HYSYS 8 8 - Manual

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AspenTech Incorporations 
Aspen Hysys V8.8 
Anees Ahmad
Typewriter
Cases Solved in Hysys Version 8.0 are same as Version 8.8
Anees Ahmad
Typewriter
 
 
 
 
 
 
 
 
 
 
Chemical Process Principles 
 
 
 
 
 
 
 
 
Matbal-001H Revised: Nov 7, 2012 
 1 
Cyclohexane Production with Aspen HYSYS® V8.0 
 Lesson Objectives 1.
 
 Construct an Aspen HYSYS flowsheet simulation of the production of cyclohexane via benzene 
hydrogenation 
 Become familiar with user interface and tools associated with Aspen HYSYS 
 Prerequisites 2.
 
 Aspen HYSYS V8.0 
 Knowledge of chemical process operations 
 Background/Problem 3.
 
Construct an Aspen HYSYS simulation to model the production of cyclohexane via benzene hydrogenation. The 
simplified flowsheet for this process is shown below. Fresh benzene and hydrogen feed streams are first fed 
through a heater to bring the streams up to reactor feed temperature and pressure conditions. This feed 
mixture is then sent to a fixed-bed catalytic reactor where 3 hydrogen molecules react with 1 benzene molecule 
to form cyclohexane. This simulation will use a conversion reactor block to model this reaction. The reactor 
effluent stream is then sent to a flash tank to separate the light and heavy components of the mixture. The 
vapor stream coming off the flash tank is recycled back to the feed mixture after a small purge stream is 
removed to prevent impurities from building up in the system. The majority of the liquid stream leaving the flash 
tank goes to a distillation column to purify the cyclohexane product, while a small portion of the liquid stream is 
recycled back to the feed mixture to minimize losses of benzene. Process operating specifications are listed on 
the following page. 
 
Matbal-001H Revised: Nov 7, 2012 
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Feed Streams 
Benzene Feed (BZFEED) Composition (mole fraction) 
Hydrogen - 
Nitrogen - 
Methane - 
Benzene 1 
Total Flow (lbmol/hr) 100 
Temperature (°F) 100 
Pressure (psia) 15 
 
Hydrogen Feed (H2FEED) 
Hydrogen 97.5 
Nitrogen 0.5 
Methane 2.0 
Benzene - 
Total Flow (lbmol/hr) 310 
Temperature (°F) 120 
Pressure (psia) 335 
 
Distillation Column 
Number of stages 15 
Feed stage 8 
Reflux Ratio 1.2 
Cyclohexane recovery 99.99 mole % in bottoms 
Condenser Pressure 200 psia 
Reboiler Pressure 210 psia 
 
Feed Preheater 
Outlet Temperature 300 °F 
Outlet Pressure 330 psia 
 
Reactor 
Stoichiometry Benzene + 3H2  Cyclohexane 
Conversion 99.8% of benzene 
Outlet temperature 400°F 
Pressure drop 15psi 
 
Flash Tank 
Temperature 120°F 
Pressure drop 5psi 
 
Purge Stream 
Purge rate is 8% of vapor recycle stream 
 
Liquid Split 
70% of liquid stream goes to distillation column 
 
 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
 
Matbal-001H Revised: Nov 7, 2012 
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 Aspen HYSYS Solution 4.
 
4.01. Start Aspen HYSYS V8.0, select New on the Start Page to start a new simulation. 
 
4.02. Create a component list. In the Component Lists folder, select the Add button to create a new HYSYS 
component list. 
 
 
 
4.03. Define components. Use the Find button to select the following components: Hydrogen, Nitrogen, 
Methane, Benzene, and Cyclohexane. 
 
 
4.04. Select a property package. In the Fluid Packages folder in the navigation pane click Add. Select SRK as 
the property package. 
 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.05. We must now specify the reaction involved in this process. Go to Reactions folder in the navigation 
pane and click Add to add a reaction set. 
 
 
 
4.06. In Reactions | Set-1 select Add Reaction. Select the Hysys radio button and select Conversion. Then 
click Add Reaction. Once a new reaction (Rxn-1) can be seen on the reaction set page, close the 
Reactions window shown below. 
 
 
 
4.07. Double click on Rxn-1 to define the reaction. In the reaction property window, add components 
Benzene, Hydrogen, and Cyclohexane to the Stoichiometry Info grid. Enter -1, -3, and 1, respectively, 
for stoichiometry coefficients. In the Basis grid select Benzene as Base Component, Overall for Rxn 
Phase, 99.8 for Co, and 0 for both C1 and C2. This indicates that the reaction will convert 99.8% of 
benzene regardless of temperature. Close this window when complete. 
 
Matbal-001H Revised: Nov 7, 2012 
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4.08. Attach this reaction set to a fluid package by clicking the Add to FP button. Select Basis-1 and click Add 
Set to Fluid Package. The reaction set should now be ready. 
 
 
 
4.09. We are now ready to enter the simulation environment. Click the Simulation button in the bottom left 
of the screen. 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.10. First we will place a Mixer and a Heater block onto the flowsheet. 
 
