data to Keyword File" option is expanded to clude check boxes to control exporting stream and column solution data to the eyword file.

output data exists, even if the solution is unconverged, the two "Include" check oxes are enabled (See figure 3-10). If the Run command was never executed, r not executed since the last time "Restore Input Data" was performed, these heckboxes are disabled.

Test for Convergence

0), in

t the ged.

turns e

PRO/II converts the current simulation flowsheet data into a PRO/II keyword input file in ASCII format. The name of the keyword file will be YYY.INP, wheYYY.PR1 is the name of the simulation flowsheet PRO/II database file.

Export Simulation Data to a Keyword File selection opens a special Save As… dialog window that allows exportin

ta of the simulation to an ".inp" keyword

Navigate toIn: field.

Enter the name of the output file in the File Name: field. Press the Save button to complete the operation.

exported keyword file then may be imported into any compatible version of PRO/II program to rerun the simulation, even on another computer. Key also are a very compact way to archive the data. Note that th

propriate data sections (General, Thermodynamtains all the ap Inink Ifboc

When the user selects either or both of the "Include" check boxes (Figure 3-1upon OK, the first thing PRO/II does is test for convergence. If the solution is an unconverged state, PRO/II displays a message box to warn the user tha

ata being written to the keyword file is unconverd Clicking "Yes" continues to the file name selection common dialog. "No" reth user to the Export window.


Notoperatio e keyword file. Previously, for keyword input files that s listed in the Seq ThisPRO/II t with a list of Available Unit Ope ludes unit operations marked Excluded at the time of export. Additionally in these instances, PRO/II writes a warning into the keyword file advising that the list of unit operations and the SEQUENCE statement do not match. The roblems if read into earlier versions

ou can export part or all of the flowsheet drawing to the Clipboard. You can en paste this drawing into other Windows applications.

o export the entire flowsheet drawing to the Clipboard:

To

n its edge on the PFD. ays the Export

wing option.

e: Beginning with PRO/II version 5.5, exported flowsheets write all unit ns in the flowsheet to th

include a User-Defined Sequence List, only unit operationuence List were exported.

change was necessary to support the new Included/ Excluded functionality. now generates a SEQUENCE statemen

rations that exc

se files may cause input processing p of PRO/II (i.e., versions prior to 5.5).

Exporting the Flowsheet Drawing to the Clipboard Yth T

Choose File/Export from the menu bar. PRO/II displays the Export window (Figure 3-10).

Choose the Flowsheet Drawing option. Click OK.

export one page of the flowsheet to the Clipboard:

Select the page to export by clicking oChoose File/Export from the menu bar. PRO/II displwindow (Figure 3-10). Choose the Selected Page of Flowsheet Dra

Click OK.


Exporting Stream or Unit Property Table Data ou can export the information in a stream property table or a unit operation roperty table to an ASCII file. The file subsequently may be imported into

Ypspreadsheet and word processing applications. To export data from a stream or unit operation property table:

Select the property table to export (select it on the PFD). Choose File/Export from the menu bar. PRO/II displays the Export

window (Figure 3-10). Choose the Stream / Unit Op Property Table option.

) from the

Click OK. The Export File Filter window will appear (see Figure 3-11). Enter a name for the Output File. Select the desired file format (tab-delimited or comma-delimited

Save File as Type drop-down list box. Click OK.

Figure 3-11: Export File Filter Window

PRO sheet or wor s included with that application.

/II then generates the ASCII file. To import this file into your spreadd processing program, follow the instruction


Exporting the PFD to an AutoCAD or PostScript File You can export your flowsheet drawing as an AutoCAD .DXF or Encapsulated PostScript (.EPS) file:

Choose File/Export from the menu bar. PRO/II displays the Export

Click Save to export the data to the file.

Exporting Tag Data to a File All tagged data in the simulation can be exported to a plain text (ASCII) file for later use in other applications.

window (Figure 3-10). Choose one of the following options Flowsheet to AutoCAD .DXF Flowsheet to AutoCAD Design XML Flowsheet to Post-Script

Click OK. The Save As window appears. Enter a name for the .DXF or .EPS file.

Choose File/Export from the menu bar. PRO/II displays the Export window (Figure 3-10).

Choose Tag data to file Click OK. The Save As window appears. Enter a name for the *.RAW file. Click Save to export the data to the file.

Exporting Data to Excel Using Spreadsheet Tools Spreadsheet tools are Excel template files and macros that can read information in the PRO/II simulation database to generate reports or perform additional on-the-spot calculations. They can also update data in the simulation database itself using data from an Excel spreadsheet. They offer functionality similar to the export functions described earlier, but export data directly to Microsoft Excel instead of to a disk file. Each Tools/Spreadsheet menu item can be used to start a spreadsheet tool.

From the Tools menu, choose Spreadsheet. The list of currently installed tools will appear in a side menu.

Click the desired tool to export data and automatically launch Excel.


Note: Microsoft Excel must be installed on your system to use these tools. Additionally, since these tools use macros to export the data, macros must be enabled in Excel. If Excel displays a security dialog, choose “Enable macros”. PRO/II comes pre-installed with some default spreadsheet tools. They can be used to create tables of stream properties, component flow rates, or distillation reports. They also can generate property tables and other reports for a limited number of supported unit operations. Copying Property Table Data to the Clipboard You can copy the information in a stream or unit operation property table to the clipboard. This table can then be pasted into any other Windows application. To copy a property table to the Clipboard:

Select the stream or unit operation property table on the PFD. Choose Edit/Copy from the menu bar.

Copying/Pasting Stream Data in an Excel Sheet Use this option to copy and paste the stream data to and from an Excel sheet. This enables the user to enter and analyze the data with ease. The feature is implemented in all dialog boxes where the data is represented in XY grid. XY grid has the following properties:

• The grid origin is numbered 0.0. • The X and Y axis divide the grid into 4 quadrants. • Display any grid variable as a distinct value per cell or smoothly varying. • No duplicate values are allowed.

Note: Ctrl+C, Ctrl+V, Ctrl+X can be used a shortcut to COPY, PASTE and CUT respectively.


Chapter 4 Building a Flowsheet This chapter describes how to construct a flowsheet. It begins by describing the various defaults that may apply to your simulation on a global, simulation, or unit level. This chapter also includes instructions for placing unit operations, connecting units, and drawing objects that enhance the presentation of your flowsheet without affecting calculations.

Setting Simulation Preferences PRO/II enables you to set global defaults for problem descriptions information, units of measure and thermodynamic systems. These global defaults apply to all simulations unless you specifically override them either for a particular simulation or unit operation. On a simulation level, you can set problem-specific input and output units of measure defaults. Simulation level settings override global defaults. In addition, you can change units of measure settings for a specific unit. This setting overrides both simulation and global defaults.

Setting Problem Description Global Defaults The Problem Description Information (Project Identifier, Problem Identifier, User Name, Date, and Site) appears on each page of a results printout as a heading and the Problem Description itself appears on the first page. All simulations use the global problem descriptive information unless you override the defaults for a particular simulation. To set problem description global defaults:

Choose Options/Simulation Defaults from the menu bar. Choose Problem Description. The Global Default for Problem Descriptive

Information window appears, as shown in Figure 4-1.

Chapter 4 Building A Flowsheet 41

Figure 4-1: Global Default for Problem Descriptive Information

Complete the window. Click OK.

Overriding the Global Default Problem Description Before laying down your flowsheet, you may want to update the problem description for the current simulation. PRO/II uses the global defaults for all simulations, unless you specifically override the data for a particular simulation. To override the global default problem definition:

Click Problem Description or choose Input/Problem Description fromthe menu bar. The Problem Descriptive Information window appears.

You can enter up to ten problem description lines (80 characters each), that will

ppear on the first page of a results printout. a


Setting Units of Measure Global Defaults By default, PRO/II uses the English units of measure set for all input data and for output reports. These defaults apply to all new simulations. You can override the default set for either input data or output reports (or both) for all new simulations. PRO/II maintains a library of units of measure sets that you can select from and add to. To set the unit of measure global defaults:

Choose Simulation Defaults from the Options menu. Choose Units of Measure. The Default Sets of Units of Measure window

appears.

Figure 4-2: Global Units of Measure Sets

Select the desired default units of measure set for entering simulation

data. The default choice is ENGLISH-SET1, i.e., the data input will be in English units.

Select the desired default units of measure set for generating the first output report. The default choice is Same as Input, i.e., the first output report will be printed in the default English units.

If any choice other than the default is selected, the second output report will no longer be available, and the list-box for selecting the alternate units of measure set for the second output report will be disabled. Select the desired default units of measure set for generating the second output report. The default choice is None, i.e., no second output report in alternate units will be generated.


Changing Global Units of Measure for One Simulation PRO/II sets English units as the default for units of measure. You can override this default, setting the global units of measure for all new simulations. In addition, you can override the default units of measure for a particular simulation problem. To set the units of measure for the current simulation:

Click Input Units of Measure or choose Input/Units of Measure fromthe menu bar. The Default Units of Measure for Problem Data Input window appears.

Figure 4-3: Default Units of Measure for Problem Data Input Window

Select different dimensional units for data input for each individual

category or choose Initialize from UOM Library... to automatically fill in the defaults from another set.

Click Standard Vapor Conditions... to enter the Problem Standard Vapor Condition window. The default temperature and pressure basis are shown in the data entry fields and may be replaced or the standard vapor

are: volume per mole may be replaced, not both. PRO/II default values Note in the following table that standard conditions for liquid molar

volume are different than standard vapor conditions.


Table 1: Standard Conditions

Temperature

Pressure

Vapor Volume

Liquid Mole Volume

English 60°F 14.696 psia 379.48 ft 3 /lb-mol 77F

Metric 0°C 1.0332 kg/cm2 22.414 m3 /kg-mol 25C

SI 273.15 K 101.32 kPa 22.414 m3 /kg-mol 298.15K

The current atmospheric pressure (Pressure Gauge Basis) is shown in a data entry field and may be replaced with another value as desired. The PRO/II default value is 14.696 psia or the metric equivalent.

Click TVP and RVP Conditions... to select the Problem TVP and RVP Conditions window. The temperature for true vapor pressure specifications may be replaced in this window. The PRO/II default for TVP calculations is 10 °F. The calculation method for Reid vapor pressure may be selected in a drop-down list box on this window. Choices are:

API Naphtha (the default) API Crude ASTM D323-73 ASTM D323-82 ASTM D4593-91 ASTM D5191-91 ASTM D323-94

Click OK.

Units of Measure Library A library of dimensional unit sets which may be used for data entry or report writing is maintained with this feature. To add a new set to the library or to edit an existing set:

Select Options/Units of Measure List from the menu bar. The Units of Measure Library window appears and may be used to create, copy, edit, rename, and delete dimensional unit sets. The Units of Measure Set Name and Description list box contains the names of the dimensional unit sets currently in the library. The program provides three initial dimensional unit sets: English (the default), Metric, and SI.


To create a new set:

Click Create... on the Units of Measure Library window to get the Create Units of Measure Set window.

Figure 4-4: Units of Measure Library

ld provided, and select

th the appropriate radio button: English, Metric, or Enter a name for the new set in the data entry fiethe basis for the set wiSI.

Figure 4-5: Create Units of Measure Set Window

Click OK to continue.


The units for the standard dimensional unit sets in PRO/II are assigned to the

easure Set Name and Description list box and click Copy on the Units f Measure Library window. The name for the new set is then entered in the

To

1. Lwindow 2. TMeasurwindow

Selecting the Output menu on the menu bar.

nu. Editing of the dimensional items is identical for these two windows.

The s premeawin

Click Initialize from UOM Library... The Initialize Units of Measure from

utput report set may be edited in this window as desired. The edited set is saved with the problem.

Rep

new set and the edit feature may be used to customize the set. Note: An alternate way to create a new set is to highlight an existing set in the Units of MoCopy Units of Measure Set window. The Edit feature may be used to customize the set.

delete, rename or edit a set:

Select the set in the Units of Measure Set Name and Description list box. Click the Delete, Rename, or Edit button on the Units of Measure Library

window. Editing the Dimensional Unit Sets for Output Reports A dimensional unit set for output reports may be edited in two places in PRO/II:

ibrary sets are edited with the Edit... feature in the Units of Measure Library .

he set being used for the current problem is edited in the Default Units of e of the Problem Output Report which is accessible from the PFD main by:

Selecting the Report Format from the Output menu. Selecting Units of Measure from the Report Format me

dimensional unit set for the output report is initialized from the global set, a

viously explained. However, a different set may be chosen from the units of sure library while in the Default Units of Measure for Problem Output Report

dow. To use a different dimensional unit set:

UOM Library window appears. Select the desired set from the drop-down list box. Click OK to continue. This set now becomes the output report set. The

newly selected o

The Print Option for output reports may also be selected using the Output

ort(s) to be Printed drop-down list box where options are:


One its (the default): When this option is selected,

an output report based on the units of measure used for the problem data e

ecting the Units of Measure option from the Input menu.

t ed on the output units of measure specified will be generated. The

currently specified output units of measure will be displayed, and they can be

wo nput Units, one in Output Units: hen this option is selected, two output reports will be generated, one each,

. measure will be displayed, and they

can be changed if desired. For the above, the displayed output units of mea m the specified input units, or initialized from one of the units of measure sets stored in the units of measure library.

Click Copy from Input UOM on the Default Units of Measure for Problem Output Report window.

o initialize the output units of measure set from a units of measure set

s of Measure for

If the results of a previously executed simulation must be printed in a different set d units through this

ed not be executed om the start just to obtain the output results in a different set of dimensional

unit

Output Report in Input Un

input will be generated. The currently specified input units of measure will bdisplayed for informational purposes, but they cannot be changed. With this option, the output units of measure can only be changed by sel

One Output Report in Output Units: When this option is selected, an outpu

report bas

changed if desired.

TW

Output Reports, one in I

based on the input and specified output units of measure will be generatedThe currently specified output units of

second and third cases discussedsure set can be copied fro

To copy the input units of measure set to be used for the output report, or to reset the explicitly specified output units to the previously specified input units:

Click OK to continue. Tstored in the units of measure library:

Click Initialize from UOM Library... on the Default UnitProblem Output Report window. Click OK to continue.

of dimensional units, it is only necessary to select the requirefeature and generate a new report. The entire simulation nefr

s.


Setting Thermodynamic System Global Defaults To set the thermodynamic system global defaults:

Choose Simulation Defaults from the Options menu. Choose Thermodynamic System. The Global Default Thermodynamic

System window appears.

Figure 4-6: Global Default Thermodynamic System Window

Complete the window. Click OK.

Note: This global default will not become effective until the next time File/New is selected. Setting General Drawing Defaults

f your workplace through the General Drawing Defaults window. You can set the snap and move tolerances,

, icon fill, unit snapping, and

PRO/II allows you to change the appearance o

zoom and pan increments, the PFD palette icondelete confirmation. The defaults, shown below in Figure 4-7, are appropriate for most scenarios and you may never need to make changes in this window.


To

make changes to the general drawing defaults:

Choose Options/Drawing Defaults/General... from the menu bar.

Figure 4-7: General Drawing Defaults Window

Changing Delete Confirmation By default, PRO/II prompts you to confirm each del

change this default setting. ete operation. You may want

s

rances criteria for es, such as the

tole The default nces are satisfactory for most problems. To set the tolerance for this flowsheet:

to

o turn delete confirmation off: T

Within the General Drawing Defaults window, uncheck Confirm Deleteto turn the option off.

Setting Global Flowsheet ToleUse this option to identify the acceptable margins of error and atisfying certain numerical methods. Some flowsheet tolerancs

rance for flash calculations, are internal and are not user-definable.flowsheet tolera

Choose Input/Flowsheet Tolerances on the menu bar to open the

Tolerances dialog.


Figure 4-8: Default Unit Specification Tolerances

lacing a Unit on the Flowsheet

he PRO/II main window is your drawing board. PRO/II supplies a floating PFD alette and drawing objects that help you draw your problem quickly.

ration that you can select to place n the fl open a new

or e To c

P Tp The PFD palette shows icons for each unit opeo owsheet. The PFD palette appears automatically when you

xisting file, or when you import a keyword file.

lose or open the PFD palette:

Click Palette on/off , or select the View menu on the main PRO/II window. Check the Palettes/PFD option on or off.

Palette

ace it on your flowsheet:

palette (see Chapter 9 for unit ). cursor where you want the unit icon to appear and click the

left mouse button.

electing a Unit from the PFDS

o select a unit icon and plT

Choose the icon from the PFD

descriptions Position the


Figure 4-9: Placing a Unit

Snapping When connecting two units with a stream PRO/II will adjust or “snap” the unit icon positions to straighten the connecting stream. By default, units you add to or move in the PFD main window snap to an invisible grid. You can turn grid snapping off. To turn grid snapping off:

Choose Drawing Defaults from the Options menu. Select General. Select Unit Snapping. The disappears from the Unit Snapping check

box. Placing Multiple Unit Icons

ou can place a series of unit icons in succession.

Y


To place more than one unit at a time:

Select the desired unit from the floating PFD palette. Press <Shift>, and while holding down <Shift>, click on the PFD main

window to place the icon. While still holding down <Shift> click on the PFD main window to place

the second icon. Repeat for each additional placement of this icon.

anceling Unit Placement

o cancel unit placement:

Click the right mouse button.

C T

Deleting a Unit To delete a unit already on the flowsheet:

Click on the unit icon you want to delete.

Click delete on the toolbar, or press <Delete>, or click the right mouse button and select Delete.

ReRO/II automatically labels each unit icon you place on the PFD main window.

change the label for a unit by modifying the label on its data entry window. By default, the label consists of a character and a one-digit auto incrementing number. To re-label a specific unit:

Double-click on the unit you want to rename. The data entry window for that unit appears.

-labeling a Unit PYou can


Figure 4-10: Unit Data Entry Window

Type over the default name for Unit. Click OK.


Dr

Streams mode is used to lay out the connections between units and feed and product streams. The product ports for each unit automatically appear when you

, while optional roduct ports are green. For some unit operations, an entire side of the unit will e red or green denoting multiple connections to that port.

or display ports:

Select Streams

awing Streams

depress the Streams button. Required product ports are redpb To use the Streams mode

on the PFD palette.

Figure 4-11: Streams Button Down

The cursor changes to an arrow with a small S to indicate Streams mode. PRO/II isplays the product ports for each unit in the layout. To display feed ports,

dep To

to.

dress the left mouse button while the Streams button is depressed.

draw a feed stream:

Click on an unoccupied area of the PFD main window. Click the mouse on the feed port you want the incoming stream

connected


To draw a product stream:

Click the left mouse button on a product port. Click the left mouse button again where you want the stream to end.

ction

utton on a port to anchor or start a stream. The colors for some unit operations change depending on the

n orthogonal line to connect the ports.

Drawing a ConneTo connect units:

Click the left mouse bports and port port you selected.

Click the mouse again at the other unit you want to connect. PRO/IIdraws a

Figure 4-12: Feed, Product, and Connection Streams Layout


Canceling a Connection

To cancel a stream connection:

sc>.

tion:

rt) of the stream and hold down the mouse button. Drag the end of the stream to a new port.

Connecting Streams When One Unit is Not Visible In o nt

ust be n window. You may open another viewport window f the same simulation and move to the end port you wish to view. Alternately,

ars, the Pan View window, Search for Unit, or earch for Stream tool to display the end port.

LabelPROdefault, the label coan change the label for a stream by changing the label on its data entry window.

eam:

Double-click the stream you want to re-label. The Stream Data window appears.

Type over the default name for Stream. Choose OK.

his stream will now show the new label; other streams retain the original beling scheme.

Click the right mouse button or press <E

Changing a Connection To change a connec

Click the end (po

Release the mouse button.

rder to complete a stream connection, the ending unit for the stream segme visible in the PFD maim

oyou can also use the scroll bS

ing a Stream /II automatically labels each stream you place on the PFD main window. By

nsists of an S followed by an auto incrementing number. You c To re-label a str

Tla


Moving Streams ou can change the route of the stream between two connections whenever you

Rer

As you add new connections, PRO/II automatically performs a stream route calculation. am or a unit operation icon, this calculation

ay no long late an unobstructed, orthogonal path for cted streams.

To reroute a stream:

Select the stream(s) you want to reroute. Choose Reroute from the Edit menu.

PRO/II calculates the best route for these streams and automatically reroutes them.

Ywish. To move a stream:

Click and hold the left mouse button at an end of the stream you want to move.

Drag the stream to the new location.

Release the mouse button to drop the stream in place.

outing Streams

When you move a streer be valid. You can recalcum

sele


Searching for a Unit or Stream

RO/II builds two lists that identify the units and streams you have placed on the it by name. The Stream List identifies

Go to Unit

Pflowsheet. The Unit List identifies each uneach stream by name. To search for a unit:

Click or select View/Unit List. The Search for Unit dialog ppears, showing the names of all units currently placed on the

t diagram. unit you want to go to. The unit appears at the center of the

window.

o r a stream:

Click Go to Stream

box aflowshee

Select the PRO/II main

T search fo

or select View/Stream List. The Search for Stream dialog box appears, showing the names of all streams currently placed on the flow diagram.

Select the stream you want to go to. The stream appears at the center of the PFD.

Note: These search tools are only available on the toolbar if the Standard

Toolbar is active.


Changing the Flowsheet Layout PRO/II provides a variety of layout templates that change the look of your process flow diagram. Each template uses a different algorithm for calculating the position of unit operations and stream connections. You do not have to re-execute a simulation in order to change its layout. To change the layout of your diagram:

Choose Lay Out Flowsheet from the View menu. A cascading menu appears to the right of the View menu.

ing layouts:

Single Line

Choose one of the follow

Multi-line Type 1 Multi-line Type 2

Figu

Sin eft to right.

re 4-13: Sample PFD

gle line format lays units in a single line from l


Figure 4-14: Single Line

Dr

ou can place on the flow diagram, to customize ing of the flow diagram without interfering with

imulatio

Rectangle Ellipse Page

awing Freehand Objects PRO/II provides six objects that ythe look and increase understands n data. These objects are:

Text Line

Polygon


EnYou ou choose text

ode, you remain in text mode as long as you continue to choose the OK or

o place text:

aw/Text from the menu bar.

tering Text use the text option to include notes on your drawing. Once y

mCancel button on the Draw Text window; choosing Cancel exits text mode. T

Choose Dr

igure 4-15: DrawF Text Window

Enter the text you want to appear on the diagram. ault is 50 pixels.

raou use the line option to add connected lines to the diagram without interfering

ovides an orthogonal poly-line feature.

To

Optionally, choose a font size for the text. The def Choose OK.

D wing Lines Ywith simulation data. PRO/II pr

draw a line:

Choose Line from the Draw menu. Click and ho ld the mouse button on the PFD main window to anchor the

line. Press <Space> to set each anchor point for drawing in a new direction.

Release the mouse button to complete your line.


To draw orthogonal connected lines:

Choose Line from the Draw menu. Click and hold the mouse button on the PFD main window to anchor the

line. Press and hold <Ctrl>, and while holding down <Ctrl>, drag the cursor. Press <Space> to set each anchor point for drawing in a new direction. Release the mouse button to complete.

rawing Shapes

ou can draw shapes to enclose figures on a diagram without interfering with

o draw a polygon:

D Ysimulation data. T

Choose Polygon from the Draw menu. Click and hold down the mouse button on the PFD main window. Press <Space> to each anchor point for drawing in a new direction. Release the mouse button to complete your object.

To draw an orthogonal polygon:

Choose Polygon from the Draw menu. Click and hold the mouse button on the PFD main window. Press and hold <Ctrl>, and while holding down <Ctrl>, drag the cursor. Press <Space> to each anchor point for drawing in a new direction. Release the mouse button to complete your orthogonal polygon.

To draw a rectangle or ellipse:

Choose Rectangle or Ellipse from the Draw menu. Click and hold down the mouse button on the PFD main window. Drag and release when you see the desired size rectangle.

To draw a square or circle:

Choose Rectangle or Ellipse from the Draw menu. Click and hold down the mouse button on the PFD main window. Press <Ctrl> then drag and release the mouse button to complete your

square.


Drawing Pages You can divide your PFD into “pages” and define separate page setup options for each page. Pages can be individually printed or copied to the clipboard (see Chapter 3, Managing PFD Files). To add a page:

Choose Page from the Draw menu. Click on the PFD. Drag and release the mouse button to the desired size.

The page name is automatically given as PG followed by an auto incrementing three-digit number.

Figure 4-16: Pages


To change the page setup

Double-click anywhere along the page border. ThSetup window.

Select your page setup options. Click OK to continue.

options:

is brings up the Page

a new location.

o make a grid of pages:

ge outline. se button to display the Page Setup window. labeled Grid in the Change Page Parameters

r of rows and columns to make a grid of pages on the PFD. The page you started with will be the upper left cell of the grid.

The grid can be resized and moved on the PFD in the same manner as a single page.

After you have set up a page, you can resize it or make this page one cell in a grid of pages. To resize the page:

Click near the page outline to highlight the page. Click and drag the sizing box.

To move the page:

Click and drag the page outline to T

Select the page by clicking near the pa Double-click the left mou

io button Click on the radgroup box.

In the Page/Grid group box, select the radio button for Multiple Pages. Change the numbe




Chapter 5 Manipulating Objects

is chapter describes how to edit and align text.

electing Objects or Groups of Objects You group of

bje n objects. ll manipulations (delete, rotate, move) are performed on selected objects.

electing Multiple Objects

t to include as

This chapter describes how to select unit icons, streams, and other objects on the PFD main window and how to move, resize, rotate, or flip them. In addition, th

S can select a single object, multiple (noncontiguous) objects, or a cts. Objects or groups of objects include units, streams and drawo

A

SYou can select a set of noncontiguous objects. To select a set of individual objects:

Click on the first object. Press <Shift>. While holding down <Shift>, click on each object you wan

part of this set.

Figure 5-1: Multiple Unit Selection Handles

Chapter 5 Manipulating Objects 67

Handles appear for the set of objects. For example, although five objects appear to be selected as part of this set (Figure 5-1), when you move the selection, the fourth and fifth objects (the valve and the compressor) do not move with the set (Figure 5-2).

Figure 5-2: Move Multiple Objects


Selecting a Group of Objects ction rectangle

oup of objects:

of the PFD adjacent to one of the items you want to select and begin dragging the cursor by moving your mouse.

all desired objects are inside the selection rectangle outline.

pear for the selected group of objects.

el

ne command. Once selected,

To

Edit menu.

eselecting Objects

you change your mind after selecting objects, you can reverse any selection.

o dese

u. n an unoccupied area of the PFD.

th, or overall size of any object or a group of

a group of objects, you change the absolute istance between the objects and maintain the relative distance.

You can gather a group of contiguous objects by dragging a seleround them. a

o select a contiguous grT

Click on an unoccupied area

Drag the cursor until

Release the mouse button to end the selection. Handles ap

S ecting All Objects You can select all objects on the flowsheet with oou can then move or delete the entire selection. y

sele on the flowsheet: ct all objects

Choose Select All from the

D If T lect or unselect all objects in the layout, do one of the following:

Choose Select None from the Edit men Click on another item or o

Resizing Objects You can change the height, widbjects on your flowsheet. o

Changing the Size of a Selected Object When changing the width ofd


To

he object is the desired size. Release the mouse button.

change the size of an object:

Click and drag the cursor until t

Figure 5-3: Resize Column

Note: C xed in size. Th Restor

you don’t like how your resized icon looks (relative to other icons and objects n your flowsheet) you can quickly return the icon to its default size.

To restore an icon to its original size:

Choose Restore Icon Size from the Edit menu. You can also click the right mouse button on a selected icon, and then choose Restore Icon Size from the Icon pop-up menu.

ondensers and reboilers shown on distillation or side columns are fiey do not resize when you change the size of the column.

ing Unit Icon Size Ifo


Rearranging Objects You can move objects to a different area of the flowsheet. You can also rotatflip a unit icon so it fits into the flow of your diagram.

or Groups of Objects e or

You can To mov

ove Tolerance controls the incremental distance for any object you move. The

ow appears.

otating Selected Objects

a selected object(s) on its axis by 90, 180 or 270 degrees.

e Rotate degrees cascade menu

e Ro

ou can also click the right mouse button on a unit icon, and then choose Rotate om the Pop-up Unit menu to display the rotation degrees.

Moving Selected Objects

move an object to a new position on the flowsheet.

e a selected object:

Click and drag the object or group of objects to a new position. Release the mouse button.

Setting Move Tolerance Mdefault is 5 pixels. To change move tolerance:

Choose Drawing Defaults from the Options menu, then General. The General Drawing Defaults wind

Type the desired value over the default Move Tolerance. Choose OK.

R

ou can rotateY To rotate a selected object:

Choose Rotate from the Edit menu. Thappears to the right of the Edit menu.

Choos 90, 180, or 270.

tating an Icon Yfr


Flipping Selected Objects

ou can flip a selected object(s) horizontally or vertically to better orient the Yobject(s) relative to other objects of the diagram. To flip a selected object:

enu. The Flip options menu appears to the

e Horizontal or Vertical.

nd then choose Flip om the Pop-up Unit menu to display the flip options.

diting Text You ny text object you placed on the

FD

ligning Text

ou can align text in two or more text boxes to the left, right or center of the box ey are drawn in.

o align text:

Select the text you want to align (you must select at least two) by clicking on the first text box, then click other boxes while holding down the <Shift> key.

Choose Align Text from the Edit menu. The align menu pop-up appears to the right of the Edit menu.

Choose Left, Center or Right.

Select an object(s). Choose Flip from the Edit mright of the Edit menu. Choos

Flipping an Icon You can also click the right mouse button on a unit icon, afr E

can size and or rotation of a change the text, main window. P

To edit text:

Double-click on the text object you want to change. The Draw Text window appears.

Edit as desired and choose OK. A Yth T


Chapter 6 Viewing Flowsheet Contents

Horizontal and vertical scroll bars allow you to change the visible portion m

mulation.

PRO/II scroll, pan, and multiple viewport

our flowsheet diagram in the PFD.

crolling the PFD

ou can scroll the PFD left, right, up, or down using the horizontal and vertical croll Bars. Both bars enable you to scroll in small or large increments or to scroll a general location.

e Pan ndow.

Zooming You m the View menu, using the zoom utt the keyboard.

r out, do one of the following:

PRO/II offers a variety of tools that aid you in viewing your flowsheet contents:

of the process flow diagra in the PFD main window. You may open additional viewport windows of your current flowsheet to display different views of your si The Pan View window is a special feature of PRO/II that enables you to

see a thumbnail of the entire flowsheet and use a bounding box in the thumbnail to move the visible area.

This chapter describes how to use the features to display portions of y S YSto

etting Scrolling Increments S YIn

ou can change the actual value for the scroll increments by altering thcrement value on the General Drawing Defaults wi

can access the PRO/II zooons on the toolbar, or using

m features frob To zoom in o

Click on the toolbar. Choose Zoom In or Zoom Out from the View menu. Choose <PgUp>or <PgDn> to Zoom in or Zoom out the PFD.

Chapter 6 Viewing Flowsheet Contents 73

Zooming in on a Selected Area

specific area of the flowsheet:

Click

You can specify the exact area of the flowsheet that you want to zoom in on.

o zoom in on a T

on the toolbar or choose Zoom Area from the View menu. encompass the desired area within the

selection rectangle outline.

PFD.

Zooming to Show the Full Flowsheet You can quickly display the entire flowsheet in the PFD. To use zoom to show the full flowsheet, do one of the following:

Click

Click and drag the mouse to

Release to complete the zoom area operation. The selected area fills the

on the toolbar. Choose Zoom Full from the View menu. Press <Home>.

Setting the Zoom Increment You can change the increment PRO/II uses to zoom in or zoom out within the General Drawing Defaults window. The default small zoom increment is 5 pixels and the default large zoom increment is 20 pixels.


Opening Multiple Viewport Windows

ou can open multiple viewports of a single simulation problem to display ifferent views of the flowsheet.

o open an additional viewport of the current simulation problem, do one f the following:

Click Multiple Viewports

Yd To

on the toolbar or choose New View on the

Note: If the multiple viewports button is not displayed on your toolbar, check tion from the View/Toolbar menu.

Window menu.

the Standard menu op

Figure 6-1: Multiple Viewports


Redrawing the Simulation You can use redraw to clear extraneous lines and dots from the PFD. To redraw the diagram, do one of the following:

Click on the toolbar. Choose Redraw on the View menu. Press <Shift+Home>.

Panning You can pan the contents of the PRO/II main window using the Pan window or the Small Pan or Large Pan options on the View menu. The Pan View window is a thumbprint of the entire flowsheet. A bounding box identifies the area of the flowsheet currently visible in the PFD main window. You move the bounding box or change its size to change how much or what portion of the flowsheet you see in the PFD. From the View menu, you can pan in large or small increments: up, down, left, or right. You can change the settings for the pan increment in the General Drawing Defaults window. Displaying and Hiding the Pan View Window To display the Pan View window:

Click on the toolbar or choose Pan View from the Window menu.


Figure 6-2: Pan View Window

an

Uwindow

indow

P

ning - Using the Pan View Window

se the bounding box to change the visible portion of the flowsheet in the PFD by moving, enlarging or reducing the bounding box in the Pan View . The flowsheet in the PFD view changes to match the area w

encompassed by the bounding box.


M ving To move the bounding box:

Click the mouse inside th Drag to a new location. The area enclosed fills the PFD.

ote: For a large flowsheet, us from

one area of the flowsheet Cha ging f the Bo To change e boun

Click and drag the bound duce the boun

Panning - Using the Menu Options

the image in the PFD nning ptions on the Zoom menu.

o pan the image a large or small amount:

Choose Large Pan or Small Pan from the View menu. The pop-up menu appears.

Choose Left, Right, Up, or Down. Setting Panning Sensitivity You can change the increment PRO/II uses to pan. The default small pan increment is 5 pixels and the default large pan increment is 20 pixels.

o the Bounding Box

e box.

N e the Pan View window to quickly switch to another.

n the Size o unding Box

the size of th ding box:

ing box border handle to enlarge or reding box. The area enclosed fills the PFD.

You can pan o

up, down, left, or right using the pa

T


Chapter 7 Data Entry Windows

ing the data ssociated with your PRO/II simulation. There are a number of libraries from

whi e data en

n

ou he Input units ar

olbar) entification string for at unit appears in red (on the PRO/II main window).

Defining the scope of the simulation involves:

Defining the simulation problem Selecting the components for the simulation Setting the thermodynamic methods for the simulation

Note: Chapter 8, Specifying Component, Thermodynamic and Stream Data,

and Chapter 9, Unit Operations and Utility Modules, provide explicit details on the use of the data entry windows introduced in this chapter.

A summary of the Data Entry Window buttons available on the PRO/II toolbar is provided below.

RO/II offers a wide variety of data entry windows for enterP

ach you can extract sets of data. This chapter provides an introduction to thes

try windows.

Defining the Simulatio Y can use the data entry window buttons on the toolbar or the options on t

menu to define the scope of the current simulation. PRO/II identifies which e missing data by putting a red border around the unit icon (on the . For units that are missing product streams, the idto

th


Problem Description Enables you to describe the current

simulation and relate it to a specific project.

Units of Measure Enables you to set units of measure

specific to this simulation. Each new simulation extracts defaults from the default Unit of Measure Set.

Component Selection Enables you to specify the components and

pseudo-components you want to use in the current simulation

Component Properties

Enables you to supply component properties.

Chapter 7 Data Entry WIndows 79

Thermodynamic Data Enables you to sele

methods for the current simuct thermodynamic

lation.

Assay Characterization

Enables you to modify TBP cut points and characterization options for the generation of pseudo-components from Assay streams.

kineProcedure Data Enables you to supply FORTRAN code for

tic reaction rate calculations without the need for compilation and linking.

Case Study Specification

Allows you to perform studies on a base case solution by altering parameters selectively and rerunning.

Reaction Data Enables you to define reactions and on, equilibrium, or

reaction sets. provide heat of reacti

kinetic data for

Calculation Sequence Enables you to specify a user-defined

calculation sequence.

Recycle Convergence Enables you to specify user-defined recycle

convergence and acceleration options.


Selecting Components Use this option to select the components and pseudo-components that you want to include in this simulation. To select components for use in this simulation:

Click on the toolbar or choose Component Selection on the Input menu. The Component Selection window appears.

Figure 7- 1: Component Selection

Select a component from the available lists or type the name of the component. Each component you select appears in the List of Selected Components box on the right side of the window.


Modifying Component Properties

m tructures feature to fill in missing component data for library or user-defined

To p

Click

You can use this option to modify fixed component properties or use the Fill froScomponents.

modify com onent properties:

on the toolbar or choose Component Properties from the Input menu. The Component Property Modification window appears.

Figu

re 7- 2: Component Property Modification


Selecting Thermodynamic Methods You use the thermodynamic data option to choose the thermodynamic method(s) for this simulation. To set thermodynamic calculation methods for this simulation:

Click on the toolbar or choose Thermodynamic Data on the Input menu.

Figure 7- 3: Thermodynamic Data

ou can specify a predefined system of thermodynamic calculation methods.

Select a category of predefined systems. PRO/II displays the predefined systems for this category in the Primary Method list box.

Select a predefined system from the Primary Method list box.

Y

Choose Add-> to define the calculation method.


Selecting Assay Data You use this option to modify the data obtained from the selected Assay Set. To select assay data for this simulation:

Click on the toolbar or choose Assay Characterization on the Inpumenu

t .

Figure 7- 4: Assay Cut points and Characterization

PRO/II always supplies the Primary TBP cut point set. You can modify the primary set or define a new cut point set or set characterization options.


Specifying Reaction Data You use this option to define reactions and enter heat of reaction, equilibrium, kinetic data for reaction data sets.

or

n: To specify reaction data sets for this simulatio

Click on the toolbar, or choose Reaction Data on the Input menu to w. open the main Reaction Data windo

Add a new Reaction Set Name or highlight an existing one. If desired, enter an optional description.

Figure 7- 5: Main Reaction Set Window

Click the Enter Data… button to open the Reaction Definitions dialog.


Figure 7- 6: Reaction Definitions Dialog


Specifying Reaction Procedure Data

r compilation and linking.

T

Use this option to create procedure blocks to calculate kinetic reaction rates. You are able to supply FORTRAN code for the reaction rate calculations without the need fo

o select procedure data for this simulation:

Click on the toolbar or choose Procedure Data on the Input menu.

Figure 7- 7: Main Procedure Data Window

Click a number at the left of a line to select an existing procedure or to add a new one.

If desired, enter an optional description. Click the Enter Data… button at the right end of the line to open the

Kinetic Procedure – Definition dialog. Write the code for performing the Kinetic calculations in this dialog.

Click OK to save the procedure and exit the dialog.


Specifying Multiple Simulations for Case Study

lation:

Use this option to make changes to input data and then examine the effect of those changes on the values of calculated data or functions of calculated data. To select case study data for this simu

Click on the toolbar or choose Camenu.

se Study Data from the Input

Check the Define Case Study box.

Figure 7- : Case Study Specification Dialog

8


Setting the Problem Calculation Sequence PRO/II performs a simulation by solving one unit operation at a time, following a

mulation:

certain calculation sequence to reach the problem solution. Use this option tospecify the method to determine this calculation sequence for the current problem.

To select calculation sequence for this si

Click on the toolbar or choose Calculation Sequence from the Input menu.

Figure 7- 9: Calculation Sequence Dialog

If desired, select a different Sequence Method. To exclude a unit operation from the calculations, highlight it in the

Available Unit(s) list and click the Exclude button. To restore an excluded unit operation to the Available Unit(s) list,

highlight it in the Excluded Unit(s) list and click the Include button. The positioning buttons (Move Up, Move Down, etc.) are most often used when the selected Sequence Method is Explicitly Defined by User.


Specifying Recycle Convergence You use this option to override the recycle loop sequence determined by PRO/II, and to specify acceleration methods and convergence tolerances for individual loops.

Note: This window is not available if you select the SIMSCI method for Calculation Sequencing, since the loops are determined automatically by this method.

To select recycle convergence for this simulation:

Click on the toolbar or choose Recycle Convergence on the Input menu.

Figure 7- 10: Recycle Convergence Options


Data Entry Windows for Unit Operations

he s

uttons, Check Boxes, Edit Fields, Spin Buttons, Standard ist Boxes, Drop-Down List Boxes, Grid and X-Y Grid, Combo Boxes, Drop-

wn Combo Boxes, Linked Text and Notes.

that e you to access different levels of help text. In addition, some main data

ntry windows (and some subordinate windows) provide UOM, Define and ble.

The data entry window for any unit operation can be accessed by highlighting tunit on the PFD and selecting the Input/Data Entry from the menu bar. Numeroutypes of data entry devices are used to supply numeric values and select calculation options in PRO/II, including: Push Buttons, Radio BLDo

Most main data entry windows provide Help, Overview, and Status buttons enableRange buttons. Grayed buttons indicate that the feature is currently unavaila

Button Description

Displays context-sensitive help for the active data entry field or for the window itself (if there is no active field).

Displays the main help window for the data entry window.

Displays the results of the data consistency checks performed for the main window after you choose OK.

field. Selects a unit of measure set for the selected data entry

References one stream or unit parameter value to another stream or unit parameter.

Displays the valid range of values for the active data entry field.

Displays the notes, associated with the unit.


Grids and the X-Y Grid Grids are used to supply data in tabular form. There may be several rows of related data entries. An X-Y Grid is a special type of grid that is used to supply data for relational curves. The two-grid columns contain an independent variable (x) and one related dependent variable (y). The Column Tray Hydraulics window shown below is an example of a grid. Notice that it provides columns for the starting tray number, ending tray number, calculation type, and entry of tray data. Each row has a numbered click button which is used to select the row for toolbar actions. For this example, several types of data entry devices are used in the grid. The starting and ending tray numbers are integer edit fields, the calculation type is a drop-down list box, and the entry of tray data is a click button, which brings up the Column Tray Sizing window or Column Tray Rating window, depe ing on the calculation type that was selected.

nd

Figure 7- 11: Column Tray Hydraulics Window

bserve that four rows are provided in the initial grid corresponding to five ections in the column. This may be expanded by clicking a row number button nd then clicking the Insert button. A row will be added below the selected row. hen the number of rows exceeds five, a scroll bar appears at the right side of e grid to provide access to the rows not displayed. To deselect a row, click the

ected row, or select a different row. To clear data entries from a row, click the row number button and then click Reset. To remove a row, click the row number button and the Cut button.

OsaWthnumber button of the previously sel


As another example, the Comshown below contains an X-Ycurve.

pressor Outlet Pressure Performance window grid for a user-supplied compressor pressure

Figure 7- 12: Compressor Outlet Pressure Performance Window

Notice that two columns are used for the pressure curve. The first column is the volumetric feed rate and the second column is the corresponding outlet pressure from the compressor. Four individual entries or cells corresponding to two rows in

e lls.

to

row may be deleted from the grid by clicking its number button and then licking Cut. To copy a row, first click its number button and then click Copy. The

row is copied into the clipboard. Next, click the row number button for the row which will be just below the copied row. Complete the copy by clicking Paste to insert a copy of the row from the clipboard.

the table are marked with a red border as mandatory input. Optionally, morpairs of information may be provided. The initial grid displays four pairs of ceNote that each row in the grid has a numbered click button which may be usedselect the row. The initial table may be expanded with the Insert button on the toolbar as described in the previous example. When the number of rows in the X-Y grid exceeds four, a scroll bar appears to provide access to rows not displayed. Ac


Linked text

ce format. Numeric values, athematical operators, stream or unit names, or various options may be

is used to input information in a sentenLinked text

msupplied as linked text. Linked text may serve to access another data entrydevice. The Feedback Controller data entry window containing linked text is shown in Figure 7-12.

Figure 7-13: Feedback Controller Main Data Entry Window - Initial Display

Linked text is used on this window to define the Specification and Variable.

arameter and Value texts in red require you to click them and provide data. TheP

oned

e type, i.e., relative ller window. Notice the

te a user-supplied value.

e

laye

text string the default tolerance is green, denoting a default value. Optionally, a different tolerance may be provided by clicking the afore-menti

w, where the appropriate text string to open the Specification Tolerance windoncradio button may be clicked to select a new tolera

ck Controtolerance. Click OK to return to the Feedbarelative tolerance text string turns blue, to indica When the value text string is clicked, a floating point entry field for th

mandatory input. The specification value is displayed with a red border signifyingow disp stead of the value text value you supply is n d in blue numbers in

string.


Clicking the Parameter text string retrieves the Parameter window in which the unit or stream and its parameter are defined. The unit or stream identifier and thparameter for the specification are now displayed in blue, replacing the Parameter text string.

e

Figu

re 7-14: Feedback Controller Data Entry Window - Final Display




Chapter 8 Specifying Component,

namic and Stream

his chapter describes several types of optional component, thermodynamic and stre upplied for PRO/II. In many cases, the default valu se sect

s considerable flexibility in the definition of component data. No limiFurtherm ata may originate from a variety of sources such as

IMSCI databanks, user-prepared databanks, user-defined components, and

tial search order when multiple databanks are used.

Tcompon te for nearly all simulation models. The AIChE

IPPR databank is also available as an add-on to PRO/II. User databanks of

hermodynamic Data Manager (TDM) programs, and maintained through PRO/II fully supported in TDM and ng experimental thermo-physical

ThermodyData T

am information which may be ses are satisfactory and it may not be necessary for you to visit theions.

Component Data General Information PRO/II provide

t is set on the number of components which may be used for any problem. ore, component d

Scomponents derived from petroleum assay data for feed streams. Moreover, you may stipulate a preferen

he SIMSCI databanks, SIMSCI and PROCESS, contain more than 1700 ents and are adequa

Dthermo-physical data can be created, using SIMSCI LIBMGR and the Tgraphical user interface. SIMSCI REGRESS isPRO/II, and provides the capability of regressidata to fit model equations.

Chapter 8 Specifying Component, Thermodynamic, and Stream Data 97

Selec Youdatabanthis win

ting Library Components

may select library components, from both SIMSCI and user-supplied ks, through the Component Selection main data entry window. To open

dow from the PRO/II main window:

Click on the toolbar, or select the menu bar item Input/Component Selection. The Component Selection window appears.

now the library access name for a component, you may enter it directly Add-> or press <Enter> to retrieve the component

If you kinto the data entry field. Click

If l t

ata entry ow.

t box. A

ost Commonly Used: Approximately 100 components representing all of the

am order: AcidAlcoAmAroEsteHalMis

ther Nitrogen Derivatives Paraffinic Hydrocarbons

from the component databank and add it to the List of Selected Components.the component cannot be located by the name you have entered, a warning wilrecommend that you use the Select from Lists… feature to locate the componenin the SIMSCI and PROCESS databanks:

Click Select from Lists… on the Component Selection main dwindow to open the Component Selection -List/ Search wind

Select a Component Family from the like-named drop-down lislarge number of component families are provided to speed the search. Abrief description is given below:

Mpure components commonly encountered in natural gas and petroleum processing. Hydrocarbon Light ends: Light gases commonly reported on analysis for oil refinery streams. All Components: Every component in the SIMSCI and PROCESS databanks. F ilies of Specific Chemical Type: Twenty families in alphabetical

s onents Additional Electrolyte Comphols Aldehydes

ides Amines matic Hydrocarbons Elements rs Ethers

ogenated Derivatives Ketones cellaneous Naphthenic Hydrocarbons

OSalts and Minerals Silicon Derivatives Sulfur Derivatives Unsaturated Hydrocarbons


For all families listed above, except for Hydrocarbon Light ends, you may define

mponents are located, transfer them to the Additions to Component ist box. When you have located all the components, click OK to return to the

Com Selecte The prio Databank

ierarchy button on the Component Selection main window to access the C This winsearch nents are always selected from the rst databank in the search order in which they appear.

dded libraries and databank names in TDM can be recognized this dialog box by Library Name: Databank Name.

Entering User-defined Components ser-defined component when you

nt Definition -

N

Def

indow. You may define any number of PETRO components in a single visit to this You mu at least two of the three correlating properties, normal boiling point, standard liquid density, and molecular weight for each component. Names

specific search criteria by selecting radio buttons and entering a search string. Use part or all of the component name, alias, or chemical formula as the search string. As coL

ponent Selection main window and to transfer the components to the List ofd Components.

rity order for databanks may be defined by pushing theH

omponent Selection – Databank Search Order window.

dow initially displays the default search order and may be modified to the databanks in any order. Compo

fi Note: The newly ain

You may want to enter a component as a uwish to use a component that is not in the PRO/II library.

Enter user-defined components by clicking User-defined… on the Component Selection main window to access the ComponeUser Defined window.

Type in the name of the user-defined component in the Component Name entry field.

Click OK to commit the new component name.

ote: At this point, you have only entered the name of the user-defined component in the database. Next, you must supply the properties for the component by the steps described below in Modifying Component Properties.

ining Petroleum (PETRO) Components Define PETRO components by clicking Petroleum… on the Component Selection main window to access the Component Selection – Petroleum Components w

window by using the tabular input provided.

st supply


may XX is the component normal boiling point. PRO/II uses internal correlations to esti All nece dynamic properties are computed from the threpredict possible

Note: ossible to enter data for assay pseudo-components (which are based on stream assay information) with this window. All properties for

cally defined by PRO/II. The components are also added to the component list by PRO/II.

Def Youspepro

be optionally provided or will be supplied by PRO/II as NBP XXX where X

mate the third parameter, when missing.

ssary physical and thermoe correlating properties. Molecular weight is the most difficult property to

accurately from generalized correlations and should be supplied when, for the most accurate characterization for a PETRO component.

It is not p

components derived from assay data are automati

ining Solid Components

can enter inputs for solid characteristics directly into PRO/II. You may cify stream properties, the particle size distribution, and the particle perties. PRO/II also allows you to input experimental solids solubility data.

To add a solid component to the flowsheet:

Click or select Input/Component Selection from the menu bar to open the Component Selection window.

Click Component Phases…. Ensure that the components that may be solid have the solid phase enabled. For example, if you enter NaCl for

sure that its component phase designation is

.g., Cyclone, Dissolver, Crystalliz

e cut points at are entered here. Grades will not be created on the open ends of the first

o change the units of measure for the particle size distribution, click in any of

ow.

use in a dissolver, make“liquid-solid”.

In a flowsheet that includes unit operations that require particle size distributions

er), choose Input/Component Property Data (efrom the menu bar. In the like-named window, click Particle Size Distribution… to open the Particle Size Distribution for Solids window. Enter PSD cut points for all relevant solid components. Particle size grades are bounded by ththand last cut points (i.e., if the cut points are 10 and 20 microns, there will be onegrade of 10 to 20 microns, not three grades of less than 10, 10 to 20, and greater than 20 microns). Tthe Distribution Ranges entry fields to enable the UOM button in the toolbar at the top of the wind


Deleting and Renaming Component Properties

.

t window. Enter the new name in the data entry field.

o reach is window:

Currently, actions on components that appear in the List of Selected Components in the Component Selection main window are limited to deletion or renaming of components. To delete a component:

Highlight the name of component in the List of Selected Components Click Delete.

To rename a component for printout purposes:

Highlight the component. Click Rename… to open the Rename a Componen

Modifying Component Properties You can modify properties for any component entered through the Component Selection main data entry window via the Component Property window. Tth

Select Input/Component Properties... from the menu bar or click on olbar.

indow is the master navigation point for changing all omponent properties.

names

tion:

tarting from this window, use the appropriate button to modify other properties:

the main to The Component Properties wc

Note: Component properties cannot be defined before the component have been entered.

There are three methods available for component property modifica Method 1: Specifying Fixed Properties Click Fixed… to open the Components Properties-Fixed Properties window. Here, you can modify fixed component properties such as molecular weight, critical temperature and NBP. With the exception of assay components, all components can be modified via this window. For those properties having UOM's, all data is displayed with the UOM’s of the current problem. S

Click Critical Properties… to specify critical temperature, critical pressure, critical volume and critical compressibility factor.


Click Molecular Constants… to specify properties such as Dipole Moment, Radius of Gyration, van der Waals Area parameter and van dWaals Volume parameter.

Click Heats of Formation… to specify Enthalpy of Formation and Gibbs Energy of Formation. In this entry, reference phase designation is a required input. The reference phase can be vapor, liquid or solid. Vapophase is the default.

er

r

Click Miscellaneous Properties to specify Acentric Factor, Solubility

Point eating

displayed will be the text “Missing.” You may reassign alues for any of these properties.

es

.

lick Temperature Dependent to open the Component Properties –Temperature

data Click ∆Ην to enter or modify latent heat data Click ρ to enter or modify liquid or solid density data Click µ to enter or modify vapor or liquid viscosity data Click κ to enter or modify vapor, liquid or solid conductivity data Click σ to enter or modify liquid surface tension data

the Component Properties - Data Source Selection window, choose the method of data entry. You may enter data either in tabular form or as coefficients for one of as many as 29 equations.

Parameter, Rackett Parameter, Liquid Molar Volume, Heat of Vaporization, Heat of Fusion, Normal Melting Point, Triple Temperature, Triple Point Pressure, Heat of Combustion, Gross HValue, Lower Heating Value, Carbon Number and Hydrogen Deficiency Number.

For PRO/II library components, the values in the database will appear in the various property windows. In cases where there is no library value to serve as the default, the defaultv Method 2: Specifying Temperature-dependent Properties You may enter or override default data for properties that change with temperature, such as density and viscosity, for the vapor, liquid or solid phasof the pure components in your simulation. You may supply new data in the form of tables or as correlation coefficients of one of 29 different equation types CDependent Properties window. All the library and user-defined components from the current problem are displayed. To enter or modify data for a property of a component, click on the corresponding push button for that component. For properties that may apply to more than one phase, you will first be required to select the phase for which you are to supply data in the Component Properties –Phase window,

Click VP to enter or modify liquid or solid vapor pressure data Click H to enter or modify vapor, liquid or solid enthalpy data Click Cp to enter or modify solid heat capacity

In


If you choose the Correlation Coefficients option, you may display the form of the

Select one of the correlations and supply coefficients as required. If the

uation that is ppears, and the border of the

e the Tabula Data o ponent Properties –Tabular Data ars.

hysical and Thermodynamic data of a chemical component has a profound

ager) – For reviewing and modifying pure component data

or generating

ata

r

equation by selecting the appropriate Correlation Number in the like-named drop-down list.

form of the equation is logarithmic, you may select the base of the logarithm. You may change the units of the equation and may impose maximum and minimum temperatures of applicability.

Note: The full range of equations can be found in the online PRO/II Reference

. If you choose an eqManual accessible via the Help systemnot standard, a message to that effect adrop-down list box will be yellow.

If you choos r ption, the Comwindow appe

Enter temperature and property data. You must enter at least one data pair.

PRO/II and TDM Integration Pimpact on the design and operation of a unit operation in a process industry. Users of PRO/II may utilize their own component data by using the Thermodynamic Data Manager (TDM program) to prepare the data; then use theLIBMGR program to store it in databases suitable for use by PRO/II. PRO/II in turn retrieves data from these libraries through library names and alias.

LIBMGR – For managing user-defined pure component and binary libraries.

TDM (Thermodynamic Data Man

REGRESS (now available from both TDM and PRO/II)– Fpure and binary interaction parameter data from experimental information.

Reporting – For publishing and archiving component and binary d Current versions of PRO/II are integrated with the Thermodynamic Data Manage(TDM). This integration provides the following advantages to all PRO/II users.

PRO/II can access data from the TDM-defined libraries as well as the default edlib.lb library provided by SIMSCI-Esscor and installed with PRO/II.


Users can launch TDM GUI in different mand databanks within libraries.

odes to define new libraries

ans, for example, a

st ver

Working w ges:

co ynamic parameters.

gra results. ry file. S

fun NeThe integration of PRO/II with TDM facilitates the simultaneous use of several lib yword inp on to the individual d s the form:

.

ISION Graphical User Interface, Library ID’s Component Selection nd Thermodynamic Data - Databank Search Order dialog box, the newly added nd existing libraries and databank names in TDM can be viewed. Users can elect and add the libraries and data banks for the current simulation.

ote: Refer to the Thermo Data Manager User Guide for detailed explanation on s functionalities.

The Thermodynamic Data Manager incorporates REGRESS functionality, so all data preparation activities may be performed withinthe single TDM program.

Due to new library naming conventions, different versions of libraries now may co-exist in the same directory. This mePRO/II version 7 library and a PRO/II version 8 library both may be used. It no longer is necessary to always replace older libraries with the newe

sion.

ith TDM provides these additional advanta

TDM allows users to build customized libraries containing pure mponent data as well as unary and binary thermod

TDM can generate and display a variety of temperature-dependent phical plots of tabulated data

Multiple databanks may be defined and available in a single libra TDM replaces DATAPREP (now obsolete) and includes REGRES

ctionality.

w Keyword Format for Declaring Library Data Banks

raries, each containing multiple databanks. Consequently, a new keut syntax now requires entering both the library (file) name in additi

ata bank name. This ha

LibraryId: DatabankId

For example, the former declaration of : BANK=SIMSCI, PROCESS

Now may be fully declared as: BANK= PROII_8.2:SIMSCI, PROII_8.2:PROCESS Note: The ID of the library shipped with PRO/II changes with each major versionRefer to the PRO/II Installagion Notes for the current library identifiers. The colon ( : ) between LibraryId and DatabankId always is required.

the PROVInaas Nit


Method 3: Specifying Fill From Structure

opens the Components Properties – Fill from ble Components list on the left side contains library

e ΟΚ

ructure using established correlations and

NIFAC Structures… on the

Data

s

boratory assay data into pseudo components.

t is defined as the weighted average temperature of its cut oint range. The TBP distillation must often be derived from another type of boratory distillation, using a conversion procedure. PRO/II accepts the following pes of laboratory distillations: TBP, ASTM D1160, ASTM D86, and ASTM 2887. While laboratory distillations are usually reported on a 760 mm Hg basis,

PRO/II has procedures to correct distillations for other laboratory pressures. Estimated values for the standard liquid gravity and molecular weight for each pseudo-component are also needed for the characterization process. The

The Fill from Structure buttonStructure window. The Availaand user-defined components from the current problem. You may add or removcomponents to be filled from structure to the like-named list on the right. Click to have the properties of the selected components filled from structure. PRO/II predicts properties from sttechniques. Joback (1985) significantly expanded the work of Lyderson (1955) in this area providing a group contribution method for the prediction of critical properties, boiling point, freezing point, ideal gas capacity, enthalpy, and Gibbsheat of formation. Joback used a4 large database of components to statisticallydetermine group parameters for 42 different functional groups. SIMSCI has extended this work to include several missing parameters. To complete the Fill from Structure procedure, click UComponent Properties window to display the like-named window. A UNIFAC Structure entry is mandatory for all components for which Fill from Structure hasbeen requested. Click UNIFAC Structures… adjacent to the component of interest to open the Define UNIFAC Structure window where you may choose from families of components or from the UNIFAC group number directly.

