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Introduction to Aspen Plus
Speaker: Bor-Yih Yu(余柏毅)
Date: 2014/09/18
f00524023@ntu.edu.tw
PSE Laboratory
Department of Chemical EngineeringNation Taiwan University
(綜合
room 402)
Edited by:程建凱
/吳義章
/余柏毅
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2
Introduction to Aspen Plus
Part 1: Introduction
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What 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.
4Ref: http://www.aspentech.com/products/aspen-plus.cfm
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What 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 Brochure 5
http://www.aspentech.com/brochures/Aspen_Plus.pdfhttp://www.aspentech.com/brochures/Aspen_Plus.pdfhttp://www.aspentech.com/brochures/Aspen_Plus.pdf
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More 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 6
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What course Aspen Plus
can be employed for• MASS AND ENERGY BALANCES
• PHYSICAL CHEMISTRY
• CHEMICAL ENGINEERING THERMODYNAMICS
• CHEMICAL REACTION ENGINEERING
• UNIT OPERATIONS
• PROCESS DESIGN
• PROCESS CONTROL
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Lesson Objectives
• Familiar with the interface of Aspen Plus
• Learn how to use properties analysis
• Learn how to setup a basic process simulation
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Outline
• Part 1 : Introduction• Part 2 : Startup
• Part 3 : Properties analysis
• Part 4 : Running Simulation in Aspen Plus (simple units)
• Part 5 : Running Simulation in Aspen Plus (Reactors)• Part 6 : Running Simulation in Aspen Plus (Distillation)
• Part 7 (additional): Running Simulation in Aspen Plus (Design,
spec and vary)
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Introduction to Aspen Plus
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Part 2: Startup
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Start with Aspen Plus
Aspen Plus User Interface
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Aspen Plus Startup
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Interface of Aspen Plus
Process Flowsheet Windows
Model Library (View| Model Library )
Stream
Help
SetupComponents
Properties
Streams
Blocks
Data Browser
Next
Check Result
StopReinitialize
Step
Start
Control Panel
Process Flowsheet Windows
Model Library (View| Model Library )
Status message13
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More Information
Help for Commands for Controlling Simulations 14
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Data 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
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Setup – Specification
Run Type
Input mode
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Input components
Remark: If available, are
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Properties
Process type(narrow the number of
methods available)
Base method: IDEAL, NRTL, UNIQAC, UNIFAC…
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Property Method Selection—General Rule
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Example 1:
water - benzene
Example 2:
benzene - toluene
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Typical Activity Coefficient Models
Non-Randon-Two Liquid Model (NRTL)
Uniquac Model
Unifac Model
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Typical Equation of States
Peng-Robinson (PR) EOS
Redlich-Kwong (RK) EOS
Haydon O’Conell (HOC) EOS
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Thermodynamic Model – NRTL
NRTL
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NRTL – Binary Parameters
Click “NRTL” and then built-in binary parameters
appear automatically if available.
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Access Properties Models and
Parameters
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Review Databank Data
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Review 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 K
Heat of vaporization at TB
Normal boiling point
Standard liquid volume at 60°F….
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Pure Component
Temperature-Dependent Properties
CPIGDP-1 ideal gas heat capacity
CPSDIP-1 Solid heat capacityDNLDIP-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
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Example: PLXANT-1
(Extended Antoine Equation)
?
Corresponding Model
Click “ ?” and then click where you don’t know
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Example: CPIGDP-1
(Ideal Gas Heat Capacity Equation)
?
Corresponding Model
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Basic Input---Summary
• The minimum required inputs to run a simulation
are:
– Setup
– Components – Properties
– Streams
– Blocks
Property Analysis
Process Simulation
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Introduction to Aspen Plus
Part 3: Property analysis
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Overview of Property AnalysisUse 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 ternarysystems
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
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***When you start properties analysis, you MUST specify components ,
thermodynamic model and its corresponding parameters. (Refer to Part 2)
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Find Components
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Component ID : just for distinguishing in Aspen.Type : Conventional, Solid….etc
Component name : real component name
Formula : real component formula
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Find Components
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TIP 1: For common components, you can
enter directly the common name or molecular
equation of the components in “component
ID”.
