Introduction to Aspen Plus

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Introduction to Aspen Plus
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1 Introduction to
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Aspen Plus
Speaker: Bor-Yih Yu(余柏毅)
Date: 2016/09/05 We think you have liked this presentation. If you wish to
PSE Laboratory download it, please recommend it to your friends in any social
Department of Chemical
system.Engineering
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National Taiwan University
(化工館RM307, ) Buttons:
2
Outline Part 1 : Introduction Part 2 : Startup
Part 3 : Properties analysis
3-1: Basic Property analysis
3-4: Validation of thermodynamic parameters
Part 4 : Running Simulation in Aspen Plus
(simple units: Mixer, Pump, valve, flash, heat exchanger )
7
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3
Outline Part 5 : Running Simulation in Aspen Plus
(Reactors)
5-1: Basic operation of Reactor System
5-2: Analysis of reacting system
Part 6 : Running Simulation in Aspen Plus (separation)
6-1: Basic Operation of separation System
6-2: Design, spec, and vary in RADFRAC
Part 7 : Running Simulation in Aspen Plus
More Complex system with recycle
4
Introduction to Aspen Plus
Part 1: Introduction
5
Ref: http://www.aspentech.com/products/aspen-plus.cfm
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.
Ref:
6
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
updated
with
data
from
U.it with
S. processors.
National ToInstitute
of you must agree to our Privacy Policy, including
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make this website
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share
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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
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controllability studies,
sizing relief
valves, and optimizing transition,
startup, and shutdown policies
Enables you build your own libraries using Aspen Custom Modeler or
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programming languages
(User-defined
models)
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Ref: Aspen Plus® Product
Brochure
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Buttons:
More
Detailed
Properties analysis Process simulation
7
Properties of pure component and mixtures (Enthalpy, density,
viscosity, heat capacity,…etc)
7
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
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Process simulation
pump, compressor, valve, tank, heat exchanger, CSTR, PFR,
distillation column, extraction column, absorber, filter, crystallizer…
etc
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8
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
9
Lesson Objectives Familiar with the interface of Aspen Plus
Learn how to use properties analysis
Learn how to setup a basic process simulation
10
Introduction to Aspen Plus
Part 2: Startup and Overview
11
Aspen Plus User Interface
Start with Aspen Plus
Aspen Plus User Interface
12
Aspen Plus Startup
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13
Help
14
More Information
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Help for
Commands for Controlling Simulations
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Properties system.
-- Setup Share buttons are a little bit lower. Thank you!
PropertiesButtons:
-- Input components
Remark: If available, are
16
7
Properties -- Methods Process type(narrow the number of
methods available)
Base method: IDEAL, NRTL, UNIQAC, UNIFAC…
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17
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18
Property Method Selection—General Rule
Example 1:
water - benzene
Example 2:
benzene - toluene
19
Typical Activity Coefficient Models
Non-Randon-Two Liquid Model (NRTL)
Uniquac Model
Unifac Model
20
Typical Equation of States
Peng-Robinson (PR) EOS
Redlich-Kwong (RK) EOS
Haydon O’Conell (HOC) EOS
21
Thermodynamic Model – NRTL
22
NRTL – Binary Parameters
Click “NRTL” and then built-in binary parameters appear
automatically if available.
23
Access Properties Models and Parameters
Review Databank Data
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24
Ideal gas heat of formation at K
Ideal gas Gibbs free energy of formation at K
Heat of vaporization at TB
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Normal boiling point
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Standard liquid volume at 60°F
….
Parameter variable
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25 Pure Component Temperature-Dependent Properties
CPIGDP-1
Buttons:
ideal gas heat capacity
CPSDIP-1
Solid heat capacity
7
DNLDIP-1
Liquid density
DHVLDP-1
Heat of vaporization
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PLXANT-1
Extended Antoine Equation
MULDIP
Liquid viscosity
KLDIP
Liquid thermal conductivity
SIGDIP
Liquid surface tension
UFGRP
UNIFAC functional group
UFGRP
26
Properties – Tools
27
Properties – Data Source
28
Properties – Run Mode
29
Properties – Analysis
30
Simulation Help Process Flowsheet Windows Data
Browser
Model Palette (View│Model Palette)
31
Simulation -- Setup – Specification
Input mode
32
Basic Input---Summary
The minimum required inputs to run a simulation are:
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Setup
Components
Methods
Simulation
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Streams
Blocks
Property Analysis
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Introduction
to Aspen Plus
Buttons:
Part 3: Property analysis
3-1: Basic Property analysis
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34
Overview of Property Analysis
Use this form
To generate
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Pure
Tables and plots of pure component properties as a function of
temperature and pressure
Binary
Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue
Residue curve maps
Ternary
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 Maps
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes,
Distillation boundary, Residue curves or distillation curves,
Isovolatility curves, Tie lines, Vapor curve, Boiling point
***When you start properties analysis, you MUST specify
components , thermodynamic model and its corresponding
parameters. (Refer to Part 2)
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35
Find Components (1/5) Component ID : just for
distinguishing in Aspen.
