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I t d ti t A Introduction to Aspen Plus Pl Short Courses on Computer Applications for ChE Students
Speaker: JianKai Cheng (程建凱) p g (程建凱) [email protected] PSE Laboratory Department of Chemical Engineering Department of Chemical Engineering Nation Taiwan University
What What is Aspen Plus 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: http://www.aspentech.com/products/aspen-plus.cfm
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What What Aspen Plus provides Aspen Plus provides • Physical Property Models – World’s largest database of pure component and phase equilibrium data for conventional chemicals electrolytes solids and polymers 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 d d l d l f f d 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)
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Ref: Aspen Plus® Product Brochure
More Detailed 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) points…etc) – Data regression from experimental deta
• Process simulation P i l ti – pump, compressor, valve, tank, heat exchanger, CSTR, PFR, di till ti distillation column, extraction column, absorber, filter, l t ti l b b filt crystallizer…etc 4
What course Aspen Plus can be employed for • • • • • • •
MASS AND ENERGY BALANCES PHYSICAL CHEMISTRY CHEMICAL ENGINEERING THERMODYNAMICS CHEMICAL REACTION ENGINEERING CHEMICAL REACTION ENGINEERING UNIT OPERATIONS PROCESS DESIGN PROCESS CONTROL
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Lesson Objectives 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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Problem Formulation 1: Calculation the mixing properties of two stream
Mole Flow kmol/hr WATER BUOH BUAC Total Flow kmol/hr Temperature C Pressure bar Enthalpy kcal/mol E t Entropy cal/mol-K l/ l K Density kmol/cum
1
2
3
4
10 0 0 10 50 0 1 ? ? ?
0 9 6 15 80 1 ? ? ?
? ? ? ? ? 1 ? ? ?
? ? ? ? ? 10 ? ? ?
Mass Balance E Energy B Balance l Enthalpy Entropy…
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Problem Formulation 2: Flash Separation 120 T-x T T-y
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
o
T=105 C P=1atm
T ( C)
115 110 105 100 0.0
What are flowrates and compositions of the two outlets?
0.2
0.4
0.6
xWater and yWater
0.8
1.0
Problem Formulation 3: Dehydration of Acetic Acid by Distillation Column ((Optional) p )
10 1.0
Duty ?
0.6 yWater
Reflux ratio ?
0.8
0.4 0.2 0.0 0 0 0.0
0.2
0.4
0.6
xWater
0.8
1.0
Outline • Startup in Aspen Plus (Basic Input) (45 min) – User Interface – Basic Input: Setup, Components, Properties. • Properties Analysis (1 hour) – Pure Component – Mixtures (phase equilibrium) • Running Simulation (1 hour) – Blocks (Unit Operations) – Streams (flow streams) – Results 10
Introduction to Aspen Plus – Part 1
Startup in Aspen Plus
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Start with Aspen Plus Start with Aspen Plus A Aspen Pl Plus User U IInterface t f
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Aspen Plus Startup Aspen Plus Startup
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Interface of Aspen Plus Interface of Aspen Plus
ProcessFlowsheet Flowsheet Windows Process Windows
ModelLibrary Library (View||| Model yy) ) Model yy ((View| ModelLibrary Library
Stream
Status message
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More Information More Information
Help for Commands for Controlling Simulations
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Data Browser 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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Status Indicators Status Indicators
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Basic Input Basic Input • The minimum required inputs to run a simulation are: – – – – –
Setup Components Properties Streams Blocks
Property Analysis
Process Simulation
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Setup – Specification Setup – Setup Run Type
Input mode
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Setup – Run Type Setup – Setup Run Type Run Type
Description
Assay Data Analysis
A standalone assay data A t d l d t analysis/pseudocomponents generation run
Flowsheet
A Flowsheet run (including sensitivity studies and ( g y optimization). also include the following calculations: Property estimation, Assay data analysis and Property analysis
Use to
Analyze assay data when you do not want to A l d t h d t tt perform a flowsheet simulation in the same run. Fit physical property model parameters required by Aspen Plus to measured pure component, A standalone data regression run. Can contain D t R Data Regression i property constant estimation and property analysis t t t ti ti d t l i VLE, LLE and other mixture data. Aspen VLE LLE d th i t d t A Pl Plus calculations. cannot perform data regression in a Flowsheet run. Prepare a property package for use with Aspen C Custom Modeler, with third party commercial M d l i h hi d i l engineering programs, or with your company's Properties Plus A Properties Plus setup run in house programs. You must be licensed to use Properties Plus. P f Perform property analysis by generating tables l i b i bl A standalone property analysis run. Can contain of physical property values when you do not Property Analysis property constant estimation and assay data want to perform a flowsheet simulation in the analysis calculations. same run E i Estimate property parameters when you do not h d want to perform a flowsheet simulation in the Property Estimation A standalone property constant estimation run same run.