(like water, CO2, CO, Chlorine…etc)
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Find Components
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TIP 2: If you know the component name
(like N-butanol, Ethanol….etc), you can
enter it in “component name”.
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Select Thermodynamic Model
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Select NRTL
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Check Binary Parameter
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Click This, it will automatically change to
red if binary parameter exists.
Properties
Parameters
NRTL-1
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Find Components
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TIP 2: If you know the component name
(like N-butanol, Ethanol….etc), you can
enter it in “component name”.
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Find Components
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You can enter
the way of
searching…
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Properties Analysis – Pure Component
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Available Properties
Property (thermodynamic) Property (transport)
Availability Free energy Thermal conductivity
Constant pressure
heat capacityEnthalpy Surface tension
Heat capacity ratio Fugacity coefficient Viscosity
Constant volume heat
capacity
Fugacity coefficient
pressure correction
Free energy departure Vapor pressure
Free energy departure
pressure correctionDensity
Enthalpy departure Entropy
Enthalpy departure
pressure correctionVolume
Enthalpy of
vaporizationSonic velocity
Entropy departure 41
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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”
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Example1: Calculation Results of CP
Data results 43
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Properties Analysis – Binary Components
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Binary Component Properties Analysis
Use this Analysis type To generate
TxyTemperature-compositions diagram at
constant pressure
Pxy Pressure-compositions diagram atconstant 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 phasesat a given temperature and pressure.
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Example: T-XY
1. 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
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Example: calculation result of T-XY
Data results
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Example: Generate XY plot
Click “plot wizard” to generate XY plot
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Example: Generate XY plot (cont’d)
Properties Analysis – Ternary
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Properties Analysis Ternary
(add one new components)
Properties Analysis – Ternary
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Properties Analysis Ternary
(Check NRTL binary parameter)
3 components -> 3 set of binary parameter
(How about 4 components??)
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Properties Analysis – Ternary
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Ternary 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)
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Calculation Result of Ternary Map (LLE)
Data results
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Property Analysis – Conceptual Design
Use this form To generate
PureTables 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
TernaryTernary maps showing phase envelope, tie lines, and azeotropes of ternary
systems
AzeotropeThis 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
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(Optional)
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Conceptual Design
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Azeotrope Analysis
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Azeotrope 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
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Error Message
Close analysis input dialog box (pure or binary analysis)
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Azeotrope Analysis Report
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Ternary Maps
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Ternary 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
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Ternary Maps
Ternary Plot Toolbar:
Add Tie line, Curve,
Marker…
Change pressure or
temperature
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Introduction to Aspen Plus
Part 4: Running simulation
Simple Units
(Mixer, Pump, valve, flash, heat exchanger)
Example 1: Calculate the mixing
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Example 1: Calculate the mixing
properties of two stream
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4
Mixer Pump
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 ? ? ? ?65
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Setup – Specification
Select Flowsheet
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Reveal Model Library
View|| Model Libraryor press F10
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Adding a Mixer
Click “one of icons”and then click again on the flowsheet window
Remark: The shape of the icons are meaningless
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Adding Material Streams
Click “Materials” and then click
again on the flowsheet window
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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)
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Adding Material Streams (cont’d)
After selecting “Material Streams”, click and pull a stream line. Repeat it three times to generate three stream lines.
