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Introduction to Aspen Plus
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Introduction to Aspen PlusShort Courses on Computer Applications for ChE Students
Speaker: Yi-Chang Wu ( 吳義章 )[email protected]
PSE LaboratoryDepartment of Chemical Engineering
Nation Taiwan University
• Extractive Distillation
Extractive distillation column
Entrainer recovery column
F2
XIPA=0.999
IPA-water feed (FF)
Entrainer feed (FE)
Entrainer recycle
Entrainer makeup
D2
B2
NFE
NFF
NF2
NT = 41NFE = 7NFF = 35
NT = 24NF2 = 9
XWater=0.999D2
P = 3 atm T = 25oC F = 100 kmol/hr X IPA =0.5 X WATER =0.5
What is Aspen PlusWhat is Aspen Plus
• 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.
3Ref: http://www.aspentech.com/products/aspen-plus.cfm
What Aspen Plus providesWhat Aspen Plus provides
• Physical Property Models– World’s largest database of pure component and phase equilibrium
data for conventional chemicals, electrolytes, solids, and polymers– 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– Extends steady-state simulation to dynamic simulation for safety and
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 Brochure4
More DetailedMore Detailed
• 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 points…etc)– Data regression from experimental deta
• Process simulation– pump, compressor, valve, tank, heat exchanger, CSTR, PFR,
distillation column, extraction column, absorber, filter, crystallizer…etc
5
What course Aspen Plus What course Aspen Plus can be employed forcan be employed for
• MASS AND ENERGY BALANCES• PHYSICAL CHEMISTRY• CHEMICAL ENGINEERING THERMODYNAMICS • CHEMICAL REACTION ENGINEERING • UNIT OPERATIONS• PROCESS DESIGN • PROCESS CONTROL
6
Lesson ObjectivesLesson Objectives
• Familiar with the interface of Aspen Plus• Learn how to use properties analysis• Learn how to setup a basic process simulation
7
Problem Formulation 1: Calculation Problem Formulation 1: Calculation the mixing properties of two stream the mixing properties of two stream
1
23
4
Mixer Pump
1 2 3 4Mole 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 ? ? ? ?
8
Mass Balance
Energy Balance Enthalpy Entropy…
Problem Formulation 2: Problem Formulation 2: Flash SeparationFlash Separation
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
T=105 CP=1atm
What are flowrates and compositions of the two outlets?
0.0 0.2 0.4 0.6 0.8 1.0100
105
110
115
120
T (
o C)
xWater
and yWater
T-x T-y
Problem Formulation 3: Dehydration of Problem Formulation 3: Dehydration of Acetic Acid by Distillation Column Acetic Acid by Distillation Column
0.0 0.2 0.4 0.6 0.8 1.00.0
0.2
0.4
0.6
0.8
1.0
y Wat
er
xWater
1
2
39
Saturated Feed P=1.2atm F=100 kmol/hr zwater=0.5 zHAc=0.5
xwater=0.99
xHAc=0.9940
20Water
Acetic Acid
Water
Acetic Acid
Reflux ratio ?
Duty ?
(Optional)(Optional)
OutlineOutline
• 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
11
Introduction to Aspen Plus – Part 1Startup in Aspen Plus
12
Start with Aspen Plus
Aspen Plus User Interface
Aspen Plus StartupAspen Plus Startup
14
Interface of Aspen PlusInterface of Aspen Plus
Process Flowsheet Windows
Model Library (View| Model Library )
Stream
HelpSetupComponentsPropertiesStreamsBlocksData BrowserNext
Check ResultStopReinitializeStepStartControl Panel
Process Flowsheet Windows
Model Library (View| Model Library )
Status message15
More InformationMore Information
Help for Commands for Controlling Simulations 16
Data BrowserData Browser
• 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
17
Basic InputBasic Input
• The minimum required inputs to run a simulation are:– Setup– Components– Properties– Streams– Blocks
Property Analysis
Process Simulation
18
Setup – SpecificationSetup – SpecificationRun Type
Input mode
19
Components – SpecificationComponents – Specification
Input componentswith Component name or Formula
20
Input componentsInput components
Remark: If available, are
21
SpecificationSpecification
To do this Click this buttonFind components in the databanks FindDefine a custom component that is not in a databank
User Defined
Generate electrolyte components and reactions from components you entered
Elec Wizard
Reorder the components you have specified
Reorder
Review databank data for components you have specified (Retrieved physical property parameters from databanks.)
