Aspen Plus basic course for Engineers.
Introduction to Process Modeling/Simulation Software.
INDEX:
Course Objectives
Introduction to Aspen Plus
User Interface & Getting Help
Physical Properties
Introduction to Flowsheet
Unit Operation Models
Reporting Results
Case Studies I, II and III
Case Study IV
Conclusion
2. Hi there, this is a free overview of the Aspen Plus Course
I hope you like it! There are no VIDEOS in SlideShare
You can get those in the Online Course
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ASPEN PLUS COURSE
7. Makes us easier/faster work
Multiple and Simultaneous Simulations
Different Real-Life Scenarios
Change on raw/feed materials scenario
Pricing and Costs calculation
Raw Materials
Plant Cost
Utilities
How it would behave under different conditions
High/Low Pressure
Humidity Changes
Temperature change (cool/warm days/seasons)
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8. Mainly:
Petrochemical
Pharmaceutical
Fine chemicals
Other commodities such as:
Sulfuric acids
Chlorine/Caustic industry
Solvents
Coatings
Many more…
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9. Excelent for your curriculum as an engineer
Perfect for analytical/numerical minds
Good for debuging and fixing
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10. 1. Course Objectives
2. Introduction to Aspen Plus
3. User Interface & Getting Help
4. Physical Properties
5. Introduction to Flowsheet
6. Unit Operation Models
7. Reporting Results
8. Case Studies I, II and III
9. Case Study IV
10. Conclusion
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11. Basic Modeling of Substances & Processes
General Flowsheet Concepts
Basic Requirements to set up a Simulation
Setting the adequate Physical Properties
Flowsheet “manipulation”
Major and Common Unit Operations
Workshop Practice
Reporting Results (Tables)
Technical Stuff (extensions, versions, exporting, saving, etc...)
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12. Course Approach
Theory
Practice
More Practice
Analysis
Course Structure (Intensive)
1st Day
2nd Day
Course Structure (Recommended)
1st
2nd
3rd
4th
5th
6th
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13. About Aspen Plus ®
Why Aspen Plus ®
Benefits of simulations
Aspen Plus® vs. HYSYS®
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14. From the website:
“Aspen Plus is the market-leading chemical process optimization software
used by the bulk, fine, specialty, & biochemical industries, as well as the
polymers industry for the design, operation, and optimization of safe, profitable
manufacturing facilities.”
http://www.aspentech.com/products/engineering/aspen-plus/
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15. My version V8.2 and V8.8 (May 2013-2015)
Most recent version V8.8 (May 2015)
https://www.aspentech.com/products/Aspen-Plus/V88/
Main differences:
Solid Modeling
Activated Heat Exchanger Sizing and Rating*
Relief Sizing in the Safety Environment
Search and Share Models with aspenONE Drive
Access Aspen Process Manuals with aspenONE® Exchange
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16. Solid Modeling
Solids Modeling for Polymers
Particle Size Definition in Reactor Models
Contact Dryer Model
Conceptual Solids Models
Fluidized Bed Reactor Model
Spray Dryer Model
NOT included in the BASIC course!
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17. Aspen Plus
Chemical Industry (H2SO4, Polymers, Coatings, etc.)
Fine Chemistry (chemical reactions)
Non-ideal models (azeotropes, L-V equilibriums, etc.)
Electrolytes
Equation Oriented Mode
Aspen HYSYS
Mainly Petrochemical (upstream/downstream)
Hydrocarbon Oriented (Oil Industry)
Assays (Mixture of petrochemicals, i.e. petroleum)
Refinery Reactors (Catalytic reformer, FCC)
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18. Graphic User Interphase (GUI)
New File, Existing simulations, Exporting, etc…
Extension
Getting Help
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19. These exercises will be mentioned as we do Workshops, Practice Scenarios
and Cases
It is pretty straight forward really…
When opening a New Project Choose a Template and you’re done
When saving; use “Save as… Aspen Plus Document”
Exporting Files are not included in this Basic Course
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20. Start Page
New, Open, Recent Files
News
Get Started
Button (Ribbons) bar
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21. Start Page
New, Open, Recent Files
News
Get Started
Button (Ribbons) bar
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22. Start Page
New, Open, Recent Files
News
Get Started
Button (Ribbons) bar
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23. Start Page
New, Open, Recent Files
News
Get Started
Button (Ribbons) bar
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24. Start Page
New, Open, Recent Files
News
Get Started
Button (Ribbons) bar
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25. Start Page
New, Open, Recent Files
News
Get Started
Button (Ribbons) bar
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26. 001 Lading Page
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27. One Aspen Plus “Project” may involve:
• Backup file (.bkp)
• Embedded backup file (.apmbd)
• FORTRAN files ( .dll, .dlopt, .obj, .F )
• Equipment design and rating files (.bjt, .edr, etc)
• etc.