Type : Conventional, Solid….etc
Component name : real component name
Formula : real component formula
36
Find Components (2/5)
TIP 1: For common components, you can enter directly the common
name or molecular equation of the components in “component ID”.
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CO,weChlorine…etc)
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Find Components (3/5)
TIP 2: If you know
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component name (like N-butanol,
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Ethanol….etc), you can enter it in “component name”.
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Find
Components
(4/5)
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TIP 3: You can alsosystem.
enter the
formula
of the
(Be aware
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the isomers)
You can also clickButtons:
“Find” to search for component of given CAS
number, molecular weight without knowing its molecular formula, or
if you don’t know the exactly component name
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39
Find Components (5/5)
You can enter the way of searching…
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40
Methods (1/2) – Select Thermodynamic Model
Select NRTL
41
Methods (2/2) – Check Binary Parameter
Properties
Methods
Parameters
NRTL-1
Click This, it will automatically change to blue if binary parameter
exists.
42
43
Properties Analysis – Pure Component (1/5)
Available Properties (2/5)
Property (thermodynamic)
Property (transport)
Availability
Free energy
Thermal conductivity
Constant pressure heat capacity
Enthalpy
Surface tension
Heat capacity ratio
Fugacity coefficient
Viscosity
Constant volume heat capacity
Fugacity coefficient pressure correction
Free energy departure
pressure
ToVapor
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Density
Enthalpy departure
Entropy
Enthalpy departure pressure correction
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Volume
Enthalpy of vaporization
Sonic velocity
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44
Example1:Buttons:
CP (Heat Capacity) (3/5)
1. Select property (CP)
4. Specify range of temperature
2. Select phase
5. Specify pressure
Add “N-butyl-acetate”
6. Select property method
3. Select component
7. click “Run Analysis” to generate the results
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45
Example1: Calculation Results of CP (4/5)
Click This, able to change units and the ability to merge different plots
Click This, able to change format of the plot, including font, axis
range…etc.
46
Example1: Calculation Results of CP (5/5)
Data results
47
Properties Analysis – Binary Components (1/7)
48
Binary Component Properties Analysis (2/7)
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.
49
Example: T-XY (3/7) 5. Select phase (VLE, VLLE) Select
analysis type (Txy)
2. Select
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6. Specify pressure
3. Select
compositions basis
7. Select property method
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4. Specify
composition range
8. click “Run Analysis” to generate the results
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50 Example: calculation result of T-XY (4/7)
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Example:
calculation
result of T-XY (5/7)
51
Data results
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52
Example: Generate XY plot (6/7)
Click “Input”
Cancel
53
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Example: Generate XY plot (7/7)
54
Properties Analysis – Ternary (1/6) (add one new
components)
55
Properties Analysis – Ternary (2/6) (Check NRTL binary
parameter)
3 components -> 3 set of binary parameter
(How about 4 components??)