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Reconnecting Material Streams
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Reconnecting Material Streams
(Feed Stream)
Right Click on the stream and
select Reconnect Destination
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Reconnecting Material Streams
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Reconnecting Material Streams
(Product Stream)
Right Click on the stream and
select Reconnect Source
B1
1
2
3
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Specifying Feed Condition (cont’d)
1 2
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Specifying Input of Mixer
Right Click on the block and select Input
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Specifying Input of Mixer (cont’d)
Specify Pressure and valid phase
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l
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Run Simulation
Click to run the simulation
Check “simulation status”
“Required Input Complete” means the input is ready to run simualtion
Run Start or continue calculationsStep Step through the flowsheet one block at a time
Stop Pause simulation calculations
Reinitialize Purge simulation results
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S l
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Stream Results
Right Click on the block and
select Stream Resu lts
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1 2 3
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1 2 3
Substream: MIXED
Mole Flow kmol/hr
WATER 10 0 10
BUOH 0 9 9 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
Vapor Frac 0 0 0
Liquid Frac 1 1 1
Solid Frac 0 0 0
Enthalpy kcal/mol -67.81 -94.3726 -83.7476
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 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
Average 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.
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Enthalpy and Entropy
Ch U i f C l l i R l
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Change Units of Calculation Results
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S D fi i Y O U i S
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Setup – Defining Your Own Units Set
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S t R t O ti
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Setup – Report Options
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Stream Results with Format of
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Mole Fraction
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Add P Bl k
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Add Pump Block
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Add A M t i l St
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Add A Material Stream
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P S ifi ti
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Pump – Specification
2. Specify pump outlet specificati(pressure, power)
1. Select “Pump” or “turbine”
3. Efficiencies (Default: 1)
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R Si l ti
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Run Simulation
Click to generate the results
Check “simulation status”
“Required Input Complete”
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Block Results (Pump)
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Block Results (Pump)
Right Click on the block and select Results
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Calculation Results
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(Mass and Energy Balances)
1
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4
Mixer Pump
1 2 3 4
Mole 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 71.20
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 969.50 783.85 825.56 824.29
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Example 2: Flash Separation
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Example 2: Flash Separation
Saturated Feed
P=1atm
F=100 kmol/hr
zwater =0.5zHAc=0.5
T=105 C
P=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 Components
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Input Components
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Association parameters of HOC
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Association parameters of HOC
Binary Parameters of NRTL
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Binary Parameters of NRTL
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T-xy plot
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T-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
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Generate xy plot
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Generate xy plot
Generate xy plot (cont’d)
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Add Block: Flash2
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Add Block: Flash2
Add Material Stream
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Add Material Stream
Specify Feed Condition
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Specify Feed Condition
Saturated Feed
(Vapor fraction=0)
P=1atm
F=100 kmol/hr
zwater =0.5
zHAc
=0.5
Block Input: Flash2
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Block Input: Flash2
Flash2: Specification
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Flash2: Specification
T=105 C
P=1atm
Required Input Complete
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Required Input Complete
Click to run simulation
**Before running simulation, property
analysis should be closed.
Stream Results
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Stream Results