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28. File Type Extension Format Description
Compound *.apwz Binary Compressed file which contains the model (the BKP or APW
file) and external files referenced by the model. You can add
additional files such as supporting documentation to the APWZ
file.
Document *.apw Binary File containing simulation input, results and intermediate
convergence information
Backup *.bkp ASCII Archive file containing simulation input and results
Template *.apt ASCII Template containing default inputs
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29. Prepared “properties” and
preferences for the user
Air Separation
Chemical Processes
Gas Processing
Pharma
Refinery (most extensive)
Solids
“User” SI or English units
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43. 003 Simulation Evironment
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44. Direct Contact
Via Udemy Private Messages/Discussion boards
Via e-mail
Contact@ChemicalEngineeringGuy.com
Chemical.Engineering.Guy@gmail.com
Q&A from Website (Click HERE)
Forums & Groups
http://www.egpet.net/
http://www.cheresources.com/
http://www.eng-tips.com/threadminder.cfm?pid=137
LinkedIn
Aspen Plus Users
Official Aspen Plus User Community Official Aspen Plus User Community (869 users)
Official Aspen HYSYS User Community (9,000 users)
Aspen HYSYS® Dynamics UsersPrivate Group (1,800 users)
Aspen Tech
http://support.aspentech.com ***You got to be registered as a valid Aspen License User(s)
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45. Using Aspen Help Bar/Button
Help Bar/Help Button
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50. 004 Getting Help - Help Button
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57. Specifications
Global Property Method
Property Methods
Method Name
Method Assistant!
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58. Component Type
Chemical
Hydrocarbon
Special Chemical (water, amine, sour, electrolyte)
Refrigerant
Process Type
Chemical, Electrolyte, Environmental, Mineral & Metallurgical
Gas Processing, Oil and Gas, Petrochemical, Refining
Polymer
Power
Pharmaceutical
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59. Method Assistant Process Type Petrochemical
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60. Type of System Recommended Property Method
TEG Dehydration PR, Glycol Package
Sour Water Sour PR, Sour SRK
Cryogenic / Air Separation PR, PRSV, TST
Atmospheric Towers PR Options, GS, TST
Vacuum Towers PR Options, GS, TST, Braun K10, Esso Tabular
Ethylene Towers Lee-Kesler-Plocker
High H2 Systems PR, ZJ, GS, TST
Steam Systems NBS Steam, ASME Steam, CS, GS
Chemical Systems Activity Models (NRTL, UNIQUAC,…), PRSV
Compression / Light Gases MBWR
Amine Systems Amine Pkg, DBR Amine Package, Elec-NRTL
Electrolyte Systems Elec-NRTL
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62. Equation of States Activity Coefficients
Good for vapor phase modeling and liquids of
low polarity
Preferable for liquid phase
Try to avoid Non-Ideal Liquids Good for non-ideal liquid mixtures
Less binary parameters required Binary parameters required (liquid-liquid)
Extrapolation of Data Only valid in Temperature Ranges given
Good for Critical Region (Pc, Tc) Avoid critical region
Examples:
– PSRK
– PENG-ROB
– RK-SOAVE
Examples:
– NRTL
– UNIQUAC
– WILSON
– UNIFAC
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63. Do you have polar components?
Is the pressure low <10 bar?
Equation of State such as SRK or PENG-ROB…
Advanced Equation of State such as PSRK or PC-SAFT…
Are there any supercritical components?