Perform process simulations 20
Components – Specification Components – Components
IInput components t t with Component name or Formula
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Input components Input components
Remark: If available, are
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Specification To do this Find components in the databanks Define a custom component that is not in a databank Generate electrolyte components and reactions from components you entered Reorder the components you have specified Review databank data for components you have specified (Retrieved physical property parameters from databanks ) property parameters from databanks.)
Click this button Find User Defined Elec Wizard Reorder Review
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Find Components Find Components
Click “Find”
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Find Components (cont Find Components (cont’d) d) Input Component name or Formula or p p CAS number
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NIST Chemistry WebBook NIST Chemistry WebBook NIST Chemistry
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Properties Process type(narrow the number of Process type(narrow the number of methods available)
Base method: IDEAL NRTL UNIQAC UNIFAC Base method: IDEAL, NRTL, UNIQAC, UNIFAC…
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Property Property Method Selection – Property Method Selection Method Selection – Assistant
Interactive help in choosing a property method
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Assistant Wizard Assistant Wizard
Specify Component type Chemical Systems
Is the system at high pressure? (NO) Two liquid phases
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Reference: http://www.et.byu.edu/groups/uolab/files/aspentech/
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Thermodynamic Model – NRTL Thermodynamic Model – Thermodynamic Model
NRTL
Vapor EOS Liquid gamma Liquid enthalpy Liquid volume Liquid volume
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Modify Property Model Modify Property Model Check “Modify y Property p y Model”
Specify p y New Method Name
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NRTL – Binary Parameters NRTL – NRTL Binary Parameters
Click Cli k “NRTL” and d th then b built-in ilt i binary bi parameters t appear automatically if available.
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Access Properties Models and Parameters
Review Databank Data
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Review Databank Data Review Databank Data Including: Ideal g gas heat of formation at 298.15 K Ideal gas Gibbs free energy of formation at 298.15 K Heat of vaporization at TB Normal boiling point Standard liquid volume at 60°F 60 F
….
Description of each parameter 35
Pure Component Databank Parameters Pure Component Databank Parameters
Help for Pure Component Databank Parameters
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Pure Component Temperature‐‐Dependent Properties Temperature
CPIGDP‐1
ideal gas heat capacity
CPSDIP‐1
Solid heat capacity
DNLDIP‐1
Liquid density
DHVLDP‐1
Heat of vaporization
PLXANT 1 PLXANT‐1
Extended Antoine Equation Extended Antoine Equation
MULDIP
Liquid viscosity
KLDIP
Liquid thermal q conductivityy
SIGDIP
Liquid surface tension
UFGRP
UNIFAC functional group 37
Example: PLXANT Example: PLXANT‐‐1 (Extended Antoine Equation) Corresponding Model Click “↖?” and then click where you don’t know
?
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Example: CPIGDP Example: CPIGDP‐‐1 (Ideal Gas Heat Capacity Equation) Corresponding Model
?
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Summary
So far, we have finished the basic settings including setup, components, and properties. This is enough to perform properties analysis. l i
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File File Formats in Aspen Plus Formats in Aspen Plus
File Type
Extension
Format
Description
Document
*.apw
Binary
File containing simulation input and results and i t intermediate convergence information di t i f ti
Backup
*.bkp
ASCII
Archive file containing simulation input and results
History
*.his
Text
Detailed calculation history and diagnostic messages
Problem Problem Description
*.appdf appdf
Binary
File containing arrays and intermediate File containing arrays and intermediate convergence information used in the simulation 41 calculations
File Type Characteristics File Type Characteristics •
•
•
Binary files fl – Operating system and version specific – Not readable, not printable Not readable not printable ASCII files – Transferable between operating systems – Upwardly compatible – Contain no control characters, “readable” – Not intended to be printed N i d d b i d Text files – Transferable between operating systems Transferable between operating systems – Upwardly compatible – Readable, can be edited – Intended to be printed 42
Introduction to Aspen Plus – Part 2
Properties Analysis in Aspen Plus 43
Overview of Property Analysis Overview of Property Analysis Use this form Use this form
To generate To generate
Binary
Tables and plots of pure component properties as a function of temperature and pressure Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue
Residue curve maps
Pure
Ternary Azeotrope
Ternary maps showing phase envelope, tie lines, and azeotropes Ternary maps showing phase envelope tie lines and azeotropes of ternary of ternary systems This feature locates all the azeotropes that exist among a specified set of components. components
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Ternary Maps Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Ti li Tie lines, Vapor curve, Boiling point V B ili i Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures Generic without flash calculations. Properties analysis of multi‐components (more ( than three) is also included. 44
Reminding • When you start properties analysis, you MUST p y components , properties model, and p p p specify corresponding model parameters. (Refer to Part I) Part I)
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Properties Analysis – Pure Component Properties Analysis – Properties Analysis Pure Component Use this form
To generate
Binary
Tables and plots of pure component properties as a function of temperature and pressure Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue
Residue curve maps
Pure
Ternaryy Azeotrope
Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systems This feature locates all the azeotropes that exist among a specified set of components.