Review
22
Find ComponentsFind Components
Click “Find”
23
Find Components (cont’d)Find Components (cont’d)
24
PropertiesProperties
Process type(narrow the number ofmethods available)
Base method: IDEAL, NRTL, UNIQAC, UNIFAC…
25
Property Method Selection – AssistantProperty Method Selection – Assistant
Interactive help in choosing a property method
26
Specify Component typeChemical Systems
Is the system at high pressure?(NO)
Two liquid phases
Assistant WizardAssistant Wizard
27
28
Property Method Choice
Polar orT < Tci
No
Yes
Property Methods Decision Diagram
Electrolyte
No Pseudo Components
Pr < 0.1 & T < Tci
No
Yes
ELECNRTL
Yes
PENG-ROBPR-BM
LK-PLOCKRK-SOAVE
RKS-BM
No High Pressure?
CHAO-SEAGRAYSON
BK10
BK10IDEAL
Yes
No
Interaction ParametersAvailable?
Interaction ParametersAvailable?
Yes
No
PSRKRKSMHV2
SR-POLARPRWS
RKSWSPRMHV2
RKSMHV2
Liq-Liq
Liq-Liq
Yes
No
Yes
No
NRTLUNIQAC
etc.
WILSONNRTL
UNIQACetc.
UNIF-LL
UNIFACUNIF-LBYUNIF-DMD
Yes
No
Yes
No
Vapor-phase Association?
WILSON, WILS-RK, WILS-LR, WILS-GLR, NRTL, NRTL-RK, NRTL-2,
UNIQUAC, UNIQ-RK, UNIQ-2, UNIFAC, UNIF-LL, UNIF-LBY, UNIF-DMB
WILS-HF
WILS-NTH, WILS-HOC, NRTL-NTH, NRTL-HOC, UNIQ-NTJ, UNIQ-HOC,
UNIF-HOC
Degree of Polymerization
No
Yes
Hexamers
Dimers
A
A
A
A
A
Reference: http://www.et.byu.edu/groups/uolab/files/aspentech/
Thermodynamic Model – NRTLThermodynamic Model – NRTL
NRTL
29
NRTL – Binary ParametersNRTL – Binary Parameters
Click “NRTL” and then built-in binary parameters appear automatically if available.
30
Access Properties Models and Access Properties Models and ParametersParameters
31
Review Databank Data
Review Databank DataReview Databank Data
Description of each parameter
Including:Ideal gas heat of formation at 298.15 KIdeal gas Gibbs free energy of formation at 298.15 KHeat of vaporization at TBNormal boiling pointStandard liquid volume at 60°F….
32
Pure Component Pure Component Temperature-Dependent PropertiesTemperature-Dependent Properties
CPIGDP-1 ideal gas heat capacity
CPSDIP-1 Solid heat capacity
DNLDIP-1 Liquid density
DHVLDP-1 Heat of vaporization
PLXANT-1 Extended Antoine Equation
MULDIP Liquid viscosity
KLDIP Liquid thermal conductivity
SIGDIP Liquid surface tension
UFGRP UNIFAC functional group
33
Example: PLXANT-1 Example: PLXANT-1 (Extended Antoine Equation)(Extended Antoine Equation)
?
Corresponding Model
Click “ ?” and then click where you don’t know ↖
34
Example: CPIGDP-1 Example: CPIGDP-1 (Ideal Gas Heat Capacity Equation)(Ideal Gas Heat Capacity Equation)
?
Corresponding Model
35
SummarySummary
So far, we have finished the basic settings including setup, components, and properties.This is enough to perform properties analysis.