AssayGeneral Information For many petroleum-based streams, the composition is not fully known in termof defined components. These stocks must be characterized by pseudo-components for which the necessary physical and thermodynamic properties have been estimated. PRO/II has extensive procedures for the translation of petroleum stream la Pseudo-components are based on boiling point or “cut point” ranges on the true boiling point (TBP) distillation for the stock. The normal boiling point for a pseudo-componenplatyD


standard liquid gravity for each pseudo-component is derived from the gravity boiling point. The gravity t be estimated, based on

r weight curve

dicted from its normal boiling point and standard liquid gravity. All ther required physical and thermodynamic properties may be estimated from

the ili

he use of assay data in PRO/II is divided into two logical steps. The first step

/II are acceptable, this

us

, C

r lation, keeping calculation times smaller.

curve for the stream, in similar fashion to the normal curve for the stream is often not available, and it musthe average stream gravity and the distillation curve. The moleculais seldom available, and the molecular weight for each pseudo-component is usually preo

normal bo ng point, standard liquid gravity, and molecular weight.

Tinvolves the definition of the cut point ranges and selection of the characterization options used in development of the pseudo components. Characterization options include distillation curve fitting and conversion methods,gravity curve generation procedure, methods for prediction of molecular weight, and methods for estimation of critical properties and ideal gas enthalpies. If the efault cut point ranges and methods furnished by PROd

step may be omitted. The properties for all pseudo-components derived from the same cut point set are averaged, based on the stream flows, to develop a common set of blend components. This technique provides reasonable results when the streams have similar chemical natures. For example, all of the assay streams are products from the crude distillation unit. However, when assay streams are dissimilar chemically, such as virgin materials and cracked materials, there may be seriorrors in the characterizations for the streams when a single set of blend e

components is used. For this reason, you are allowed to define additional cut point sets. For examplean additional cut point set may be defined to represent the products from an FCreactor. Note that it is not necessary or desirable to define a separate cut point set for each assay stream. Similar streams may be grouped by using the same cut point set without a serious loss of accuracy. This also minimizes the numbe

f components in the simuo The second step is supplying the petroleum stream laboratory assay data to PRO/II. This step is accomplished in the setup of initial feed streams and is discussed in the Stream Data section of this chapter.


TBP Cut point Sets TBP cut point sets are defined in the Assay Cut points and Characterization maindata entry window. This window may be reached from the PF

D main window in

o ways: tw

• Click with the distillation pseudo-component curve on the toolbar, orselect the menu bar item Input, then select the menu item Assay Characterization.

A Primary Cut point Set is always provided as a default by PRO/II. This set has the following cut point definitions:

he default cut point ranges are usually reasonable for crude oil problems. They

r form is provided r editing of the primary cut point set.

king

m is provided for efinition of the cut points. This window is also used to modify existing secondary

Modify on the Assay Cut points and hting a secondary cut point

ighlighted secondary cut point sets in the Assay Cut points and ....

he Default Cut point Set is used for all streams for which a cut point set is not spe e or more point sets have been defined, the default cut point set may Cut points and

haracterization main data entry window. It is convenient to define the cut point

Cut point Range, Deg F Cut point Range, Deg C No of Cuts 100 - 800 38 - 427 28 800 - 1200 427 - 649 8 1200 - 1600 649 - 871 4 Tmay be modified in the Assay Data Primary TBP Cut points Definition window which is accessed by clicking Modify... on the Assay Cut points and Characterization main data entry window. A convenient tabulafo Additional or Secondary cut point sets may be added to the problem by clicDefine New Cut point Set... on the Assay Cut points and Characterization main data entry window to access the Assay Data Secondary Set of TBP Cuts. A cut point set name is supplied on this window and a tabular entry fordcut point sets and is accessed by clicking

haracterization main data entry window and highligCset in the Defined Secondary Sets list box, on the Assay Cut points and Characterization main data entry window. HCharacterization main data entry window may be deleted by clicking DeleteThis action removes the secondary cut point set from the problem. T

cified. Initially, it is defined as the Primary Cut point Set by PRO/II. After on Secondary cut

be changed via the drop-down list box on the Assay Cset which is used the most often as the default cut point set.


Assay Characterization Options Assay characterization options are selected on the Assay Characterization

w. Several roupings of options are shown in this window, with all options selectable with

BP Curve

I

Procedure: Cubic Spline (default), Quadratic Polynomials, or

in

of NBP for Cuts: Liquid Volume Average (default) or Temperature Midpoint.

8 or Version 6

nd became the default in PRO/II 8.0. In PRO/II 8.1, yet another improvement

Options window which is reached by clicking Characterization Options on the Assay Cut points and Characterization main data entry windogradio buttons. The option groups are as follows:

Criticals, Ideal-Gas Enthalpy: SIMSCI (Twu) method (the default), Cavett method, or Lee-Kesler method.

Molecular Weight: SIMSCI (Twu) method (the default), Old (1967) API method, or Extended 1980 API method.

Gravity Curve Generation Method: Constant Watson K from T(default), or Constant Watson K from D86 Curve.

Distillation Curve Inter-conversions: API 1987 (the default), API 1963, AP1994, or Edmister-Okamoto.

Fitting Probability Density Function (PDF).

Distillation Boundaries: Initial Point and End Point percentages.

Include in PDF: Include Initial Boiling Point in fit, and/or include End Pointfit.

Calculation

Curve Fit: Current or Version

The characterization options are explained in greater detail in the PRO/II helptext and the online PRO/II Reference Manual accessed via the Help menu. Version 6 was the only available option until the Improved method was implemented for PRO/II version 7.0. This was renamed the Version 8 method awas made and now is called the Current option. The Current option always will be the default, even if upgraded. In the future, when the Current option is upgraded, the older Current method will be renamed and be made available as a new option.


Thermodynamic Data General Information The selection of appropriate thermodynamic methods is an important and necessary step in the solution of flowsheet problems. PRO/II provides a wide

nge of methods to allow solution of the wide variety of systems which occur in cess industries.

ermodynamic ethods in PRO/II and are comprised of liquid and vapor viscosities, liquid and

ies, and liquid diffusivities. While not strictly a transport nsion is also included. Transport properties find use in

g Curves

PRO/II, the selection of thermodynamic methods has been simplified by the

met uid and vapor enthalpies, entropies,

ther ected for each flowsheet. For example, a sed

r individual units.

ed

rathe chemical pro Thermodynamic properties are an integral part of the flowsheet calculations. The equilibrium K-values (both VLE and LLE) are used to determine the phase separations. The enthalpies for the streams are used to determine the energy required to take a system of components from one set of thermal conditions to another. Entropies are used in the calculation of the isentropic operations and the Gibbs free energy minimization reactor. Liquid and vapor densities are used in heat transfer, pressure drop, and column tray sizing. Transport properties are selected in conjunction with the thmvapor thermal conductivitproperty, liquid surface terigorous heat transfer calculations, pressure drop determination, and columnsieve tray and packing calculations. Transport properties are also reported in thestream properties reports and may be requested in Heating/Coolinreports. Inconcept of the method set. Method sets consist of predefined thermodynamic

hods for K-values (VLE and LLE), liqvapor fugacities, and densities. Numerous predefined sets are provided. Multiple

modynamic method sets may be seldefault set may be specified for the overall flowsheet and other method sets ufo A facility is also provided to modify the thermodynamic methods in the predefinmethod sets. Certain parameters for some of the thermodynamic methods may also be supplied.


Selecting Predefined Method Sets

in Selection of thermodynamic method sets is accomplished via the Thermodynamic Data window which may reached from the PFD main windowtwo ways:

Click with the phase diagram on the toolbar or select the menu bar item Input/Thermodynamic Data.

ategories of method sets can be selected in the list

The Rename option is used

later in this section.

ets are provided:

e used to calculate all thermodynamic

KS), -

For convenience, several Cbox on the Thermodynamic Data window. The Primary Method, i.e., the method used for calculation of equilibrium K-values, for each method set in the selected Category appears in a drop-down list box and may be selected to add the method set to the Defined Systems for the problem. The Defined Systems appear in a list box and each may be selected for further action by highlighting the desired method and clicking Modify..., Delete..., and Rename... on the Thermodynamic Data window. The method set for which action is to be taken is selected (highlighted) in the Defined Systems list box. Delete removes the selected method set from the problem. to change the name of the selected method set. This is useful when it is desired to use a method set more than one time in a problem, perhaps with different parameters. Modification of method sets is discussed The following Categories of method s Most Commonly Used: These method sets may be used for a wide variety of problems. Nearly all gas processing and oil refining calculations are handled satisfactorily. Method sets in this category are: Soave-Redlich- Kwong (SRK), Peng-Robinson (PR), Grayson-Streed (GS), Braun K-10 (BK10), Ideal, NRTL, UNIQUAC, and UNIFAC. Equations of State: Equations of state are applicable to wide ranges of emperatures and pressures. They can bt

properties, using the ideal gas state as the reference state. The cubic equations, in particular, are able to accurately predict critical and supercritical conditions. Equation of state method sets are: Soave-Redlich-Kwong (SRK), SRK-Kabadi-Danner (SRKKD), SRK-Huron-Vidal (SRKH), SRK-Panagiotopoulos-Reid (SRKP), SRK-Modified-Panagiotopoulos-Reid (SRKM), SRK-SIMSCI (SRSRK-Hexamer (HEXAMER), Peng-Robinson (PR), PR-Huron-Vidal (PRH), PRPanagiotopoulos-Reid (PRP), PR-Modified-Panagiotopoulos-Reid (PRM), BWRSBWRS), Lee-Kesler-Plöcker (LKP), and Uniwaals (UNIWAALS). (

Liquid Activity: Liquid activity methods use liquid phase activity coefficient models to represent the liquid mixture in phase equilibrium calculations. This


approach is useful for modeling strongly non-ideal liquid solution behavior. Methods available in PRO/II include: NRTL, UNIQUAC, Wilson, van Laar, Margules, Regular Solution, Flory-Huggins, UNIFAC, UNIFAC TDep-1, UNTDep-2, UNIFAC TDep-3, UNIFAC Free Volume, and Ideal. Generalized Correlations: Generalized correlations predict K-values with semi-rigorous equations. The Gray

IFAC

son-Streed and Chao-Seader correlations use the apor fugacities and empirical relationships for the s based on the convergence pressure concept. A

EAL).

r

ets tha

he PRO ation guidelines for the various

ite

tion

odynamic methods may be changed for the method set eing modified, including: K-value (VLE), K-value (LLE), liquid enthalpy, vapor

Redlich Kwong equation for vliquid fugacities. Braun K-10 ivariety of other correlations are used to predict the other properties, i.e., enthalpies, entropies, and densities. Generalized correlations are: Braun-K10 (BK10), Grayson-Streed (GS), Improved-Grayson-Streed (IGS), Grayson-Streed-Erbar (GSE), Chao-Seader (CS), Chao-Seader-Erbar (CSE), and Ideal (ID

pecial Packages: Special packages are designed to solve a particulaSindustrial application. Special packages in PRO/II are: Alcohol (ALCOHOL), Glycol (GLYCOL), Sour Water (SOUR), GPA Sour Water (GPSWATER), and

mine (AMINE) and CAPE-OPEN. A All Primary Methods: This category includes all of the primary thermodynamic

t are listed above. User-added Methods: This category includes all of thes15 user-added method sets that may be defined by the user.

/II online help texts provide applicTmethod sets, as well as a brief description for each method. More detailed information may also be found in the PRO/II Reference Manual (also available online). Table 8-1 at the end of this section gives a detailed list of the composthermodynamic methods used for each predefined method set. Modifying Predefined Method Sets Predefined method sets are modified via the Thermodynamic Data-Modificawindow which is accessed by clicking Modify... in the Thermodynamic Data window. The pre-selected thermodynamic methods for the various thermodynamic properties may then be changed in this window by following the steps given below:

Click on the Current Method drop-down list box corresponding to the Property type.

Select the replacement thermodynamic method. Any or all of the thermb


enthalpy, liquid entropy, vapor entropy, liquid densityfugacity (where applicable).

, vapor density, and vapor

d

... in the Property-specific ata field. Many of the methods use specific parameters, such as binary

be ic

are supplied by SIMSCI and may also be prepared by the user with the SIMSCI LIBMGR program.

uid activity methods include: fill

e

ey selection is optional and PRO/II will determine them when not

d by pre-selecting the key

t

n, trope bank. The

hoice of fill-in property prediction is entered on the Binary Data Fill Options ng the corresponding Enter Data... button on ification-Property Specific Data window.

Note: The newly added libraries and databank names in TDM can be recognizein this dialog box by Library Name: Databank Name. Some property-specific data may also be supplied and/or modified in this window for the thermodynamic methods by clicking Enter DataDinteraction factors, modified acentric factors, etc. A priority search order maydefined for the selection of these parameters from more than one thermodynamdatabank. Note that thermodynamic databanks

Property-specific data which apply only to the liqoptions for missing parameters, Henry’s Law options, and Poynting correction options. For the liquid activity methods, a vapor fugacity method may also bselected. Other property-specific data which may be modified include the dimensionless residence time correction factor for amines DGA and MDEA and the key (or dominant) components in each liquid phase for K-value (LLE) methods. Kcomponent supplied. However, convergence time may be enhancecomponents.

Fill-in Property Prediction PRO/II allows missing data to be “filled in” under several circumstances. For example, when the composition of an azeotrope and activity coefficient values ainfinite dilution are known for some pair of species, you can use this option to predict missing activity coefficient values at intermediate concentrations. VLE and LLE K-value parameters for liquid activity coefficient methods may be estimated by the UNIFAC, Temperature-Dependent UNIFAC, Regular Solutioor Flory-Huggins methods, or they may be obtained from an azeocwindow, which is reached by clickithe Thermodynamic Property ModChecking the box will fill in missing data from the azeotrope databank. A methodfor filling in missing binary parameters (using the UNIFAC, modified UNIFAC, Regular Solution, or Flory-Huggins methods) may be selected by choosing the appropriate radio button.


Equation of State Alpha Data The form to be used for equation of state alphas may be specified on the AlphSelection window. This window is reached by clicking the appropriate Enter Data... button on the Thermodynamic Property Modification-Property Specific Data window. The source of the alphas to be used in the equation of state may be designated by selecting the appropriate radio button.

Henry’s Law The Henry’s Law win

a

dow is used to specify whether or not Henry’s Law is to be sed in conjunction with a liquid-activity K-value method. This window is brought

w ne the solubility of certain components.

or

om

PoThecorrbro ing the appropriate Enter Data... button on the

hermodynamic Property Modification-Property Specific Data window. There are

. Default: This choice specifies that the Poynting correction will be used only if

2. U

. Do Not Use Poynting Correction: Do not use Poynting correction factor.

If eimet be selected from the following choices: Standard (25°C) Volumes,

ackett, Rackett One-Fluid, or Library Density Correlations. The default method is

standar ons on age 45.

uup by clicking Enter Data... on the Thermodynamic Property Modification-

ing the box on the Henry’s Law windoProperty Specific Data window. Checkauses Henry’s Law to be used to determic

Designation of solute components may either be determined by the programselected explicitly by choosing the appropriate radio button. If the solute

ponents are to be designated explicitly, the desired solute components must cbe selected from the list box on the Henry’s Law window.

ynting Correction Poynting Correction window is used to specify the use of the Poynting ection factor for liquid-phase fugacities. The Poynting Correction window is ught up by click

Tthree options to using the Poynting correction:

1a vapor fugacity method is chosen. se Poynting Correction to Liquid Activities: Use the Poynting correction factor for the liquid phase fugacity.

3

ther of the first two options is selected, then the liquid molar volume calculation hod may

RStandard (25°C) Volumes. Note standard vapor conditions are different from

d conditions for liquid molar volume. See Table 1: Standard Conditip


Amine Residence Time Correction Factor ine Residence Time Correction window is available only for the Amine data package thermodynamic method for K-valu

The Amspecial es. It is accessed by clicking Enter Data... on the Thermodynamic Property Modification-Property

es

A may be entered in this window. The default value for this

-Property Specific Data window, then clicking LLE Key

.

d in th

Bin.

The -activity-

eached by clicking Enter Data... next to

ntered must first be selected from the drop-down list oxes in the first two rows of the grid.

epending on the thermodynamic method set which has been selected, one or ore parameters characterize the interaction between the two components.

n the Binary Interaction Parameters window is initially brought up, the box at e top of the window must be checked in order to enable the grid where dividual binary interaction parameters are entered. For the NRTL and

UAC methods, there are several different forms of the binary interaction quations. For the NRTL method, the 5-Parameter equation is the default form.

UAC method, the default is the 4-Parameter form of the equation. or these two methods, a different equation form may be selected for each

Specific Data window, then clicking LLE Key Components... on the LLE K-valuwindow. A value for the residence time correction factor for systems containing amines MDEA or DGfactor is 0.30.

LLE Key Components The LLE Key Components window can be accessed whenever an LLE K-Value method is selected, by clicking Enter Data... on the Thermodynamic Property ModificationComponents... on the LLE K-value window. Both the light liquid phase and the heavy liquid phase can either be Determined During Calculations or User-specified by selecting the appropriate radio buttons. When the User-Specified radio button is chosen, a component must be selected in the associated drop-down list box. This drop-down list contains all available liquid-phase components. One component may be selected for each key Note: The newly added libraries and databank names in TDM can be recognize

is dialog box by Library Name: Databank Name.

ary Interaction Parameters A number of methods in PRO/II allow the entry of binary interaction parameters

se include equations of state for many properties and liquidcoefficient models for K-values. These parameters are entered on the Binary Interaction Parameters window, which is rBinary Interaction Parameters on the Thermodynamic Property Modification-Property Specific Data window. For each column of the grid, the two components for which the data is being eb DmWhethinUNIQe For the UNIQF


component pair from the Equation Format drop-down list box, in order to enter e data in the most convenient form. Depending on the selection in the Equation ormat list box, the appropriate rows in the grid become active. For most quation formats, many active parameters have default values of 0.0, except for e SRK-Modified Panagiotopoulos-Reid, PR-Modified Panagiotopoulos-Reid, lycol, Sour, GPA Sour Water, and Amine methods, where the default value for arameters cij and cji is 1.0.

ser supplied K-values

Av

rope se ed s d x. r x r K n

odynamic Property Modification-Property Specific Data window.

-values are supplied through Thermodynamic Data - User supplied dialog box by selecting either rrelated or tabular form.

tion Coefficient: Antoine equa s a default correl as re nce pr re. Th efficie have lt val f 0.0

ata: User needs t pply K st 2 temperature pointsall the relevant components.

nforma n def e in e lecting the “User Supplied n fo /K the

dynamic Property Modification window can aLE me

Mixing Data

specified. be uid y o h na p dif

c t b g a enamic Property-Modification-Liquid Enthalpy window beside the Heat

data ite hecki e box H f M indo tivauttons, and the excess enthalpy calculation method may be selected

the d ed rad utton. her o Red r ess s is chosen, then the Redlich-Kister binary parameters may be

e Binary Redlic ister P eters ow h is accessed. When entering the Redlich-Kister binary parameters for

re d and othe e aves of 0.0.

thFethGp

U

number of methods in PRO/II allow the user to overwrite the primary method K-alues. The user supplied K-values are entered for all related components on the

Thermo P rties - Uking Ente

r suppli K-valuet to Use

ialog bosupplied

This dialog box is the opened by clic Data... ne -values o

Therm The KK-values

the co

Correlaatm

tion is used ae co

ation with ues o

1 . fere essu nts defau

Tabular D o su -value for at lea for

Detailed iManual. Se

tion o ault correlations is avail” optio

ablr KVLE

PRO/II ReferencLLE in

ThermoKVLE/KL

lso overwrite the entire thod.

Heat of For the ideal thermodynamic method, an excess enthalpy method may be

on the Heat of Mixing window. This window is accessed by clicking Enter Data.. side liq enthalp n the T ermody mic Pro erty-Mo ication Data window, hecking he check ox and then clickin Enter D ta on th Thermodyof Mixing m. C ng th on the eat o ixing w w ac tes three radio bby choosing esir io b If eit f the lich-Kiste ExcEnthalpy methodentered in th h-K aram wind , whic by clicking Enter Data...any component pair, the Aij field is default value

quire the r param ters h


User-added Thermodynamic Data ect a user-added thermodynamic method, select one of the fifteen user-

ds from the drop wn list box in the ary Method ic Data window. The User-added Parame indow allows

meters for user-added thermodynamic subroutines. For each row of par nu rom 60 tered in the first colum

e parameter value is entered in the second column.

Notge ire er- the am ho ta

o

PRO/II CAPE- N ther ynam sers d thPEN property packages to perform thermodynamic property r str on fl eet. C -OP anda re th iform

dards for interfacing process modeling software components developed the n and ration em oce The anda

on of different software components like Unit Operations and amic Property Packages from different vendors into a single

Package ew CA OPEN Property

the v he pro ho orm all actions neces t om nd he d in the Wind

ins n, yo launch PRO/II and immediately use the new PEN soft omp . W AP N i ed in the

gory" list box, a dialog displays a tree control filled with registered CAPE- pa s an mod s st s t

ckage. To view the vendor information, components supported, pported and phase supported for the particular property package,

APE-OPEN property packa d c w. y package system can be selected for unit operations and streams.

Cape Open Property Package is selected for stream or unit operation s, the PRO/II Flash calls the Equi function in the proper

e. If CalcEquilibrium fails, PRO/II us other properties, such as fugacity m ty pa .

To seladded methoThermodynaminput of para

-do Prim field on the ters w the

the grid, the ameter mber (f 1 to 2 0) is en n and th

e: The User-added Subroutines supplement (an add-on to the standard PRO/II packa ) is requ d for us added rmodyn ic met ds. Con ct your local SIMSCI office for more inf rmation.

CAPE-OPEN Property Package The OPE mod ics capability enables u to ad ird party CAPE-Ocalculations fo eams owsh APE EN st rds a e un stanspecifically for allow integrati

desig ope of ch ical pr sses. se st rds

Thermodynsimulation.

Selecting the CAPE-OPEN PropertyTo install a n PE- Package, execute the install program provided byto copy the files

endor. To your c

install puter a

gram sset up t

uld perf require

sary ows entries

Registry. After CAPE-O

tallatioware c

u canonents hen C E-OPE s select

“CateOPEN propertyproperty pa

ckage d ther ynamic ystems. User mu elec

properties suselect the Cthermo

ge an lick Vie Propert

Property Calculations When acalculationpackag

Calces

librium ty

coefficients, fro proper ckage


Defining Transport Properties

w s d n port Propert hec M n o tie

herma ctivities, liquid surface n, uid itiemay be selected on a global basis dio buttons a : specify individually, pure-

t averag trol sed ations, the TRAPP m r methods. Note that the TRAPP method does not predict liquid

ension. The petroleum method d ict operty when selected.

wn list box y be to r an e g etoptions for the pro

sities , pu po er etr cor , rrelation, Bromley-Wilkey c E

sities: Non , pure-component average, petroleum correlation, correl PI tion CI ti ma osi

ray-Clark, Twu viscosity w/Twu Bull mixing rule, API viscosity mi e, T oef ro d), m (p

oose Woeflin (petro method), Tight Woeflin (pure method), ef oe re ), P.

mal conductivities: None, pure-component average, petroleum TR orre CA E -a

Liquid thermal conductivities: None, pure-component average, petroleum ons, TRAPP cor , L rre AP roc 2A

API 96 Procedure 12A4.1 (High Pressure), CAPE-OPEN, user-added.

Liq

d.

Th ption r the s a on the Specify Individ ptio lec the ort System.

iffu No ke-

d d is not allowe qui ivity latio

u d ort method, c the dd rourom the Transport Properties window and select one of the five methods

from the drop-down list.

Transport proProperties wi

perty methods are selected in the Thermodynamics –Transport ndo

Thermodynami which i

System – accesseodificatio

by clicki window

g Trans. Transp

ies on ts, i.e.,

rt proper

viscosities, t l condu tensios

and liq diffusiv s via ra

componenuser-added

es, pe eum-ba correl ethod, o

surface tTRAPP is

is use to pred this pr

Drop-dowith these

es ma used perties:

eplace y of th lobal m hods,

Vapor visco : None re-com nent av age, p oleum relation

TRAPP co

orrelation, CAP -OPEN, user-added.

Liquid viscoTRAPP

eation, A correla , SIMS correla on, kine tic visc ty,

Lohrenz-Bw/Twu Bull xing rul ight W lin (pet metho Mediu Woeflin etro method), LMedium Wo lin (pure method), Loose W flin (pu method CAPE-O EN, user-added

Vapor ther

correlation,

APP c lation, PE-OP N, user dded.

correlati relation atini co lation, I 96 P edure 1 3.2,

uid surface tension: None, pure-component average, petroleum correlations, Parachor/Tacite, API 82 Procedure 10A3.2, CAPE-OPEN, user-adde

Note: e None o fo method above is vailable ly when

ually o n is se ted for Transp Liquid d sivity: ne, Wil Chang.

Note: A user-adde metho d for li d diffus calcu ns.

To select aoption f

ser-adde transp hoose User-a ed Sub tine


Note: T

PRO/II package) is he User-add rou upp t (a n t tan

required for user-added transport methods. Contact your local SIMSCI office for more information.

The PRO/II online help text provides additional information about the various transport property methods. More information may also be found in the PRO/II Reference Manual.

Specifying Water Decant Options When a method set which supports two-liquid phase calculations is selected via the Thermodynamic Data window, the Thermodynamics -Liquid- Liquid Options window appears. Radio buttons on this window may specify using a single liquid phase in the calculations (the default) or that two-liquid phase calculations are performed.

For method sets that support water decant, the user may optionally select to decant water as a pure phase. The methods used for the decant water calculations are selected via radio buttons in the Water Options window which is reached by clicking Water Options... on the Thermodynamic System-Modification window. The following options are available:

Calculation of Water Solubility in Non-aqueous Phase: SIMSCI Method (the default), Kerosene correlation, Compute from Equation of State (SRK and PR methods only). Additional options are available from the 1999 API Technical Data Book, Procedure 9A1.3. Options include LUBE, NAPH, APIKERO, PARA, GASO, JP3, and JP4.

Calculation of Decanted Water Properties: Vapor-Liquid Saturation Values, Steam Tables and IAPWS-IF97 Steam Tables.

Optionally, the user may also check a check box to use GPSA Data Book values for calculating the water partial pressure.

More details on decant of free water are given in the online help text and in the PRO/II Reference Manual.

ed Sub tines S lemen n add-o o the s dard


Table 8-1a: Predefined Most Commonly Used Thermodynamic Method Sets

Common: K

Vapor Liquid Vapor Liquid Vapor Liquid Vapor ity -value Method Enthalpy Enthalpy Entropy Entropy Density Density Fugac

Soave-Redlich-Kwong (SRK)

SRK SRK SRK SRK SRK API NONE

Peng- Robinson (PR) PR PR PR PR PR API NONE

Grayson-Streed (GS) CP CP CP CP SRK API NONE

Braun-K10 (BK10) JG JG CP CP IDEAL API NONE

NRTL (NRTL) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

UNIQUAC (UNIQUAC) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

UNIFAC IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL(UNIFAC)

Note: CP= Curl-Pitzer method, JG = Johnson-Grayson method, API= API Method

Table 8-1b: Predefined Generalized Correlation Method Sets

Generalized: K

Vapor Liquid lpy

Vapor Entropy

Liquid Entropy

Vapor Density

Liquid Density

Vapor Fugacity -value Method Enthalpy Entha

Braun-K10 (BK10) JG JG CP CP IDEAL API NONE

Chao-Sea(CS) NE der CP CP CP CP SRK API NO

Chao CP SRK API NONE -Seader- CP CP CP Erbar (CSE)

Grayson-Streed (GS) CP CP CP CP SRK API NONE

Grayson-treed-Erbar

CP CP CP CP S

SRK API NONE


Table 8-1b: Predefined Generalized Correlation Method Sets (GSE)

Improved-Grayson-Streed (IGS)

CP CP CP CP SRK API NONE

Ideal (IDEAL) IDEAL IDEAL NONE NONE IDEAL IDEAL NONE

Table 8-1c: Predefined Equation of State Thermodynamic Method Sets Eqn of State: K-value Method

Liquid Enthalpy

Vapor Enthalpy

Vapor Entropy

Liquid Entropy

Vapor Density

Liquid Density

Vapor Fugacity

BWRS (BWRS) BWRS BWRS BWRS BWRS BWRS BWRS NONE

Peng-Robinson (PR) PR PR PR PR PR PR NONE

PR-Huron-Vidal (PRH) PRH PRH PRH PRH PRH API NONE

PR-Panagiotopoulos-Reid (PRP)

PRP PRP PRP PRP PRP API NONE

PR-Modified-Panag.-Reid (PRM)

PRM PRM PRM PRM PRM API NONE

Soave-Redlich- SRK API NONE Kwong (SRK) SRK SRK SRK SRK

SD

RK-Kabadi-anner (SRKKD) SRKKD SRKKD SRKKD SRKKD SRKKD API NONE

S(S

RK-Huron-Vidal RKH) SRKH SRKH SRKH SRKH SRKH API NONE

SRK-anagiotopoulos-eid (SRKP)

SRKP SRKP SRKP SRKP SRKP API NONE PR

SRK-Modified-anag.-Reid RKM)

SRKM SRKM SRKM SRKM SRKM API NONE P(S

S(S

RK-SIMSCI RKS) SRKS SRKS SRKS SRKS SRKS API NONE

SRK-Hexamer EXA) HEXA HEXA HEXA HEXA HEXA API NONE (H

Lee-Kesler-öcker LKP LKP LKP LKP LKP API NONE Pl

Uniwaals (UNIW) UNIW UNIW UNIW UNIW UNIW UNIW NONE


Table 8-1d: Predefined Liquid Activity Thermodynamic Method Sets

Liq AK-va

Vapor Density

Liquid Density

Vapor Fugacity

ctivity: Vapor Liquid Vapor Liquid lue Method Enthalpy Enthalpy Entropy Entropy

NRT AL IDEAL L (NRTL) IDEAL IDEAL NONE NONE IDEAL IDE

UNIQUAC (UNIQUAC) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

UNIFAC (UNIFAC) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

Wilson (WILSON) IDEAL IDEAL NONE NONE IDEAL IDEAL NONE

van Laar (VANLAAR) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

Margules (MARGULES) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

Regular Solution (REGULAR) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

Flory-Huggins (FLORY) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

UNIFAC TDep-1 (UNIFAC TDep-1) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL



UNIFAC Free Volume (UNIFAC Free Volume)

IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

Ideal (IDEAL) IDEAL IDEAL NONE NONE IDEAL IDEAL NONE

Table 8-1e: Predefined Special Package Thermodynamic Method Sets

Special: K-value Vapor

EnthalpyLiquid

Enthalp Vapor Entropy

Liquid Entropy

Vapor Density

Liquid Density

Vapo

Method y

r Fugacit

y Alco(NRT IDEAL hol SRKM IDEAL SRKM SL) RKM SRKM IDEAL

Amin(AM NONE e

INE) SRKM AMINE SRKM SRKM SRKM IDEAL

Glyc(GLY I NONE ol

COL) SRKM SRKM SRKM SRKM SRKM AP

Sour Water NE (SOUR) SRKM IDEAL SRKM SRKM SRKM IDEAL NO


GPA Sour Water SRKM IDEAL SRKM SRKM SRKM(GPSWAT)

IDEAL NONE


Stream Data

e. Supplied data for tear streams or any other erations are used as estimates only and

ce streams are always assigned the composition of the

r rovide

s may

w point conditions, or fraction quid. For reference streams, only the temperature and pressure may be defined.

Enterin

ou can try window that

To ente

General Information This section of data is used to specify the thermal conditions and compositions for all feed streams in the flowsheet. It may also be used to furnish initial estimates of the composition and thermal conditions for recycle tear streams to enhance recycle convergencstreams which are products from unit opalways replaced by the next calculated set of values. Finally, Reference streams may be defined to eliminate thermal recycles. Compositional streams may be of two types: composition fully defined in terms of

efined components, or pseudo-components to be generated from petroleum dassay data. Referenparent stream. Compositions may be defined on a mole, weight, standard liquid volume or vapovolume basis, corresponding to typical laboratory data. It is necessary to pboth a laboratory distillation and stream average gravity for petroleum assay streams. Light ends analyses, gravity curves, and molecular weight curveoptionally be furnished to improve the characterization of petroleum assay streams. The stream thermal conditions may be specified in a variety of ways including: defined temperature and pressure, bubble or deli

g Stream Data

enter data for a stream on the flowsheet. The data enYappears contains any data you previously entered (as well as default values) for the selected stream.

r data for a stream:

Double-click on the stream or right-click on the unit icon and select EnterData... or select the stream and choose Input/Data Entry... from the menu bar.

Select the desired stream operation.

am name automatically assigned by the program is displayed in the ft hand corner of this window and may be edited as desired. If the streaermediate or product stream, a check box appears on this windowl estimate may be supplied for the stream.

The streupper le m is an int so that an initia


Select the Stream Type.

Figure 8-1: Stream Data Entry Window - Feed Stream


Specifying Composition Defined Streams

w rate basis as: Total Fluid Rate, r Individual Component Flow rates. A data entry box adjacent to the Total Fluid

ed standard vapor basis. Components

isplays

rate or a ge or action) an e ck box is provided to normalize the

Stream Thermal Condition

e supplied. re or Pressure via

r Liquid Volu re and the liquid fraction specifications

onally be specified for a reference tream. If not specified, the thermal conditions for the parent stream are used.

Within the Stream Data main data entry window:

Select the Composition Defined radio button. Click Flow rate and Composition to access the Flow rate and

Composition window. Radio buttons are used to select the stream flooRate button is used to enter the total stream flow in mole, mass, standard liquid volume, or standard vapor volume units. The stream composition is supplied in a drop-down list box, and may be suppli

n a mole, mass, standard liquid volume, or onot defined are assigned zero flow rates. If the total fluid rate was not given, the flow rate for the stream is taken as the sum of the stream composition. PRO/II

a running total for the composition as it is entered. d When the total fluid rate is supplied and the composition does not sum to that

rate of 100.00 ± 1.0 or 1.00 ± 0.01 (indicating composition percentarror is signaled. Optionally, a chefr

composition based on the specified total fluid rate, in which case no error is signaled for the above condition.

Specifying The thermal condition for all supplied streams except reference streams must be specified on the Stream Data main data entry window. Two specifications must

The first specification is selected as Temperatubthe First Specification drop-down list box and the value entered in an adjacentdata entry field. The second is chosen from the Second Specification drop-down list box as: Pressure, Bubble Point, Dew Point, Liquid Mole Fraction, Liquid Weight Fraction,

me Fraction. The pressuohave an adjacent data entry field. Thus, the thermal condition may be:

Defined temperature and pressure. Bubble or dew point (pressure defined, temperature calculated). Bubble or dew point (temperature defined, pressure calculated). Liquid fraction (pressure defined, temperature calculated). Liquid fraction (temperature defined, pressure calculated).

he temperature and pressure may optiT

s


Specifying Petroleum Assay Streams Within the Stream Data main data entry window:

Select the Petroleum Assay radio button. Assay window.

y field provided as selected by

clickingpseudopoint se

stimate mponents on the assay blend

and the

window. This window is used to enter the am.

The basVolume TM D2887 which is efaulted as weight. Note that gravity and molecular weight curves must be on e same basis, volume or weight, as the distillation curve. The distillation data

60 are assumed to be at a pressure basis of

The dis e required d is used. When only two points are give uadratic fitting option, at least three points must be given for TBP’s and five

as

Click Flow rate and Assay to enter the Flow rate and The flow rate for the assay stream is entered in the data entr

eight or liquid volume units. The cut point set for the blend may bewclicking the hypertext string default set of TBP cut points to retrieve a list of theproblem cut point sets. The pseudo-component blending option is selected by

the text string included in. This option is the default and includes the -components generated for the stream in the assay blending for the cut t. The excluded from option is used when the assay stream is a recycle and the effect of its estimated pseudo-coe

properties is not wanted. Entry of the various assay data is discussed below. More information on the various laboratory tests is given in the PRO/II help text

PRO/II Reference Manual. Laboratory Distillation

Click Define/Edit Assay... on the Petroleum Assay Stream window to enter the Assay Definition laboratory assay data for the petroleum stre

Select the type of distillation via radio buttons as: True Boiling Point (TBP), ASTM D86, ASTM D1160, or ASTM D2887.

is for the distillation may be chosen as: Liquid Volume or Weight. Liquid is the default for all distillations except the AS

dthfor TBP, ASTM D86, and ASTM D1114.696 psia. If not, enter the laboratory pressure in the data field provided. For ASTM D86 distillations, a Correct for Cracking check box is provided for application of the API Data Book cracking correction to the distillation

mperatures. te

tillation data are entered in the table provided. At least two points ar when the cubic spline fitting metho

n, PRO/II uses a probability density function to fill in the curve. For theqpoints for other types of distillations. PRO/II needs the entire distillation curve from zero percent to one hundred percent and extrapolates and interpolates necessary. Wise engineers perform their own extrapolations outside of PRO/II, using their knowledge of the stream being characterized.


Gravity Data The type of gravity data is denoted by radio buttons on the Assay Definition window as: API Gravity, Specific Gravity, or Watson K-Factor. The stream

verage value must be supplied in the data entry wia ndow provided. Optionally, a

ght...

ght dow.

ds... on the Assay efinition window to access the Assay Light ends Data window. The light ends

composition may be entered on a mole, mass, standard liquid volume, or le 1: Standard Conditions on page 45 for

The light ends rate is determined such that the normal id percent of the highest boiling light end exactly

matches the TBP curve. The light end components are kept in the same

Fractio

asis on

e light ends

ction)

Percent

ist box. If no basis is selected, the basis for the distillation

curve is assumed. When this option is chosen and the light ends r

gravity curve for the stream may be given by clicking Gravity Curve... on this window to access the Assay Gravity Curve window which provides a convenient tabular form for entry of the gravity curve.

Molecular Weight Data A molecular weight curve may be optionally given by clicking Molecular Weion the Assay Definition window to access the Assay Molecular Weight Data window. This window provides a tabular form for entry of the molecular weicurve. Optionally, the stream average value may also be supplied in this win Light ends Data ight ends data may be optionally provided by clicking Light enL

D

standard vapor volume basis. See Tabdifferences in standard conditions. Any library component or petroleum component that was defined as a PETRO component may be designated as a light end. Several choices are available for specification of the total light ends flow. These choices are selected via radio buttons and are: Match to TBP Curve:

boiling point for the m

proportions as the supplied composition (the default).

n of Assay: The light ends rate is a specified fraction of the total stream rate. A basis of liquid volume or weight may also be selected in the Bdrop-down list box. If no basis is selected, the basis for the distillaticurve is assumed. When this option is chosen and thcomposition does not add to the specified fraction or to 100.0 ± 1.0 or 1.00 ± 0.01 (indicating composition percentage or composition fraan error is signaled.

of Assay: The light ends rate is a specified percent of the total stream rate. A basis of liquid volume or weight may also be selected in the Basisdrop-down l

composition does not add to the specified percent or to 100.0 ± 1.0 o


1.00 ± 0.01 (i mposition percentage or composition fraction) an error is signaled.

ndicating co

se Compositions as Actual Rates: The supplied composition is assumed to ional composition or percentage

Optionaspecifie

tal wh ual fraction, percent or a supplied rate and does not add 100.0 ± 1.0 or 1.00 ± 0.01.

e

Ube component flows, not fractcomposition.

Light ends Rate: The light ends rate is supplied directly in the data entry field

provided. When this option is chosen and the light ends composition does not add to 100.0 ± 1.0 or 1.00 ± 0.01 (indicating composition percentage or composition fraction) an error is signaled.

lly, a check box is provided to normalize the composition based on the d total light ends rate, in which case no error is signaled for a composition ich does not eqto

to

Assay Stream Thermal Conditions The thermal conditions for petroleum assay streams are specified in the samfashion as that already discussed for compositionally defined streams.


Specifying Recycle Streams ets

r may lculation details. Acceleration techniques can also be

pplied to speed closure of the recycle tear streams.

etting Recycle Convergence Options

ecycle convergence options are entered in the Problem Recycle Convergence and

win

The PRO/II calculation engine recognizes recycle loops and automatically sup loop calculations as needed. For many problems, the default techniques are satisfactory. For complicated flowsheets with nested recycle loops, the useprefer to define the loop caa S R

Acceleration Options window which may be reached from the PFD main

dow by clicking on the toolbar. The following Recycle Convergence Opt Converge all Streams:

rged within the recycle tolerances. This is the default.

sed by the SIMSCI PROCESS

d fied loops in which tolerances are supplied.

oleTole Com

em o

t.

re ult is

ing on the linked text numeric

diate results printed for recycle calculations by lick

com

ions can be selected with radio buttons:

Convergence is not attained until all flowsheet streams are conve

onverge only Tear Streams: Convergence is reached when all tear streams C

are converged. This is the option uSimulation Program.

Global recycle tolerances may be set in this window. These tolerances are useor all loops except user specif

T rances may be specified as relative or absolute via drop-down list boxes. rances are:

ponent: The allowed change in a stream component rate from one iterationto the next. The default is 0.01 on a relative basis.

T perature: Allowed change in a stream temperature from one iteration tanother. The default is ±1.0°F or equivalen

P ssure: Allowed change in stream pressure between iterations. The defa

0.01 on a relative basis. The smallest stream component mole fraction to test for convergence may be hanged from the default value of 0.01 by clickc

value. Note that for some problems such as amine plants, this threshold must be wered to test the residual acid gas components in the recycle amine solution. lo

Set the frequency of intermec ing the underlined value in the print statement: Print recycle stream

position every 0 recycle iterations.


The be enteredmaximu r of trials for each recycle loop to 20. Note that this is a global alue which may be superseded for a user specified loop.

ons are chosen via radio buttons:

Dire

pply Wegstein Acceleration: Use the Wegstein acceleration method. The ing

), er

pply Broyden Acceleration: Use the Broyden acceleration method. When this

e underlined (linked text) default value of 2. OrdStre window. This window has

o options available:

ccelerate User-specified Tear Streams: When this option is selected, tear s are selected in a drop-down list box and moved to the

Accelst m

User-spe fTo select user e or Explicitly Defin the Problem Calculation Seque

Click Convespecif

Then, click the check box beside User-specified Recycle Loops.

tabular form is used to supply recycle loop information. Each line in the table as drop-down list boxes which are used to select the Starting Unit and the nding Unit for each loop. The adjacent Enter Data... button is clicked to enter dditional recycle information via the Individual Recycle Loop Data window.

number of recycle trials to allow before non-convergence is signaled may by clicking the underlined value in the trials statement: Set default m numbe

v Acceleration opti

ct Substitution (No Acceleration): This is the default. A

following additional options may be chosen with Wegstein by clickunderlined default values: first iteration to accelerate (default is 2iteration interval for acceleration (default is 1), Wegstein lower and uppfactors (defaults are -5.00 and 0.00)

A

option is selected, the first iteration to accelerate may also be supplied by clicking th

inarily, all recycle tear streams are accelerated. Click Accelerated Tear ams... to access the Accelerated Tear Streams

tw Accelerate All Tear Streams: This is the default. A

streamerated Streams list box. Acceleration is only applied to these tear

rea s in the Accelerated Streams list box.

ci ied Recycle Loops -specified recycle loops, the user must first select the Alternated by User calculation sequence methods in

nce window.

User-specified Recycle Loops on the Problem Recycle rgence and Acceleration Options window to reach the User-ied Recycle Loops window.

AhEa


Information which may be entered in this window includes: Number of Trials: Number of iteration trials before non-convergence is signaledIf not supplied, the global value is used. Recycle Stream Conver

omponent, Temperatur

.

gence Tolerances: Tolerances may be supplied for the e, and Pressure changes. A threshold component level

te that the ow.

AccBroydenstre tein by clicitera

efaults 0). For Broyden, the first iteration to accelerate may lso be supplied by clicking the highlighted default value of 2.

may

h rent feed rates, one run may be made and the complete result scaled,

cluding the feed rate such that the desired product rate is achieved. To use

Cmay be supplied by clicking the underlined (linked text) default. Nolobal defaults are used when values are not supplied in this windg

eleration Options: The Direct Substitution, Wegstein Acceleration, or

Acceleration methods may be selected for acceleration of the tear am. The following additional options may be chosen with Wegsking highlighted default values: first iteration to accelerate (default is 2), tion interval for acceleration (default is 1), Wegstein lower and upper factors

are -5.00 and 0.0(da

Scaling Product Streams Scaling provides an easy way to ratio all of the results in a simulation such that the flow of one of the products is equal to a specified flow. For example, itbe desired to build a plant which produces a specified quantity of product, but theexact quantity of feed required is not known. Instead of making multiple runs witdiffein

the scaling feature:

Select Report Format from the Output menu. Select Miscellaneous Data from the Report For mat menu to access the Miscellaneous Report Options window.

to display the Product Stream Scaling window.

list box in the Product Stream Scaling window and select the stream

list boxes and the scaling rate is applied to the total of all components in

The rate ified range of components, is supplied in the data entry field provided. The Units of

Click Product Stream Scaling

Click the check box beside Scale Stream Flow rate. Next, pick the stream to scale from the Stream Name drop-down

components on which the scaling rate is based, with the radio button provided. The default is All Components. If the Range of Components isselected, the starting and ending components are chosen in drop-down

this range.

for the scaled product stream, either the total stream or a spec


Measure feature may be used to supply the scaling rate as moles, masd liquid volume units, or standard vapor volume units.

s, standar

on-scaleable Unit Operations Sdepend

ssur n the flow through e pipe and may not be directly scaled for other flow rates. PRO/II disables the

s are present which are non-scalable. The llowing unit operations are non-scalable:

SpA re a stream of identical composition to its parent stream.

ha sition of the parent stream immediately update the the new values in the parent ting thermal recycles in flowsheets.

ef to

ox.

Nome unit operation results are not scaleable, that is, the calculated results are

ent on the absolute flow through the unit. For example, the calculated e drop through a pipe of specified diameter depends opre

thscaling option when unit operationfo

Column Hydraulics, Rigorous Heat Transfer, Pipe, Depressuring, Plug Flow Reactor.

ecifying Reference Streams ference stream is nges in the compoC

composition of the reference stream to matchtream. This concept is very useful in eliminas

R erence streams are designated by double-clicking the stream on the PFD retrieve the Stream Data main data entry window, selecting the radio button Referenced to Stream, and choosing the parent stream in the drop-down list bOptionally, a rate may be supplied for the reference stream. If not supplied, the rate of the parent stream is assumed. Optionally, a temperature and pressure may be specified for the reference tream. If not specified, the thermal conditions of the parent stream are used. s


Copying Stream Data PRO/II allows you to copy the thermal and composition data for a selected stream. Process data for a selected stream can be copied to a new flowshstream or can be used to replace (overwrite) the currently existing data in another selecte

eet

d stream.

In the P

Select the desired stream to copy by clicking on the stream label with the

Creating a New Stream from an Existing Stream

RO/II main window:

mouse. D main

window or choose Select None on the Edit Menu to deselect the selected

he data for the selected stream can now be copied to a new stream as follows:

te on the Edit Menu.

T te that the PFD is

pied area of the PFD or feed port

Cre

exit stream mode. Theand Cop m In th

Select the desired stream to copy by clicking on the stream label with the left mouse button.

Choose Copy on the Edit menu. Click the left mouse button on an unoccupied area of the PF

stream. T

Choose Pas

he cursor will change to an arrow with a small “s” visible to indica now in stream mode.

Create a new stream by clicking the left mouse button on an unoccupiedarea of the PFD main window or on one of the available exit ports for a unit icon.

Drag the mouse to the desired unoccuof another unit.

Release the mouse button to complete the creation of the stream.

ate additional duplicate streams if desired, or

Click the right mouse button or press <Esc> to

newly created stream(s) will have the same thermal conditions, composition, description as the original source stream.

ying Data From One Existing Stream to Another Existing Strea

e PFD main window:

Choose Copy on the Edit menu.


Click the left mouse button on an unoccupied area of the PFD main window or choose Select None on the Edit menu to deselect the selected stream.

The data for the selected stream can now be copied to one or more existing treams as follows: s

Select the desired destination stream(s) with the left mouse button. Choose Paste on the Edit menu.

The data from the original source stream will be copied to thestream(s), overriding any existing. For compositionally-define

destination d streams

ted data tion, or vapor

com to

stream to copy by clicking on

containing calculated data, PRO/II allows the user to copy the calcula(temperature, pressure, and one of total composition, liquid composi

position) in the designated stream(s).

Select the desired compositionally-definedthe stream.

tton.

Choose Copy on the Edit menu. Select the desired destination stream(s) with the left mouse bu Choose Paste Special from the Edit menu.

You mainput da or liquid

s is because the product streams

are not involved in the calculation of new stream properties.

sets. Again, Paste Special can be

on the data if a new

pseudo-component is generated anywhere in the flowsheet.

y choose to paste only the input data of the selected stream or paste the ta and calculated data (using the total composition, or vapor composition, composition).

Note:

• Copy/Paste of an assay stream on to the product stream changethe blend option to XBLEND. This

• The Paste Special option is not allowed if new pseudo-components generate i.e., flowsheet reenabled by generating the calculated data.

• Pasting a calculated data of an assay stream using Paste Special (total composition, liquid composition, or vapor composition) targeted stream will erase their assay composition


Copying Input Stream Data Across Simulation Databases

lculated ata from the source stream to the input data slots of the destination stream. To

copthe Win To tran

p the second database using the File/Open menu. Paste

Special menu.

The Stream Data Link feature allows for the transfer of calculated stream data y

estination eature enables you

:

ake use of stream data previously calculated in an upstream

del each section of the flowsheet as a separate simulation, with

To

ing on it. Link option from the Input menu.

This n this winand the

lect from a list of available database files.

The Stream Data Link feature described previously will only transfer cad

y input stream data from one simulation database to another, you must use dows Clipboard.

sfer input stream data from one database to another:

Select File/Open menu to open the first database. Highlight the stream of interest and copy the input data of this stream to

the Windows clipboard by using the Edit/Copy menu. Open u

Paste the clipboard data into the destination stream using the Edit/

Linking Stream Data Across Simulation Databases

across PRO/II simulation databases. By using this feature, you can copcalculated stream data from a source database to the input data of a ddatabase. When modeling a large flowsheet, this practical fto

Quickly msection of the plant Avoid possible simulation errors due to manual re-entry of stream data Easily moeach section connected by a stream data link.

define a Stream Data Link:

Highlight the stream to be linked to a previous database by clickSelect the Define Stream Data

brings up the Define Stream Data Link window as shown in Figure 7-15. Idow you must select both the name of the previously-run database file, stream from that simulation to be linked to your current simulation.

Click on the Define Link check box. Enter the name of the previously-run database file, or click on the Browse button to se


Enter the name of the stream from the previously-run database tlinked to the stream in your current simulation, or click on the Bro

o be wse

button to select from a list of available streams.

Click to return to the main PFD.

N

Upd You ma ta link while defining that link or you may update all defi To u

e ent in the

ation will be ignored. If the source stream ontains assay pseudo-components, no component data will be copied to the

tion.

ta -import the keyword file.

ote: You can link a stream in the current flowsheet to another stream in the same flowsheet. This includes linking the input of the currently selected stream to the calculated output data for that stream.

ating Stream Data Links

y update a stream daned links at a later time via the Input menu.

pdate a Stream Data Link while defining that link:

Check the Update Now check box in the Define Stream Data Link window. Click Modify.

To update all defined Stream Data Links:

Select Update Stream Data Links menu option from the Input menu. Note: If the components are different in the two simulation databases, some component rate information may be discarded during the data transfer. If thsource stream has rate information for a component which is not pressecond database, that rate informctarget stream unless an identical assay exists in the current (target) simula Note: All stream data link information will be lost if you export the simulation dato a PRO/II keyword file and then re


RefinRef e in PROproperti ed in the PRO/II output and can be used in performance spe Ref

ecifying unit operation

Us -

whicexa

Using RefProperties Refinery Inspection Properties and User-defined Special Properties are used in the following ways:

Global pthrougheverywhData wi

Through the Stream Data Window

For streams that are to be defined in terms of assay curves, stream values of Refinery Inspection Properties and User-defined Special Properties can be

ntered either as curves or as average values or both.

Throughhe pro d are specified in the Thermodynamic Data i

anotherCompon

d ta entered for a thermodynamic at

ery Inspection and User-defined Properties inery Inspection Properties and User-defined Special Properties are availabl

/II for calculating bulk stream properties. The stream values of the es can be includ

cifications.

inery Inspection Properties comprises fifty-three predefined properties, commonly used by refineries for measuring and spperformance. Examples are cetane index, sulfur content, pour point, andkinematic viscosity.

er defined Special Properties can be defined for any other property for h component data or assay data can be provided. Possible

mples include auto-ignition temperature, color, $/tonne.

inery Inspection Properties and User-defined Special in a Flowsheet

Globally Through the Component Properties Window roperty data for each component in the flowsheet are entered

the Component Properties window. Values entered here are used ere in the flowsheet unless overridden through the Thermodynamic

ndow, as described below.

e

the Thermodynamic Data Window perties that are to be useT

w ndow. If there is more than one thermodynamic system in the flowsheet, some properties may be specified for use in one system and others in

. ent data for each specified property can also be entered for each ynamic system. Any component dathermo

system will be used in preference to the data provided globally wherever ththermodynamic system is invoked.


No e: A property is available only if it has been specified for a thermodyntem through the Thermodynamic Data window and is available only

t amic sys in those unit operations where that thermodynamic system is used.

Entering G Global com nent Properties w Values entered here are used everywhere in the f h

ntering

lobal Data Through the Component Properties Window

ponent data are entered for each component through the Compoindow of PRO/II.

lows eet unless overridden through the Thermodynamic Data window.

Refinery Inspection Properties ETo enter component refinery inspection property data globally:

Click on the toolbar or select Input/Component Properties.... The ponent Properties window appears.

k Refinery Inspection P

Com

Clic roperties to bring up the Component Property ow.

Select a property from the Property Name drop-down list box.

Use

ch component enter either a Data value or an Index value. For

may be entered. If the property is Kinematic Viscosity, enter values at two temperatures.

he stream y value is calculated from the individual component values

Note: these data will be used if no value is entered in the input. If

Selection for Refinery Inspection Properties wind

Click Enter Data... to enter global values. If the property is Kinematic Viscosity, the Component Data Entry for Kinematic Viscosity window willopen. Otherwise the Component Data Entry for Refinery Inspection and

r-defined Special Properties window will open.

For easome properties the index method is not applicable and no index values

Tu

propertsing a chosen stream mixing method.

The SIMSCI databank contains Refinery Inspection Properties for somecomponents; no data are present for a component, a fill method can be chosen through the Thermodynamic Data window (see below).


User-To ente

defined Special Properties r component user-defined special property data globally:

Click on the toolbar or select Input/Component Properties... fromenu bar. The Component Properties window appears. Click User-defined Special Properties to access the Component ProSelection for User-defined Special Properties window. Enter the name of a new Special Property in the Property Name drop-down list box or select a special property from

m the

perty

the list.

or

pecial Properties ry

spection Properties and User-defined Special Properties can be entered either as c

AsTo

d

Click Enter Data... to enter global values. The Component Data Entry fRefinery Inspection and User-defined Special Properties window will open. For each component, enter either a Data value or an Index value.

Entering Assay Data for Stream SFor streams that are defined in terms of assay curves, stream values of RefineIn

urves or as average values.

say Data for Refinery Inspection Properties enter assay data for refinery inspection properties:

Double-click on the stream on the PFD. The Stream Data window appears.

In the Stream Data window, click the Petroleum Assay radio button anthen click Flow rate and Assay to access the Flow rate and Assay window.

say Definition window.

priate dist

oInsp

In the Flow rate and Assay window, click Define/Edit Assay... to accessthe Stream Data - AsIn the Stream Data - Assay Definition window, first click the appro

illation method radio button and then click Refinery Inspection Pr perties to access the Assay Property Selection for Refinery

ection Properties window. Select a property from the Property Name drop-down list box.

Clicopen.

t es at

k Enter Data... to enter global values. If the Property is Kinematic Viscosity, the Assay Data Entry for Kinematic Viscosity window will Otherwise the Assay Data Entry for Refinery Inspection and User-defined Special Properties window will open. Enter the property value(s) as a stream average, a curve against PercenDistilled, or both. If the property is Kinematic Viscosity, enter valutwo temperatures.


AssaTo ente

ow

y Data for User-defined Special Properties r assay data for user-defined special properties:

Double-click on the stream on the PFD. The Stream Data window appears. In the Stream Data window click Flow rate and Assay to access the Flrate and Assay window.

In the Flow rate and Assay window click Define/Edit Assay... to access the Stream Data - Assay Definition window. In the Stream Data - As say Definition window click User-defined Special

the name of a new Special Property in the Property Name drop-down list box or select a special property from the list.

Properties to access the Assay Property Selection for User-defined Special Properties.