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Ternary Maps Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures Generic without flash calculations. Properties analysis of multi‐components (more than three) is also included. 46
Properties Analysis – Pure Component Properties Analysis – Properties Analysis Pure Component
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Available Properties Available Properties Property (thermodynamic)
Property (transport)
Availability Free energy Constant pressure Constant pressure Enthalpy heat capacity Heat capacity ratio Fugacity coefficient Constant volume heat Fugacity coefficient Constant volume heat Fugacity coefficient capacity pressure correction Free energy departure Vapor pressure Free energy departure Density pressure correction Enthalpy departure Entropy Enthalpy departure Volume pressure correction py Enthalpy of Sonic velocity Sonic velocity vaporization Entropy departure
Thermal conductivity Surface tension Viscosity
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Example1: CP (Heat Capacity) Example1: CP (Heat Capacity)
1. Select property (CP) 4. Specify p y range g of temperature p 2. Select phase 5 S 5. Specify if pressure Add “N-butyl-acetate”
3. Select component
6. Select property method 7. click Go to generate the results 49
Example1: Calculation Results of CP Example1: Calculation Results of CP
Data results
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Example2: H (Enthalpy) Example2: H (Enthalpy)
1. Select property (H) 4. Specify range of temperature 2. Select phase 5. Specify pressure
3. Select component
6 S 6. Select l t property t method th d
7. click Go to generate the results
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Example: Example: Calculation Results of H Calculation Results of H
Data results 52
Properties Analysis – Binary Components Properties Analysis – Properties Analysis Binary Components Use this form
To generate
Binary
Tables and plots of pure component properties as a function of temperature and pressure Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue
Residue curve maps
Pure
Ternaryy Azeotrope
Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systems This feature locates all the azeotropes that exist among a specified set of components.
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Ternary Maps Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures Generic without flash calculations. Properties analysis of multi‐components (more than three) is also included. 53
Properties Analysis – Binary Components Properties Analysis – Properties Analysis Binary Components
Binary Component Properties Analysis Binary Component Properties Analysis Use this Analysis type To generate Temperature‐compositions diagram at Txy constant pressure Pressure‐compositions diagram at Pxy constant temperature Gibbs energy of mixing diagram as a function of liquid compositions. The A Aspen Physical Property System uses this Ph i l P S hi Gibbs energy of mixing diagram to determine whether the binary system will form two liquid phases at a given temperature and pressure at a given temperature and pressure.
Example: T‐ Example: T‐XY Example: T 1. Select analysis y type yp ((Txy) y)
2. Select two component
2. Select phase (VLE, VLLE)
5. Specify pressure
3. Select compositions basis
6 Select property method 6. 4. Specify composition range 7. click Go to generate the results
Example: calculation result of T‐ Example: calculation result of T‐XY Example: calculation result of T
Data results
Example: Generate XY plot Example: Generate XY plot
Click “plot wizard” to generate XY plot
Example: Generate XY plot (cont Example: Generate XY plot (cont’d) d)
Shortcoming of Binary Analysis Shortcoming of Binary Analysis Water-BuOH 120
110
o
T ( C)
100
90
?
80
70 0.0
0.2
0.4
0.6
Mole Fraction (Water)
Bi Binary A l i cannott generate Analysis t LLE data d t below b l azeotrope. t
0.8
1.0
Property Analysis – Generic Property Analysis – Property Analysis Use this form
To generate
Binary
Tables and plots of pure component properties as a function of temperature and pressure Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue
Residue curve maps
Pure
Ternaryy Azeotrope
Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systems This feature locates all the azeotropes that exist among a specified set of components.
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Ternary Maps Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures Generic without flash calculations. Properties analysis of multi‐components (more than three) is also included. 61
Properties Analysis – Ternary Properties Analysis – Properties Analysis
Ternary Map Ternary Map
1 Select three component 1. 4. Select phase (VLE, LLE) 2. Specify number of tie line
5. Specify pressure
3. Select property method
6. Specify temperature (if LLE is slected) 7. click Go to generate the results
Calculation Calculation Result of Ternary Map (LLE) Result of Ternary Map (LLE)
D t results Data lt
Property Analysis – Generic Property Analysis – Property Analysis Use this form
To generate
Binary
Tables and plots of pure component properties as a function of temperature and pressure Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue
Residue curve maps
Pure
Ternaryy Azeotrope
Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systems This feature locates all the azeotropes that exist among a specified set of components.
