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7/22/2019 Aspen-Plus Ternary Mixture
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n ro uc on o spen usShort Courses on Computer Applications for ChE Students
S eaker: JianKai Chen
PSE Laboratory
Nation Taiwan
University
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• Aspen Plus is a market‐leading process modeling tool
for conceptual
design,
optimization,
and
performance monitoring for the chemical, polymer,
specialty chemical, metals and minerals, and coal
power industries.
2Ref: http://www.aspentech.com/products/aspen-plus.cfm
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• Physical Property Models
– World’s largest
database
of
pure
component
and
phase
equilibrium
, , ,
– Regularly updated with data from U. S. National Institute of Standards
and Technology (NIST)
• Comprehensive Library
of
Unit
Operation
Models
– Addresses a wide range of solid, liquid, and gas processing equipment
– Exten s stea y‐state simu ation to ynamic simu ation or sa ety an
controllability studies, sizing relief valves, and optimizing transition,
startup, and
shutdown
policies
– Enables you build your own libraries using Aspen Custom Modeler or programming languages (User‐defined models)
Ref: Aspen Plus® Product Brochure3
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• Properties analysis
– Properties of
pure
component
and
mixtures
(Enthalpy,
density, viscosity, heat capacity,…etc)
– Phase equilibrium (VLE, VLLE, azeotrope calculation…etc)
– Parameters estimation
for
properties
models
(UNIFAC
method for binary parameters, Joback method for boiling
…
– Data regression from experimental deta
• rocess s mu a on
– pump, compressor, valve, tank, heat exchanger, CSTR, PFR,
s a on co umn, ex rac on co umn, a sor er, er,
crystallizer…etc 4
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What course Aspen Plus What course Aspen Plus
can be
employed
forcan
be
employed
for
• MASS AND ENERGY BALANCES
• PHYSICAL CHEMISTRY
• CHEMICAL ENGINEERING THERMODYNAMICS
• UNIT OPERATIONS
• PROCESS DESIGN
• PROCESS CONTROL
5
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• Familiar with the interface of Aspen Plus
• Learn how
to
use
properties
analysis
• Learn how to setup a basic process simulation
6
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Problem Formulation 1: Calculation Problem Formulation 1: Calculation
the mixing
properties
of
two
stream
the
mixing
properties
of
two
stream
1 2 3 4Mole Flow kmol/hr
WATER 10 0 ? ?
BUOH 0 9 ? ?
BUAC 0 6 ? ?
Total Flow kmol/hr 10 15 ? ?
Mass Balance
Temperature C 50 80 ? ?
Pressure bar 1 1 1 10
Enthalpy kcal/mol ? ? ? ?
nergy a anceEnthalpy
Entropy…
Entropy cal/mol-K ? ? ? ?
Density kmol/cum ? ? ? ?7
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Problem Formulation 2: Problem Formulation 2:
Flash SeparationFlash Separation
120
115
-x
T-y
Saturated Feed
T=105 CP=1atm
110
T ( o C
)
P=1atm
F=100 kmol/hr
z =0.5 0.0 0.2 0.4 0.6 0.8 1.0100
zHAc=0.5 xWater
and yWater
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Problem Formulation 3: Dehydration of Problem Formulation 3: Dehydration of
Acetic Acid
by
Distillation
Column
Acetic
Acid
by
Distillation
Column
O tionalO tional
0.8
.
Reflux
0.4
0.6
y W a t e rratio ?
0.2
Duty ?
0.0 0.2 0.4 0.6 0.8 1.0.
xWater
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• Startup in Aspen Plus (Basic Input) (45 min)
– User Interface
– Basic Input: Setup, Components, Properties.
• Properties Analysis (1 hour)
– Pure Component – Mixtures (phase equilibrium)
• Running Simulation (1 hour)
– Blocks (Unit Operations) – Streams (flow streams)
– Results
10
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Introduction to Aspen Plus – Part 1
Startup in Aspen Plus
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spen us ser n er ace
12
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Process Flowsheet WindowsProcess Flowsheet Windows
Model Librar View Model LibrarModel Librar View Model Librar
Stream
Status message14
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Help for Commands for Controlling Simulations 15
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• The Data Browser is a sheet and form viewer with a
hierarchical tree
view
of
the
available
simulation
input, results, and objects that have been defined
16
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17
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• The minimum required inputs to run a simulation
are: – Setup
– Components Property Analysis
– Properties – Streams
– Blocks
18
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Input mode
19
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Run Type Description Use to
Assay Data Analysis s an a one assay a a
analysis/pseudocomponents generation run
na yze assay a a w en you o no wan o
perform a flowsheet simulation in the same run.