56
Properties Analysis – Ternary (3/6) (Ternary Maps)
57
Properties Analysis – Ternary (4/6) (Ternary Maps)
58
Properties Analysis – Ternary (5/6) Calculation Result of
Select
three component
2. Select
property method
5. Specify pressure
3. Select
phase (VLE, LLE…)
4. Specify
number of tie line
6. Specify temperature
(if LLE is slected)
7. click “Run Analysis” to generate the results
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Ternary Map (LLE)
59
Properties Analysis – Ternary (6/6)
Calculation Result of
Ternary Map
(LLE)
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Data results
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Property
Analysis
– Conceptual
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Use this form
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To generate
Buttons:
Pure
Tables and plots of pure component properties as a function of
temperature and pressure
Binary
7
Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue
Residue curve maps
Ternary
Cancel
Download
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 Maps
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes,
Distillation boundary, Residue curves or distillation curves,
Isovolatility curves, Tie lines, Vapor curve, Boiling point
61
Conceptual Design -- Azeotrope Analysis (1/3)
62
Conceptual Design -- Azeotrope Analysis (2/3)
1. Select components (at least two)
2. Specify pressure
6. click “Report” to generate the results
3. Select property method
4. Select phase (VLE, LLE…)
5. Select report Unit
63
Conceptual Design -- Azeotrope Analysis (3/3)
(Azeotrope Analysis Report)
64
Distillation Synthesis Ternary Maps (1/3)
Conceptual Design –
Distillation Synthesis Ternary Maps (1/3)
65
Distillation Synthesis Ternary Maps (2/3)
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Distillation Synthesis Ternary Maps (2/3)
3. Select property method
1. Select three components
4. Select phase (VLE, LLE)
5. Select report UnitDownload presentation
6. Click “Ternary Plot”
to generate the results
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(If liquid-liquid envelope
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66
Distillation Synthesis Ternary Maps (3/3)
Conceptual Design –
Distillation Synthesis Ternary Maps (3/3)
Change pressure or temperature
Ternary Plot Toolbar:
Add Tie line, Curve, Marker…
7
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67
Introduction to Aspen Plus
Part 3: Property analysis
3-2:
Validation of thermodynamic parameters
68
Finding Experimental Data in Aspen Plus
Build in the components
69
Finding Experimental Data in Aspen Plus
Open the access to data bank.
70
Finding Experimental Data in Aspen Plus
71
Finding Experimental Data in Aspen Plus
Various kinds of data.
(Choose VLE data here)
Different set of VLE data (with different temperature or different
pressure)
72
Finding Experimental Data in Aspen Plus
One of the data set.
Save into Aspen Plus.
73
Save to Data
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Save to Data
75
Comparing the VLE with Built-in Parameter
77
Comparing the VLE with Built-in Parameter
78
Comparing the VLE with Built-in Parameter
79
Comparing the VLE with Built-in Parameter
80
Comparing the VLE with Built-in Parameter
81
Comparing the VLE with Built-in Parameter
<Goal>
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Compare the experimental VLE data and the predicted VLE data by
NRTL model.
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Comparing
the VLEShare
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Built-inare
Parameter
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Do not close this plot in the following steps.
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82
Comparing the VLE with Built-in Parameter
2.Click “Single Y Axis”. (Combine the axis into one.)
Right click, and choose “Y Axis Map”
83
Comparing the VLE with Built-in Parameter
The predicted VLE by NRTL is pretty good.
84
Introduction to Aspen Plus
Part 4: Running simulation
Simple Units (Mixer, Pump, valve, flash, heat exchanger)
85
Example 1: Calculate the mixing properties of two stream
234
Mole Flow kmol/hr
WATER
10 ?
BUOH
9
BUAC
6
Total Flow kmol/hr
15
Temperature C
50 80
ToPressure
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Enthalpy kcal/mol
Entropy cal/mol-K
Density kg/cum
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Simulation -- Setup – Specification
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87
Reveal Model
Library
Buttons:
View→ Model Library
or press F10
7
88
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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89
Adding Material Streams
Click “Materials” and then click again on the flowsheet window
90
Adding Material Streams (cont’d)
When clicking the mouse on the flowsheet window,
arrows (blue and red) appear.
91
Adding Material Streams (cont’d)
When moving the mouse on the arrows, some description appears.
Red arrow(Left) Feed (Required; one ore more if mixing material
streams)
Red arrow(Right): Product (Required; if mixing material streams)
Blue arrow: Water decant for Free water of dirty water.
92
Adding Material Streams (cont’d)
After selecting “Material Streams”, click and pull a stream line.
Repeat it three times to generate three stream lines.