Enter

Click Enter Data... to enter global values. The Assay Data Entry for Refinery Inspection and User-defined Special Properties window will

st Percent

As l ProperThe pro e

hermo than one thermodynamic system be specified for use in one system and le only if it has been specified for a

erthermo Comthermoystem d in preference to the component Global data wherever that ermodynamic system is invoked.

o assign refinery inspection properties to a Thermodynamic System:

open. Enter the property value(s) as a stream average, a curve again

Distilled, or both.

signing Refinery Inspection Properties and User-defined Speciaties to Thermodynamic Systems perties that are to be used in the simulation must be specified through thdynamic Data window. If there is moreT

in the flowsheet, some properties may thers in another. A property is availabo

th modynamic system and only in those unit operations where that dynamic system is used.

ponent data for each specified property can also be entered for each dynamic system. Any component data entered in a thermodynamic will be uses

th T

Click or select Thermodynamic Data... on the Input menu bar item. The Thermodynamic Data window appears.

Select the system for which modifications are to be made in the Defined Systems box.

Click Modify... to access the Thermodynamic Data –Modification Window.

Refinery Inspection Properties. The Thermodynamic Method window appears. This

ow has a table in which properties and associated parameters and

Click Selection for Refinery Inspection Properties wind


data will be entered. To eliminate the need to enter standard sets of properties repeatedly, predefined lists of properties have been s

To load the table with a predefined list of properties, select from the et up.

table. operty from the Property Name drop-down list box in the table.

ns, and default selections, for the selected red. The options are:

ines the method used to mix component property for the stream. The available options are:

erty value and the component . The fraction may be molar, weight or liquid volume and is

am dry composition except for kinematic the dry liquid part of the stream. Any Index

data supplied for the property will be converted to property values

Predefined Lists list. Selecting None in this list removes all properties from the

Select a pr

This displays the available optioproperty. Change these as requi

Stream Method, which devalues to produce a value

f

i. Summation: The stream property value is determined by summing the product of the component propfractioncalculated from the total streviscosity when it is from

before the summation, using the equation: γ

Refe

Index ValueReference Value ⎟

⎞⎜⎝⎛

×= Index rence ⎠

ex is determined by summing the product of

ii. Index: The stream property indthe component property index and the component fraction. The fraction may be molar, weight or liquid volume and is calculated from the total stream dry composition except for kinematic viscosity when it is from the dry liquid part of the stream. Before the summation, any supplied property values will be converted to index values using the equation:

γ⎟⎞

⎜⎛

×= Value

Index Reference Index ⎠⎝ ValueReference

am property value.

iii. U

ch component and up to 20 real and integer

iv. am property value is determined by a user-added subroutine, which is linked into PRO/II. The same data as for the Index method is available to the user-added subroutine.

This equation is then used to convert the stream index value to the stre

ser-Formula: The stream property value is determined from the equation

in a user-added subroutine, which is linked into PRO/II. Data values may be entered for eadata values may also be supplied.

User-Index: The stre


v. SIMSCI: This method isviscosity. It is an i

vi. API: API procedures may be used to calculate flash point, cetane

mean average boiling point, cubic average boiling point, maverage boiling point, weight-average boiling point, volume-averaboiling pointcomponent d

only available for cloud point and kinematic ndex method but uses specific index equations.

index, ole-

ge , or net heating value. The API method requires no ata.

l

r

Formula Data Entry window opens. Otherwise, if the property is Kinematic Viscosity, the Kinematic Viscosity Data Entry window will open

vii. Nelson: This is an alternative correlation to calculate flash point and no component data are required.

viii. Stream Basis, which specifies whether the component values will be

mixed using their mole, weight or liquid volume fractions.

ix. Component Fill, which specifies the actvalues are missing for petro

ion to be taken when component eum fractions in the stream. The

available options are:

a. Zero: This option sets the prope ty value to 0.0. b. No fill: This produces warning messages for missing data and set to 0.0. c. SIMSCI: This option estimates m

kinematic viscosity, smoke pissing data by SIMSCI correlations for oint, hydrogen content, carbon content

or carbon-hydrogen ratio. d. API: This estimates missing data by API methods for kinematic viscosity,

pour point or refractive index. e. Nelson: This option estimates missing data by Nelson method for smoke

point. x. Component Blend, which defines the way in which missing data are

handled when calculating properoptions are:

ties from blended assay streams. The

a. Zero: The property value for the cuts in the assay with no data is set to 0.0.

b. Exclude: The property is calculated by blending only those assays, which have data for this property.

c. Missing: For this option, the blended property is not calculated and is reported as “Missing”.

Click Data… to enter data for thissystem. If the Stream Method is

property, for this thermodynamic defined as User-Formula, the User


and for oSpecial P

ther properties, the Refinery Inspection and User-defined roperties Data Entry window will open.

In the Kinematic Viscosity Data Entry window or the Refinery Inspection cial Properties Data Entry window, for each er a Data value or an Index value. For each

alue

ter values at two temperatures.

component, enter a ed Subroutine. Up the subroutine.

ubroutine. Us To odynamic System:

and User-defined Specomponent, enter eithcomponent, enter either a Data value or an Index value. If an Index vis entered, Reference Index Data must also be entered. For some properties, the Index method is not applicable and neither Index valuesnor Reference Index Data may be entered. If the property is KinematicViscosity, en

In the User Formula Data Entry window, for each Data value, which will be passed to a linked User-addto twenty real and integer values an also be passed toThe meaning of the data is determined by the calculation s

er-defined Special Properties

assign user-defined special properties to a Therm

Click or select Thermodynamic Data... on the Input menu bar item.

w. r

erty from the list. Change the

re

Formula Data Entry window opens. Otherwise, the Refinery Inspection ined Special Properties Data Entry window opens.

The Thermodynamic Data window appears. Select the system for which modifications are to be made in the Defined

Systems list box. Click Modify... to access the Thermodynamic Data Modification Windo Click User-defined Properties. The Thermodynamic Method Selection fo

User defined Properties window appears. This window has a table in which properties, associated parameters and data will be entered.

Enter the name of a new special property in the Property Name drop-down list box or select a special propavailable options and their default selections as required. The options are:

• Stream Method, which defines the method used to mix the component property values to produce a value for the stream.

• Stream Basis, which specifies whether the component values will bemixed using their mole, weight or liquid volume fractions.

• Component Blend, which defines the way in which missing data ahandled when calculating properties from blended assay streams.

Click Data... to enter data for this property, for this thermodynamic system. If the Stream Method is defined as User-Formula, the User

and User-def


In the Refinery Inspection and User-defined Special Properties Data Entry window, for each component, enter either a Data value or an Index value. If an Index value is entered, Reference Index Data must also be

Note: dynamic

ill include these Refinery

PrintinProper Refinclu

enu. Next, select the

entered.

In the User Formula Data Entry window, for each component, enter a Data value, which will be passed to a linked User-added Subroutine. Up to twenty real and integer values can also be passed to the subroutine. The meaning of the data is determined by the calculation subroutine.

If you have assigned Refinery Inspection Properties to a Thermomethod set, the standard Stream Data Report wInspection properties.

g Refinery Inspection Properties and User-defined Special ties

inery Inspection Properties and User-defined Special Properties can be ded in the PRO/II output reports.

Select Report Format from the Output mMiscellaneous Data... menu option. The Miscellaneous Report Options window appears. In the Refinery Inspection and User-defined Special Properties box, check one or both of the following options: Include Input Data —for a printout or data that has been input and/or Input Program Data —for a printout of data generated by PRO/

II. For

output of kinematic viscosity data:

Select Report Format from the Output menu. Next, select the Stream Properties... menu option. The Stream Property Report Options window appears. Enter two temperatures at which the kinematic viscosity results are required.


B

y be

(e.g., NRTL or UNIFAC), the following

s,

window which Binary VLE option from the Tools menu or by clicking is only available when at least two components and a

• Select

VLE (Validating Equilibrium Data) Tables and plots of binary equilibrium data for given pairs of components magenerated in order to ensure that they are valid in the required range of operation. Any thermodynamic VLE or VLLE K-value method may be used.

or liquid activity thermodynamic methods Fare calculated:

• K-values, • Liquid activity coefficient• Vapor fugacity coefficients, • Vapor pressures, and • Poynting correction.

For non-liquid activity methods, such as equations of state or generalized correlations, the following are determined:

• K-values, • Liquid fugacity coefficients, and • Vapor fugacity coefficients.

he validation is carried out in the PRO/II - Binary VLE/VLLE Data T

is opened by selecting theBVLE toolbar. This windowthermodynamic method have been selected. To generate a BVLE plot or table:

from the Tools menu or click BVLE toolbar to bring up the

BVLE to view Component and Thermodynamic dialog box. Users can view all the components that have been used in the current flowsheet on the left-hand side of this dialog box. Use

ta et format. Here, BVLE plots can be viewed similar to

PRO/II, but this plot uses TDM and Modular Thermo Data. elect the required components for the equilibrium calculations from the

r the value.

will m the

se,

ic in the PRO/II Reference Manual.

PRO/II - Binary VLE/VLLE Data window. • Click TDM Calculated

Diagram Tab to calculate and view the BVLE plot and its associated dain the Excel she

• Sdrop-down lists.

• Next, select constant pressure or temperature operation and ente

• Finally, click Calculate to generate plots (by default, all available plots be generated). If Excel is selected on the Plot Setup option, froOptions menu, tabular data are available in the spreadsheet. Otherwionly the plots are shown.

Note: For complete technical details, see the Utilities top



Chapter 9Unit Operations and Utility Modules This chapter describes how to use of utility modules such as t ptimizer

ilar functionalities.

ce, both th ules are resented. Simply <CTL >+click the hyperlinked name to go to the proper page.

. . . . . . 148 Heating/Cooling Curves. . . . . . . . 270

use unit operation models. Also described are the he Calculator, Controller, Flowsheet O

and sim

For ease of referen e unit operation models and the utility modp

Calculator . . . . . . . . . . . .

Column, Batch . . . . . . . . . . . . . . 170 Mixer . . . . . . . . . . . . . . . . . . . . . . . 274

Column, Distillation. . . . . . . . . . . 171 Multivariable Controller . . . . . . . 276

Column, Liq–Liq Extraction . . . . 193 Phase Envelope. . . . . . . . . . . . . . 280

Column, Side . . . . . . . . . . . . . . . . 199 PIPEPHASE Unit Operation . . . . 282

Compressor . . . . . . . . . . . . . . . . . 203 Pipe. . . . . . . . . . . . . . . . . . . . . . . . 286

Co ctor . . . . . . . . . . . . . 292 ntroller . . . . . . . . . . . . . . . . . . . 207 Polymer Rea

Cr cedure Data . . . . . . . . . . . . . . 294 ystallizer . . . . . . . . . . . . . . . . . 211 Pro

Cyclone . . . . . . . . . . . . . . . . . . . . 215 Pump. . . . . . . . . . . . . . . . . . . . . . . 302

Depressurizing Unit . . . . . . . . . . . 221 Reaction Data. . . . . . . . . . . . . . . . 304

Dissolver . . . . . . . . . . . . . . . . . . . 231 Reactor . . . . . . . . . . . . . . . . . . . . . 308

Expander . . . . . . . . . . . . . . . . . . . 238 Reactor, Batch. . . . . . . . . . . . . . . . 323

Excel Unit . . . . . . . . . . . . . . . . . . 232 Solid Separator . . . . . . . . .. . . . . . 324

Flash . . . . . . . . . . . . . . . . . . . . . . 240 SPEC/VARY/DEFINE . . . . . . . . . . 332

Flash with Solids. . . . . . . . . . . . . 244 Splitter . . . . . . . . . . . . . . . . . . . . . 326

Flowsheet Optimizer. . . . . . . . . . 246 Stream Calculator . . . . . . . . . . . . 328

Heat ser-added Unit Operations. . . . 348 Exchanger, LNG . . . . . . . . . 252 U

Heat Valve . . . . . . . . . . . . . . . . . . . . . . . 362 Exchanger, Rigorous. . . . . 256

Heat porator . . . . . . . . . 364 Exchanger, Simple . . . . . . . 266 Wiped Film Eva

Chapter 9 Unit Operations and Utility Modules 147

Calculator

GenThe C ile utility module useful for a variety of purposes in flowsheet simulation. Parameters may be retrieved from the flowsheet and calculations performed using a FORTRAN-like language. Parameters may be

se by other unit operations. Some uses for the

l stream properties

u

ecial output values for re

Computing utility costs and economic functions

t; the usefulness of this module is limited

ll Calculators have two main sections: Setup and Procedure. In the setup

sare defi lculated results, a sequence table is set up

r the streams used for input and output, and the dimensions for the various orking arrays may be expanded if desired.

he Procedure section is where all calculations are performed, using a simple nguage based on FORTRAN 77. The language permits the use of athematical functions, branching and looping, and assignment statements

ommonly used in programming. Special intrinsic functions are available for trieving flowsheet component and stream information. Special subroutines are

rovided for storing calculated results directly in flowsheet streams. Calculated sults may also be stored in the “Results” array, making them available to the

ther unit operations in PRO/II. A special solution “flag” is provided for use when Calculator models a unit operation.

eral Information alculator is a versat

returned to the flowsheet for uCalculator include:

Calculating specia

Simulating special processing units such as reactors

Determining operating conditions for other unit operations

Performing design calculations sing flowsheet information

Producing sp ports

Calculating target values for Controllers or objective functions for Flowsheet Optimizers

This is by no means an exhaustive lisnly by the ingenuity of the user. o

Aection, unit and stream parameters are retrieved from the flowsheet, constants

ned, names are assigned to cafow Tlamcrepreoa


Calculator Setup

y clicking Edit/View Declarations on the Calculator maStart Setup bindow to open the

in data entry View Area: w

Click Parameter rs into the Calculator.

These variabl s are accessed in the Calc dure aarray P. Click the Calculator parameter l pen ition

er cify the stre it et ter to retrieved. is window is identica at us r the FINE and PEC/VA /DEF ectio is pter. In th nd a list the un streameters t eved via DEF E.

s… to retrieve flowsheet parametee ulator proce

inked text to os elements of

the Definwindow wh e you can spe am or un flowshe paramebe DE

The format for th is described in th

l to thINE s

ed fon of the S

is window, you will fiRY

cha of it and am par hat may be retri IN

k Consta stant va s. Th aria essed in t dure as e ents ay C ough

n ente the pro dure, this array provides a ans for col that need upd cca ly into mmon lo

Clicacc

nts… to enter the conhe Calculator proce

lue ese v bles arelem of arr . Alth

you ca r constants directly in ceme lecting constants to be ated o sionala co cation.

k Results… to enter names for the Calculator r . The lues accessed procedure as eleme f ar ese

s will be utput report.

Clic esults se vaare in the Calculator nts o ray R. Thname used in the o

ick Stream define an ordered tab lowsams. The s for this t le. Firs rovidessary lin ure an e flow t stre or rmation fl n loo may b ormedure fo , using the positio theble to c

Cl Sequence… to le of f heet stre re are two function ab t, it p es a necinfo

k between the procedow. Second, a calculatio

d thp

sheee perf

ams fed in the

streams in proc r a range of streams ns of the ta ontrol the loop order.

Arrays… of the orage s use the ulator. T e the P, C arrays ed a , and

array t tream variables. T rray ed Calcula sion. Two additi rray ar

here. In earlier versions of the Calculator, all local variables had to reside in one of these arrays, V for real variables and IX for integers. Now that any valid FORTRAN variable name can be used, these arrays are no longer needed. Nonetheless, they are still available so that older Calculators will work without rewriting.

nce Setup is complete, click Hide Declarations to close the View Area.

Click to declare the length st array d by Calc hese arrays includ , R defin bovethe IS hat is used to hold s his a is describin the tor Procedure discus onal a s appe

O


Calculator Procedure

Note: The PROCEDURE section is required and must end with a RETURN statement.

The FORTRAN procedure is entered directly into the Procedure field on the Calculator main data entry window. The procedure may be checked as is it composed by clicking Check Procedure.

The supported features of the lang ctions. Elements of the Language Ea nt may con e ampersand (&) at the end of a line denotes continuati g line. Note that an asterisk (*) is not valid as ignifies multiplication. Al except th ay be preceded by a un label from in this manual). A $) causes a on the remainder of the line to be int a commen de. Unlike in FORTRAN, a ‘‘C’’ in co ot desi Predefined Variables Definitions of predefined va s for arrays, ap ing ta Calculator se t the Ar R sto y IX stores integer va e incl An

, P tes a single y.

A(index)

C, P, V, R, expression, such as (IX2 * 5). heses are r the same element as “An”.

In addition t FORTRAN va e used. T d may not du mes of an otherwise they follow the conventional FORTRAN tion of this feature in PRO/II 5.0

eans that the V and IX arrays need not be used. If this is the case, the arrays an be dimensioned to one word each to save memory.

uage are discussed in the following se

ch stateme tain up to 80 characters. Thon of a statement on the followin

a continuation marker, since it s

l lines of codeique numeric

e PROCEDURE statement m 1 to 99999 (shown as ‘‘nn’’

dollar sign ( ll following characterserpreted as t rather than as column one does n gnate a comment statement.

riables, including default dimensionpear in the follow ble. Use a DIMENSION statement in thetup section to rese number of elements in each array.

rays C, P, V, and lues. Forms of us

re values in floating-point form. Arraude:

where A is any of Celement of the arra

, V, R, or B, and n is an integer that indica

A is any of or B, and (index) is anThe parent equired. “A(n)” denotes

stead of, or inriables may

o the supplied V and IX arrays, standahey may be up to 8 characters long an

rd b

plicate the na y supplied variables; rules. The introduc

mc


Array "IS" is normally used as the index of a DO loop to step through a sequence of streams in the order defined on the SEQUENCE statement. It may serve as the stream index in PRO/II intrinsic functions. The only form allowed is ISn. IS(index) is never valid.

Predefined Variables

Variable Name

and F

Default Size (for

orm arrays) Description and Comments

Cn or C(index

1<=n<=50 d in the setup section. ide of assignment )

Constant values defineUsed only on the right sstatements

Pn or P 1<=n<=50 EFINE f

(index) Flowsheet parameters set by Dstatements. Used only on the right side o

. assignment statements

Vn or V <=n<=200 ay used on either the ssignment statements.

These elements are initialized to a large

(index) 1 A floating-point work arrleft or right side of a

negative value and are not available outside the calculator.

Rn orR(ind

1<=n<=200 The array of calculator results, used on either side of assignment statements. This results vector is available to other flowsheet modules external to the Calculator. These elements are

ex)

o a large negative value. initialized t

IXn or IX(index)

either side of assignment statements.

0<=n<=9 An array of integer values. The form IX(index) is invalid on a DO statement. It may be used on

ISn 0<=n<=9 An array of elements used as indices of DO loops for stepping through a series of streams in the order defined on the SEQUENCE statement.

ISOLVE This variable indicates whether or not the Calculator solved. It is initialized to 0 upon each entry into the calculation procedure. The user assigns all subsequent values using an assignment statement. 0 The Calculator has not yet executed (default)

or has solved successfully. 1 The Calculator solved. 2 The Calculator did not solve, but continue


Predefined Variables

VaN

and

Default Size (for arrays)

riable ame Form

Description and Comments

flows3 The Calculat

stop u

tion flag to ‘SOLVED’.

heet calculations within a recycle loop. or did not solve, all calculations

nconditionally. 4 The Calculator solved; but stops all

subsequent flow sheet calculations. This sets the flowsheet solu

MAXC Total number of components in the problem.

MAXS Maximum number of streams in the problem.

AN Statements FORTR

Prohis statement marks the start of the FORTRAN-based procedure section of the

3(j, k)... name1(i), name2(j, k)...

n the code. eparated

en defined by statement, variables assume the normal FORTRAN convention es starting with I through N as integers, and all others as real.

nged

cter.

ust not conflict with any reserved words or predefined variables Predefined Variables).

90:1995)

cedure TCalculator. It is required.

eclaration Statements DREAL rname1, rname2(i), rname3(j, k)... INTEGER iname1, iname2(i), inameDIMENSION

These statements are used to define local scalars and arrays for use iEach subscript may be an integer constant, or two integer constants sy a colon to specify both the lower and upper array bounds. Whb

the DIMENSION that assigns namName lengths may be 8 characters long. Variables defined here may be chain the code. Variables not defined here are assumed to be real or integer according to the first chara

Variable names msee table entitled(

Examples:

DIMENSION A(20,20), B(20), X(20) REAL MASS INTEGER COUNT, TAB(100) REAL REVENU(1990:1995), PROFIT(1990:1995), LOSS(19


Note: A variable may only appear once in these statements. The following is

in standard FORTRAN, but not in a Calculator Procedure:

MOLWT

Both standard FORTRAN and the Calculator accept this equivalent form: REAL MOLWT(50)

Assignment Statements nn variable =e ion

The “expression verned ORTRAN conventions. The operations on a given stateme g order: 1. Expressions w renthe ons and divisions ( *, /) 2. Functions nd subtractions (+,-) 3. Exponential ( With the exception of exponen ons with the same precedence are evaluated from l t. Mu ions without parentheses to explicitly specify the evaluatio rmitted.

For id:

L = A**B**C

The Calculator-supplied arrays C and may not appear on the left side

valid REALDIMENSION MOLWT(50)

xpress

” is go by standard Fnt are executed in the followin

ithin pa

ses ( )

4. Multiplicati5. Additions a

** )

tiation, calculatieft to righ ltiple exponentiat

n order are not pe

example, the following is inval

BADVA

Note: P of an assignment statement.


FORTRAN Intrinsic Functions he FORTRAN intrinsic functions tabulaT ted below can be used in

expressions:

FORTRAN Intrinsic Functions

Arguments Result Function Description Number Type Type

ABS DIM

Absolute Value Positive Difference

1 2

rearea

EXP INT LOG LOG10 MIN MAX

Exponential e Truncation Natural Logarithm Common Logarithm Minimum Value Maximum Val

1 1 1 1

>=2

real real real real real

real integer

real real real

MOD ue

Remainder >=2

2 1 1

l l

real real real real

real real

real real

integer real

NINT SQRT

Nearest integer Square Root

SIN Sine (radians) 1 COS Cosine (TAN ASIN ACOS ATAN

Tangent (radians) Arc Sine (radians) Arc Cosine (radian) Arc Tangent (radian)

1 1 1 1

real real real

real radian radian

SINH COSH

Hyperbolic Sine Hyperbolic Cosine

1 1

real real

real

TANH Hyperb

radians)

olic Tangent

1

1

real real

real

real

real real

real

real real


PRO/II Intrinsic Functions

ieval of stream and

r

Tc

he following table lists special functions that allow direct retromponent properties. In the table, “cno" represents an integer component

number which is an integer constant or variable, “sid” is a stream identifier or ISn value. This identifier must appear on the SEQUENCE statement to be used by a PRO/II intrinsic function. Property values are retrieved in the UOM used foproblem input.

PRO/II Intrinsic Functions

Function Description of Property

Pure Component Properties

CMW(cno) MolecuCNBP(cno)

CPC

lar weight Normal boiling temperature Specific gravity (60F/60F) Critical temperature Critical pressure

CSPGR(cno) CTC(cno)

(cno) CVC(cno) COMEGA(cno)

Critical volume, cc/gm-mole Acentric factor

Properties of Components in Streams

SCMF(cno sid) , sid)

Molar fraction of component in stream Weight

,SCWF(cno

(cnoo, sid)

fraction of component in stream ction

onent in stream Weight rate of component in stream

me rate of component of component

SCVF(cno, sid) SCMR , sid)

Standard liquid volume fraMolar rate of comp

SCWR(cnSCLVR(cno, sid) Standard liquid volu

s volume rate SCGVR(cno, sid) Standard ga

Stream Properties

SMR(sid) Mole rate of stream am

perature

SWR(sid) Weight rate of streSLVR(sid) SGVR(sid) STEMP(sid)

Standard liquid volume rate of stream Standard gas volume rate of stream Stream tem

SPRES(sid) Stream pressure


Stream Property Storage Subroutines nn CALL SRXSTR(type, value, sid) A call to SRXSTR stores a Calculator vector element as a property of stream “sid”. Values being stored must be

input. The resulting stream is ermodynamic state.

pe This entry identifies the stream property to store. Available options are

computed in the dimensional units used for dataflashed at the new conditions to determine its th tytabulated below.

Stream Properties Stored by SRXSTR

Type= Description

SMR mole rate of stream

standard liquid volume rate SWR SLVR

weight rate of stream

SGVR STEMP SPRES

standard gas volume rate of stream stream temperature stream pressure

valu . It

sid roperty. It may

CALL S 4), SR4)

nn C

type

e This argument supplies or identifies the value of the property to storecan be a real constant or variable.

The sid entry identifies the stream in which to store the pbe any stream identifier listed on the SEQUENCE statement of the setupsection, or an element of array IS in the form ISn. For example:

RXSTR(STEMP, R(1

SRXSTR stores the value of element 14 from array R as the temperature of stream SR4.

ALL SRVSTR(type, array, sid, i, j) A call to SRVSTR stores a range of values representing component stream properties from a Calculator array into a stream. The resulting stream is flashed at the new conditions to determine its thermodynamic state.

This entry identifies the component property to store in the stream. Available options are listed in the following table.


Stream Component Properties Stored by SRVSTR

Type= Description

SCMR SCWR

molar rate of component in stream

SCLVR

GVR

component standard of liquid volume rate componentSC

weight rate of component in stream

standard gas volume rate array culator array containing values to store as

onents in a stream.

sid o store the property. It may d on the SEQUENCE statement of the setup ay IS in the form ISn.

i, j ponent id numbers. They indicate the first and which the property is stored.

For exa

100 ) The sta lements V(12) - V(15) as the weight flow rates of compon ough 5 in stream FD1. Stream FD1 is re-flashed using the new omposition with the previous temperature and pressure.

alculation Flow Control Statements nn GOTO mm This is the standard FORTRAN statement that branches to label mm unconditionally. Writing “GO TO” as two words also is allowed. nn CONTINUE This statement serves as a branch destination or the end of a DO loop. It performs no calculations. IF Statements nn IF (expression) conditional clause. This statement allows logical branching during calculations and conforms to standard FORTRAN rules for “IF” statements. If the parenthetic expression is true, it executes the conditional clause. The conditional clause may not be one of the following:

The initial elperties of comp

ement of a real Calpro

The entry identifies the stream in which tsid be any stream identifier liste

rsection, or an element of ar

These two entries are comlast components, respectively, for

mple,

CALL SRVSTR( SCWR, V(12), FD1, 2, 5

tement stores eents 2 thr

c C


IF ELSEIF ELSE ENDIF

The following table lists logical operators allowed in the expression.

Logical Operators in IF Statements

Operator Description

.EQ.

.GT.

.NOT.

equal to

greater than

or equal to qual to

ivalent

true/false toggle

.NE. not equal to

.LT. less than

.GE.

.LE. greater than less than or e

.AND.

.OR.

.EQV.

both true either true equ

.NEQV. not equivalent

nn IF (expression) THEN

EIF (expressionELS

END These sallowing o words a

O Lo

Thisthrough tively. The nn DO

) THEN ELSE

IF

tatements conform to standard FORTRAN IF-THEN-ELSE statements, for structured branching of code. “ELSE IF” and “END IF” written as twre also accepted. Block “IF” constructs may be nested.

ops D nn DO mm iname= i, j, k

statement defines the beginning of a DO loop having a range extending statement label mm. “i” and “j” are initial and final indices, respec

increment step “k” is optional and defaults to 1.

mm ISn= sid1, sid2


his statement defines the beginning of a stream DO loop having a range l mm.

ds appearing on the ntal step index (comparable to k) is allowed.

RWRITE or APPEND)

LCULATOR output. For PC, VAX, and ms, the default output name is fileid.CAL, where fileid is the current

ame. A unique filename of up to 12 characters can be specified, if ary. It must, however, have a “.CAL” extension. Underscore characters

1). Any OPEN statement automatically closes the viously opened file.

ORMAT Statements

WRITE (*, format) expression, expression, ...

ORTRAN format control. Output will be he OPEN statement. The WRITE statement

riables, expressions, or array names. Specifying an array to be written.

statement refers to a FORMAT statement defining the output format. standard FORTRAN format items are supported.

ms Function

nIw.d Output integer data nFw.d, nEw.dEe, nDw.d, nGw.dEe Output real data ‘xxxxx’, nHxxxxx Output character constants Tn, TLn, TRn, nX Tab control kP Scale factor S, SS, SP Control of sign output /, : Line control n(...) Grouping

Textending through statement labe ISn is a stream variable, and sid1 and sid2 must be stream iSEQUENCE statement. No increme OPEN Statement nn OPEN(FILE=fileid, ACCESS=OVE The OPEN statement opens a file for CA

orUNIX platfe ninput fil

cessneare not allowed (e.g., FILE_0pre WRITE and F nnnn FORMAT (item, item, ...) These statements allow output using

the file most recently opened with t full F

tolist may include constants, va

causes all elements of the array nameRITE The W

The following Format Ite


OUTPUT Statement

nn OUTPUT {R(i :j ),P(i :j ),C(i :j ),V(i :j ),IX(i :j ),IS (i :j )}

provided with PRO/II. It outputs calculator-upplied arrays or portions of these arrays to the currently open file. Entries “i” nd “j” refer to the first and last elements of the array to be output. If they are bsent, the entire array will be output.

ISPLAY Statement

nn DISPLAY {R( i :j ),P( i :j ),C( i :j ),V( i :j ),IX(i :j ),IS(i :j )}

The DISPLAY statement prints out calculator-supplied array values to the standard report file during calculations. Entries “i” and “j” are defined in the same way as the OUTPUT statement. TRACE Statement

nn TRACE option TRACE statements control printing an historical trace as calculations proceed to facilitate debugging the code in the procedure. Options are:

ON Prints line number, statement number, and (action taken/new variable value) as each statement executes.

BRANCH Prints TRACE information only for branching statements such as IF, GOTO or DO.

OFF Turns off all TRACE options.

Examples:

TRACE BRANCH Traces branching only.

TRACE OFF No trace at all.

TRACE ON Traces every statement. Calculation Termination Statements nn STOP - This statement stops all flowsheet calculations and proceeds directly to the output report. The solution flag for the entire flowsheet is set according to the user-defined value of ISOLVE. nn RETURN The RETURN statement signals the end of the calculation procedure of the Calculator and must appear as the last statement in the

This is a special OUTPUT statementsaa D


procedure section. Othe Calculator is set a

nly one RETURN statement is allowed. The solution flag for ccording to the user-defined value of ISOLVE. RETURN

always sets TRACE to OFF.

Sample Calculator Procedures xample 1: Determination of Flash Point

stimate the flash point from D86 distillation

P= 0.64 * (D86(10)+D86(ip))/2.0 - 100.0

ures) for each stream:

entry field to enable the

ck the Set Up Definition for Calculator Parameter P(1) box to enable

meter… hypertext to open the Parameter window where fy whether the parameter will be a constant, a stream

have been placed on the flowsheet. For this sample problem, select the Stream option and choose V1 from

hoosing a stream name enables the Parameter… hypertext.

.

Volume Percent Distillate drop-down list box.

E

se Nelson’s method to eUcharacterization data. This sample shows how to calculate the flash points ofstreams V1, V2, V3, V4, V5, and V6 using the formula:

where the D86 points are in °F. The final results in °C are stored in R(1) through R(6). Before entering the procedure FORTRAN code, it is necessary to specify the streams (V1 through V6) and establish the two pertinent parameters (the D86 10% and IBP temperat

Open the Calculator main data entry window by double-clicking the

Calculator icon on the PFD. Click Edit/View Declarations to display the View Area box. Click

Parameters to display the Parameters data entry table. Enter a number in the Parameter Number data

Calculator Parameter linked text. Click on the linked text to open the Definitions window.

Chethe “Calculator Parameter = Parameter” linked text.

Click the Parayou can speciparameter or a unit parameter. The Constant/Stream/Unit list box displays a list with the options “Constant,” “Stream” and the various types of unit operations that

the Stream Name: drop-down list box. C

Click the linked text to open the Parameter Selection data entry window For this sample, choose Distillation Curve from the options in the

Parameter window. The center window will now display the available distillation curve options. Select D86 from the distillation curve options and choose the desired cut point (here, 10%) from the


This completes the parameter specification for the D86(10%) point of the first stream, V1. Repeat these steps to define the D86(Initial Point) for the first

t) for the remaining

,

Commit the code by clicking OK.

stream, V1, then define the D86(10%) and D86(Initial Poinfive streams.

Enter the following code into the Procedure window (at this point, this window should still be outlined in red).

DIMENSION D8610(6), D86IP(6) DO10 I =1, 6 $ $ COPY PARAMETERS TO LOCAL ARRAYS$ CONVERTING TO DEG F D8610(I) = P(2*I-1) * 1.8 + 32. D86IP(I) = P(2*I-1) * 1.8 + 32. $ $ EVALUATE FORMULA D86AVG = (D8610(I) + D86IP(I)) / 2. FP = (D86AVG * .64 - 100. $ $ CONVERT BACK TO DEG C AND STORE R(I) = (FP - 32.) / 1.8 10 CONTINUE RETURN


Example 2: Material Balancing with the Calculator

ned ariables table on page 152 for a listing of solution flags and for an explanation

of the use of the e in SEQUENCE

cedu

Establish the Strea e for the recycle loop. label for

The streams pertinent to this example are a hydrogen feed stream (H2FD), two ), a and va liquid

reams (PRDV, PR

To set up the stream sequence that will be used by the Calcula y out the

pen the Calculato a entry window by doubl

culator icon. que ows, one c of

Available Streams a list of Selected Streams. ams H2 d given

r. If you add th can ea ange nce by removin ed stream from the reams w or

appropriate stream highlighted in the Selected Streams

e Result:

When you have established the desired stream seque Results display the Resu and Print Name data ent

Enter “1” in the Result Number field of the first row to e e Print e entry field. T r is stored in the first posi

call the result “Relative Enter the following code into the Procedure window, w uld still be

outlined in red at this point:

This sample demonstrates the use of the Calculator to compute the material balance of hydrogen (component 2) about a recycle loop. We will set the solution flag to indicate “unit not solved” if the hydrogen balance is not met to within 0.01% based on the overall feeds. This specification forces the recycle to continue iterating, even if the flowing streams have changed less than the flowsheet stream tolerance. See the ISOLVE and ISn entries in the PredefiV

Isn variabl statements.

Before entering the pro

re code, we must:

m Sequenc Provide a the Result.

Establishing the Stream Sequence:

feed streams (FD1, FD2 purge gas stream (PURG), por andproduct st

DL).

tor, carrfollowing steps:

OCal

r main dat e-clicking the

Click Stream Se nce to display two windand the other

ontaining a list

Add the streorde

FD, FD1, FD2, PURG, PRDV ane streams in the wrong order, you

PRDL in the sily ch

their sequeSelected St

g the improperly positionindow and reinserting it before

that you haveafter the

window.

Labeling th

nce, click to lt Number ry table.

nable thNamarray. For this sample problem,

his intege tion of the R() MB.” hich sho


$ SUM UP H2 IN FEED STREAMS $ HYDROGEN IS THE SECOND COMPONENT IN THE COMPONENT

2, n) IS THE MOLAR TE IN THE nth STREAM $

0.0 = H2FD, FD2

H2FEED = H2FEED + SCMR(2,IS1) NUE

$ CHECK IF ANY H2 IN FEED. IF NOT, SET “NOT SOLVED” FLAG

HEN 0 E = 2

GO TO 99 ENDIF

H2 IN PRODUCTS $ H2PROD= 0.0

G, PRDL OD + SCMR

20 CONTINUE ATE IMBALANCE

R(1) = (H2FEED - H2PROD) /

$ CHECK IF IN BALANCE. IF SO, RETURN. D

IF(ABS(R(1)).LE.0.001) THENOLVE =1

LIST $ SCMR( FLOWRA

H2FEED =DO 10 IS1

10 CONTI$

. $ IF (H2FEED .LT. 0.0001) TR(1) =ISOLV

$ $ SUM UP

DO 20 IS1 = PURH2PROD = H2PR (2, IS1)

$ CALCUL$

H2FEED $

$ IF NOT, SET “NOT SOLVE$

” FLAG.

ISELSE ISOLVE =2 ENDIF $ 99 RETURN


This page intentionally is left blank.


CAPE-OPEN

General Information The PRO/II CAPE-OPEN unit operation enables the users to add third party CAPE-OPEN units. This will help the user to simulate and perform any type of calculation for a specific unit operation placed in a flowsheet. CO-LaN (the CAPE-OPEN Laboratories Network) is a neutral industry and an academic association promoting open standards in process simulation software.CAPE-OPEN has uniform standards for interfacing process modeling software components developed specifically for the design and operation of chemical

rocesses. These standards

allow integration of different software components

N Unit Operation has access to the following:

age.

ed between PRO/II and CAPE-OPEN unit operation are

ram provided by the vendor. The install program should perform all actientries in the Windows Registry. After installation, you can launch PRO/II and

mediately use the new CAPE-OPEN software components.

plike unit operations and thermodynamic property packages from different vendorsinto a single simulation. PRO/II supports both versions of 0.9.3 and 1.0 of the CAPE-OPEN interfaces.

he CAPE-OPET

• Flash and Physical property calculations provided by PRO/II • Third party CAPE-OPEN property pack

roperty values exchangP

in SI units. CAPE-OPEN interface descriptions and information are available at ttp://www.colan.org/ h

Note: If transport properties are required in the CAPE-OPEN unit operation, you must select a suitable method in the Thermodynamic Data if PRO/II

ermodynamics is selected. th nstalling CAPE-OPEN Unit Operations I

To install a new CAPE-OPEN unit operation or property package, execute the install prog

ons necessary to copy the files to your computer and set up the required

im


If the CAPE-OPEN unit operation does not have an installation program, follow the steps mentioned below to manually register the unit operation. 1. Identify the DLL file of the CAPE-OPEN unit operation. 2. Type "regsvr32 myunitop.dll", where "myunitop.dll" is the name of the DLL of

the CAPE-OPEN Unit Operation. . Identify the "progid" of the CAPE-OPEN unit operation. The "progid" is a short

y the DLL.

peRegister.exe progid". "CapeRegister.exe" is a utility available in the PRO/II "bin" directory.

st program ID of the required unit.

ts nit Operation may have multiple feed streams and use the data for various flash

mber

ergy and information type ports a

DisTo the icon on the PFD. If the nit I for the unit operation is

If the unit operation does not support a custom GUI, PRO/II displays all arameters in the default data entry window. All values are displayed in SI units.

aving the state of CAPE-OPEN Unit Operations

RO/II supports COM Persistence mechanisms through IStream, IStreamInit, torage and IPropertyBag interfaces. PRO/II creates a file named przname-

id.dat for storing state.

CAPE-OPEN Unit does not support COM persistence, PRO/II saves the state of the CAPE-OPEN unit operation by querying all input and output parameters and storing their values in the underlying PRO/II database.

3text string, such as "SimSci.Mixer" that Windows uses to identifContact the developer of the unit operation to determine the "progid".

4. From the command prompt, type "Ca

Selecting the CAPE-OPEN Unit Operation Install the CAPE-OPEN unit operation, as described above, and launch PRO/II to use the new CAPE-OPEN software components. When the new CAPE-OPEN unit operation is laid down on the PFD, a dialog will be displayed with a drop-down list box filled with registered CAPE-OPEN unit operations. The user muselect the

Feeds and ProducUand property calculations. PRO/II queries the unit operation for a required number of unit ports. The icon is automatically supplied with the required nuof ports with one stream allowed for each port. Note: Material type ports are handled while the en

re not supported.

play Unit Operation on PFD place a CAPE-OPEN unit operation, double-click operation supports a custom GUI, the built-in GUu

displayed.

p S PISu If


Calculation During calculations, PRO/II calls the Validate() and Calculate() method of the CAPE-OPEN unit operation. Property and flash calculations are delegated to property package if property package is selected as unit thermodynamics. If PRO/II thermodynamics is selected for a CAPE-OPEN unit operation, it may call

TP, TH, PH, TV, and PV flashes (CalcEquilibrium) for input or output streams. The following properties can be calculated using PRO/II thermodynamics.

CAPE-OPEN identifier Property meaning Phases Supported

vaporPr Vapor Pressure only for Pure Liquid essure calc type

surface ace Tension Liquid Tension Surf

Compressibility Factor Compressibility Factor Z= PV/RT

Liquid, Vapor, Overall

heatCapacity Heat Capacity Liquid, Vapor, Overall

idealGasHeatCapacity Heat Capacity of ideal gas Vapor

viscosity Viscosity Liquid, VapoOverall

r,

ThermaOverall

l Conductivity Thermal Conductivity Liquid, Vapor,

fugacity Fugacity Liquid, Vapor

logFugacityCoefficient Logarithm of Fugacity Coefficients

Liquid, Vapor

kvalues K factors of a pair of phases in Equilibrium

Overall

dewPointPressure Dew point Pressure at a given temperature

Overall

dewPointTemperature Dew point Temperature at a given Pressure

Overall

temperature Temperature Liquid, Vapor, Overall

pressure Pressure Liquid, Vapor, Overall

volume Volume Liquid, Vapor, Overall


CAPE-OPEN identifier Property meaning Phases Supported

density Density Liquid, Vapor, Overall

enthalpy Enthalpy Liquid, Vapor, Overall

entropy Entropy Liquid, Vapor, Overall

gibbsFreeEnergy Gibbs Free Energy Liquid, Vapor, Overall

flow List of partial Molar(or mass) Liquid, Vapoflows for each component within

phase

r, Overall

a given

fraction List of partial Molar(or mass) Liquid, Vapor, fractions for each component within a given phase

Overall

phaseFraction The fraction of the fluid that is in specified phase

Liquid, Vapor

totalFlow Mass flow of a phase or whole mixture

Liquid, Vapor, Overall

molecularWeight MolecularWeight Liquid, Vapor, Overall

boilingPointTemperature Only supported for “Pure” calc type

eport supported by CAPE-OPEN unit operation, select and

n. This action will display a menu with “Produce

eters

R GenerationIf the custom reports isght-click the unit operatiori

Report” as one of the options. Select Produce Report to open a text file. If the custom reports are not supported, the menu will have “View Results” as one of the options. Select View Results to display all input and output parameters with their values.

ote: The standard report of PRO/II will have all input and output paramNwith their values for CAPE-OPEN units.


Column, Batch

General Information

mes, or in a semi-batch mode where feedstock on and products drawn from the column or

, or as drawn from the column uring distillation) is also made because of the cyclic operation. A representation

am comes from the amount of product divided y the batch cycle time.

e

on all s and heat duty specification for trays apart from Batch distillation.

it

The Batch Column unit operation models a wide range of column operating scenarios. The Batch Column unit may be run in a true batch simulation mode,

ith the feedstock charged to the stillpot prior to distillation and products taken wfrom the accumulator at various timay be introduced during distillatiaccumulator over some time interval. Batch distillation calculations may also be integrated into a steady-state process simulation. The unit configuration automatically considers the presence of implicit holding tanks for continuous flow streams which provide the time-variant feedstock to the batch unit. Implicit consideration of holding tanks for all product streams (as drawn from the accumulator at different timesdof the product continuous flow streb Thermodynamic System The thermodynamic system for the Batch Column may be specified for the unitas a whole or for selected trays. Batch Column also allows the use of electrolytthermodynamic methods. BATCHFRAC®

This is a batch distillation model obtained from Koch-Glitsch, LP. BATCHFRAC® has been integrated with PRO/II to handle reaction on trays for VLE, VLLE the stage Detailed Information For detailed information about the use of BATCHFRAC® and Batch Column unoperations, consult the PRO/II Add-On Modules User Guide.


Column, Distillation

eneral Information G The Column unit operation may be used to simulate any distillation or liquid-liquid

xtraction process. Liquid-liquid extraction units are described in the Liquid-t

he ber

n present, is always numbered as tray one and the reboiler, when present, is assigned the highest tray number in the model. Any tray may

, or duty. The top and bottom trays must have either a

it on e feed flash convention to use for all

the vapor is placed on the feed tray when it is the bottom tray

d in olumn may

eLiquid Extraction Column section of this chapter. A column must contain at leasone equilibrium stage or theoretical tray. For purposes of this discussion, the term “trays” is used to denote “equilibrium stages”. The trays are considered to be linked with the vapor from each tray entering the next higher tray and tliquid from each tray feeding the next lower tray. There is no limit on the numof trays in a column model. The condenser, whe

have a feed, product drawfeed or a duty. Distillation columns may simulate vapor/liquid, vapor/liquid/water or vapor/liquid/liquid equilibrium processes. Feeds and Products Column feeds and products are added during the flowsheet construction in thePFD main window. Click Column Feeds and products… on the Column main data entry window to open the Column Feeds and Products window. Feed tray numbers may be added or changed in this window. There is no limhe number of feeds a column may have. Tht

feeds to the distillation column is selected with radio buttons as: Vapor and liquid to be on the feed tray: The default. Flash the feed adiabatically, vapor onto the tray above and liquid onto thefeed tray.

For this option, of the column.

For products, the product type, phase, tray number, and flow rate are suppliethis window. There is no limit on the number of products a distillation c


have and products may be withdrawn from any tray of the column. Product typeinclude: Overhead, Bottoms, Fixed Rate Draw, Total Phase Dra

s w, and Pseudo-

roduct. Every column must have an overhead product leaving tray one and a IO)

ms may have a decanted water product from tray one he condenser).

The Suvapor/li y be draw You mu , or liquid vo . You must also provide an estimated value for either the

verhead or bottoms product. For total draw products, the supplied rate is always

se a Performproduct. Pseud

streamsproductclicking followin

pass flow Thermosiphon reboiler feeds and products

Thermo

pbottoms product leaving the highest numbered tray. The Sure, Inside-Out (and Enhanced IO algorith(t

re algorithm may also have water draws from any tray. For quid/liquid equilibrium (VLLE) processes, either of the liquid phases man from any tray in the column.

st supply product rates for all fixed rate draw products in molar, masslume units

oassumed to be an estimate. The estimated value for the overhead or bottoms rate should be as accurate as possible to enhance convergence. You must u

ance Specification to set a desired flow for the overhead or bottoms

o-products Pseudo-products are used to create streams corresponding to column internal

, making them available for flowsheet calculations. Define pseudo-s in the Column Pseudo-products window which you may reach by Pseudo-products on the Column Feeds and Products window. The g types of pseudo-products are available:

Net tray liquid or vapor flow Total tray liquid or vapor flow Pumparound liquid or vapor by

siphon reboiler streams are limited to the Inside-Out algorithm.


Column Algorithm elect the solution algorithm from the drop-down list box, on the Column main ata entry window. The available algorithms are: Inside-Out (the default), Sure, hemdist, Liquid-Liquid, Enhanced IO, and Electrolytic. Detailed information bout the column algorithms is available in the online help.

Inside-Out algorithm is the preferred option for most distillation

r columns where free water exists on multiple trays.

iquid-Liquid: The Liquid-Liquid algorithm is used to model liquid-liquid

Enh c orithm extends the capabilities of the IO allows zero flow rates, water s and pumparounds.

ous electrolytic distillation columns involving ionic species. Refer to the

del used

in RATEFRAC is a “rate-based” model. That algorithm uses

ATEFRAC® is a registered trademark of Koch-Glitsch, LP.

SdCa Inside-Out: The

problems, especially those involving systems of hydrocarbons, because of its speed and insensitivity to the estimated solution profiles.

Sure: The Sure algorithm should be used fo

Chemdist: The Chemdist algorithm is well suited to highly non-ideal systems and VLLE processes.

Lextraction units described in the Liquid-Liquid Extraction Column section of this chapter.

an ed IO: The Enhanced IO column alg Enhanceddefault Inside-Out algorithm.

decant off any tray, total draws from tray

Electrolytic: The Electrolytic method is used to model non-ideal aque

PRO/II Add-On Modules User Guide for detailed information on this column algorithm.

RATEFRAC® Software: Rate-based distillation (RATEFRAC®) routines rigorously calculate the actual mass transfer on the stage, avoiding theneed for component efficiencies. The non-equilibrium stage mo

®

fundamental heat and mass transfer calculations to model a distillation stage.

R


Reactions Reactions in the column can be modeled by the Chemdist or Liquid-Liquid

rithms found in the Algorithm drop-down list of ent data in the Column – Reaction Selection

extraction and RATEFRAC® algothe Column window. Enter pertinwindow accessible via the Reactions… button on the Column window. In the Column - Reaction Selection window, you can select and modify column reactions, specify stage-wise reacting volumes, designate non-condensacomponents, select non-volatile catalysts and specify data for user-added subroutines or kinetic procedures. The reactions specified here are limited in scope to the simu

ble

lation of reactive distillation and (reactive) liquid-liquid xtraction.

s in ata

from Reaction Data, and a local set-name and description reover, the individual reactions can be modified in the

the s

.

can specify volume available for reaction (effective volume) per stage reactions in the Column –Tray Effective Reaction m the Reaction Selection window. A tabulation of

er can specify segment volume percents of both liquid nd p is used in non-equilibrium calculations of Ratefrac. Data

sup l be copied to all other trays and data supplied to ul e ated to any missing trays during calculations.

e Column - Reaction Selection To modify reaction sets defined in Reaction Data, select the Include ReactionColumn Calculations check-box. All the reactions defined via Input/Reaction Dare now available to the column. Reactions can be selected from a drop-down list under Reaction Set can be assigned. MoReaction Definitions window by clicking Modify Data. The selected reaction sets can also be assigned to individual trays (or ranges of trays) by selecting reaction sets from a drop-down list under Column Reaction Set and then entering a tray range, i.e., starting tray to ending tray.

Note: Although you can modify a local copy of a reaction set in the column, original reaction set specified in the ‘Reaction Data’ section remainunchanged

Reacting Volumes The user for both liquid and vapor phaseVolumes window accessible frotray numbers and the respective volumes is provided for data entry. This specification is used in calculating the rate of kinetic reaction.

Ratefrac column, usFor a va or. This data

plied on only one tray wiltipl trays will be interpolm


Nonvolatile Catalyst Components that catalyze a reaction without volatilizing can be selected and the uantity of their charge specified as an amount or a fraction in the Column - Non-

tion

on-condensing components can be specified in the Column - Non-Condensing n Selection window.

r n

utine/Procedure Data button. See the Reaction he

ll data pertaining to a reaction (in a specified reaction set) can be modified ow

ccessible via Modify Data… in the Column-Reaction Selection window. The

subrout action type can data that

ichiometry) can be

Instructi ntering data for the three types of reactions (Kinetic, Equilibrium

Calcul

rithms also support the apor/liquid/liquid system. In addition, the Sure and Enhanced IO algorithms

qVolatile Catalyst for Boiling Pot window accessible from the Column - ReacSelection window. Non-condensable NComponents window accessible from the Column –Reactio Subroutine/Procedure Data Data used for user-added subroutines and kinetic procedures can be specified in the form of Integer, Real and Supplemental Data entries in the Column - UseSubroutine and Procedure Data window accessible from the Column - Reactio

election window via the SubroSData and Procedure Data sections, in this chapter, for detailed information on tdata requirements for these utility modules. Modify Data (Reaction Data) Aexcept for reaction stoichiometry - in the Column-Reaction Definitions windacalculation method for a reaction can be modified to follow a user-added

ine, procedure or kinetic power-law expression. The realso be changed to Kinetic, Equilibrium or Conversion. All reactioncompletely specify any of the above reaction types (except stochanged in the data entry fields accessible via the Enter Data… button under the Additional Data column for the respective reaction.

ons for eand Conversion) are covered in detail, in the Reaction Data section of this chapter.

ated Phases

Select the appropriate phase system in the drop-down list box on the Column main data entry window. All distillation algorithms support the default phase system of vapor/liquid. The Sure and Chemdist algov


support the phase system vapor/liquid/water that allows a free water phase on ny tray of a column.

nter the number of trays in the model, in the data entry field provided on the

upply the number of iterations in the data entry field provided on the Column er of

f erations is performed and the column equations are not satisfied within the

Sure algalgorith

The preare perfColumn ure Profile…supplied window

across t per tray andapplicat Individuand bot

ressures. Missing pressures are determined by linear interpolation of supplied th

Cond

a Number of Trays EColumn main data entry window. Every Column must have at least two trays. There is no limit on the number of trays in a Column. Number of Iterations Smain data entry window. The number of iterations corresponds to the numbouter loop trials for the Inside-Out algorithm and the number of trial solutions for the other algorithms. A non-convergence is flagged when this number oittolerances. The default values are 15 for the Inside-Out algorithm, 10 for the

orithm, 20 for the Chemdist algorithm, and 30 for the RATEFRAC® m.

Pressure Profile ssure for every tray in a column model must be defined. All calculations ormed at the defined tray pressures. Define the tray pressures in the Pressure Profile window which you may reach by clicking Press on the Column main data entry window. Tray pressures may be on an overall or tray-by-tray mode by choosing a radio button in this

. For the overall mode, supply the top tray pressure (tray two for columns with condensers) and either the pressure drop per tray or the total pressure drop

he column. A default value of zero is supplied for the pressure drop the column pressure drop. All tray pressures are derived by linear ion of the supplied pressure drop.

al tray pressures are supplied for the tray by tray mode. Note that the top tom trays must be included when supplying a table of individual tray

pvalues. This method is useful for defining the pressure profile for columns wiirregular pressure profiles such as refinery vacuum units.

ensers The condenser is always a heat sink on tray one. It is defined in the Column Condenser window, which you may access by clicking Condenser… on the Column main data entry window. The top products from columns with


condensers correspond to the products from the reflux accumulator drum. Thpressure for all types of condensers is supplied in this window. The condenser type is selec

e

ted with the appropriate radio button from the llowing options:

t

l

supplied.

tray two is cooled to a bubble point liquid a is returned as reflux to tray two, the other

d” product from the column. An ndenser temperature may be supplied in the . The condenser pressure and duty may also

Subcoo d e: The vapor from tray is cooled below its bubble

temperature provided in this n rtains that the product is subcooled, and if,

“Overhead” product from the column. The condenser pressure and lied.

e f sub cooling

below the product bubble point is defined, always resulting in a r

ed. If the duty is designated

This option is enabled only by selecting Partial or denser Type. Select the appropriate

Temperature specification namely, Fixed Temperature or Temperature

fo Partial: This condenser is an equilibrium stage and may or may not have a ne

liquid product as well as vapor product. The net liquid product, if present, is defined as a “Fixed rate liquid draw” from tray one. The condenser temperature is the dew point of the equilibrium vapor. An optionaestimate for the condenser temperature may be supplied in the ColumnCondenser window. The condenser pressure and duty may also be

Bubble Temperature: The vapor from

ph se. While one portionportion is withdrawn as the “Overheaoptional estimate for the coColumn Condenser windowbe supplied.

le , Fixed Temperaturpoint as defined by a subcooled wi dow. PRO/II ascenot, signals a non-convergence condition with an appropriate diagnostic message. The subcooled liquid product is designated the

duty may also be supp Subcooled, Fixed Temperature Drop: This condenser is the same as th

subcooled type described above except that the degrees o

subcooled “Overhead” product. The duty and pressure for the condensemay also be supplied in this window, if desiras a parameter to vary, any supplied duty for any of these condenser options is used as an estimate.

Sub-cooled Reflux Only:

Bubble Temperature under Con

Drop that needs to be followed in the Subcooled reflux for the chosen condenser type.


Reboilers Column reboilers are described in the Column Reboiler window which is envia the Reboiler button on the Column ma

tered in data entry window. The reboiler type

selected with a radio button on this form.

rithms, only default type is made available to the user.

es and should be modeled as such.

ermosiphon reboilers by choosing the ppropriate radio button and entering a value in the field provided. Choices

in

• • •

An estimm be e suppa

is The default type is the Kettle (Conventional) reboiler, which corresponds to a duty on the bottom tray of the column with the equilibrium liquid withdrawn as the “Bottoms” product. For both Inside-Out and Enhanced IO algorithms, following reboiler types are vailable to the user. a

• Thermosiphon without Baffles, and • Thermosiphon with Baffles.

or other algoF

The thermosiphon without baffles type corresponds to the case when the Columnbottom product and reboiler feed are withdrawn from a common sump. Note: Thermosiphon reboilers with baffles in which the reboiler return flows into the reboiler sump and overflows to the product sump are equivalent to the “no baffles” type for simulation purpos One specification may be selected for tha

clude:

Reboiler return liquid fraction Return temperature Temperature change across the reboiler

• Reboiler circulation rate.

ate for the return fluid liquid fraction or circulation rate, as is applicable, given to enhance convergence. The duty for the reboiler may also bay

plied in this data entry window, if desired. If the duty is designated as a rameter to vary, any supplied duty is used as an estimate.


HeateSide he ia the Column Side Heaters/Coolers

indow accessible via the Heaters and Coolers… button on the Column main dpumpara positiv e heaters/coolers. RATEF(Liquid/V

d heoretical stage. Liquid from the tray above the flash zone or

abnamed . Specification options include red heater efficiency, vapor and liquid by-pass fractions and transfer line

te Not ®

Column Heat Leaks olumn heat leaks may be modeled by clicking Heat Leak on the Column Side

H k may be

• Overall, or, • By Individual Trays

rs and Coolers aters and coolers may be supplied v

wata entry window. Side heaters and coolers that are associated with a

ound are not entered with this window. A negative duty indicates cooling; e duty is used for heating. There are no limits on the number of sid

RAC® routines support heating and cooling for both phases apor).

For each side heater/cooler, the following information must be provided: tray number, a reference name, and the duty, with the appropriate algebraic sign.

Flash Zones The Flash Zone calculation models a fired heater added to a tray in an Inside-Out column. Flash zones are associated with column heaters when a feed stream entering the column is heated in a separate furnace. The furnace is considereas an additional tv por from the tray below the flash zone could enter the flash zone or they can ypass it. Data entry fields for flash zones can be accessed through the like-

button on the Heater data entry windowfi

mperature drop.

e: If you are working with RATEFRAC , this option is disabled.