 
 
4.11. Double click on the mixer (MIX-100) to open the mixer property window. Create 2 inlet streams: 
H2FEED, BZFEED; and 1 outlet stream: ToPreHeat. 
 
Matbal-001H Revised: Nov 7, 2012 
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4.12. Go to the Worksheet tab to define streams H2FEED and BZFEED. First we will define the Conditions of 
each stream. For H2FEED, enter a Temperature of 120°F, a Pressure of 335 psia, and a Molar Flow of 
310 lbmole/hr. For BZFEED, enter a Temperature of 100°F, a Pressure of 15 psia, and a Molar Flow of 
100 lbmole/hr. Note that you can change the global unit set to Field if the units are different than those 
displayed below. 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.13. Next we will define the Composition of the two feed streams. In the Worksheet tab go to the 
Composition form. Enter the compositions shown below. You will notice that after inputting the 
composition, the mixer will successfully solve for all properties. 
 
 
 
 
4.14. Double click on the heater block (E-100) to configure the heater. Select stream ToPreHeat as the inlet 
and create an outlet stream called R-IN. Add an energy stream called PreHeatQ. 
 
Matbal-001H Revised: Nov 7, 2012 
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4.15. Go to the Worksheet tab and specify the outlet stream R-IN temperature and pressure. Enter 300°F for 
Temperature and 330 psia for Pressure. 
 
 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.16. The flowsheet should look like the following at this point. 
 
 
4.17. We will now add a Conversion Reactor to the flowsheet. Press F12 on the keyboard to open the 
UnitOps window. Select the Reactors radio button and select Conversion Reactor. Press Add. 
 
 
 
4.18. In the Conversion Reactor property window, select the inlet stream to be R-IN, and create a Liquid 
Outlet called LIQ and a Vapour Outlet called VAP. In the Parameters form, enter a Delta P of 15 psi. 
 
Matbal-001H Revised: Nov 7, 2012 
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Matbal-001H Revised: Nov 7, 2012 
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4.19. In the Reactions tab, select Set-1 for Reaction Set. Notice that when the reactor solves, the contents of 
the reactor are entirely in the vapor phase, therefore there is no liquid flow leaving the bottom of the 
reactor. 
 
 
 
 
 
 
 
 
 
 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.20. Next we will add a Cooler to the main flowsheet to cool down the vapor stream leaving the reactor. 
 
 
 
4.21. Double click on the cooler block (E-101) to open the cooler property window. Select VAP as the inlet 
stream and create an outlet stream called COOL. Also add an energy stream called COOLQ. In the 
Parameters form enter a Delta P of 5 psi. 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.22. Go to the Worksheet tab to specify the outlet stream temperature. Enter 120°F for the Temperature of 
stream COOL. The cooler will solve. 
 
 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.23. We will now add a Separator block to separate the vapor and liquid phases of streamCOOL. From the 
model palette add a Separator to the flowsheet. 
 
 
 
4.24. Double click on the separator block (V-100). Select COOL as the inlet stream and create liquid and vapor 
outlet streams called LIQ1 and VAP1. The separator should solve. 
 
Matbal-001H Revised: Nov 7, 2012 
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4.25. The flowsheet should now look like the following. 
 
 
 
4.26. We will now add 2 Tee blocks, 1 for each of the separator outlet streams. One tee will be used to purge 
a portion of the vapor stream to prevent impurities from building up in the system. The other tee will 
be used to recycle a portion of the liquid back to the mixer and the rest of the liquid will be fed to a 
distillation column. 
Matbal-001H Revised: Nov 7, 2012 
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4.27. Double click on the first Tee block (TEE-100). Select stream VAP1 as the inlet, and create 2 outlet 
streams VAPREC, and PURGE. 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.28. Go to the Parameters page and enter 0.08 for the Flow Ratio for stream PURGE. 
 
 
 
4.29. You can rotate the icon for a block by selecting the icon and clicking the Rotate button in the 
Flowsheet/Modify tab in the ribbon. 
 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.30. Double click the second Tee block (TEE-101). Select LIQ1 for the inlet stream and create 2 outlet 
streams LIQREC, and ToColumn. 
 
 
 
4.31. In the Parameters tab enter a Flow Ratio of 0.7 for stream ToColumn. 
Matbal-001H Revised: Nov 7, 2012 
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4.32. The flowsheet should now look like the following. 
 
 
(FAQ) Useful Option To Know: Saving Checkpoints 
 
Save “checkpoints” as you go. Once you have a working section of the flowsheet, save as a new 
file name, so you can revert to an earlier checkpoint if the current one becomes too complex to 
troubleshoot or convergence errors become persistent. 
 
Matbal-001H Revised: Nov 7, 2012 
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4.33. We are now ready to connect the recycle streams back to the mixer. On the main flowsheet, add 2 
Recycle blocks. 
 
 
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4.34. Double click on the first recycle block (RCY-1). Select stream VAPREC as the inlet stream and create an 
outlet stream called VAPToMixer. 
 
