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Requirements
Basic understanding of Plant Design & Operation
Strong Chemical Engineering Fundamentals
Aspen Plus V10 (at least 7.0)
Aspen Plus – Basic Process Modeling (Very Recommended)
Aspen Plus – Intermediate Process Modeling (Somewhat Recommended)
Description
This BOOTCAMP will show you how to model and simulate common industrial Chemical Processes.
It is focused on the “BOOTCAMP” idea, in which you will learn via workshops and case studies, minimizing theory to maximize learning.
You will learn about:
Better Flowsheet manipulation and techniques
Understand Property Method Selection and its effects on simulation results
More than 15 Unit Operations that can be used in any Industry
Model Analysis Tools required for process design
Reporting Relevant Results Plot relevant data
Analysis & Optimization of Chemical Plants
Economic Analysis
Dynamic Simulations
At the end of this Bootcamp, you will be able to model more industrial processes, feel confident when modeling new processes as well as applying what you have learnt to other industries.
4. Benzene stream is to be heated from 75°F to 145°F @50psia
O-toluidine is to be used as heating material. It is available at 230°F and should not drop
below 150°F @45 psia
Max. Pressure dorp is 10 psia per side (Tube/Shell)
Identify the best Heat Exchanger if this must be a small heater, i.e. use multiple passes (6)
to avoid long sizing
www.ChemicalEngineeringGuy.com https://www.youtube.com/watch?v=wE8TxtWKX18
https://www.youtube.com/watch?v=9-UdleyXfUs
5. (A) Verify Energy Balances Heating and Cooling Duties
Get Mass require of heating fluid
Get Heat duty of heat exchanger
(B) Get Heat-X Shortcut
(C) Convert to Rigorous, verify results
(D) Specify Shell & Tube Exchanger
(E) Change conditions
HEAT-X RATING!
If Benzene Inlet 90,000 lb/h to 100,000 lb/h to 120,000 lb/h to 180,000 lb/h
www.ChemicalEngineeringGuy.com https://www.youtube.com/watch?v=wE8TxtWKX18
https://www.youtube.com/watch?v=9-UdleyXfUs
6. (A) Verify Energy Balances Heating and Cooling Duties
Get Mass require of heating fluid
Get Heat duty of heat exchanger
(B) Get Heat-X Shortcut
(C) Convert to Rigorous, verify results
(D) Specify Shell & Tube Exchanger
(E) Change conditions
HEAT-X RATING!
If Benzene Inlet 90,000 lb/h to 100,000 lb/h to 120,000 lb/h to 180,000 lb/h
www.ChemicalEngineeringGuy.com https://www.youtube.com/watch?v=wE8TxtWKX18
https://www.youtube.com/watch?v=9-UdleyXfUs
7. Try to get something similar to this:
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https://www.youtube.com/watch?v=9-UdleyXfUs
13. Add Heat flow
No need to specify Heat duties in UNITS
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15. (B) Get Heat-X Shortcut
Select TEMP
Avoid DUTIES
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18. (C) Convert to Rigorous
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19. (C) Convert to Rigorous
Size with recommended data
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20. (C) Convert to Rigorous
Size with recommended data
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22. (C) Convert to Rigorous
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23. (C) Convert to Rigorous
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24. (C) Convert to Rigorous
From EDR Results only:
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30. (D) Specify Shell & Tube Exchanger
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32. (E) Change conditions
If Benzene Inlet
90,000 lb/h to 120,000 lb/h
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33. (E) Change conditions
If Benzene Inlet
90,000 lb/h to 120,000 lb/h
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34. Learn to stablish relevant column internals in RadFrac
Pressure Profile
Temperature Profile
Molar Flow Rate Profile
Selecting between trays and packings
35. Acetone is to be absorbed into water from air mixture
Specs: 15 Stages, P = 1 atm, Isobaric
Feed Gas:
%Acetone = 2%; Air = 98%