36
File Formats in Aspen PlusFile Formats in Aspen Plus
37
File Type Extension Format Description
Document *.apw Binary File containing simulation input and results andintermediate convergence information
Backup *.bkp ASCII Archive file containing simulation input andresults
History *.his Text Detailed calculation history and diagnosticmessages
Problem Description
*.appdf Binary File containing arrays and intermediateconvergence information used in the simulationcalculations
Introduction to Aspen Plus – Part 2Properties Analysis in Aspen Plus
38
Overview of Property AnalysisOverview of Property Analysis
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 systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
39
RemindingReminding
• When you start properties analysis, you MUST specify components , properties model, and corresponding model parameters. (Refer to Part I)
40
Properties Analysis – Pure Component Properties Analysis – Pure Component
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 systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
41
Properties Analysis – Pure Component Properties Analysis – Pure Component
42
Available PropertiesAvailable PropertiesProperty (thermodynamic) Property (transport)
Availability Free energy Thermal conductivityConstant pressure
heat capacity Enthalpy Surface tension
Heat capacity ratio Fugacity coefficient ViscosityConstant volume heat
capacityFugacity coefficient pressure correction
Free energy departure Vapor pressure Free energy departure
pressure correction Density
Enthalpy departure EntropyEnthalpy departure pressure correction Volume
Enthalpy of vaporization Sonic velocity
Entropy departure 43
Example1: CP (Heat Capacity)Example1: CP (Heat Capacity)
1. Select property (CP)
2. Select phase
3. Select component
4. Specify range of temperature
5. Specify pressure
6. Select property method
7. click Go to generate the results
Add “N-butyl-acetate”
44
Example1: Calculation Results of CPExample1: Calculation Results of CP
Data results 45
Example2: H (Enthalpy)Example2: H (Enthalpy)
1. Select property (H)
2. Select phase
3. Select component
4. Specify range of temperature
5. Specify pressure
6. Select property method
7. click Go to generate the results46
Example: Calculation Results of HExample: Calculation Results of H
Data results
47
Properties Analysis – Binary ComponentsProperties Analysis – Binary Components
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 systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
48
Properties Analysis – Binary ComponentsProperties Analysis – Binary Components
Binary Component Properties AnalysisBinary Component Properties Analysis
Use this Analysis type To generate
Txy Temperature-compositions diagram at constant pressure
Pxy Pressure-compositions diagram at constant temperature
Gibbs energy of mixing
Gibbs energy of mixing diagram as a function of liquid compositions. The Aspen Physical Property System uses this diagram to determine whether the binary system will form two liquid phases at a given temperature and pressure.
Example: T-XYExample: T-XY1. Select analysis type (Txy)
2. Select phase (VLE, VLLE)
2. Select two component
4. Specify composition range
5. Specify pressure
6. Select property method
3. Select compositions basis
7. click Go to generate the results
Example: calculation result of T-XYExample: calculation result of T-XY
Data results
Example: Generate XY plotExample: Generate XY plot
Click “plot wizard” to generate XY plot
Example: Generate XY plot (cont’d)Example: Generate XY plot (cont’d)
Property Analysis – GenericProperty Analysis – Generic
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 systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
55
Properties Analysis – TernaryProperties Analysis – Ternary
Ternary MapTernary Map
4. Select phase (VLE, LLE)
1. Select three component
5. Specify pressure
3. Select property method
2. Specify number of tie line
7. click Go to generate the results
6. Specify temperature (if LLE is slected)
Calculation Result of Ternary Map (LLE)Calculation Result of Ternary Map (LLE)
Data results
Property Analysis – Conceptual DesignProperty Analysis – Conceptual Design
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 systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
59
(Optional)
Conceptual DesignConceptual Design
Azeotrope AnalysisAzeotrope Analysis
Azeotrope AnalysisAzeotrope Analysis
4. Select phase (VLE, LLE)
1. Select components (at least two) 2. Specify pressure
3. Select property method
5. Select report Unit
6. click Report to generate the results
Error MessageError Message
Close analysis input dialog box (pure or binary analysis)
Azeotrope Analysis ReportAzeotrope Analysis Report
Ternary MapsTernary Maps
Ternary MapsTernary Maps
4. Select phase (VLE, LLE)1. Select three components
2. Specify pressure
3. Select property method
5. Select report Unit
6. Specify temperature of LLE (If liquid-liquid envelope is selected)
6. Click Ternary Plot to generate the results
Ternary MapsTernary Maps
Ternary Plot Toolbar:Add Tie line, Curve, Marker…
Change pressure or temperature
Introduction to Aspen Plus – Part 3 Running Simulation in Aspen Plus
68
Example 1: Calculate the mixing Example 1: Calculate the mixing properties of two stream properties of two stream
1
23
4
Mixer Pump
1 2 3 4Mole 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 ? ? ? ?