Ceaters/Coolers window to open the Column Heat Leak window. The heat lea

designated as:


For the Overall option, the heat leak duty for all of the trays except the reboiler nd condenser is given on a per tray basis or total column basis. A heat leak may lso be provided for the condenser and the reboiler, if desired.

or the By Individual Trays option, heat leak duties for ranges of trays are supplied as tabular input. At least two values must be supplied. Heat leaks for trays not given, but which lie between trays with defined heat leaks, are determined by linear interpolation. Note: If you are working with RATEFRAC® routines, this option is disabled.

Pumparounds and Vapor Bypasses Column pumparounds and vapor bypasses may be defined for the Inside-Out and Sure algorithms in the Column Pumparounds window, which is accessed via the Pumparounds… button on the Column main data entry window. A pumparound may be either a liquid or vapor, with vapor pumparounds more commonly termed “bypasses”. Pumparounds are added and edited in a tabular form by clicking on hypertext strings. Entries for each pumparound include: phase, pumparound name, draw tray, return tray, return pressure, and two specifications. Supply these specifications in the Column Pumparound Specifications window which is entered by clicking the two specifications hypertext string. The following specification combinations are selectable via radio buttons: Rate and Duty: The rate and duty data entry fields are enabled for input. A

reference name may also be supplied for the heater.

Rate without Heater: The rate field only is enabled for input.

Rate and Return Condition: The rate and return condition fields are enabled for input. The return condition may be the temperature or the temperature drop or the liquid fraction. A reference name may also be supplied for the heater.

Duty and Return Condition: The duty and return condition fields are enabled for input. The return condition may be the temperature or the temperature drop or the liquid fraction. A reference name may also be supplied for the heater.

For the Sure algorithm only, the pumparound rate may be designated as the total fluid leaving the tray. Total liquid pumparounds must pump down the column and total vapor pumparounds (bypasses) must flow up.

aa F


algorithms use an iterative solution technique, starting from an initial stimate of the tray temperature, flow and composition profiles. The initial

replace values produced by an estimate generator.

rovided are:

are

te for e

s designed for complex refinery columns which have ad of reboilers such as crude and vacuum columns, nators, etc. These columns may also have side

by the

odel. Adjustments in the profiles

Che ic chemical

g and uses successive series of adiabatic flashes up and down the column to establish the tray compositions.

provide temperature ottom tray of column, and

Initial Estimates All column eestimate may be produced internally using an initial estimate generator and/or provided by the user as initial profile data. User-supplied profiles may also be used to selectively Click Initial Estimates on the Column main data entry window to enter the Column Initial Estimates window. To use an initial estimate generator, select thegenerator method from the drop-down list box. Methods p Simple: Profiles are determined by a simple material balance. Temperatures

determined from estimated product compositions. This model is quick and adequate for simple column configurations.

Conventional: A general method designed to produce an adequate estima

most distillation problems. Shortcut calculations are used to estimate thproduct flows and compositions. The compositions are used to estimatetemperatures. Internal flows are estimated by using the product flows and a reflux estimate. This method works best for conventional fractionators with condensers and reboilers in which classic Fenske techniques provide reasonable results. Special techniques are also included for absorbers and strippers.

efinery: This method iR

bottom steam insteF.C.C. main fractiocolumns, pumparound cooling circuits, and decanted water at the overhead accumulator. A multi-product shortcut technique developedSIMSCI is used for these columns. The user-supplied estimates for product rates are used in the shortcut mare made for side coolers.

m al: This generator should be restricted to highly non-ideal distillation problems. The method is time-consumin

When using an estimate generator, you may optionallyestimates for the following trays: condenser, top tray, b


reboiler. You may also provide an estimate for the reflux rate or reflux ratio. is provided by the user, PRO/II supplies a reflux ratio of olumns). Any supplied data replaces values predicted

y the estimate generator.

itial profiles are entered in tables accessed by clicking the following buttons on

res…

n-ideal mixtures; however,

s By defahave an Check I timate to include design specifications to be onsidered during Initial Estimate.

Toleran Liq / low Transformation: Select the appropriate Liquid/Vapor Flow Tra o the drop list.

• Standard

• Logarithmic

When no reflux estimate 3.0 (which solves many cb When an initial estimate generator is not used, the minimum data which must besupplied as input profiles are tray temperatures and flows, vapor, liquid, or a combination thereof. Note that the minimum data which may be supplied are the temperatures and flows for the top and bottom trays for the column. While theseare the minimum data required, they are rarely adequate to produce an acceptable initial estimate. It may also be desirable to provide solution profiles from a converged solution to speed future calculations with a column model. Inthe Column Initial Estimates window:

• Net Vapor Rates…

• Vapor Composition…

• Liquid Composition…

• Tray Temperatu

• Net Liquid Rate…

• Mass Transfer… Composition estimates may be helpful for highly nothey are rarely needed for most problems. RATEFRAC® Initial Estimate:

ForE

RATEFRAC® routines, Initial Estimate may be used to perform Initial timate. Option is also provided to include design specifications.

ult, the Perform Initial Estimate option is checked to provide the user to estimate on Temperature and Reflux, etc.

nclude Design Specs in Esc

ce: Enter the Tolerance value.

uid Vapor Fnsf rmation from

• Square


PPerformstedfeed stream rate, heat duty, or the draw rate for a “fixed rate draw.” Furthermore, foS

ply SPEC’s and define VARY’s for a column, click Performance cess the Column

in are entered or edited

SPE ’s y

the SPEC/VARY/DEFINE section of this chapter. A list of the stream and en in

C olerances, Homoto ifications and Convergence History (pri u r Column iterations. These data are entered in the Column Con r ata window accessible via the Convergence Data… button on the Column try window.

Factor: Using a damping factor of less than unity often improves convergence when the convergence is oscillating. Refinery complex fractionators should be given damping factors of 0.8. Chemdist columns may require more severe damping. A default value of 1.0 is supplied by PRO/II. Damping cannot be applied to the Sure algorithm.

Damping Cutoff: The Chemdist algorithm uses the damping factor cutoff

value. The damping factor is only applied when the sum of the errors is larger than this value. A default value of 10-8 is supplied by PRO/II.

in the sum of the errors

from iteration to iteration. PRO/II supplies a default value of 1.0 for the

erformance Specifications ance specifications or SPEC's may be imposed on a column operation

duct stream flows or properties, column internal flows, column tray uch that promperatures, etc., are at desired values in the solution. For each SPEC, a egree of freedom or VARY must be calculated. For a column, a VARY may be a

r convergence to be achieved, there must be a direct effect on all of the PEC's by the collective set of VARY's.

To supSpecifications on the main Column data entry window to acSpecifications and Variables w dow. SPEC’s and VARY’sby clicking on the hypertext strings. PRO/II requires that there be an equal number of SPEC’s and VARY’s. Thus, whenever you add or delete a SPEC, you are required to add or delete a VARY.

C and VARY’s use the general form in PRO/II and are discussed more fullincolumn parameters which may be used for SPEC’s and VARY’s also is givthat section. Convergence Data

onvergence data include Convergence Parameters, Convergence Tpy Options for Convergence Spec

nto t options) fove gence D

main data en Convergence tuning parameters

Damping

Error Increase Factor: This factor limits the increase


Inside-Out algorithm or 100 for the Chemdist algorithm. Thisnot apply to the Sure algorithm.

factor does

ns is used for the Sure algorithm. A factor of 1.0 gives equal the current and last set of compositions; a factor of 2.0 gives

In rare circumstances, specifying a key component can he convergence for the Sure algorithm. The key component is

Sure ou can

string.

Not T red to s e

onvergence Tolerances

h this should n.

Tole n

B b f ®

En ha

t

TEFRAC®.

Component Balance: The maximum relative component balance error for each tray. Not used for the Inside-Out algorithm. The default is 10-3.

Component Averaging Factor: This weighting factor for update of

compositioweight todouble weight to the last set of compositions, and so forth. A default value of 0.0 is supplied by PRO/II.

Key Component:

enhance tnormally determined by PRO/II but may be specified by the user.

St p o if no improvement after 5 iterations: The number of consecutive

algorithm iterations allowed without improvement in the solution. Ychange the number of iterations by clicking on the hypertextChanging this parameter rarely, if ever, results in convergence.

he use of tuning factors ue: sually results in an increase in the time requiolv a distillation problem.

C Tolerances for the column equations may also be changed althougrare , ifly ever, be done and never as a means to reach a converged solutio

ra ces are:

ub le Point: The maximum bubble point error for each tray. The default o-310 is not used by the RATEFRAC .

lpy Balance: Thet maximum heat balance error for each tray. The default is 10-3.

Equilibrium K-value: The maximum allowable relative change in a componenK-value generated in the outer loop of the Inside-Out algorithm versus the last value used in the inner loop. The default of 10-3 is not used by RA


RATEFRAC® is a registered trademark of Koch-Glitsch, LP.


Homotopy Options for Convergence on Specification ation

ay be used for any column lgorithm.

es

he homotopy option allows you to solve the simulation with an initial value for set

initial alue of the specification and the number of intervals to use in moving from the

.

is varied by a er the field entitled

erations will be carried ut to meet the given column specification. If the specification value is then

changed by another unit operation, the column will solve without homotopy selected, the homotopy iterations will be carried out every

erged after the specification has been changed. In this ase, the initial value will be the last converged specification value, not the

column iterations is useful in the diagnosis of a convergence failure. History printout for the iterations may be requested by selecting the

Print Column Profiles in Keyword Input File Form Format RATEFRAC® routines Initial Estimate Print Level


The homotopy option is an aid to converging simulations where the specificis difficult to meet by virtue of the value of the specification (as opposed to the type of specification). The homotopy option was designed for Reactive Distillation where convergence is more complex, but it ma One example of the use of homotopy is to systematically increase tray volumto very large values, to determine the equilibrium compositions for reversible kinetic reactions. Tthe specification and then automatically move to the desired final value in anumber of steps. The column is converged at each step. To use the homotopy option for any specification, you must supply thevinitial value to the final value. You cannot change the final value in this window The homotopy option may be used for a specification whichController or Flowsheet Optimizer. If Initially is selected undApply During Control Loop (the default), the homotopy ito

iterations. If Always istime the column is re-convcsupplied value. Convergence History Printout of the

printout level desired for the following options.

• Convergence History Print Level • •

R


Tray Hydraulics Tray hydraulic calculations may be used to size new columns and to rate existing tray or packed columns. To perform sizing or rating calculations, click Tray and Packing Data… on the Column main data entry window. For sizing and rating purposes, the column is divided into sections of trays or packing on the Column Tray Hydraulics window. Enter tray/packing sizing and rating information in the

olumn Tray/Packing Rating or Column Tray/Packing Sizing windows accessible e

packings are available, as are various types of metallic and ceramic rings and saddles. For sizing calculations, column diameter for each tray is sized independently to

eet the specified or default flooding criteria. The largest diameter in each section is then selected and the entire section is re-rated using the largest

quired standard diameter.

or rating calculations, the percent of flood is calculated for each tray. The ature of multiple sections of trays is useful in representing existing columns,

which often have a variety of tray and downcomer arrangements.

olumn RATEFRAC® Tray Options olumn RATEFRAC® routines tray options may be used to select the following

• Vapor and liquid mixing characteristics • Correlation used to calculate Mass, Heat Transfer and Interfacial Area.

Base Segment: Enter the Tray number on which the characteristics need to be set. Base Segment will be made available to the user only if you have selected the following in the Column – Tray Hydraulics dialog box:

• Internal – Tray • Calculation Type - Sizing

Liquid/Vapor Mixing: Select the appropriate Liquid/Vapor Mixing

characteristics from the drop list: • Complete • Linear • Logarithmic


Cvia the Enter Data… button. The Glitsch valve tray method is used to perform thtray calculations. The valve tray results are de-rated by five and twenty percent respectively, to represent the performance of sieve and bubble cap trays. For packed columns, random or structured

m

re

Ffe

CC


The options are explained below:

Complete – Select, if therecolumn. This corresponds

is a complete mixing of liquid or vapor phase in the to a flat concentration profile across a tray. It

n

ter the uired for calculation:

• Vapor and liquid mixing characteristics

ritical Surface Tension: Enter the Critical Surface Tension, if you have sele Internal in the Column - Tray Hydraulics dialog box

L i elect the appropriate Liquid/Vapor Mixing characteristics from the drop list:

ds to enter the above-mentioned data for both Sizing and Rating alculation.

is the default value and for most cases provides good results. Linear – This option indicates that there is a linear concentration profile across

the tray. Logarithmic – This option indicates that there is a logarithmic concentratio

across the tray.

Column RATEFRAC® Packing Options ATEFRAC® Packing Options may be used to select the following and enR

data req

• Correlation used to calculate Mass, Heat Transfer and Interfacial Area C

cted Random Packing under .

iqu d/Vapor Mixing: S

• Complete • Linear • Logarithmic

User neec



RATEFRAC® Transport Calculation Methods

n - Colburn Correlation from the drop-down ransfer.

Mass Transfer Check Correlation and select the appropriate correlation name from the drop-down list to calculate Mass Transfer:

• Scheffe & Weiland (Internals - Trays and Sizing calculation type) • Chan & Fair (Internals - Trays and Rating calculation type)

Packing and for both Sizing and

dom Packing and for both Sizing and Rating

d correlation to calculate Interfacial Area: rnals - Trays and Sizing calculation type)

ternals - Trays and Rating calculation type)

tion type) • Onda (Internals - Random Packing and for both Sizing and Rating

pe) als - Random Packing and for both Sizing and Rating

calculation type) If the user-defined correlation is available for any of the parameters mentioned bove, check Subroutine and select the user-defined correlation from the drop-


RATEFRAC® Transport Calculation Methods is used to select a suitable correlation for calculating Heat Transfer, Mass Transfer and Interfacial Area.

Heat Transfer Check Correlation and Select Chiltolist to calculate Heat T

• Rocha 1996 (Internals - Structured Rating calculation type)

• Onda (Internals - Rancalculation type)

Interfacial Area elect any of the listeS

• Scheffe & Weiland (Inte• Chan & Fair (In• Rocha 1996 (Internals - Structured Packing and for both Sizing and

Rating calcula

calculation ty• Bravo (Intern

adown list.

R


Tray Efficiencies All trays in a column model are treated as equilibrium stages or theoretical trays unless one of the tray efficiency models is used. This implies that the user mustapply some type of tray efficiency to the actual number of trays in the columndetermine the number of theoretical trays to use in the model. Engineers tyuse overall tray efficiency factors based on experience to convert actual trays theoretical tra

, to

pically to

ys. This is almost always the best manner in which to model tray

dist algorithm, only the Vaporization model may be used.

predicts the overall tray efficiency. All of the osition

y y efficiencies may be given for all components on a tray or

tray. An overall scaling factor may also be provided to ncies. This factor may be adjusted by a Controller unit

to meet a desired SPEC.

efficiency, since generalized correlations for overall tray efficiency are nonexistent in the literature. For the Inside-Out algorithm, PRO/II provides several tray efficiency models:

• Murphree • Equilibrium • Vaporization.

For the Chem However, none of these models models use an equation or factor to adjust the equilibrium vapor compleaving a tray. The models are useful for tuning a tray or a few trays in a Column model, but their general application to all trays in a column is not recommended. To use tray efficiencies, click Tray Efficiencies… on the Column main data entrywindow to enter the Column Tray Efficiency window. Select the efficiency modelwith a radio button and click Efficiency Data… to begin the tabular entry of traefficiencies. Traselected components on abe applied to all tray efficie


Side Columns A column using the Inside-Out or Sure algorithm may have attached Side Columns, where a Side Column is a stripper or rectifier. The Side Columfeed from the main Column and returns a product to the main Column. A finisheproduct is withdrawn from the Side Column.

n draws d

tion that irrelevant features are

eliminated.

umn with the main column, for RY’s

’s

Print Options: Click RateFrac… to bring up Print ptions dialog box. By default, Calculated HETP for each segment option is

checked. Check the other options to make the data available in the generated report.

Side Columns are attached as part of the flowsheet construction in the PFD main window. They may be completed and edited by double-clicking on the side column icon on the PFD. The side column data entry windows are identical to theColumn main data entry windows with the excep

The Inside-Out algorithm merges a side colcalculations. This simultaneous approach means that the SPEC’s and VAfor the main column and side columns need not be balanced provided that the SPEC’s and VARY’s for the total column configuration are balanced. The Sure algorithm solves side columns as separate columns in recycle. This approach is more time consuming, and demands that the SPEC’s and VARYfor the main column and every side column are balanced. The Chemdist algorithm does not permit side columns.

Print Options Click Print Options… on the Column main data entry window to enter the Column Print Options data entry window. Select the desired report options with the check boxes provided. To request plotted results, click Plot Column Results… and select the desired plots with the check boxes on the Column Plot Options data entry window. RATEFRAC® SoftwareO


T

AThe theColumnclicking n the Column main data entry window. A ingle thermodynamic system may be defined for the complete column or

may be used in individual sections of the column. If with the rformed to determine which trays have two liquid phases by clicking the Test for VLLE or Vvapor/li id system for those trays. If perform a in Column- VLLE Test Data window.

TEFRAC® is a registered trademark of Koch-Glitsch, LP.

hermodynamic Systems

thermodynamic system is required for the equilibrium calculations on each tray. rmodynamic system may be changed from the global default in the Thermodynamic Systems data entry window, which is reached by Thermodynamic Systems… o

sdifferent systems

a vapor/liquid equilibrium thermodynamic system is used for part of a column Chemdist or RATEFRAC algorithm, additional checks may be pe

LE Trays check box. The thermodynamic system is then changed to a quid/liqu

you are working with RATEFRAC®, tests for VLLE or VLE Trays can be ed by entering appropriate dat

RA


Column, Liquid–Liquid Extraction

eneral Information e Column unit operation may be used to simulate any distillation or liquid-liquid

xtraction process. Distillation columns are described in the Distillation Column section of this chapter. Although liquid-liquid extraction (llex) columns are generally not trayed, the distillation column nomenclature is used and the term tray denotes an equilibrium stage. A Liquid–Liquid Extraction Column must contain at least two trays. The trays are considered to be linked with the light-liquid phase moving up the column and the heavy liquid moving down. There is no limit on the number of trays in a liquid-liquid extraction column model. Any tray may have a feed, product draw, or duty. There must be a feed to the top and bottom trays.

Note: Side columns may not be used with liquid-liquid extraction columns. The following distillation column features are not applicable to LLEX columns and will be disabled:

• Condenser and reboiler • Pumparounds • Tray hydraulics • Tray efficiencies.

Feeds and Products Column feeds and products are added as part of the flowsheet construction in the PFD. They may be accessed from the Column Feeds and Products window accessible via the Feeds and Products… icon on the Column main data entry window. Feed tray numbers may be added or changed in this window. There is no limit on the number of feeds a column may have. For products, the product type, phase, tray number, and flow rate are supplied in this window. There is no limit on the number of products a liquid-liquid extraction column may have and products may be withdrawn from any tray of the column. Product types include: Overhead, Bottoms, Fixed Rate Draw, and Pseudo-product. Every column must have an overhead product leaving tray one and a bottoms product leaving the highest numbered tray. The product phase may be Light Liquid (Liquid 1) or Heavy Liquid (Liquid 2).

GThe


Product rates must be supplied for all draw products. Rates may be supplied in molar, mass, or liquid volume units. An estimated value must also be provided for

ither the overhead or bottoms product. The estimated value for the overhead or urate as possible to enhance convergence. It is ce Specification to set a desired flow for the

rnal

The following pes of pseudo-products are available:

liquid flow

The solution algorithm is selected in the drop-down list box on the Column main data entry window. The Inside-Out (default), Sure, and Chemdist algorithms are

pecify a liquid-liquid extraction column, select the

stem will automatically d/liquid.

Num eThe m

e Column main data entry window. Every Column must have at least two trays. There is no limit on the number of trays in a Column. Number of Iterations

m number of trial solutions is supplied in the data entry field provided

ebottoms rate should be as accnecessary to use a Performanoverhead or bottoms product.

Pseudo-products Pseudo-products are used to create streams corresponding to column intestreams, making them available for flowsheet calculations. Pseudo-products aredefined in the Column Pseudo-products window accessible via the Pseudo-products… button on the Column Feeds and Products window. ty

Net tray light or heavy Total tray light or heavy liquid flow

Column Algorithm

for distillation columns. To sLiquid-Liquid option. Calculated Phases

d, the phase syWhen the Liquid-Liquid algorithm is selectebe set to liqui

b r of Trays nu ber of trays in the model is entered in the data entry field provided on

th

The maximuon the Column main data entry window. The default value is 30 for the Liquid-Liquid algorithm.


Pr sThe preare perf d in

es ure Profile ssure for every tray in a column model must be defined. All calculations ormed at the defined tray pressures. The tray pressures are define

the Colu re mn Pressure Profile window, which is reached by clicking PressuProfile… on the Column main data entry window. Tray pressures may be

radio button in this

rovided: tray number, a reference name, and the duty, with the appropriate

starting from an n profiles. By default, timate generator.

supplied on an overall or tray by tray mode by choosing a window.

For the overall mode, the top tray pressure must be supplied and either the pressure drop per tray or the total pressure drop across the column. A default value of zero is supplied for the pressure drop per tray and the column pressure drop. All tray pressures are derived by linear application of the supplied pressure drop.

Individual tray pressures are supplied for the tray by tray mode. Note that the top and bottom trays must be included when supplying a table of individual tray pressures. Missing pressures are determined by linear interpolation of supplied values.

Heaters and Coolers Side heaters and side coolers may be configured in the Column Side Heaters/Coolers window that is accessed using the Heaters and Coolers… icon on the Column main data entry window. A negative duty indicates cooling; a positive duty is used for heating. There are no limits on the number of side heaters/coolers. For each side heater/cooler, the following information must be palgebraic sign.

Initial Estimates he Liquid-Liquid algorithm uses an iterative solution technique, T

initial estimate of the tray temperature, flow and compositiothe initial estimate is produced internally using the initial esUser-supplied profiles may be used to replace some or all of the values producedby the estimate generator. Click Initial Estimates… on the Column main data entry window to enter the Column Initial Estimates window. When using the initial estimate generator, profiles are determined by a simple material balance. Temperatures are determined from estimated product compositions. You may optionally provide temperature estimates for the top an

ottom trays whid

ch replace values predicted by the estimate generator, as well stimate of the ratio of the liquid flows on tray 1.

bas an e


When the initial estimate generator is not used, the data which must be supas input profiles are tray temperatures and flows, either light or heavy liquid, or a combination thereof. Note that the minim

plied

um data which may be supplied are the temperatures and flows for the top and bottom trays for the column. While these

s

o speed future calculations with a column model.

itial profiles are entered in tables accessed by clicking the following buttons on e Column Initial Estimates window: Net Vapor Rate…, Vapor Composition…, ray Temperature…, Liquid Composition…, and Net Liquid Rate… Composition stimates are rarely needed for most problems.

erformance Specifications Performance specifications or SPEC’s may be imposed on a liquid-liquid

xtraction column operation such that product stream flows or properties, column ternal flows, column tray temperatures, etc., are at desired values in the olution. For each SPEC, a degree of freedom or VARY must be calculated. For liquid-liquid extraction column, a VARY may be a feed stream rate, heat duty, r draw rate. Furthermore, for convergence to be achieved, there must be a irect effect on all of the SPEC’s by the collective set of VARY’s.

o supply SPEC’s and define VARY’s, access the Column Specifications and ariables window via the Performance Specifications… button on the main olumn data entry window. SPEC’s and VARY’s are entered or edited via the

hypertext strings. PRO/II requires that there be an equal number of SPEC’s and ARY’s. Thus, when a SPEC is added or deleted, you are required to add or elete a VARY.

PEC’s and VARY’s use the general form in PRO/II and are discussed more fully the SPEC/VARY/DEFINE section of this chapter. A list of the stream and uid-liquid extraction column parameters available for SPEC’s and VARY’s also

given in this section.

onvergence Data

onvergence data include algorithm tuning parameters, tolerances, and history rintout options for Column iterations. Open the Column Convergence Data indow via the Convergence Data… button on the Column main data entry indow to enter these data. The tuning parameters are as follows:

Damping Factor: A damping factor of less than unity usually improves convergence when the convergence is oscillating. A default value of 1.0 is supplied by PRO/II.

are the minimum data required, they are rarely adequate to produce anacceptable initial estimate. It may also be desirable to provide solution profilefrom a converged solution t InthTe

P

einsaod TVC

Vd Sinliqis C Cpww


Error Increase Factor: This factor limits the increase in the sum of the errors from iteration to iteration. PRO/II supplies a default value of 100.

Note: The use of tuning factors usually increases the solution time. Tolerances for the liquid-liquid extraction column equations may also be changed although this should rarely, if ever, be done and never as a means to reach a converged solution.

Tolerances are:

Liquid-liquid: The maximum liquid-liquid equilibrium tolerance (equal to the bubble point tolerance for VLE) for each tray. The default is 10-3.

Enthalpy Balance: The maximum heat balance error for each tray. The default

is 10-3. Component Balance: The maximum relative component balance error for

each tray. The default is 10-3. Printout of the liquid-liquid extraction column iterations is useful in diagnosing a convergence failure. History printout for the iterations may be requested by

clicking Convergence Data… and selecting the printout level desired.

Print Options Click Print Options… on the Column main data entry window to enter the Column Print Options data entry window. Select the desired report options with the check boxes provided. To request plotted results, click Plot Column Results… and select the desired plots with the check boxes on the Column Plot Options data entry window.

Thermodynamic Options A thermodynamic system which supports liquid-liquid equilibrium is required for the equilibrium calculations on each tray. The thermodynamic system may be changed from the global default in the Column Thermodynamic Systems data entry window which is reached by clicking Thermodynamic Systems… on the Column main data entry window. A single thermodynamic system may be defined for the complete column or different systems may be used in individual sections of the column.



Column, Side

GThe Sidassocia olumn model is currently restricted to th in the D e methodColumn. Multiple Side Columns attached to one main Column are possible and, in fact, are common practice in the petroleum refining industry. Feeds and Products SiattacheColumn ch exits the complex column a

Solution Methods Solution methods for Side Columns vary with the algorithm. The Inside-Out (and EnhansoThere a

cision in the solution. ses less computing

s.

F(95%) s e this same set of specifications with the un The d usspecial method ompared to the Inside-Out column simultaneous treatment:

eneral Information e Column unit operation models side strippers and side rectifiers ted with a main Column. The Side C

e Inside-Out, Enhanced I/O and Sure algorithms. See Column Algorithmistillation Column discussion (page 191) for further information on thes

s. Side Columns always use the same distillation algorithm as the main

de Columns are added to the flowsheet with the Side Column unit icon and d to the main Column with the feed and product streams. Every Side has at least one external product whi

rrangement.

ced I/O) algorithm merges the Side Column with the main column and lves the complex column arrangement simultaneously.

re three benefits to this approach:

• The simultaneous method results in more pre• The simultaneous solution is more efficient and u

time. • The simultaneous solution provides more flexible product specification

or example, the last benefit permits the use of both a D86 (5%) and a D86

pecification for a side stripper product. To solvSure method requires the use of a Multi-variable Controller

it wrapped around the main column/side column units.

Sure method solves each side column separately from the main column anes recycle streams to relate the side column and main column. When using

recycle logic to converge the column/ side column recycle problem, this has three disadvantages c


• The solution is less precise since a recycle stream tolerance is used in

• • cept the main column draw rate) cannot be

ASide strliquid prfrom thetypically he bottom e lightest her

actionation together with the stripping medium. The stripped liquid is withdrawn duct. Steam side strippers d can be represented with

tripped apor loading for the

ain column. Reboiled side strippers have higher tray efficiencies than those which use a stripping medium. Therefore, three to five theoretical trays are typically used to model these strippers. Side strippers do not normally have any other items of equipment such as condensers, pumparounds, side heaters/cooler etc. Only the Sure method permits the use of a condenser on a side stripper. This capability may be useful whe modeling some unusual types of column configurations.

dditional Information on Side Rectifiers to remove heavy materials from vapor draw products by section. The vapor draw from the main column is fed to

he overhead product from the side rectifier is removed as a finished product. The liquid from the bottom tray is returned to the main column for further fractionation.

addition to the column equation tolerances. The recycle approach is much slower. Main column variables (exdirectly related to the side stripper products. This makes it necessary to use controllers to solve for more than one specification on a side product.

dditional Information on Side Strippers ippers are widely used to control the front end volatility (flash point) of oducts such as diesel, fuel and kerosene. The liquid product is drawn main column and charged to the top tray of the side stripper, which has 6 to 10 actual trays. A stripping medium (usually steam) is fed to ttray of the side stripper to strip about ten percent of the liquid feed (thmaterial) which is then returned to the main column for furt

frfrom the bottom tray of the stripper as a finished proave an overall tray efficiency of about 25 percent anh

two theoretical trays. A variation in side stripper design is the use of a reboiler on the bottom of the side stripper to "heat strip" the liquid feed. No stripping medium is used for reboiled side strippers. The advantage of this arrangement is a smaller svapor return stream to the main column which reduces the vm

s,

n

ASide rectifiers are used

roviding a rectificationpthe bottom tray of the side rectifier which may have a large number of trays. The side rectifier must have a condenser or cooling duty at the top to condense the liquid reflux which is used to rectify the vapor product. T


The side rectifier corresponds to the rectification section of a conventional for

as umparounds, side heaters/coolers, etc. Reboilers are never used for these

distillation column. An overall tray efficiency of 45 to 55 percent is reasonablemany applications. Side rectifiers do not normally have other items of equipment suchpcolumns.



Compressor

General Information

he Compressor simulates a single stage isentropic compression. Outlet Tconditions and work requirements may be determined using either adiabatic or polytropic efficiency. Optional tabular input may be used to determine perf pressure or pressure ratio, head,

or n oler calculation may be included. compressors may be

ssor operation may have multiple feed streams, in which case the inlet

entry window. Note that for compressors s from the after-

ressure, Work, or Head Specification

dow. At least one specification must be s include:

Outlet Pressure: The outlet pressure from the compressor.

ormance from supplied curves for outletk, a d/or efficiency. An optional after-cow

Both VLE and VLLE calculations are supported. Multistage modeled by linking single stage compressor units. Feeds and Products

compreApressure is assumed to be the lowest feed stream pressure. Compressors may have one or more product streams. The product phase condition for units with one product stream is automatically set by PRO/II. For compressors with two or more product streams, the product phases must be specified in the Product Phases window which is accessed by clicking Product

hases… on the Compressor main dataPwith after-coolers, the products correspond to outlet conditioncooler. Product phases allowed include: vapor, liquid, decanted water, heavy liquid, and mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with vapor and liquid products and is not allowed when four product streams are specified.

PThe pressure, work, or head specification is selected from a drop-down list box in

e Compressor main data entry winthsupplied for every compressor. Option

Pressure Increase: The pressure rise across the compressor.


Pressure Ratio: Compression ratio (absolute outlet pressure/absolute inlet

metric

Adiabatic Work Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to adiabatic work in the Compressor Work Performance Curve window.

Polytropic Work Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to polytropic work in the Compressor Work Performance Curve window.

Actual Work Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to actual work (efficiency has been applied) in the Compressor Work Performance Curve window.

Adiabatic Head Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to adiabatic head in the Compressor Head Performance Curve window.

Polytropic Head Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to polytropic head in the Compressor Head Performance Curve window.

Actual Head Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to actual head (efficiency has been applied) in the Compressor Head Performance Curve window.

Efficiency or Temperature Specification An efficiency or outlet temperature specification may be selected from a drop-down list box in the Compressor main data entry window. Options are:

Adiabatic Efficiency: Compressor adiabatic efficiency in percent. This is sometimes called the “isentropic” efficiency.

Polytropic Efficiency: Compressor polytropic efficiency in percent.

Outlet Temperature: Compressor outlet temperature. Efficiency is calculated.

Single Adiabatic Efficiency Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to adiabatic efficiency in the Compressor Efficiency Curve window.

pressure).

Work: Actual work for the compressor.

Pressure Curve: Click Enter Curve… to supply a curve relating volufeed rate to outlet pressure in the Compressor Outlet Pressure Performance Curve window.

Pressure Ratio Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to compression ratio in the Compressor Pressure Ratio Performance Curve window.


Single Polytropic Efficiency Curve: Click Enter Curve… to supply a curve to polytropic efficiency in the Compressor

Efficiency Curve window.

Multiple Adiabatic Efficiency Curve: Click Enter Curve… to supply multiple curves at designated Compressor inlet or outlet pressures, which relate volumetric feed rate to adiabatic efficiency in the Compressor Multiple Efficiency Curves window.

Multiple Polytropic Efficiency Curve: Click Enter Curve… to supply multiple curves at designated Compressor inlet or outlet pressures, which relate volumetric feed rate to polytropic efficiency in the Compressor Multiple Efficiency Curves window. Selection of an efficiency or temperature specification is optional, and if none is selected a default value of 100 percent adiabatic efficiency is used. Note that this corresponds to a perfect isentropic compression.

RPM Adjustment of Compressor Curves Curves for head, work, and efficiency are usually based on a specific compressor speed. Therefore, they should be adjusted when the compressor is operated at a different speed. PRO/II performs adjustments for these curves when values are supplied for the Reference RPM (curve basis) and the Operating RPM. Adjustments are based on the fan laws and are as follows:

relating volumetric feed rate

[ ] 0.2referenceRPM / RPMrefHead Head =

[ ]3.0

referenceRPM / RPMref Work Work =

[ ]referenceRPM / RPMrefEfficiency Efficiency = Aftercooler Option An aftercooler may be added via the Aftercooler… icon on the Compressor main data entry window and supplying the cooler outlet temperature and pressure drop in the Compressor Aftercooler window.


Outlet Temperature Estimate n estimate for the outlet temperature for the compressor may optionally be

supplied in the Compressor main data entry window to speed convergence. Note that this is not the same as the Outlet Temperature specification.

alculation Method the Compressor head by clicking Calculation

compute head.

sed

try

ation” is used to compute the

or compressors with Work specifications, a relative convergence tolerance may

sure

is value.

mpressor calculations op-

A

CSelect the method to calculateMethod… on the Compressor main data entry window. This displays the Compressor Calculation Mode window. The method may be chosen with the radio buttons provided, with choices as follows:

GPSA Engineering Data Book: The GPSA Data Book equation is used to

ASME Power Test Code 10: The ASME Power Test Code 10 equation is uto compute head. This method, the default, is the most rigorous.

The compression ratio above which the head equation is used to compute the isentropic/ polytropic coefficient may also be supplied in this window. This enonly applies to the GPSA method, with a default value of 1.15 supplied. Belowhis compression ratio, the GPSA “temperature equtisentropic/polytropic coefficients. Relative Convergence Tolerance for Work Specifications Foptionally be supplied in the Compressor main data entry window. A default value of 0.001 is used when no value is supplied. Maximum Outlet Pressure For compressors with Work specifications, a maximum outlet pressure may optionally be supplied in the Compressor main data window. The outlet preswill be reset to this value when the supplied work results in a pressure exceedingth Thermodynamic System

he thermodynamic system of methods to be used for coTmay be selected by choosing a method from the Thermodynamic Systems drdown list box on the Compressor main data entry window.


Controller

General Information

h ack process controlled by adjusting meter to achieve a specified result for a process ontroller must have one Specification and one

Vco unflo

pecification ied via the appropriate underlined hypertext in the

sed y double-clicking on the Controller flowsheet icon). By clicking the hypertext

eter to use as the SPEC. The SPEC may be a single arameter or a mathematical expression that relates two flowsheet parameters.

Yappropriate linked text. See the SPEC/VARY/DEFINE section of this chapter for further details on the generalized SPEC form used in PRO/II. V riabTParame . The Parameter window is used to designate the stream or unit parameter to use for th e SVARY find tables of the flowsheet variables that may be us ’s in controller units.

T e Controller simulates the action of a feedban upstream flowsheet parastream or unit operation. A c

ARY, where the SPEC may be a stream flow rate or property, a unit operating ndition, or a Calculator result. The control variable (VARY) must be a stream orit operation flowsheet parameter that is otherwise at a fixed value in the wsheet.

SThe Specification is supplSpecification field of the Feedback Controller main data entry window (accesbstring Parameter, the Parameter window appears in which you can select the unit parameter or stream paramp

ou may next enter the value and the tolerance for the SPEC by clicking the

a le he control variable (VARY) is selected by clicking the linked text string

ter in the Variable field of the Feedback Controller window

e VARY in a manner analogous to that used in selecting the SPEC above. ThPEC/VARY/DEFINE section of this chapter gives more information on the

concept. You will alsoPEC’s and VARYed for S


Limits and Step Sizes Limits and step sizes for the control variable may be supplied by clicking Limits and Step Sizes… on the Feedback Controller window. A maximum value, m ntered in the L the control to replaYou ma PSeveralthis sec um numberselect the action taken when the control variable exceeds the prescribed limits:

• The value is set to the limit as a solution and flowsheet calculations continue (the default), or

• Flowsheet calculations are halted.

oller Iterations

he refore, it

the r ired

may keep the control function ithin a range of feasible solutions.

inimum value, and/or maximum change in the control variable may be eimits and Step Sizes window. Optionally, you may supply a value forvariable for the second iteration by selecting the appropriate radio button ce the default change of 2.0 percent of the initial control variable value. y specify a different percent or value for the second iteration.

arameters parameters regarding the operation of the Controller may be supplied on tion of the Feedback Controller window. You may change the maxim of iterations from the default value of 10. Use the radio buttons may to

Print Results for ContrThe default setting prints a summary for each iteration of the controller. To eliminate this printout, deselect the check box on the Feedback Controller

indow. w Next Unit Calculated after Control Variable is Updated Ordinarily, this is the first unit operation in the calculation sequence that is affected by the control variable and is determined automatically (“calculated”) by PRO/II. You may specify a different return unit by using the drop-down list box on the Feedback Controller window. Non-convergence of Controllers The controller uses a Newton-Raphson technique to search for the value of tcontrol variable that meets the specified flowsheet parameter result. Theis important that there be a continuous and monotonic relationship betweencontrol variable and the specification. Control functions with discontinuities olocalized maxima and minima may fail to converge or converge to an undesresult. For some cases, the limits and step sizes entriesw


Controllers and Recycle Loops

nstream ected by

ler and the recycle solve simultaneously. To reach convergence of the controller in each iteration of the loop, changes must be made to the calculation order. This typically is accomplished by re-ordering the controller to execute after the last downstream unit that is referenced by the controller. Tolerances are another area of attention. To ensure convergence, It is important for the tolerance of the controller to be tighter than the tolerance of the encompassing recycle loop.

Controllers always create a recycle loop in the flowsheet, from the dowunit at which the specification is evaluated to the first upstream unit affthe control variable. When a controller is located within a recycle loop, PRO/II normally solves the controller as part of the loop. This means the control




Crystallizer

General Information

tion simulates crystallization processes for the

sign or Rating calculations in the Crystallizer Calculation ode window. In design mode, a specification is required and the volume is

, the vessel volume is defined.

ssions in the Crystalli tion Rates window. These relationships are similar t r power law kinetics used for chemical reactions. Full

l.

Feeds and Products The Cry ny number of feed streams. The inlet pressure is taken to pressure of all the feed streams.

The Crystallizer unit operamanufacture of organics, inorganics, fertilizers, biochemicals and polymers. The crystallizer transforms a supersaturated solution into a mixed solid/liquid crystal slurry. The crystallizer is modeled as a Mixed Suspension Mixed Product Removal (MSMPR) crystallizer or Continuous Stirred Tank Crystallizer (CSTC). These models assume ideal mixing in the unit and that the product conditions are the same as the bulk conditions. The model also assumes that breakage or agglomeration of solid particles is negligible. A feed heat exchanger may be included in the model with recirculation if required. The crystallization process depends on phase equilibria as well as kinetic or non-equilibrium considerations. Solid-liquid equilibrium is defined in terms of solubility, which is calculated from either the Van't Hoff equation or user-supplied solubility data.

ou must select DeYMcalculated. In the rating mode The formation rate relationships are expressed as power law expre

zer Growth and Nucleao equations fo

details of the calculation method can be found in the PRO/II Reference Manua

stallizer can have a be the lowest

Both an overhead and bottoms product must be specified in the Crystallizer Products window. The bottoms product contains the crystals in the solid/liquid slurry. The overhead contains any vapor generated in the unit.


Unit Specification rystA C ified by filling in the data variables for Solute

and Solvent, Crystal Shape Factor, Calculation Mode, Design Specification (in esign Mode) and Growth and Nucleation Rates. Access the appropriate data

of p/6 in

Solut n

Select the solute and solvent components. The solute must be defined as a liquid-solid are no liquid-solid components available in the simul yed prior to opening the Crystallizer main data ent component as liquid-solid, select

Crystal Production Rate: Enter the production rate of the crystals in weight

e crystallized.

Magm ttom Product: Enter the density of the bottom

eight of crystals per unit volume of slurry.

S ersaturation ratio which is defined as:

(Xexit - Xsat)/ Xsat where:

product.

allizer unit operation is spec

Dentry windows from the Crystallizer main data entry window. Access the main Crystallizer Data Window by double-clicking the Crystallizer unit icon.

rystal Shape Factor CThe shape factor defaults to 1.0 which indicates cubic crystals. A value

dicates spherical crystals.

e a d Solvent

component. If thereation, a warning message is displa

ry window. To specify a Input/Component Selection/ Component Phases.

Calculation Mode Click Calculation Mode… to specify the Design or Rating calculation mode. In Design mode, a specification is required and the vessel volume is calculated.Specification options are:

units. Fraction of Solute Crystallized: Enter the fraction of the total solute in the

combined feeds that is to b

a Density product as w

in the Bo

upersaturation Ratio: Enter the sup

Xexit is the liquid phase mole fraction of the solute in the bottom product, andXsat is the saturation mole fraction of the solute in the bottom

In Rating mode, the vessel volume is defined.


Grow tion Rates

Cryst upply the Rate Constant for the rate

sec or m/sec. Growth rates are typically in the range 2.0x10 to 2.0x10-8 m/sec. By default, the rate is directly proportional to

ou must supply the Rate and specify its dimensional units. By default, the

proportional to the Supersaturation Ratio. You may change this by overriding the default Exponential Factors.

Opera

lick Op nditions. By

w Po

is selected either th

ecirculation Flow rate: Some of the bottom product may be remixed with the

either spacross t Alternat of entering a numeric value for the parameters in this

indow, they may be referenced using the DEFINE system relative to any available unit operation or stream parameter calculated elsewhere in the simulation. See the table of Crystallizer Parameters available for Cross-

th and NucleaClick Growth and Nucleation Rates… to specify Growth and Nucleation Rates.

al Growth Rate: You must sequation in ft/

-7

the Supersaturation Ratio. You may change this by overriding the defaultExponential Factor. Factors are usually in the range 0.0 to 2.5.

Crystal Nucleation Rate: The Nucleation Rate is the number of crystals nucleated per unit time, per unit liquid volume. YConstant for nucleationrate is directly

Typical values for the Supersaturation Ratio Factor are in the range 0.5 to 2.5 for secondary nucleation and up to 10 for primary nucleation. If an exponent is specified for the Impeller Speed, you may need to change the default value of 100 RPM.

ting Conditions erating Conditions… to specify Crystallizer Operating CoC

default, the crystallizer operates at the combined feed temperature and pressureith no recirculation.

ressure Specification: The pressure may be specified as a drop below the mbined feed pressure or you may specify the pressure value directly. c

Second Specification: If an option other than At Merged Feed Temperature

, the unit is assumed to include a feed heat exchanger. You may specifye crystallizer operating Temperature or the Duty of the exchanger.

Rfeed and passed through the feed exchanger. To specify this option, you must

ecify the recirculation Volumetric Rate or the Temperature Change he exchanger. A negative change denotes a temperature drop.

ively, instead w

Referencing in the online help for more details.


Print Options Click Print Options… to access the Crystallizer Print Options window. Check the Include Crystal Size Distribution box to request additional output, including tables of fractions and population densities for the feed and product

as functions of thstreams e crystal size distribution.


Cyclone

al Information Gener

n ined by the low

e ll

isotherm ms such as agglomeration and crumbling are

se specified, the inlet est pressure. The

st be two product omes in as well as

ds. The bottom stream will contain only the collected solids. mponents that enter a cyclone must have a particle size distribution.

e user.

efficiencCycloneunit icon RatinIf you seother di ill be generated from the diameter. If you select

ser Defined Geometry, you must also enter all of the geometric ratios as escribed below. In Rating Mode, PRO/II will calculate: pressure drop, total fficiency, component efficiencies, grade efficiencies and weight percent solids in e overhead stream.

The Cyclone unit operation models the separation of particulate solids from a d gas stream. The particulate collection efficiency is determsolid a

solids loading, component characteristics, particle size distribution, stream frate, and cyclone geometry. The Cyclone unit operation will calculate thcollection efficiency for every particle size range of each solid component as weas the pressure drop through the unit. The Cyclone is assumed to operate

ally and mechanisdiscounted. Feeds and Products A Cyclone may have up to ten feed streams. Unless otherwipressure will be taken as that of the feed stream with the lowfeed streams may not contain a liquid phase, and there mustreams. The overhead stream will contain all the gas that cany uncollected soliAll solid coThis distribution may be set by another unit or defined by th Unit Specification A cyclone unit operation is specified by filling in the appropriate real and integer data variables for operating mode, geometry, pressure drop calculations,

y calculations, and multiple cyclone configuration in the Gas/Solid main data entry window that is accessed by double-clicking the Cyclone on the PFD.

g Mode lect Rating Mode, you must supply the diameter of the cyclone. The

mensions of the cyclone wUdeth


Design Mode If you select Design Mode, you need not provide the cyclone diameter. Again, if you select User Defined Geometry, you must enter all of the geometric ratios as described below. In addition, you must specify a target for total solids collection (see entry fo RPARM(13) below). You may also wish to override the default

inches of water by entering a value in whatever r (see entry for RPARM(16) below). In addition to

e normal Rating Mode output, Design Mode will calculate the number and size

he Cyclone can model a system of identical cyclones that are arranged either in parallel or in series. In the case of parallel cyclones, the feed streams are split evenly among the cyclones. The overhead products from all cyclones merge into one overhead and the bottoms products from all cyclones merge into one bottom stream. In the case of series cyclones, the overhead from the first cyclone is the

ed to the second and so on. The overhead product is the overhead product e the bottom product is the combined bottom product system. Both product streams are at the outlet

increase efficiency and pressure decrease the efficiency and pressure drop in a

Calculation Mode (IPARM(1)) This input is optional. Options are: lt)

Effici

Deicht

The Liame hich are collected with 50% efficiency). The API ethod is based on a ratio of particle diameter to critical diameter (the diameter

r maximum pressure drop of 10input pressure units you prefethof identical cyclones that are necessary to meet the specification. There may be many cyclone systems that meet the specification. In all cases, Design Mode will return the system requiring the fewest cyclones. Multiple Cyclones T

fefrom the final cyclone whil

om all the cyclones in thefrpressure of the final cyclone in the system. It is not possible to specify recycle streams inside the unit or to reference intermediate stage data from the flowsheet. For example, if you wish to set a specification on the second cyclone in a three-cyclone series or set a recycle from the second cyclone to the first cyclone, you should model the system as three separate units. Note that while increasing the number of identical cyclones will drop in a series system, it will parallel system.

Integer Data for Unit

1. Rating (defau2. Design

ency Model (IPARM(2)) This input is optional. Options for Rating and sign mode are: 1. Koch & L2. API (default) 3. Lapple

apple model is based on a ratio of particle diameter to cut diameter (the ter of the particles wd

m


of particles which would be collebased on a particle size ratio.

cted at 100%). The Koch & Licht method is not

nother vessel, the API method allows values for the Inlet

M(4)) This input is optional. Options for both

If th height ratio, inlet widdiamete , gas outlet tube length ratio, height of cylindrical section ratio, and

Shape of Gas Inlet Flag (IPARM(6)) This input is optional. Options for both

Rating and Design mode are: 1. Tangential (default) 2. Scroll or volute 3. Axial

Cyclone is inside Vessel Flag (IPARM(7)) This input is optional. Options for

both Rating and Design mode are: 1. No (default) 2. Yes

For a value of 2, the Inlet Width Ratio and the Superficial Gas Velocity must be specified. Dipleg Size is calculated if the value of 2 is entered.

Pressure Model (IPARM(3)) This input is optional. Options for both Rating and

Design mode are: 1. Koch & Licht (default) 2. API

If the cyclone is inside aWidth Ratio and the Superficial Gas Velocity (described later in the section titled Real Data for Unit) to be specified.

yclone Geometry (IPARCRating and Design mode are:

1. Stairmand (default) 2. High efficiency Swift 3. Lapple 4. General purpose Swift 5. Peterson & Whitby 6. User-defined geometry

e user-defined geometry is used, values must be specified for the inletth ratio, cyclone dust outlet diameter ratio, cyclone gas outlet

r ratiototal cyclone height ratio as appropriate for the calculation method used as shown. Inlet Vane Flag (IPARM(5)) This input is optional. Options for both Rating and

Design mode are: 1. No (default) 2. Yes


Efficiency AdjustmOptions for both

ent Due to Loading Flag (IPARM(8)) This input is optional. Rating and Design mode are:

1. Adjust (default) 2. Do not Adjust

Automatically Switch Pressure Drop Model (IPARM(9)) This input is optional. Options for both Rating and Design mode are:

op model

onfiguration of Multiple Cyclones Flag (IPARM(10)) This input is optional. nd Design mode are:

2. Series Number of Identical Cyclones (Series or Parallel) (IPARM(11)): This input is

optional and is used only in Rating Mode. The default value is 1 cyclone.

umber of Particle Size to be Specified (IPARM(12)) This input is optional and is for Rating Mode only. This and the following entry can be used together to specify the component and PSD size range whose weight fraction in the overhead will be output to RPARM(64). This latter value can be accessed by a Controller, MVC or Optimizer.

For example, if a solid with PSD data: 10, 20, 30, 40 (in default input units) is required to have a weight fraction of 0.20 in size range 20 to 30, the value for

second size range) and the value for a DEFINE . The default value is 1 (the first size range).

fied (IPARM(13)) This input is optional

a PSD that the design mode may evaluate.

input is optional and is for umber of cyclones in parallel

or series as appropriate based on the value specified above for the e Cyclones Flag. The default is 20 for parallel and

1. Do not Switch (default) 2. Switch

This entry allows changes to be made automatically in the pressure drbetween the Koch & Licht and API methods based on solids loading. C

Options for both Rating a1. Parallel (default)

N

this entry would be 2 (thestatement would be 0.20

Number of the Component to be Speci

and is for Rating Mode only. This optional input is the number of the component with particle size distribution data to be used in the design. The default is the first solid component with

Maximum Number of Cyclones (IPARM(14)) This

Design Mode only. The value indicates the n

Configuration of Multipl3 for series.


Real Data for Unit The cyclone geometry is input as the ratio of length divided by overall cyclone body diameter, so that an inlet height of 0.1 meters on a cyclone of diameter 0.2

eters would have an inlet height ratio of 0.1/0.2 = 0.5.

Diameter of Cyclone Cylinder (RPARM(1)) This input is required and is for Rating Mode only.

let Height Ratio (RPARM(2)) This Rating/Design Mode entry is optional.

nal.

M(5)) This Rating/Design Mode

Gas Ou th Ratio (RPARM(6)) This Rating/Design Mode entry is

Height of Cy Section Ratio (RPARM(7)) This Rating/Design Mode

otal Cyclone Height Ratio (RPARM(8)) This Rating/Design Mode entry is optional.

Diameter of Vessel Housing (RPARM(9)) This Rating/Design Mode entry is optional.

Superficial Gas Velocity (RPARM(10)) This Rating/Design Mode entry is optional.

.

t pressure differs from feed stream pressure. The default is the lowest feed stream pressure.

esign Mode entry is optional. The default is 0.1 m.

al.

clones in a unit The

default is 2.488 kPa.

m

In

Inlet Width Ratio (RPARM(3)) This Rating/Design Mode entry is optional.

Cyclone Dust Outlet Diameter Ratio (RPARM(4)) This Rating/Design Mode entry is optio

Cyclone Gas Outlet Diameter Ratio (RPARentry is optional.

tlet Tube Lengoptional.

lindrical entry is optional.

T

Pressure Drop to Inlet (RPARM(11)) This Rating/Design Mode entry is optionalThis value is the pressure drop between the feed stream and the inlet to the cyclone. The default is 0.0.

Absolute pressure at cyclone inlet (RPARM(12)) This Rating/Design Mode entry is optional. For use if cyclone inle

Goal Efficiency for Design Mode (wt%) (RPARM(13)) This Design Mode entry is required.

Minimum Cyclone Diameter (RPARM(14)) This D

Maximum Cyclone Diameter (RPARM(15)) This Design Mode entry is option

The default is 0.5 m.

Maximum Pressure Drop (RPARM(16)) This Design Mode entry is optional.This value is the maximum pressure drop across cy


Tolerance for Cyclone Body Diameter (RPARM(17)) This Design Mode entry is optional. The default is 0.001.

Real Number Output from Cyclone The output values calculated by the Cyclone model are stored in the indicated locations in the RPARM() array and can be accessed by a Controller, MVC or Optimizer. All RPARM() outputs are produced in both Rating and Design modes. Overall Efficiency (wt%) (RPARM(51)) In Design mode, this is an input value

included in the output report for the cyclone unit. Diameter Of Cyclone Cylinder (RPARM(52)) In Rating mode, this is an input

value included in the output report for the Cyclone model. Pressure Drop (RPARM(53)) This is adjusted for loading by the user. Total Solids In Overhead (RPARM(54)) This is the weight % of the total

overhead stream. Inlet Height Dimension (RPARM(55)) Inlet Width Dimension (RPARM(56)) Cyclone Dust Outlet Diameter Dimension (RPARM(57)) Cyclone Gas Outlet Diameter Dimension (RPARM(58)) Gas Outlet Tube Length Dimension (RPARM(59)) Height of Cylindrical Section Dimension (RPARM(60)) Total Cyclone Height Dimension (RPARM(61)) Dipleg diameter (RPARM(62)) This requires that the cyclone be located above a

fluidized bed, i.e., the cyclone must be located inside a vessel. This value is output in the cyclone output report only if applicable. PSD weight fraction in the overhead RPARM(64) This value is the particle size distribution weight fraction in the overhead of the size and component specified. See entries for IPARM(12) and IPARM(13) above. This is the ratio of weight in the specified size range divided by the weight of the component in the overhead. This value is output in the cyclone output report only if applicable.


Rotary Drum Filter

General Information

he Rotary Drum Filter unit is used to decrease the liquid content of a stream lly

n be multiple Feed Streams but only two products for Rotary Drum onsists of the liquid components removed from the lids. The Cake stream is a mixed phase stream

real ng by es

re discussed below.

Calcu

e Rotary Drum Filter can be operated

i. Rating Mode

If one selects the Rating Mode, then Diameter and Width of the Rotary Drum Filter must be supplied. The Maximum Pressure Drop across the Rotary Drum Filter and Width to Diameter Ratio will be calculated.

ressure ter of

Tcontaining solids. The model assumes a rotating, horizontal drum partiasubmerged in a trough of slurry mixture, which is to be filtered. Feeds and Products

here caTFilter. The Filtrate product cfeed(s) and contains no socontaining predominantly solids with some liquids. Unit Specification A Rotary Drum Filter unit operation is specified by filling in the appropriate and/or integer data variables in the tabs named as: Calculation mode, OperatiConditions and Cake Properties in the main data entry window. It is accesseddouble-clicking the Rotary Drum Filter unit icon on the PFD. The variabl

ssociated with each tab aa

lation Mode In calculation mode Tab, one will see that thin either of the two modes:

ii. Design Mode

If one selects the Design Mode, one must provide the Maximum PDrop across the Rotary Drum Filter diameter whereas Width to DiameRatio is optional. This will lead to the calculation of Diameter and Width Rotary Drum Filter.


Operating conditions Value for Rotational speed of the drum (in RPM’s) is a mandatory user input, but one has a choice to specify either the angle of filtration or the percentage of drum

Por Resistance at e t values and

ce are optional fields.

to e

(i) Particle Size Distribution (PSD) should be given so that PRO/II can calculate Average Particle Diameter and use it in further calculation

iltration Resistance or ask PRO/II

ration Resistance, then the Specific Resistance is a mandatory user input.

submerged. The default values for angle of filtration and percentage of drum submerged are available. Cake properties

osity, Percentage of solids in the cake, Average Sphericity, Cakexis ing pressure drop and Cake Compressibility have default

hen User can either specify the percentage of solids in the cake or ask PRO/IIcalculate it. In the latter case, Average Particle Diameter has to be madavailable through one of the following possible ways:

sequence.

(ii) It can be given directly as a user input in the Float field provided.

PS: Though the Float field is shown as optional, there is no default value for Average Particle Diameter.

In the similar way, user can either specify the Fto calculate it. If user wants PRO/II to calculate the Filt


Solids Dryer

General Information

s used to decrease the liquid content of a stream containing the liquid being removed is water. The Solids Dryer may be

operated at a fixed temperature and pressure or at a fixed heat duty requirement. Alternatively, the pressure or temperature may be fixed and a design specification placed on one of the product streams, generally, the dried solid stream.

Calculation Method The the option of specifying two specifications to satisfy the degrees of freedom. Two types of specifications are available for this unit peration; they are Operation Specification and Design Specification. Flash

econd Specification

elect one of the Unit Specification or supply product specification.

The Solids Dryer isolids. Generally,

Solids Dryer provides

ocalculations are used to meet the provided specifications.