93
Reconnecting Material Streams (Feed Stream)
Right click on the stream and select “Reconnect Destination”
94
Reconnecting Material Streams (Product Stream)
Right click on the stream and select “Reconnect Source”
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Change Material Streams Names
Double click to rename
the stream
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SpecifyingWe
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97
SpecifyingButtons:
Feed Condition (cont’d)
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98
Specifying Input of Mixer
Right click on the block and select “Input”
99
Specifying Input of Mixer (cont’d)
Specify Pressure and valid phase
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100
Run Simulation Click ► to run the simulation Run
Start or continue calculations
Step
Step through the flowsheet one block at a time
Stop
Pause simulation calculations
Reinitialize
Purge simulation results
Check “simulation status”
“Required Input Complete” means the input is ready to run
simualtion
101
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
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current input.
102
Stream Results
Right click on the block
and select
“Stream Results”
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Buttons:
104
Change Units of Calculation Results
105
Setup – Report Options
106
Stream Results with Format of Mole Fraction
107
Add Pump Block
108
Add A Material Stream
109
Connect Streams
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110
Pump – Specification 1. Select “Pump” or “turbine”
2. Specify pump outlet specification
(pressure, power)
3. Efficiencies (Default: 1)
111
Run Simulation Click “Next” to check if all required
input is complete
Click “OK” to run the simulation
112
Block Results (Pump)
Right click on the block and select “Results”
114
Streams Results
115
Calculation Results (Mass and Energy Balances)
1234
Mole Flow kmol/hr
WATER
10
BUOH
9
BUAC
6
ToTotal
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Flow
kmol/hr
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15 25
Temperature C
50 80
71.22
72.33
Pressure bar
Enthalpy kcal/mol
-67.81
-94.34
-83.73
-83.67
Entropy cal/mol-K
-37.53
-95.61
-95.45
Density kg/cum
969.50
783.85
824.28
823.01
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116
Exercise 1 2 3 4 5 6 Mole Flow kmol/hr Water 10 ?
Ethanol Methanol 15
?
Ethanol
Methanol
15
Total Flow kmol/hr
Temperature C
50 70 40
Pressure bar
Enthalpy kcal/mol
Entropy cal/mol-K
Density kmol/cum
Please use Peng-Robinson EOS to solve this problem.
117
Example 2: Flash Separation
118
Input Components
T=105 C
P=1atm
Saturated Feed
P=1atm
F=100 kmol/hr
zwater=0.5
zHAc=0.5
What are flowrates and compositions of the two outlets?
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119
Thermodynamic Model: NRTL-HOC
120
Check Binary Parameters
121
Association parameters of HOC
122
Binary Parameters
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T-xy plotButtons:
5. Select phase (VLE, VLLE) 1. Select analysis
type (Txy)
6. Specify pressure
2. Select two component
7
3. Select compositions basis
7. Select property method
4. Specify composition range
8. click “Run Analysis” to generate the results
Cancel
124
125
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Calculation Result of T-xy
126
Calculation Result of T-xy
Data results
127
Generate xy plot
128
Generate xy plot (cont’d)
129
Flash Separation T=105 C P=1atm Saturated Feed
P=1atm F=100 kmol/hr
zwater=0.5
zHAc=0.5
What are flowrates and compositions of the two outlets?
130
Add Block: Flash2
131
Add Material Stream
132
Specify Feed Condition
Saturated Feed
(Vapor fraction=0)
P=1atm
F=100 kmol/hr
zwater=0.5
zHAc=0.5
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133
134
Block Input: Flash2
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Flash2: Specification
T=105 C
P=1atm
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Required
Input Complete
135
Buttons:
1.Click “Next” to check required input completeness
2.Click “OK” to run the simulation
136
Results Available
137
Stream Results
138
Stream Results (cont’d)
139
Heat Exchange (Simple Heater)
7
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kmol/hr
zwater=0.501
zHAc=0.409
T=105 C
P=1atm
Saturated Feed
P=1atm
F=100 kmol/hr
zwater=0.5
zHAc=0.5
kmol/hr
zwater=0.432
zHAc=0.568
Q:
Calculate the enthalpy required to heat the mixture from 1 atm, 50 ⁰C
to 5 atm 250 ⁰C using Peng-Rob model.
Species
Flow rate (Kmol/h)
Methane
10
Ethane
Propane
20
Using Thermodynamic model calculation that you learn…
Heat capacity for each component.
PR EOS calculation algorithm from textbook
Departure function from ideal gas.
Matlab program or Excel Calculation.
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….