Stream Results (cont’d)
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Stream Results (cont d)
Saturated Feed
P=1atm
F=100 kmol/hr
zwater =0.5
zHAc=0.5
T=105 C
P=1atm
42.658 kmol/hr
zwater =0.501
zHAc=0.409
57.342 kmol/hr
zwater =0.432
zHAc=0.568
HEAT EXCHANGE
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HEAT EXCHANGE
熱物流
入口温度:200 入口壓力:0.4 MPa
流量:10000kg/hr
组成:苯 50%,苯乙烯 20%,水 10%
冷卻水
入口温度:20 入口压力:1.0 MPa
流量:60000 kg/hr
熱流出口氣相分率為
0(飽和液相)
COMPONENTS – SPECIFICATION
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Thermodynamic Model – NRTL
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ADD BLOCK: HEATX
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Feeds Conditions
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Feeds Conditions
HOT-INCLD-IN
BLOCK INPUT
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Check result
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Check result
Check result
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Introduction to Aspen Plus
Part 5: Running simulation
Reactor Systems
(RGIBBS, RPLUG,RCSTR)
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Equilibrium Reactor: RGIBBS
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q
222
2422
242
24
3
H COO H CO
O H CH H CO
O H CH H CO
Reactions:
Fresh Feed
Flow rate 1000 (kmol/h)CO 0.2368
H2 0.7172
H2O 0.0001
CH4 0.0098
CO2 0.0361
T=300 k
P=470 psia
Equilibrium Reactor: RGIBBS
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127
q
Equilibrium Reactor: RGIBBS
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q
Inside the Block:
Check result
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KINETICS REACTORS: RPLUG
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KINETICS REACTORS: RPLUG
Reaction :Exothermic & reversible
222 H COO H CO )/(09.41 mol KJ H
)
85458
exp(1.3922
)47400
exp(545.51
)(222
RT k
RT k
skgcat
kmol Y Y k Y Y k Rate
r
f
H COr O H CO f
Rate [=] Kmol/Kgcat/s
Activation Energy [=] KJ/Kmol
KINETICS REACTORS: RPLUG
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KINETICS REACTORS: RPLUG
Reaction :Exothermic & reversible
222 H COO H CO )/(09.41 mol KJ H
Catalyst Loading = 0.1865 Kg
Bed Voidage = 0.8928
Feed Temperature = 583K
Feed Pressure = 1 bar
Reactor Length = 10 m
Reactor Diameter = 5m
Fresh Feed
Flow rate 200 (mol/h)
CO 0.030
H2 0.430
H2O 0.392CO2 0.148
KINETICS REACTORS: RPLUG
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KINETICS REACTORS: RPLUG
Feed Stream:
KINETICS REACTORS: RPLUG
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KINETICS REACTORS: RPLUG
Reaction Setting:
KINETICS REACTORS: RPLUG
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KINETICS REACTORS: RPLUG
Reaction Setting:
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KINETICS REACTORS: RPLUG
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KINETICS REACTORS: RPLUG
RPLUG Setting:
KINETICS REACTORS: RPLUG
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KINETICS REACTORS: RPLUG
RPLUG Setting:
Check result
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138
Check result
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139
Check result
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140
Select Reactor Length column
Plot -> x-Axis variable
Select Temperature Column
Plot -> y-Axis variable
Display Plot
Check result
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141
Block B2 (RPlug) Profiles Process Stream
Reactor length MIXED meter
T E M P E R A T U R
E K
0.0 0.5 1.0 1.5 2.0 2.5 3.0 3.5 4.0 4.5 5.0 5.5 6.0 6.5 7.0 7.5 8.0 8.5 9.0 9.5 10.0
5 8 5 . 0
5 8 7 . 5
5 9 0 . 0
5 9 2 . 5
5 9 5 . 0 5
9 7 . 5
6 0 0 . 0
6 0 2 . 5
6 0 5 . 0
6 0 7 . 5
Temperature MIXED
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Check result
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143
Select Reactor Length column
Plot -> x-Axis variable
Select all other columns
Plot -> y-Axis variable
Display Plot
Check result
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Block B2 (RPlug) Profiles Process Stream
Reactor length MIXED meter
0.0 0.5 1.0 1.5 2.0 2.5 3.0 3.5 4.0 4.5 5.0 5.5 6.0 6.5 7.0 7.5 8.0 8.5 9.0 9.5 10.0
0 . 0 5
0 . 1
0 . 1 5
0 . 2
0 . 2 5
0 . 3
0 . 3 5
0 . 4
0 . 4
5
0 . 5
Mole fraction MIXED CO
Mole fraction MIXED H2OMole fraction MIXED CO2
Mole fraction MIXED H2
KINETICS REACTORS: RCSTR
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Reaction :Exothermic & Irreversible
Aniline + Hydrogen Cyclohexylamine (CHA)
C6H7N + 3H2 C6H13N
Reactor Conditions
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Reactor :
Reactor
condition
Reactor type
Reactor liquid level
595 psi
250 F
1200 ft3
Temperature
Volume
Vertical cylindrical vessel
80%
Pressure
Reactor Conditions Input
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Reaction Kinetics
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CHA R A H R kV C C
8
0 10k
0 exp( ) E k k RT
3lbmole ft
Reaction rate :
Where
VR: reactor volume
C A: concentration of AnilineCH: concentration of Hydrogen
• Reaction kinetics :
Where
E : activity energy
T : temperature (R)2000 Btu E
lbmole
3lbmole
ft
3 ft
Reaction Kinetics Input
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Reaction Kinetics Input
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Reaction Kinetics Input
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Feeds Conditions
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1
100 lbmolhr
1400 lbmolhr
Two fresh feed stream :
Aniline feed Hydrogen feed
mole rate
temperature
pressure
100 F 100 F
650 psia 650 psia
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Check result
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154
(1) Compare the conversion between RSTOIC and RCSTR.