A standalone
data
regression
run.
Can
contain
Fit physical property model parameters required
by Aspen Plus
to
measured
pure
component,
ata egress on property constant est mat on an property ana ys s
calculations.
, an ot er m xture ata. spen us
cannot perform data regression in a Flowsheet
run.
Prepare a property package for use with Aspen
Properties Plus A
Properties
Plus
setup
run
ustom Mo e er, w t t r party commerc a
engineering programs,
or
with
your
company's
in house programs.
You must be licensed to use Properties Plus.
Property Analysis
A standalone property analysis run. Can contain
property constant estimation and assay data
analysis calculations.
Per orm property ana ys s y generat ng ta es
of physical property values when you do not
want to perform a flowsheet simulation in the
same run
Property Estimation A standalone property constant estimation run
Est mate property parameters w en you o not
want to perform a flowsheet simulation in the
same run.
A Flowsheet run includin sensitivit studies and
Flowsheet optimization). also include the following
calculations: Property
estimation,
Assay
data
analysis and Property analysis
Perform process simulations
20
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npu componen s
with Component name or Formula
21
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Remark: If available, are
22
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To do this Click this button
Find components
in
the
databanks Find
Define a custom component that is not in
a databank
User Defined
Generate electrolyte
components
and
reactions from components you enteredElec Wizard
Reorder the components you have
specified
Reorder
Review databank data for components
you have specified (Retrieved physical
Review
.
23
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Click “Find”
24
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’’
In ut Com onent name or Formula or CAS number
25
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methods available)
, , , …
27
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Interactive help in choosing a property method
28
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Specify Component type
Chemical Systems
Is the system at high pressure?
(NO)
Two liquid phases
29
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30Reference: http://www.et.byu.edu/groups/uolab/files/aspentech/
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Vapor EOS
NRTL Liquid
gammaLiquid enthalpy
qu vo ume
31
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Check “Modif Pro ert Model”
S ecif New Method Name
32
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c an en u - n nary parame ers
appear automatically if available.
33
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Access Properties Models and Access Properties Models and
ParametersParameters
Review Databank Data
34
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Including:Ideal gas heat of formation at 298.15 K
Ideal gas Gibbs free energy of formation at
298.15 K
Heat of vaporization at TB
Normal boiling point°
….
Description of
each
parameter35
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Help for Pure Component Databank Parameters 36
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Pure Component Pure Component
TemperatureTemperature‐‐Dependent
PropertiesDependent Properties
CPIGDP‐1 ideal gas heat capacity
CPSDIP‐1 Solid heat capacity
DNLDIP‐1 Liquid density
DHVLDP‐1 Heat of vaporization
‐
MULDIP Liquid viscosity
KLDIP Li uid thermal conductivit
SIGDIP Liquid surface tension
UFGRP UNIFAC functional group
37
ll
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Example: PLXANTExample: PLXANT‐‐1 1
(Extended Antoine
Equation)(Extended
Antoine
Equation)Corresponding Model
Click “ ?” and then click where you don’t know
38
E l CPIGDPE l CPIGDP 11
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Example: CPIGDPExample: CPIGDP‐‐1 1
(Ideal Gas
Heat
Capacity
Equation)(Ideal
Gas
Heat
Capacity
Equation)
Corresponding Model
39
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So far, we have finished the basicsettings including setup, components,
and properties.
This is enough to perform properties
ana ys s.
40
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File Type Extension Format Description
Document *.apw Binary File containing simulation input and results and
n erme a e convergence n orma on
Backup *.bkp ASCII Archive file containing simulation input and
resultsHistory *.his Text Detailed calculation history and diagnostic
messages
*
41
Description
.
convergence information used in the simulation
calculations
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• Binary i es
– Operating system and version specific
–
,
• ASCII files
– Transferable between operating systems
– Upwardly compatible
– Contain no control characters, “readable”
– ot nten e to e pr nte
• Text files
–
– Upwardly compatible
– Readable, can be edited
– Intended to be printed
42
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Introduction to Aspen Plus – Part 2
Properties Analysis in Aspen Plus
43
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Pure Tables and plots of pure component properties as a function of temperature
and pressure
Binary Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue Residue curve maps
Ternary , ,
systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of
.