140
Heat Exchange (Simple Heater)
Using Aspen Plus…Download presentation
Build in the components
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Heat
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142
Heat Exchange (Simple Heater)
Check the parameters
7
143
Heat Exchange (Simple Heater)
Add the unit, connecting the material streams…
Cancel
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144
Heat Exchange (Simple Heater)
Double click the material stream on the flow sheet…
Entering the stream input page.
145
Heat Exchange (Simple Heater)
Double click the heater on the flow sheet…
Entering the heater input page.
146
Heat Exchange (Simple Heater)
147
Heat Exchange (Simple Heater)
3. Run
Input all the condition,
including streams and blocks
2. “Input changed” or “required input completed”
148
Heat Exchange (Simple Heater)
Right click the “HEATER”
And, choose “Stream Results…”
149
Heat Exchange (Simple Heater)
Right click the “HEATER”,
Click “Result…”
150
Heat Exchange (Simple Heater)
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151
Heat exchange (HeatX) 熱物流 冷卻水 熱流出口氣相分率為 0
152
Components – Specification
153
Thermodynamic Model – NRTL
154
Thermodynamic Model – NRTL
155
Add Block: HeatX
156
Feeds Conditions
157
Feeds Conditions
158
Block Input
159
Check result
160
Check result
（飽和液相）
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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%
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冷卻水
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入口温度：20℃、入口压力：1.0 MPa
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流量：60000 kg/hr。
熱流出口氣相分率為Buttons:
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CLD-IN
HOT-IN
161
Introduction to Aspen Plus
Part 5-1: Basic operation of Reactor System
Reactor Systems (RGIBBS, RSTOIC,RCSTR,RPLUG)
162
Equilibrium Reactor: RGIBBS
RGIBBS unit predicts the product by minimizing GIBBS energy in the
system
It is very Useful When…:
Reaction Kinetics are unknown.
There are lots of products
163
Equilibrium
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Fresh Feed
Flow rate
1000 (kmol/h)
CO
0.2368
H2
0.7172
H2O
0.0001
CH4
0.0098
CO2
0.0361
Reactions:
T=300 k
P=470 psia
164
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Equilibrium Reactor: RGIBBS
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165
Equilibrium Reactor: RGIBBS
Inside the Block:
166
Check result
167
Kinetics Reactors: RPLUG
Reaction :Exothermic & reversible
Rate [=] Kmol/Kgcat/s
Activation Energy [=] KJ/Kmol
168
Kinetics Reactors: RPLUG
Reaction :Exothermic & reversible
Fresh Feed
Flow rate
200 (mol/h)
CO
0.030
H2
0.430
H2O
0.392
CO2
0.148
Catalyst Loading = Kg
Bed Voidage =
Feed Temperature = 583K
Feed Pressure = 1 bar
Reactor Length = 10 m
= we
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169
Kinetics Reactors: RPLUG
Feed Stream:
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170
Kinetics Reactors:
RPLUG
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Buttons: RPLUG
Kinetics Reactors:
Reaction Setting:
171
172 Kinetics Reactors: RPLUG
Reaction Setting:
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173
Kinetics Reactors: RPLUG
RPLUG Setting:
174
Check result
175
Check result
176
Check result
177
Check result
178
Check result
179
Check result
180
Check result
181
Kinetics Reactors: RCSTR
Reaction :Exothermic & Irreversible
Aniline + Hydrogen  Cyclohexylamine (CHA)
C6H7N + 3H2  C6H13N
182
Vertical cylindrical vessel
Reactor Conditions
Reactor :
Pressure
595 psi
Reactor
condition
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250 F
Volume
1200 ft3
Reactor type
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Vertical cylindrical vessel
Reactor liquid level
80%
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183 Reaction Kinetics Reaction rate : Where VR: reactor
volume
Buttons:
CA: concentration of Aniline
CH: concentration of Hydrogen
Reaction kinetics :
7
Where
T : temperature (R)
E = (cal/mol)
E : activity energy
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184
Reaction Kinetics Input
185
Reaction Kinetics Input
186
Reaction Kinetics Input
187
Reactor Conditions Input
188
Reactor Conditions Input
189
Feeds Conditions Two fresh feed stream : Aniline feed
Hydrogen feed
mole rate
temperature
100 F
100 F
pressure
650 psia
650 psia
190
Feeds Conditions
191
Check result (1) Compare the conversion between
RSTOIC and RCSTR.