F = 80 kmol/h, T = 25°C, P = 1 atm (101.3 kPa)
Solvent
%Water = 100%
F = 80 kmol/h, T = 25°C, P = 1 atm (101.3 kPa)
36. (A) Perform the Simulation of Absorption, verify Results
(B) Compare Sieve Trays vs. Bubble-Cap Trays
(C) Change Tray Spacing to verify results
(D) Change from Tray Columns to Packed Column, verify Results
37. Try to get:
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38. (A) Perform the Simulation of Absorption, verify Results
42. (B) Compare Sieve Trays vs. Bubble-Cap Trays
Now, continue to calculate the height and diameters:
Assume:
Trays
Sieves
Packed column:
Rashing Rings
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44. RUN an get:
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45. for:
Trays Bubble-Caps
Spacing = NA m recommended 0.855 diameter
46. (C) Change Tray Spacing to verify results
From 0.5m to 0.80 m
Verify Pressure drop, Column Diameter and
47. (C) Change Tray Spacing to verify results
From 0.5m to 0.20 m
Verify Pressure drop, Column Diameter and
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48. (C) Change Tray Spacing to verify results
If required, you could change the % flood approach
Typical values are between 70-80%
49. (D) Change from Tray Columns to Packed Column, verify Results
From trays Packing
Select RASHIG Rings
Metallic 25-mm
50. (D) Change from Tray Columns to Packed Column, verify Results
Select BETA-Rings
Metallic No. 2
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51. (D) Change from Tray Columns to Packed Column, verify Results
Select BETA-Rings
Metallic No. 2
52. Use RadFrac for rigurous distillation operations
Multiple / Binary Distillation
D:F, RR, DR effects
Number of Stages
Use Sensitivity Analysis
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https://www.youtube.com/watch?v=8P3vOOXbiF4
WKS
29
53. A 1:2 water-methanol mixture must be separated
The feed conditions are given as follows:
P = 18.4 psi, T = ? Unkown, X = saturated vapor, i.e. it is in its dew point
Water = 0.632 and Methanol = 0.368; asume mol Flow raltes
Since polar-polar interaction, use activity models such as NRTL / NRTL-RK
A series of analysis are to be run
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https://www.youtube.com/watch?v=8P3vOOXbiF4
WKS
29
54. (A) Run a RadFrac for this Distillation Column, optimize No. Stages, Feed, Recycle
Ratio and purities.
(B) Change Column Internals
(C) Perform Sensitivty Analysis on the column
S-1 : Vary Feed Stage (1-9); verify Purity of Distillate
S-2 : Vary Reflux Ratio (1.5-5); verify Purity of distillate
S-3 : Vary Operating Pressure (Stage 1 – Condenser P = (18.4-184); verify Purity of distillate
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https://www.youtube.com/watch?v=8P3vOOXbiF4
WKS
29
55. Try to get this:
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https://www.youtube.com/watch?v=8P3vOOXbiF4
WKS
29
57. Phys.Prop.Env.
Components water, metanol
Prop. Method NRTL-RK
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https://www.youtube.com/watch?v=8P3vOOXbiF4
WKS
29
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70. S-3 : Vary Operating Pressure (Stage 1 – Condenser P = (18.4-184); verify Purity of distillate
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72. Plant Economy & Dynamic Control
11. Ammonia Economics
12. Plant Dynamics & Control
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73. Setting up Utilities
Operating Costs Reports
Setting up Material Cost
Raw Material pricing
Optimization of profits
What if scenarios
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74. Ammonia is to be produced via the reaction of N2 and H2 using the Haber process.
There is no oxygen in the feed, only trace material such as methane, argon and
carbon monoxide. The reactor is isothermal, and has a 40% conversion based on the
inlet of nitrogen gas. The cryogenic mix is then cooled down to separate it. The gases,
mostly Nitrogen and Hydrogen gas are recycled, all other material purged and the
liquid product goes to the “Ammonia” product line.