Activity coefficient model with Henry’s law
Activity coefficient Model (NRTL, UNIQUAC, …)
no
START
no
no
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64. A stream of 10 kg/h of ethanol is added to another stream of 50/h kg of water.
Both at 25°C and 1 atm.
They are mixed.
There is no heat exchange with the surroundings (no heat gain/loss)
Then we heat it from 25°C to 77°C
The streams go out in a single pipe
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65. 005 Filling Physical Properties Environment
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66. You are ready to run the property simulation
Aspen will run
Model Methods
Compounds
If any compound has a modeling problem, you will receive errors (non-typical)
You are ready to work in the Simulation Environment!
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71. Set System/Process
Must have 0 Degrees of Freedom (System is “Fixed”)
Set Input Data in Streams (energy, work and materials)
Set Properties to Unit Operations (Blocks)
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72. 1. Set Physical Properties (Physical Environment)
2. Set Process in Flowsheet
Mass Streams (T,P, mass flow, fractions, etc.)
Heat/Work Explicit Duties (Q,W)
Unit Operations
Mass transfer (Distillation, flashes, etc.)
Heat Transfer (Heat Exchanger, single/double HEX, etc.)
Momentum Transfer (mixing, transportation of fluids, pumps, compressors, etc.)
Reaction Kinetic (Reactor, Equilibrium Reactors, Stoichiometric Reactors, etc.)
3. Run Simulation
4. Expect no Errors
If no errors Check solution in Reports
If there are errors Check type of error, try to fix if needed, re-run simulation
5. Analysis of Results, Sensitivity Analysis, Optimization, etc…
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73. 1. Set Physical Properties (Physical Environment)
2. Set Process in Flowsheet
Mass Streams (T,P, mass flow, fractions, etc.)
Heat/Work Explicit Duties (Q,W)
Unit Operations
Mass transfer (Distillation, flashes, etc.)
Heat Transfer (Heat Exchanger, single/double HEX, etc.)
Momentum Transfer (mixing, transportation of fluids, pumps, compressors, etc.)
Reaction Kinetic (Reactor, Equilibrium Reactors, Stoichiometric Reactors, etc.)
3. Run Simulation
4. Expect no Errors
If no errors Check solution in Reports
If there are errors Check type of error, try to fix if needed, re-run simulation
5. Analysis of Results, Sensitivity Analysis, Optimization, etc…
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74. 1. Set Physical Properties (Physical Environment)
2. Set Process in Flowsheet
Mass Streams (T,P, mass flow, fractions, etc.)
Heat/Work Explicit Duties (Q,W)
Unit Operations
Mass transfer (Distillation, flashes, etc.)
Heat Transfer (Heat Exchanger, single/double HEX, etc.)
Momentum Transfer (mixing, transportation of fluids, pumps, compressors, etc.)
Reaction Kinetic (Reactor, Equilibrium Reactors, Stoichiometric Reactors, etc.)
3. Run Simulation
4. Expect no Errors
If no errors Check solution in Reports
If there are errors Check type of error, try to fix if needed, re-run simulation
5. Analysis of Results, Sensitivity Analysis, Optimization, etc…
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75. Mass Streams Mainly
All inlet to process (raw material)
Intermediate streams (intermediate material)
All outlet to process (final products & by-products)
Heat and Work only if Required (direct Duty)
500 kJ must be applied
Loss of Heat due to cold temperature is 1054 KJ/s
14 HP Shaft Power Requirement
Pump has 12 BHP
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76. A stream of 10 kg/h of ethanol is added to another stream of 50/h kg of water.
Both at 25°C and 1 atm.
They are mixed.
There is no heat exchange with the surroundings (no heat gain/loss)
Then we heat it from 25°C to 77°C
The streams go out in a single pipe
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80. Your Process is Set!
Let’s Run the Simulation!
As follows…
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81. 1. Set Physical Properties (Physical Environment)
2. Set Process in Flowsheet
Mass Streams (T,P, mass flow, fractions, etc.)
Heat/Work Explicit Duties (Q,W)
Unit Operations
Mass transfer (Distillation, flashes, etc.)