69
Setup – SpecificationSetup – Specification
Select Flowsheet
70
Reveal Model LibraryReveal Model Library
View|| Model Libraryor press F10
71
Adding a MixerAdding a Mixer
Click “one of icons” and then click again on the flowsheet window
Remark: The shape of the icons are meaningless
72
Adding Material StreamsAdding Material Streams
Click “Materials” and then click again on the flowsheet window
73
Adding Material Streams (cont’d)Adding Material Streams (cont’d)
When clicking the mouse on the flowsheet window,arrows (blue and red) appear.
74
Adding Material Streams (cont’d)Adding Material Streams (cont’d)
When moving the mouse on the arrows, some description appears.
Blue arrow: Water decant for Free water of dirty water.
Red arrow(Left) Feed (Required; one ore more if mixing material streams)
Red arrow(Right): Product (Required; if mixing material streams)
75
Adding Material Streams (cont’d)Adding Material Streams (cont’d)
After selecting “Material Streams”, click and pull a stream line.Repeat it three times to generate three stream lines.
76
Reconnecting Material Streams Reconnecting Material Streams (Feed Stream)(Feed Stream)
Right Click on the stream and select Reconnect Destination
77
Reconnecting Material Streams Reconnecting Material Streams (Product Stream)(Product Stream)
Right Click on the stream and select Reconnect Source
B1
1
2
3
78
Specifying Feed ConditionSpecifying Feed Condition
Right Click on the stream and select Input
79
Specifying Feed ConditionSpecifying Feed Condition
You must specify two of the following conditions:TemperaturePressureVapor fraction
You can enter stream composition in terms of component flows, fractions, or concentrations.
If you specify component fractions, you must specify the total mole, mass, or standard liquid volume flow.
80
Specifying Feed Condition (cont’d)Specifying Feed Condition (cont’d)
1 2
81
Specifying Input of MixerSpecifying Input of Mixer
Right Click on the block and select Input
82
Specifying Input of Mixer (cont’d)Specifying Input of Mixer (cont’d)
Specify Pressure and valid phase
The corresponding description about this blank:Outlet pressure if value > 0Pressure drop if value 0≦
83
Run SimulationRun Simulation
Click ► to run the simulation
Check “simulation status”“Required Input Complete” means the input is ready to run simualtion
Run Start or continue calculations
Step Step through the flowsheet one block at a time
Stop Pause simulation calculations
Reinitialize Purge simulation results
84
Status of Simulation Results Status of Simulation Results
Message Means
Results available The run has completed normally, and results are present.
Results with warnings
Results for the run are present. Warning messages were generated during the calculations. View the Control Panel or History for messages.
Results with errors Results for the run are present. Error messages were generated during the calculations. View the Control Panel or History for messages.
Input Changed
Results for the run are present, but you have changed the input since the results were generated. The results may be inconsistent with the current input.