 
 
4.35. Double click the second recycle block (RCY-2). Select LIQREC as the inlet stream and create an outlet 
stream called LIQToMixer. 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.36. Connect the recycle streams back to the mixer. Double click the mixer block (MX-100). On the Design | 
Connections sheet add LIQToMixer and VAPToMixer as inlet streams. The flowsheet should converge. 
 
 
 
4.37. The flowsheet should now look like the following. 
 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.38. We are now ready to add the distillation column to the flowsheet. From the Model Palette add a 
Distillation Column Sub-Flowsheet. 
 
 
 
4.39. Double click on the Distillation Column Sub-flowsheet. This will launch the Distillation Column Input 
Expert. Enter 15 for # Stages and specify ToColumn as inlet stream on stage 8_Main TS. Select Full 
Reflux for Condenser, create an Ovhd Vapour Outlet stream called Off Gas, create Bottoms Liquid 
Outlet stream called Bot, and add a Condenser Energy Stream called Cond Q. When finished click Next. 
 
Matbal-001H Revised: Nov 7, 2012 
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4.40. On page 2 of the Distillation Column Input Expert keep the default selections for Reboiler Configuration 
and click Next. 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.41. On page 3 of the Distillation Column Input Expert enter a condenser pressure of 200 psia and a reboiler 
pressure of 210 psia. Click Next. 
 
 
 
4.42. On page 4 of the Distillation Column Input Expert leave fields for temperature estimates blank and click 
Next. On the final page of the column expert enter a molar Reflux Ratio of 1.2 and click Done to 
configure the column. 
 
Matbal-001H Revised: Nov 7, 2012 
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4.43. After completing the input for the column expert the Column property window will open. We want to 
create a design specification in order to ensure that 99.99% of the cyclohexane is recovered in the 
bottoms stream. Go to the Design | Specs sheet. Click Add and select Column Component Recovery. 
In the Comp Recovery window specify Stream for Target Type, Bot@COL1 for Draw, 0.9999 for Spec 
Value, and Cyclohexane for Components. Close this window when finished. 
 
 
Matbal-001H Revised: Nov 7, 2012 
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4.44. Go to the Specs Summary sheet and make sure that the only active specs are Reflux Ratio and Comp 
Recovery. The column should converge. 
 
 
 
 
 
4.45. The flowsheet is now complete and should look like the following. 
 
 
Matbal-001H Revised: Nov 7, 2012 
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This flowsheet is now complete. 
 Conclusion 5.
This is a simplified process simulation, however you should now have learned the basic skills to create and 
manipulate a steady state chemical process simulation in Aspen HYSYS V8.0. 
 Copyright 6.
 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Matbal-002H Revised: Nov 7, 2012 
 1 
Calculation of Gasoline Additives with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Learn how to specify a mixer 
 Learn how to use the spreadsheet in Aspen HYSYS to perform customized calculations 
2. Prerequisites 
 Aspen HYSYS V8.0 
3. Background 
Ethyl tert-butyl ether (ETBE) is an oxygenate that is added to gasoline to improve Research Octane Number 
(RON) and to increase oxygen content. The goal is to have 2.7% oxygen by weight in the final product. The legal 
limit is that ETBE cannot exceed more than 17% by volume. For simplicity, we use 2,2,4-trimethylpentane to 
represent gasoline. Since ETBE's molecular weight is 102.18 g/mol, the ETBE in the product stream can be 
calculated as following: 
 
 
 
 
 
 
 
This yields 17.243% of ETBE by weight in the product stream. Given this, the spreadsheet tool can be utilized to 
target the ETBE feed to achieve the desired oxygen content. 
In this tutorial we will calculate: 
 For a certain flow rate of gasoline (e.g., 100 kg/hr), how much ETBE should be added to achieve the 
oxygen content of 2.7% by weight in the blended gasoline. 
 Check whether or not the legal limit of ETBE content is satisfied. 
A HYSYS spreadsheet is used to perform calculations on each criterion. Both targets should be met in the 
simulation. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
Matbal-002H Revised: Nov 7, 2012 
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4. Aspen HYSYS Solution 
4.01. Start a new simulation in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component Lists folder select Add. Add 2,2,4-trimethylpentane and 
ETBE to the component list. 
 
 
4.03. Define property package. In the Fluid Packages folder select Add. Select Peng-Robinson as the 
property package. 
 
4.04. Enter the simulation environment by clickingthe Simulation button in the bottom left of the screen. 
 
4.05. Add a Mixer to the flowsheet from the Model Palette. 
Matbal-002H Revised: Nov 7, 2012 
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4.06. Double click on the mixer (MIX-100). Create two Inlets called ETBE and Gasoline. Create an Outlet 
called Blend. 
Matbal-002H Revised: Nov 7, 2012 
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4.07. Define feed streams. Go to the Worksheet tab. For stream ETBE enter a Temperature of 25°C and a 
Pressure of 1 bar. Leave Mass Flow empty as we will solve for it later. 
 