(2) Compare the net duty inside the RSTOIC and RCSTR
Question:
192
Introduction to Aspen Plus
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Part 6: Running Simulation
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6-1: Basic Operation of separation System
Separation of Benzene/Toluene Mixture (DSTWU, RADFRAC)
193
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System Containing Benzene/Toluene
Example :
A mixture of benzene
and toluene
containing
mol% benzene
is wish
to to
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your friends
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than 10%
benzene
in
bottom
product.
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enters the column as saturated liquid, and the vapor leaving the
column which is Buttons:
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.
7
(2) The position of the entry.
(Problem is taken from Coulson & Richardson’s Chemical Engineering,
vol 2, Ex 11.7, p.564)
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194
1. By what you learned in Material balance and unit
operation
From Overall Material Balance:
100 = D+B
From Benzene Balance:
100*0.4 = 0.9 * D+ 0.1* B
Thus, D=37.5 and B=62.5.
37.5
62.5
195
1. By what you learned in Material balance and unit
operation
From thermodynamic phase equilibrium, and the calculation of
operating line:
We can get the number of theoretical plate to be 7.
196
2. By the shortcut method in Aspen Plus (DISTWU) (Add
components)
Built in the components
197
2. By the shortcut method in Aspen Plus (DISTWU)
(Select property method)
Select NRTL
198
2. By the shortcut method in Aspen Plus (DISTWU)
(Select property method)
Check the binary parameters
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199
2. By the shortcut method in Aspen Plus (DSTWU)
Add the unit “DSTWU”
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The red arrows are the required material stream!
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2.
By
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Aspen Plusit(DSTWU)
200
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Connect the required
material
stream
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201
2. By the shortcut method in Aspen Plus (DSTWU)
“Feed1” Stream specification
7
202
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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203
2. By the shortcut method in Aspen Plus (Column
Specification)
Light Key recovery
= (mol of light component in distillate) / (mol of light component in
feed)
= (37.5*0.9)/(100*0.4)
=
204
2. By the shortcut method in Aspen Plus (Column
Specification)
Heavy Key recovery
= (mol of heavy component in distillate) / (mol of heavy component in
feed)
= (37.5*0.1)/(100*0.6)
=
205
2. By the shortcut method in Aspen Plus (Column
Specification)
Get results by varying the number of stages. (Initial Guess)
206
2. By the shortcut method in Aspen Plus (DSTWU)
RUN THE SIMULATION
207
Results)
2. By the shortcut method in Aspen Plus (Stream
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Right click on the unit,
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and select “Stream Results”
208
2. By the shortcut method in Aspen Plus (Stream
209
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Results)
Required product quality
of stage)
For RR=3, at least 7Buttons:
theoretical stages are required.
210
3. More rigorous method in Aspen Plus (RADFRAC)
Add the unit “RADFRAC”
The red arrows are the required material stream!
7
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211 3. More rigorous method in Aspen Plus (RADFRAC)
Connect the required material stream
Download
212
3. More rigorous method in Aspen Plus (RADFRAC) (Feed
Specification)
Same as Case 2
213
3. More rigorous method in Aspen Plus (RADFRAC)
(Column Specification)
Double left click on the unit….
214
3. More rigorous method in Aspen Plus (RADFRAC)
(Column Specification)
7 stages from previous calculation.
RR=3 from the problem,
distillate rate = 37.5 (kmol/h)
from previous calculation
215
3. More rigorous method in Aspen Plus (RADFRAC)
(Column Specification)
Specify the feed stage
216
3. More rigorous method in Aspen Plus (RADFRAC)
(Column Specification)
Specify the pressure at the top of column
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217
3. More rigorous method in Aspen Plus (RADFRAC)
(Calculation of tray
size—Traypresentation
Sizing)
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218
3. More rigorous method in Aspen Plus (RADFRAC)
(Calculation of tray
Sizing)
Wesize—Tray
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*Calculation from 2th
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*Select a tray type.
Buttons:
219
3. More rigorous method in Aspen Plus (RADFRAC)
(Pressure drop calculation– Tray Rating)
7
220
3. More rigorous method in Aspen Plus (RADFRAC)
(Pressure drop calculation– Tray Rating)
*Calculation from 2th tray from the top to 2th tray from the Cancel
bottom.