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Ternary Maps Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures Generic without flash calculations. Properties analysis of multi‐components (more than three) is also included. 65 Generic analysis is used if properties analysis of mixture is performed.
When to Use Generic Analysis When to Use Generic Analysis
Enthalpy of Mixtures
?
Water-BuOH 120
110
o
T ( C)
100
90
70 0.0
?
?
80
Specific composition
LLE 0.2
0.4
0.6
Mole Fraction (Water)
0.8
1.0
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Property Analysis – Generic Property Analysis – Property Analysis
Select Property analysis
67
Add New Analysis Add New Analysis
Select Generic
68
Specification Specification of System of System
3. Specify component flow
. Select “flash calculation” or not
2. Select phase (VLE, LLE) 4 S 4. Specify if the th corresponding di composition iti
69
Determine Determine Adjusted Variables Adjusted Variables
Specify feed condition
Temperature Pressure Vapor fraction Mole flow Mass flow StdVol flow Mole fraction Mass fraction StdVol fraction Specify range of adjusted variables 70
Specify Property‐ Specify Property‐Sets for Calculation Results
71
Add New Property‐ Add New Property‐Set (User‐ Add New Property Set (User‐Defined) Set (User
Select Physical Property
Description 72
Add New Property‐ Add New Property‐Set (cont Add New Property Set (cont’d) d) If the system requires VLLE calculation… calculation Select “Vapor” “1st liquid” “2nd liquid”
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Specify Property‐ Specify Property‐Sets Specify Property
74
Run Properties Analysis Run Properties Analysis Click ► to generate the results
Check “simulation status” “Results Available” means convergency convergency. 75
Example1: Calculation of Enthalpy Change for binary mixtures Change for binary mixtures Molar ratio of Butanol/Water=1:1
o
Temperature = 50 C
-60000
-56000 -58000 Liquid Vapor
-64000
-60000
-66000 66000 -68000 -70000
Liquid Vapor
-62000 Enthalpy (cal/m E mol)
Enthalpy (cal//mol)
-62000
-64000 -66000 -68000 -70000 -72000 -74000
-72000
-76000 -74000 40
50
60
70
80 o
Temperature ( C)
90
100
-78000 0.0
0.2
0.4
0.6
0.8
1.0
Mole fraction of Water in BuOH and Water
76
Search Physical Properties for Enthalpy of Mixtures (HMX) Select HMX. Others are optimal.
Add Property-Set
77
Calculate of Enthalpy Change As Calculate of Enthalpy Change As Temperature Varies Temperature Varies 1
2
3 4
78
Read Calculation Read Calculation Results Read Calculation Results Results
79
Exercise o
Temperature = 50 C -56000 -58000 -60000 Liquid Vapor
Enthalpy (ccal/mol)
-62000 -64000 -66000 -68000 -70000 -72000 -74000 -76000 -78000 0.0
0.2
0.4
0.6
0.8
1.0
Mole fraction of Water in BuOH and Water
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Example 2: Example 2: Calculation of Calculation of LLE LLE for Binary system for Binary system Water-BuOH 120
110
o
T ( C)
100
90
80
70 0.0
0.2
0.4
0.6
0.8
1.0
Mole Fraction (Water)
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Add Add New Property Add New Property‐ New Property‐Set (cont Set (cont’d) d)
Select “Vapor” “1st liquid” “2nd liquid”
Specify System, Variable and Property‐ Specify Specify System, Variable and Property System Variable and Property‐Set 1
2
Select Vapor-liquid-liquid
3 4
Calculation Results Calculation Results
Water-BuOH 120
110
o
T ( C)
100
90
80
70 0.0
0.2
0.4
0.6
Mole Fraction (Water)
0.8
1.0
Property Analysis Property Analysis – Property Analysis – Conceptual Conceptual Design Design (Optional) Use this form
To generate
Binary
Tables and plots of pure component properties as a function of temperature and pressure Txy Pxy or Gibbs energy of mixing curves for a binary system Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue
Residue curve maps
Pure
Ternary Azeotrope
Ternary maps showing phase envelope, tie lines, and azeotropes y p gp p , , p of ternary y systems This feature locates all the azeotropes that exist among a specified set of p components.