(2) Compare the net duty inside the RSTOIC and RCSTRQuestion:
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155
Introduction to Aspen Plus
Part 6: Running simulation
Distillation Process
(DSTWU, RADFRAC)
Distillation Separation
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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
• There are two degrees offreedom to manipulate
distillate composition and
bottoms composition to
manipulate the distillate andbottoms 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 ?
Distillation SeparationExample :
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Example :
A mixture of benzene and toluene containing 40 mol% benzeneis to be separated to dive a product containing 90 mol%
benzene at the top, and no more than 10% benzene in bottom
product. The feed enters the column as saturated liquid, and
the vapor leaving the column which is condensed but not
cooled, provide reflux and product. It is proposed to operate
the unit with a reflux ratio of 3 kmol/kmol product. Please
find:
(1) The number of theoretical plates.
(2) The position of the entry.
(Problem is taken from Coulson & Richardson’s Chemical
Engineering, vol 2, Ex 11.7, p.564)
1. By what you learned in Material balance and
unit operation
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1
Saturated Feed
P=100 Kpa
F=100 kmol/hr
xben=0.4
xtol=0.6
xben=0.9
xben
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From thermodynamic phase equilibrium, and the calculation of operating line:
We can get the number of theoretical plate to be 7.
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2. By the shortcut method in Aspen Plus (DISTWU)(Select property method)
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Select NRTL
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2. By the shortcut method in Aspen Plus (DSTWU)
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Add the unit “DSTWU”
The red arrows are the required material stream!
2. By the shortcut method in Aspen Plus (DSTWU)
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Connect the required material stream
2. By the shortcut method in Aspen Plus (DSTWU)
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“Feed1” Stream specification
2. By the shortcut method in Aspen Plus(Column Specification)
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From the problem Assume no pressure drop
Inside the column
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2. By the shortcut method in Aspen Plus(Column Specification)
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Get results by varying the
number of stages. (Initial
Guess)
2. By the shortcut method in Aspen Plus (DSTWU)
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RUN THE SIMULATION
2. By the shortcut method in Aspen Plus(Stream Results)
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Click right button on the unit, and select “Stream
Results”
2. By the shortcut method in Aspen Plus(Stream Results)
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The required product
quality
2. By the shortcut method in Aspen Plus(RR vs number of stage)
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For RR=3, at least 7
theoretical stages are
required.
3. More rigorous method in Aspen Plus (RADFRAC)
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Add the unit “RADFRAC”
The red arrows are the required material stream!
3. More rigorous method in Aspen Plus (RADFRAC)
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Connect the required material stream
3. More rigorous method in Aspen Plus (RADFRAC)(Feed Specification)
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Same as Case 2
3. More rigorous method in Aspen Plus (RADFRAC)(Column Specification)
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Double click left button on the unit….
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3. More rigorous method in Aspen Plus (RADFRAC)(Column Specification)
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Specify the feed stage.
3. More rigorous method in Aspen Plus (RADFRAC)(Column Specification)
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Specify the pressure at the top of column
3. More rigorous method in Aspen Plus (RADFRAC)(Calculation of tray size—Tray Sizing)
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3. More rigorous method in Aspen Plus (RADFRAC)(Pressure drop calculation – Tray Rating)
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3. More rigorous method in Aspen Plus (RADFRAC)(Pressure drop calculation – Tray Rating)
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*Calculation from 2th tray from the top to
2th tray from the bottom. (WHY??)
