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

[email protected]

PSE Laboratory

Nation Taiwan

University



• 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



• 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



• 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



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



• Familiar with the interface of Aspen Plus

• Learn how

to

use

properties

analysis

• Learn how to setup a basic process simulation

6



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



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



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



• 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



Introduction to Aspen Plus – Part 1

Startup in Aspen Plus

11



spen us ser n er ace

12



13



Process Flowsheet WindowsProcess Flowsheet Windows

Model Librar View Model LibrarModel Librar View Model Librar

Stream

Status message14



Help for Commands for Controlling Simulations 15



• 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



17



• The minimum required inputs to run a simulation

are: – Setup

– Components Property Analysis

– Properties – Streams

– Blocks

18



Input mode

19



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



npu componen s

with Component name or Formula

21



Remark: If available, are

22



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



Click “Find”

24



’’

In ut Com onent name or Formula or CAS number

25



26



methods available)

, , , …

27



Interactive help in choosing a property method

28



Specify Component type

Chemical Systems

Is the system at high pressure?

(NO)

Two liquid phases

29



30Reference: http://www.et.byu.edu/groups/uolab/files/aspentech/



Vapor EOS

NRTL Liquid

gammaLiquid enthalpy

qu vo ume

31



Check “Modif Pro ert Model”

S ecif New Method Name

32



c an en u - n nary parame ers

appear automatically if available.

33



Access Properties Models and Access Properties Models and

ParametersParameters

Review Databank Data

34



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



Help for Pure Component Databank Parameters 36



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



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



Example: CPIGDPExample: CPIGDP‐‐1 1

(Ideal Gas

Heat

Capacity

Equation)(Ideal

Gas

Heat

Capacity

Equation)

Corresponding Model

39



So far, we have finished the basicsettings including setup, components,

and properties.

This is enough to perform properties

ana ys s.

40



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



• 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

–


– Readable, can be edited

– Intended to be printed

42




Properties Analysis in Aspen Plus

43



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



• When you start properties analysis, you MUST

s ecif com onents ,

ro erties model,

and

corresponding model parameters. (Refer to

45



Use this form To generate


and pressure

Binary Txy, Pxy,

or

Gibbs

energy

of

mixing

curves

for

a

binary

system


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



Tie lines, Vapor curve, Boiling point

Generic




than three) is also included.

46



47



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



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



Data results 50



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



Data results

52





and pressure

Binary Txy, Pxy,

or

Gibbs

energy

of

mixing

curves

for

a

binary

system




locates

all

the

azeotropes that

exist

among

a

specified

set

of

components.

Ternary Maps




Generic





53







‐‐

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.




‐‐

Data results



Click “plot wizard” to generate XY plot

’’



’’



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.





and pressure

Binary Txy,

Pxy,

or

Gibbs

energy

of

mixing

curves

for

a

binary

systemResidue Residue curve maps



locates

all

the

azeotropes that

exist

among

a

specified

set

of

components.

Ternary Maps




Generic

Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures



61





4. Select phase (VLE, LLE)

.

5. Specify pressure2. Specify number of tie line

3. Select property method

6. Specify temperature

(if LLE is slected)




a a resu s





and pressure

Binary Txy,

Pxy,

or

Gibbs

energy

of

mixing

curves

for

a

binary

systemResidue Residue curve maps



locates

all

the

azeotropes that

exist

among

a

specified

set

of

components.

Ternary Maps




Generic

Tables and

plots

of

properties

of

either

multi

‐phase

mixtures

(for

example,




Generic analysis is used if properties analysis of mixture is performed.65



Enthalpy of Mixtures?

Water-BuOH

110

120

90

T ( o C )

660.0 0.2 0.4 0.6 0.8 1.070




Select Property analysis

67



Select Generic

68



. Select “flash calculation” or not 3. Specify component flo

2. Select phase (VLE, LLE)

. pec y e correspon ng compos on

69



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



Calculation ResultsCalculation Results

71



’’‐‐



…

Select “Vapor” “1st liquid” “2nd liquid”

73

‐‐



74



Check “simulation status”

.

75

Example1: Calculation of Enthalpy Example1: Calculation of Enthalpy



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



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



Temperature

Temperature VariesVaries

1

3

4

78



79



-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



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


81

’’ ‐‐



Select “Vapor” “1st liquid” “2nd liquid

, , ‐‐



1 2

Select Vapor-liquid-liquid

3

4



120

Water-BuOH

90

100

T ( o C )

0.0 0.2 0.4 0.6 0.8 1.070

80




Use this form To generate(Optional)


and pressure

,

,


Ternar ma s showin hase envelo e, tie lines, and azeotro es of ternar

ernarysystems


locates

all

the

azeotropes that

exist

among

a

specified

set

of

com onents.