Heat Transfer (Heat Exchanger, single/double HEX, etc.)
Momentum Transfer (mixing, transportation of fluids, pumps, compressors, etc.)
Reaction Kinetic (Reactor, Equilibrium Reactors, Stoichiometric Reactors, etc.)
3. Run Simulation
4. Expect no Errors
If no errors Check solution in Reports
If there are errors Check type of error, try to fix if needed, re-run simulation
5. Analysis of Results, Sensitivity Analysis, Optimization, etc…
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83. 006 Filling the Simulation Environement
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84. 1. Set Physical Properties (Physical Environment)
2. Set Process in Flowsheet
Mass Streams (T,P, mass flow, fractions, etc.)
Heat/Work Explicit Duties (Q,W)
Unit Operations
Mass transfer (Distillation, flashes, etc.)
Heat Transfer (Heat Exchanger, single/double HEX, etc.)
Momentum Transfer (mixing, transportation of fluids, pumps, compressors, etc.)
Reaction Kinetic (Reactor, Equilibrium Reactors, Stoichiometric Reactors, etc.)
3. Run Simulation
4. Expect no Errors
If no errors Check solution in Reports
If there are errors Check type of error, try to fix if needed, re-run simulation
5. Analysis of Results, Sensitivity Analysis, Optimization, etc…
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85. No!
Perfect!
Continue with Results and Analysis
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86. 1. Set Physical Properties (Physical Environment)
2. Set Process in Flowsheet
Mass Streams (T,P, mass flow, fractions, etc.)
Heat/Work Explicit Duties (Q,W)
Unit Operations
Mass transfer (Distillation, flashes, etc.)
Heat Transfer (Heat Exchanger, single/double HEX, etc.)
Momentum Transfer (mixing, transportation of fluids, pumps, compressors, etc.)
Reaction Kinetic (Reactor, Equilibrium Reactors, Stoichiometric Reactors, etc.)
3. Run Simulation
4. Expect no Errors
If no errors Check solution in Reports
If there are errors Check type of error, try to fix if needed, re-run simulation
5. Analysis of Results, Sensitivity Analysis, Optimization, etc…
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87. Solutions
Water + Ethanol mix will increase about 3°C due to its “real mixture”
Stream Results
Mixture: 60 kg/h; T = 301 K
Product: 60 kg/h; T = 301 K
Block Results
Mixer Final Temperature = 310.71 K
Heater Duty: 12360.66 kJ/h
*** More info in Section 7. Flowsheet Results
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89. 007 Results and Analysis
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90. Mixers/splitters
Separators
Exchangers
Columns
Reactors
Pressure Changers
Manipulators *
Solids *
Solid Separators *
User Models *
* Not Relevant in this Course
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91. Mixers/splitters
Separators
Exchangers
Columns
Reactors
Pressure Changers
* Not Relevant in this Course
Momentum Heat
Kinetics Mass
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92. Mixers/splitters
Separators
Exchangers
Columns
Reactors
Pressure Changers
* Not Relevant in this Course
Momentum
Mixers/Splitters
Pressure Change
Heat
Exchangers
Kinetics
Reactors
Mass
Separators
Columns
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93. This data is from
Aspen Plus Help Data
Sheet
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94. This data is from
Aspen Plus Help Data
Sheet
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96. 008 Introduction to Unit Operations
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97. Mixer
FSplit
Ssplit*
*Basic Course does not includes SSplit
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98. Required
One streams inlet (Q,W,M)
One stream outlet (Q,W,M)
Useful for
In-pipe blending (T-shape)
Mixing tanks (Adiabatic Only)
Static Mixers
Methods/Conditions
Ideal, Adiabatic Mixing
Pressure drop may be added
Either Mass, Q or W!
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99. Required
One streams inlet (Q,W,M)
One stream outlet (Q,W,M)
Useful for
Valves
Tanks
Back-Mixing
Purge/Vents
T-Shape Pipe
Methods/Conditions
N/A
Either Mass, Q or W!