Ternary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Ternary Maps Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines Vapor curve Boiling point Tie lines, Vapor curve, Boiling point Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures Generic without flash calculations Properties analysis of multi‐components (more without flash calculations. Properties analysis of multi‐components (more than three) is also included. 85
Conceptual Design Conceptual Design
Conceptual Design Conceptual Design • Conceptual design enables the user to: 1. Locate all the azeotropes (homogeneous and heterogeneous) present in any multicomponent mixture 2. Automatically compute distillation boundaries and residue curve maps for ternary mixtures id f t i t 3. Compute multiple liquid phase envelopes (liquid‐liquid and vapor liquid liquid) for ternary mixtures and vapor‐liquid‐liquid) for ternary mixtures 4. Determine the feasibility of splits for distillation columns
Azeotrope Analysis Azeotrope Analysis
Azeotrope Analysis Azeotrope Analysis 1. Select components (at least two)
2. Specify pressure
3. Select property method 6. click Report to generate the results 4 Select phase (VLE 4. (VLE, LLE)
5. Select report Unit
Error Message Error Message
Close analysis input dialog box (pure or binary analysis)
Azeotrope Analysis Report Azeotrope Analysis Report
Ternary Maps Ternary Maps
Ternary Maps Ternary Maps 3 Select property method 3. 1. Select three components
4. Select phase (VLE, LLE)
2. Specify pressure
5. Select report Unit
6. Click Ternary Plot to generate the results
6. Specify temperature of LLE (If liquid-liquid envelope is selected)
Ternary Maps Ternary Maps Change pressure or temperature
Ternary Plot Toolbar: Add Tie line,, Curve,, Marker…
Introduction to Aspen Plus – Part 3
Running Simulation in Aspen Plus 95
Example 1: Calculate the mixing properties of two stream
Mole Flow kmol/hr WATER BUOH BUAC Total Flow kmol/hr Temperature C Pressure bar Enthalpy kcal/mol E t Entropy cal/mol-K l/ l K Density kmol/cum
1
2
3
4
10 0 0 10 50 0 1 ? ? ?
0 9 6 15 80 1 ? ? ?
? ? ? ? ? 1 ? ? ?
? ? ? ? ? 10 ? ? ?
96
Example 2: Flash Separation Example 2: Flash Separation 120 T-x T T-y
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
o
T=105 C P=1atm
T ( C)
115 110 105 100 0.0
What are flowrates and compositions of the two outlets?
0.2
0.4
0.6
xWater and yWater
0.8
1.0
Example 3: Dehydration of Acetic Acid by Distillation Column (Optional) 10 1.0
Duty ?
0.6 yWater
Reflux ratio ?
0.8
0.4 0.2 0.0 0 0 0.0
0.2
0.4
0.6
xWater
0.8
1.0
Setup – Specification Setup – Setup
Select Flowsheet
99
Reveal Model Library Reveal Model Library
View|| Model Library or press F10
100
Model Library: Mixer/Splitter Model Library: Mixer/Splitter
Model
Description
Purpose
Use for
Mixer
Stream mixer
Combines multiple streams into one stream
Mixing tees. Stream mixing operations. g p Adding heat streams. Adding work streams
FSplit
Stream splitter Stream splitter
Divides feed based on splits Divides feed based on splits specified for outlet streams
Stream splitters. Bleed Stream splitters Bleed valves
SSplit
Substream splitter
Divides feed based on splits Divides feed based on splits specified for each substream
Stream splitters. Perfect Stream splitters Perfect fluid‐solid separators 101
Model Library: Pressure Changers Model Library: Pressure Changers
102
Model
Description Purpose Use for P Pump or hydraulic h d li Changes stream pressure when the Ch t h th Pumps and hydraulic P d h d li Pump turbine power requirement is needed or turbines known C Compressor or Ch Changes stream pressure when t h P l t i compressors, Polytropic Compr turbine power requirement is needed or polytropic positive known displacement compressors, isentropic compressors isentropic compressors, isentropic turbines Changes stream pressure across Multistage polytropic Mcompr Multistage compressor or compressor or multiple stages with intercoolers compressors, polytropic multiple stages with intercoolers. compressors polytropic turbine Allows for liquid knockout streams positive displacement from intercoolers compressors, isentropic compressors isentropic compressors, isentropic turbines Valve pressure Models pressure drop through a Control valves and pressure Valve drop valve changers Single segment Models pressure drop through a Pipe with constant diameter Pipe pipe single segment of pipe (may include fittings) Multiple segment Models pressure drop through a Models pressure drop through a Pipeline with multiple Pipeline with multiple Pipeline Multiple segment pipeline pipe or annular space lengths of different diameter or elevation103
Adding a Mixer Adding a Mixer
Click “one of icons” and d then th click li k again i on the th flowsheet fl h t window i d Remark: The shape of the icons are meaningless
104
Adding Material Streams Adding Material Streams
Click “Materials” and then click again on the flowsheet window
105
Adding Material Streams (cont’d) Adding Material Streams (cont d)
When clicking the mouse on the flowsheet window window, arrows (blue and red) appear.