4.08. In the Composition form under the Worksheet tab, enter a Mole Fraction of 1 for ETBE in the ETBE feed 
stream. 
Matbal-002H Revised: Nov 7, 2012 
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4.09. Define gasoline feed stream. In the Conditions form in the Worksheet tab, enter a Temperature of 
25°C, a Pressure of 1 bar, and a Mass Flow of 82.76 kg/h. 
 
 
4.10. In the Composition form enter a Mole Fraction of 1 for 224-Mpentane in the Gasoline stream. The 
gasoline stream should solve. However. the mixer will not solve because the flow rate of ETBE is still 
unknown. 
 
 
Matbal-002H Revised: Nov 7, 2012 
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4.11. We will now create a spreadsheet to calculate the target mass flowrate of stream ETBE. Add a 
Spreadsheet to the flowsheet from the Model Palette. 
Matbal-002H Revised: Nov 7, 2012 
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4.12. Double click on the spreadsheet (SPRDSHT-1). Go to the Spreadsheet tab and enter the following text in 
cells A1 and A2. 
 
 
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4.13. Right click on cell B1 and select Import Variable. Select the following to import the Mass Flow of stream 
Gasoline to cell B1. Press OK when complete. 
 
 
4.14. Click cell B2 and enter the following formula: = (B1*0.17243) / (1-0.17243). This will calculate the mass 
flow rate for stream ETBE. From the background section, we know that in order to reach the oxygen 
content goal of 2.7%, we will need the gasoline stream to contain 17.243% ETBE by weight. 
Matbal-002H Revised: Nov 7, 2012 
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4.15. We now wish to export the calculated flow rate in cell B2 to stream ETBE. Right click cell B2 and select 
Export Formula Result. Make the following selections and click OK when complete. The mixer should 
now solve. 
 
Matbal-002H Revised: Nov 7, 2012 
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4.16. We will now calculate the volume percent of ETBE in the blended stream to make sure that the ETBE 
content is below the legal limit of 17 volume percent. This can easily be observed in the spreadsheet. In 
the spreadsheet, enter the following text in cell A4. 
 
4.17. Right click on cell B4 and select Import Variable. Make the following selections to import Master Comp 
Volume Frac of ETBE in the blended stream. Click OK when complete. 
Matbal-002H Revised: Nov 7, 2012 
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4.18. The volume fraction of ETBE in the blended stream is 0.1596, which is below the legal limit of 0.17. It is 
determined that the target flow rate of ETBE to be mixed with this gasoline stream is 17.24 kg/h. 
 
 
Matbal-002H Revised: Nov 7, 2012 
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5. Conclusions 
For a specified gasoline mass flow rate of 82.76 kg/hr, 17.24 kg/hr of ETBE is needed to achieve 2.7% oxygen 
content by weight in the final product. Furthermore, after blending, the product does not exceed the legal limit 
for ETBE of 17% by volume. If gasoline contains a single component, manual calculation should be easy without 
a simulator. However, real gasoline contains many unknown components and gasoline’s contents vary as 
feedstock or plant operation conditions change. Therefore, manual calculation becomes very difficult and the 
use of a simulator such as Aspen HYSYS can be helpful to carry out the calculation. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their re spective companies. 
 
 
 
 
 
 
 
 
 
 
Thermodynamics for Chemical Engineers
Prop-001H Revised: Nov 16, 2012 
 1 
Generate Ethylene Vapor Pressure Curves with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Generate vapor pressure curves for Ethylene 
2. Prerequisites 
 Aspen HYSYS V8.0 
 Introduction to vapor-liquid equilibrium 
3. Background 
Separation processes involving vapor-liquid equilibrium exploit volatility differences which are indicated by the 
components’ vapor pressure. Higher vapor pressure means a component is more volatile. 
Ethylene is an important monomer for polymers and there are many ethylene plants around the world. A vital 
step in ethylene production is separating it from other compounds and as a result the vapor pressure of 
ethylene is an important physical property for ethylene production. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Problem Statement and Aspen HYSYS Solution 
Problem Statement 
Determine the vapor pressure of ethylene at 5 °C, and its normal boiling point. Also create a plot of vapour 
pressure versus temperature. 
Aspen HYSYS Solution 
4.01. Create a new simulation in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component List folder select Add. Add Ethylene to the component list. 
Prop-001H Revised: Nov 16, 2012 
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4.03. Double click on Ethylene to view the pure component properties. Go to the Critical tab. Make a note 
that the Critical Temperature is 9.2°C and the Normal Boiling Point is -103.8°C. 
 
Prop-001H Revised: Nov 16, 2012 
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4.04. Define property methods. Go to the Fluid Packages folder and click Add. Select Peng-Robinson as the 
property package. 
 
 
4.05. Move to the simulation environment. Click the Simulation button in the bottom left of the screen. 
 
 
4.06. Add a Material Stream to the flowsheet. 
 
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4.07. Double click on material stream (1). The vapor pressure of liquid is the atmospheric pressure at which a 
pure liquid boils at a given temperature. The point at which the first drop of liquid begins to boil is 
called the bubble point, which is found in HYSYS by specifying a vapour fraction of 0. Therefore, we can 
find the vapor pressure of pure liquid by specifying a temperature and vapour fraction of 0. 
4.08. In material stream 1, enter a Vapour Fraction of 0, a Temperature of 5°C, and a Molar Flow of 1 
kgmole/h. In the Composition form under the Worksheet tab enter a Mole Fraction of 1 for Ethylene. 
 