Ternary Maps
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes,
Distillation boundary, Residue curves or distillation curves, Isovolatility curves,
e
nes,
apor curve,
o ng
po nt
Tables and plots of properties of either multi‐phase mixtures (for example,
VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures
without flash calculations. Properties analysis of multi‐components (more
than three)
is
also
included. 44
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• When you start properties analysis, you MUST
s ecif com onents ,
ro erties model,
and
corresponding model parameters. (Refer to
45
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Use this form To generate
Pure Tables and plots of pure component properties as a function of temperature
and pressure
Binary Txy, Pxy,
or
Gibbs
energy
of
mixing
curves
for
a
binary
system
Residue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary
Azeotrope This feature
locates
all
the
azeotropes that
exist
among
a
specified
set
of
components.
Ternary Maps
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes,
Distillation boundary, Residue curves or distillation curves, Isovolatility curves,
Tie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example,
VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures
without flash calculations. Properties analysis of multi‐components (more
than three) is also included.
46
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47
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Property (thermodynamic) Property (transport)
Availability Free energy Thermal conductivity
heat capacity Enthalpy Surface tension
Heat capacity ratio Fugacity coefficient Viscosity
ons an vo ume ea
capacity
ugac y coe c en
pressure correction
Free energy departure Vapor pressure
Free energy departure
pressure correction Density
Enthalpy
departure EntropyEnthalpy departure
pressure correction Volume
Enthalpy of
vaporization
on c ve oc y
Entropy departure 48
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1. Select property (CP)
4. S ecif ran e of tem erature
2. Select phase
. pec y pressure
Add “N-butyl-acetate”
3. Select component 6. Select property method
7. click Go to generate the results
49
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Data results 50
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1. Select property (H)
4. Specify range of temperature
2. Select phase
5. Specify pressure
3. Select component. e ec proper y me o
7. click Go to generate the results 51
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Data results
52
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Use this form To generate
Pure Tables and plots of pure component properties as a function of temperature
and pressure
Binary Txy, Pxy,
or
Gibbs
energy
of
mixing
curves
for
a
binary
system
Residue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary
Azeotrope This feature
locates
all
the
azeotropes that
exist
among
a
specified
set
of
components.
Ternary Maps
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes,
Distillation boundary, Residue curves or distillation curves, Isovolatility curves,
Tie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example,
VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures
without flash calculations. Properties analysis of multi‐components (more
than three) is also included.
53
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‐‐
1. Select anal sis t e Tx2. Select phase (VLE, VLLE)
2. Select two component 5. Specify pressure
3. Select compositions basis
4. Specify composition range.
7. click Go to generate the results
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‐‐
Data results
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Click “plot wizard” to generate XY plot
’’
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’’
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120
Water-BuOH
110
90 T ( o C )
0.0 0.2 0.4 0.6 0.8 1.070
80
Mole Fraction (Water)
nary na ys s canno genera e a a e ow azeo rope.
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Use this form To generate
Pure Tables and plots of pure component properties as a function of temperature
and pressure
Binary Txy,
Pxy,
or
Gibbs
energy
of
mixing
curves
for
a
binary
systemResidue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary
Azeotrope This feature
locates
all
the
azeotropes that
exist
among
a
specified
set
of
components.
Ternary Maps
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes,
Distillation boundary, Residue curves or distillation curves, Isovolatility curves,
Tie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures
without flash calculations. Properties analysis of multi‐components (more
than three) is also included.
61
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4. Select phase (VLE, LLE)
.
5. Specify pressure2. Specify number of tie line
3. Select property method
6. Specify temperature
(if LLE is slected)
7. click Go to generate the results
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a a resu s
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Use this form To generate
Pure Tables and plots of pure component properties as a function of temperature
and pressure
Binary Txy,
Pxy,
or
Gibbs
energy
of
mixing
curves
for
a
binary
systemResidue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary
Azeotrope This feature
locates
all
the
azeotropes that
exist
among
a
specified
set
of
components.