106
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. water
Red arrow(Left) Feed (Required; one ore more if mixing material streams)
Red arrow(Right): Product (Required; if mixing material streams)
107
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 lines.
108
Reconnecting Material Streams (Feed Stream) Right Click on the stream and select Reconnect Destination
109
Reconnecting Material Streams (Product Stream)
Right Click on the stream and select Reconnect Source
B1
1
3
2
110
Specifying Feed Condition Specifying Feed Condition
Right Click on the stream and select Input
111
Specifying Feed Condition Specifying Feed Condition
You must specify two of the following conditions: Temperature p Pressure Vapor 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. 112
Specifying Feed Condition (cont’d) Specifying Feed Condition (cont d) 1
2
113
Specifying Input of Mixer Specifying Input of Mixer
Right Click on the block and select Input
114
Specifying Input of Mixer (cont Specifying Input of Mixer (cont’d) d)
Specify Pressure and valid phase
The corresponding description about this blank: Outlet pressure if value > 0 Pressure drop if value ≦ 0 115
Run Simulation 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 q Input p Complete” p means the input p is ready y to run simualtion 116
Status Status of Simulation Results of Simulation Results Message Results available
Means The run has completed normally, and results are present. present
Results for the run are present. Warning messages were generated during the esu ts t a gs Results with warnings calculations. View the Control Panel or History l l i Vi h C l P l Hi 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 p , y changed the input since the results were generated. The results may be inconsistent with the current input. 117
Control Pannel Control Pannel Click here
1.A message window showing the progress of the simulation by displaying the most recent messages from the calculations 2.A status area showing the hierarchy and order of simulation blocks and convergence loops executed 118
Stream Results Stream Results
Right Click on the block and select Stream Results
119
Pull down the list and select “Full” to show more properties results.
Enthalpy and Entropy
Substream: MIXED Mole Flow kmol/hr WATER BUOH BUAC Total Flow kmol/hr Total Flow kg/hr Total Flow cum/hr Temperature C Pressure bar V Vapor Frac F Liquid Frac Solid Frac Enthalpy kcal/mol Enthalpy kcal/mol Enthalpy kcal/kg Enthalpy Gcal/hr Entropy cal/mol‐K Entropy cal/gm‐K Density kmol/cum Density kg/cum Average MW Average MW Liq Vol 60F cum/hr
1
2
3
10 0 0 10 180.1528 0.18582 50 2 0 1 0 ‐67.81 67.81 ‐3764.03 ‐0.6781 ‐37.5007 ‐2.0816 53.81564 969.5038 18 01528 18.01528 0.1805
0 9 6 15 1364.066 1.74021 80 1 0 1 0 ‐94.3726 94.3726 ‐1037.77 ‐1.41559 ‐134.947 ‐1.48395 8.619647 783.851 90 93771 90.93771 1.617386
10 9 6 25 1544.218 1.870509 70.08758 1 0 1 0 ‐83.7476 83.7476 ‐1355.82 ‐2.09369 ‐95.6176 ‐1.54799 13.36534 825.5604 61 76874 61.76874 1.797886 120
Change Change Units of Calculation Results Units of Calculation Results
121
Setup – Defining Setup – Setup Defining Your Own Units Set Your Own Units Set
122
Setup – Report Options Setup – Setup Report Options
123
Stream Results with Format of Mole Fraction
124
Add Pump Block Add Pump Block
125
Add A Material Stream Add A Material Stream
126
Connect Streams Connect Streams
127
Pump – Specification Pump – Pump Specification 1. Select “Pump” or “turbine” 2. Specify pump outlet specificati (pressure, power)
3. Efficiencies (Default: 1)
128
Run Simulation Run Simulation Click ► to generate the results
Check “simulation status” “Required q Input p Complete” p 129
Block Results (Pump) Block Results (Pump)
Right Click on the block and select Results
130
131
Streams Results Streams Results
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Calculation Results (Mass and Energy Balances)
1
2
3
Mole Flow kmol/hr WATER 10 0 10 BUOH 0 9 9 BUAC 0 6 6 Total Flow kmol/hr 10 15 25 Temperature C 50 0 80 70.09 0 09 Pressure bar 1 1 1 Enthalpy kcal/mol -67.81 -94.37 -83.75 E t Entropy cal/mol-K l/ l K -37.50 37 50 -134.95 134 95 -95.62 95 62 Density kmol/cum 969.50 783.85 825.56
4 10 9 6 25 71.20 1 20 10 -83.69 -95.46 95 46 824.29
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Exercise
Mole Flow kmol/hr Water Ethanol Methanol Total Flow kmol/hr Temperature C Pressure essu e ba bar Enthalpy kcal/mol Entropy cal/mol-K Densityy kmol/cum
1
2
3
4
5
6
10 0 0 10 50 1 ? ? ?