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101. Fash2
Flash3*
Decanter*
Sep
Sep2*
*Basic Course includes only Flash2 and Sep
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102. Separates feed into
2 (vapor liquid) or 3 (vapor liquid liquid)
using rigorous vapor-liquid or vapor-liquid-liquid equilibrium
Required
Inlet (1)
Outlet (2)
Recommended Use:
Flash drums
Evaporators
Knock-out drums
Single stage separators
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103. Separates inlet stream components into multiple outlet streams, based on
specified flows or split fractions
Required
(1) inlet
(1) outlet
Recommended Operations:
Component separation operations
Distillation
Absorption,
*** when the details of the separation are unknown or unimportant
Essentially to avoid computation time
Not that recommended actually
“Black Box”
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107. Calculations:
Bubble or dew point calculations
Add or remove any amount of user specified heat duty
Match degrees of superheating or subcooling
Determine heating or cooling duty required to achieve a certain vapor fraction
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109. DSTWU*
Distl
RadFrac
Extract*
MultiFrac*
SCFrac*
PetroFrac*
ConSep*
BatchSep*
*Basic Course includes only Distl and RadFrac
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110. Shortcut multicomponent distillation rating model
Number of theoretical stages
Reflux ratio
Overhead product rate
Determines separation based on reflux ratio, number of stages, and distillate-
to-feed ratio
Assumes constant mole overflow and constant relative volatilities.
Recommended Operation
Columns with one feed and two product streams
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111. Rigorous fractionation
Performs rigorous rating and design calculations for single columns
Operation Recommendations
Ordinary distillation
Absorbers/Strippers
Extractive and azeotropic distillation
Three-phase distillation
Reactive distillation
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112. Multistage Vapor-Liquid Calculations:
Ordinary distillation
Absorption
Reboiled absorption
Stripping
Reboiled stripping
Extractive and azeotropic distillation
RadFrac is suitable for:
Two-phase systems
Three-phase systems (only in equilibrium mode)
Narrow and wide-boiling systems
Systems exhibiting strong liquid phase nonideality
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113. Model columns in which two liquid phases and chemical reactions occur
simultaneously, using different reaction kinetics for the two liquid phases.
Can model both random and structured packings.
Calculation of size and rate columns consisting of trays and/or packings.
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115. Balance/Stoichiometry Based
RStoic
RYield
Equilibrium Based
Requil*
Rgibbs*
Kinetic Model Based
RCSTR*
Rplug*
Rbatch*
*Basic Course includes only RStoic and RYield
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116. Stoichiometric reactor
Models stoichiometric reactor with specified reaction extent or conversion
Models:
Reactors where reaction kinetics are unknown or unimportant but stoichiometry
and extent of reaction are known
Reaction kinetics are unknown or unimportant and
Stoichiometry and the molar extent or conversion is known for each reaction
Performs:
Product selectivity and heat of reaction calculations
Simultaneously or sequentially
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117. Yield reactor
Models reactor with specified yield
Models:
Reactors where stoichiometry and kinetics are unknown or unimportant but a yield
distribution is known
Reaction stoichiometry is unknown or unimportant
Reaction kinetics are unknown or unimportant
Yield distribution is known
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119. Pump
Compr
Mcompr*
Valve*
Pipe*
Pipeline*
*Basic Course includes only Pump and Compr
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120. Has 1 input and 1 output at least
Must be in liquid state or incompressible gas. Otherwise, it must be stated
It may also be used as a Turbine
Pressure Ratio is allowed
Power Requirements are also input/output
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121. At least 1 inlet and 1 outlet
Excellent for Pressure Increases in gas phase
It might be used as a Turbine
Performance Curves are also included
Pinlet/Poutlet
Workload
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122. 014 Pressure Changers
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123. BASIC approach
Table
Graph
Chart
Etc…
*** Continue to intermediate for more!
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124. 015 Results P1
015 Results P2
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126. Now you know how to model the most Basic Unit Operations of Aspen Plus ®
You can model plenty of Common Processes by now!
You should go now:
Case Study I, II, III Apply all the knowledge into one process, step by step.
Case Study IV Apply your knowledge by your own. Compare final results with the
template result!
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127. Lets do a a Workshop!
No worries you won’t be alone!