4.09. You can see that the Pressure is 45.93 bar. This is equivalent to the vapour pressure of ethylene at this 
temperature. Next we would like to determine the normal boiling point of ethylene. Instead of 
specifying temperature, we will specify pressure. Empty the field for temperature and enter a value of 1 
bar for Pressure. 
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4.10. The newly calculated temperature is -104.3°C. This is the boiling temperature of ethylene at a pressure 
of 1 bar. 
4.11. Next we would like to create a plot of vapour pressure versus temperature. First, in the Material 
Stream 1 window, empty the field for Pressureand enter any Temperature (below critical temperature). 
This will allow us to vary temperature when we perform a case study. Go to the Case Studies folder in 
the Navigation Pane and click Add. 
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4.12. In Case Study 1, click Add to select the variables. Select the Temperature and Pressure of stream 1. In 
the Independent Variable field enter a Low Bound of -150°C, a High Bound of 0°C, and a Step Size of 
10°C. Click Run. 
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4.13. After running the case study, go to the Plots tab. Here you will see a plot of Pressure vs Temperature. 
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4.14. Note that by looking at the plot you can verify that at around -104°C the vapour pressure if 
approximately 1 bar, indicating the normal boiling point. 
5. Conclusions 
As we can see from the generated plot, ethylene is a very volatile component. At 5°C, its vapor pressure is 
about 45.93 bar. From this analysis, we also see that ethylene’s normal boiling point temperature is about –104 
°C. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Prop-003H Revised: Nov 5, 2012 
 1 
Retrieve Pure Component Property Data with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Learn how to retrieve property data for pure components in Aspen HYSYS. 
2. Prerequisites 
 Aspen HYSYS V8.0 
3. Background 
There are many reasons that we need physical properties of pure components. 
When we look for a solvent for extractive distillation (a technology that uses a third component, the solvent, to 
separate two components in a mixture that are difficult to separate directly via distillation), we look for 
components with normal boiling point temperatures that are higher (but not too much higher) than the 
components to be separated. For such a case, we need to know the normal boiling point temperatures of 
candidate solvents during the search. 
When we look for a solvent for extraction, we need to check the densities of candidate solvents to ensure the 
two liquid phases formed during extraction have enough differences in density. For the selected solvent, we 
also need to check its density against the existing liquid phase so that we know which liquid phase is heavier. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Problem Statement and Aspen HYSYS Solution 
Problem Statement 
The pre-condition of this example is that 3-methylhexane is now considered a promising candidate solvent for 
separation of acetone and water. The task is to determine whether the density of 3-methylhexane is different 
enough from the density of water. We also need to determine which of the two liquid phases formed mainly by 
these two components is heavier. 
Prop-003H Revised: Nov 5, 2012 
 2 
Aspen HYSYS Solution 
4.01. Create a new case in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component Lists folder select the Add button to add a new component 
list. 
 
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4.03. Enter 3-methylhexane in the Search for box. Aspen HYSYS should display the relevant search results. If 
the component you are looking for does not appear, you can also use the Filter or Search by drop-down 
list for different search criteria. Click the < Add button to add the component to the component list. 
 
 
 
Prop-003H Revised: Nov 5, 2012 
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4.04. To retrieve and view the pure component property data and, double-click the component 3-Mhexane. A 
new window should appear. 
 
4.05. Go to the Critical tab in the new window. You will see a list of property data in the Base Properties and 
Critical Properties frames. Note that the Ideal Liquid Density for 3-methylhexane is 690.2 kg/m3. 
Prop-003H Revised: Nov 5, 2012 
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4.06. In the navigation pane, go to the Components | Component List -1 sheet. Enter water in the Search for 
box and add the component to the component list. 
 
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4.07. Double-click on the component H2O. A new window should appear. 
 
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4.08. Go to the Critical tab in the new window. You will see a list of property data in the Base Properties and 
Critical Properties frames. Note that the Ideal Liquid Density for Water is 998.0 kg/m3. 
 