Feeds and Product Streams The Solids Dryer unit can have any number of feed streams. The Solids Dryer unit requires two product streams. Both an overhead and bottoms product streams must be specified. First Specification Select one of the following parameters: Pressure Drop: The decrease in outlet pressure over the lowest feed stream pressure. Negative values indicate a pressure rise. Pressure: The pressure in the Solids Dryer Temperature: The temperature in the Solids Dryer. S S


Unit Specification choices

n Pressure, Pressure Drop and Duty are avail ction in the unit specification list box. Temper u an estimate for the temperature value, w h int of the iterative calculations to determi t Pressur E tionally, supply an estimate for the pressure value, which will be t n of the iterative calculations to determine the actual pressure.

r a molar (M) basis. The default is weight. Molar may only be used if all solids

n of a particular component or group of components in the VHD or BTMS stream on a weight (WT) basis or a molar (M) basis. The default

ion. PHASE=L must be entered

PPM: rts per million of a particular component or group of components in the OVHD or BTMS stream on a weight (WT) basis or a molar (M) basis. The default is weight. Molar may be used only if all solids have their molecular

If Pressure/Pressure Drop is selected in the first specification Temperature and Duty are available for selection in the unit specification list box. If Temperature is selected in the first specificatio

able for sele

at re Estimate: Optionally, supply hic will be taken as the starting po

ne he actual temperature.

e stimate: Opake as the starting point

Product Specification Choices

• Rate • Moisture Content • PPM • Fraction • Vapor Fraction

Rate: The flow rate of either the OVHD or BTMS stream on a weight (WT) basis ohave their molecular weights defined. If COMPONENT is also used, then rate refers to the flow rate of a component or group of components. When RATE is used with the BTMS keyword, the rate may refer either to the total BTMS rate (PHASE=T and default) or to the liquid portion of the BTMS rate (PHASE=L). Fraction: The fractioOis weight. Molar may be used only if all solids have their molecular weights defined. The COMPONENT entry is also required. PHASE=T is not allowed withthis specificat

Moisture: The moisture content of the BTMS stream on a weight (WT) basis ora molar (M) basis. The default is weight. Molar may only be used if all solids have their molecular weights defined. Moisture Content is defined as the ratio of mass or moles of water to mass or moles of total solids.

The pa


weights defined. The Callowed with this specif

OMPONENT entry is also required. PHASE=T is not ication. PHASE=L must be entered

Vapor Fraction: The fraction of the feed vaporized on a weight (WT) basis or a molar (M) basis. The default is weight. Molar may only be used if all solids have their molecular weights defined. The fraction may refer either to the total feed rate (PHASE=T and default) or to the liquid portion of the feed (PHASE=L). The BTMS keyword is not allowed with VFRAC.


Depressuring Unit

General Information The Depressuring Unit simulates the time-pressure-temperature relationships

at occur when a vessel is depressured through a relief or control valve. Several different valve models, vessel configurations and models for heat flow into the unit are available. An optional external makeup stream may also be specified.

ustry standards.

ns

lt

imulation (time zero.)

al depressuring conditions, values may be entered for either or both nal Vessel Pressure and Elapsed Time. The elapsed time can be measured

ser-supplied values for the relative volume tolerance per time step, the aximum number of time steps, and the time step size can be entered on the alculation Options window. This window is brought up by clicking Calculation

Options… on the Depressuring Unit main data entry window.

th

The initial phase of the vessel contents may be either a vapor or a vapor-liquid mixture. Calculation Options Calculation options include procedures from API Standard 2000, API Recommended Practice 520, and other ind Initial Relief ConditioThe initial relief conditions can be based on either a specified initial time or a specified initial pressure by selecting the appropriate radio button. The defauselection is to start the depressuring calculations at the beginning of the s

Note: This option is only available if the heat input model type “Fire Relief Model” is selected.

Final Depressuring Conditions To set the finfifrom Time Zero or from the Start of Relief by choosing the desired toggle text. If both final Vessel Pressure and Elapsed Time are selected, the depressuring calculations will stop when the first criterion is satisfied. Time Step Size Calculation Options UmC


The default valuealue for the Ma

for the Volume Tolerance per Time Step is 0.0001. The default ximum Number of Time Steps allowed in the depressuring

imulation is 100. The default value for the Time Step size is calculated using default values for the sizing param ters. User-supplied values for the parameters used in this alculation may be entered via the appropriate hypertext string. The step size

st, which includes

er (a) or (a)

Efficiency

D w models except for

ure profile errors are detected. Clicking on the Stop hypertext on the Calculation Options window toggles the option to Continue and allows the simulation to continue even if pressure profile errors are dete VaDatcharacteclicking Model m te radio butto Con ation for tvalvdefa

vs

ecbasis is selected from a pop-up li

a. total fluid quantity in increments of the amount* (a constant) b. vapor quantity in increments of the amount* (a constant), or c. the smaller of (1) or (2).

he default selection for time step size basis is (a). Choosing eithT

allows entering user-supplied values for the constants in the pop-up float field. For the time step size basis of (1), the default value of the constant is 0.04. For(2), the default value of the constant is 0.50. Specification of IsentropicEither the default isentropic efficiency or a user-supplied value may be used in the blowdown calculations by selecting the appropriate radio button on the

epressuring Unit - Calculation Options window. For all heat floRigorous Blowdown or Semi-rigorous Blowdown, the default value is 0.0. If

Rigorous Blowdown or Semi-rigorous Blowdown is selected for the Heat Flow Model, the default isentropic efficiency is 1.0. Action when Errors are Detected By default, the simulation will stop if press

cted.

lve Data a can be entered on the Depressuring Valve Data window to define the flow

ristics of the relief valve or control valve. This window is brought up by Valve Data… on the Depressuring Unit main data entry window. A Valve ust be selected from the four choices by choosing the appropria

n. The available valve models are Supersonic Flow, Subsonic Flow,stant Flow, and User Model. The default is Supersonic Flow. The equhe selected model is displayed as an aid to entering the parameters in the e equation. The units displayed for the equation are consistent with the ult UOM for the problem and may not be changed.


A VFor , the valve constant is the only entry allowed. For

model, an optional back pressure may be entered along with alve constant. For the Constant Flow model, the only allowable

entry is the valve constant. For the User model, the control valve coefficient must be entered. The default back pressure value is 0.0, while the default value for the criti ffactor m VesseThe e on of the

via the Vessel Data button on the ne of the following must be

• Sphere • Horizontal Cylinder

Unspecified Shape Sphere is the selected vessel geometry, a value for the diameter must be

entered. If Horizontal Cylinder is the selected vessel geometry, the diameter and ngent-to-tangent length must be entered. For the Vertical Cylinder vessel

geometry, the diameter and tangent-to-tangent height must be entered. For vessels of any of these defined geometries, entering a value for liquid height is

ume must be entered. Liquid Holdup is optional only if the geometry is Unspecified Shape. By default, the holdup liquid is saturated liquid of the combined feed comp or in e ili l volume tion basis. The Vessel Weight and the Vessel Specific Heat may be input for any vessel geometry. If oThe i , othe i ) The lCylicorr if not supplied

alve Constant (C) must be entered for all models except for the User Model. the Supersonic Flow model

the Subsonic Flowthe required the v

cal low factor is 1.0 Different values for the back pressure and critical flow ay be entered.

l Data D pressuring Vessel Data window is used to define the configurati

depressuring unit. This window is accessible Depressuring Unit main data entry window. Oselected by choosing the appropriate radio button.

• Vertical Cylinder

If

ta

optional. For vessels of the Unspecified Shape geometry, the vessel vol

osition at the initial conditions. The remaining vessel volume contains vapqu brium with this liquid. The holdup may be on a mole, weight, or actua

fraction basis with the default being the mole frac

ne of these two variables is entered, then both must be entered. se tems are required only if “Blowdown” appears on the Heat Input window

se they are optional. (See discussion on vessel Heat Input optionrw s below. vo ume correction factor is an optional entry for the Sphere, Horizontal

r, and Vertical Cylinder vessel geometries onnde ly. This entry is used to ect the vessel volume for pipes, fittings, and end plates and defaults to 1.00

.


HeClick Heat IHeat Input w t box, which

• • • API 2000 Method with Scaling

• • • • • .

Usedifference b ls is the phyalonselected, fro coefficients may be supplied. For the User-

orous Blowdown models, values for these

.

default value of 1.0.

T In t Scaling Factor may be input for any heating model except the Semi-rigorous fault value of 1.0.

Semi-rigorbutton options Overall coefficiThe default is tfactor of 1.0.

at Input nput… on the Depressuring Unit main data entry window to open the indow. A heat input model may be selected from the drop-down lis

includes the following options:

User-defined API 2000

• API RP 520 with Scaling API RP 520 Isothermal Rigorous Blowdown Semi-rigorous Blowdown Fire Relief

r-Defined is the default as this supplies no heat input to the vessel. The etween the Rigorous and Semi-rigorous Blowdown mode

sical property calculations. The selected heat transfer equation is displayed, g with the equation’s units of measure. Depending on the Heat Flow Model

m one to five of the Defined or Semi-rigorous or Rigcoefficients default to 0.0. For the Fire Relief Model only, the first two coefficients C1 and C2 are required The Initial Wetted Area field is made unavailable when a value has been entered for Liquid Height on the Vessel Data window. Otherwise, a value for Initial WettedArea must be entered for the API 2000, Scaled API 2000, RP 520, Scaled RP 520, and Fire Relief Models. The Area Scaling Factor is an optional entry for these same heat input models only when the Initial Wetted Area is input. It has a

he Heat pu

and Rigorous Blowdown and Isothermal models. It has a de

The ous and Rigorous Blowdown models provide the following radio

for the heat transfer coefficient: Calculated Using Scaling Factor, ent, or individual vapor and liquid phase heat transfer coefficients. he Calculated Using Scaling Factor option with a default scaling


Makeup Stream One feed stream to the depressuring unit can be designated as a constant-rate

eup stream try window to opendesignated. Chnames of all festream may be ays begin at time =makeup stream

nt Results for Depressuring Unit The Print Options window allows the user to control the intermediate and final printed results for the Depressuring Unit. This window can be accessed through the Output/Report Format/Unit Operations menu option or from the Depressuring

main d The default for allows the user t basis.

lt, ponent compositions are printed for all steps. The user may choose to p r only the initial, final, and relief conditions, by clicking the hypertext. The user may suppress all composition printout by deselecting the

Intermediate pr r may select a di ich brings up the Intermediate Print Interval Options

ption g the print frequeStep, and User radio

ThermodynFor problems wa drop-down list box allows the selection of a thermodynamic method set to be

or th e

mak . Click Makeup… on the Depressuring Unit main data en the Makeup Stream window, where a makeup stream can be ecking the box enables a drop-down list box which contains the ed streams to the depressuring unit shown on the PFD. One selected as a makeup stream. The flow of this stream will alw 0, regardless of when the depressuring begins. By default, no is included.

Pri

Unit ata entry window.

all stream printout is a molar basis; clicking on the toggle text to select weigh

By defau com

rint all steps, o

box.

intout is printed at each calculation step time by default. The usefferent interval by clicking the default time step linked text, wh

window. The Intermediate Print Interval O s window provides the following radio button options for specifyin

ncy of intermediate results: Default Time Step, User-defined Time -defined Pressure Interval. Simply select the appropriate

button.

amic System here more than one thermodynamic method has been specified,

used f e D pressuring Unit.


Dissolver

General InfThe Dissol u ns. This mass organic as well Feeds and The dissolver u

en to be e

Both an overhemay be modifiecontains the liq The overhead

tains an a CalculationThe dissolver tPRO/II models hich is the stirred tank

lver. A e

A Solid-liquid ecalculated fromYou must selecwindow. In Des for a given feedmode, the vess article size distribution is

T w

d in the Thermodynamic Data.

thod can be found in the PRO/II Reference

ormation vertran

nit operation models the dissolution of solids into liquid solutiosfer operation is widely used in the chemical industry in both as inorganic processes.

Products nit can have any number of feed streams. The inlet pressure is

tak

th lowest pressure of all the feed streams.

ad and bottoms product must be specified. The default allocation d in the Dissolver Products window. The bottoms product uid product along with any remaining crystals.

con y v por generated in the unit.

Method ransforms crystals in solution from the solid to the liquid phase. the most common type of dissolver w

disso

fe d heat exchanger may be included in the model if required.

quilibrium method must be defined in terms of solubility, which is either the Van't Hoff equation or user-supplied solubility data. t Design or Rating calculations in the Dissolver Calculation Mode ign mode, a specification is required and the volume is calculated particle size distribution and operating conditions. In Rating el volume is defined and the exit p

determined.

he mass transfer coefficient may be specified in the Dissolver Dissolution Rateindow. Alternatively, you may specify that the coefficient should be calculated

from diffusivity data entere Full details of the calculation meManual.


Excel Unit

General Information The Excel unit operation allows using Microsoft Excel spreadsheet files to model general unit operations in the flowsheet. During calculation, PRO/II transfers feed stream information to the spreadsheet, invokes a user-defined macro, then reads the resulting product stream information back into PRO/II. An Excel file usually contains several worksheets of information. One of these worksheets is used to exchange data between PRO/II and Excel. This data transfer worksheet has a specific format which is described below in the section Data Transfer Sheet. All other sheets in the workbook are ignored by PRO/II and can be used for any other purpose.

When PRO/II is installed, an "empty" Excel file (ExcelTemplate.xls) is installed which can be used as a starting point for developing custom spreadsheets.

Note: ExcelTemplate.xls does not perform any calculations.

A developer can copy and customize the spreadsheet by adding the required macros and/or spreadsheet formulas to calculate the output stream conditions based on the input feed streams and the unit operation data. After the spreadsheet has been customized, a user can add it to a PRO/II flowsheet using the Excel unit operation:

After starting PRO/II, select File/New from the menu. The PFD Icon palette is displayed.

Scroll to the bottom of the PFD palette, click the Excel button, and click an empty area of the flowsheet to add a new Excel unit operation.

Connect the required feed and product streams. Double-click the Excel icon to display the tabbed dialog box (see next

section Excel Configuration Dialog Box). This tabbed dialog box is used to specify the name of the Excel file, the name of the worksheet used as the data transfer area, and the name of the macro to invoke at calculation time.

After configuring is complete, click OK to exit the tabbed dialog.

After the flowsheet solves, PRO/II transfers feed stream information to the spreadsheet, invokes the user-defined macro, and then reads the resulting product stream information back into PRO/II.


The default text report that PRO/II generates includes the values of the Excel unit operation data arrays.

Limitations The Excel unit operation has the following limitations:

• The Excel macro cannot make any direct function calls back into PRO/II. through the data transfer sheet.

M Server functions to access data in the current flowsheet is not supported.

• The Excel spreadsheet is not stored in the .prz simulation file.

Excel Configuration Dialog Box hen the user double-clicks on the Excel unit icon, the following tabbed dialog

All communication with PRO/II is done • Use of the PRO/II CO

Wbox is displayed.

Figure9- d Dialog

se the main Excel Data Entry Window to specify the configuration and general

1: Excel Unit Tabbe

Uunit operation information. The window is organized into five tabs.


Spreadsheet Information: contains Excel configuration information.

ons: If checked, the state of the Excel spreadsheet is saved after PRO/II calculations.

name of the spreadsheet file. If no path is ust reside in the same directory as the

is "Sheet1". • Macro name: Specify the name of the macro to invoke by PRO/II during

"Macro1". eger data array similar to the "Integer

Data" grid in the generic "User-added Unit Operation". This data is transferred to Excel during calculations; therefore, the values can be used to supply additional data to the Excel spreadsheet. A user can specify descriptions and values for this data.

is

DEFINE mechanism, which allows Excel spreadsheets to interact with controllers, MVC units, Optimizers, and the Case Study feature. This data is transferred to Excel during calculations; therefore, the values can be used to supply additional data to the Excel spreadsheet. A user can specify descriptions and values for this data.

Double data: This tab contains a double-precision data array similar to the

"Supplemental Data" grid in the generic "User-added Unit Operation". This data is transferred to Excel during calculations; therefore, the values can be used to supply additional data to the Excel spreadsheet. A user can specify descriptions and values for this data.

Thermodynamics: This tab contains a drop-down list box that can be used

to select the Thermodynamic set for the unit operation. Note: This tab contains two text boxes that allow specifying a unit description

and the unit notes.

Data Transfer Sheet The worksheet used to transfer data between PRO/II and Excel has a specific format as described in the following table. The Column and Cell identifiers assume that the spreadsheet is configured to support five feed streams and five product streams. If the spreadsheet is modified to increase or decrease this

• Display Excel during calculations: If checked, Excel is displayed when invoked by PRO/II. If unchecked, Excel executes in 'hidden' mode.

• Save Excel file after calculati

• Spreadsheet name: Enter thespecified, then the Excel file mPRO/II simulation file.

• Worksheet name: Specify the name of the worksheet in the Excel file that is used as the transfer area. The default value

calculations. The default value is Integer data: This tab contains an int

Parameter data: This tab contains a double-precision data array similar tothe "Real Data" grid in the generic "User-added Unit Operation". Thdata is accessible via PRO/II's SPEC/VARY/


number, then the actual cells for the rows highlighted with an asterisk (*) change ccordingly. For example, increasing the number of feed streams to 6 changes

n corresponding to the first product stream from column H to column I.

athe colum

Column or Cell * Contents

D2 At calculation time, PRO/II fills this cell with the number of components in the simulation.

F2 Maximum number of feed streams supported by the spreadsheet. At calculation time, PRO/II reads this value to insure that the number of actual feed streams is less than or equal to the numbof columns reserved in the spreadsheet. PRO/II does

er not change

this value. This value must match the number of 'blue' columns used to store feed stream information. If a user customizes the

mber spreadsheet to add one or more blue columns, then this numust be increased to match.

H2 Maximum number of product streams supported by the

f duct stream information. If a

user customizes the spreadsheet to add one or more yellow

spreadsheet. At calculation time, PRO/II reads this value to insurethat the number of actual product streams is less than or equal to the number of columns reserved in the spreadsheet. PRO/II does not change this value. This value must match the number o'yellow' columns used to store pro

columns, then this number must be increased to match.

J2 Number of rows (starting with row 5) reserved for bulk streamproperties. At calculation time, PRO/II reads this number to determine in which row to begin writing stream compositions. PRO/II does not modify this value.

W4 * Number of additional parameters to be included in the text reAt report time, PRO/II reads this val

port. ue to determine how many

additional data items in columns V and W will be written to the rt. output repo

C5:G24 * At calculation time, PRO/II fills this range of cells with feed streaminformation. The number of columns is defined by cell F2; the maximum number of rows is defined by J2.

C25:Gnn * At calculation time, PRO/II fills this range of cells with component rate information of the feed streams. The number of columns is defined by cell F2; the number of rows is defined by D2. The values are expressed in PRO/II internal units-of-measure.



H5:L24 * At calculation time, the spreadsheet fills this range of cells with product stream information. The number of columns is definedcell H2; the maximum number of rows is defined by J2.

by

H25:Lnn At calculation time* , the spreadsheet must fill this range of cells nent rate information of the product streams. The columns is defined by cell H2; the number of rows is

l

with componumber of defined by D2. The values should be expressed in PRO/II internaunits-of-measure.

, O * At calculation time, PRO/II will write values to columns M and O. Column M will contain the names of the unit operation Integer (INT) attributes as defined in the Unit Operation Data Definition (.ini) file; column O will contain the current values. After the spreadsheet macro is complete, the updated values in colum

M

n O will be returned back to PRO/II.

P, R ter

sheet macro finishes, updated values in column R are

returned back to PRO/II. Values are transferred in the units-of-n file.

* During calculations, PRO/II writes values to these columns. Column P contains the names of the unit operation Parame(PAR) attributes defined in the Unit Operation Data Definition (.ini) file. Column R contains their current values. After thespread

measure specified in the [UOM] section of the Data Definitio

S, U

current values. After the

* During calculations, PRO/II writes values to these columns. Column S contains the names of the double-precision (DBL) attributes as defined in the Unit Operation Data Definition (.ini) file. Column U contains theirspreadsheet macro ends, updated values in column U are returned back to PRO/II. Values are transferred in the units-of-measure specified in the [UOM] section of the Data Definition file

V s.

ber in cell W4.

* Contains the descriptions of the attributes that are included in thePRO/II default text report. PRO/II does not change these valueThe number of descriptions and values included in the PRO/II report is specified by the num

W * Contains the values calculated by the spreadsheet macros and/orformulas. PRO/II does not change these values. When generating the default text report, PRO/II will include the descriptions from column V and values from column W in the text report. The number of descriptions and values included in the report is specified by the number in cell W4.



X, Y or between input and internal units of

measure. Normally this value is not required because PRO/II

* Column X contains the list of unit-of-measure classes. Column Y contains the conversion fact

writes all values to the spreadsheet in the same units-of-measure regardless of the units-of-measure selected in the input file. For details on the unit-of-measure classes, refer to the PRO/II User-Added Subroutines User Guide.

* The afeeds and products. Changing the number of feeds or products changes the

ctual column used for this data depends upon the declared number of

column correspondingly. As delivered, the unit has 5 feeds and 5 products. AdditioThe Exccapabiliof the Modula s can

ames and full support for units-of-measure. • Custom tabbed dialog box. • Custom icon on the PFD palette.

To perform these modifications, refer to the PRO/II User-Added Subroutines

er Guide.

nal Customization el unit operation in PRO/II provides generic data attributes and GUI

ty. It is possible to perform additional customization using the capabilities r User-Added Unit Operations. Specifically, the following item

be customized:

• Custom Data attributes n

Us


Expander

General Information

to model any isentropic expansion such as

eeds and Products

uct stream is automatically set by PRO/II. ders with two or more product streams, the product phases must be

specified in the Expander Product Phases window which is accessed by clicking Product Phases… on the Expander main data entry window. Allowable product phases include: vapor, liquid, decanted water, heavy liquid, and mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with apor and liquid products and is not allowed when four product streams are pecified.

indow. A pressure or work cification is required for every expander. Options are as follows:

• Outlet pressure • Pressure ratio (absolute outlet pressure/absolute inlet pressure) • Pressure drop • Work

ce in percent may also be defined for convergence of work

pecifications. If none is given, a default value of 0.001 percent is used.

The Expander operation may be usedan expander unit in a natural gas processing plant or a steam turbine, etc. Adiabatic expansion efficiency may be applied to the calculations. Rigorous calculations may be performed for both VLE and VLLE systems. FAn expander operation may have multiple feed streams, in which case the inlet pressure is assumed to be the lowest feed stream pressure. An expander may have one or more product streams. The product phase ondition for operations with one prodc

For expan

vs

Pressure and Work Specifications The outlet conditions for an expander may be selected with the radio buttons provided on the Expander main data entry wspe

A relative tolerans


Adiabatic Efficiency The isentropic work is adjusted by application of the adiabatic efficiency supplied in the Expander window. When not supplied, a default value of 100 percent is used (perfect isentropic expansion).

inimum Outlet Pressure ifications, a minimum outlet pressure may

er main data entry window. The work will be reset as needed so this minimum pressure is not violated.

utlet Temperature Estimate An estimate for the outlet temperature may be optionally supplied in the Expander main data entry window to speed the calculations.

Thermnder calculations

may be selected by choosing a method from the Thermodynamic System drop-dow is

MFor expanders with work specoptionally be defined in the Expand

O

odynamic System

The thermodynamic system of methods to be used for expa

n l t box on the Expander main data entry window.


Flash

General Information

he Flash unit may be used to model any equilibrium calculation where two of e conditions are defined, e.g., temperature and pressure, pressure and nthalpy, etc. The phase equilibrium is determined and the product may be eparated into product streams corresponding to the phases. The duty required, any, to bring the feed to the final conditions is also reported. Both VLE and LLE calculations are supported by this unit.

eeds and Products flash operation may have multiple feed streams, in which case the inlet ressure is assumed to be the lowest feed stream pressure.

flash may have one or more product streams. The product phase condition for ash operations with one product stream is automatically set by PRO/II. For flash

or more product streams, the product phases must be specified in e Flash Product Phases window which is accessed by clicking Product

s… on the Flash main data entry window.

ct phases allowable include: vapor, liquid, decanted water/second liquid, nd mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with

d liquid products and is not allowed when four product streams are pecified. Note that for Dew Point and Bubble Point calculations, only two roduct phases are allowed, vapor and liquid. The optional liquid product from a

Dew Point calculation corresponds to a pseudo-stream with the equilibrium liquid omposition and the optional vapor product from a Bubble Point calculation orresponds to the equilibrium vapor composition.

irst Specification he temperature, pressure, or pressure drop from feed conditions is supplied by hoosing the appropriate drop-down list box on the Flash main data entry window nd supplying the value in the data entry field provided. Only one entry is llowed.

TthesifV FAp Aflunits with twothPhase Produavapor ansp

cc FTcaa


Second Specification This specification is used in conjunction with the First Specification given above to define the equilibrium calculation desired. The Second Specification may be

ither a Unit Specification or a Product Specification as denoted by the radio buttons on the Flash main data entry window. These two types of specification

w.

abatic (duty defined) flash. When the lied as the primary specification, the pressure is

ied is calculated by PRO/II.

Dew Point: The dew point pressure for the hydrocarbon portion of y

rimary specification. ned when the pressure or pressure

ification. This option is only e.

e

are discussed separately belo Unit Specification The desired second specification is chosen with the drop-down list box and the data entry supplied in the field provided. Options are: Pressure Drop or Pressure: These entries are only applicable when the

temperature is chosen as the primary specification and correspond to an isothermal (constant temperature and pressure) flash. The Duty required to bring the feed to the specified conditions is calculated by PRO/II.

Duty: This entry corresponds to an adi

temperature is suppcomputed. When the pressure or pressure drop is supplied as the primary specification, the temperature is computed. The duty may be positive (heating), negative (cooling), or zero (constant enthalpy calculation).

Dew Point: The dew point pressure is computed when the temperature is

supplied as the primary specification. The dew point temperature is determined when the pressure or pressure drop is provided as the primary specification. The Duty required to bring the feed to the specifconditions

Hydrocarbon

the stream is computed when the temperature is supplied as the primarspecification. The dew point temperature is determined when the pressure or pressure drop is provided as the primary specification. This option is only applicable for thermodynamic systems which support a free water phase. The Duty required to bring the feed to the specified conditions is calculated by PRO/II.

Water Dew Point: The dew point pressure for the water portion of the stream is

computed when the temperature is supplied as the pThe dew point temperature is determidrop is provided as the primary specapplicable for thermodynamic systems which support a free water phasThe Duty required to bring the feed to the specified conditions is calculated by PRO/II.


Bubble Point: The bubble point pressure is computed when the temperature is supplied as the primary specification. The bubble point temperature is determined when the pressure or pressure drop is provided as the primary specification. The Duty required to bring the feed to the specifiedconditions is calculated by PRO/II.

entropic: A constant entropy flash is calculated from feed conditions to final e product pressure is computed when temperature is given

y specification. The product temperature is given when the

e he

roduct Specification utton is selected, the pressure is computed when the

uty

rings

r

upplied. Note that a default relative tolerance of 0.02 is used if none is given.

ntrainment ntrainment from one phase to another phase is requested in the Flash Drum

Entrainment dialog. Access that window by clicking Entrainment… on the Flash ain data entry window. Users must identify the From and To phases, and

pecify the quantity of entrainment as either (a) the fraction or percent of the onor phase, or (b) the absolute rate of material. The entrained material has the

same composition as the donor phase. Since entrainment calculations are performed after the flash calculations, the resultant products may be different from the original flash specifications. Multiple entrainments are permitted.

Isconditions. Thas the primarpressure or pressure drop is given as the primary specification. The Duty required to bring the feed to the specified conditions is calculated by PRO/II.

Upper Dew Point: The Upper dew point pressure is available only when the

temperature is chosen as the primary specification. This option is applicable for Vapor Liquid Equilibrium phases where a retrograde condensation region occurs. This option computes the upper dew point pressure if a temperature above the critical temperature and below thcricondentherm is supplied. The Duty required to bring the feed to tspecified conditions is calculated by PRO/II.

PWhen this radio btemperature is provided as the first specification such that a calculated stream parameter meets a specified value. When the pressure or pressure drop is supplied as the first specification, the temperature is computed. The Drequired to bring the feed to the final conditions is also calculated by PRO/II. The stream parameter specification is entered by clicking on the hypertext stand uses the general PRO/II specification format. This format is further described in the SPEC/VARY/DEFINE section of this chapter. The stream parameter specification must correspond to one of the flash unit products and may be eithean absolute or relative value. An absolute or relative tolerance value may also be s EE

msd


Temperature or Pressure Estimates

at

n is the pressure

seudo-stream Flow Rate o-product, and Bubble Point

lthough these pseudo-products are imaginary flows (they have actual rates of zero), they include all other equilibrium properties, such as temperature, pressure

sition. The pseudo-products are useful because other unit operations re able to reference their data and use it for other purposes, such as formulating

.

The rate (actually, an imaginary pseudo-rate) of a pseudo-stream may be supplied in the data entry field provided on the Flash main data entry window. This allows computing the property values of the imaginary phase based upon a seful flow rate datum. However, care must be taken to ensure that pseudo-

articipate in the

Thermodynamic System

he thermodynamic system of methods to be used for flash calculations may be elected by choosing a method from the Thermodynamic System drop-down list

Estimated temperatures or pressures may be supplied in the data entry boxesthe bottom of the Flash main data entry window. These estimates are optional, with a temperature estimate relevant when the first specificatioor pressure drop, and a pressure estimate relevant when the first specification isthe temperature. They do not apply to isothermal flash calculations. PDew Point calculations allow an optional liquid pseudcalculations allow an optional vapor phase pseudo-product. These are virtual streams that are in phase equilibrium with the dew vapor or bubble point liquid, respectively. A

and compoaSpec, Vary, and Define constructs

ustreams having non-zero rates neither feed other units nor pflowsheet material and energy balances.

Tsbox on the Flash main data entry window.


Flash With Solids

GenerThe t stream. I ent, you must use the Flash with Solids unit rather than the conventional Flash unit operation. F

Flash with ssure is assumed to be that of the feed stream with the lowest pressure.

• A solid phase bottom stream from the separator section. The default is , there

The bottominternaluser. T is identical to that of th is requirPRO/II and may be reviewed in the s window accessible via th main data entry window. For furthdiscussi (page 240, seq.).

al Information Flash with Solids unit models a flash drum unit operation with a solid produc

f a solids product stream is to be pres

eeds and Products Solids unit may have multiple feed streams, in which case the inletA

pre

A Flash with Solids unit typically has four product streams:

• A vapor phase overhead stream from the flash drum section. • A liquid phase stream from the flash drum section. • A decanted water/second liquid from the solids separator section.

complete separation of the solid from the fluid stream and, henceis no required input data for this unit.

s stream from the flash drum section feeding the solids separator is to the Flash with Solids unit and is not subject to specification by the

he main data entry window for the Flash with Solids unit e ordinary Flash unit except that no specification of product phases by the user

ed. The phases for the product streams are automatically specified by ct PhaseFlash Produ

e Product Phases… button on the Flash

er instructions on unit and product specifications, see the detailed ons in the Flash section above


This

page intentionally is left blank.


Flowsheet Optimizer

General Information The Flowsheet Optimizer maximizes or minimizes an objective function by varying one or more flowsheet variables while meeting a number of

mum riables. The objective function may be an operational

riterion, such as maximum recovery or minimum loss, or an economic criterion, such as maximum profit or minimum cost. In order to optimize an economic

nction, you must first include a Calculator in the flowsheet in order to define the rofit or cost. Then use the Optimizer to minimize or maximize the Calculator

result.

Objective Function ither you must choose either Maximize or Minimize as the objective function by electing the appropriate radio button in the main Optimizer window. Enter the bjective function by clicking the linked text string Parameter in the Objective unction field to make the Parameter window available selecting the unit or tream parameter to use as the Objective Function. This Parameter window is

similar to the SPEC Parameter window, except that there is no entry allowed for e parameter value and tolerance. The Objective Function may be a single

owsheet parameter or a mathematical expression that relates two flowsheet parameters. Variables The optimizer variables (VARY’s) are selected by clicking the linked text string Parameter in the Variables grid of the Optimizer main data entry window. In the Parameter window, designate the stream or unit parameter that will be varied, selecting from the same choices given above for the Objective Function. For unit or stream variables, you must also input minimum and maximum values. The SPEC/VARY/DEFINE section of this chapter gives more information on the VARY concept. The tables in that section list the flowsheet variables that may be used for SPEC’s and VARY’s for flowsheet optimizer units.

specifications. Optionally, you can place constraints on minimum and maxivalues on the flowsheet vac

fup

EsoFs

thfl


Variable Step Sizes and Limits You may enter limits on the step size for each control variable. Click the linked text string default step sizes in the main Optimizer window to open the Variable Step Sizes window. You may enter a relative minimum step size and/or absolute maximum step size per iteration in this window. You may also enter a non-default step size used to calculate the derivative in this window. The default relative step size depends on the Optimizer scaling option selected (see the section following titled Scaling of Optimization Variables). Alternatively, a user-supplied step size can be used in the calculations. The alternative step size may be sized on either a relative or absolute basis by selecting the appropriate radio button. Specifications Specifications (SPEC’s) may be entered for flowsheet parameters other than the

s

the parameters for each Specification by clicking the appropriate text strings in nked text string Parameter, to open the Parameter the unit or stream parameter to use as the SPEC.

The SPEC may be a single flowsheet parameter or a mathematical expression that relates two flowsheet parameters. Next, enter the value and the default

Constraints may also be entered for flowsheet parameters other than the control variables. Constraints limit a variable to a specified range. Click Constraints… on the main Optimizer window to open the Constraints window from the

PEC/VARY system. Check the Use Constraints box to enable the constraint grid. Enter the parameters for each Constraint by clicking the appropriate text strings. Click the hypertext string Parameter to open the Parameter window

iate text strings.

control variables. Click Specifications… on the Optimizer main data entry window to bring up the standard Specifications window. Check the Use Specificationbox to enable the grid which contains the standard specification linked text. Enter

each specification. Click the liwindow where you can select

tolerance for the SPEC by clicking on the appropriate text strings. See the SPEC/VARY/DEFINE section of this chapter for details on the generalized SPEC form. Constraints

S

where you can select the unit or stream parameter to use as the Constraints. Theuse of this window is analogous to the Parameter window used in selecting the SPEC above. The Minimum Value, Maximum Value, and the default tolerance alues for the Constraints are entered by clicking on the approprv


Calculation Options Number of Calculation Cycles Several options regarding the operation of the Optimizer may be specified by clicking Options… on the Optimizer main data entry window.

Scaling of Optimization Variables y default, Optimizer scales the optimization variables in the convergence

algorithm. This scaling can be suppressed by deselecting the Use Scaling box on

he derivative step size that appears on the V reased from 2 percent to 5 percent. Ov lThe default value for the overall error in any variable is 10-7. You may enter a diffe n or in the corresponding data entry field in the Options

bjective Function

ow. Select e is Updated

ormally, the first unit operation in the calculation sequence that is affected by e control variable is the next unit calculated after the control variable is

updated. Normally, this is determined automatically by the program. However, you must specify the next unit calculated whenever any optimization constraint or variable is a thermodynamic parameter. Specify the return unit by selecting the desired unit from the drop-down list box on the Options window.

The default for the number of calculation cycles is set by PRO/II as 18 plus the current number of variables. Alternatively, you may specify the number of cycles by selecting the appropriate radio button on the Options window.

B

the Options window. If scaling is not selected, the default value of t

ariable Step Sizes window is inc

era l Error in any Variable

re t value for the overall err window.

Minimum Relative Change in OThe default value for the Minimum Relative Change in the Objective Function from one calculation cycle to the next is 0.005. You may enter a different value for the minimum relative change in the box on the Options wind

ing the Next Unit Calculated After Control VariablNth


Type of Thermodynamic Method The PRO/II Optimizer currently supports the use of both Rigorous and Local Thermodynamic Models during the perturbation steps. Specify the

ermodynamic model by selecting one of the following options in the Type of own list box:

e tives.

Local Taxi Model This option specifies that PRO/II will generate local K-value models for T, P, and Liquid and Vapor composition derivatives.

Advanced Options he Optimizer Advanced Options are intended for experienced users of PRO/II. If

ecified Number own list box enables this feature.

dating reater

thThermodynamic Model drop-d

Rigorous This option specifies that PRO/II will use rigorous thermodynamic calculation models. This is the default selection.

Local TP Model This option specifies that PRO/II will generate local K-value models for T and P derivatives.

Local TPx Model This option specifies that PRO/II will generate local K-valumodels for T, P, and Liquid composition deriva

Tyou are unsure how these features may apply to your simulation, consult SIMSCI Technical Support or refer to the PRO/II Reference Manual.

Click Advanced Options... to specify additional options for the Optimizer.

Special Line Search Logic This option enables a line search mode method for optimization calculations. By default, this feature is Off. The option Spof Trials in the drop-d

When this feature is enabled, you may specify the maximum number of line search trials for any one optimizer cycle. The number must be a positive integer no greater than 20.

Number of Independent Variables to Eliminate This allows specifying the number of independent variables to eliminate during the solution of the optimizer calculations.

Start Broyden Updating at Cycle This allows specifying the optimization cycle at which Broyden Upbegins. By default, this option is Off. Specify a positive integer gthan 1 to enable this feature.

Derivative Analysis By default, this option is Off. Select On in the drop-down list to produce an analysis printout of the derivative step sizes for each optimizer cycle; in addition, a modified perturbation step size will be suggested, if appropriate.


Limit Optimization Step Sizes By default, this option is Enabled (Yes). When enabled, this option limits thestep sizes taken by the optimizer to 30, 60, and

90 percent of the upper or

lower bounds during optimization cycles 1, 2, and 3, respectively. This is

nds. For maximization problems, a positive shadow price indicates that the constraint is being pushed against its upper bounds, a negative shadow price indicates that the lower bound is still active, and a zero shadow price indicates that the constraint does not affect the solution By default, printout of these values is disabled (the None option in the Separate Shadow Price Output File drop-down list box).

Brief This option produces a separate output report with the same file

name as the input file (with a .shd extension). This report contains the IDs of the variables, specifications, and constraints, along with their corresponding shadow prices as part of the standard output report.

All This option produces a separate output report with the same file

name as the input file (with a .shd extension) containing a detailed summary of the final Optimizer solution. This summary includes the values of the objective function, all variables, specifications, and constraints, along with the shadow prices for all active bounds and constraints.

Complete technical details may be found under the topic Flowsheet Solution Algorithms in the PRO/II Reference Manual.

intended as a safety feature to prevent the Optimizer from moving too far, particularly when the derivatives are inaccurate. Selecting No in the drop-down list box disables this feature.

Separate Shadow Price Output File Once the flowsheet optimization has converged and the appropriate operating conditions have been determined, the shadow prices or Lagrange multipliers can be used to assess the sensitivity of the objective function to the specifications, onstraints and bouc


Print Results for Flowsheet Optimizerhe default is to suppress printing of a co

nvergence report. Click Print Options…

n the main Optimizer window to open the Print Options window. Select the desired printout level from a drop-down list that includes the print levels History, Brief, and All. By default, no intermediate printout is produced. Print-out levels for intermediate printout of derivative and/or variable values can be selected from a drop-down list

None, Print after each cycle, or Print after the final

a plot of the onvergence diagnostics.

To

which includes the print levelscycle. The program limits the options for the variable printout selection such thatthe level of printout is greater than or equal to the derivative printout option. Select the Include Convergence Plots check box to generatec


Heat Exchanger, LNG

General Information The LNG Heat Exchanger simulates the exchange of heat between any number of hot and cold streams. The exchanger is divided into cells representing the individual cross-flow elements. Cells are designated as Hot, where the streams are cooled or as Cold where they are heated. The unit must contain at least one hot cell and one cold cell.

he number of cells is initially defined on the LNG Heat Exchanger Configuration

anger window.

multiphase product from a cell may be separated into streams containing one or more phase. The allowable product stream phases are vapor, liquid, decanted water, or mixed (vapor + liquid). A mixed phase product is not allowed with a vapor or a liquid product. The decanted water product is also used as the second liquid product phase with rigorous VLLE calculations. If a cell has more than one product stream, the phases must be allocated to the treams in the Product Phases window. This window is accessed via the Cell

Heat Exchanger window, then via the Product n LNG Heat Exchanger Cell Data window.

Any cell may have either a duty or an outlet temperature specification. However, at le t st remain unspecified. The product streams from all uns c hanger at the same temperature.

he pressure drop for each cell defaults to zero. Pressure drop values are d in the LNG Heat Exchanger Cell Data window. The thermodynamic

system used for the calculations for an individual cell may also be changed in this window.

Twindow that appears when the unit is first placed on the PFD. Cells may be added or deleted in the main LNG Heat Exch

Feeds and Products Each cell may have one or more feed streams. If multiple feed streams are defined, the mixed feed is flashed at the lowest feed stream pressure. A

sData… button in the main LNG Phases… button in the now ope Performance Specifications

as one cell mupe ified cells leave the exc

Cell Data Tentere


Zones Analysis Zones Analysis may be requested in the LNG Heat Exchanger Zones Awindow accessible via the Zones Analysis… button on the main data entry window. This feature allows internal temperature cros

nalysis

sovers and pinch points to e identified by dividing the exchanger into a number of zones. Warnings are

The Zon ormally performed when the exchanger is alculated. However, if the exchanger is in a recycle, computation time may be

Zone A t calculation time if required by

ontroller specifications on the LNG heat exchanger.

Print OThe Pri is opened via the Print Options… button on the main ata entry window. A number of different Y versus X plots may be generated for

•

• ∆T vs. Duty

•

amic System stem of methods to be used for LNGHX calculations may

be selected by choosing a method from the Thermodynamic System drop-down list box on the LNG Heat Exchanger main data entry window.

Note: The thermodynamic system used for the calculations for an individual cell (specified in the LNG Heat Exchanger Cell data window) overrides this thermodynamic system for specific cells.

bissued if crossovers or pinch points are found.

es Analysis calculations are ncsaved by performing the analysis at output time.

nalysis will always be performed aC

ptions nt Options window

dtemperature, duty, and UA. The options are:

Temperature vs. Duty (default) • UA vs. Duty (default) • ∆T vs. Temperature (default)

• UA vs. ∆T Duty vs. Temperature.

ThermodynThe thermodynamic sy


Heat Exchanger, Air Cooled

General Information An Air Cooled Heat Exchanger (ACE) uses air as the cooling medium to remove heat from a process fluid. The process fluid is a stream that flows through the tube-side of the ACE through a tube bundle. Configuration options allow either

eating or cooling. The air side is analogous to the shell side of a shell-and-tube exchanger, but the air is propelled using fans. A forced draft configuration locates fans at the air entrance below the tube bundle. An induced draft configuration

The model allows a single (air side) bay that exchanges heat with one or more

options ed, all bund physical configuration. Tube-side options allow tube fins and tube-side nozzles.

he model executes in either rating (performance) mode or design (sizing) mode. The default rating mode computes heat transfer and other performance data based on a fixed exchanger configuration. It allows either none or one operating pecification. Design mode varies the physical dimensions of the exchanger to

with add figuration.

Feeds and Products oth the air side and the tube side of the exchanger require at least one feed

llowed) and at least one product stream (4 are allowed). All ts are declared using keyword input, or by laying them down

and connecting them to the ACE directly on the PFD window of the simulation. ACE data entry windows do no support configuring feed or product streams. The ACE model now supports ‘Air‘ as Utility stream. To use ‘Air’ as Utility, air side

orts need not be connected and also Air / Oxygen and Nitrogen need not be

specifieSpecifc ow and specify the Utility side specifications.

possibly IR could b

h

places the fans above the tube bundle at the air exit.

(process side) tube bundles configured in series, in parallel, or both. Tube side configure one tube bundle. When more than one bundle are configurles have the same

T

ssatisfy a performance specification. It requires exactly one operating specification

itional design constraints on the physical con

Bstream (10 are afeeds and produc

pdefined in the Component Selection DEW. Air as a Utility stream may be

d by unchecking the 'Air is a Process Stream' check box on the ation wind

The feed to the air side should deliver a process stream that represents air and

some contaminates or trace components. For example, component Ae present, or air could be represented by a mixture of nitrogen and


oxygen. However, there are no explicit constraints upon the composition of the

Feeds t n-solid) ph d feed is f

streamsdraw, si e more co s

re vapor, liquid, and mixed (vapor + liquid). A mixed phase product is not

active, aproductVLLE c

ry ow equirements. More complete information about

vailable options and modes of operation are available in the PRO/II Keyword

air side feed. Other mixtures that define other gaseous fluids are allowed. o the tube side may be any process streams that include a fluid (noase. When multiple feed streams are defined on either side, the mixelashed at the lowest feed stream pressure.

A multi-phase product from the exchanger may be separated into separate draw

containing one or more phases. The air side often takes a single product nce the air flow typically represents a utility. Multiple product draws armmon on the tube (process) side. The allowable product stream phase

aallowed with a vapor or a liquid product. When the water DECANT=ON option is

n additional decanted water draw is supported. The water decant also serves as the second liquid product phase when modeling rigorous alculations.

PRO/II Online Help provides extensive information about the various data ent

s and the input data rwindaManual. In the chapter titled “Air Cooled Heat Exchanger”.


Heat Exchanger, Rigorous

General Information

exchang etermine the

ase, the foul

ay be separated into streams

se with rigorous VLLE calculations.

e stre e Product Phases…

The cal eat xchanger window. The available options are:

Rating:efault.

ixed Duty: Determine the fouling factors and exit temperatures from the defined duty.

The Rigorous Heat Exchanger simulates the operation of an existing heat er. The geometry of the unit has to be defined and the unit is rated to

duty, exit temperatures, and pressure drops. d The exchanger duty, or one of the exit temperatures, may be defined. In this

ing resistance is calculated. c Feeds and Products Each side of the exchanger may have one or more feed streams. If multiple feedstreams are defined, the mixed feed is flashed at the lowest feed stream pressure.

multiphase product from the exchanger mAcontaining one or more phase. The allowable product stream phases are vapor,liquid, decanted water and mixed (vapor + liquid). A mixed phase product is not allowed with a vapor or a liquid product. The decanted water product is also used s the second liquid product phaa

If either side has more than one product stream, the phases must be allocated to

ams in the Product Phases window accessed via ththbutton in the Rigorous Heat Exchanger–Feeds and Products Data window. Calculation Type

culation type is selected from a drop-down list in the Rigorous HE

Determine the heat transferred with the defined area and fouling factors. This is the d

F


Tube Outlet Tempetemperature

rature: Determine the duty, fouling factors, and shell exit from the defined tube outlet temperature.

temperature from the defined shell outlet temperature. If the selected uty or

xcha ns

either hh t side on the Rigorous Heat Exchanger–

eed and Products Data window and supply the appropriate information in the

colum as one side of the exchanger and a rocess stream is defined for the other side.

Attached exchangers may be used to represent the condenser or reboiler for the rs, the

s

ine the duty required to

he overall configuration is defined in the Rigorous Heat Exchanger window by ntering one or more of the configuration parameters:

• Number of Tubes/Shell • Area/Shell • Shell Inside Diameter

value for at least one of these parameters must be supplied. If any of these arameters is missing, it will be calculated from the others.

Shell Outlet Temperature: Determine the duty, fouling factors, and tube exit

calculation type is not Rating, a value must be supplied for the dexit temperature as appropriate.

ngers Attached to ColumEExchangers may be attached to any tray of a column for which a duty is defined,

eating or cooling. To attach an exchanger to a column, double-click o Column… for the shell or tubeAttac

Fwindow provided.

n internal stream is consideredAp

column, a pumparound, or side heater/cooler. For side heaters and coolecolumn stream may be the vapor or liquid from the tray to which the exchanger iattached, the vapor from the tray below, or the liquid from the tray above. If the Calculation Type does not fix the exchanger duty or one of the outlet temperatures, the exchanger duty will be fixed by the column heater or cooler. It is generally best to allow the column operation to determmeet the defined performance. If the duty is fixed by an exchanger specification, it is considered a “fixed” duty for the column calculations. Overall Configuration Te

Ap


ConfiguraThe configur re defined in t rous Heat ExchaConfiguratio cessible uration… o entry wind this w have ult s:

hells in S i um f id l shel cteunit. Both shel b s ar sidere e piped in

e def l Number of Shells in Par his is the nu of identical shells connec

parallel in the unit. Both shell and tube re considere iin parallel. The default is 1 shell.

N e Passes This can be any integer value between 1 and16. The default is 2. Odd numbered values are allowed, but are not

d.

ch ta s from the drop list as either Horizontal or Vertical. The default is Horizontal.

e dire ui s ed fr he dro n lis

r Countercurrent or Cocurrent. The default is Countercurrent.

e ch ell and rear of thexchanger) are selected m drop-do n lists. The default is

Detail nger tubes are entered in the Rigorous Heat Exchanger Tube Data window which is a Tubes… e m ta e dow

default v

Length: e length includes the thickness of both tube-sheets. For inclu c f d t baf

length defaults to 20 ft (6.1 m).

: The tube outside d lmm).

T he tube thickness may be defined as: meter

kness

tion Data ation details an Data window ac

he Rigo via Config

nger n the main data

ow. All data in indow defa value

Number of Sseries in the

eries: This s the nl and tu

ber oe side

enticae con

ls conned to b

d in

series. Th ault is 1 she l.

allel: T mber sides a

ted inped d to be p

umber of Tub /Shell:

recommende

Orientation: The ex anger orien tion is elected -down

Configuration: Theithe

ction of fl d flow i select om t p-dow t as

TEMA Type: The thre aracters for the TEMA type (front, sh e

separately fro wAES.

Tube Data s of the excha

ccessed via on th ain da ntry win . All tube data have

The nominal tub

alues.

U-tubes, it The

des the thi kness o the tube sheet an he last fle.

Outside Diameter iameter defau ts to 0.75 inches (19.05

hickness: T

Inside DiaWall ThicBWG


Bare tubes default to an inside diameter of 0.58402 inches (14.834 mm). Finned tubes default to an inside diameter of 0.49598 inches (12.573 mm).

Pitch: The center-to-center distance between tubes d to 1 (2

mm).

d from the drop-down list. The options are Triangular–30 D uare–90 es (default), Rotated

60 D d ed Square– egree

he tube sheet t ss is calculated if it is not supplied Fin Data The default is not to have finned tubes. If fins are specified, the surface area may

r c o in Extended Surface Area: the u are e tub ludin

finned and bare s are al tere re, overrid s the calculated area.

Fins/Inch: This is the number of fins per inch of tube length. (Default is 19).

qual to 0.5/ (Fins pInch).

H Above Root: The fin height above the root defaults to a value equal to utside D R m 2.

he ro r u t the of the

it defaults to 0.625 inches.

Baffle Data Details of the exchang e s Heat Exchanger Baffle Data window accessible via Baffles… on the main data entry window. All baffle data have defaul

affle Type: The type is selected from the drop-down list. The options are No Baffles, Single (default), Single Baffles - No Tubes in Window and Double.

affle Geometry Data: The baffle cut is the height of the window divided by the shell inside diameter and it defaults to 0.2. Alternatively, the Net Free Area Ratio may be entered instead. This is the area of the window divided by the cross-sectional area of the shell.

efaults .0 inch 5.4

Pattern: The tube pattern is selecte

egrees, Sq DegreTriangular–

egrees, an Rotat 45 D s.

Sheet Thickness: T hickne .

be entered directly o alculated fr m the f data.

This isurface

total sas. A v

rface ue en

a of thd he

es ince

g the

Thickness: The fin thickness defaults to a value in inches e er

eight

(Tube O iameter - oot Dia eter)/

Root Diameter: Tand

ot diamete is the t be diameter a base fins

er baffles ar entered in the Rigorou

t values.

B

B


Center Spacing: If a value is not supplied, the baffle center-to-center spacing is

efined and the value will be calculated to provide even spacing.

Inlet Spacing: This is the center-to-center spacing between the tube sheet and the inlet baffle. If the inlet spacing is not supplied, it is calculated to meet the center spacing or, if no center spacing is defined, it defaults to 5 inches (133 mm) for bare tubes or 3 inches (88 mm) for finned tubes.

Outlet Spacing: This is the center-to-center spacing between the tube sheet and

the outlet baffle. If the outlet spacing is not supplied, it is calculated to meet the center spacing or, if no center spacing is defined, it defaults to 5 inches (133 mm) for bare tubes or 3 inches (88 mm) for finned tubes.

Thickness: If a value is not supplied, the baffle thickness defaults to 0.1875 inches (4.763 mm).

Number of Sealing Strips: This is the number of pairs of sealing strips per

cross-flow pass. It defaults to zero.

il Cilm Coefficient Data are entered in the Rigorous Heat Exchanger Film

via Film Coefficients… on the main data djustment factors and override values for the

sed in the calculation. The default is 50 Btu/hr·ft ·°F (244.1 kCal/hr·m2 021.9 kJ/hr·m2 ·K).

Overall U-value Scale Factor: This is a multiplier which is applied to all calculated heat transfer coefficients. It can be used in order to match plant data more closely. It defaults to 1.0.

calculated by default to be 0.2*(Shell Inside Diameter). Any value entered will be ignored if both Inlet Spacing and Outlet Spacing are d

F m oefficient Data FCoefficient Data window accessibleentry window. These data provide aheat transfer parameters. Overall U-value Estimate: This is the initial value for the heat transfer coefficient

u 2

·°C or 1


Tubeside and Shellside Data The following items have separate entries for each side of the heat exchanger. Scale Factor: This is a multiplier which is applied to the film coefficient for the

xchanger. It defaults to 1.0.

Coefficient: If a value is entered, it overrides the calculated film coefficient for the specified side.

Fouling Resistance: Thermal fouling resistance defaults to 0.002 ft2 ·hr·°F/Btu

(0.00041 m2 ·hr·°C/kCal or 0.00010 m2 ·hr·K/kJ). If a duty or exit temperature is specified, the fouling will be calculated.

kness of the fouling layer may be entered to model re drop. The default value is zero.

rop data are entered in the Rigorous Heat Exchanger Pressure Drop ata window accessible via Pressure Drop… on the main data entry window.

side or the pressure rops may be overridden.

the

P / Unit: If a value is entered, the pressure drop for the exchanger unit

fault) for the Bell-Delaware method or Stream for the stream analysis technique.

specified side of the e

Fouling Thickness: The thic

its effect on the pressu Pressure Drop Data Pressure dD These data provide adjustment factors and override calculated values for the pressure drops. All data may be defaulted. By default the pressure drops are calculated for each side of the exchanger. A scale factor may be applied to the calculated value for eitherd DP Scale Factor: This is a multiplier which is applied to the pressure drop for

specified side of the exchanger. It defaults to 1.0. DP / Shell: If a value is entered, the pressure drop per shell overrides the

calculated pressure drop for the specified side. D

overrides the calculated pressure drop for the specified side. Shellside Pressure Drop Method: The method may be selected from Bell

(de


Print Options Additional output reports are selected in the Rigorous Heat Exchanger Print Options window accessible via Print Options… on the main data entry window. Extended: By default, a standard TEMA data sheet is produced for the

exchanger. Checking the Extended check box produces an additional data sheet with information about stream properties, heat exchanger configuration and hydrodynamics.

ones: Checking the Zones check box produces an additional table showing the

phase and zone boundaries used to calculate the duty-averaged log-mean-temperature difference.

ones Plot: Checking the Zones Plot check box produces a plot showing the

phase and zone boundaries used to calculate the duty-averaged log-mean-temperature difference.

Material Data

Exchan Materials…entry window. The default material is carbon steel. A different material may be selected from a

rop-down list which shows the materials in the library. Individual properties of the selected material may be overridden. Alternatively,

ame

Z

Z

Tube and shell material property data are entered in the Rigorous Heat ger Material Data window accessible via on the main data

d

the user may select User-added Material from the list and then supply the nand properties of the material. The list of materials in the library is tabulated below.


Heat Exchanger Materials of Construction

Material Density Conductivity

Description Label lb/ft3 kkg/ 3

Btu/ kCal/ W/m.K m hr.ft.°F hr.m.°C

Carbon Steel CARB STL 490.8 7862 30.0 44.6 51.9

Carb -m0 ,

7900 29.0 43.2 50.2 on oly Steel CARB MLY 493.2.1C 0.5Mo

Chro -1 r,

0.1 7851 27.0 40.2 46.7 me moly Steel CHRM 49.0C 0.5Mo MLY

Low C ro2.25C

h me Steel r, 1.0Mo

LOW CHRM

487.0 7801 25.0 37.2 43.3

Medium Chrome Steel 5.0Cr, 1.0Mo

MED CHRM

480.7 7700 21.0 31.2 36.3

Straight C STR CHRM 487.0 7801 14.0 20.8 24.2 hrome Steel 12Cr

304 Stainl18Cr, 8N

501.1 8027 9.3 13.8 16.1 ess Steel i

304 S.S.

310 Stai25Cr, 20

nless Steel Ni

310 S.S. 501.1 8027 7.8 11.6 13.5

316 Stai17Cr,

nless Steel 12Ni

316 S.S. 501.1 8027 9.4 14.0 16.3

321 Stainl 2 7916 9.2 13.7 15.9 ess Steel 321 S.S. 494.18Cr, 10Ni

Aluminum 1060 H14 A1060H14 170.0 2723 128.3 190.9 222.1

AluminumAnneale

1100 d

A1100 AN 169.3 2712 128.3 190.9 222.1

AluminAnnea

um 3003 H14 led

A3003H14 171.1 2741 111.0 165.2 192.1

Aluminum 3003 H25 led

A3003H25 171.1 2741 111.0 165.2 1Annea

93.1

Aluminum 6061 T4 red

A6061 T4 169.3 2712 95.0 141.4 Tempe

164.4

AluminumTempe

4 6061 T6 red

A6061 T6 169.3 2712 95.0 141.4 164.

