Designer: Fatma Al-Turkait Supervised by: Prof.M.Fahim Eng.Yusuf Ismail

Designer:Fatma Al-Turkait

Supervised by: Prof.M.Fahim

Eng.Yusuf Ismail

Agenda

Distillation column design

Compressor design

Valve design

Distillation column design

Introduction:Distillation unit is used to separate the components by their volatilities (Boiling point Temperature).

Objective: To separate CO and CO2 from propane and propene

Types of distillation columns

One way of classifying distillation column type is to look at how they are operated .

Thus we have:

Continuous Columns

Batch Columns

Continuous Columns

Batch Columns

1 -Regular batch column.

2 -It is also possible to locate the feed vessel at the top of a stripping column and to operate the column as an inverted batch column.

3 -Middle vessel column

The type of column Internals:

Bubble cap trays ,valve trays ,and sieve trays.

The best type for our process Is continuous distillation and sieve trays.

Material construction

The material chosen for our equipments is carbon steel due to its low cost and ease fabrication . In addition, it resists corrosion.

Main design parametersA- Number of stages

B- Dimensions:

1-Diameter

2-Height

3-Tray Design

4-Wier

5-Thickness

6-Cost

A- Minimum and Actual number of stages

)1(Number of stagesCalculate vapor pressure of the light and heavy key components by Antoine equation.

Where: a, b, c, d, e & f are Antoine Coefficient.

)2(Determine the values of liquid-gas constant (K) for both the light and heavy key components.

)3(Calculate the average relative volatility of the light key with respect to the heavy key.

Where,

feTTdcT

baP

)ln()ln(

P

PK i

bCtCC)()(

222

3

2

2,)(

C

CbC K

K

)4(Obtain the minimum number of stages by Fenske equation

)5(Estimate the plate efficiency.Plate efficiency = 0.6

Obtain the actual number of stages

)(Log

x

x

x

xLog

N2

2

3

3

2

C

bC

C

tC

C

m

efficiencyplate

NN m

Detailed calculation for Nm,N

• Open File

Diameter

5.0// LVWWLV VLF

liquid vapor flow rate

1975.076.585/601.21066.2/104.4 5.044

2.011 20/tensionSurfaceKK

140347.020/014005.06.0 2.0

Correction for surface tension

5.0

1 / VVLF Ku

sm /118274.2601.2/601.276.585140347.0

.

The flooding vapor velocity (m/s).

The actual velocity based on net area.

Maximum volumetric flow rate

Net area required

As first trial take down comer area as %12 of the total column cross sectional areaA@12%

= net area required / 0.88

smUU Fn /800533.1118274.285.085.0

sm /886184.2601.23600/074.285.947 3

VMwtVV 3600/max

nnet urateflowvolumetricA /max2602961.1800533.1/886184.2 m

2821547.188.0/602961.1 m

Column diameter

5./4 netAD

m522936.1/4821547.1 5.0

Height

H=N*Spacing

H=30*.9=27 m

Tray design

Column area (m2) 24/ DAc

Down comer area (m2) ActotalofareacomerdownofPercentAd

The net area (m2) AdAcAn

AdAcAa 2The active area (m2)

2603009.1218592.0821601.1 m

234416.1218592.02821601.1 m

2218592.0821601.112.0 m

22 821601.1522936.14/ m

weir

Ad/Ac=0.21859/1.82*100

= 12%

Iw/Dc=0.76

Dc=1.522936m

Iw=1.157431m

weir height=50mm

Hole diameter=5mm

Plate thickness=5mm

Check weeping

K2=30.9 from graph @Minimum rate (hw + how)

uh=[K2-0.90(25.4-dh)]/g0.5

Actual min vap=145.9 m/s

3/2/max750 lengthweirrateliquidhMax low

liquid mm 51.69409

3/2L/min750 lengthweirrateliquidhMin ow

liquid mm 40.75425

liquid mm 90.75425 40.7542550

sm /8.75601.2/54.259.09.30 5.0

Downcomer backup

owtdcwb hhhhh

51.69409 260.3317 33.97246 50 mm998.395

hb < .475(.5*(plate spacing +weir height)

m395998.0

Number of holes

Area of one holes=

Number of holes=Ah/Ahole=

Holes on one plate= Numbers of holes/actual number of plates =705.1

23-105/4 -5101.964

-510.9640.138442/1

7051

Shell thickness

Where;t: shell thickness (in)P: internal pressure (psig)ri: internal radius of shell (in)EJ: efficiency of jointsS: working stress (psi)Cc: allowance for corrosion (in)

cJ

i CPSE

t

6.0

Pr

11025.139.296.085.013700/97905.2939.29 t

mmt 1.5

Cost

Cost=Vessel cost+ Trays cost+ Reboile Cost+ Condenser unit cost

Cost=$21800+12000+36200+49800

$= 119800

Results: Equipment nameT-101

TypeContinuous distillation LocationAfter T-100 distillation

Material of Construction Carbon steel

Insulation Glass wool

Cost ($) 119800

Number of stages (hysis)10

Tray spacing0.9

Type of tray Sieve tray

Diameter (m) 1.522936

Height (m) 10.5

Number of Holes 705

Compressor design

Procedure

1 -Select centrifugal compressor (single stage) according to this figure.

1 .Calculate the adiabatic head for a compressor(k100)

2 .Calculate the adiabatic power for single stage compression.

3 .Calculate the adiabatic discharge temperature.

9 .Calculate the adiabatic efficiency .

1/1/ /1121

' kkad PPkkTRH N.m/kg 0.247129

hpKW 38.24107.180 adP adHm

kkPPTT /11212 /

K35.860

1/1//1/1/ 1212 nnPPkkPPad = 72.02%

Cost

K101= 49300

K100= 53800

Specification for compressor K100

Equipment nameCompressor

TypeCentrifugal Compressor, single stage

LocationAfter CRV-103/ propylene process

Material of Construction Carbon steel

Insulation Glass wool objectiveTo increase the pressure of stream

12

Cost $49300

Power (Hp)8.0757

Efficiency (%)73.693

Inlet Temperature485.7 (C°)

Outlet Temperature626.1 (C°)

Inlet Pressure

Outlet Pressure

14.7 (psia)

44.09

Equipment nameCompressor

TypeCentrifugal Compressor, single stage

LocationAfter V-101/ amine process

Material of Construction Carbon steel

Insulation Glass wool objectiveTo increase the pressure of stream

1

Cost $53800 Power (Hp)35.66

Efficiency (%)89.418

Inlet Temperature25 (C°)

Outlet Temperature695.3 (C°)

Inlet Pressure

Outlet Pressure

14.7 (psia)

734.8

Specification for compressor K101

Valve design

Introduction:A valve is a device that regulates the flow of substances either gases, fluidized solids, slurries, or liquids) by opening, closing, or partially obstructing various passageways.

Objective: to reduce the pressure of flow rates.

Main design parameter

Valve Type

Pipe Diameter

Cost

Valve Type globe valve

Best Suited Control : Linear and Equal percentage.Recommended Uses:  Throttling service/flow regulation, Frequent operation.Applications: Liquids, vapors, gases, corrosive substances, slurries. Advantages:

1 .Efficient throttling2 .Accurate flow control

3 .Available in multiple ports.

Disadvantages:1 .High pressure drop

2.More expensive than other valves.

Pipe diameter

A=V/v

A=2.177E-3 m2

D=(A*4/ )0.5

D=0.526 m

Cost

Thank you for listening