We will be analyzing 3 cases:
Case Study I: Solvent Recovery (RadFrac, Mixers)
Case Study II: Cumene Production (Rstoic, Flash2, Heater)
Case Study III: 3 Gas Pressure (Compressor, Mixer, Valve, Heater)
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128. Statement
Read it carefully, write down all important data. Find data that might be useful
Building the diagram
Build the diagram accordingly, “after”, “before” and “then”, “pre” are pretty important words
Data Input
Name Streams logically. Add all substances, fractions, masses that are required.
Add Blocks, name them accordingly to their functions. Add all data needed
Run Simulation
Results Go to results; review there are no warnings, errors.
Write a Results Report & Check Results
Finally, make an analysis and make your final conclusion
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129. 1. Statement
2. Building the diagram
3. Data Input
Streams
Blocks
4. Run Simulation
5. Results & Reporting
6. Analysis
7. Conclusion
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130. A previous process contains a mixture of solvents which we are required to
recover. We are interested in pure acetone, methanol and water.
Source 1 (Process 1) – Contains a 5%-75%-20% water/acetone/methanol mix
350 gal/h are being sub-produced
Source 2 (Process 2) – Contains a 5%-35%-60% water/acetone/methanol mix
50 gal/h are being currenty treated in an old storage facility
You, as an junior engineer, propose a 2 separaton process: Split acetone (most
volatile); then Split water form methanol.
The previous process was not suitable for the separation, it used flash drums.
Instead you propose a distillation column system.
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131. Since there is no CAPEX left; we are not able to do 2 separate process. The idea is to
mix both stream sources; add water for the methanol/water interaction.
You decide to use an old distillation column from a Project which is in standby.
It has 40 trays; it owns a kettle reboiler and a total condenser. After calculations you
got that you should start working with a reflux ratio of 1:2 with respect to mass
The D/F ratio should be pretty similar, i.e. 1:1 per mole. Water is fed in the 12 stage
and the solvent mix in the 24th
Operation Pressure is about P = 15 psia (it could be optimized)
For the methanol-wáter rich bottom product; we require a NEW distillation column.
The Senior Engineers recommended the next data:
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132. Total condenser, Kettle Reboiler, 17 Stages. Similar operater reflux ratios to your
initial column. It must be feed between 9 and 11 stage.
Since you are operating at P = 15 psi, opérate at similar pressures
Utilities:
Water is available at 15 psia, T = 100 F.
Mass balance calculation requires a Vol. Flow rate of 100 gal/h
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133. Find:
Acetone purity
Methanol purity
Heat Duty in Reboiler-1
Heat Duty in Condenser-1
Heat Duty in Reboiler-2
Heat Duty in Condenser-2
If methanol prices are $ 1.13 per gallon, how much money we earn per day?
Is this water suitable for drinking?
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136. Distillation Column 2
RadFrac
P = 15 psia
Equilibrium operated, N-stages = 17, Total Condenser, Total Kettle Reboiler
Reflux Ratio = 2 (per mass); D/F Ratio = 1 per mol
Water Feed = 10
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137. Run the simulation!
Debug required?
Warnings
Errors?
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138. Acetone purity
Methanol purity
Heat Duty in Reboiler-1
Heat Duty in Condenser-1
Heat Duty in Reboiler-2
Heat Duty in Condenser-2
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139. Are purities achieved?
How much is recovered % of each material
If methanol prices are $ 1.13 per gallon, how much money we earn per day?
Is this water suitable for drinking?
Is this better tan flashes? Why?
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140. 016 Case Study I - Solvent Recovery
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141. 1. Statement
2. Building the diagram
3. Data Input
Streams
Blocks
4. Run Simulation
5. Results & Reporting
6. Analysis
7. Conclusion
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142. Cumene is typically produced from a benzene + propylene reaction at very low
pressures (vaccum).
The plant feedstock is 50%-50% B/P. It is about 80 lbmol/h.
It comes from a pump which delivers it at T = 220 F and P = 36 psia
The reactor is typically operated with a recycle stream of all volatile material in the
reactor’s outlet.