Ternary Maps
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes,
Distillation boundary, Residue curves or distillation curves, Isovolatility curves,
Tie lines, Vapor curve, Boiling point
Generic
Tables and
plots
of
properties
of
either
multi
‐phase
mixtures
(for
example,
VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures
without flash calculations. Properties analysis of multi‐components (more
than three) is also included.
Generic analysis is used if properties analysis of mixture is performed.65
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Enthalpy of Mixtures?
Water-BuOH
110
120
90
T ( o C )
660.0 0.2 0.4 0.6 0.8 1.070
Mole Fraction (Water)
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Select Property analysis
67
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Select Generic
68
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. Select “flash calculation” or not 3. Specify component flo
2. Select phase (VLE, LLE)
. pec y e correspon ng compos on
69
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Specify feed condition
Temperature
Pressure
Mole flow
Mass flow
StdVol flow
Mole fraction
Mass fraction
StdVol fraction
Specify range of adjusted variables
70
Specify PropertySpecify Property‐‐Sets for Sets for
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Calculation ResultsCalculation Results
71
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’’‐‐
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…
Select “Vapor” “1st liquid” “2nd liquid”
73
‐‐
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Check “simulation status”
.
75
Example1: Calculation of Enthalpy Example1: Calculation of Enthalpy
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Change
Change for
binary
mixturesfor
binary
mixtures
-60000
Molar ratio of Butanol/Water=1:1
-56000
Temperature = 50oC
-64000
-62000
m o l )
Liquid
Vapor
-64000
-62000
-60000
-58000
o l )
Liquid
Vapor
-70000
-68000
-
E n t h a l p y ( c a l
-72000
-70000
-68000
-66000
E n t h a l p
y ( c a l /
40 50 60 70 80 90 100-74000
-72000
0.0 0.2 0.4 0.6 0.8 1.0-78000
-76000
-74000
Temperature (oC) Mole fraction of Water in BuOH and Water
76
Search Physical Properties for Search Physical Properties for
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Enthalpy of
Mixtures
(HMX)
Enthalpy
of
Mixtures
(HMX)
Select HMX.
Others are optimal.
Add Property-Set
77
Calculate Calculate of Enthalpy Change As of Enthalpy Change As
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Temperature
Temperature VariesVaries
1
3
4
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-58000
-56000
Temperature = 50oC
-66000
-64000
-62000
-60000
a l / m o l )
Liquid
Vapor
-74000
-72000
-70000
-68000
E n t h
a l p y ( c
0.0 0.2 0.4 0.6 0.8 1.0-78000
-76000
Mole fraction of Water in BuOH and Water
80
Example 2: Example 2: Calculation of Calculation of LLE LLE
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for
for Binary
systemBinary system
120
Water-BuOH
110
90
100
T ( o
C )
80
0.0 0.2 0.4 0.6 0.8 1.070
Mole Fraction (Water)
81
’’ ‐‐
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Select “Vapor” “1st liquid” “2nd liquid
, , ‐‐
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1 2
Select Vapor-liquid-liquid
3
4
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120
Water-BuOH
90
100
T ( o C )
0.0 0.2 0.4 0.6 0.8 1.070
80
Mole Fraction (Water)
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Use this form To generate(Optional)
Pure Tables and plots of pure component properties as a function of temperature
and pressure
,
,
Residue Residue curve maps
Ternar ma s showin hase envelo e, tie lines, and azeotro es of ternar
ernarysystems
Azeotrope This feature
locates
all
the
azeotropes that
exist
among
a
specified
set
of
com onents.
Ternary Maps
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes,
Distillation boundary, Residue curves or distillation curves, Isovolatility curves,
, ,
Generic
Tables and plots of properties of either multi‐phase mixtures (for example,
VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures
‐ .
than three) is also included.
85
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• Conceptual design enables the user to:
1. Locate all the azeotropes (homogeneous and
heterogeneous) present
in
any
multicomponent
mixture
2. Automatically compute distillation boundaries and
res ue curve maps or ternary m xtures
3. Compute multiple
liquid
phase
envelopes
(liquid
‐liquid
‐ ‐
4. Determine the feasibility of splits for distillation columns
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1. Select components (at least two) 2. Specify pressure
3. Select property method
6. click Report to generate the results
. ,
5. Select report Unit
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Close analysis
input
dialog
box
(pure
or
binary
analysis)
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4. Select phase (VLE, LLE)1. Select three components
.