Pressure is approx. 270 atm through all the system
Main focus is to produce 95%+ Ammonia product
Utilities are to be added, as well as some raw materials / products economics
Analysis is carried out in Europe and USA
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75. Prices in USA
Materials
Syngas = $0.26/kg
Product = $0.50/kg
Utilities
Electricity = $0.06/kWh
Cooling Water = $0.0251$/tonne -33.44 kJ/kk
Natural Gas = $5.8 / MMBTU $20.63 MBTU/lb
Prices in EU
Materials
Syngas = $0.32/kg
Product = $0.550/kg
Utilities
Electricity = $0.075/kWh
Cooling Water = $0.0301$/tonne 35.44 kJ/kk
Natural Gas = $5.2 / MMBTU $18.49 MBTU/lb
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76. (A) Create the plant
(B) Add Materials Costs & Utilities
(C) Compare USA vs. Europe Costings
(D) Sensitivity Analysis of Prices
(E) Verify the “Economic Analysis” and Economic Reports
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81. Unit Operations - RKT
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90. Add Utilities to each unit
Compressors electricity
Heaters Gas
Coolers Water
Isothermal Reactors Water for Exothermic, Gas for Endothermic
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91. RESULTS
$, k$, or MM (million $)
S, h, Day, Year
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92. RESULTS
$, k$, or MM (million $)
S, h, Day, Year
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95. www.ChemicalEngineeringGuy.com https://www.youtube.com/watch?v=ZPCGXMPtM_U
A distillation column of Benzene-Toluene mix (50-50% molar) is to be separated
The Pressure of the column is 1 bar, and has a 0.2 psi pressure dropper stage
Condition of the feed 500 mol/h, 25°C, 5bar
Valve 1 will adjust pressure to the 20th stage pressure, approx. P = 1.262bar
D = 250 mol/h approx., 99% purity required
Ppressure +6 bar extra
Pvalve pressure drop 3 bar
96. www.ChemicalEngineeringGuy.com https://www.youtube.com/watch?v=ZPCGXMPtM_U
The idea is to:
Create Aspen Plus – Simulation
Add the Dynamic Data Requirements
Export to Dynamics
(a) Verify the pressure Controller
(b) Add Flow-Controller to the feed
(c) Add Level-Controllers to the vessels in reflux/reboiler streams
(d) Add and tune a Temperature-Controller in the 34th stage - Reboiler
112. www.ChemicalEngineeringGuy.com
(a) Verify the pressure Controller
(b) Add Flow-Controller to the feed
(c) Add Level-Controllers to the vessels in reflux/reboiler streams
(d) Add and tune a Temperature-Controller in the 34th stage - Reboiler
116. Add Step Function
1) Normal run:
Step up + 1%
Verify time of stabilization
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117. Add Step Function
1) Normal run:
Step up + 1%
Verify time of stabilization
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118. Now change tuning
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From previous test:
119. www.ChemicalEngineeringGuy.com
(a) Verify the pressure Controller
(b) Add Flow-Controller to the feed
(c) Add Level-Controllers to the vessels in reflux/reboiler streams
(d) Add and tune a Temperature-Controller in the 34th stage - Reboiler
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120. www.ChemicalEngineeringGuy.com
Add a Flow Controller
Get info FROM:
Pre-Feed Stream
Send info TO
B1 (Flow controller)
STREAM(‘PRE-EED’)F , Total mole flow
121. www.ChemicalEngineeringGuy.com
Add a Flow Controller
Get info FROM:
Flow-Controller
Send TO
V1 (valve1)
STREAM(‘PRE-EED’)F , Total mole flow
122. www.ChemicalEngineeringGuy.com
(a) Verify the pressure Controller
(b) Add Flow-Controller to the feed
(c) Add Level-Controllers to the vessels in reflux/reboiler streams
(d) Add and tune a Temperature-Controller in the 34th stage - Reboiler
123. www.ChemicalEngineeringGuy.com
Add a Level Controller (BOTTOMS)
Get info FROM:
Level-Controller
Send TO
V3 (valve3)
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124. www.ChemicalEngineeringGuy.com
Add a Level Controller (Distillate)
Get info FROM:
Flow-Controller
Send TO
V2 (valve2)
STREAM(‘PRE-EED’)F , Total mole flow
125. www.ChemicalEngineeringGuy.com
Flow-Controller
If flow increases, valve must close to avoid
accumulation in tower
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128. www.ChemicalEngineeringGuy.com
(a) Verify the pressure Controller
(b) Add Flow-Controller to the feed
(c) Add Level-Controllers to the vessels in reflux/reboiler streams
(d) Add and tune a Temperature-Controller in the 34th stage - Reboiler
130. www.ChemicalEngineeringGuy.com
Add Temperature
Steup tuning
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132. 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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