(WHY??)
*Initial guess of the tray size
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221
3. More rigorous method in Aspen Plus (RADFRAC)
(Pressure drop calculation– Tray Rating)
222
3. More rigorous method in Aspen Plus (RADFRAC)
(Stream Results)
Click right button on the unit, and select “Stream Results”
223
3. More rigorous method in Aspen Plus (RADFRAC)
(Stream Results)
Different from the shorcut method.
(WHY??)
224
Introduction to Aspen Plus
Part 6: Running Simulation
6-2: Design, spec, and vary in RADFRAC
Separation of Benzene/Toluene Mixture
225
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
226
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
What do we want??
90%
at top.
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thisBenzene
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Select “Mole Purity”…
227
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec andDownload
Vary)
presentation
What do we want??
--- 90% Benzene at top.
Select “Mole Purity”…
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228
3. More rigorous
Buttons: method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
Select “Benzene”
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229
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
Cancel
Select the distillate stream
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230
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
Add a Vary
(1 Design Spec Vary)
231
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
Varying Reflux ratio to
reach the design target.
232
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
Specify the varying range.
(Should contain the initial value)
233
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
2nd Design Spec
234
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
What do we want??
--- 10% Benzene at bot.
Select “Mole Purity”…
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235
3. More rigorous method in Aspen Plus (RADFRAC)
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Vary)
presentation
What do we want??
--- 10% Benzene at bot.
Select “Mole Purity”…
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236
3. More rigorous
Buttons: method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
Select the Benzene
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237
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
Cancel
Select the bottom stream
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238
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
239
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
Varying distillate rate to
reach the design target.
Specify the varying range.
(Should contain the initial value)
240
3. More rigorous method in Aspen Plus (RADFRAC)
(Design , Spec and Vary)
RUN THE SIMULATION, and click right button on the unit, select
“Stream results”
241
3. More rigorous method in Aspen Plus (RADFRAC)
(Stream Results)
The required product quality
242
3. More rigorous method in Aspen Plus (RADFRAC)
(Column Results--top)
Calculated Reflux Ratio = 5.98
(from problem: 3)
243
3. More rigorous method in Aspen Plus (RADFRAC)
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The required heat duty for separation is (KW)
244
3. More rigorous method in Aspen Plus (RADFRAC)
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(Profile Inside the Column)
T : Temperature
P : Pressure
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Q: Heat Duty
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245 3. More rigorous method in Aspen Plus (RADFRAC)
(Profile Inside the Column)
You can select the vapor or
liquid composition profile.
(also in mole or mass basis)

7
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3.
More
rigorous
method
in
Aspen
Plus
(RADFRAC)
246
(Plotting Temp
3. More rigorous method in Aspen Plus (RADFRAC) (Plotting Temp.
Profile)
Download
247
3. More rigorous method in Aspen Plus (RADFRAC)
(Plotting Temp
3. More rigorous method in Aspen Plus (RADFRAC) (Plotting Temp.
Profile)
248
Exercise
Example:
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)
249
Introduction to Aspen Plus
Part 6: Running Simulation
6-3: Design and analysis of a Water/HAC system
Flowsheet Construction
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Design, Spec, Vary
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250
Distillation Separation: Water-HAC System
There are two Download
degrees ofpresentation
freedom to manipulate distillate
composition and bottoms composition to manipulate the distillate
and bottoms compositions.
If the feed condition
theyou
number
of stages
are given, how
much
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QR ?
Buttons:
251

Flowsheet/Connect Material Stream
252
Specify Feed Condition
Saturated Feed
(Vapor fraction=0)
P=1.2atm
F=100 kmol/hr
zwater=0.5
zHAc=0.5
253
Block Input: Radfrac
254
Radfrac: Configuration
255
Radfrac: Streams (Feed Location)
256
Radfrac: Column Pressure
7
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257
Run Simulation
Click ► to run simulation
258
Check Convergence Status
259
Stream Results
260
Stream Results D B
261
Change Reflux Ratio Click ► to run simulation
Increase RR from 2 to 2.5
262
DB
263
Again…
You can iterate RR until the specification is achieved.
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264
Using Design/Spec Function
Aspen Plus provides
a convenient
function (Design Specs/Vary) which
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can iterate operating variables to meet the specification.