2. Specify pressure 5. Select report Unit
6. Click Ternary Plot to generate the results
6. Specify temperature of LLE
(If liquid-liquid envelope is selected)
Change pressure or
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Change pressure or
Ternary Plot Toolbar:Add Tie line, Curve,
Marker…
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Introduction to Aspen Plus – Part 3
Running Simulation in Aspen Plus
95
Example 1: Calculate the mixing Example 1: Calculate the mixing
properties of two streamproperties of two stream
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properties of
two
stream
properties
of
two
stream
1 2 3 4
Mole Flow kmol/hr
WATER 10 0 ? ?
BUOH 0 9 ? ?
BUAC 0 6 ? ?
Total Flow kmol/hr 10 15 ? ?
Temperature C 50 80 ? ?Pressure bar 1 1 1 10
Enthalpy kcal/mol ? ? ? ?
Entropy cal/mol-K ? ? ? ?
Density kmol/cum ? ? ? ?
96
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120
115
-x T-y
Saturated Feed
T=105 C
P=1atm
110
T
( o C )
P=1atm
F=100 kmol/hr
z =0.5 0.0 0.2 0.4 0.6 0.8 1.0100
zHAc=0.5 xWater
and yWater
Example 3: Dehydration of Acetic Example 3: Dehydration of Acetic
Acid by Distillation ColumnAcid by Distillation Column (Optional)(Optional)
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Acid by
Distillation
Column
Acid
by
Distillation
Column
( p )( p )
0.8
.
Reflux
0.4
0.6
y W a
t e rratio ?
0.2
Duty ?
0.0 0.2 0.4 0.6 0.8 1.0
.
xWater
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Select Flowsheet
99
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or press F10
100
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Model Description Purpose Use for
Mixer Stream mixer Combines
multiple
streams
into one streamMixing
tees.
Stream
mixin o erations.
Adding heat streams.
Adding work streams
specified for
outlet
streams
.
valves
specified for each substream
.
fluid‐solid separators
101
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102
Model Description Purpose Use for
Pump ump or y rau c
turbine
anges stream pressure w en t e
power requirement is needed or
known
umps an y rau c
turbines
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Compr ompressor or
turbine
anges s ream pressure w en
power requirement is needed or
known
o y rop c compressors,
polytropic positive
displacement compressors,
, isentropic turbines
Mcompr Multistage Changes stream pressure across Multistage polytropic
turbine
.
Allows for liquid knockout streams
from intercoolers
,
positive displacement
compressors, isentropic
,
turbines
Valve Valve pressure
dro
Models pressure drop through a
valve
Control valves and pressure
chan ers
Pipe Single segment
pipe
Models pressure
drop
through
a
single segment of pipe
Pipe with
constant
diameter
(may include fittings)
pipeline
pipe or annular space
lengths of different
diameter or elevation103
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Click “one of icons”
an en c c aga n on e ows ee w n ow
Remark: The shape of the icons are meaningless
104
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Click “Materials” and then click
105
’’
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,
arrows (blue and red) appear.
106
’’
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When moving the mouse on the arrows, some description appears.
Blue arrow: Water
decant for Free water
Red arrow(Left) Feed
(Required; one ore more
Red arrow(Right):
Product (Required; if.
streams)
107
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Reconnecting Material Streams Reconnecting Material Streams
(Feed Stream)(Feed Stream)
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(Feed Stream)(Feed Stream)
Right Click on the stream and
select Reconnect Destination
109
Reconnecting Material Streams Reconnecting Material Streams
(Product Stream)(Product Stream)
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(Product Stream)(Product Stream)
Right Click on the stream and
B1
1
2
3
110
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Right Click on the stream
111
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You must specify two of the following
conditions:
Temperature
Pressure
Vapor fraction
You can enter stream composition in terms of component flows,fractions, or concentrations.
, ,
mass, or standard liquid volume flow.
112
’’
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1 2
113
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Right Click on the block and select Input
114
’’
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Specify Pressure and valid phase
The corresponding description about this blank:
Outlet pressure if value > 0
Pressure drop if value 0
115
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Click to run the simulation
Run Start or continue calculations
Step Step through the flowsheet one block at a time
Stop Pause simulation
calculations
Reinitialize Purge simulation results
Check “simulation status”
“Re uired In ut Com lete” means the in ut is read to run simualtion
116
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Message Means
Results available The run has completed normally, and results are
.