Copper COPPER 556.4 8913 225.0 334.2 389.4


Heat Exchanger Materials of Construction

Material Density Conductivity

Description Label lb/ft3 kkg/ m3

Btu/ hr.ft.°F

kCal/ hr.m.°C

W/

m.K

Arsenical Copper AS COPPER 560.0 8970 187.0 278.3 323.6

Copper Nickel 90/10 CUNI9010 559.0 8954 26.0 38.7 45.0

Cop 38.1 per Nickel 80/20 CUNI8020 558.5 8946 22.0 32.7

Copper Nickel 70.30 CUNI7030 585.0 9371 17.0 25.3 29.4

Copper Nickel 60/40 CUNI6040 554.7 8885 12.9 19.2 22.3

Red Brass 85Cu, 15Zn RED BRAS 546.0 8746 92.0 136.9 159.2

Admiralty Brass 71Cr, 28Zn, 1Sn

ADMRALTY

531.0 8506 64.0 95.2 110.8

Commercial Brass COM 529.0 847455Cu, 34Zn BRAS

67.0 99.7 116.0

Muntz Metal 60Cu, 40Zn

MUNTZ 524.0 8394 71.0 105.7 122.9

Aluminum Bronze 93Cu, 5Al

AL BRONZ 510.0 8169 48.0 71.4 83.1

Aluminum Brass 78Cu, 2Al

AL BRASS 520.0 8330 58.0 86.3 100.4

Nickel Annealed NICKEL 556.4 8913 45.2 67.3 78.2

Low Carbon Nickel Annealed

L CRB NI 554.7 8885 35.0 52.1 60.6

Monel Nickel 70Ni, 30Cu

MONEL NI 551.2 8829 14.5 21.6 25.1

Inconel 600 76Ni, 16Cr, 8Fe

INCNL600 525.3 8414 8.7 12.9 15.0

Titanium Grade 2 TITANIUM 281.6 4511 9.5 14.1 16.4


Nozzle Data The default nozzle type and sizes can be overridden in the Rigorous Heat Exchanger Nozzle Data window accessible via Nozzles… on the main data entry window.

he default i to use conventional nozzles with calculated inside diameters. alculated pressure drop in the exchanger.

Outlet diameter may be entered.

indow to enter the

nozzle details. The required data are:

• Inlet and outlet annular-shell wall clearances

Thermodynamic System The thermodynamic system of methods to be used for each side of the rigorous heat exchanger may be selected by choosing a method from the Thermodynamic

ystem drop-down list box on the Rigorous Heat Exchanger main data entry indow.

T sNozzle data only affects the c Use Tube Side Nozzle or Use Shell Side Nozzle: If either check box is unchecked, the nozzle pressure drop will not be calculated for that side of the exchanger. Inside Diameter: The calculated diameters may be overridden. The Inlet and/or

Use Annular Shell Side Nozzles: If this box is checked, the pressure drop will

be calculated for annular rather than conventional nozzles. In this case,click Enter Data… to open the Annular Nozzle Data w

• Inlet and outlet annular passage lengths • Inlet and outlet groove areas

Sw


Heat Exchanger, Simple

eneral Information used to heat or cool a single process

stream, exchange heat between two process streams, or exchange heat etween a process stream and a utility stream. Rigorous calculations may be

a

or reference, streams and products are grouped according to the side of the exchanger as “hot” or “cold”, where the feed stream(s) on the hot side are cooled

The product from each side of an exchanger may be phase separated as desired into multiple product streams, where products may be liquid, vapor, mixed phase, and decanted water (hydrocarbon systems only). The “water” product stream may also be used to represent a second liquid phase for systems in which rigorous modeling of VLLE thermodynamics is considered.

Process Heat

e

ct Phases window accessible by clicking Product Phases… on the Heat Exchanger Process Streams window. Product phases allowable include: vapor, liquid, decanted water, heavy liquid, and mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with vapor and liquid products and is not allowed when four product streams are specified.

GThe Simple Heat Exchanger may be

bperformed for VLLE systems. It is also possible to attach an exchanger to any tray of a distillation column and exchange heat between a process stream andcolumn internal stream, either liquid or vapor. Feeds and Products F

and the feed stream(s) on the cold side are heated. Multiple process feed streams are permitted, with the lowest stream pressure used as the inlet pressure.

Feed and product streams are accessed via the Heat ExchangerStreams window which is opened by clicking Process Stream… on the Exchanger main data entry window. The product phase condition for units with one product stream is automatically set by PRO/II. For simple heat exchangerswith two or more product streams from a given side, the product phases must bspecified in the Produ


Utility Streams For simple heat exchangers with one process side, a hot or cold utility stream may be defined. The required utility rate for the specified heat transfer is always computed. Utility streams may be specified by clicking Utility Stream… on the Heat Exchanger main data entry window to access the appropriate hot or cold utility window. Cold utility streams are supplied in the Heat Exchanger Cold Side Utility window.

erature in and out must be supplied. Sensible heat transfer only.

Refrigerant: A designated component is vaporized at its saturation pressure or

ot utility streams are supplied in the Heat Exchanger Hot Side Utility window. Options are:

Steam: nsed at its sa tion temper ture or pressure. Latent

r only. Heating esignated component is cond d at its sa ation

or pressure. Lat heat transf nly. Config ta

ur pplied in the eat Exchan Configurat Data indow accessed by clicking Configuration… on the main data entry window.

These data only apply to exchangers with two sides and are optional for all ification is provided (see below).

s the number of tube passes is twice the number of shell

passes. The “FT” LMTD correction factor is computed based on a correlation for N -2N exchangers. Default is two tube and one shell pass, i.e., true countercurrent flow.

T Factor: The LMTD correction factor for the exchanger. Note that this entry is mutually exclusive with the Tube and Shell Passes.

Options are: Water: Temperature in and out must be supplied. Sensible heat transfer only. Air: Temp

temperature. Latent heat transfer only. H

Steam is conde tura aheat transfe

Medium: A d ense turtemperature ent er o

uration DaConfigw

ation data are su H ger ion

exchangers for which a Performance Spec Flow Direction: Countercurrent or cocurrent. Default is countercurrent. Tube and Shell Passes: When supplied, an N -2N configuration is alway

assumed, where

F


Performa cificaExchan specified in the Heat Exch er Specifications window pecifications… the main da entry window. Exchan may be specif d in a variety of ways:

Outlet T perature out f r hot or cold p ess fluid. Temperature Approa changers only

• Hot out minus cold out. • inus cold in. • HICO: Hot in minus cold out. • Minimum: Smaller of HOCI and HICO. • perature Approach (MITA): Minimum internal

sed on a zones analysis for the exchanger.

Duty: Overall heat transfer duty for the exchanger.

Outlet Strea The liquid fraction for the hot or cold side exit e 1.0 indicates bubble point and 0.0 indicates dew point

Degree he degrees of superheat (above the dew point) for the

Degrees o rees of subcooling (below the bubble point) for the hot or cold side exit fluid.

Overall Heat Transfer Coefficient (U): The area is calculated from is entry d. When both U and Area are given, the heat transfer is

satisfy the U*Area d no other ance s cifications for the exchanger.

Exchan rall heat tran efficien r the excha er is n ot supplied. When both U and Area are

fer is computed to satisfy the U*Area and no other performance specifications are allowed for the exchanger.

UA Specification: The product of overall heat transfer coefficient and

values for the overall heat transfer coefficient and exchanger area may be supplied directly.

Maximum U *Area: A maximum U*Area may be supplied to limit the heat f ped UA

nce Spe tions ger performance is ang accessed via Sger performance

onie

ta

emperature: Tem o rocch (Two-sided ex

HOCO:

)

HOCI: Hot out m

Minimum Internal Temapproach ba

m Liquid Fraction:fluid wherconditions.

s of Superheat: Thot or cold side exit fluid.

f Subcooling: The deg

thwhen not suppliecomputed toare allowed

an perform pe

ger Area: The ove sfer co t fo ngcalculated from this entry whegiven, the heat trans

n

Lumpedexchanger area may be supplied directly.

Individual U and Area Specification: Individual

transfer otherwise determined by a performance specification inecessary. This specification is not allowed when either a Lumspecification or the exchanger overall U and Area have been supplied individually.


Zone AnaZone ana

lysis lysis is requested by clicking Zones Analysis… on the main data entry

window. The duty-weighted LMTD of exchangers that encounter phase changes may be computed by dividing the exchanger into at least five zones of equal duty. More zones may be requested as desired. Zones analysis is automatically performed during convergence calculations for exchangers with MITA, a zoned

ay be performed during exchanger calculations or at the completion of all calculations, as requested.

is of interest is the one performed on the final case, convergence calculations may be reduced

Exchangers Attached to Columns Exchangers may be attached to any tray of a column for which a duty is defined, ither cooling or heating. To attach an exchanger to a column, click Attach to

nd supply the appropriate information

as one side of the exchanger; a process tream or utility stream defined for the exchanger is the other side. Note that for

utili t he column calculations.

tta e y be used to represent the condenser or reboiler for the heaters and y to which the

xchanger is attached, the vapor from the tray below the tray to which the exchanger is attached, or the liquid from the tray above the tray to which the exchanger is attached.

, it is considered a “fixed” duty for column calculations.

Thermodynamic System The thermodynamic system of methods to be used for each side of the simple heat exchanger may be selected by choosing a method from the Thermodynamic System drop-down list box on the Heat Exchanger main data entry window.

MTD specification, a UA specification, or both a U and an AREA specification together. Each of these configurations requires a zone analysis to reach a solution. Warning messages are given for temperature crossovers.

For other types of specifications, the zone analysis m

Usually, the only zone analysconverged exchanger. In this significantly by requesting zone analysis during OUTPUT rather than during calculations.

eColumn… on the main data entry window ain the window provided.

An internal column stream is considered s

ty s reams, the duty must be determined by t

Ac

ch d exchangers maolumn, a pumparound cooler, or a side heater or cooler. For side

coolers, the column stream may be: the vapor or liquid from the trae

It is generally best to let the exchanger duty be determined in the column operation to meet a desired separation criterion. If the duty is defined by a performance specification for the exchanger


Heating/Cooling Curves

eneral Information he Heating/Cooling Curve utility module develops heating or cooling curves for

any stream in the flowsheet. The tables are a composite of equilibrium flashes, nd present the data typically required for the design of heat transfer equipment.

Curves may be generated by using equal temperature increments or equal duty crements. Additional points are included when phase boundaries are crossed.

or the Flash, Heat Exchanger, and Column unit operations, a convenient means provided to retrieve the streams involved in heat transfer and generate curves ased on the actual duties for the units. For other flowsheet streams, you may efine the desired temperature or duty ranges for the curves.

In addition to the standard thermal properties, additional properties may be quested for the reports. These properties include physical, critical, ermodynamic, transport, and petroleum properties.

eating/Cooling Curves for Flowsheet Streams drop-down list box is used to retrieve flowsheet streams for which curves are

desired in the Heating/Cooling Curves main data entry window. After selecting a tream, click Enter Data to open the Heating/Cooling Curve for Flowsheet

Stream window. This window is used to select the boundaries for the curves, pe of curves, number of points for the curves, and the report options.

combination of two specifications is used to define the type and boundaries for e curves. Curves may be at equal temperature increments, equal duty crements, or may be the dew point or bubble point curve for the fluid. Dew and ubble points may be calculated at defined pressures or at defined temperatures. hen the temperature and pressure ranges are defined for a curve, the resultant

oints are always at equal temperature/pressure intervals. When a temperature, ressure, or duty increment is defined for a curve, the starting point is always

taken to be the current stream conditions.

The number of points for the curves may be selected on this form by replacing the default value of 11. Crossing phase boundaries adds points to the report. The

dditional points represent the phase transitions.

check box may be used to select printout of liquid activity coefficients, vapor fugacity coefficients, and Poynting correction factors for thermodynamic systems

GT

a

in

Fisbd

reth

HA

s

ty AthinbWpp

a

A


based on liquid activity coefficients. The equilibrium K-values for the components a check box.

Heating/Cooling Curves for Unit Operations A drop-down list box is provided for selection of unit operations for which curves

sired in the Heating/Cooling Curves main data entry window. Units for hich curves may be requested include the Flash, Heat Exchanger, and Column.

m K-values for the

nd outlet conditions for the Flash.

he curves may be defined as isothermal, i.e., at equal temperature increments, t equal duty increments. The number of points for the

heck boxes and radio buttons are used on the Heating/Cooling Curves for Heat ndow to select the options for the curves. The temperature and is predefined as the inlet and outlet conditions for each side of

ents, e

may also be selected for printout with

are dew

To select the options for the unit:

Click Enter Data adjacent to the unit name. The appropriate window for the unit operation appears for selection of curve options. In each case, the user may specify printout options for liquid activity coefficients, vapor fugacities, and Poynting corrections for thermodynamic systems based on liquid activity coefficients. The equilibriucomponents may also be selected for printout. Heating/Cooling Curves for Flash Units Check boxes and radio buttons are used on the Heating/Cooling Curves for Flash Drum window to select the options for the curves. The temperature and

ressure range is predefined as the inlet ap Tor as adiabatic, i.e., acurves may be selected on this form by replacing the default value of 11. Crossing phase boundaries adds points the report. The additional points represent the phase transitions. Heating/Cooling Curves for Heat Exchangers CExchangers wipressure rangethe Heat Exchanger. The curves may be defined as isothermal, i.e., at equal temperature incremor as adiabatic, i.e., at equal duty increments. The number of points for thcurves may be selected on this form by replacing the default value of 11. Crossing phase boundaries adds points the report. The additional points represent the phase transitions. Note: 11 points result in 10 intervals.


Heating/Cooling Curves for Columns

l, iabatic, i.e., at equal

nthalpy and pressure increments. The temperature and duty ranges are itions. A pressure range may be added to

effects of pumping.

rt. The

Column streams are selected in a drop-down list box on the Heating/Cooling Curves for Column Internal Streams window. Streams available include the condenser and reboiler feeds, and feeds to trays with duties such as side reboilers and pumparound coolers. The curves may be defined as isothermai.e., at equal temperature and pressure increments, or as adepredefined as the unit operating condpumparound streams to simulate the The number of points for the curves may be selected on this form by replacing the default value of 11. Crossing phase boundaries adds points the repoadditional points represent the phase transitions. Note: 11 points result in 10 intervals.

Standard Reports Standard reports include the data in the table below:

Property Total Feed Vapor Liquid

Temperature X

Pressure X

Molar Flow X X

Enthalpy X X X

Weight Flow X X

Molar Entropy X X X

Additional Stream Properties These properties are requested by clicking Report Additional Stream Properties

n the Heating/Cooling Curve main data entry window. These properties are

oreported in addition to the standard reports for all curves selected for the Heating/Cooling Curve. Additional Stream Properties Reports Additional reports may include the data tabulated below:


Property Total Feed Vapor Liquid

Molecular Weight X X

Actual Density X X

Volumetric Flow X X

Compressibility Factor

X

Specific Gravity X

Flowing Entropy X X X

Enthalpy (unit basis) X X X

Latent Heat X X

Heat Capacity X X

Viscosity X X

Thermal Conductivity X X

Surface Tension X

Critical Temperature X X

Critical Pressure X X

Critical Compressibility

X X

API Gravity X X

Watson K Factor X X

Molar Average Boiling Point Temp.

X X

Plots Refer to Chapter 11, Printing and Plotting, for more information about generating graphical plots of Heating/Cooling Curve results. Thermodynamic System You may select the thermodynamic system of methods to be used for heating/cooling curves calculations by choosing a method from the Thermodynamic System drop-down list box on the Heating/Cooling Curves main data entry window.


Mixer

General Information

he Mixer unit combines two or more streams into a single product stream. The utlet pressure may be specified if desired. The outlet temperature and phase ondition are always determined with an adiabatic flash from the feed conditions. his unit supports both VLE and VLLE calculations.

eeds and Products he inlet pressure is assumed to be the lowest feed pressure. There is no limit n the number of feed streams to a mixer.

nly one product stream is allowed for a mixer. PRO/II automatically sets the mperature and phase condition for the product. If phase separation of the

roduct is desired, a separate flash unit must be used for this purpose.

utlet Pressure Specification he pressure specification for the mixer product is selected with the appropriate dio button on the Mixer window:

• Pressure drop from feed conditions, or • Outlet pressure

neither entry is supplied, the default is a pressure drop of zero.

hermodynamic System he thermodynamic system of methods to be used for mixer calculations may be elected by choosing a method from the Thermodynamic System drop-down list ox on the Mixer main data entry window.

TocT FTo Otep OTra

If TTsb


This page intentionally is l

eft blank.


Multivariable Controller

ral Information ltivariable Controller (MVC) is an expanded form of the Controller and s two or more feedback process controllers. The MVC is capable of g an unlimited number of upstream variables to reach the same number

GeneThe Musimulateadjustinof specified objectives. Each Specification may be a stream flow rate or property, a stream and Calculator

sults that are otherwise at fixed values in the flowsheet.

number of variables must equal the number ove the Specifications grid in the Multivariable

pecifications Establish the Specifications by clicking the appropriate linked text in the Specification grid of the Multivariable Controller window. MVC Specifications are established in the same manner as for the simple Controller Specifications. See the SPEC/VARY/DEFINE section of this chapter for further details on the generalized SPEC form. Variables Establish the control variables (VARY’s) by clicking the linked text string Parameter in the Variable grid of the Multivariable Controller window. MVC VARY's are established in exactly the same manner as simple Controller VARY’s. See the SPEC/VARY/DEFINE section of this chapter for more information on the VARY concept. Tables are also given in that section listing the flowsheet variables that may be used for SPEC’s and VARY’s for multivariable controller units.

unit operating condition, or a Calculator result. The control variables may be and unit operation conditions, thermodynamic parameters,

re For the Multivariable Controller, theof specifications. The linked text abController main data entry window indicates whether the current number of specifications equals the number of variables. If they are unequal, the hypertext string “does not equal” will appear in red. S


Variable Limits and Step Sizes You may input limits for the each control variable, if desired. Variable limits and steps sizes for MVC are established in exactly the same manner as simple Controller limits and step sizes. In contrast to the simple Controller which has a default percent change of 2.0% of the initial control variable for the second eration, e MVC has a default percent change of 10.0%.

ling imits

this

meters lues

operation of the MVC through the MVC

ntroller window.

um or able

using the limiting value if

pply a User-Defined Calculation Sequence whenever any f the control variables are thermodynamic parameters. You may specify the

it th Optional Variable ScaSelect the Use User-defined Variable Scaling check box on the Variable Lwindow to enable a linear formula for scaling the variable. In order to accesswindow, click on the default limits linked text in the Variables field in the Multivariable Controller window. After you have enabled the Scaled Variable formula, the default limits linked text will change to read user-defined limits. Defaults for the scaled variable data are displayed on the Options window whichan be accessed via MVC Options on the Multivariable Controller window. Thec

same initial value, step sizes and tolerances are applied to all scaled parain the MVC. You may enter your own values here to replace the default va00, 10, and 10-5 respectively. 1

Number of Calculation CyclesYou may access several options for the Options button on the Multivariable Co The default for the number of calculation cycles is calculated by the program as 18 plus the current number of variables. Alternatively, you may specify the number of cycles by selecting the appropriate radio button on the Options window. By default, the simulation will stop if any variable exceeds the maximminimum limits. You may select the Continue Calculations if Any Vari

xceeds the Limits check box to continue calculationsEthe limit is exceeded. Select Next Unit Calculated After Control Variable is Updated Normally, the first unit operation in the calculation sequence affected by the control variable is the next unit calculated after the control variable is updated. Normally, the calculation sequence is determined automatically by PRO/II. However, you must suoreturn unit by choosing a unit from the drop-down list box on the Options window.


Print Results for Multivariable Controller The default is to suppress printing of a convergence report. The Print Options window allows you to override the default. This window is accessed by clicking

Multivariable Controller window or be selecting at/Unit Operations from the menu. A convergence summary

appropriate e

ecycle Loops of this chapter for a discussion of recycle loops.

Print Options on theOutput/Report Formcan be printed after the last cycle or after every cycle by selecting the radio button. Select the Include Convergence Diagnostics check box to generata plot of the convergence diagnostics. Select the Include Convergence Diagnostics check box to generate a plot of the convergence diagnostics. Non-convergence of Multivariable Controllers See the Controller section of this chapter for a discussion of convergence techniques used in the Multivariable Controller calculations. Controllers and RSee the Controller section




Phase Envelope

General Information

he Phase Envelope utility module generates phase envelopes for multi-omponent streams using the Soave-Redlich-Kwong or Peng-Robinson quations of state. The module is not available for other thermodynamic systems.

hase envelope generation is performed after the completion of flowsheet alculations and has no effect on flowsheet convergence. For systems with non-ondensable gases such as hydrogen, helium, and nitrogen it may be impossible r the bubble point calculations to converge. The results should be reviewed

arefully.

election of Streams ou may select feed and product streams from any unit operation in the owsheet for phase envelope generation. Up to five flowsheet streams may be elected using drop-down list boxes in the Phase Envelope main data entry indow. You may optionally supply a liquid mole fraction for any of the selected owsheet streams to generate a curve at a constant liquid mole fraction. This ption is useful for generating liquid fraction curves to be superimposed on the hase envelope. Normally, you would first select a flowsheet stream with no quid fraction entry to generate the phase envelope, followed by one or more elections with specified liquid fraction entries to generate a family of curves. It is ot permissible to duplicate the same stream with the same liquid mole fraction in single phase envelope.

lot Options elect a plot option for the phase envelope in the Phase Envelope Plot Options indow which you can access by clicking Plot Options on the Phase Envelope ain data entry window.

or each selected stream, a default descriptive label is provided in this window. he default label will contain the stream name and an L/F value if specified. You ay modify each label. Duplicate labels are not allowed. An example default

tream label with a specified L/F is: “S100 - L/F= 0.9".

Tce Pccfoc SYflswfloplisna PSwm FTms


A drop-down list box contains plot options as follows:

None - This is the default. No plots are generated.

rates a plot with only the stream selected. e

se

he range

Phase Envelope alculations by choosing a method from the Thermodynamic System drop-down

Individual - Individual gene

Comparison All streams with the Comparison option are plotted on thsame graph. The Comparison option is useful for plotting a stream phaenvelope with superimposed curves of constant liquid mole fraction. When you select the Comparison option for a stream, you will be prompted to provide a comparison plot symbol to label the data points for the generated curve. The symbol may be an integer number in tone through nine. If you do not provide a symbol is not provided for the comparison plot, the next available integer between one and nine is used

Individual and Comparison - The Individual and Comparison option performs

both the Individual and Comparison options for a stream. Thermodynamic System Select the thermodynamic system of methods to be used for clist box on the Phase Envelope main data entry window.


PIPEPHASE Unit Operation

General Information The PIPEPHASE Unit Operation (PPUOP) encapsulates a PIPEPHASE imulation enabling it to be solved in sequential modular form within a

s the user to link PRO/II s

reams

n be specified with one feed stream only where

is allowed only if the number of components in both PRO/II

ed

sconventional PRO/II simulation. The PPUOP allowsimulation streams to PIPEPHASE simulations streams so that stream propertiefrom a PRO/II simulation is passed to the PIPEPHASE simulation, and back to PRO/II upon solution of the PIPEPHASE simulation. As with any unit operation inPRO/II, the PPUOP can be accessed multiple times in calculation loops, and a PRO/II simulation can have multiple instances of PPUOP's in the flowsheet. The PPUOP is represented as an icon and is similar to other PRO/II unit operations. It can be initialized with a PIPEHASE simulation. Note: Refer to the PRO/II Installation Notes for the specific versions of

IPEPHASE currently supported by PRO/II. P Feed and Product StThe PIPEPHASE Unit Operation (PPUOP) can have multiple feed and product streams connected to it. The PRO/II feed streams are always mapped to the Sources in a PPUOP and the product streams are mapped to the Sinks in a

PUOP. The PPUOP Source caPas the Sink unit operation data can be mapped to multiple product streams. The stream properties that can be transferred through mapping are: Temperature, Pressure, Flow rate and Composition. Component mapping

omponent mappingCand PIPEPHASE are equal. The components can be mapped by either Name or Index. These two options can be selected from the Component mapping drop- down list in the PRO/II PIPEPHASE window, which can be accessed by double- clicking the PPUOP. If the components are mapped by Name, the PRO/II component data is mappwith the PIPEPHASE component of the same name.


If the components are mapped by Index, then the first component in the PRO/II

r ng

imulation… in the PRO/II PIPEPHASE window. If the ASE simulation with another simulation, then all the

heet. The

PIPEPHASE GUI PRO/II PIPEPHASE window.

pp1) e

the keyword file. However, for PIPEPHASE he PIPEPHASE GUI automatically are

component data list is mapped with the first component of the PIPEPHASE component data list, irrespective of the component names. Initialization The PPUOP can be initialized with a PIPEPHASE simulation (.inp foPIPEPHASE 8.2 and either an .inp or a .ppzip for PIPEPHASE 9.0) by clickiInitialize from PIPEPHASE suser reinitializes a PIPEPHinformation of the previous simulation will be removed. Note: When using PIPEPHASE version 8.2 files for initialization, it is necessary for the GUI database files, (.pp0 and .pp1) to be present. Otherwise, the user must generate the PIPEPHASE GUI database files by importing the corresponding keyword file. PIPEPHASE GUI

he PIPEPHASE GUI can be launched from within the PRO/II flowsTuser can commit the changes made to the simulation in the GUI, and export thechanges to the keyword input file. The user can launch the PIPEPHASE GUI by licking the button in the c

Note: The PIPEPHASE v8.2 requires the PIPEPHASE GUI files (.pp0 and .

of the simulation. If not present, a warning message is displayed and thuser is required to exportversion 9.0, changes made in texported to the keyword file while saving the simulation.

Export The user can export a copy of the PIPEPHASE simulation to an external locationy clicking Export to external PIPEPHASE simulation…. b

PIPEPHASE Reports The PIPEPHASE Report displays only the results of the PIPEPHASE simulation and not the PRO/II PIPEPHASE integration flowsheet.

You can view the results of a solved PIPEPHASE simulation by clicking PIPEPHASE Report…button in the PRO/II PIPEPHASE window or right-click thePIPEPHASE icon and select View Results.


Stream link specifications A link between the PRO/II simulation and a PIPEPHASE simulation can be established on the Stream Link Specifications grid, in the PRO/II PIPEPHASE wPR n the left rid. PIPEPHASE Source streams are available on the drop- down lists on the right side, adjacent to PRO/II feed streams, and PIPEPHASE

on the drop-down lists on the right side, adjacent to s.

t operation can be specified as pe ithin a PRO/II simulation to control either a

PRO I network simulation.

ons

e option Define data link

h FD, and initialize it with a PIP H SE file along with its database

es s directory. This Temp folder is called the

ges unched

nd

e ation

e ID of the PIPEPHASE unit in the simulation. This O/II .prz, along with the conventional PRO/II (.pr1,

indow. This window can be accessed by double-clicking the PPUOP icon. O/II streams that have been attached as feeds and products are displayed o

side of the g

Sink streams are availablethe PRO/II product stream Define Data link specifications

he parameters of a PIPEPHASE uniTS c/Vary/Define variables from w

/I flowsheet or a PIPEPHASE The Spec/Vary/Define variables can be specified in the Data Link specificatigrid. This grid is available in the PRO/II PIPEPHASE window, which can be

ccessed by double-clicking the PPUOP. Check thaspecifications to access the grid. For more details on these concepts, refer to the SPEC/VARY/DEFINE section of

hapter 9 in this manual. C File Handling W en you drag and drop a new PPUOP on the P

the PIPEPHAEP ASE simulation, a copy of is tored in the PRO/II Temp fil

Managed folder and it will be the working directory for that specific PPUOP. All PIPEPHASE related files reside in this folder during the PRO/II simulation run. The files in the Managed folder are under the control of PRO/II and any chan

ade to these files by providing inputs through the PIPEPHASE GUI lamby clicking PIPEPHASE GUI… are saved to the files in the Managed folder anot to the PIPEPHASE database files in the original location. When PRO/II saves a set of simulation files, a new zip file is created by copying all the PIPEPHASE files from the Managed folder. These include all the PIPEHASE files (.inp, .pp0, .pp1, .out , and other intermediate files for PIPEHASE version 8.2, or ppzip for PIPEPHASE version 9.0) The .zip file namhas the form “PRZfilename_UnitID.zip”, where “PRZfilename" is the simulle name and “UnitID" is thfi

.zip file is archived in the PR

.pr2, .sfd, etc.) files.




Pipe

General Information The Pipe unit is used to model single or multiphase pressure drops in pipes and/or fittings which connect unit operations. This unit may be used in two modes: Rating Mode where the pressure drop is computed based on a specified line diameter, and Design Mode where the line diameter is calculated to meet a specified pressure drop and/ or velocity criteria. Numerous algorithms are provided for the pressure drop calculations to model a variety of piping applications. A rigorous heat balance may also be performed for the calculations, in which heat is transferred through the pipe to or from an ambient medium, or a duty is uniformly applied to the length of the pipe. The phase equilibrium is determined for the product and it may be separated into streams according to the phases. Both VLE and VLLE calculations are supported by this unit. Feeds and Products A pipe operation may have multiple feed streams, in which case the inlet pressure is assumed to be the lowest feed stream pressure. A pipe may have one or more product streams. The product phase condition for pipe operations with one product is automatically set by PRO/II. For pipe units with two or more product streams, the product phases must be specified in the Product Phases window which is accessed by clicking Product Phases… on the Pipe main data entry window. Allowed product phase declarations include: vapor, liquid, decanted water, heavy liquid, and mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with vapor and liquid products and is not allowed when four product streams are specified. It is important to note that where two liquid phases are present in multiphase calculations, all pressure drop methods consider only a single liquid phase which has fluid properties that are an average of the properties for the two liquid phases. Calculation Type The Calculation Type may be selected with the radio buttons provided on the Pipe main data entry window. Options are as follows:

• Fixed Line Diameter - Forward Calculation (default)


• Fixed Line Diameter - Backward Calculation culation

Backward calculations determine the pressure drop in a backward, or reverse, direction starting at the pipe outlet conditions. The pipe inlet conditions are defined by the results of the backward calculations. The line sizing option may be used for des mode, in which case the diameter of the pipe is determined to

eet a spec ied design criterion.

Note: Pipe calculations require liquid and vapor viscosities, and, for two phase hosen for

tion for certain types of calculation failures. The default option of Continue uses the best available solution or sets a negative computed outlet pressure to a small value and allows the flowsheet calculations to continue. For line sizing calculation failures, the line diameter which most closely satisfies the design criteria is selected and flowsheet calculations continue. A maximum of three consecutive failures i e loops. The Stop option r the pipe unit fails to reach a soluti ed. Pressure DroSelect the press ethod window accessible via Pressure Drop Method… on the Pipe main data entry window. The pressure drop method is selected with the drop-down list box in this window, and includes the following methods: Beggs-Brill-Moody (BBM), Beggs-Brill-Moody with Palmer Correction (BBP),

ult

An optional estimated pressure drop may be supplied in this window to reduce the computing time. The convergence tolerance default of one percent and the default flow efficiency of 100 percent may be replaced in this window. The flow efficiency is a linear adjustment factor that is applied to the calculated pressure drop to better match actual conditions.

• Line Sizing - Forward Cal

ign ifm

flow, the liquid surface tension. Therefore, the thermodynamic system cthe calculations must provide these properties. Corrective Action for Calculation Failures The Continue text string on the Pipe main data entry window may be clicked to select the corrective ac

s allowed for pipe units in recycl

terminates all flowsheet calculations wheneveon, or a negative outlet pressure is encounter

p Method ure drop method in the Pipe Pressure Drop M

Olimens (OLIMENS), Dukler-Eaton-Flanigan (DEF), Mukherjee-Brill (MB), Gray (GRAY), and Hagedorn-Brown (HB). Beggs-Brill-Moody is selected as the defacorrelation.


The Moody friction factor for thdirectly in this window, if desir

e pressure drop calculations may be supplied ed. If no value is entered, the Moody friction factor

used to include or exclude the pressure drop contribution om acceleration. Under certain high velocity or high pressure drop conditions,

this term becomes unrealistically high for the Beggs-Brill-Moody equation. Under these situations, excluding this term results in a more reasonable answer. Note: The Beggs-Brill-Moody equation does not cover critical flow.

Line/Fitting Data Line and fitting data are supplied in the Pipe Line/Fitting Data window which is reached by clicking Line/Fitting Data on the Pipe main data entry window. For fixed line diameter calculations, radio buttons on this window are used to select the input mode for the pipe diameter. When the Inside Diameter radio button is selected, the pipe inside diameter is supplied directly. When the Nominal Pipe Size radio button is selected, a drop-down list box is used to select the desired pipe nominal diameter from a table of common pipe sizes. For this option, the pipe schedule may also be chosen with a drop-down list box. When no schedule is chosen, schedule 40 pipe is assumed in most cases. The line length is supplied directly in this window. The maximum allowable line length is 900,000 feet (274,000 meters). An elevation change over the line length may be entered in the Pipe Line/Fitting Data window. A plus value indicates an increase in elevation; a minus sign indicates a decrease in elevation. The absolute value of the elevation change must not exceed the line length. One fitting K-factor may be attached to a pipe unit and supplied in this window. The K-factor is defined as the total resistance coefficient, and is limited to a maximum value of 100.0. Note that the supplied K-factor may be used to represent multiple fittings, valves, and exit losses. When a pipe unit is being used to represent a fitting or fittings only, a negligible line length should be provided. Radio buttons are used to select the pipe roughness in this window. The Absolute roughness may be entered in length units or the Relative roughness may be supplied. The roughness applies to both the line and the fitting. A default absolute roughness of 0.0018 inches or equivalent (new steel pipe) is used when no roughness is supplied. The number of calculation segments is selected by clicking the text string at the bottom of this window. A maximum of 50 segments may be used. The pressure drop calculations are based on the average fluid properties in a segment;

is calculated using the modified Colebrook-White equations. The check box may befr


therefore, it is important to use multiple segments for systems in which the fluid tly over the line length (such as multiphase systems). n segments has a significant effect on the calculated

s. It is also recommended that long lines be

t

upplied in the Pipe Line Sizing window which is accessed zing

he maximum pressure drop or the minimum outlet pressure are provided.

as

• Use Nominal Pipe Sizes A defauvalues mtable. T A table

plied ter .

n s. The corresponding schedule numbers are also selected via drop-down

st boxes. Pipe schedule numbers default to schedule 40 in most cases. The lear All button may be used to clear all selected nominal pipe sizes and orresponding schedules.

properties vary significanThe number of calculatiopressure drop for such systemdivided into segments of 10,000 feet (3040 meters) or less. Note that a default of one segment is used for a pipe unit unless otherwise specified.

Note: When line sizing calculations are performed, the line/fitting diameter andfitting K-factor cannot be supplied, and these data entry fields are noavailable.

Line Sizing Data Line sizing data are sby clicking Line Sizing Data on the Pipe main data entry window. Primary sicriterion options are:

• Maximum Pressure Drop • Minimum Outlet Pressure

alues for tV

supplied directly in the data entry fields A Maximum Average Fluid Velocity constraint may also be defined. This constraint can not be violated, and the primary sizing criterion will be relaxedneeded to not exceed the supplied maximum velocity. The Line Inside Diameter Selection Method is chosen with radio buttons as follows:

• Use Explicitly-defined Inside Diameters

lt inside pipe diameter table with ten diameters is provided. The default ay be replaced as desired. Use Clear All to clear the pipe diameter

he Restore Defaults button restores the ten default diameters.

of nominal pipe sizes and corresponding schedule numbers may be in the Nominal Pipe Sizes window which is reached by clicking Ensup

Data… on the Pipe Line Sizing window. Up to ten pairs of data may be providedNominal pipe sizes are selected from a table of supplied values via drop-dowlist boxeliCc


Heat Transfer Data Heat transfer data are supplied on the Pipe Heat Transfer window accessible via

e Heat Transfer icon on the Pipe main data entry window. The duty calculation

For Fixelength of the line. A positive value issigndefault ocalculations. An overall U factor and ambient temperature must be provided for the Ambient Heat Transfer option. The U factor has units of energy/ (area)(time)(degree). A defacomputeinside a is option may not be used with bac The Iso rforms all pressure drop calculations at the

let temperature to the pipe unit. This option is not allowed for backward

Default

thoption is selected via radio buttons:

• Fixed Duty • Ambient Heat Transfer • Isothermal Operation

d Duty calculations, the supplied duty is applied evenly over the entire

used for heating and a negative value ifies cooling. This option with a duty of zero is used as the heat transfer

ption. This option may be used for both forward and backward

ult value of 6°F is used for the ambient temperature. The heat transfer is d from the pipe segment inlet and outlet temperatures, U factor, pipe

rea, and the ambient temperature. Thkward calculations.

thermal Operation option peincalculations. Thermodynamic System The thermodynamic system for the pipe calculations may be selected with the rop-down list box on the Pipe main data entry window. The problemd

system is used when no other thermodynamic system is selected.




Polymer Reactor

formatioThe Polymer Reactor mo lates either a free ra al or s wise polymerization process in l Continu Stirred nk Rea r (CST or

) lymerization reactio are ass ed to take phase stem is assumed to be homogeneous. The un in th al or no otherm modes and the operating

cal odel allows for up reactio m s to be used i er free radical kine s. Not a are intended to

aneously; in fact, the fewer mechanism specified for the polymer re realistic and reliable the model.

lymerization ion in the liq phase f the

reaction leads to a two phase situation, a ing message is given and the user must pe perati condit s to

the the o hase ion. Th ergy balances are solved to identify a single stable

lymer which exists at this operating condition is thef the method of moments to provide number and weight h

energ s are so ed to identify a sequence of stable ng the axial dimension. The polym r which e ists at e

aracterivide num weight average mol lar wei s.

c ctor o d thermo-

ided.

General In n del simu an idea

dic Ta

tepctoous R)

Plug Flow Reactor (PFR . The po ns umplace in the liquidreactors may be r

and the sye isotherm n-is al

pressure may be set.

The Polymer Reactorechanism

culation mn copolym

to 79 differenttic

nll

be used simultsystem, the mo

s

It is assumreact

ed that the pos occur uid . I

warnthen s cify new o

system inng ne p

ionregkeep

e CSTR mass and enoperating point. The pocharacterized in terms o

n

average molecular weig ts.

The PFR mass and y balance lvoperating points alo e x achpoint along the axial profilemoments to pro

is then chber and

zed in terms of the method of ecu ght

The user must supply the feed component temperature, pressure, and omposition along with an estimate of the temperature of the isothermal rear a temperature estimate for the non-isothermal reactor. Kinetic an

dynamic data for the reaction between chemical species must also be prov


Detailed Information For detail ts, and range of applicability of the P eactor model, consult the PRO/II Add-On Modul ide.

ed information regarding operating modes, data requiremenolymer R

es User Gu


Procedure Data General Information

a late the re tion rate based on a user’s n cal thod. The reaction rate calculation is re d by the plug, CSTR, rea ts. PRO/II’s default method for reaction rat n is based o aw rate expressions. For any ther rat

ch as Langmuir-Hishelwood) or any reaction rate which ase ra s a reaction with a ass tra er limitation),

and the alternative User-Added Kinetic Subroutines (see PRO/II tines User Guide) can b sed to lculate proper rate for

ulations. Procedu re essentially in line routines written in a language ased on FO . There are tions to a Procedure and Code. The

for th n of each Procedure’s name, descriptio , eters section where l calculations are

n resembles a subroutine written in a FORTRAN-like

Pr Setup Us dure Data dialog to enter proc ure data. Access the dialog

Procedures provide a w y to calcu ac owculation mective distillation and batch reactor uni

quire

e calculatio n power l o e, expression type (sudeviates from the bProcedures

te (such a m nsf

User-Added Subroureactor sim

e u ca the

res a bRTRAN 77 two sec : Setup

setup section allowsvariables and param

e definitio. The code

nis al

performed. This sectiolanguage.

oceduree the Proce ed

window through the I

Procedure Data toolba

nput/Procedure Data… menu option, or by clicking the

r button . Each Procedure in this window has a d an optional description. As soon as the name for a

the Enter Data… button becomes available. The button ed on wind where u may k Edit/View

the Declarations of variables and parameters.

nam d in Defin Proce re Variables will bs tion from e rea Proce es it b in the reactor unit, and accessed in the

variable in the Procedure code. e is only one availab to be s d, which is the

um numbe owed. This only need chang if mu more th ctions.

fter completing the setup, click Hide Declaration to close the Declarations

mandatory name anProcedure is entered, opens the Kinetic ProcDeclaration to access

ure Definiti ow yo clic

Any variable

available to trancalls. They can same manner as any other

es entere ed du e fer informa th ctor unit to the dure DEFINE'd

Thermaximthe Procedure

Parameter r of reactions allst handle

le pecifies be ed

an the default of 15 rea

Adialog.


P

he actual FORTRAN procedure is entered directly in the Code field on the

Kinetic Pro rocedure as you comp iables are provided from the calling rea

ese are the kinetic parameters are provided via K… of at Unit Reaction Definitions… of the

tor unit. ese data include the reactor sizing parameters and

ioata include the thermo-physical property data of

the pure components (e.g., molecular weight or critical pressure), and the property data of the individual components and mixture at the

ction conditions. r data: These are the integer, real, and supplemental data provided

by the user via Enter Data… when the proce e name is specifie for lculations for a Reactor unit.

Procedure data: These are the defined procedure variables entered dure setup. Their values are DEFINE’d in the same

window as the User data.

e features are discussed below. Elements of the Language E ins a maximum of 80 characters. An ampersand (&) at the e continuation on the following line. Note that an asterisk (*) is not valid as a continuation marker, since it signifies multiplication. All lines of code except the CODE statement may be preceded by a unique

l from 1 to 99999 (shown as “nn” in this manual).

es all following data on the line to be interpreted asn as code. Unlike in FORTRAN, a “C” in column 1 doe ot

d comment statement.

rocedure Code Note: The Procedure Code section is required and must terminate with a

RETURN statement.

Tcedure Definition data entry window. You may check the p

ose it by clicking Check Code. The following predefined varctor unit:

Kinetic data: Ththe Reaction DReac

a section, and/or

Reactor data: Thoperating condit

Property data: These dns.

rea Use

dur d rate ca

during the Proce

The supported languag

ach statement contand of a line indicates

numeric labe A dollar sign (“$”) causcomment rather tha

a s n

esignate a Predefined Variables The following variable names are reserved. They are used to pass values between the procedure and the unit operation that uses the procedure.


The first tables list variables that provide input values to the procedure. They may ot appear on the left side of an assignment statement.

n

Procedure Data ed REAL Scalar Variables Predefin

Property VaName PFR CSTR Batch RxDist riable

REAL Scalar Variables - Supplied in standard problem dimensional units

T RTEMP X X X X emperature Pressure RPRES X X X X Total Molecular weight RMW X X X XV RVMW X apor Phase

Liquid Pha RLMW X se

L1 Phase RL1MW X L RL2MW X 2 Phase Specific gravity (60/60) RSPGR X X X X T RMRATE X X X X otal Molar Rate

V R apor Phase VMRAT X Liquid Phase RLMRAT X L RL1MRA X 1 Phase

L2 Phase RL2MRA X Weight Rate R X X WRATE X X Standard Volumetric

Rate2 R X X X SVRAT

Actual Volumetric Rate RAVRAT X X X Vapor Phase RVVRAT X Liquid Phase RLVRAT X L1 Phase RL1VRA X L2 Phase RL2VRA X Liquid Fraction RLFRAC X X X X L1 Phase RL1FRA X L2 Phase RL2FRA X Vapor Phase Viscosity RVVISC X X X X Liquid Phase Viscosity RLVISC X X X X


Procedure Data Predefined REAL Scalar Variables

Property Variable Name PFR CSTR Batch RxDist

REAL Scalar Variables - Supplied in standard problem dimensional units Vapor Phase

Conductivity RVCOND X X X X

Liquid Phase Conductivity RLCOND X X X X

Vapor Phase Sp. heat RVCP X X X X Liquid Phase Sp. heat RLCP X X X X Surface tension RSURF X X X X Absolute Temperature RTABS X X X X Tube Diameter (fine

length) TDIAM X

Tube Length TLEN X X Cumulative Length CUMLEN X Plug Flow Step Size

(fine length) DELX X

Total reactor volume ( T

or olu

PLUGFLOW reactor

VOLUME X X X CS R & BATCH)

v me step size of

Vapor Phase Volume RVVOLU X Liquid Phase Volume RLVOLU X L1 Phase Volume RL1VOL X L2 Phase Volume RL2VOL X Gas Constant RGAS X X X X 1 Volumetric flow rates for CSTR and PLUGFLOW are calculated using bulk

compositions assuming the specified reactor phase, even if the phase is actually mixed. A warning is printed if the actual phase is mixed.

2 Standard vapor volume conditions are different from liquid mole volume standard conditions. Refer to Table 1: Standard Conditions on page 45.


Procedure Data Predefined INTEGER Scalar Variables


Total # of components NOC X X X X Total # of reactions NOR X X X X Reaction phase IRPHAS X X X Basis for Rate Calculation

0 = molar 1 = partial pressure 2 = fugacity 3 = mole-gamma

ICPFA X X X

Step # ISTEP X Unit # for output file IOUT X X X X Unit # for index file INDX X X X X Maximum # of reactions MAXNOR X X X X

Procedure Data Predefined REAL Variable Arrays


Dimension : NOC Total Molar Composition XTOTAL X X X X

Total Molar Concentration XCONC X X X

Vapor Phase XVCONC X Liquid Phase XLCONC X

L1 Phase XL1CON X L2 Phase XL2CON X

Vapor Phase Fugacity XVFUG X X X X Liquid Phase Fugacity XLFUG X

L1 Phase XL1FUG X L2 Phase XL2FUG X


Procedure Data Predefined REAL Variable Arrays


Liquid Phase Activity XLACT X L1 Phase XL1ACT X L2 Phase XL2ACT X

Vapor phase Mole ractions XVAP X X X F X

Liquid phase Mole Fractions XLIQ X X X X

L1 Phase XLIQ1 X L2 Phase XLIQ2 X

Vapor phase Mass Fractions XVMFRA X

LFra

iquid phase Mass ctions XLMFRA X

L1 Phase X XL1MFR L2 Phase X XL2MFR

DnumberRDATA

imension: 70 Real s supplied on statement

RDATA X X X X

Dimension: 200 Real numbers supplied on SUPPLE SUPPLE statement

X X X X

Dimension: NOR ACTIVE X X X Activation Energy*

X

Pre-exponential factor Temperature Exponent

PREEXP TEXPON

X X

X X

X X

X X

Dimension: NOC,NOR)

X (Stoichiometric factor Reaction order

STOICH ORDER X

X X

X X

X X

* Th een the values of activation energy for in and calculations invol

n sets are assumed to be in

ere is an important distinction betwline procedures ving local reaction sets in distillation columns or reactors. The values of activation energy supplied the reference reaction set (in RXDATA) or in the local reactio


thousands of energy units per mole units, whereas, in the case of procedures, the s t the above assumption. E.g., for the SI sy m TA or local rxnset is used as dure using the same variable, say AC V

u er-supplied value is used withouste , a value of ACTIV=123 kJ/kmol in the RXDA 123,000 kJ/kmol in calculations. A proceTI (1), would calculate based on a value of 123 kJ/kmol.

Procedure Data Predefined INTEGER Variable Arrays

Variable Name PFR CSTR Batch RxDist

Dimension: 10 Integer supplied on IDATA statement

IDATA X X X X

Dimension: NOR Base Component IDBASE X X X X

Calculation basis for each reaction rate (liquid phase) 0 = molar

2 = fugacity I X1 1 = partial pressure ILBAS

3 = mole-gamma 4 = mole fraction 5 = mass fraction

Calculation basis for each reaction rrate (vapor phase) 0 = molar 1 = partial pressure IVBASI X1 2 = fugacity 3= mole-gamma 4 = mole fraction 5 = mass fraction

Dimension: (NOC,NOR) Phase of

ents in rxn por

IPHASE compon1 = Va2 = Liquid

X

1Available only for Boiling Pot CSTR

he following variables are the PROCEDURE block results available to PRO/II after control is returned to the PLUGFLOW, CSTR or Reactive Distillation unit operation. RRATES must be defined for all reactions.

T


PROCEDURE Results

Variable Name PFR CSTR Batch RxDist

Values of solution flag: Default value.

PROC

in a reloop. PROC

0Assumes the PROCEDURE step has solved.

EDURE solved. 12 PROCEDURE failed;

continue calculations if cycle or control

EDURE failed,

X X X X

3stop all flowsheet calculations.

Reactioreactiotime) fPHAS

moles/(OPERPHASE=

n rates for each n moles/ (liqvol* or OPERATION E=L1 , vapvol*time) for ATION

V1

RRATES (NOR)

X X X X

Temperature derivatives DRDT 2for each reaction (NOR) X

Compofor X sition derivatives

DRDX (NOC, each reaction NOR)2

1 CSTR and PLUGFLOW should not be used whenare expected. Except for Reactive Distillation and

multiphase reactions the CSTR boiling pot

The us

model, PRO/II assumes the phase is 100% liquid or vapor as defined on the OPERATION statement.

e of this is optional. 2 Procedure Data Programming Language

discussion of the CalcSs

ee the ulator module at the beginning of this chapter for a urvey of the proper us

Flow Co

e of Declaration Statements, Assignment Statements, Fortran Intrinsic Functions, PRO/II Intrinsic Functions, IF Statements, Calculation

ntrol Statements , and Calculation Termination Statements ).


Pump

al Information Gener

he Pump may be used to compute the energy required to increase the pressure f a process stream. This quantity of energy is added to the feed enthalpy to etermine the outlet temperature. Only the bulk liquid phase is considered in the

calculations.

s pump operation may have multiple feed streams, in which case the inlet ressure is assumed to be the lowest feed stream pressure. A single liquid roduct stream is allowed from a pump.

pecifications utlet Conditions

ssure Specification for a pump is selected with the appropriate radio utton on the Pump main data entry window as:

• Outlet pressure • Pressure rise (∆P) • Pressure ratio based on the lowest feed stream pressure.

ciency pumping efficiency in percent may be supplied in the data entry field provided

on the Pump main data entry window. This value is used for the work and outlet mperature calculations. If not supplied, a default value of 100 percent is used.

odynamic System he thermodynamic system of methods to be used for pump calculations may be

selected by choosing a method from the Thermodynamic System drop-down list ox on the Pump main data entry window.

Tod

Feeds and ProductApp

SOThe Preb

Pump EffiA

te ThermT

b




he Reaction Data Sets data entry window to supply reaction stoichiometry, eat of reaction, kinetic and equilibrium data, and to specify the base component

data setenergy plug flow, CSTR, and boiling pot reactors). Multiple unit

perations can have common access to the same reaction data.

The PRexpressi

and equilibrium and kinetic data in the Reactor data entry window. For conversion reactors, these data are considered to be local and are entered at the unit operation level. See the Reactor section later in this chapter.

Reaction Data General Information Use thfor each reaction. One or more reactions may be saved as separate reaction

s and used in all reactor types (conversion, equilibrium, Gibbs free minimization,

o

O/II graphical user interface now supports multiple equilibrium ons for each Equilibrium Reactor.

Note: You may specify the base component of the reaction and provide heat of

reaction

To access the Reaction Data window:

Click Reaction Data on the main toolbar.

Any data entered in the Re

Note: action Data window is passed to the Unit

Speci Reaction Sets

description for each reaction data set in the main Reaction ame is required but the description is optional.

ry windomponents for each reaction must be selected from a previously-defined

onent list. To enter data for each newly-defined reaction data set, or to modify the data for imported sets:

Click Enter Data… for that set. This opens the Reaction Definitions window for that set. Here, you may enter the following information for the reaction data set:

Reaction Definitions dialog (a sub-window of the main Reactor window)and used as default values.

fyingProvide a name andData window. The n Note: You must define the component list in the Component Selection data ent

ow before entering reaction data. This order is important because ccomp


• Kinetic rate calculation method • The name of all reactions in the set (required) • The reaction stoichiometry (required) • The heat of reaction and the base component (required) • Equilibrium data (optional)

d:

reaction rate subroutine based rocedure or by the user’s kinetic

ta user-

dded k can be selected from the Subroutine Name

PRO/ Installation Guide.

linked text Reactants = tion Components window.

Here, you may select the reactants and products for the reaction and supply the stoichiometric coefficient for each. You may define the reaction based on the chemical formula of the component (library components only), or based on the name (for library, non-library, or petro components).

ou may define the heat of reaction for any selected reaction in a specific reaction data set, in the Heat of Reaction Data window. This window appears when you click H… located beside the selected reaction on the Reaction Definitions window. In this window, you may choose one of two options:

to calculate the ction

rence reaction phase.

do not have heat of formation data. You must also specify the base component for the reaction.

• Kinetic data (optional).

o select the kinetic rate calculation methoT

The kinetic rate can be calculated from PRO/II’sn the power law rate expression, by an inline po

subroutine. The inline procedure must be first defined in the Procedure Dasection and selected from the Procedure Name drop-down list box. When a

inetic subroutine is used, it adrop-down list box. The user’s added kinetic subroutine must be named as one of the five USKIN1, USKIN2, USKIN3, USKIN4 and USKIN5 routines and linked

II as described in the PRO/II UAS/PDTSto

o define the stoichiometry: T Define the reaction stoichiometry by clicking on theProducts in the Definition column to open the Reac

To define the heat of reaction: Y

Calculated from Heat of Formation: This option allows PRO/II

heat of reaction based on the heats of formation for the reacomponents. This is the default.

User-specified: You supply the heat of reaction (in units of energy/ weight). If

you do so, you may also optionally supply the reference temperature, component, and refe

Note: You must supply heat of reaction data for non-library components that


ply equilibrium data for a specific reaction in a reaction data To sup

et:

Data check box to enter equilibrium data. You may Equ b

easure for the

Equ b

apor and liquid phases, component reaction phases, and

ach . The vapor activity basis is used for all vapor phase activity phase while the liquid components specified with liquid phase

activity phase. To ic reaction in a reaction data set:

itions ars.

Click the Define Kinetic Data check box to enter kinetic data.

Pre-exponential Factor (A): The pre-exponential factor of the power law kinetic rate equation for the reaction. The default is 1.0.

Act tion Energy: The activation energy of the power law kinetic rate equation

for the reaction in units of energy/weight. A default of zero is used if a value is not supplied.

Temperature Exponent: The temperature exponent of the power law kinetic rate

equation for the reaction. A default of zero is used if a value is not supplied.

s

Click E… located beside the selected reaction in the Reaction Definitionswindow. The Reaction Equilibrium Data window appears. Click the Define Equilibrium

supply the following data in this window:

ili rium Coefficients: Up to 8 (A-H) coefficients for the equilibrium equation(at least one coefficient must be supplied).

Units: Temperature, weight, volume and pressure units of m

equilibrium data may be supplied by clicking on the linked (underlined) text in the Units box. (If you do not change the temperature units, the global units are used by default).

ili rium Constant Expression: The default reaction phase, reaction activitybases for vexponent orders can be entered here. Click Activity Exponent and Activity Phase to specify the exponent order and activity phase for ecomponent in the reactioncomponents specified withactivity basis is used for all

supply kinetic data for a specif

Click K… located beside the selected reaction in the Reaction Definwindow. The Reaction Kinetic Data window appe

You may supply the following data in this window:

iva


Rea : The data declared using this option on phase, reaction activity bases for vapor

at ck Reaction Order and Activity

Phase to specify the kinetic reaction order and activity phase for each component, which appeared in the rate expression. The vapor activity

ction Order and Activity Basisinclude: the default reactiphase, liquid phase, component reaction phase and kinetic orders thdefine the kinetic rate expression. Cli

basis is used with all components specified with vapor activity phase while the liquid activity basis is used with all components specified with liquid activity phase.


Reactor General Information The Reactor unit operation simulates the operation of many chemical reactors

cluding conversion reactors, equilibrium reactors, Gibbs (Free Energy

additi and

Methanation reaction data sets for either conversion or equilibrium reactors.

eeds and Products the

reactor allowab d (vapor +

roduct. The decanted water product is also used as the second liquid product

If this istreams ct Phases window. Access this window by clicking Product

.

eactor Type e

ropriate reactor icon from the PFD palette. CSTR and boiling r

u must select a reaction data ox (options include a built-in set) on the Reactor main data

tion

ecifying reaction data set

inMinimization) reactors, Plug Flow Reactors (PFR’s), Continuous Stirred Tank Reactors (CSTR’s), and Boiling Pot Reactors.

on to the above reactor types, PRO/II contains built-in ShiftIn

FEach reactor may have one or more feed streams. A multiphase product from

may be separated into streams containing one or more phase. The le product stream phases are vapor, liquid, decanted water and mixe liquid). A mixed phase product is not allowed with a vapor or a liquid

pphase with rigorous VLLE calculations.

more than one product stream, the phases must be allocated to the in the Produs

Phases… on the main Reactor data entry window for the particular reactor type RFor conversion, equilibrium, Gibbs, or plug flow reactors, select the reactor typ

y choosing the appbpot reactors share the CST/Boiling Pot Reactors icon. Select the desired reactotype from a drop-down list box on the main Reactor data entry window. Reaction Set

or all reactor types other than the Gibbs reactor, yoFset from the Reaction Set Name drop-down list beaction set, e.g., Shift reaction, or a user-definedr

entry window. For the Gibbs reactor type, either no reaction data set may beselected (option None), or a user-defined set may be specified. See the ReacDat r in this chapter, for more information on spa section, earlie

s.


Thermal Specifications For most reactor types, the fixed operating temperature, the temperature rise across the reactor, or the fixed reactor duty may be specified by using radio buttons and entering values in the appropriate data fields. The available options are:

is ion and equilibrium reactors only where it is

the default.

Combinailable for plug flow and Gibbs reactors,

and CSTR's only where it is the default.

Fixed Duty: You may specify the reactor duty for all reactor types. A default

xterna

window.

r length, or as a function of percent

lick Reactor Data… from the main Reactor data entry window to open the eactor Data window where you can supply reactor configuration information.