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Add
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Design Specs
265
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Design
Specs:
Specification
266
Buttons:
Input current mole purity first
267
Design Specs: Components
268
Design Specs: Feed/Product Streams
269
Add New Very
270
Vary: Specifications Specify the range of the adjusted
7
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variable
Not all variables cane be selected.
In this case, only reflux ratio and reboiler duty can be used.
271
Selection of Adjusted Variables
The options of adjusted variables must correspond to the operating
specification.
272
Run Simulation
Click ► to run simulation
273
Check Convergence Status
274
Change Target of Mole Purity
Click ► to run simulation
Increase Target from to 0.99
275
DB
276
Column Performance Summary
277
Summary of Condenser
Include condenser duty, distillate rate, reflux rate, reflux ratio
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Summary of Reboiler
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278
Include reboiler duty, bottoms rate, boilup rate, boilup ratio
279
Column Profile: TPFQ
280
Column Profile: Vapor Composition
281
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Column Profile:
Liquid
Composition
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283
system. Share buttons are a little bit lower. Thank you!
Plot Composition Profile
Buttons:
Temperature Profiles
284
Plot Composition Profile
285
Composition Profiles
282
286
Introduction to Aspen Plus
Part 7 : Running Simulation
7-1: More Complex system with recycle
System with IPA/Water/DMSO
7
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287
Rename components ID
Isopropyl Alcohol
Water
Dimethyl Sulfoxide
288
Thermodynamic Model – NRTL
289
NRTL – Binary Parameters
Click “NRTL” and then built-in binary parameters appear
automatically if available.
290
NRTL – Binary Parameters-USER
Comp,i
IPA
H2O
Comp,j
DMSO
aij
aji
1.7524
bij
185.4
bji
777.3
Tocij
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0.3
0.30
291
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Ternary Maps
292
Ternary Maps 1. Select three components 3. Select
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4. Select phase (VLE, LLE)
5. Select report unitButtons:
6. Click Ternary Plot to generate the results
Ternary Maps Change pressure Ternary Plot Toolbar: 7
Add Tie line, Curve, Marker…
293
294
Cancel
Extractive Distillation
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295
Setup – Specification
Input mode
296
Add Block: RADFRAC
297
Add Block: MIXERS
298
Add Material Stream
299
Add Material Stream
300
Rename stream
Doulbe click to rename streams or blocks.
301
Specify Feed Condition
(Saturated Liquid Feed)
Temperature= 25°C
P = 3 atm
F = 100 kmol/hr
z IPA =0.5
z WATER =0.5
302
Specify Feed Condition
EF
P = 2 atm
T = oC
ToFmake
thiskmol/hr
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z DMSO =1
303
Specify Feed Condition
MAKEUP
P = 3 atm
T = 25 oC
F = 0 kmol/hr
z DMSO =1
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304
Buttons:
Block Input
305
Block Input
306
Block Input
307
Run Simulation
Click ► to run simulation
7
Cancel
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308
Check Convergence Status
Check result
309
Check streams result
310
Design Specs/Vary
311
Add New Design Specs
312
Design Specs: Specification
313
Design Specs: Components
314
Design Specs: Feed/Product Streams
315
Add New VAry
316
Very: Specifications
317
Run Simulation
Click ► to run simulation
318
Check Convergence Status
319
Design Specs/Vary
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320
Add New Design Specs
321
Design Specs: Specification
322
Design Specs: Components
323
Design Specs:
Feed/Product
Streams
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325
Buttons:
VAry: Specifications
326
Run Simulation
Click ► to run simulation
327
Check Convergence Status
328
Check streams result D1 D2
329
Recycle stream
330
Recycle stream
331
Recycle stream
332
tear
333
Check streams result
7
Cancel
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334
Summary of Reboiler B1 B2
Include reboiler duty, bottoms rate, boilup rate, boilup ratio
335
Tray Sizing
336
Tray Sizing
Click ► to run simulation
337
Tray Sizing
338
Tray Rating
339
Tray Rating
340
Update Pressure Drop of Stages
Click ► to run simulation
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341
342
Check Pressure Drop result
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Thanks for your attention!
PSE Laboratory
Department of Chemical
Engineering
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National Taiwan University
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Edited by: 程建凱/吳義章/余柏毅/陳怡均
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