Results with warnin s
Results for the run are present. Warning
messages were generated during the
ca cu at ons. V ew t e Contro Pane or H story
for messages.
Results for
the
run
are
present.
Error
messages
Results with errors were generated during the calculations. View the
Control Panel or History for messages.
Results for the run are resent, but ou have
Input Changed changed
the
input
since
the
results
were
generated. The results may be inconsistent with
the current input.
117
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Click here
1.A message window showing the progress
of the simulation by displaying the most
2.A status area showing the hierarchy and
loops executed118
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select Stream Results
119
1 2 3
Substream: MIXED
Mole Flow kmol/hr
WATER 10 0 10
BUAC 0 6 6
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BUAC 0 6 6
Total Flow kmol/hr 10 15 25
Total Flow kg/hr 180.1528 1364.066 1544.218
Total Flow
cum/hr 0.18582 1.74021 1.870509
Temperature C 50 80 70.08758
Pressure bar 2 1 1
apor rac
Liquid Frac 1 1 1
Solid Frac 0 0 0
Enthal kcal mol ‐67.81 ‐94.3726 ‐83.7476Pull down the list and select
Enthalpy kcal/kg ‐3764.03 ‐1037.77 ‐1355.82
Enthalpy Gcal/hr ‐0.6781 ‐1.41559 ‐2.09369
Entropy cal/mol‐K ‐37.5007 ‐134.947 ‐95.6176
“Full” to show more properties
results.
Entropy cal/gm‐K ‐2.0816 ‐1.48395 ‐1.54799
Density kmol/cum 53.81564 8.619647 13.36534
Density kg/cum 969.5038 783.851 825.5604
. . .
Liq Vol 60F cum/hr 0.1805 1.617386 1.797886
120
Enthalpy and Entropy
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121
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123
Stream Results with Format of Stream Results with Format of
Mole
FractionMole
Fraction
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125
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2. Specify pump outlet specificati
1. Select “Pump” or “turbine”
(pressure, power)
3. Efficiencies (Default: 1)
128
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Check “simulation status”
“Re uired In ut Com lete”
129
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Right Click on the block and select Results
130
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131
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132
Calculation Results Calculation Results
(Mass
and
Energy
Balances)(Mass
and
Energy
Balances)
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1 2 3 4
Mole Flow kmol/hr
WATER 10 0 10 10BUOH 0 9 9 9
BUAC 0 6 6 6
Total Flow kmol/hr 10 15 25 25
Temperature C 50 80 70.09 71.20
Pressure bar 1 1 1 10
Enthalpy kcal/mol -67.81 -94.37 -83.75 -83.69
Entropy cal/mol-K -37.50 -134.95 -95.62 -95.46
Density kmol/cum 969.50 783.85 825.56 824.29133
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1 2 3 4 5 6
Mole Flow kmol/hr
Water 10 0 0 ? ? ?
Ethanol 0 5 0 ? ? ?
Methanol 0 0 15 ? ? ?
Total Flow kmol/hr 10 15 15 ? ? ?
Temperature C 50 70 40 ? ? ?
Pressure bar 1 1 1 1 4 2
Enthalpy kcal/mol ? ? ? ? ? ?Entropy cal/mol-K ? ? ? ? ? ?
Densit kmol/cum ? ? ? ? ? ?
134Please use Peng-Robinson EOS to solve this problem.
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120
115
-x
T-y
Saturated Feed
T=105 C
P=1atm
110
T ( o C )
P=1atm
F=100 kmol/hr
z =0.5 0.0 0.2 0.4 0.6 0.8 1.0100
zHAc=0.5 xWater and yWater
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‐‐
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Vapor ESHOC
Li uid
ammaLiquid enthalpy
Liquid volume
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‐‐
1 S l t l i t (T )
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1. Select analysis type (Txy) 2. Select hase VLE VLLE
2. Select two component 5. Specify pressure
6. Select property method.
4. Specify composition range
7. click Go to generate the results
‐‐
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Data results
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’’
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120
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120
115
-x
T-y
Saturated Feed
T=105 C
P=1atm
110
T ( o C )
P=1atm
F=100 kmol/hr
z =0.5 0.0 0.2 0.4 0.6 0.8 1.0100
zHAc=0.5 xWater and yWater
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Saturated Feed
(Vapor fraction=0)
P=1atm
F=100 kmol/hr
zwater =0.5
zHAc=0.5
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T=105 C= a m
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Close binary analysis window
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’’
42.658 kmol/hr
z =0.501
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zHAc=0.409
T=105 CSaturated Feed
P=1atm
P=1atm
zwater =0.5zHAc=0.5
57.342 kmol/hr z =0.432
zHAc=0.568
1
McCabe- Thiele Graphical Method
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L D
Rectifying section: 0.8
1n n D
R R
y x xV V
Stripping section:
0.6
y
1
S
n n B
S S
L B y x x
V V
0.4
0
.