*Initial guess of the tray size
3. More rigorous method in Aspen Plus (RADFRAC)(Pressure drop calculation – Tray Rating)
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3. More rigorous method in Aspen Plus (RADFRAC)(Stream Results)
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Click right button on the unit, and select “Stream
Results”
3. More rigorous method in Aspen Plus (RADFRAC)(Stream Results)
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Different from the shorcut method.
(WHY??)
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188
Introduction to Aspen Plus
Part 7: Running simulation(Additional)
Design, spec, and vary in RADFRAC
3. More rigorous method in Aspen Plus (RADFRAC)(Design , Spec and Vary)
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What do we want??
--- 90% Benzene at top.
Select “Mole Purity”…
And the target is 0.9.
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3. More rigorous method in Aspen Plus (RADFRAC)(Design , Spec and Vary)
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Add a Vary
(1 Design Spec 1 Vary)
3. More rigorous method in Aspen Plus (RADFRAC)(Design , Spec and Vary)
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Varying Reflux ratio to
reach the design target.
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3. More rigorous method in Aspen Plus (RADFRAC)(Design , Spec and Vary)
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2nd Design Spec
3. More rigorous method in Aspen Plus (RADFRAC)(Design , Spec and Vary)
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What do we want??
--- 10% Benzene at bot.
Select “Mole Purity”…
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3. More rigorous method in Aspen Plus (RADFRAC)(Design , Spec and Vary)
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Select the Benzene
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Select the bottom stream
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2nd Vary
3. More rigorous method in Aspen Plus (RADFRAC)(Design , Spec and Vary)
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Varying distillate rate to
reach the design target.
Specify the varying range.
(Should contain the initial value)
3. More rigorous method in Aspen Plus (RADFRAC)(Design , Spec and Vary)
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RUN THE SIMULATION,
and click right button on
the unit, select “Stream
results”
3. More rigorous method in Aspen Plus (RADFRAC)(Stream Results)
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The required product
quality
3. More rigorous method in Aspen Plus (RADFRAC)(Column Results--top)
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Calculated Reflux Ratio = 6.14
(from problem: 3)
3. More rigorous method in Aspen Plus (RADFRAC)(Column Results--bottom)
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The required heat duty for
separation is 2341.8 (KW)
3. More rigorous method in Aspen Plus (RADFRAC)(Profile Inside the Column)
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T : Temperature
P : Pressure
F : Liquid and vapor flow rate.
Q: Heat Duty
3. More rigorous method in Aspen Plus (RADFRAC)(Profile Inside the Column)
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You can select the vapor or
liquid composition profile.
(also in mole or mass basis)
3. More rigorous method in Aspen Plus (RADFRAC)(Plotting Temp. Profile)
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Select the column “Stage”
Click “Plot”
Select “X-axis variable”
3. More rigorous method in Aspen Plus (RADFRAC)(Plotting Temp. Profile)
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Select the column “Temp.”
Click “Plot”
Select “ Y-axis variable”
3. More rigorous method in Aspen Plus (RADFRAC)(Plotting Temp. Profile)
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Then, select “Display
Plot”
3. More rigorous method in Aspen Plus (RADFRAC)(Plotting Temp. Profile)
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ExerciseExample:
Typically 90 mol% product purity is not enough for a product to
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Typically, 90 mol% product purity is not enough for a product to
sale. In the same problem, assume the number of stages
increase to 10. Try the following exercises:
(1) Is it possible to separate the feed to 95 mol% of benzene in
the distillate, and less than 5% of benzene in the bottom
product? If yes, what is the RR and Qreb?
(2) As in (1), is it possible to separate the feed to 99 mol% of
benzene in the distillate, and less than 1% of benzene in the
bottom product? If yes, what is the RR and Qreb?
(3) As in (2), if no, how many number of stages is required to
reach this target?
(Hint: Use design, spec, and vary to do this problem)
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Thanks for your attention!
PSE LaboratoryDepartment of Chemical Engineering
Nation Taiwan University(綜合 room 402)