85
Stream ResultsStream Results
Right Click on the block and select Stream Results
86
1 2 3Substream: MIXED Mole Flow kmol/hr
WATER 10 0 10 BUOH 0 9 9 BUAC 0 6 6
Total Flow kmol/hr 10 15 25Total Flow kg/hr 180.1528 1364.066 1544.218
Total Flow cum/hr 0.18582 1.74021 1.870509Temperature C 50 80 70.08758
Pressure bar 2 1 1Vapor Frac 0 0 0Liquid Frac 1 1 1Solid Frac 0 0 0
Enthalpy kcal/mol -67.81 -94.3726 -83.7476Enthalpy kcal/kg -3764.03 -1037.77 -1355.82Enthalpy Gcal/hr -0.6781 -1.41559 -2.09369
Entropy cal/mol-K -37.5007 -134.947 -95.6176Entropy cal/gm-K -2.0816 -1.48395 -1.54799Density kmol/cum 53.81564 8.619647 13.36534
Density kg/cum 969.5038 783.851 825.5604Average MW 18.01528 90.93771 61.76874
Liq Vol 60F cum/hr 0.1805 1.617386 1.797886
Pull down the list and select “Full” to show more properties results.
87
Enthalpy and Entropy
Change Units of Calculation ResultsChange Units of Calculation Results
88
Setup – Defining Your Own Units Set Setup – Defining Your Own Units Set
89
Setup – Report OptionsSetup – Report Options
90
Stream Results with Format of Stream Results with Format of Mole FractionMole Fraction
91
Add Pump BlockAdd Pump Block
92
Add A Material StreamAdd A Material Stream
93
Connect StreamsConnect Streams
94
Pump – Specification Pump – Specification
2. Specify pump outlet specification(pressure, power)
1. Select “Pump” or “turbine”
3. Efficiencies (Default: 1)
95
Run SimulationRun Simulation
Click ► to generate the results
Check “simulation status”“Required Input Complete”
96
Block Results (Pump)Block Results (Pump)
Right Click on the block and select Results
97
98
Streams ResultsStreams Results
99
Calculation Results Calculation Results (Mass and Energy Balances)(Mass and Energy Balances)
1
23
4
Mixer Pump
1 2 3 4Mole Flow kmol/hr
WATER 10 0 10 10 BUOH 0 9 9 9 BUAC 0 6 6 6
Total Flow kmol/hr 10 15 25 25Temperature C 50 80 70.09 71.20Pressure 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 969.50 783.85 825.56 824.29
100
ExerciseExercise12 4
6
Mixer Pump3
5
1 2 3 4 5 6Mole 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 ? ? ? ? ? ?Density kmol/cum ? ? ? ? ? ?
101Please use Peng-Robinson EOS to solve this problem.
Example 2: Flash SeparationExample 2: Flash Separation
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
T=105 CP=1atm
What are flowrates and compositions of the two outlets?
0.0 0.2 0.4 0.6 0.8 1.0100
105
110
115
120
T (
o C)
xWater
and yWater
T-x T-y
Input ComponentsInput Components
Thermodynamic Model: NRTL-HOCThermodynamic Model: NRTL-HOC
Check Binary ParametersCheck Binary Parameters
Association parameters of HOCAssociation parameters of HOC
Binary Parameters of NRTLBinary Parameters of NRTL
Binary AnalysisBinary Analysis
T-xy plotT-xy plot
1. Select analysis type (Txy) 2. Select phase (VLE, VLLE)
2. Select two component
4. Specify composition range
5. Specify pressure
6. Select property method3. Select compositions basis
7. click Go to generate the results
Calculation Result of T-xyCalculation Result of T-xy
Data results
Generate xy plotGenerate xy plot
Generate xy plot (cont’d)Generate xy plot (cont’d)
Flash SeparationFlash Separation
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
T=105 CP=1atm
What are flowrates and compositions of the two outlets?