Temperature Rise: This is the temperature increase across the reactor. Th

option is available for convers

ed Feed Temperature: Enter the average temperature for all feed streams to the reactor. This is av

Fixed Temperature: You may specify the final reactor temperature for all reactor

types.

value of 0 will be used if a value is not specified. The following additional reactor information may also be given via the main Reactor window:

l Heat: You may specify information on the external heating or cooling Esource by selecting the External Heat option. This is for plug flow reactors only. Click Enter Data… and enter data in the External Heating/Cooling

Temperature Profile: You may enter the reactor temperature profile in tabular

form as a function of the actual reactoor fractional distance along the reactor. This is for plug flow reactors only.

Reactor DataCR


Conversion and Equilibrium Reactors

For these reactor types, you may choose an error handling option by clicking the

top calculations hypertext. The options are:

top Calculations: This stops calculations if an error occurs (e.g., for negative component flows). This is the default.

Continue Calculations with no Reaction: Continue calculations with no reaction if an error occurs.

dd Makeup of Limiting Reactant: Reduce conversion by adding a makeup of the limiting reactant if an error occurs.

Reduce Conversion: Reduce conversion if an error occurs.

ontinuous Stirred Tank Reactor

S

S

A

C

You must provide the reactor volume for CSTR’s in the Reactor Data window.

ptionally, you may also provide estimates of the product flow rate.

lug Flow Reactor

O P

Enter the following data for PFR’s in the Reactor Data window:

eactor Length: The total length of the reactor. Data for this field is mandatory.

ube Inside Diameter: The inside diameter of the PFR tubes. Data for this field is mandatory.

umber of Tubes: The total number of tubes in the PFR. Default is 1.

R T

N


Number of Points for

reactor length fProfile: The number of equidistant locations along the or the temperature profile. Default is 10.

Integration Options: You may select one of four integration options:

0

•

ce = 0.1%). • s)

nter th

d for Reactor Type

is packed with catalyst

presssure

• Pressure Profile • Pressure Drop Method • Packed Bed Pressure Drop

If you have selected Open Pipe under Reactor Type, the first three options

entioned above will be made available to the user. If you have selected Packed Pipe under Reactor Type, except Pressure Drop

ethod all other options will be made available to the user. Inlet and Outlet Pressure: Selecting this option will enable the Inlet and Outlet

section. User is prompted to enter data listed under the following section. • Inlet • Outlet

start entering the data for Location and Pressure.

• Fixed step size Runge-Kutta method. The Runge-Kutta method with 2steps is the default. Runge-Kutta method with user-specified step size.

• Gear integration method with user-specified gear tolerance (default toleranLSODA (Livermore Solver of Ordinary Differential Algebraic equationmethod with user-specified tolerance (default tolerance = 0.1%).

E e following data for PFR’s in the Pressure window: Select between the two options liste

• Open Pipe: Select this option, when the packing is not found in PFR. • acked Pipe: Select this option, when the PFRP

particles. Select an appropriate option from the list to enter the

ure specification • Inlet and Outlet Pres

m

M

Pressure Profile: Selecting this option will enable the Enter Data button. Click

Enter Data to open the Pressure Profile dialog box. Select the appropriate Location option from the drop-down list and


• Actual Tube Length • Percentage of Tube Length • Fraction of Tube Length

If you have selected Open Pipe in the Reactor Type section, Pressure Drop

In case ed Pressur

Pressur Enter Data button.

Method will be made available for selection. you have selected Packed Pipe in the Reactor Type section, Packed Be Drop will be made available for selection.

e Drop Method: Selecting this option will enable the Click on it to open the Pressure Drop Method dialog box.

Pressure Drop Correlation: Select the appropriate pressure drop method listed in the drop list.

Pressure Drop Correlation Significance

Beggs-Brill-Moody This is the default PRO/II method, and is the recommended method for most systems, especiallsingle phase systems.

y

Olimens Used for gas condensate systems, which uses the up and Eaton correlation to calculate liquid hold

Moody diagrams for friction factor.

Dukler-Eaton-Flanigan This hybrid correlation is for gas condensate systems that are mainly gas.

Gray systems. It is not suitable for horizontal lines. Recommended for vertical gas condensate

Hagedorn-Brown This method also is recommended for vertical pipe lines, and should not be used for horizontal pipes.

Mukherjee-Brill Used for gas condensate systems. This method must be used with care due to its discontinuities. Use at least 2 pipe segments to avoid failures due to changing flow regimes.

Beggs-Brill-Moody-Palmer This is the same as Beggs-Brill-Moody, but also includes the Palmer modification to account for liquid holdup, based on experimental data for uphill and downhill lines.

Convergence Tolerance: Supplies a relative convergence tolerance value for

the calculated pressure drop per reactor segment. The tolerance applies to changes between successive iterations. By default, PRO/II uses a one percent tolerance.


Flow Efficiency: This parameter is used for linear adjustment of the calculated pressure drop to match actual conditions. For given flow conditions,

te

calibration of results.

hite

a value for this field if desired.

lue can be supplied either in Absolute or Relative O/II supplies an absolute roughness of 0.0018 inch.

ure conditions, the

Packedethod

Pressure Drop Correlation: Select Ergun Equation to calculate the pressure drop across the packed bed.

Diameter of Catalyst: Enter the diameter of the catalyst. Data for this field is mandatory. Void Fraction of the Packed Bed: Enter the Void fraction of the packed bed. Data for this field is mandatory.

nder Shape Factor section, enter data for the shape of the catalyst. Select

Enter the sphericity of the catalyst.

decreasing this value causes an increase in the calculated pressure drop. The value may be greater than 100 percent. It is recommendedthat data for roughness or Moody friction factor be provided for accura

Moody Friction Factor: PRO/II usually calculates the friction factor from reactor

roughness and Reynolds number using the modified Colebrook-Wequations. You can supply

Roughness: A roughness va

units. By default, PR Acceleration Term: Check this option to include the acceleration pressure

gradient. Under certain high velocity or high pressBeggs and Brill acceleration term becomes unrealistically large and dominates the equation. Dropping the term often results in a better answer in these cases.

Bed Pressure Drop: Selecting this option will enable the Enter Data button. Click Enter Data to open the Packed Bed Pressure Drop Mdialog box.

Ueither of the two options depending on the catalyst. Sphericity: Shape of the Catalyst: Selecting this option will make the following option vailable to the user. Select either of the two options. a

• Spherical • Cylindrical: If you have selected Cylindrical, enter the Length.


Boiling Pot Reactor

y supply the following reactor calculation options for the boiling pot in the Reactor Data window:

You mareactor

nd relative mole fraction and enthalpy nged from their default values of

Note: IfwindowReactor- 457.87 Maximu ctor

Initial V ied

Compo duct

stimates… on the Reactor Data window. The number of Broyden trials before the Jacobian matrix is updated may be specified along with the derivative step size multiplier by clicking on the appropriate underlined linked text. The defaults are 3 trials and a step size multiplier of 0.01.

Tolerances: The absolute temperature a

tolerances for the reactor may be cha0.1º, 10-5, and 10-4 respectively.

the Fixed Duty option is specified on the main Reactor data entry , an estimate of the reactor temperature may optionally be provided in the Data window. The minimum and maximum temperature defaults of F and 4940.33 F may also be overridden.

m Liquid Volume: If a fixed volume is not supplied on the main Reawindow, you may supply a maximum liquid reactor volume in this window. A default of 3531.5 ft3 will be used if a value is not provided.

olume Estimate: An initial volume estimate may optionally be supplin this window.

nent product rate estimates may also be supplied by clicking ProE




Gibbs Reactor

For the Gibbs reactor, the user may provide a number of optional calculation options in the Reactor Data window:

Maximum Iterations: The maximum number of iterations allowed. The efault is 50.

e: The relative convergence tolerance. The default is 10-4 for isothermal conditions and 10-6 for adiabatic conditions.

Fibonacci Tolerance: The convergence tolerance for the Fibonacci search calculations. The default is 0.01.

may specify the physical property evaluation method by

al

tion: The physical property values from the previous You malinked te PRO/II default: The default generates an initial estimate of the product rates

using the PRO/II method. Average of all feeds: This uses the average of all feed rates to generate an

initial product rate estimate. Supplied reacting component rates: This option instructs the algorithm to use

the user-supplied values instead of calculating its own rate estimates for the reacting components. Supply reacting components and estimated rates in the Reacting Components window, which is reached by clicking

Parameters window. This opens by Phase Split Parameters on the Reactor Data window.

d Convergence Toleranc

In addition, you clicking on the underlined hypertext. The options are:

Evaluated at each step: This is the default setting. It evaluates physic

property values at each step of the search. This is the default. Used from previous itera iteration are used.

y select the product rate estimate option by clicking on the underlined xt. The available options are:

Reacting Components and Estimates on the Reactor Data window. The options to specify the parameters for the free energy minimization phase alculations are found in the Phase Splitc

clicking


he Phase Split PNote: T arameters window is available only if the Reactor

peration Phase is specified as Calculated on the Unit Reaction Definitions

atoms. Usually, the number of effective atoms is the number of atomic species..

n o or m ether in the same proportion. For example,

Owindow. See below for Unit Reaction Definitions. Specfying Reactions: The number of chemical reactions (i.e., the number of

REACTION statements) must equal the number of chemical species minus the number of effective

The number of effective atoms differs from the number of atomic species wheore atoms always occur togtw

consider the chlorination of ethylene:

Keq

242242 ClHCClHC +⇔+ There are 3 atomic species (C, H, Cl), but C and H always occur in a 1:2 ratio.

ctive is

itial Phase Estimate: This entry is the phase used for the initial reactor calculations. The user may select the vapor, liquid, vapor–liquid, liquid–

phase. The default is vapor–liquid.

First Phase Evaluation at Iteration: Specify the first iteration where the phase will be reevaluated. The phase should not be evaluated too early because the reaction results may still be far from the final solution. The default is 6.

hase Evaluation Frequency: Specify the number of iterations between phase evaluations. The default is 4.

inimum Phase Tolerance: When the molar ratio of a phase to the total quantity of material is less than this value, the phase is considered as non-existent. The default is 10-6.

Atomic groups can be provided in the Atomic Groups window. This window can be reached by clicking the User-specified Atomic Groups button on the Reactor Data window.

Therefore, the number of effective atoms is 2 (Cl and CH2). These two effeatoms represent the three chemical species, so only one chemical reactionllowed. a

The options available on the Phase Split Parameters window are: In

liquid, or vapor–liquid–liquid

P

M


nit Reaction Definitions

The reaction phase, heat of reaction, equilibrium data, and kinetic data for the reactor may be entered in the Unit Reaction Definitions window. Bring up this window by clicking Unit Reaction Definitions… on the main Reactor window. Note: Any data previously entered in the Reaction Data Category window will be transferred to the Unit Reaction Definitions window and used as default values. You can overwrite the data for a particular reactor in the Unit Reactions Definitions window for that reactor. Equilibrium Reactor You may supply the operation phase of the reactor in the Unit Reaction Definitions window. By clicking Equilibrium Data… in this window, you gain access to the fields where you may supply the following:

quilibrium Coefficients: Eight coefficients (A-H) of the equilibrium equation. Units: The temperature, weight, volume and pressure units of measure for the

equilibrium equation can be changed by clicking on the underlined linked text. Options are restricted to ºR or ºK for the temperature units.

Conversion Reactor

cients are to be etermined from the calculation results of the selected Calculator unit.

lied to use a single reaction to represent the overall r and, therefore, there is only a single reaction

id previously defined in the

eaction Data section.

ontinuously Stirred Tank Reactor and Boiling Pot eactor ou may supply the reactor operation phase, reaction activity basis and kinetic

rate calculation method in the CSTR Unit Reaction Definitions window. Reactor Operation Phase: The options are vapor or liquid phase for the CSTR,

but restricted to liquid phase for the BPR.

U

E

You may overwrite the stoichiometric coefficients for the first reaction in the selected reaction set by clicking the Define the Stoichiometry for the First Reaction check box. The values of stoichiometric coeffidFrequently, this feature is appreaction behavior in the reactodefined in the entire reaction set. The stoichiometric data displayed in the grbox are merely used to echo the reaction equationR CRY


Reaction Activity Basis: ForPartial Pressure or Fu

vapor phase, the options are Molar Concentration, gacity. For liquid phase, the options are Molar

tions s, heterogeneous reaction rate

expressions are allowed.

nius

For any of these methods, kinetic data can be entered through

Power Law: This is the default method.

e a n

2” …

, you can enter local values (i.e., specific just to this reactor) for variables to be used for the rate calculation. Use the upper left table to supply local values for an array of real variables, the lower left table for any array of integer variables and the upper right for an additional (Supplemental) array of real variables. These local data, kinetic reaction data specified in the selected reaction set, and thermo-physical property data of the reaction mixture will be provided to the selected kinetic subroutine for reaction rate calculations. Refer to the PRO/II User-added Subroutines User Manual for instructions on creating and installing UAS’s.

inetic Procedure: This option directs the CSTR module to use a user-supplied in line kinetic Procedure to perform reaction rate calculations. After selecting the name of the Procedure (which must be first defined in the Procedure Data section), you can enter values for local variables similar to the procedure for the User Added Kinetic Subroutine mentioned above. Additionally, you may provide the values for those procedure variables (PDATA) used by the selected Procedure.

ata that may be specified for the Plug Flow Reactor are the same as those escribed above for the CSTR.

re-exponential Factor: The pre-exponential factor for the kinetic power law rate equation. The default is 1.

Concentration, Fugacity or Activity. Currently, only homogeneous reaction rate expressions based on either vapor or liquid phase reacare allowed for the CSTR. For BPR'

Kinetic Rate Calculation Method: The options are Power Law, User Added

Subroutine or Kinetic Procedure. If the default is used, the reaction ratesare computed by power law kinetics in the form of the general Arrheequation. the Kinetic Data… button.

User-added Kinetic Subroutine: This option directs the CSTR module to us

User-added Subroutine (UAS) written in FORTRAN to perform reactiorate calculations. Specify a Subroutine Name in the Unit Kinetic Data window. The identifying arguments for the subroutine name “U1”, “U“U5” correspond to user-added subroutines “USKIN1” … “USKIN5” respectively. After selecting the user-added kinetic subroutine

K

Plug Flow Reactor Dd P


ctivation Energy: The activation energy for the kinetic power law rate

equation. The default is 0.

Temperature Exponent: The temperature exponent for the kinetic power law rate equation. The default is 0.

ase Component: A base component must be supplied for the kinetic reaction rate report.

eaction Order and Activity Basis: As is done in the Reaction Data section on a global basis, the default reaction phase, reaction activity bases for both vapor and liquid phases, component reaction phase and kinetic orders that are used to define the kinetic rate expression can be entered here as local data for this reactor. Click Reaction Order and Activity Phase to specify the kinetic reaction order and activity phase for each component which appears in the rate expression. The vapor activity basis is used for all components specified with vapor activity phase while the liquid activity basis is used for all components specified with liquid activity phase.

ibbs Reactor You may specify the phase of the reactor operation in the Unit Reaction Definitions window. The reaction phase options are Calculated (default), Vapor, Liquid, Vapor–Liquid, Liquid–Liquid or Vapor–Liquid–Liquid. If Calculated is selected, PRO/II determines the phase as part of the free energy minimization calculation. If a phase is selected, the calculations are based on the selected phase.

xtent of Reaction To specify the extent of a conversion reaction (in Equilibrium and Gibbs reactors only); click Extent of Reaction… on the main Reactor data entry window to open the Extent of Reaction window.

onversion Reactor ou may select the base component from which the conversion data were etermined. If the base component is not selected (select “None”), the

nts of the reaction are taken as the absolute moles may supply constants for the second order temperature-dependent

fractional conversion equation in this window. Default values for the constants are given in the table. Click on the underlined linked text to change the temperature units of measure for the conversion reaction. If the temperature units of measure are not specified locally, the problem temperature units are used.

A

B

R

G

E

CYdstoichiometric coefficiereacted. You


Equilibrium Reactor The base component for user-supplied reactions must be specified in the Extentof Reaction window. You may access this window via the Reaction Set winwhich contains a list of the reactions that have earlier been defined for the flowsheet. Upon choosing the desired equation, the Extent of Reaction windowappears. (The base components of built-in reactions such as Shift and

dow,

ethanation are predetermined and need not be supplied by the user.)

h to conversion either as a temperature or a

r temperature-dependent fractional onversion equation in this window. Default values for the constants are given in

e not

ibbs Reactor ided on a global basis in the Extent of

t

• You must specify the catalytic component with a reaction stoichiometry of ‘0.’ (Input/Reaction Data(Enter Data…)/ Reaction Definitions(Definition)/ Reaction Components). See the previous section on Reaction Data for more information on defining reaction data sets.

• You must specify the reaction order for the catalytic component as any number other than ‘0’ in the Reaction Order & Activity Phase window. This window may be accessed by clicking on the like-named button located on the Unit Reaction Definitions/Unit Kinetic Data window for the boiling pot reactor, or by the following path: Input/Reaction Data(Enter Data…)/Reaction Definitions/(K…)/Kinetic Reaction Data(Reaction Order & Activity Phase).

M You may specify the approacfractional approach. As was the case with the Conversion reactor, you may supply constants for the second ordecthe table. Click on the underlined linked text to change the temperature units of measure for the conversion reaction. If the temperature units of measure arspecified locally, the problem temperature units are used. GThe extent of reaction can be provReaction window (as a component percent converted, or as a componenproduct rate). The extent of reaction can also be specified for each individual reaction as a temperature approach or a base component product rate. Amount of Catalyst For boiling pot reactors only, you can specify the amount of a nonvolatile catalyst component on a weight or molar fraction, or total weight or mole basis in the Catalytic Components window (which may be reached by clicking Catalysts on the Reactor Data window). Before the button becomes active, the followingonditions must be met: c


Pressure For conversion, equilibrium, Gibbs reactors and CSTR’s, click Pressure on tmain Reactor window to enter the following reactor pressure options in the Pressure data entry window:

he

ressure Drop: Provide the pressure drop across the reactor. This defaults to 0

ssure at the reactor outlet.

let and outlet pressure or a pressure profile rcent or fraction of tube length) may

default is 0 psi), or the inlet pressure may be supplied.

Outlet: Either the pressure drop below inlet (the default is 0 psi), or the outlet

pressure may be supplied.

Print Options For all reactor types except the Gibbs reactor, the following print option is available in the Print Options window:

hermodynamic System The thermodynamic system of methods for the reactor calculations may be

Pif not supplied.

Outlet Pressure: The pre

For the plug flow reactor, either the inalong the reactor length (actual length, or pebe entered on the Pressure window: Inlet: Either the pressure drop below feed (the

Print Calculation Path for Enthalpy Balance: This option prints the calculation

path for the heat of reaction calculation. T

selected by choosing a method from the Thermodynamic System drop-down listbox on the main Reactor window.


Reactor, Batch

General Information The Batch Reactor unit operation models material production as a result of simultaneous and/or sequential reactions in the liquid contents of a reactor essel. Phase equilibrium analysis during the reaction allows for the tracking or

removal of vapor phase products. The Batch Reactor may be run in a true batch simulation mode, with the reactants charged to the reactor vessel prior to the

t

ams to provide the time-variant reactants to the batch unit. Implicit holding tanks are also considered for the

quantity ccumulated into a given product.

Currently, the Batch Reactor supports only liquid-phase reactions. A reaction may produce one or more vapor constituents. Whether the vapor constituent(s)

ill return to the liquid phase and again be available for reaction(s) will be

odynamic ystem drop-down list box in the Batch Reactor dialog box. Batch Reactor also

allows the use of electrolyte thermodynamic methods. Detailed Information

or detailed information about the use of the Batch Reactor unit operation, Modules User Guide.

v

onset of reactions, and product taken from the vessel at the end of reaction process, or in a semi-batch mode where reactants may be introduced throughouthe reaction process. Batch reactor calculations may also be integrated into a steady-state process simulation. The unit configuration automatically considers the presence of holding tanks for steady flow stre

product streams to provide a coupling of the time-variant process to the continuous process simulation environment. A representation of the product steady flow stream comes from an overall process time average of the a

wdetermined by equilibrium analysis done at the end of each time step. Thermodynamic System The thermodynamic system for the unit is selected by using the ThermS

Fconsult the PRO/II Add-On


Solid Separator

General Information The Solid Separator unit models the separation of solid phase material from a

mal

sure.

alculation Method es the option of specifying the fraction of the solid

t

utlet

hase)

l and VLLE Model for more etails. To access the main data entry window for VLE and VLLE calculations,

mixture of feed streams. The unit operates adiabatically at the lowest of the individual feed stream pressures. Feed and Product Streams The solid separator unit can have up to ten (10) feed streams. The inlet thercondition is determined by an adiabatic flash calculation at the lowest feed stream pres The solid separator requires both overhead and bottoms product streams. CThe solid separator providcomponents in the total feed that is removed in the bottoms stream. The defaulfraction of the solid components removed in the bottoms stream is 1.00. An adiabatic flash calculation is used to determine the product phases and the otemperature based upon the thermal condition of the combined feed. The solid separator unit supports both VLE (two phase) and VLLE (three pcalculations to determine the individual phase compositions. See the online Technical Information discussion entitled VLE Modedselect Tools/Binary VLE from the menu bar.




Splitter

General Information This unit may be used to split a single feed or mixture of feeds into two or more products of identical composition and phase condition. The outlet stream pressure may be specified, if desired, and an adiabatic flash used to determine the outlet temperature and phase. A choice of options is provided for splits in which insufficient feed is available to meet the specified product rates. Feeds and Products A splitter may have multiple feed streams. The lowest feed pressure is used for the pressure of the combined feed. A splitter must have two or more product streams. All product streams have identical compositions and phase conditions. Phase separation of product streams is not available in this unit, and, if desired, a Flash unit operation must be used for this purpose. Product Rate Specifications For a splitter with N product streams, N-1 product stream rates must be specified. Product rate specifications are supplied by clicking on the underlined hypertext strings in the Product Rate Specifications section of the Splitter main data entry window. All of the splitter product streams are listed and any one may be used for the unspecified rate. Specifications use the general specification format and are further described in the SPEC/VARY/DEFINE section of this chapter. Only specifications that are rate dependent are allowed, e.g., stream or component(s) rate total, stream or component(s) recovery, stream enthalpy, etc.


Outlet Pressure Specification litter products may be changed by applying a

site

o Splitter main data entry window:

ed

is the default option.)

d ons are satisfied and the resultant rates are

am Specification Order… on the Splitter main data entry indow. You can reset a stream specification by clicking Reset Stream

litter main data entry window.

e selected by choosing a method from the Thermodynamic System drop-down

dow.

The outlet pressure for the sppressure drop to the lowest feed pressure. This value is supplied in the Pressure Specification window, which is accessed by clicking Pressure Specification… on the Splitter main data entry window. When a pressure drop is supplied, the resulting outlet temperature and phase condition are determined by an adiabatic flash calculation from the compofeed inlet conditions. Inadequate Feed Rate Options There are two options for situations in which insufficient feed is available to satisfy all product stream rate specifications. They may be selected by radibuttons on the Satisfy Each Specification in Order Until Feed is Exhausted: Each

specification is satisfied in the order of the products until the feed is exhausted. The product stream that encounters insufficient feed islimited to the feed available and the remaining products are assignzero rates. (This

Satisfy Each Specification and Normalize Flow rates if Needed: All specifie

product rate specificatinormalized to the total feed rate. The product with the unspecified rate is assigned a zero flow.

The order of the product streams in the list box may be changed, if desired, by clicking Change StrewSpecification on the Sp Thermodynamic System The thermodynamic system of methods to be used for splitter calculations mayblist box on the Splitter main data entry win


Stream Calculator

General Information The ed streams and splits them intoalso beefining ount of each component in the stream.

eeds and Products The

ositive or n e Feed Scaling window in a mixed feed with the desired composition. If scale factors other

aterial balance. Multiple feed streams re

ms products are required. In ord efined. The feeds may be plit roduct stream created in the same stream calculator unit.

sized. Pse ms, and must not feed unit pe rticipate in the material balance of the flowsheet.

d into streams on r,

ed water and mixed (vapor + liquid). A mixed phase product is not product is also used

s t ations.

If any product, overheads or bottoms, has more than one stream attached, the phases must be allocated to the streams in the Product Phases window, which is

ccessed by clicking Product Phases in the overhead or bottoms product

Mode of Operation The munit so it is imp

Stream Calculator unit blends any number of fe two product streams with defined compositions and thermal condition. It may

used to synthesize a product stream based on the blended feeds, or by the amd

F

stream calculator may have any number of feed streams. Scale factors egative) may be applied to all feeds in th(p

order to createthan 1.0 are used, the unit will not be in m

flashed at the lowest feed stream pressure. a For stream splitting, both the overhead and botto

ate a stream, a pseudo-product must be der to cre and a ps

If there is no feed to the unit, only a pseudo-product may be synthe

virtual rather than actual streaudo-products are rations or otherwise pao

A multiphase product from the stream calculator may be separate

taining one or more phase. The allowable product stream phases are vapocliquid, decantallowed with a vapor or a liquid product. The decanted water

he second liquid product phase with rigorous VLLE calcula

awindows.

ode of operation is specified by the number of feeds and products attached to the ortant to connect the streams correctly before entering the unit data.


Stream Splitting In order to define the component splits, specifications must be entered in the Product Specifications window to define how much of each component goes into either the overhead or the bottoms product. Specifications may be on single compon or on ranges of contiguous nents. Several specifications may

ome may specify the amount of components in the overhead and oth ent must appear in one, an pec e component rates, recovery or composition

ay be specified.

The thermal condition of the products may optionally be defined in the Overhead P window. Pre ature specification is

ct, the product temperatures are set equal at a value

Calculator wind other temperature is calculated to meet the enthalpy balance. If both temperatures are given, duty is calculate

cifications may e a tem ure rise r b ubble point.

In order to synthesize a pseudo-product, specifications must be entered in the window to define how much of each component is ay be on single components or on ranges of

s red. At least one specific ot appear in a

e pseudo-product. If the unit has feeds, tes, recovery, or composition in the product may be specified.

Otherwise, the component rates must be defined. If th ined

and e pressure defaults to lowest feed

and the temperature is calculated to satisfy the enthalpy balance. If a plied, it is used only for the stream splitting enthalpy balance. Duty is

ents compobe required and s

ers the amount in the bottoms product. Each compond only one, s ification. Th

in a product m

roduct Conditions window and the Bottoms Product Conditionsssure defaults to the lowest feed pressure. If no temper

supplied for either producalculated from the enthalpy balance, using the duty entered on the Stream

ow. If one temperature is supplied, the

d.

Temperature speabove the feed, d

b perature value, the temperatew o ubble point or an approach to dew or b

nthesis Stream Sy

Pseudo-product Specifications in the product. Specifications mcontiguous component and several specifications may be requi

ation must be defined. Any component that does nspecification has a zero rate in thcomponent ra

ere is no feed to the unit, pseudo-product thermal conditions must be defions window. If there is a feed, the temperaturein the Pseudo-product Condit

ressure specifications are optional. Thppressure, duty is supnot used for the pseudo-product enthalpy balance. Temperature specifications may be a temperature value, a temperature rise above the feed, dew, or bubble point, or an approach to dew or bubble point. If there is no feed, a temperature rise specification is not allowed.


Negative Component Rates It is possible to specify the unit to generate negative component rates in a product stream. Options to handle this situation include:

• reset any negative rates to zero (this is the default)

ream Calculator may dynamic System drop-down indow.

• reset the rates to their absolute value • the unit should fail.

Thermodynamic System The thermodynamic system of methods to be used for the stbe selected by choosing a method from the Thermolist box on the Stream Calculator main data entry w




SPEC EGenePRO/II has an extensive system of cross-referencing for flowsheet parameters. Flowshe clude operating conditions for unit operations, calculated results ns, and stream flows, compositions, and properties. For

r a Pump, the calculated temperature for the simulated D86 ninety-five percent distilled

m are all flowsheet parameters.

relative to VARY

a flowsheet p ut value.

arameters: S op or stream p c on ted result)

red value, either on an absolute basi

unit ope n or stream flowsheet para is varied from the plied value.

nit operation parameter i ined by s-refere to anothewshee meter.

II uses a common format for the Specification (SPEC), VARY, and DEFINE ch fe is discussed s tely be Tables are also presented

rence availabilities of the flowsheet parameters for s and ion

atioa SPEC always must be a culated . The

s use the gene ed SPE mat to e the nce of the unit: Flash, Splitter, Column/Side Column, and Controller.

has the following general form:

eter = value within the default tolerance

A c y y

absolute aced by direct ntry.

/VARY/DEFINral Information

et parameters infrom unit operatio

example, the supplied outlet pressure foa dew point Flash, and temperature for a Column ct strea produ Most unit operation parameters may be either DEFINE'd or SPEC'dany other flowsheet parameter in the problem. Some unit operations may

arameter that would ordinarily remain constant at the inpow summarizes the methods for cross-referenThe table bel

pcing flowsheet

PEC: A unit eration erforman e specificati (calculas or relative bmust meet a

desi asis.

VARY: A ratio metersup

DEFINE: A u s def cros nce r

flo t para PRO/features. Ea ature epara low. with cross-refethe unit operat

streams.

Specific ns By definition, following unit operationperforma

calraliz

flowsheet reC for

sultdefin

A SPEC

Param

hoice for the Parameter and a numeric entry for the value must be supplied bclicking the underlined hypertext strings to gain access to the pertinent data entrfields. Optionally, the tolerance basis may be changed from the default to

or relative and the default tolerance value of 0.02 reple


Click o w. Choose the Stream o Select the in the drop-down list box

, clic ter hypertext a red eter e that is displayed. Note that only those

stream parameters that are e as a SPEC are available.

If the SPEC is not related to another flowsheet parameter:

Click OK to return to the unit specification. Click on the v rtext, and enter the desired numeri e for the

e a mathematical expression for the SPEC:

ct the = s n linke t and ct an option from the pop-up ces are as follows:

ator Primary parameter only (the default)

ator

imary parameter plus reference p eter

rameter minus reference meter CE)

Primary parameter divided by refere meter ATIO)

meter times reference parameter (TIMES)

Select the Reference Param lick on the Parameter text string, and select the desire rence meter from the list w s displayed.

nit or s parameters th valid for e in SPE re

available.

OK to n to nit spe tion windo ; then cli the ue linked strin nter the desired numeric value for the SP

The following examples illustrate the use of SPEC’s:

n the Parameter hypertext to access the Parameter windor Unit from the drop-down list box.

unit or stream name . Finally

paramk on the

from thParamewindow

nd select the desi unit or

valid for us

alue hype c valuSPEC.

To creat

Sele ig d tex selewindow. Choi

No Oper

+ OperPr aram(SUM)

- Operator

Primary pa para(DIFFEREN

/ Operator

nce para (R x Operator

Primary para

eter and cd refe para hich i

Note: Only u tream at are us C’s a

Click retur the u cifica w ck onval

text g to e EC.


Example 1: R re of stream S103 = 6.Un par hin a relative tolerance of 0.02

| |

fication Stream Name {Parameter Wind

ream] [Smeter

r Pressure

analog: AM=S103, RVP, S VALUE=6.0, RTOL=0.02

Duty f exchanger X103 / Duty of exchanger X104 = 1.0 with lative leran 0.001 ram r = a value within a relative tolerance of 0.

| | | [absolute [0.0

eam Unit Name {Par er Window} hange [X103

Reference: [/ Parameter =]

aramete Unit Name {Param Window}

[Heat Exchange [X104] Parameter

[Duty]

alog: =X103, DUTY, DIVIDE, HX=X104, DUTY, VA 1.0, RTOL=0.001

ser input.

in a flowsheet, there mu one VARY to provide one degVAR for the unit is implicitly def ed, i.e., n fine

explicitly by the user. For Flash units with specifications, the degree of freedom is the temperature when the pressure or pressure drop is given and the pressure when the temperature is supplied. Other unit Operations which have VARY’s are the Column/Side Column and the Controller. A VARY is always a flowsheet parameter that has a fixed versus calculated value in the flowsheet.

eid Vapor Pressu 0 it or stream

| ameter = a value wit

[6.0]

SpeciUnit/Stream [St

ow} 103]

Para [Vapo ]

KeywordSPEC STRE

A

Example 2: o re to ce of

Unit or stream pa ete 001 | | [1.0] ] 01]

Specification Unit/Str amet

[Heat Exc r] ] Parameter

[Duty]

Reference PUnit/Stream

r eter

r]

Keyword anSPEC HX

Note: [ ] denotes uLUE=

VARY For each SPEC st be ree of freedom. The in ot de d Y Flash


For Columns/S duct draw rate, or a heat duty. For example, the ledefined as a VARY pecification on the propan r th dina le ed rate would or constanin the flowsheet.

VARY’s that are a e rati r pplied outlet pressure fo ompress y be a Y for

e that flowsh t para would o rily hav xed in the wsheet n the nd, th ulated eratFlash it could not be u s a VAR ce this flows

at is determined b he flow t calculations.

struct ha he follo ng gen orm:

Vary Parameter

ck on the u erlined hypertext string to acce Variab wind

m this win w, se e typ ary, i.e., stream or unit type, in the -down list box.

Next, select t unit o am name in the adja ent drop-do n list Finally, click on the Paramete ext string and select the desired

meter to varied om the

nit or str m para ters th valid for use as a V are .

xampl llustrate the use ’s:

ple 3: The temperature for isothermal flash unit D101 is varied by a Controller.

Vary unit or stream parameter | |

tion Stream Unit Name {Var Window

[D101er

[Temperature

word analog: ARY FL H=D10 P s put.

ide Columns a VARY may be a feed stream rate, proan oil feed rate to a column may be

in order to meet a s e recovery foe column. Or rily, the an oil fe have a fixed t rate

Controllers haveexample, the su

ssociated with oth r unit opeor ma

ons. Fo VARr a C a

Controller. Not this ee meter rdina e a fi or constant valuefor a dew point

floun

. O other hased a

e calcY, sin

temp is a

ure heet

parameter th y t shee

A VARY con s t wi eral f

To enter a parameter:

Cli nd ss the ow. le

Frodrop

do lect th e of v

he r stre c w box. r hypert

para

be fr list.

Note: Only u ea me at are ARY available The following e e i s of VARY

Exam

SpecificaUnit/ iable } [Flash] Paramet

]

]

Key V AS 1, TEM

Note: [ ] denotes u

er in


DEFINE The DEFINE is used to dynamically define the value for a flowsh th as e culated value eet. Thus, tva ope be set to a value that is based on

sheet rameter. For example, the DE may be used to perature for a sotherm l Flash temper that is calculated

tlet st m plus degrees. This concept greatly en ces PRO/II, and, in fact, nearly every unit operation input

ay be DEFINE’d in PRO/II.

flowshee ameter:

Select the pa r in the approp ration. At this point, the efine button on the toolbar is a ted if th ame

’d. Clic Define to access the ition w . m this win w, sele the ch ox to ena he DEF

Parameter text string and select the desired pa er from window which is displayed.

nit or stream pa eters that are valid for use as a DEFINE le.

DEFINE d to another flowsh aramete k OKurn to the it windo If the is related to anothe flowsh

eter, e blish the approp mathemat al relationship. ematical xpressi s for a NE are created in a manner letely analogous that de ed above on page 309 for a SPt the re ce pa meter type in the same manner as sed to

m ter. Click the OK tton in child windows to return to the unit operation

stant:

Select Const from the Const tream/Un p-down ox i eter wi ow.

nter a numerical cons nt in the supplied data entry field. ng example illustrates the use of a DEFINE:

Example 4: DEFINE th rum D103 to be the temperature of stream S10

d on the Flash Second Specification]

from the Toolbar]

[Select the check box to set up the Defin

eet parameterat ordinarily hlue for a unit

a fixed vrating condition may

rsus cal in the flowsh he a

calculated flowthe tem

pan i

set for a

FINEaturea to the

Compressor ou rea 10 han the flow-sheeting capability of parameter m

To define a t par

ramete D

riate window for the unit opectiva

e par ter

may be DEFINE k Defin indow Fro do ct eck b ble t INE options. Click on the

theramet

Note: Only u

availabram are

If the is not relate eet p r clic to ret un w. r eet DEFINE paramMath

sta e

riate DEFI

icon

comp to scrib EC. Selec

select the priferen ra u

ary paramebu the

window.

For a con

ant ant/S it dro list b n theParam nd

E taThe followi

e temperature for Flash d4 minus 15 degrees.

[Select the temperature fiel

[Click Define

e]


| Primary Parameter: Unit/Stream/Constant Unit Name {Definition Window}

ream 104]

nce: [= Parameter - Parameter]

/Constan Value nt] 15.0]

FINE nearly identical in structure to the SPEC.

[St Parameter

] [S

[Temperature] RefereReference Parameter: Unit/Stream t [Consta [

Note that the DE is

Stream Parameters Available for Cross-r ferencing e SPE DEFIN VARYCS E1 2

Parameter Flash Split roller All Units Controller ter Column Cont

Temperature Yes - Yes Yes Yes Yes Pressure Yes - Yes Yes Yes Yes Enthalpy Yes - Yes Yes Yes - Mole Weight Yes - Yes Yes Yes - Total Flow Yes Yes Yes Yes Yes Yes Comp nt Yes Yes Yes Yes Yes - oneFlow Composition Yes - Yes Yes - Yes Phase Fraction Yes - Yes Yes - Density/Volume Yes - Ye Yes Yes s - Distill. Curve Yes - Ye Yes Yes s - Vapor Pressure Yes - Yes Yes Yes - Transport Propert

Yes - Yes Yes - Yes y

Refini Yes - Yes Yes Yes ng Property

-

Special User Property

Yes - Yes Yes Yes -

1. In general,condition.

any appli le strea rty be used t ine a uni ingNot all stream prop le to all un perating nditio

xception o he Colu , only the Controller m ry strea amet Column may vary the tot flow of stream.

cab m propeerties are app

maylicab

o defit o

t operat co

ns.

2. With the e f t mn ay va m par ers. The al a feed


Unit Parameters Available for Cross-referencing

Within Operation External Controllers

Parameter SPEC VARY DEFINE SPEC VARY Reference1

Calc ulatorResult - Yes Yes Yes Yes Yes

Parameter - Yes Yes

Stream C lator alcu

Temperature Yes Yes - Yes - Yes

Pressure - Yes Yes Yes - Yes

Delta T - Yes Yes Yes - Yes

Temp. Below Yes - Yes Yes - Yes Bubble Pt.

Temp. Above Dew Pt. - Yes - Yes Yes Yes

Delta P - Yes Yes Yes - Yes

Feed Cofactor Yes - Yes - Yes Yes

Duty - Yes Yes Yes Yes Yes

Frac. Overhead Yes - Yes - Yes Yes

Frac. Bottoms Yes Yes - Yes - Yes

Frac. Product - Yes Yes Yes - Yes

Overheat Rate Yes - Yes - Yes Yes

Bottoms Rate - Yes Yes Yes - Yes

Product Rate - Yes - Yes Yes Yes

Comp. Overhead Yes - Yes - Yes Yes

Comp. Bottoms Yes - Yes - Yes Yes

Comp. Product Yes - Yes - Yes Yes

Con troller

Specification Yes Yes Yes Yes Yes

MVC

Specification Yes Yes Yes Yes Yes

Optimizer

Specification Yes Yes Yes Y Yes es

Constraint Yes Yes Yes Yes Yes



External Within Operation Controllers

Parameter SPEC VARY DEFINE Reference1 SPEC VARY Column

Reflux Yes Yes Y Yes Yes Yes es

Reflux Ratio Yes Yes Yes Yes Yes Yes

Duty Yes Yes Yes Yes Yes Yes

Feed Rate - Yes Yes Yes Yes

Draw Rate Yes Yes Yes - Yes

Specification Yes Yes - - Yes

Percent of Flood Yes Yes - - Yes Yes

Max % of Flood - Yes Yes Yes - Yes

Downcomer B/U Yes - - Yes Yes Yes

Max D.C. B/U - Yes - Yes Yes Yes

CS Approach Yes - - Yes Yes

Flood Approach - Yes - Yes Yes

Tray Diameter - Yes - Yes Yes Yes

Max Tray Diam. - Yes Yes Yes - Yes

Condenser Pres - Yes Yes - Yes

Top Tray Pres - - Yes Yes Yes

Tray Delta P Yes - - Yes Yes

Column Delta P - - Yes Yes Yes

Tray Temp Yes - - Yes Yes Yes

Feed Tray No - - Yes Yes Yes Yes

Draw Tray No - - Yes Yes Yes Yes

Duty Tray No - - Yes Yes Yes Yes

Tray Effic Factor - Yes - Yes Yes Yes

P/A Rate - Yes Yes - Yes

P/A Return T - Yes Yes - Yes

Product Moles - - Yes Yes Yes




Parameter SPEC VARY DEFINE Reference1 SPEC VARY Thermosiphon Reboiler

Circulation Rate Yes - - Yes Yes Yes

Vapor Fraction - - Yes Yes Yes Yes

Liquid Fraction - Yes Yes - Yes Yes

Outlet Temp Yes Yes - - Yes Yes

Delta T incr. Yes Yes Yes - - Yes

LLEX

Specification - - Yes Yes

Top Tray Pres Yes - - Yes

Feed Rate - Yes Yes Yes

Draw Rate Yes Yes - Yes

Duty - Yes Yes Yes

Pump

Temperature - Yes Y - es

Outlet Pres - Yes Yes - Yes Yes

Delta P - - Yes Yes Yes Yes

Pressure ratio Yes Yes - - Yes Yes

Work - Yes - Yes

Head - - Yes Yes

Efficiency - - Yes Yes

Pipe

Diameter - - Yes Yes Yes Yes

Max velocity - - Yes Yes Yes Yes

Average velocity Yes - - Yes Yes

Delta P - - Yes Yes Yes

Duty - Yes - Yes Yes Yes

Rel Roughness - Yes - Yes Yes

Abs Roughness - Yes Yes Yes -

Friction Factor Yes Yes - - Yes

Flow Efficiency - - Yes Yes Yes

Length - - Yes Yes Yes




Parameter SPEC VARY DEFINE Reference1 SPEC VARY Heat Transfer - - Yes Yes Coeff. Yes

Ambient Temp - - Yes

Delta P Max - Yes -

K-Factor - - Yes Yes

Simple E nger xcha

Duty - - Yes Yes Yes Yes

Cold Delta P - - Yes Yes Yes Yes

Cold T Out - - Yes Yes Yes Yes

Cold Liq Fr - - Yes Yes Yes

Cold Subcool Yes - - Yes Yes

Cold Sup’heat Yes - - Yes Yes

Hot Delta P - Yes Yes - Yes Yes

Hot T Out - Yes - Yes Yes

Hot Liq Fr ac - Yes - Yes

Hot Subcool - - Yes Yes

Hot Sup’heat - - Yes Yes

LMTD - - Yes Yes

Zoned LMTD - Yes - Yes

Overall U - - Yes Yes Yes Yes

Area - Yes Yes Yes - Yes

U * Area - Yes - Yes Yes Yes

Ft Factor - - Yes Yes Yes Yes

Approach - - Yes Yes Yes Yes

MITA (Pinch) - - Yes Yes

Min. Approach - - Yes Yes Yes Yes

Rigorous He changer at Ex


Overall U - - Yes Yes Yes

Estimated U - -

Area - Yes Yes Yes - Yes




Parameter SPEC VARY DEFINE Reference1 SPEC VARY U*Area - - Yes Yes Yes

LMTD - - Yes Yes

Shell T Out - - Yes Yes Yes Yes

Tube T Out - - Yes Yes Yes Yes

Tube Foul Factor - Yes Yes - Yes Yes

Shell Foul Factor - Yes Yes - Yes Yes

Required Foul Factor - - Yes Yes Yes

LNG Heat Exchanger

Duty - - Yes Yes

Cell i Temp Out - - Yes Yes Yes Yes

Cell i Duty - - Yes Yes Yes Yes

Cell I Delta P - - Yes Yes Yes

U*Area - - Yes Yes

LMTD - - Yes Yes

MITA - - Yes Yes

Splitter

Temperature - - Yes Yes Yes

Pressure - - Yes Yes Yes Yes


Specification - - Yes

Valve

Temperature - - Yes Yes



Compressor

Outlet Temp - - Yes Yes Yes Yes

Outlet Pres - - Yes Yes Yes Yes


Compr. Ratio - - Yes Yes Yes Yes

Actual Work - - Yes Yes Yes Yes




Parameter SPEC VARY DEFINE Reference1 SPEC VARY Head - - Yes Yes Yes Yes

Adiab. Efficiency - - Yes Yes Yes Yes

Poly Efficiency - - Yes Yes Yes Yes

Max. Press - - Yes Yes

Cooler DP - - Yes Yes

Cooler Temp - - Yes Yes

Temp Estimate - - Yes Yes

RPM - - Yes Yes Yes

Curve RPM - - Yes Yes Yes

Expander

Outlet Temp - - Yes Yes Yes


Pressure Drop - - Yes Yes Yes Yes

Expans. Ratio - - Yes Yes Yes Yes

Actual Work - - Yes Yes Yes Yes

Head - - Yes Yes Yes

Adiab. Effy - - Yes Yes Yes Yes

Min. Pressure - - Yes Yes

Flash

Temperature - - Yes Yes Yes Yes


Delta Pres - - Yes Yes Yes Yes


Specification - - Yes

Entrainment - - Yes Yes

Pseudo Prod. - - Yes

Mixer / Splitter

Tempera ture - - Yes



Specifica Yes tion - -




Parameter SPEC VARY DEFINE Reference1 SPEC VARY Pump

Temperature - - Yes Yes Yes



Press Ratio - - Yes Yes Yes Yes

Work - - Yes Yes

Head - - Yes Yes

Efficiency - - Yes Yes

Equilibrium Reactor





Conversion i - - Yes Yes Yes Yes

Stoic. Coeff. - - Yes

Conversion Reactor




Duty Yes - - Yes Yes Yes

Con - Yes Yes Yes Yes version i -

Gibbs Reactor








Parameter SPEC VARY DEFINE Reference1 SPEC VARY PFR (Plug-Flow Reactor)



Delta Pres - - Yes Yes

Inlet Pres. - - Yes Yes

Delta P In - - Yes Yes


Tube Diameter - - Yes Yes

Length - - Yes Yes

No. of Tubes - - Yes Yes

U (HTC) - - Yes Yes

Max Veloc. - - Yes Yes Yes

Temp In - - Yes Yes Yes

Temp Out - - Yes Yes

Pre-exp. Factor - - Yes Yes

Acti - Yes Yes Yes vation E i -

Con Yes Yes Yes version i - -

CSTR/Boiling Pot Reactor





Conversion i - - Yes Yes

Pre-exp factor i - - Yes Yes Yes

Activation E i - - Yes Yes Yes

Volume - - Yes Yes Yes

Min. Temp. - - Yes Yes

Max. Temp. - - Yes Yes

Max. Veloc. - - Yes Yes


Unit Parameters ailabl Av e for Cross-referencing


P DEFINE eference1 SPEC VARY arameter SPEC VARY RDe ssuring pre

Final Pres. - - Yes Yes Yes Yes

Relief Pres. - - Yes Yes Yes

Final Time - - Yes Yes Yes Yes

Relief Time - - Yes Yes Yes

Relief Duration - - Yes Yes Yes Yes

Valve Constant - - Yes Yes Yes

Valve Back P. - - Yes Yes

Valve Coeff. - - Yes Yes Yes

Critical Flow Factor - - Yes Yes Yes

Init. Wet Area - - Yes Yes Yes

HT Area - - Yes Yes Yes

HT Coeff. - - Yes Yes Yes

HTC Factor - - Yes Yes Yes

Vapor HTC - - Yes Yes Yes

Liquid HTC - - Yes Yes Yes

Coeff. C1 - - Yes Yes Yes




Coe - - s Yes ff. C5 Yes Ye

Final Temp - Yes - Yes Yes

Final Dut - es Yes y - Yes Y

Final Vent Rate - - Yes Yes Yes

Vessel Volume - - Yes Yes

Liquid Holdup - - Yes Yes

Vessel Diameter - - Yes Yes

Vol. Corr. Factor - - Yes Yes

Ht. of Holdup - - Yes Yes

Vessel Weight - - Yes Yes




Parameter SPEC VARY DEFINE Reference1 SPEC VARY Vessel Cp - - Yes Yes

Tan-tan Vessel ength - - Yes YesL

Tan-tan Vessel Height - - Yes Yes

Tim te - e S p - Yes Yes

Isen pi - - es Yes tro c Eff. Yes Y

Hea c - Yes Yes t S ale Fac. - Yes

Area Scale Fac. - - Yes Yes Yes

1 Available for any SPEC or DEFINE.


User-added Unit Operations

ral Information GeneThe PRO/II User-added Unit Operation capability enables users to add their own FORTRAN subroutines to simulate any type of unit operation or to perform calc to the PRO/II program and it is then accessed via the graphical user interface in the same way as any other unit operation. The Us ta and ma lculation subroutines. Other information, such as input and output dimensional units, is also available. See the PRO/II Data Transfer System and User-Added Subroutine User Guide for information on writing and interfacing User-added Unit Operation subroutines.

he developer of the User-added Unit Operation can also customize the User-d Unit Operation Data window to request only data which may be required

for the calculations. Note: If transport properties are required in the User-added Unit Operation, you must select a suitable method in the Thermodynamic Data. Selecting the Subroutine When a User-added Unit Operation is laid down on the PFD, the User-added Unit Operation window opens in which the user must select the name of the required subroutine. Calculation or Output Execution A User-added Unit Operation may be executed during the flowsheet

n

feeds and/or products are allowed. The default is to perform the calculations for the user-added unit as part of the normal flowsheet convergence alculations.

alculation time: The User-added Unit Operation is calculated as part of the

normal flowsheet convergence. Additional calculations may be performed at output time and an output report may be produced.

ulations on flowsheet parameters. The subroutine must first be linked in

er-added Unit Operation has access to the PRO/II physical property day call the PRO/II flash and property ca

Tadde

convergence calculations or at output time only. The User-added Unit OperatioData window will show when the selected subroutine is calculated. This affects whether

c

C


Output time: If the User-addflowsheet data for ca

ed Unit Operation requires only converged lculations and reports, it can be executed at output g the flowsheet convergence.

Feeds and Products The User-added Unit Operation may have up to ten feed streams. The

routine can retrieve each feed separately. They are not mixed or flashed. If hey re ixed, the user must do this in the subroutine. User-added Unit Operations which are to be executed during the flowsheet convergence must hav t Those which are only executed at output time need no User-ad g the flowsheet con g s. These may be any com ded Unit Operations which are only executed at outp t duct streams. Str m

the Us roduct, they will be re laid down on the PFD. The user may need

are presented in the correct order to the User-

ser-added Unit Operation Data

les:

alues, available to SPEC, VARY, DEFINE) ta

Dat a User-added Unit Operation using either a “Customized Dat n standard “Developers Data Entry Window.” These two choi s .

ata also may be entered into the variables in the Real Data table using the iables in the Real Data table are available to

SPEC, VARY and DEFINE constructs. Data in the other tables are available only internally in each user-added subroutine.

time rather than durin

subt a to be m

e a least one feed stream. any feeds. t have

ded Unit Operations which are to be executed durinver ence may have up to ten product streambination of phases. User-adut ime cannot have any pro

ea Reordering If er-added Unit Operation has more than one feed or pshown in the order in which they weto reorder the streams so that they added Unit Operation. For example, the User-added Unit Operation may alwaysfeed vapor to the first product stream and liquid to the second. Reordering is done in the User-added Subroutine - Stream Reordering windowaccessible by clicking Reorder Streams on the Uwindow.

Entering Data Data are supplied to the User-added Unit Operation in four tab

• Real Data (PARAM v• Supplemental Da• Integer Data • Heat Balance Data

a c n be supplied to a a E try Window” or the ce are explained below

DPRO/II Define feature. Only the varother unit operations by using


“Cu toUse h indow” to use for all user- user-added calculation ubroutine. The standard PRO/II User-added Unit Operations use the default

ed try window for a user-added calculation subroutine, the name that is

elected for it replaces one of the default names in the list of available subroutine d played unit is laid down on the PFD).

tomi Entry Window mized be used for a specific user-added tine, two ASCII files must be created in the directory specified

n gDir= e PVISION.INI file. These two files are called USER described below.

g to the subroutines USER41 - USER60. Each line in the file has

f a typica

1.2.

hese ilable ser-added calculation subroutines being displayed when a User-added Unit peration is laid down on the PFD:

ile USERXX.INI his file contains the variable names and array locations for all of the Real, upplemental, Integer, and Heat Balance Data values that the specific user-dded calculation subroutine requires or that can be input by the user. For a ser-added subroutine with a customized data entry window, a user will only be ble to enter values for the data items specified in this file. The “XX” in the name f the USERXX.INI file corresponds to the respective user-added subroutine ferenced, i.e. the user-added subroutine USER41 with a user-specified name

f “PIPE DP Routine” above would need a “USER41.INI” file to describe the quired data for the calculations. An example of a typical USERXX.INI file is

hown below:

s mized” Data Entry Window rs ave the option of defining a “Customized Data Entry W

added unit operations that utilize a specificsnames USER41 - USER60 (displayed as US1-US20). If you create a customizdata ensnames (the list is when a user-added Creating a “Cus zed” Q DataTo create a custo

subrodata entry window to

calculation ufi ntry in theby the “UserCo

UASLIST.INI and XX.INI and are File UASLIST.INI This file contains the user-specified names for specific user-added calculation subroutines that will be displayed in place of the default names US1 - US20, correspondintwo entries; the entry number in the list of user-added subroutine names, and the actual text that is to be displayed for the user-added subroutine. An example o

l UASLIST.INI file is shown below:

PIPE DP Routine Stream Heating Value

entries in the UASLIST.INI file will result in the following list of avaTuO FTSauaoreores


Example: USER41.INI file:

he first entry on each line indicates to which data array the variable belongs.

subroutine.

must be enclosed in double quotes (“”).

The fourth entry on each line indicates whether or not data entry for the item is Optional or is Required. The default is Optional, and this entry is not required.

he USER41.INI file shown above will result in the following quired data values and variable names being shown in the custom window

Operation where the user-ubroutine when the unit was laid

own on the PFD as shown below.

ustomized UAS Data Entry Window tomized User-added Unit

ar in the SERXX.INI file.

he limits on the number of variables that can be entered for each array are hown below. These limits are:

• Real Data - up to 500 elements • Supplemental Data - up to 10,000 elements • Integer Data - up to 250 elements • Heat Balance Data - up to 10 elements

Each table shows the name(s) of the variable(s) for which values must be entered. They will scroll if they contain more than four rows. All data entries displayed using a customized data entry window are required. No checks on validity or completeness of the data are carried out until the User-added Unit Operation is executed.

IPARM 1 iPPrint ControllN Required RPARM 1 iPDiameter (in)lm Required RPARM 2 iPLength (ft)lg Required ... SUPPLE 1 “No. Of Segments” Required ...

TThe second entry is the array number where the data value entered by the Userwill be stored for access by the User-added calculation The third entry is the label to be displayed for the variable in the customized data entry window. This entry

The entries in tredisplayed for data entry, for any User-added Unit selected “PIPE DP Routine” as the user-added sd

CThe order in which the variable labels appear on the cusOperation Data window is the same as the order in which they appeU Ts


The Standard Developer’s Data Entry Window elopers of User-added Unit Operations. It is ser-added Unit Operation if a “Customized

ata Entry Window” has not been defined for the specific unit.

he developer’s data entry window has no variables names and any number of ariables may be entered up to the limits of each array.

hese limits are:

• Real Data - up to 500 elements • Supplemental Data - up to 10,000 elements • Integer Data - up to 250 elements • Heat Balance Data - up to 10 elements

he user must know which elements of each array are used by the User-added nit Operation and enter the array element number along with the value. Values ay be entered for any or all of the elements in the arrays. The elements defined eed not be contiguous and may be entered in any order.

RO/II knows nothing about the data requirements of a User-added Unit Operation and so no restrictions are imposed in the data entry. Note: Unless the user defines a custom Data Entry Window for a specified User-added Unit Operation, the data entry for that unit will be via the developers' data entry window.

Modular User-Added Unit Operations The new modular interface for user-added subroutines first released in PRO/II 6.0 continues to evolve with this release. The interface addresses many of the limitations of the “classic” user-added interface described above. Enhancements have been made to all phases of simulation, including input, data cross-checking, data storage, calculations, and output reporting. These features are fully supported through both key words and the PROVISION Graphical User Interface. Highlights of the new functionality for user-added unit operations include:

• Almost no restrictions on the number of subroutines or their names (no reserved names).

• User-defined data supports user-defined text labels that may be used in key word files to identify input data. Unlimited data size; defined and organized by the developer, including integer, double precision real, and text data. Scalar through two-dimensional arrays are allowed.

A special window is available for devhe default window displayed for a Ut

D Tv T

TUmn P


• Automated keyword input prostructures and data labels. Cr

cessing, using the user-defined data oss-check calls the user-added subroutine

to perform its own data validation, in addition to generic cross-checks performed automatically by PRO/II.

f the d

“native” PRO/II error processor.

• Full support for user-defined output reports written to the standard

ed subroutines and PRO/II.

Modular User-Added Utilities Modula uired by n iv sent a user alternative to calculation

already available in PRO/II. Currently, the RATEFRAC® rate-based olumn algorithm is the only model that utilizes modular utilities. Available user-

added utilities are supported for the following calculations in a column segment: • Interfacial Area between fluid phases

• Binary mass transfer coefficients in each fluid phase

• Heat transfer coefficients

dded subroutines is beyond the scope of this Guide. Please refer to the “PRO/II User-Added Subroutines User

RATEFR

• Completely dynamic execution. No restrictions on the location odynamic-link libraries created by the developer. The DLL’s may be storein a single location for access by multiple users.

• Extensive new features for handling stream data, performing flash calculations. Improved access to the

PRO/II text report.

• Full support for multi-sided models, such as heat exchangers.

• User-defined units of measure, used for all data transfer between the user-add

• Full GUI support, including unit lay-down and custom input windows. User-developers may create these using the “AutoGui” feature with the user-defined data structures and labels.

r utilities are called from PRO/II to perform specific calculations reqat e PRO/II features. They always repre

methodsc

Detailed Information Comprehensive discussion of modular user-a

Guide”.