Final Reactors Temerature is not know but tt is imperative to cool down at T = 130 F
The sepation is carried out with a flash drum at P = 1 atm (for final product storage).
The flash is operated adiabatically
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143. Find:
Reactor’s Operation Temperature
Heat Duty of Cooler
Split Fraction of Separator
Flow rate of Recycle
Flow rate of product
Mol fraction of Cumene in product
Try it without recycle! (Same questions)
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145. Feed:
P = 36 psi
T = 220 F
F = 80 lbmol/h
X = 0.5 Benzene; 0.5 Propylene
Reactor
This is typically done via the reaction of Benzene + Propylene in a Reactor
Use Rstoic
Reaction is 1:1 1
90% conversión with respect to Benzene
Adibatical; i.e. Q = 0
P = 0 atm
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146. Cooler:
T cool = 130 F
P final = -0.1 psia (i.e. vacuum)
Flash Drum
P = 1 atm (final product)
Adiabatical, i.e. Q = 0
Recycle vapors
Liquids go to final product
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147. Run the simulation!
Debug required?
Warnings
Errors?
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148. Products:
X fraction of Cumene
Mol Flow of Product Stream
Recycle Mol flow stream
Blocks:
Reactor Temperature
Coolers Heat Duty
Recycle Split Fraction
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150. 017 Study Case II - Cumene Production
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151. 1. Statement
2. Building the diagram
3. Data Input
Streams
Blocks
4. Run Simulation
5. Results & Reporting
6. Analysis
7. Conclusion
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152. You are in charge of mixing, transport and compressing a mixture of gases used for a
furnace application. They are stored in separate tanks reservoirs.
The furnace operates at 5 bar so we need to mix all gases and then transport it to the
furnace.
Due to friction losses; we have a 1.5 bar pressure loss from the mixer to the furnace.
Compression is required.
The methane gas (essentially natural gas) is stored at 15 bar; ethane gas is at 2 bar
and the propane gas is already at 5 bar.
Compressors work with the given isentropic and mechanical efficiencies
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153. Find:
Compressor 1 - Duty
Compressor 2 - Duty
Final Product Gas Composition
Initial Temperature of mixture
Final Temperature
Try it with a final heater!
Try it with a cooler before the Compressions!
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155. Feed:
Methane – 30°C, 15 bar, 155 kg/h
Ethane – 25°C, 2 bar, 200 kg/h
Propane – 35°C, 5 bar, 120 kg/h
COMP1
Compressor
Isentropic
Discharge P = 5 bar
95% Isentropic Efficiency
88% Mechanical Efficiency
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156. Mixer:
P = 5 bar
Friction loss:
Model as Valve
Pressure Drop = 1.5 bar
Adiabatic Flash
COMP2
Compressor
Isentropic
Discharge P = 5 bar
90% Isentropic Efficiency
85% Mechanical Efficiency
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157. Run the simulation!
Debug required?
Warnings
Errors?
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158. Products:
Mass Fraction of all gases
Final Temperature
Final Pressure
Blocks:
Compressor 1 Workload
Compressor 2 Workload
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159. Tempearture increases:
What if, cooling before any compression?
Workload of heater/cooler vs. Compression
Energy optimization?
$$??
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160. 018 Case Study III - Gas Compression
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161. Now its time to practice alone!
Make your simulation
Compare with the results shown in the Course’s Workshop
If there are warning/error shown
Try troubleshooting
Send your results to me! @CHEMENG (any contact given before)
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162. Problem: Petrochem – (Natural Gas Separation, LP Gas, Pentanes + Hexaes)
Statement
Diagram…
Compare Results
Analysis and Conclusion (send feedback to Contact@Course)
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163. A Petrochemical Industry requires to Split the next Stream
Tank Status 150F; 800 psia
Max. Flow Rate 1000 lbmol/h
Composition of petroleum mix:
Try using only 3 distillation columns!
A flash drum s convenient for water removal prior to distillation.