0.0 0.2 0.4 0.6 0.8 1.0100
105
110
115
120
T (
o C)
xWater
and yWater
T-x T-y
Add Block: Flash2Add Block: Flash2
Add Material StreamAdd Material Stream
Specify Feed ConditionSpecify Feed Condition
Saturated Feed (Vapor fraction=0) P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
Block Input: Flash2Block Input: Flash2
Flash2: SpecificationFlash2: Specification
T=105 CP=1atm
Required Input IncompleteRequired Input Incomplete
Close binary analysis window
Connot click ► to run simulation
Required Input CompleteRequired Input Complete
Click ► to run simulation
Stream ResultsStream Results
Stream Results (cont’d)Stream Results (cont’d)
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
T=105 CP=1atm
42.658 kmol/hr zwater=0.501 zHAc=0.409
57.342 kmol/hr zwater=0.432 zHAc=0.568
1
2
39
Saturated Feed P=1.2atm F=100 kmol/hr zwater=0.5 zHAc=0.5
xwater=0.99
xHAc=0.99
40
20
Distillation SeparationDistillation Separation
• There are two degrees of freedom to manipulate distillate composition and bottoms composition to manipulate the distillate and bottoms compositions.
• If the feed condition and the number of stages are given, how much of RR and QR are required to achieve the specification.
RR ?
QR ?
Add Block: RadfracAdd Block: Radfrac
Add Material StreamAdd Material Stream
Connect Material StreamConnect Material Stream
Specify Feed ConditionSpecify Feed Condition
Saturated Feed (Vapor fraction=0) P=1.2atm F=100 kmol/hr zwater=0.5 zHAc=0.5
Block Input: RadfracBlock Input: Radfrac
Radfrac: ConfigurationRadfrac: Configuration
1
2
39
Saturated Feed P=1.2atm F=100 kmol/hr zwater=0.5 zHAc=0.5
xwater=0.99
xHAc=0.99
40
20
Radfrac: Streams (Feed Location)Radfrac: Streams (Feed Location)
1
2
39
Saturated Feed P=1.2atm F=100 kmol/hr zwater=0.5 zHAc=0.5
xwater=0.99
xHAc=0.99
40
20
Radfrac: Column PressureRadfrac: Column Pressure
Run SimulationRun Simulation
Click ► to run simulation
Check Convergence StatusCheck Convergence Status
Stream ResultsStream Results
D B
Change Reflux RatioChange Reflux Ratio
Click ► to run simulation
Increase RR from 2 to 2.5
D B
Again…Again…
You can iterate RR until the specification is achieved.
Smarter WaySmarter Way
Aspen Plus provides a convenient function (Design Specs/Vary) which can iterate operating variables to meet the specification.
Add New Design SpecsAdd New Design Specs
Design Specs: SpecificationDesign Specs: Specification
Input current mole purity first
Design Specs: ComponentsDesign Specs: Components
Design Specs: Feed/Product StreamsDesign Specs: Feed/Product Streams
Add New VeryAdd New Very
Very: SpecificationsVery: Specifications
Not all variables cane be selected.In this case, only reflux ratio and reboiler duty can be used.
Specify the range of the adjusted variable
Selection of Adjusted VariablesSelection of Adjusted Variables
The options of adjusted variables must correspond to the operating specification.
Run SimulationRun Simulation
Click ► to run simulation
Check Convergence StatusCheck Convergence Status
Change Target of Mole PurityChange Target of Mole Purity
Click ► to run simulation
Increase Target from 0.95229424 to 0.99
Check Convergence StatusCheck Convergence Status
D B
Column Performance SummaryColumn Performance Summary
Summary of CondenserSummary of Condenser
Include condenser duty, distillate rate, reflux rate, reflux ratio
Summary of ReboilerSummary of Reboiler
Include reboiler duty, bottoms rate, boilup rate, boilup ratio
Column Profile: TPFQColumn Profile: TPFQ
Column Profile: Vapor CompositionColumn Profile: Vapor Composition
Column Profile: Liquid CompositionColumn Profile: Liquid Composition
Plot Wizard for Column ProfilePlot Wizard for Column Profile
Plot Wizard for Column Profile (cont’d)Plot Wizard for Column Profile (cont’d)
After entering the block, “Plot” appears.