0 5 0 15 70 1 ? ? ?
0 0 15 15 40 1 ? ? ?
? ? ? ? ? 1 ? ? ?
? ? ? ? ? 4 ? ? ?
? ? ? ? ? 2 ? ? ?
Please use Peng-Robinson EOS to solve this problem.
134
Example 2: Flash Separation Example 2: Flash Separation 120 T-x T T-y
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
o
T=105 C P=1atm
T ( C)
115 110 105 100 0.0
What are flowrates and compositions of the two outlets?
0.2
0.4
0.6
xWater and yWater
0.8
1.0
Input Components Input Components
Thermodynamic Thermodynamic Model: NRTL Thermodynamic Model: NRTL‐ Model: NRTL‐HOC
Vapor ESHOC Liquid gamma q g Liquid enthalpy Liquid volume
Check Binary Parameters Check Binary Parameters
Association parameters of HOC Association parameters of HOC
Binary Parameters of NRTL Binary Parameters of NRTL
Binary Analysis Binary Analysis
T‐xy plot 1. Select analysis type (Txy)
2. Select two component 3 Select compositions basis 3.
2. Select p phase (VLE, ( , VLLE))
5. Specify pressure 6. Select property method
4. Specify composition range 7. click Go to generate the results
Calculation Calculation Result of T Calculation Result of T‐ Result of T‐xy
Data results
Generate xy plot Generate xy Generate
Generate xy plot (cont Generate xy Generate plot (cont’d) d)
Flash Separation Flash Separation 120 T-x T T-y
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
o
T=105 C P=1atm
T ( C)
115 110 105 100 0.0
What are flowrates and compositions of the two outlets?
0.2
0.4
0.6
xWater and yWater
0.8
1.0
Add Block: Flash2 Add Block: Flash2
Add Material Stream Add Material Stream
Specify Feed Condition Specify Feed Condition
Saturated Feed (Vapor fraction=0) P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
Block Input: Flash2 Block Input: Flash2
Flash2: Specification Flash2: Specification
T=105 C P 1 t P=1atm
Required Input Incomplete Required Input Incomplete Connot click ► to run simulation
Close binary analysis window
Required Input Complete Required Input Complete Click ► to run simulation
Stream Results Stream Results
Stream Results (cont Stream Results (cont’d) d) 42.658 kmol/hr zwater=0.501 zHAc=0.409
Saturated Feed P=1atm F=100 kmol/hr zwater=0.5 zHAc=0.5
T=105 C P=1atm
57.342 kmol/hr zwater=0.432 zHAc=0.568
Review Distillation Separation Review Distillation Separation McCabe- Thiele Graphical Method
1 Rectifying section:
LR D xn 1 xD VR VR
Stripping pp g section:
LS B yn xn 1 xB VS VS
0.6 y
yn
0.8
0.4 02 0.2 0 0
02 0.2
04 0.4
06 0.6 x
08 0.8
1
Trade‐off Between Trade‐ Capital Cost and Operating Cost
Shortcut Design: RR≈1.2×RRmin NT ≈ 2×NTmin
Distillation Separation Distillation Separation
RR ?
QR ?
• There are two degrees of freedom to manipulate d ll distillate composition and d bottoms composition to manipulate the distillate and manipulate the distillate and bottoms compositions. • If the feed condition and the If the feed condition and the number of stages are given, how much of RR and QR are required to achieve the specification.
Add Block: Radfrac Add Block: Radfrac Add Block:
Add Material Stream Add Material Stream
Flowsheet Connectivity for Connectivity for RadFrac Connectivity for RadFrac
RadFrac numbers stages from the top down, starting with the condenser (or starting with the top stage if there is no condenser).
Connect Material Stream Connect Material Stream
Specify Feed Condition Specify Feed Condition
Saturated Feed (Vapor fraction=0) P=1.2atm F=100 kmol/hr zwater=0.5 zHAc=0.5
Block Input: Radfrac Block Input: Radfrac Block Input:
Radfrac:: Configuration Radfrac: Configuration Radfrac : Configuration
Radfrac::: Streams (Feed Location) Radfrac: Streams (Feed Location) Radfrac Streams (Feed Location)
Types of Feed Stage Types of Feed Stage Use this convention To introduce a feed g Between stages, above the designated stage g , g g Above‐stage On‐stage On the designated stage On the designated stage, all‐liquid feed On‐stage‐liquid On stage liquid which is never flashed On the designated stage, all‐vapor feed On‐stage‐vapor g p which is never flashed which is never flashed To the decanter attached to the designated Decanter stage
Radfrac:: Column Pressure Radfrac: Column Pressure Radfrac : Column Pressure
Run Simulation Run Simulation Click ► to run simulation
Check Check Convergence Status Convergence Status
Stream Results Stream Results
D
B
Change Reflux Ratio Change 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 achieved.