5. Conclusions 
The density of 3-methylhexane is around 690.2 kg/m3, which is clearly less than the density of water (998.0 
kg/m3). The liquid phase formed mainly by 3-methylhexane should be lighter than the phase formed mainly by 
water and, thus, the aqueous phase should be at the bottom and the other liquid phase should be at the top. 
Prop-003H Revised: Nov 5, 2012 
 8 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Prop-005H Revised: Nov 7, 2012 
 1 
Hypothetical Components and Petroleum Assays 
with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Create hypothetical components in Aspen HYSYS 
 Characterize a petroleum assay 
2. Prerequisites 
 Aspen HYSYS V8.0 
3. Background 
Aspen HYSYS allows you to create non-library or Hypothetical components. These hypothetical components can 
be pure components, defined mixtures, undefined mixtures, or solids. A wide selection of estimation methods 
are provided for various Hypo groups to ensure the best representation of behavior for the Hypothetical 
component in the simulation. 
In order to accurately model a process containing a crude oil, such as a refinery operation, the oil properties 
must be defined. It is nearly impossible to determine the exact composition of an oil assay, as there are far too 
many components in the mixture. This is a situation where hypothetical components are useful. Boiling point 
measurements of distillate fractions of an assay can be used to characterize the oil properties. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Problem Statement and Aspen HYSYS Solution 
Problem Statement 
Create a hypothetical componentgroup in Aspen HYSYS and characterize a petroleum assay to be used in a 
refinery simulation. 
Aspen HYSYS Solution 
4.01. Start a new simulation in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component Lists folder select Add. Change the Select field to 
Hypothetical and enter the Initial and Final Boiling Points for the hypothetical group shown below. 
Click Generate Hypos when complete. This will generate a group of hypothetical components with 
estimated properties based on the specified boiling point of each cut. 
Prop-005H Revised: Nov 7, 2012 
 2 
 
4.03. Click Add All to add the entire hypothetical group to the component list. 
Prop-005H Revised: Nov 7, 2012 
 3 
 
4.04. Define property package. In the Fluid Packages folder select Add. Select Peng-Robinson as the 
property package. 
 
4.05. Enter the simulation environment by clicking the Simulation button in the bottom left of the screen. 
Prop-005H Revised: Nov 7, 2012 
 4 
 
4.06. Add a Material Stream to the flowsheet from the Model Palette. Double click the stream and go to the 
Composition form under the Worksheet tab. 
 
4.07. You will notice that the mole fractions of all the components are empty. If you would like to assign an 
oil assay to this stream go to the Petroleum Assay form under the Worksheet tab. Select the option 
Create New Assay On Stream. 
Prop-005H Revised: Nov 7, 2012 
 5 
 
4.08. Click the Petroleum Assay Specifications button. This page allows you to enter assay distillation data or 
import data from a known oil assay. 
 
Prop-005H Revised: Nov 7, 2012 
 6 
4.09. Click the Import From button and select Assay Library to import data from a known assay in the HYSYS 
assay library. 
 
4.10. Say, for example, that we want to model a refinery process using Bachaquero heavy crude from 
Venezuela. Scroll down the list of assays and select Bachaquero, Venezuela. Click Import Selected 
Assay. 
 
Prop-005H Revised: Nov 7, 2012 
 7 
4.11. After a few moments the MacroCut Data window will be filled with distillation cut data for Bachaquero 
heavy crude. 
 
4.12. Click the Calculate Assay button to assign mole fractions to the hypothetical components defined for 
the stream. Exit the MacroCut Data window and view the Components form of the material stream. 
 
Prop-005H Revised: Nov 7, 2012 
 8 
4.13. The composition for the stream is now defined and will model the properties of the selected petroleum 
assay through the use of hypothetical components. 
5. Conclusions 
This example demonstrates how to create hypothetical components and how to assign a petroleum assay to a 
stream in order to model the assay properties in a simulation. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Thermo-002H Revised: Nov 6, 2012 
 1 
Flash Calculation in Aspen HYSYS® V8.0 
1. Lesson Objective 
 Learn how to model a Flash separator and examine different thermodynamic models to see how 
they compare. 
 Flash blocks in Aspen HYSYS 
2. Prerequisites 
 Aspen HYSYS V8.0 
3. Problem 
 
We want to investigate Vapor-Liquid separation at different pressures, temperatures and compositions. Assume 
you have a feed with an equimolar binary mixture of ethanol and benzene at 1 bar and 25°C. Examine the 
following flash conditions using the heater block in Aspen HYSYS. Use Vapor-Liquid as the Valid Phase in the 
computation. 
 Condition #1 (P-V Flash): At 1 bar and a vapor fraction of 0.5, find the equilibrium temperature and 
the heat duty. 
 Condition #2 (T-P Flash): At the temperature determined from Condition #1 and a pressure of 1 bar, 
verify that the flash model results in a vapor fraction of 0.5 at equilibrium. 
 Condition #3 (T-V Flash): At the temperature of Condition #1, and a vapor fraction of 0.5, verify that 
the flash model results in an equilibrium pressure of 1 bar. 
 Condition #4 (P-Q Flash): At 1 bar and with the heat duty determined from Condition #1, verify that 
the temperature and vapor fraction are consistent with previous conditions. 
 Condition #5 (T-Q Flash): At the temperature and heat duty determined from Condition #1, verify 
that the pressure and vapor fraction are consistent with previous conditions. 
 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
 
4. Aspen HYSYS Solution: 
4.01. Start Aspen HYSYS V8.0. Select New to start a new simulation. 
 
4.02. Create a component list. In the Component Lists folder select Add. Select Ethanol and Benzene. 
 
Thermo-002H Revised: Nov 6, 2012 
 2 
 
 
4.03. Create a fluid package. In the Fluid Packages folder select Add, and select NRTL as the property package. 
 
4.04. Go to the simulation environment. Click the Simulation button in the bottom left of the screen. 
 
4.05. Place a Heater block onto the flowsheet from the Model Palette. 
 
 
 
Thermo-002H Revised: Nov 6, 2012 
 3 
4.06. Double click the Heater to open the property window. Create an Inlet stream called FEED, an Outlet 
stream called OUT, and an Energy stream called Q. 
 