Plot WizardPlot Wizard
Plot TypesPlot Types
Steps for Composition PlotSteps for Composition Plot
Composition ProfilesComposition Profiles
Temperature ProfilesTemperature Profiles
Examples:
1.IPA-Water-DMSOIsopropyl Alcohol
WaterDimethyl Sulfoxide
INTRODUCTION TO ASPEN PLUSINTRODUCTION TO ASPEN PLUSMore Complex SystemMore Complex System
INTERFACE OF ASPEN PLUS
COMPONENTS – SPECIFICATION
Input componentswith Component name or Formula
167
Click “Find”
RENAME COMPONENTS IDRENAME COMPONENTS ID
168
Isopropyl AlcoholWater
Dimethyl Sulfoxide
Thermodynamic Model – NRTLThermodynamic Model – NRTL
NRTL
169
NRTL – Binary ParametersNRTL – Binary Parameters
Click “NRTL” and then built-in binary parameters appear automatically if available.
170
NRTL – Binary ParametersNRTL – Binary Parameters
171
NRTL – Binary Parameters-USERNRTL – Binary Parameters-USER
172
Comp,
iIPA IPA H2O
Comp,
jH2O DMSO DMSO
aij 0 0 -1.2449
aji 0 0 1.7524
bij 185.4 115.2787 586.801
bji 777.3 -25.0123 -1130.215
cij 0.50 0.3 0.30
Ternary Maps
Ternary MapsTernary Maps
4. Select phase (VLE, LLE)
1. Select three components
2. Specify pressure
3. Select property method
5. Select report Unit
6. Click Ternary Plot to generate the results
Ternary MapsTernary Maps
Ternary Plot Toolbar:Add Tie line, Curve,
Marker…
Change pressure
Entrainer / Azeotrope Feed Ratio
0.0 0.5 1.0 1.5 2.0 2.5 3.0
Rel
ativ
e V
ola
tility
(IP
A/H
2O)
1.0
1.5
2.0
2.5
3.0
3.5
4.0
4.5
DMSO
How to finish the relative volatility curve IPA – Water -DMSO System
ADD BLOCK: FLASH2
ADD MATERIAL STREAM
ADD MATERIAL STREAM
ADD MATERIAL STREAM
SPECIFY FEED CONDITION
Saturated Liquid Feed (Vapor fraction=0)
P=1 atm
F=10 kmol/hr zIPA=0.6932
zWATER=0.3068
Saturated Liquid Feed (Vapor fraction=0)
P=1 atm
F=10 kmol/hr zDMSO=1
BLOCK INPUT : FLASH2
Click ► to run simulation
LV
CHECK STREAMS RESULTCHECK STREAMS RESULT
2 2
1
/ 0.861/ 0.3463.23
/ 0.118 / 0.153IPA IPA
H O H O
Entrainer feedwhen
Azeotrope feed
y x
y x
A-F(kmol/h)
E-F(kmol/h)
(A-F)/(E-F) α
10 2.5 0.25 1.8
10 5 0.5 2.43
10 7.5 0.75 2.9
10 10 1 3.23
10 12.5 1.25 3.5
10 15 1.5 3.7
10 17.5 1.75 3.86
10 20 2 3.98
10 22.5 2.25 4.08
10 25 2.5 4.16
10 27.5 2.75 4.22
10 30 3 4.28
Entrainer / Azeotrope Feed Ratio
0.0 0.5 1.0 1.5 2.0 2.5 3.0
Rel
ativ
e V
olat
ility
(IP
A/H
2O)
1.0
1.5
2.0
2.5
3.0
3.5
4.0
4.5
DMSO
Finish the relative volatility curve IPA – Water -DMSO System
Introduction to Aspen PlusIntroduction to Aspen Plus
• Extractive Distillation
Extractive distillation column
Entrainer recovery column
F2
XIPA=0.999
IPA-water feed (FF)
Entrainer feed (FE)
Entrainer recycle
Entrainer makeup
D2
B2
NFE
NFF
NF2
NT = 41NFE = 7NFF = 35
NT = 24NF2 = 9
XWater=0.999D2
P = 3 atm T = 25oC F = 100 kmol/hr X IPA =0.5 X WATER =0.5
Aspen Plus Startup
INTERFACE OF ASPEN PLUS
SETUP – SPECIFICATION
Run Type
Input mode
188
Add Units-Sets
Add Units-Sets
REPORT OPTIONS
COMPONENTS – SPECIFICATION
Input componentswith Component name or Formula
192
Click “Find”
RENAME COMPONENTS IDRENAME COMPONENTS ID
193
Thermodynamic Model – NRTLThermodynamic Model – NRTL
NRTL
194
NRTL – Binary ParametersNRTL – Binary Parameters
Click “NRTL” and then built-in binary parameters appear automatically if available.