Ternary Maps



, ,

Generic



‐ .


85





• 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





1. Select components (at least two) 2. Specify pressure

3. Select property method

6. click Report to generate the results

. ,

5. Select report Unit



Close analysis

input

dialog

box

(pure

or

binary

analysis)







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



Change pressure or

Ternary Plot Toolbar:Add Tie line, Curve,

Marker…




Running Simulation in Aspen Plus

95

Example 1: Calculate the mixing Example 1: Calculate the mixing

properties of two streamproperties of two stream



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



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)



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



Select Flowsheet

99



or press F10

100



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



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



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



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



Click “Materials” and then click

105

’’



,

arrows (blue and red) appear.

106

’’



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



Reconnecting Material Streams Reconnecting Material Streams

(Feed Stream)(Feed Stream)



(Feed Stream)(Feed Stream)

Right Click on the stream and

select Reconnect Destination

109

Reconnecting Material Streams Reconnecting Material Streams

(Product Stream)(Product Stream)



(Product Stream)(Product Stream)

Right Click on the stream and

B1

1

2

3

110



Right Click on the stream

111



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

’’



1 2

113



Right Click on the block and select Input

114

’’



Specify Pressure and valid phase

The corresponding description about this blank:

Outlet pressure if value > 0

Pressure drop if value 0

115



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


“Re uired In ut Com lete” means the in ut is read to run simualtion

116



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



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



select Stream Results

119

1 2 3

Substream: MIXED

Mole Flow kmol/hr

WATER 10 0 10

BUAC 0 6 6



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



121



122



123

Stream Results with Format of Stream Results with Format of

Mole

FractionMole

Fraction



124



125



126



127



2. Specify pump outlet specificati

1. Select “Pump” or “turbine”

(pressure, power)

3. Efficiencies (Default: 1)

128




“Re uired In ut Com lete”

129



Right Click on the block and select Results

130



131



132

Calculation Results Calculation Results

(Mass

and

Energy

Balances)(Mass

and

Energy

Balances)



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



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.



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



‐‐



Vapor ESHOC

Li uid

ammaLiquid enthalpy

Liquid volume









‐‐

1 S l t l i t (T )



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


‐‐



Data results



’’



120



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







Saturated Feed

(Vapor fraction=0)

P=1atm

F=100 kmol/hr

zwater =0.5

zHAc=0.5





T=105 C= a m



Close binary analysis window





’’

42.658 kmol/hr

z =0.501



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



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



Shortcut Design:

RR≈1.2 RRmin

NT ≈ 2 NTmin

• There are two degrees of

freedom to manipulate



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.







RadFrac numbers stages from the top down, starting with the condenser

(or starting with the top stage if there is no condenser).





Saturated Feed

(Vapor fraction=0)

P=1.2atmF=100 kmol/hr

zwater =0.5

zHAc=0.5







Use this convention To introduce a feed

Above‐sta e Between sta es, above the desi nated sta e



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



Click to run simulation









D B




Increase RR from 2 to 2.5



D B

……



.



Aspen Plus provides a convenient function (Design Specs/Vary)

which can iterate operating variables to meet the specification.





Input current mole purity first









Specify the range of the adjusted variable

.

In this case, only reflux ratio and reboiler duty can be used.



correspond to the operating specification.








Increase Target from 0.95229424 to 0.99





D B





nc u e con enser u y, s a e ra e, re ux ra e, re ux ra o



nc u e re o er u y, o oms ra e, o up ra e, o up ra o









’’

After enterin the block “Plot” a ears.















Some

Tips

and

Others

202

Invokes the Aspen Plus expert system. Guides you through theste s re uired to com lete our simulation.



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

“ ”“ ”



204

“ ’ ”“ ’ ”

c an en c c w ere you on now

?



?

205

“ ’ ”“ ’ ”



?

206



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”



208



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



210

Fil T E t i F t D i ti



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

– Contain no control characters, “readable”

– ot

nten e

to

e pr nte

• Text files

–


– Readable, can be edited

– Intended to be printed

212

• Please contact

PC

Teaching

Assistant:

Name: 侯冠宇

Phone:

02‐

3366‐

3005 . .



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



Aspen-Plus Ternary Mixture

Documents