 
 
4.07. Specify conditions of FEED stream. Go to the Worksheet tab and enter a Temperature of 25°C, a 
Pressure of 1 bar (100 kPa), and a Molar flow of 1 kgmole/h. Also enter Mole Fractions of 0.5 for each 
component on the Composition form. 
 
 
 
Thermo-002H Revised: Nov 6, 2012 
 4 
4.08. Condition #1 Compute the temperature to get 0.5 vapor fraction at 1 bar. In the Conditions form under 
Worksheet, enter a Vapour Fraction of 0.5 and a Pressure of 1 bar (100 kPa) for stream OUT. The 
heater will automatically solve and you will see that the calculated temperature is 67.03°C. 
 
 
 
4.09. Condition #2 Compute vapor fraction at 1 bar and at the temperature obtained in Condition #1. Clear 
the field for Vapour Fraction for stream OUT, then enter a Pressure of 1 bar (100 kPa) and a 
Temperature of 67.03°C. In order to be able to enter a temperature, you must first empty the entry 
field for Vapour Fraction. This is done by clicking the entry field and pressing delete on the keyboard. 
Once a Temperature is entered, the Vapour Fraction will solve. 
 
Thermo-002H Revised: Nov 6, 2012 
 5 
 
 
4.10. Condition #3 Compute pressure at the temperature obtained in Condition #1 with 0.5 vapor fraction. 
Delete the value in the Pressure field and enter a Vapour Fraction of 0.5. The pressure should solve. 
 
Thermo-002H Revised: Nov 6, 2012 
 6 
 
4.11. Condition #4 Compute temperature and vapor fraction at 1 bar and using the heat duty obtained in 
Condition #1. Empty the fields for Temperature and Vapour Fraction in stream OUT. In stream OUT 
enter a Pressure of 1 bar. In stream Q, enter a Heat Flow of 2.363e004 kJ/h. The Temperature of 
67.03°C and Vapour Fraction of .500 are consistent with Condition #1. 
 
 
4.12. Condition #5 Compute pressure and vapor fraction at the temperature and heat duty obtained in 
Condition #1.In stream OUT, empty the field for Pressure. Enter a Temperature of 67.03°C. The 
Pressure and Vapor Fraction should be the same as Condition #1. 
Thermo-002H Revised: Nov 6, 2012 
 7 
 
5. Conclusion 
 
You have gone through the five flash methods which are most common in Aspen HYSYS. Here is a brief 
summary. 
 Flash Method T (C) P (bar) V (-) Q (MJ/hr) 
 P-V Flash 67.03 1 0.5 23.63 
 T-P Flash 67.03 1 0.5099 23.98 
 T-V Flash 67.03 1 0.5 23.63 
 P-Q Flash (or P-H) 67.03 1 0.5 23.63 
 T-Q Flash (or T-H) 67.03 1 0.5 23.63 
 
Specified Computed 
 
Feed Condition: ETHANOL/BEZENE (Equimolar mixture) at 1 bar and 25 Celsius. 
 
Thermo-002H Revised: Nov 6, 2012 
 8 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
 
Thermo-003H Revised: Nov 6, 2012 
 1 
Steam Tables in Aspen HYSYS® V8.0 
1. Objective 
 Learn how to access Steam Tables in Aspen HYSYS, and how to interpret the Steam Table data. 
2. Prerequisites 
 Aspen HYSYS V8.0 
3. Background 
Aspen HYSYS offers 2 types of Steam Tables Properties Methods: 
Property Method Name Models (Steam 
Tables) 
Note 
ASME Steam ASME 1967 
The ASME Steam property method uses the: 
 1967 International Association for 
Properties of Water and Steam (IAPWS, 
http://www.iapws.org) correlations for 
thermodynamic properties 
 
STEAM-TA method is made up of different 
correlations covering different regions of the P-T 
space. These correlations do not provide 
continuity at the boundaries, which can lead to 
convergence problems and predict wrong trends. 
NBS Steam NBS 1984 
The NBS Steam property methods uses the: 
 1984 International Association for 
Properties of Water and Steam (IAPWS, 
http://www.iapws.org) correlations for 
thermodynamic properties 
 
Use the NBS Steam property method for pure 
water and steam with temperature ranges of 
273.15 K to 2000 K. The maximum pressure is 
over 10000 bar. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
http://www.iapws.org/
http://www.iapws.org/
Thermo-003H Revised: Nov 6, 2012 
 2 
4. Problem 
Using Aspen HYSYS, we want to calculate saturated steam properties from 100°C to 300°C. We would like to 
create a table that displays mass enthalpy, mass entropy, pressure, and density. 
Aspen HYSYS Solution: 
4.01. Start Aspen HYSYS V8.0. Select New to start a new simulation. 
 