195
NRTL – Binary ParametersNRTL – Binary Parameters
196
NRTL – Binary Parameters-USERNRTL – Binary Parameters-USER
197
Comp,
iIPA IPA H2O
Comp,
jH2O DMSO DMSO
aij 0 0 -1.2449
aji 0 0 1.7524
bij 185.4 115.2787 586.801
bji 777.3 -25.0123 -1130.215
cij 0.50 0.3 0.30
ADD BLOCK: RADFRAC
ADD BLOCK: MIXERS
ADD MATERIAL STREAM
ADD MATERIAL STREAM
RENAME STREAM
SPECIFY FEED CONDITION Feed
(Saturated Liquid Feed) Vapor fraction = 0
P = 2 atm F = 100 kmol/hr
z IPA =0.5 z WATER =0.5
SPECIFY FEED CONDITION EF
P = 2 atm T = 184.5 oC
F = 100 kmol/hr z DMSO =1
SPECIFY FEED CONDITION MAKEUP
P = 2 atm T = 25 oC
F = 0 kmol/hr z DMSO =1
BLOCK INPUT
BLOCK INPUT
BLOCK INPUT
Click ► to run simulation
RUN SIMULATION
CHECK CONVERGENCE STATUS
Check result
CHECK STREAMS RESULT
DESIGN SPECS/VARYDESIGN SPECS/VARY
ADD NEW DESIGN SPECSADD NEW DESIGN SPECS
DESIGN SPECS: SPECIFICATIONDESIGN SPECS: SPECIFICATION
DESIGN SPECS: COMPONENTSDESIGN SPECS: COMPONENTS
DESIGN SPECS: FEED/PRODUCT STREAMSDESIGN SPECS: FEED/PRODUCT STREAMS
ADD NEW VERYADD NEW VERY
VERY: SPECIFICATIONSVERY: SPECIFICATIONS
RUN SIMULATIONRUN SIMULATION
Click ► to run simulation
CHECK CONVERGENCE STATUSCHECK CONVERGENCE STATUS
DESIGN SPECS/VARYDESIGN SPECS/VARY
ADD NEW DESIGN SPECSADD NEW DESIGN SPECS
DESIGN SPECS: SPECIFICATIONDESIGN SPECS: SPECIFICATION
DESIGN SPECS: COMPONENTSDESIGN SPECS: COMPONENTS
DESIGN SPECS: FEED/PRODUCT STREAMSDESIGN SPECS: FEED/PRODUCT STREAMS
ADD NEW VERYADD NEW VERY
VERY: SPECIFICATIONSVERY: SPECIFICATIONS
RUN SIMULATIONRUN SIMULATION
Click ► to run simulation
CHECK CONVERGENCE STATUSCHECK CONVERGENCE STATUS
D2D1
CHECK STREAMS RESULTCHECK STREAMS RESULT
RECYCLE STREAM
RECYCLE STREAM
RECYCLE STREAM
TEAR
CHECK STREAMS RESULT
SUMMARY OF REBOILERSUMMARY OF REBOILER
Include reboiler duty, bottoms rate, boilup rate, boilup ratio
B1 B2
TRAY SIZINGTRAY SIZING
237
TRAY SIZINGTRAY SIZING
238
Click ► to run simulation
TRAY SIZINGTRAY SIZING
239
240
TRAY RATINGTRAY RATING
241
TRAY RATINGTRAY RATING
UPDATE PRESSURE DROP OF STAGESUPDATE PRESSURE DROP OF STAGES
242
Click ► to run simulation
CHECKS PRESSURE DROP RESULTCHECKS PRESSURE DROP RESULT