. . . .
x
TradeTrade‐‐off Between off Between
Capital Cost and Operating CostCapital Cost and Operating Cost
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Shortcut Design:
RR≈1.2 RRmin
NT ≈ 2 NTmin
• There are two degrees of
freedom to manipulate
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isti ate
composition
an
bottoms composition to
RR ?
bottoms compositions.
•
number of stages are given,
how much of RR and QR are QR ?
required to achieve the
specification.
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RadFrac numbers stages from the top down, starting with the condenser
(or starting with the top stage if there is no condenser).
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Saturated Feed
(Vapor fraction=0)
P=1.2atmF=100 kmol/hr
zwater =0.5
zHAc=0.5
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Use this convention To introduce a feed
Above‐sta e Between sta es, above the desi nated sta e
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On‐stage On
the
designated
stage
‐ ‐
On the designated stage, all‐liquid feed
which is never flashed
On‐stage
‐vapor
On the designated stage, all‐vapor feed
Decanter To the decanter attached to the designated
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Click to run simulation
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D B
Click to run simulation
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Increase RR from 2 to 2.5
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D B
……
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.
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Aspen Plus provides a convenient function (Design Specs/Vary)
which can iterate operating variables to meet the specification.
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Input current mole purity first
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Specify the range of the adjusted variable
.
In this case, only reflux ratio and reboiler duty can be used.
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correspond to the operating specification.
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Click to run simulation
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Increase Target from 0.95229424 to 0.99
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D B
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nc u e con enser u y, s a e ra e, re ux ra e, re ux ra o
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nc u e re o er u y, o oms ra e, o up ra e, o up ra o
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’’
After enterin the block “Plot” a ears.
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Some
Tips
and
Others
202
Invokes the Aspen Plus expert system. Guides you through theste s re uired to com lete our simulation.
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Status message Meaning
Flowsheet Not
CompleteFlowsheet
connectivity
is
incomplete.
To
find
out
why,
click
the Next button in the toolbar.
Required Input Not Input specifications for the run are incomplete. Click Next
Comp ete on t e too ar to n out ow to comp ete t e nput
specifications, and to go to sheets that are incomplete.
203
“ ”“ ”
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204
“ ’ ”“ ’ ”
c an en c c w ere you on now
?
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?
205
“ ’ ”“ ’ ”
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?
206
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If you are using You should
Workbook mode Click the Process Flowsheet tab
Flowsheet as Wallpaper Click the flowsheet in the background
Normal View Select the Process Flowsheet window207
Go to “Hel ”
Select “Help Topics”
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208
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n pera on o e e erence anua
Physical Property Methods and Models
Physical Property Data Reference Manual
209
Calculation of Properties Using an Equation-of-State Property Method
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210
Fil T E t i F t D i ti
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File Type Extension Format Description
Document *.apw Binary File containing simulation input and results and
n erme a e convergence
n orma on
Backup *.bkp ASCII Archive file containing simulation input and
results
History *.his Text Detailed calculation history and diagnostic
messages*
211
Description
.
convergence information used in the simulation
calculations
• Binary
i es
– Operating system and version specific
– ,
• ASCII
files – Transferable between operating systems
– Upwardly compatible
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Upwardly compatible
– Contain no control characters, “readable”
– ot
nten e
to
e pr nte
• Text files
–
– Upwardly compatible
– Readable, can be edited
– Intended to be printed
212
• Please contact
PC
Teaching
Assistant:
Name: 侯冠宇
Phone:
02‐
3366‐
3005 . .
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Office: 101 電腦教室
213
如何進入講義 載及填寫問卷何進入講義 載及填寫問卷何進入講義 載及填寫問卷何進入講義 載及填寫問卷