Smarter Way Smarter Way
Aspen Plus provides a convenient function (Design Specs/Vary) which can iterate operating variables to meet the specification.
Add New Design Specs Add New Design Specs
Design Design Specs: Specification Specs: Specification
Input current mole purity first
Design Design Specs: Components Specs: Components
Design Design Specs: Feed/Product Streams Specs: Feed/Product Streams
Add New Very Add New Very
Very: Specifications Very: Specifications
Specify the range of the adjusted variable Not all variables cane be selected selected. In this case, only reflux ratio and reboiler duty can be used.
Selection of Adjusted Variables Selection of Adjusted Variables
The options of adjusted variables must correspond to the operating specification.
Run Simulation Run Simulation Click ► to run simulation
Check Check Convergence Status Convergence Status
Change Target of Mole Purity Change Target of Mole Purity Click ► to run simulation
Increase Target from 0.95229424 to 0.99
Check Check Convergence Status Convergence Status
D
B
Column Column Performance Summary Performance Summary
Summary of Condenser Summary of Condenser
I l d condenser Include d duty, d t distillate di till t rate, t reflux fl rate, t reflux fl ratio ti
Summary of Reboiler Summary of Reboiler Summary of
I l d reboiler Include b il duty, d t bottoms b tt rate, t boilup b il rate, t boilup b il ratio ti
Column Profile: TPFQ Column Profile: TPFQ
Column Profile: Vapor Composition Column Profile: Vapor Composition
Column Profile: Liquid Composition Column Profile: Liquid Composition
Plot Wizard for Column Profile Plot Wizard for Column Profile
Plot Wizard for Column Profile (cont’d) Plot Wizard for Column Profile (cont d) After entering g the block,, “Plot” appears. pp
Plot Wizard Plot Wizard
Plot Types Plot Types
Steps Steps for Composition Plot for Composition Plot
Composition Profiles Composition Profiles
Temperature Profiles Temperature Profiles
INTRODUCTION TO ASPEN PLUS INTRODUCTION TO ASPEN PLUS
Some Tips and Others 202
Tips: Next Tips: Next
Invokes the Aspen Plus expert system. Guides you through the p required q to complete p your y simulation. steps Status message Flowsheet Not Complete Required Input Not C Complete l
Meaning Flowsheet connectivity is incomplete. To find out why, click the Next button in the toolbar. Input specifications for the run are incomplete. Click Next on the toolbar to find out how to complete the input h lb fi d h l h i specifications, and to go to sheets that are incomplete.
203
Example: Example: “NEXT” NEXT
204
Tips: “What’s Tips: What s this this” Cli k “↖?” and Click d then th click li k where h you don’t d ’t know k
?
205
Tips: “What’s Tips: What s this this”
?
206
Tips: Window Tips: Window
If you are using
You should
Workbook mode Flowsheet as Wallpaper p p Normal View
Click the Process Flowsheet tab Click the flowsheet in the background g Select the Process Flowsheet window
207
Help Topics Help Topics Go to “Help” p Select “Help Topics”
208
Help Topics Help Topics
Unit U it O Operation ti M Model d l Reference R f Manual M l Physical Property Methods and Models Physical Property Data Reference Manual
209
Help Topics Help Topics Calculation of Properties Using an Equation-of-State Property Method
210
File File Formats in Aspen Plus Formats in Aspen Plus
File Type
Extension
Format
Description
Document
*.apw
Binary
File containing simulation input and results and i t intermediate convergence information di t i f ti
Backup
*.bkp
ASCII
Archive file containing simulation input and results
History
*.his
Text
Detailed calculation history and diagnostic messages
Problem Problem Description
*.appdf appdf
Binary
File containing arrays and intermediate File containing arrays and intermediate convergence information used in the simulation 211 calculations
File Type Characteristics File Type Characteristics •
•
•
Binary files fl – Operating system and version specific – Not readable, not printable Not readable not printable ASCII files – Transferable between operating systems – Upwardly compatible – Contain no control characters, “readable” – Not intended to be printed N i d d b i d Text files – Transferable between operating systems Transferable between operating systems – Upwardly compatible – Readable, can be edited – Intended to be printed 212
Access Aspen Plus Software Access Aspen Plus Software • Please contact PC Teaching Assistant: Name: 侯冠宇 Phone: 02‐3366‐3005 Email: chemeng@ntu edu tw Email: [email protected] Office: 101 電腦教室
213
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