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164. Find:
Final composition of Natural Gas Line (C1 mainly)
Final composition of Light gases (LPG C2-C4)
Final composition of Heavy Keys (C5 and C6)
Water flow rate from flash drum
Blocks
Heat Duty of Boiler + Condenser of each
Final Product Pressures
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165. Try changing:
Number of stages (trays)
Distillate/Feed Ratio
Reflux Ratio
Pre-coolers and Pre-heater before distillation
Pressure drop in columns
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168. Feed:
T = 150F; P = 800 psia
Max. Flow Rate 1000 lbmol/h
Flash
P = 300 psia
Q = 0 (adiabatic flashing)
Light Distillation
RadFrac
P = 150 psia; N = 18; feed = 10
Partial-Vapor Condenser; Kettle Boiler
Reflux Ratio = 2 (molar)
D/F ratio = 0.5 (mass)
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169. Mid-Light Distillation
RadFrac
P = 15 bar psia; N = 25; feed = 12
Partial-Vapor Condenser; Kettle Boiler
Reflux Ratio = 8 (mass)
D/F ratio = 0.5 (mass)
Heavy Distillation
RadFrac
P = 250 psi; dP = 15psia; N = 15; feed = 8
Total Condenser; Kettle Boiler
Reflux Ratio = 8 (mass)
D/F ratio = 0.5 (mass)
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170. Mixer:
P = 5 bar
Friction loss:
Model as Valve
Pressure Drop = 1.5 bar
Adiabatic Flash
COMP2
Compressor
Isentropic
Discharge P = 5 bar
90% Isentropic Efficiency
85% Mechanical Efficiency
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171. Run the simulation!
Debug required?
Warnings
Errors?
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172. Products:
% composition of all products
% vapor/liquid in products (should be either 1 or 0)
Blocks:
Compressor 1 Workload
Distillators:
Heat Duty of Condenser
Heat Duty of Reboiler
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174. Heat load requirements if previous chilling/cooling
Change in % composition due to Reflux Rate and F/D ratio
Compare Flashing vs. Not Flashing
Chance Flashing conditions (Pressure)
Overall Try to get better results for % compositions of streams!
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176. Finally! You made it!
By now you should be able to know:
General Flowsheet Concepts
Basic Requirements to set up a Simulation
Setting the adequate Physical Properties
Flowsheet “manipulation”
Major and Common Unit Operations
Workshop Practice
Reporting Results (Tables)
Technical Stuff (extensions, versions, exporting, saving, etc...)
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177. 1. Course Objectives
2. Introduction to Aspen Plus
3. User Interface & Getting Help
4. Physical Properties
5. Introduction to Flowsheet
6. Unit Operation Models
7. Reporting Results
8. Case Studies I, II and III
9. Case Study IV
10. Conclusion
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178. Continue with the next course Intermediate and Advance!
You will learn…
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179. Files:
Creating and editing templates
Reviewing samples/exercises/previous projects
More on extensions and backup, onedrive
Exchange, Support and Live chats
Continuous training
Physical Properties Environment:
More on Methods and how to use them
More on substances and YOUR own substances/assays
Graphs + Substances Properties charts
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180. Transient State
Steady vs. Unsteady/Transient states
Batch modeling
Economy Environment
Safety Environment
Energy Environment
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181. Unit Operations:
Rigourous/Detailed Heat Exchange
Rigourous/Detailed Distillation; Petroleum Refinery
Batch Separation (Columns)
MultiFrac and PetroFrac insights
Reactors All reactors left (Requil, Rgibbs, RCSTR, Rplug, Rbatch)
Modeling for mechanisms and kinetic theory
Extraction (liquid-liquid and many others)
Manipulators/Calculators
dP Valves, Pipes, Pipelines and Piping (drop of pressure, frictions, duty load)
Review of Unit Operations with Solids
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182. Running Simulations
More on Debugging, warnings, and fixing Errors
Degrees of Freedom
Process simplification
Reporting Results
Excel export/import
Sensitivity Analysis
Charts, Graphs, Tables
Programming tools
Fortran coding
Manipulator
Hierarchy
Calculator
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183. It was awesome to share the course!
Hope you like it
Please leave a Review! It really helps other students to find the course easier
If I get students; I get motivated to do MORE material XD
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184. www.ChemicalEngineeringGuy.com
This is a Free Trial…
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ASPEN PLUS COURSE