AC® is a registered trademark of Koch-Glitsch, LP.


Ele teneral Information

ontaining electrolytes. See the PRO/II Add-On Modules User Guide for more information. The following unit operations can be used with this electrolyte version:

• Flash

nger, LNG heat exchanger • Conversion reactor, Equilibrium reactor • Stream calculator

dynamic Models

a ensities.

is not possible to define individual methods for K-value, enthalpy or density models.

N : used to calculate the following properties: (1) Non-aqueous electrolyte systems; (2) Free water decant;

city.

ase:

• LLE and Hydrate Systems

To select an electrolyte model:

c rolyte Module GTc

he optional Electrolyte Module of PRO/II allows you to handle systems

• Pump • Valve, Mixer, Splitter • Pipe • Simple heat excha

• Heating/Cooling curve • Calculator • Controller, Optimizer • Column (Electrolytic Algorithm, see below)

hermoT

Eight built-in electrolyte models in PRO/II simulate aqueous systems in a wide range of industrial applications. The models apply to fixed component lists withpredefined set of thermodynamic methods for K-values, enthalpies and dItwhen using electrolyte thermodynamic

ote Electrolyte models may not be

(3) Water dew points; (4) Hydrocarbon dew points, (5) Entropy and heat capa

he following electrolyte models are available in this releT

• Amine Systems • Acid Systems • Mixed Salt Systems • Sour Water Systems • Caustic Systems • Benfield Systems • Scrubber Systems


• Click Thermodynamic Data on the toolbar to open the Thermodynamics Data main data entry window.

• Select the Electrolyte option in the Category list box. • Choose an appropriate electrolyte model.

The suggested range of applicability for the electrolyte models is summarized elow:

32-390 F (0-200 C) ressure: 0-200 atm

Dissolved gases: 0-30 mole %

ou may add your own models, specifically suited to your application, by using ,

SCI support office for more formation.

s. e but

o avoid this, select the electrolyte enthalpy ermodynamic systems in a mixed

a atio

b Temperature: P

Ionic solutes: 0-30 ionic strength Amine Systems Pressure: 0-30 atm LLE Systems Organic solutes: 0-10 weight % Ythe PRO/II and the Electrolyte Chemistry Wizard available from OLI SystemsPLC. If you wish to do this, contact your nearest SIMin Note: Take care when using non-electrolyte and electrolyte thermodynamic

methods in the same application. The PRO/II electrolytic models use a different enthalpy basis from that used for other thermodynamic systemWhen both are used, PRO/II automatically takes care of the differencit may appear to be confusing. Tmethod for all non-electrolyte thpplic n. All systems will then use the electrolyte model basis.


Electrolytic Column Algorithm (ELDIST) This column algorithm was designed to solve non-ideal aqueous electrolytic

istillation columns involving ionic species. It uses a Newton-Raphson method to olve the mass balance, vapor/liquid equilibrium and specification equations imultaneously. The K-values and enthalpies are supplied by the electrolyte ermodynamic model.

he Electrolytic Column Algorithm is selected from the Column Algorithm drop-own list box on the Column main data entry window.

ote: Electrolytic thermodynamic models only support VLE and so total phase raws are not permitted.

Advantages and disadvantages of the Electrolytic Column Algorithm are given below:

dvantages

) Rigorously models ionic equilibrium systems. ) Solves highly non-ideal distillation columns.

isadvantages

) Side columns are not supported. ) Pumparounds and tray hydraulics are not available. ) Certain Column Specifications and Variables are not permitted.

dssth Td Nd

A (1(2 D (1(2(3




Simsci Add-on Modules

Add-on modules can be obtained in this version of PRO/II to extend the

nctionality of the program. These modules include units for modeling polymer s, separating solid components from feed streams, blending streams with

ifferent component and refinery inspection properties, as well as Profimatics reformer reactor models.

IMSCI POLYMER CSTR Unit Operation RO/II contains features for handling polymers (e.g., van Krevelen property

prediction method, polymer moment attributes, ALM thermodynamic method, and olymer flash).

he SIMSCI Polymer CSTR Add-on Model offers you the capability of modeling a olymerization reactor operating under the following conditions:

• Single monomer producing a linear homo-polymer. • Single phase reaction (effects of heat and mass transfer on the mass

transport are not considered). • Ideal CSTR (steady-state, well-mixed, constant volume reactor). • Free radical polymerization kinetics. • Bulk or solution polymerization.

This reactor unit has been added to PRO/II as part of the SIMSCI Add-on Models olymer CSTR) and is available from SIMSCI as the SIMSCI Polymer CSTR odule.

equired Data for the Polymer Reactor Unit

his version of PRO/II does not allow you to enter the necessary Component, tream, or Thermodynamic Data via required the data entry windows. However, ou can enter the necessary Polymer CSTR data using the Polymer CSTR data ntry window for the SIMSCI Add-on Model.

o enter data for the Polymer CSTR:

nce you have entered your simulation data, including the data for the Polymer STR, but excluding any polymer-specific thermodynamic, stream, or component ata, you will need to do the following:

fusystemdhydrotreating and

SP

p Tp

(Pm R

TSye T

OCd


• Export the simulation data to a PRO/II keyword file.

cific data to the keyword file. ation

problem in Run-Only mode.

er to the PRO/II Add-On Modules User Guide.

ed w.

nput is required.

end two or more streams to give one product tream with different component and refinery inspection properties. This unit is elected from a drop-down list box on the SIMSCI Add-on Units main data entry indow.

The feed streams should have different thermodynamic methods for this unit to nction correctly, but this is not necessary. The unit thermodynamic method ust be different from any of the feed stream thermodynamic methods.

he following data must be provided:

• Product stream temperature.

he product stream pressure may also be supplied, but if it is not given, the pressure will be set to the lowest feed stream pressure.

The unit thermodynamic method component properties will be recalculated from e blend of the feed streams properties and will then be stored as part of that

thermodynamic method data storage. Only petroleum and assay generated omponent properties will be recalculated; it is assumed that Library component

properties do not change in the flowsheet. The unit first recalculates the normal oiling point, molecular weight and specific gravity for all the petroleum omponents. These recalculated properties are then used to re-characterize all e other petroleum fraction properties such as the critical temperature.

• Add the necessary polymer-spe• Import the modified keyword file into PRO/II and run the simul

For additional information, ref

SIMSCI COMPONENT PROPERTY REPORTER Unit Operation

This unit prints out the Component Properties and Refinery Inspection Properties for all the thermodynamic methods in the current flowsheet. This unit is selectfrom a drop-down list box on the SIMSCI Add-on Units main data entry windo

o data iN

SIMSCI BLEND Unit Operation The Blend unit allows you to blssw

fum T

T

th

c

bcth


Using the Blend Unit with Refinery Inspection Properties

ecified in the input will also be blended from e specified blending method for that

property. It is necessary that every thermodynamic method must have the same refinery inspection properties specified and that these properties must use the same property method and blending basis in order for the unit to work. A check is done at input time to check that all the methods in the problem have the same refinery properties, methods and bases specified. You can request this check to be done, at calculation time, on the methods used in the current unit using the IPARM entry. Note: Requesting this check at calculation time should be used with care and is not recommended.

SIMSCI RESET Unit Operation The RESET unit allows you to reset the product stream enthalpy datum using the thermodynamic method specified within the unit. This unit is selected from a drop-down list box on the SIMSCI Add-on Units main data entry window. Only one feed and one product stream are allowed for the unit. Note: If you try to import a keyword file that specifies more than one feed or product stream, PRO/II will produce an input error. The feed stream pressure is always kept constant and you are required to specify whether the temperature, enthalpy, dew point, bubble point or vapor fraction is kept constant. The new product stream conditions will be calculated based on the option specified. The available calculation options are entered through the first value in the Integer Data for Unit field and are as follows:

Value Entered Calculation Option

1 Specify the product stream at the feed stream temperature 2 Specify the product stream at the feed stream enthalpy 3 Specify the product stream at the feed stream vapor fraction 4 Specify the product stream at the dew temperature 5 Specify the product stream at the bubble temperature

Note: In this version, a warning message will alert you if the thermodynamic method of the unit operation is different from the thermodynamic method of any of the feed streams. This warning message applies to all unit operations except for the RESET unit, the BLEND unit and any Profimatics reactor models.

Any refinery inspection properties spthe feed streams properties using th


SIMSCI Profimatics Reactor Unit Operations drotreater and Reformer Reactor unit om a drop-down list box on the SIMSCI Add-on

These units model Profimatics Hyoperations and can be selected frUnits main data entry window.


Valve

General InformThe Valve is used to across a pressure res re for the exit fluid is com suming that the operation is adiabatic.

us calculations may be performed for both VLE and VLLE systems. Feeds and Prod

ed A valve may have on uct streams. The product phase condition for valve operations with valve units with two ospecified in the ValveProduct Phases… on ntry window.

ses allowable include: vapor, liquid, decanted water, heavy liquid, and mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with vapor and liquid products and is not allowed when four product streams are specified.

Outlet ConditioThe outlet condition f ton on the Valve main data e

• Pressure drop

Thermodynami

he thermodynamic system of methods to be used for valve calculations may be selected by choosing a method from the Thermodynamic System drop-down list ox on the Valve main data entry window.

ation model the Joule-Thompson effect that occurs triction such as a valve, orifice plate, etc. The temperatuputed by as

Rigoro

ucts A valve operation may have multiple feepressure is assum

d streams, in which case the inlet to be the lowest feed stream pressure.

e or more prodone product stream is automatically set by PRO/II. Forr more product streams, the product phases must be Product Phases window which is accessed by clicking the Valve main data e

Product pha

ns or a valve is selected with the appropriate radio butntry window as:

• Outlet pressure

c System T

b




Wiped Film Evaporator

General Information The Wiped Film Evaporator unit operation (WFE) provides the capability to model

e separation of solvents and/or monomers from a polymer melt. A Wiped Film Evaporator should be used when the removal of volatiles from a viscous polymer

side the wiped film evaporator continually on the wall of the evaporator. As the melt

Detailed Information or detailed information regarding operating modes, data requirements, and

e of applicability of the Wiped Film Evaporator model, consult the PRO/II Add

th

melt is diffusion limited. The blades inmix and spread a thin film of the meltmoves down the evaporator, the volatiles diffuse out of it and into the vapor space of the evaporator. The volatiles are pulled out of the evaporator under vacuum.

Frang

-On Modules User Guide.




Cunning and Viewing a

et

his chapter describes how to run a simulation, interactively change the calculation sequence, use breakpoints, and view calculation history and results.

Using the Run Palette

e Run palette. If all hoose Run, PRO/II will complete.

Display Run palette:

Select/deselect the View/Palettes/Run option from the menu bar. The Run palette appears/disappears on the PRO/II main window.

hapter 10 RFlowsheT

The PRO/II Run palette shown in Figure 10-1 provides options for data verification, interaction with the simulation (running the simulation by stepping through the units) and viewing convergence or simulation results. You access these features by choosing the appropriate button on threquired input data have not been provided when you cdisplay a warning message telling you which data are in

/hide the

Figure 10-1: Run Palette


The palette displays push buttons that execute or access a feature:

Operation Description Status Displays the global messages for the current simulation. Check Data Checks the input data to determine whether there are any

data inconsistencies. Run simulation, either from the beginning or from

reakpoint. Check Data is automatically performed, if necessary.

Executes the a b

Step Steps through the execution of the simulation by stopping unit operation in the calculation sequence. at each

Stop The re stopping.

Interrupts or stops the simulation while it is executing.program completes its current calculation befo

Set Breakpoints Selects the units you want to assign as breakpoints. The program then executes the simulation, stopping at these breakpoints.

Goto Starts the executioselect the unit by clickin

n from any specified unit. You can g the mouse cursor on the desired

unit in the flowsheet.

Messages Displays the calculation history as it is being produced. This window can be displayed when the PRO/II calculation engine is executing the simulation, in which case, the

roceeds. history will be updated as the calculation p

Vie results of the highlighted unit sly run nits or

reams, if desired. If the simulation has been run previously, you can view its results without executing it again by opening the appropriate .OUT file.

w Results Displays the detailed output operation or stream in the flowsheet of the previousimulation. You can review the results of multiple ust

Show Breakpoints

Shows which units are assigned as breakpoints by displaying their icons in a different color. Clicking the button a second time disables the breakpoint display.

Chapter 11 Printing and Plotting 367

Checking the Simulation Status Useview the status messages for the current simulation. This button is ighlighted as a selectable operation only if Check Data has been previously

around the Status button indicate the Check Data results:

A re

A y generated.

A b t no rrors were found when Check Data was last erformed.

al status messages for your simulation:

tatus window le window.

Status to display the Flowsheet Status window. This window allows you to global

hinvoked either directly from the palette or indirectly from execution of the Run operation. The following colors

d border indicates that errors were found.

ellow border indicates that warnings were

lack border indicates tha ep

In all cases, the status can be viewed by selecting Status.

To see the current glob

Choose Status from the Run palette. The Flowsheet Sappears. The Check Data results appear in a scrollab

Figure 10-2: Flowsheet Status

If errors were detected, you must correct your simulation data.

Choose Close to exit the Flowsheet Status window.

Correct your simulation errors.

If no errors were detected, run the simulation.


Understanding the Unit Color Coding Cues As the simulation progresses, you will observe that the individual units change olor. Refer to the following for the default color codes. c

Unit Color Coding Color Significance

Yellow Unit operation at initial condition.

Red Unit operation has not been solved.

Green Unit operation in process of being calculated.

Blue Unit operation has been solved.

Dark Blue Unit operation has been calculated. This color is displayed only when you use the Run button, and a unit operation was previously calculated.

Purple Breakpoint set directly before or after a unit operation. Using the No Colors Feature If you do not wish to see the unit icon colors update as the flowsheet solves, you

et a performance benefit by deselecting the View/Show Run Colors option n the menu bar. This option operates exactly like the Run button on the Run

the simulation finishes or

n close th again on Messages or by double-clicking on the

Use Ru

can gopalette, but unit icon colors are updated only whenstops at a breakpoint. Running the Simulation When you begin executing the simulation, the flowsheet convergence can be viewed in a Messages window by clicking Messages on the Run palette. You ca

is window by clickingMessage window’s control-menu box.

n to begin executing the simulation. The program starts from:

The first unit, if this is the first run; The unit at which the calculations were stopped; The unit you selected using the Goto option.

The Run option automatically runs Check Data.


To begin executing the simulation:

ng simulation execution, you may cho

y-unit basis by selecting Step.

If the ru Flowsheet Status

xt unit

o step through the execution of the simulation:

ing Run palette.

If the Messages window is open, you can observe that execution ceases after completion of the current unit.

StoppUse Stop he program completes its current calculation before stopping.

the

Choose Run from the Run palette.

When stepping through or stoppiose to examine the status of the simulation.

Select Status from the Run palette. You may continue stepping through the simulation on a unit-b

Alternatively, you may choose to run the simulation without stepping byselecting Run.

n encounters problems, warnings will appear in the window. You have the option to close the window and correct the warnings or continue the run by clicking Run Simulation.

Stepping Through Simulation Execution Use Step to execute the calculations for the current unit (stopping at the nein the calculation sequence). In this manner, you can step through the executionof the simulation by stopping at each unit operation in the calculation sequence. T

Choose Step from the float

ing Simulation Execution to interrupt or stop the simulation while it is executing. T

To stop or interrupt simulation execution:

Choose Stop from the Run palette.

The unit calculations stop. The next unit in the calculation sequence becomescurrent unit, as indicated by its color.


Using Goto

initiation

o start the execution from a specified unit:

The sele nt unit. When execution completes on this

Usingou can before the unit

loop usi To set b or:

kpoint

you want to set a breakpoint. Choose Close to exit the Breakpoints window.

PRO/II purple and updates the values in the

To dele

RO/II u oints window to show that there is no

The Bre nd identifiebreakpo e during the current session. PRO/II does not save breakpoint information.

e Breakpoints window appears.

Use Goto to start execution from a selected unit. This can be invoked at program or after execution pauses while stepping or stopping.

T

Select a unit on the PFD. Choose Goto from the Run palette.

cted unit becomes the curreunit, its Goto status is removed.

Breakpoints set a breakpoint on any unit. Breakpoints can beY

operation, after it, or both. You can set breakpoints using the cursor or by utilizingthe Breakpoints window. In addition, you can set breakpoints before and after a

ng the Breakpoints window.

reakpoints using a curs

Choose Set Breakpoints from the Run palette to turn on the Breamode. This automatically brings up the Breakpoints window. Select the unit for which

turns units selected as breakpoints

Breakpoints window.

te a breakpoint in Breakpoint mode:

Select the unit. PRO/II will no longer show this unit as purple.

pdates the values in the BreakpPlonger a breakpoint attached to this unit.

akpoints window lists all unit operations in the calculation sequence as the breakpoint type for each unit: (before, after, both). Units without a int are considered “Off.” Breakpoints are for us

To set breakpoints using the Breakpoints window:

Choose Set Breakpoints from the Run palette. Th

Note: Click Show Breakpoints to highlight those units or loops where breakpoints have been previously set.


Figure 10-3: Breakpoints Window

Set the desired breakpoint type by clicking on the check boxes. You canset before, after, or both.

Select a unit from the list.

lect.

To close th

o turn off Breakpoint mode:

Vie Viewing Calculation History Use Messages to view the calculation history that has been produced so far. This can be used while the simulation is executing, after the simulation finally ends, or when the simulation reaches a breakpoint.

The breakpoint for the unit is set based on the breakpoint placement you se

e Breakpoints window:

Choose Close. Note: Closing the Breakpoints window does not turn off Breakpoint mode. T

Choose Set Breakpoints on the Run palette a second time.

wing Results


To view the calculation history for the simulation thus far:

Choose Messages from the Run palette. The Messages window appears. This is a multi-line data window that is continuously updated. Viewing Results for Streams and Unit Operations Use View Results to display results for the selected stream or unit in the default text editor. To view results for a stream or unit:

Select the desired stream or unit.

Click View Results on the toolbar, or Choose View Results from the Run palette, or Right-click on the unit and select “View Results” (for most unit operations

other than columns), or Right-click on the unit and select “View results (Molar Units)” (for

columns only), or Right-click on the unit and select “View results (Mass Units)” (for columns

w process unit and stream results via the Unit List and Stream List (Go To) windows:

Click unit or stream

only). Alternatively, you can vie

to open the Unit List or Stream List window

. Highlight the desired unit or stream.

Click View Results . The r creates a single ASCII file.

e

Viewi s The stream property tables provide a convenient means to display selected results for a group of streams on the PFD. Four predefined report formats are

dified as desired and/or additional formats am properties selected for

isplay, the titles anpro

PRO/II report generatoThe default text editor will be used to display the standard PRO/II output for thselected stream or unit.

ng Results in Stream Property Table

supplied. These formats may be moed by the user. In addition to the stremay be defin

d d number of decimal places to display for each stream perty may be chosen by the user. A quick check of the material balance for



the prob the prob

electig

Include All Streams: This is the default. All the streams in the flowsheet are s list box.

s: Only those streams entering the owsheet as products are displayed

or

Streams list box may be sorted using the Up, own, Top and Bottom buttons.

ables

The appearance of a stream property table may be customized with options provided on the Stream Property Table window. The property list (format) to use

e selected in the Property List to be Used list box. Note that perty lists supplied by PRO/II, the user may also prepare

w for

strings of components may be grouped into a single component p for printout. For example, a C6 plus component group might be used to

group all components from NC6 and heavier. Any number of component groups may be set up. To specify a component group, click Define Component Groups… on the Stream Property Table window to access the Group Components window. This window may be used to define and name component groups, as well as to edit existing component groups. The appearance of the steam property table itself may be altered by the user in the Stream Property Table window. Options include multiple rows per table, displaying the row grid lines, and setting the widths for the borders, lines, and property cell characters.

lem may be accomplished by displaying the source and sink streams forlem.

S ng Streams for Property Tables Stream property tables are set up from the PFD palette by addina stream properties icon to the PFD.

Double-click the stream properties icon on the PFD to display the Stream Property Table window.

Choose the method for available stream selection by selecting the appropriate radio button:

displayed in the Available Stream Include Flowsheet Source/Sink Stream

flowsheet as feeds and leaving the flin the Available Streams list box, producing a material balance check fthe flowsheet.

The streams in the DisplayedD

Customizing the Stream Property T

for the display may bin addition to the prospecial property lists for selection. See Defining Stream Property Lists beloinformation.

ontiguous Cgrou

Defining Stream Property Lists (Formats) Stream property lists are defined and edited via the Define Property List window. This window is accessed by choosing Options/Stream Property Lists from the menu bar. PRO/II provides four default lists that may be edited if desired:

Short Property List: Temperature, Pressure, Molar flow rate, Phase.

Material Balance List: Temperature, Pressure, Molar flow rate, Phase, Molar- based composition.

Stream Summary: Phase, Molar flow rate, Standard liquid flow rate, Temperature, Pressure, Molecular weight, Enthalpy, Specific enthalpy, Mole fraction liquid, Reduced temperature, Reduced pressure, Acentric factor, UOP K-value, Standard liquid density, Vapor and liquid molar flow rate, Vapor and liquid mass flow rate, Vapor and liquid volumetric flow rate, Vapor and liquid molecular weight, Vapor and liquid specific enthalpy, Vapor and liquid CP, Vapor and liquid density, Vapor and liquid viscosity, Vapor and liquid thermal conductivity, Liquid surface te ion.

Comp. Molar Rates: Molar component and total flow rates, Temperature, Pressure, Enthalpy, Molecular weight, Mole fraction vapor and liquid.

To

To crea

nter a name for the new list

window and click the button to transfer the property to the Property Description Format list box.

The property that was selected is expanded in this window, with the addition of a description and a format which may be edited in the data entry fields provided. The description for the property may be changed from the default value and the number of decimal places for printout may also be changed if desired.

When editing an existing property list, properties may be selected in the Property Description Format list box and edited, deleted, or rearranged as desired.

In addition to such properties as temperature, pressure, enthalpy, etc., property items such as “double line,” “line,” and “text” may be incorporated in a property list to add blank lines and special headings.

ns

edit an existing property list:

Use the drop-down list box to select the property list name. te a new property list:

Click New to access the New List window and elist in this window. This window also allows you to select an existingfrom a drop-down list box to be copied to create the new list.

To add a property to a property list:

Select the property in the Select Properties drop-down list box on the Define Property List


Running a Case Study Case Study is an executive level feature that allows you to perform studies onbase case solution by altering parameters selectively and rerunning the simulation.

a

Access the Case Study main data entry window by selecting Input/Casestudy Data… from the menu bar.

Figu tudy Main Data Entry Window

Enable the window by checking the Define Case Study box.

In this window, you can specify the changes you want to make to your input

arameters and to define the Results you want to examine. You may define as

t the

er click on the data field and enter a new name.

re 10-4: Case S

Pmany parameters and results as you want. Parameters: The table of parameters initially has one row. You may insert or

remove as many rows as you wish. Parameter Identifier: The parameter identifier defines the way you wan

output data to be presented after the Case Study has been executed. Adefault identifier (here “PARAM1”) is supplied. To change the parametidentifier,


o open ange.

you have specified appears in place of the original text.

tart Value: Click Base Case Value to open the Parameter Start Value window

value for the parameter. The starting value rameter in the base case. When you close

ycle number. By default, the starting cycle is one (1).

End Cycle: Cycles after the end cycle use the value in the end cycle. If

necessary, enter a new end cycle number. The end cycle defaults to the value of the start cycle.

You may insert or remove as many rows as you wish. You may define a Result as one flowsheet

tion of two flowsheet parameters or as a function eter and a constant. See SPEC/ VARY/DEFINE

using and changing mathematical operators

n you define how you se Study has been

r,

only) parameter to open the Parameter arameter that you want as a Result or as

er (or constant) that you want of the function you are defining.

Exe e

Parameter: You must identify a parameter to change. Click Parameter tthe Parameter window. Select the parameter that you want to chWhen you close this window, the parameter

Swhere you define the startingdefaults to the value of the pathis window, the starting value will be displayed.

Start Cycle: The start cycle is the cycle after which the incremental changes are

implemented. Cycles before the start cycle use the value in the base case. If necessary, enter a new start c

Step Value: Next, define the value of the incremental step change per cycle. The new step value will be displayed.

Results: The table of results initially has one row.

parameter or as a funcof one flowsheet paramin Chapter 9 for details on and composing specifications.

Result Identifier: The result identifier will be used whe

want the output data to be presented after the Caexecuted. A default identifier is supplied. To change the result identifieclick on it and enter a new identifier.

First Parameter: Click on the first (or

window where you select the pthe first element of the function you are defining.

Second (Reference) Parameter: Click on second parameter to open the

arameter window where you select the parametPas the second element

cution Options: Select from the Execute: list to execute the base case only

or the base case and the case study. If you do not want to execute all thcycles of the case study, select Base Case and Specified Cycles and specify a beginning and ending cycle.


Viewing Case Study Results Select Output/Case Study/Plots… or Output/Case Study/Table… from the menu bar to specify the format of the Case Study results. Enter a name (required) and an optional title for the plot or table. Click Data… to open a window where you specify the parameters and results to plot or tabulate. The dialog also has entries for labels of plot axes, table rows and columns, and other related data. Running Files in Batch Mode You can execute one or more PRO/II ASCII keyword input files or flowsheet simulation files in Batch Mode from within PRO/II. The keyword input file may be one that was created using a text editor or word processor, or one that was previously created using the Keyword File Export capability. You can also execute flowsheet simulations that were created using

RO/II from the GUI, or were created by importing a PRO/II keyword input file.

ile for each

hile executing simulation problems in batch mode, you can continue to work with other Windows applications. You can terminate the currently executing roblem or the batch execution mode completely by pushing the Terminate

un buttons, respectively.

o sele a previou

Close the currently open simulation. Choose File/Run Batch from the menu bar. PRO/II displays the Run

s Selection window.

P Batch execution generates the standard PRO/II ASCII output fsimulation it runs. This occurs regardless of whether the selected files are keyword input files or simulation (.prz) files. W

pCurrent Problem or Terminate Batch R T ct a PRO/II keyword input file, simulation file (or group of files), or

sly stored execution list file:

Batch - Input and/or Simulation File


Figure 10-5: Run Batch - Input and/or Simulation Files Selection

Initially, there are no keyword input (*.INP) or simulation files (*.PR1) displayed in the File Sequence window. There are two methods of adding keyword input or simulation files to the file sequence list:

ng the Add Files… button, or Load a previously saved list of files using the Load List… button.

o select the desired keyword input or simulation files:

Click Add Files… PRO/II displays a list of available existing keyword input files. The default file type is keyword files (*.INP). You can change the file type to simulation files (*.PR1, *.PRZ) using the Files of type drop-down list-box.

Select the files explicitly usi

T


Figure 10-6: Run Batch - File Select

Type or select the name of the file that you want to execute. You can

tory. Only the keyword input files ctory will be added to the list of

put ulation Files Selection window.

To load an existing list of keyword input and/or simulation files:

Click Load List…. PRO/II displays a list of available existing execution list files. The default file type is Run Batch List (*.LST). These files contain the complete path and name of keyword input and simulation files in the execution order previously specified by the user. An example of the typical contents of an execution list file is given below: C:\SIMSCI\PROII_W\USER\CASE1.INP C:\SIMSCI\PROII_W\USER\CASE2.INP C:\SIMSCI\PROII_W\USER\CASE3.INP Execution list files may include comment lines (beginning with a semicolon ;), and include list file directives given by #include followed by the .LST file name. An example is given below:

select multiple files within a given direchighlighted in the currently selected direfiles to execute when you exit this window. Click OK to validate your selection and return to the Run Batch - Inand/or Sim


; This is a comment C:\SIMSCI\PROII_W\USER\CASE1.INP C:\SIMSCI\PROII_W\USER\CASE2.INP ; The following is the list of files to load. ; contains flash problems #include flash.LST Note: The #include directives may be nested, e.g., in the example above, flash.LST itself could contain the directives #include dewpt.LST and #include bubpt.LST.

0-7: Run Batch - Load File List Figure 1

Type or select the name of the execution list file that you want to load.

iven directory. Only the list files ll be used to create the

ted.

s Selection n list file(s) will have

ox. Selected les displayed in

You can select multiple list files within a ghighlighted in the currently selected directory wilist of keyword input and simulation files to be execu

Click OK to validate the selection and exit. When you return to the Run Batch - Input and/or Simulation Filewindow, the contents of the previously selected executiobeen expanded and are now displayed in the File Sequence list bles will be added to the bottom of the list of previously selected fifi

the File Sequence list box.


Revising the File Execution Sequence Order After creating a list of files, you can revise the order of file execution. Simply highlight one or more files in the list and us the Move Up, Move Down, Move Top, and Move Bottom buttons. Clicking the Remove button only removes the highlighted file from the list; not from the hard drive.

Creating an Execution File List You can store a list of keyword input or simulation files as an Execution File List that can be retrieved and executed at a later date.

Click Select from Lists…. PRO/II displays the Run Batch - Save File List As window containing the execution file list options.

Figure 10-8: Run Batch - Save File List As

e.

a *.LST file in ASCII format. Enter a name for the Execution List Fil Click OK to store the list as


ExecWhen you return to the Run Batch - Input and/or Simulation Files Selection window, you can begin the execution of the specified file list. To start the batch mode execution of the list:

Click OK.

The specified list will be executed in the order shown in the File Sequence box. When the execution is complete, a message will be displayed to notify you that the batch mode execution has been completed.

Terminating Execution of a Batch List You have the choice of terminating the currently executing simulation problem, or terminating the batch mode execution completely.

To terminate batch mode execution of the selected keyword files:

Click Terminate Current Problem to terminate the currently executing problem.

Problem execution stops after the current unit calculations are complete.

Note: You can terminate an executing problem only during calculation.

To terminate batch mode execution completely:

Click Terminate Batch Run to end the execution.

esults of Batch Execution of Keyword Input (*.INP) Files: By default, the ro f

spe t will e locat ding .OUT file(s).

esults of Batch Execution of Simulation (*.PR1, *.PRZ) Files: By default, the rogram will not delete the simulation files that remain after the batch mode xecution of specified simulation files (*.PR1, *.PRZ), or the ASCII format tandard output report located in the corresponding .OUT file. You can open the sulting simulation file(s) with the File/Open command, and then proceed to

enerate reports or modify the simulation flowsheet as desired in PRO/II.

hatever type of file (keyword input or simulation) was executed in batch mode, ou can always view and edit the corresponding standard ASCII output files with ny ASCII-capable text editor or word processor.

uting the Batch List

Viewing Output ResultsRp gram deletes the simulation files that remain after batch mode execution o

cified keyword input files (*.INP). The standard PRO/II ASCII output repored in the corresponb

Rpesreg

Wya


Chapter 11 Printing and Plotting Thisand pri

d lved

without re-executing the simulation.

mat:

Format s Data,

chapter describes how to generate, view and print reports, and generate

nt plots. Printer setup is also described.

Defining Output Reports PRO/II provides a variety of report options for streams, unit operations andimensional units. You can change the output format of a report for any sosimulation To define the output for

Choose Output/Report Format from the menu bar. The Reportmenu appears with options for Units of Measure, MiscellaneouStream Properties, and Unit Operations.

Figure 11-1: Report Format Menu

etting Miscellaneous Data Report Options ou can set the report dimensions, identify the data you want to include and set e product stream scaling using the Miscellaneous Data option.

SYth


To set misce

llaneous data options:

window appears.

Choose the Option/Report Format/Miscellaneous Data from the menubar. The Miscellaneous Report Options

Figure 11-2: Miscellaneous Report Options


Setting Product Stream Scaling To change the scale stream flow rate:

Choose Product Stream Scaling… from the Miscellaneous Report Options window. The Report Options - Product Stream Scaling window appears.

Select the Scale Stream Flow rate checkbox. Specify the stream to be scaled, the components to be scaled, and the

scaled flow rate.

Figure 11-3: Scale Stream Flow Rate

es and return to the PFD.

Click OK twice to commit the chang


Setting Stream Properties Report Options To set the stream properties report options:

Choose the Output/Report Format/Stream Properties menu item. The Stream Property Report Options window appears (Figure 11-4).

Select the desired flow rate, fractions, or percent values for the Standard Component Flow rate/Composition Report.

Click OK to commit the entries and return to the PFD.

Figure 11-4: Stream Property Report Options

ettin easure Report Options s of measure you set

so set Problem Units of Measure for output reports. You of-

making individual value adjustments.

o set units of measure for output reports:

Choose the Units of Measure menu item from the Report Format menu. The Default Units of Measure for Problem Output Report window appears.

g Units of MS

In addition to the global, problem and unit level default unitr input data, you can alfo

can change the output values for all the fields by applying a different units-easure set, or bym

T


Figu

ault values from another set or replace the default values, as necessary.

change the vapor condition settings for this problem. The Problem Standard Vapor

ars.

re 11-5: Default Units of Measure for Problem Output Report

Click Initialize from UOM Library… to extract def

Optionally, click Standard Vapor Conditions… to

Condition window appe

Figure 11-6: Problem Standard Vapor Conditions


Specify the desired standard vapor conditions. ndows to return to the PFD.

port options:

Click OK in the child wi Setting Unit Operations Report Options You can set specific print options for each type of unit operation.

o set the unit operations reT

Choose the Output/Report Format/Unit Operations menu item. The Unit Operation Output Report Options window appears.

Figure 11-7: Unit Operations Output Report Options


Select the desired unit operation. Choose Print Options… The Column Print Options window appears.

Figu

re 11-8: Column Print Options

Select the items you want to include in a Column Report.


Optionally, click Plot Column Results… to set optionsColumn Plot Options window appears.

for a plot. The

Figure 11-9: Column Plot Options

Click OK in the child windows, then Close to commit the entries and

return to the PFD.


Generating a Report You can generate a report to a file. Use the Define Format option to define the format of the report. To generate a report from an executed simulation:

Click Generate Reports on the toolbar, or choose Output/Generate Reports from the menu bar.

As PRO/II generates the report, a window appears, displaying the status of the report as it runs. Once the report has been generated, the default editor window appears displaying the contents of the report. PRO/II appends an .OUT extension to the current simulation name and saves the file in the USER directory.

Viewing a Report To view a previously generated report of the current simulation:

Choose Output/View Report from the menu bar.

rated report for any simulation:

Printing a Report

list box in the Print window. Click OK.

To view a previously gene

Choose File/Open from the menu bar. Select Report Files in the List Files of Type list box and choose the

desired file.

To print the report:

Print from your text editor while viewing the report, or Choose File/Print from the menu bar. Select Report in the Print drop-down


Plotting PRO resu

• Distillation column profiles (temperature, flow rates, composition, and separation factor)

• Zones analysis for simple and rigorous heat exchangers • Phase envelopes • Heating/Cooling curves

Plot can be displayed using PRO/II’s Plot Viewer or Microsoft Excel. The section Setting Up the Plot Driver later in this chapter describes how to select and configure the plot driver.

GeTo gAss

urve

To g

lot from the menu bar. PRO/II displays the Generate Plot window as shown in Figure 11-10.

/II generates and displays a variety of plots for input data and tabulatedlts. The following plots can be generated:

• Input Data • Assay stream analysis Output Results •

s

nerating a Plot enerate an assay stream analysis plot, select View Curve... on the Stream

ay Definition window. Three curves will be generated:

• The actual user input distillation data• The regressed TBP c• The component cuts generated.

enerate one of the output results that PRO/II supports:

Choose Output/Generate P

Figu

re 11-10: Generate Plot Window


By default, the Units for Selection list box displays all the Unit Operations in the you check the Selected Units option, the PFD for which plots are available

ill be shown.

ion in the Units for Selection list box, the Available e for that unit. You may select a plot then

plot. If the plot requires additional options to be chosen, e to an Options… button. Currently, additional data is

olumn Plots.

:

Choose Vapor and Liquid Compositions; then choose Options… to open the Column Vapor and Liquid Composition Plot window.

flowsheet that can provide data for plots. Ifonly those units you previously selected onw When you select a unit operatPlots list box displays all plots availablclick Plot… to display the the Plot… button will changrequired only for Distillation C Plotting a Column

o obtain a plot of vapor and liquid compositionsT

Figure 11-11: Column Vapor and Liquid Composition Plot

Enter the additional data required. Plot….

Click


Setting Up the Plot Driver PRO/II can display plots using its internal Plot Viewer or Microsoft Excel (throuversion 7). The PRO/II Plot Viewer is a built-in utility that also prints plots.

gh

icrosoft Excel provides a complete set of formatting features. With Excel, you an change plot colors, axis titles, and other attributes to create a presentation-

quality graph.

ally set up the options in this

list box.

Mc

To select and configure the plot driver:

Choose Options/Plot Setup on the menu bar to open the Plot Setup dialog. PRO/II’s installation wizard initiwindow.

Select the desired plot driver using the drop-down

Figure 11-12: Plot Setup Window

To configure the currently selected plot driver:

Press Setup to display the Setup Plot Driver window. You cannot configure the PRO/II Plot Viewer (option “SIMSCI”).


F ure 11-13: Setup Plot Driver Window

he configuration options are:

Driv r

Driv Comma ommand line to invoke the plotting application. Options: Additional driver-specific options.

ig

T

er File: The complete path and filename of the dynamic link library (DLL) fothe plot driver.

er Function: The function name to invoke the driver.

nd Line: The full c


ThPRO

not supported. If and formatting features for your plot,

cho To

K. You can ter.

enu. To expo n ASCII file:

comma-delimited) and click OK. To the clipboard:

w menu. Setting Up the Printer To

Choose File/Print Setup from the menu bar. Select a printer. Select paper orientation and size and click OK.

rinting a Flowsheet Layout o print a flowsheet diagram:

Choose File/Print from the menu bar. Select the range of pages and click OK.

e Plot Viewer /II’s Plot Viewer utility lets you view a plot, print it, copy it to the clipboard,

and export its data to a file. Modifications of plot attributes are you want access to comprehensive editing

ose the Excel plot driver.

save a plot:

Choose File/Save As from the Plot window menu. Enter the desired plot file name and click O

send a plot from the Plot window to your plot

To send a plot to the plotter:

Choose File/Print from the Plot window m

rt a plot to a

Choose File/Export from the Plot window menu. Select the file type (tab- or

copy the plot image to

Choose Edit/Copy from the Plot windo

set up the printer:

PT


Chapter 12

Workplace omization of PFD appearance. You can control unit

and stream appearance, modify the stream property tables, and set the font style used on your PFD. Changing Unit Operation SPRO/II allows users to specify a different icon, name, label, and label starting number for each type of unit operation. Figure 12-1 illustrates the global Unit Style dialog.

Customizing the PFD

This chapter surveys the cust

tyles

Figure 12-1: Global Unit Style Window


Changing the Unit Icon Globally To Change the Style of A Unit Globally:

Choose Options/Drawing Defaults/Unit Display… from the menu bar. The Unit Style window shown in Figure 12-1 appears.

Select the type of unit operation you want to change using the drop-dlist box at the t

own op of the dialog.

in the Auto Label Format field. In Figure 12-1, the ng “F%d”.

The he flow r the changes are made.

ntax of Au

The Auto Label Format defines the template used to generate labels for one type of unit operatio w). Each type of

tax of the template is:

hat res.

e, an Auto Label Format field containing FDrum-%d-A. would generate a series of labels in the form FDrum-1-A, FDrum-2-A, FDrum-3-A, as three new unit operations of this type are added to the flowsheet.

Auto Label Starting Number:

er used to generate the series of

ts

D

to represent the unit operation. Simply highlight the desired icon in the scroll box. The selected icon will be used for all unit operations of this type subsequently added to the flowsheet drawing.

Changing the Font of the Label

ch the label.

Enter label changes field contains the stri

changes do not apply to any unit operations already present on tsheet drawing. They apply only to new unit operations added afte

Sy to Label Format:

n (see Auto Label Starting Number belounit operation uses a separate Auto Label Format. The syn

“prefix %d suffix”,

where prefix and suffix represent any text, and %d is a macro command tdisplays the unit number. The label may not contain spaces or undersco

For exampl

This field defines the starting unit numblabels defined by the Auto Label Format field. The number must be an integer equal to or greater than zero. For example, setting this field to 7 starunit numbering at 7. Assuming the Auto Label Format for the Flash unit operation were FDrum-%d, subsequent Flash units placed on the PFwould be labeled FDrum-7, FDrum-8, and so forth.

Using Alternative Icons

The Unit Style dialog includes a list of icons available

Click the Select button in the Unit Labels group box of the Unit Style dialog to open the Font dialog. The topic Changing the Default Font (later in this

apter) describes modifying the type face and type size used in

Chapter 12 Customizing the PDF Workplace 399

C

hanging the Unit Icon for a Single Unit

Figure Unit Menu

cify a different display icon for

ly shown in the e unit operations may

. useful when modeling

different variants of the same unit operation.

User-Added Subroutine.

In the PFD window, right-click the icon of

igure 12-2 appears.

It is possible to speany unit operation currentsimulation flowsheet. Sombe represented by any of several different iconsThis choice is particularly

Note: Any available icon may be assigned to a

To change the style of a single unit:

the unit to modify. The unit menu shown in F

Select Display.. from this menu (or select

Edit/Display Sty

12-2:

le… from the menu bar) to open the Unit Style window for the selected

selecting the unit type, and does not allow changing the Auto Label fields. (Compare to Figure 12-1.) This prevents conflicts with the

f icons available to represent the unit operation. Simply h sired icon in the scroll box. Th eady highlighte

unit type.

As shown in Figure 12-3, the Unit Style for a specific unit operation does not require

global labeling discussed previously.

Using Alternative Icons The Unit Style dialog shown in Figure 12-3 includes a list o

ighlight the dee selected icon is used only for the specific unit operation (alr

d on the flowsheet drawing).


Figure 12-3: Individual Unit Style Window

Changing the Label Font

Click the Select button in the Unit Labels group box of the Unit Style dialog to open the Font dialog. The topic Changing the Default Font later in this chapter describes modifying the attributes of the font used in the label.

Changing the Label Displayed for a Specific Unit PRO/II automatically labels each unit placed on the PFD using the global Auto Label fields (see Figure 12-1). You can change the label for an individual unit, but cannot alter the auto-numbering sequence. To change a unit label:

Double-click on the unit on the PFD, (or right-click the unit icon and select Data Entry.. from the unit menu).

t in the “U ” label field of the data entry allow a percent sign (%), which prevents acro.

ressing OK.

Type over the existing texwindow. Note: the field does notredefining the autonumbering mCommit the change b

nit

y p


Changing Stream StylesThe display of streams on the PFD mstreams) or individually. By definsettings for individua

ay be customized globally (for all

ition, global settings serve as defaults, while -rides of the global settings. To help

mization of individual streams is nd cannot override all global settings.

hovers over a stream. Because the stream display remains unchanged, this

Changing the Global Stream Style The options for changing stream labels function in the same manner as changing unit labels (described earlier in this chapter), and the format syntax is the same. The global Stream Style dialog allows customizing the following attributes:

• The height and width of the arrows • The fill of the arrows • The segments on which the arrows appear • The label format • The starting number for auto-generated stream labels • The stream label location • The stream label border (shape) and font attributes • The stream label type (stream ID or list of properties) • ToolTip display (stream ID or list of properties)

To Change the Default Style of Streams:

l streams are overmaintain a consistent appearance, custolimited a

A related set of customizations allows modifying the ToolTip display. For example, instead of changing a stream label to always display a property list, the ToolTip could display the property list only when the mouse cursor

approach leaves the PFD uncluttered, while still providing convenient accessto the information in the property table.

• The contents of the property list (material balance, gas report, etc.)

Choose Options/Drawing Defaults/Stream Display… from the menu bar own in Figure 12-4.

to open the global Stream Style dialog sh

Configure the desired options for Stream Arrows, Stream Labels, and Font. The Stream Tooltip Display options do not affect the default streamstyle directly (these features are described later in this chapter).

Click OK to apply the changes.

ate automatically to the PDF drawing, click If all the changes do not propagthe View/Redraw option on the menu bar.


-4: Global Stream Style Dialog

Sample Custom Stream Display As illustrated in Figure 12-5, default stream labels display imple stream ID’s, have ctangular borders, and

ppear on the stream line. rocess stream arrows are

appear only on e horizontal segments of rthogonal process streams.

Figure 12

Figure 12-5: Default Stream Style

sreaPnot filled, andtho


Figure 12-6 illustrates the

same flowsheet after using the following options from the global Stream Styles dialog:

• Stream Label Location: Above Line with Stem

• Stream ArrowsHeight: 10; Width: 20

• Fill Arrows

• Stream Label Border: Diamond

:

Figure 12-6: Sample of Typical Custom Stream Style

These are merely samples of the available customizations. The global settings always apply to new streams added to the flowsheet, but existing streams are not automatically updated. This avoids changing streams that already have local style settings. The topic Changing An Individual Stream Style (later in this chapter) describes how to apply new global settings to individual streams.

Di l Lists As Stream Labels RO/II allows you to display various stream properties on labels attached to the treams on the PFD. Display options include:

• Select a global property list for all stream labels in the flowsheet • Choose from a group of predefined property lists • Create a custom stream label property list • Position property labels anywhere (on or beside) streams on the PFD • Choose the type of border for any label • Choose a different font for any label

sp ay Stream PropertyPs


To Select a Global Default Steam Property:

Choose Options/Drawing Defaults/Stream Display… from the menu bar to open the Stream Style window.

Type drop-down list, choose the Properties option.

Choose one of the predefined property lists and click OK to commit your choice.

The selected property list will appear on all streams subsequently added to the PFD.

Create Custom Stream Property Lists PRO/II allows you to create custom property lists for use in Stream Property Tables. You can use the same property list in more than one simulation. The default Stream Property Table is outlined by a single-lined rectangular box. You may arrange the properties in any desired order, and you may separate entries by single or double horizontal lines to improve the legibility of the list. To select a property list:

Choose Options/Stream Property Lists from the menu bar to display the Define Property List window (Figure 12-7).

From the Stream Label

Figure 12-7: Define Stream Property List Dialog

Select a list from the Property List box (Figure 12-8).


Figure 12-8: A Typical Property List

You can add or delete properties, modify the property description and

change the numerical format.

To create a property list:

Choose New… from the Define Property List window. The New List window appears.

Figure 12-9: New List Window

Enter a name for the new list, or Select the list from which you want to copy an existing property list. Choose OK to commit the entries.


To add one or more pro

Select thcontrol-cli

perties to a list:

e desired properties. (The usual Windows click, shift-click and ck selection options are supported.)

Add->. lected properties are added to the bot .

the properties in a

properties you want to movewn, Top, Bottom button roperties.

e description or the format o

property you want to changeEnter the new description and format he entry fields under the

e changes using the Repla

To delete a property from a list:

ties you want to deve.

To ) all properties from a list:

r.

arcate sections of a list:

ble horizontal lines

Choose The se tom of the property list

To change the order of list:

Select the . Use the Up, Do s to move the selected p

To change th f a property:

Select the . in t

property list. Commit th ce button.

Select the proper lete. Choose Remo

clear (delete

Choose Clea

To dem

Insert

single or dou where desired.


Changing the Style of an Individability to over-ride so obal stream style

des apply only to the spe t. Lim prevent compromising certai s the strea ring sequence.

ual Stream Each stream provides the me of the glsettings. These over-ri

itations exist tocific stream of interesn global features, such a

m numbe

F enu

To Modify the Stream:

Right-c F to open its Stream Figure 12-10.

Click th e individual Stream 2-11).

igure 12-10: Stream M

Style of an Individual

the PDlick a stream on Menu, as shown in

e Display item to open th Style dialog. (shown below in Figure 1

Figure 12

y of the options in the indiv yle menu. Notice ited to some label properties and font formatting. They behave

gously to the same options describ l Stream g.

local over-rides and r am Style e Defaults

-11: Individual Stream Style Dialog

Choose an are lim

idual Stream Sttheyanalo ed above for the globaStyle dialo

To remove alsettings, click the Restor

l e-apply the global Stre button.

Click the OK button to apply the changes to this one stream.


Changing the ID Name of an Individual Stream ly labels each new stream . You can r or label for just one strea oing

To

open t dow. am ….

PRO/II automaticalcha mbe

as it is placed on the PFDut altering the ongnge the nu m witho

numbering sequence.

change a stream label:

Double-click on the stream toAlternatively, right-click on the stre

he Stream Data win Data Entry and choose

Figure 12-12: Stream Data Entry Window

Enter the new stream name in the Stream entry field.

Positioning Stream Property Labels on the PFD You may place stream labels on, above, below or beside the streams on the PFD. The labels may appear with or without stems connecting them to the streams.



To position stream labels:

Choose Options/Drawing Defaults/Stream Display… from the menu bar. Select the desired position from the Stream Label Location drop-down list. Click OK to commit your selection.

Alternatively, drag a stream label to any of these positions from the PFD itself. While in the Stream Styles window, you may also choose a text font and a border style for the labels from the corresponding drop-down lists. Toggle Stream Property List Button

Users may configure a stream property table to display on demand by using the Stream Toggle button on the PRO/II tool bar. Clicking the Stream Toggle button switches all stream labels to display the property table. Clicking again switches back to the stream label display. Before the button is used, a property list should be selected and assigned to the button.

Choose Options/Drawing Defaults/Stream Display… from the menu bar to open the global Stream Style dialog shown in Figure 12-13.

Select a property table to be controlled by the toggle button. Figure 12-13 highlights the Toggle Stream Property List box in red.

Figure 12-13: Toggle Stream Property List

Click the OK button to complete the configuration.


Users may choose any one of the stream property tables in the drop-down list. The "Property Label List" is the default selection.

All custom property tables created by users are included in the drop-down list. They are available for selection, just as any of the pre-defined property tables.

Adding the Toggle Stream Button to the Tool Bar

If the Stream Toggle button is not already on the tool bar, it must be added to make the feature available for use.

Choose View/Toolbar… from the menu bar to open the Toolbar Customization dialog shown in Figure 12-14.

Figure 12-14: Adding the Toggle Stream Button to the Tool Bar

Scroll the Available Items: list box and highlight the Toggle Stream entry as shown in the figure.

Click the Add -> button to move the Toggle Stream entry to the Selected Items list. (The Add -> button is circled in blue in Figure 12-14.)

Use the Up, Down, Top, and Bottom buttons at the right side of the dialog to position the Toggle Stream button in the desired location in the list of selected items. The list order determines the position of items on the tool bar.

Click the OK button to complete the installation.


Click the button on the toolbar and observe that all stream labels change to the selected property table. This is illustrated in Figure 12-15.

Figure 12-15: The Toggle Stream Button Displays A Property

List Instead of the Stream Labels

Click the Toggle Stream button again to change back to the normal stream ID display.

Customizing Stream ToolTips PRO/II supports customizable tool tips for streams. As shown in Figure 12-16, hovering the mouse cursor over a stream displays the stream label.

While the default stream tooltip displays the stream label, PRO/II allows reconfiguring stream tooltips to display a stream property list instead of the stream label. This is similar to replacing stream labels with stream property list in


the global and individual stream display styles (described earlier in this chapter). It also is similar to configuring the Toggle Streams button.

Figure 12-16: Default Stream Label ToolTip

To Configure the Stream ToolTip:

Choose Options/Drawing Defaults/Stream Display… from the menu bar to open the global Stream Style dialog.

Scroll the Stream Tooltip Display list box and highlight an option.

The Stream Tooltip Display list box shown in Figure 12-17 is highlighted in green in the Stream Style dialog is shown in Figure 12-13. Click the OK button to complete the installation.

Figure 12-17: Stream ToolTip Display List Box

Most entries in the Stream Tooltip Display list box are the names of stream property lists.

The Off entry sets the tooltip to display the basic stream label. It is the default setting.


. Figure 12-18 illustrates displays by both the Toggle Stream and the customized ToolTips features.

Figure 12-18: ToolTip and Stream Label Displaying Stream Property Lists

Modifying Drawing Preferences Drawing preferences include settings for snap and move tolerances, zoom and pan increments, the PFD palette icon, icon fill, unit snapping, and delete confirmation. To modify drawing preferences:

Choose Options/Drawing Defaults/General… from the menu bar. The General Drawing Defaults window appears with current settings. The settings can be changed as desired.


Specifying a Default Editor You can specify a default editor (such as Brief, Edit or Notepad) for use with PRO/II to display output reports and keyword input files. Using the editor, you can save any displayed text to a file or printer. The default editor is the Programmer’s File Editor (pfe.exe). To specify a default editor:

Choose Options/Editor from the menu bar to open the Set Text Editor window.

Enter the full path name to the editor executable program file.

Figure 12-19: Set Text Editor


Changing the Default Font The Default Font option enables you to set the default font, font style, and size used in PRO/II’s main and data entry windows. This option is useful when the default font size for your system is too large for PRO/II’s data entry windows. Note that you cannot change the fonts for the title, menu, and status bar text. Also, changing the font size does not change the size of PRO/II’s windows.

To specify the default font: Choose Options/Font from the menu bar to display the Font dialog. Choose the desired font, font style, and size.

Figure 12-13: Font Window



Index i

Index Aligning Text, 72 Basics

Simulation, 15 Boiling Pot Reactor, 309 Border Handles, 5 Bounding Box

Changing the size, 78 Moving, 78

Button PFD Palette, 9

Buttons Delete, 12 Help, 13 Run/Results, 11 Toolbar, 9 Toolbar, customizing, 13 Using Data Entry, 10 Using Navigation, 11 View, 12 VLE tools, 11

Calculator calculator, 149

cancel Unit placement, 53

Cancel Delete, 53

Changing Window Size, 4 Column, Side, 199 Components, 18

Define, 16 Continuous Stirred Tank Reactor, 305 Control Menu, 5 Convergence

Test for, 36 Conversion and Equilibrium Reactors,

305 Copy

stream property table, 40 to Excel, 40

Data Default, 23

Data Entry Window Buttons, 10 Default

global override, 42 units of measure, 43

Depressuring Unit, 221 Dissolver, 226 edit text, 72

Entering Text, 62 Excel Unit, 227 Expander, 233 Exporting

Drawing to clipboard, 37 keyword file, 35 stream property table, 38 to AutoCAD, 39

Features Unsupported, 33

file import keyword input, 32

Fill from Structures, 82 Fixed Properties, 101 Flash, 235 Flash With Solids, 239 Floating Palettes. See Flowsheet

Building, 17, 41 Connect Unit Operations, 16 Define Components, 16 Draw, 15

Flowsheet Optimizer, 241 Gibbs Reactor, 311 Go To Buttons, 11 Heat Exchanger

Air Cooled, 249 LNG, 247 Rigorous, 251 Simple, 261

Heat Exchanger, Lng, 247 Heat Exchanger, Rigorous, 251 Heat Exchanger, Simple, 261 Heating/Cooling Curves, 265 Help Button, 13 Henry’s Law, 113 import

Keyword input file, 32 Importing a PRO/II keyword input file, 32 Linked text, 94 Main Window

Using, 14 Menus

Using, 6 Minimize/Maximize Buttons, 4 Mixer, 269 mode

Run Only, 33, 34

ii PRO/II User Guide April 2009

Multiple View and PFD Palette Buttons, 9

Multivariable Controller, 271 Objects

Deselecting, 69 Flipping, 72 Moving, 71 Rearranging, 71 Resizing, 69 Rotating, 71 Selecting all, 69 Selecting group, 69

Palettes Using, 9

Pan Left, Right, Up or Down, 78

Panning, 76 PFD

Toolbar button, 9 Phase Envelope, 275 Pipe, 281 Properties

Transport, 117 Property Methods

Thermodynamic and Transport, 16 Pump, 297 Reactor

Polymer Reactor, 287 Reactor, Batch, 318 Report options, 379 Run/Results Buttons, 11 Save

Current Simulation, 27 Save as dialog box, 27 Simulation to another name, 27

Screen Color Coding, 5 Scroll Bar

Horizontal, 4 Vertical, 4

Scrolling increments, 73 PFD, 73

Select all objects, 69 Group of objects, 69 Multiple objects, 67

Set Breakpoints, 366

Setting Up the Printer, 392 Simsci Add-On Modules, 353 Simulation

Analyze results, 17

Basics, 15 Building the flowsheet, 17 Closing, 28 Connect Streams, 16 Copying, 30 Copying to Excel, 40 Declaring components, 18 Default data, 23 Define Components. See

Components, Define Deleting, 28, 29 Draw Flowsheet, 15 Exporting to AutoCAD, 40 Opening, 25 Opening an existing simulation, 26 Run Only mode, 34 Save current, 27 Saving, 27 Savings to another file name, 28 setting preferences, 41 setting units of measure, 44

Simulation Data Exporting to a keyword file, 36

Simulation defaults Problem Description, 42 Units of measure, 43

Simulation Defaults, 41 Snapping, 52 Solid Separator, 319 Splitter, 321 Spreadsheet Tools

Using, 39 Starting PRO/II, 1, 2 Stream Calculator, 323 Stream Information, 19 Stream Property, 38 Temperature-Dependent Properties,

102 Thermodynamic Methods, 18 Toolbar

Buttons, 9 Customizing, 13 Navigation buttons, 11

Tools Spreadsheet, 39

Transport properties, 117 turn off, 367 Unit data entry window, 19 unit icon, 51 unit opeartion

Cyclone, 215 unit operation, 147

Index iii

Column, Batch, 171 compressor, 203 Controller, 207 Crystallizer, 211 Distillation, 172

Unit Operations, 19 Connect, 16

Units of Measure Library, 45 User defined special properties

Thermodynamic Data, 140 User-Added Unit Operations, 167, 343 User-defined Special Properties, 137,

139

Valve, 357 Vertical Scroll Bar, 4 View Buttons, 12 Viewing Results, 368 VLE Tools Buttons, 11 Water Decant Options, 118 Window

Changing Position, 5 Customizing, 4

Wiped Film Evaporator, 359 Zoom Area, 12 Zoom Increment, 74 Zooming, 73

Documents

User Guide