4.02. Create a component list. In the Component Lists folder, select Add. Add Water to the component list. 
 
 
 
 
4.03. Create a fluid package. In the Fluid Packages folder, select Add. Select NBS Steam as the property 
package. 
 
4.04. Go to the simulation environment. 
 
 
 
Thermo-003H Revised: Nov 6, 2012 
 3 
4.05. Add a material stream to the flowsheet from the Model Palette. Double click on the stream to open the 
property window. Rename this stream STEAM and enter a Mole Fraction of 1 for water. 
 
 
 
4.06. In the navigation pane, go to Stream Analysis and click on the dropdown arrow next to Add and select 
Property Table. In the Select Process Stream window that appears, select STEAM and press OK. 
 
 
 
4.07. Next, double click on Property Table-1 to open the property window. Under Independent Variables 
select Temperature as Variable 1. Enter a Lower Bound of 100°C and an Upper Bound of 300°C. Enter 
100 for # of Increments. Select Vapour Fraction for Variable 2 and select State for Mode. Enter a value 
of 1 for State Values. We are going to be varying the temperature while holding the vapour fraction 
constant at 1. 
 
Thermo-003H Revised: Nov 6, 2012 
 4 
 
 
4.08. We must now define the dependent properties that we are interested in viewing results for. Go to the 
Dep. Prop form under the Design tab. Select Add. Here we will add Mass Enthalpy, Mass Entropy, 
Pressure, and Mass Density. 
 
Thermo-003H Revised: Nov 6, 2012 
 5 
 
 
4.09. Click Calculate to generate the property table. Results can be viewed in the Performance tab of the 
property table window. 
 
Thermo-003H Revised: Nov 6, 2012 
 6 
 
 
5. Conclusion 
After completing this exercise you should now be familiar with how to access and interpret thermodynamic 
properties for steam using Aspen HYSYS. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Thermo-004H Revised: Nov 6, 2012 
 1 
Heat of Vaporization with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Learn how to calculate heat of vaporization using the heater block in Aspen HYSYS 
 Understand the impact of heat of vaporization on distillation 
2. Prerequisites 
 Aspen HYSYS V8.0 
3. Background 
The driving force for distillation is energy. The most energy consuming part of a distillation column is the 
vaporization of material in the reboiler to cause vapor to flow from the bottom of the column to the top of the 
column. Heat of vaporization determines the amount of energy required. Therefore, it is important to know the 
heat of vaporization of various species during solvent selection. With everything else equal, we should select a 
component with lower heat of vaporization so that we can achieve the same degree of separation with less 
energy. This example contains three isolated heater blocks. Each heater block is used to calculate the heat of 
vaporization for a pure component. 
 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
Thermo-004H Revised: Nov 6, 2012 
 2 
4. Aspen HYSYS Solution: 
4.01. Create a new simulation in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component Lists folder, select Add. Select Water, 3-methylhexane, 
and 1,1,2-trichloroethane. 
 
4.03. Create a fluid package. In the Fluid Packages folder, select Add. Select UNIQUAC as the property 
package and select RK as the Vapour Model. 
 
 
4.04. Enter the simulation environment. 
 
 
Thermo-004H Revised: Nov 6, 2012 
 3 
4.05. Add three separate Heater blocks to the flowsheet. 
 
4.06. Double click on E-100 to open the property window.This first heater will vaporize a stream of pure 
water. Create an Inlet stream called Feed-Water, an Outlet stream called Water-Out, and an Energy 
stream called Q-Water. 
 
Thermo-004H Revised: Nov 6, 2012 
 4 
4.07. Go to the Worksheet tab. Specify the feed stream to be at a Pressure of 100 kPa, a Vapour Fraction of 
0, and with a Molar Flow of 1 kgmole/h. In the Composition form under the Worksheet tab, enter a 
Mole Fraction of 1 for Water in the feed stream. Lastly, we must specify the outlet pressure and the 
outlet vapour fraction. Enter 100 kPa for Pressure, and 1 for Vapour Fraction of the Water-Out stream. 
The heater should solve. Make note of the Heat Flow of the energy stream Q-Water. 
 
4.08. We will now repeat this process for heaters E-101 and E-102. E-101 will vaporize 3-methylhexane and E-
102 will vaporize 1,1,2-trichloroethane. 
4.09. Double click on E-101. Create an Inlet stream called Feed-3MH, an Outlet stream called 3MH-Out, and 
an Energy stream called Q-3MH. 
Thermo-004H Revised: Nov 6, 2012 
 5 
 
4.10. In the Worksheet tab, for the feed stream enter a Vapour Fraction of 0, a Molar Flow of 1 kgmole/h, 
and a Pressure of 100 kPa. In the Composition form, enter a Mole Fraction of 1 for 3-methylhexane in 
the feed stream. Lastly specify the outlet conditions of 100 kPa for Pressure and a Vapour Fraction of 1. 
Make note of the Heat Flow for the energy stream. 
 
 
 
Thermo-004H Revised: Nov 6, 2012 
 6 
4.11. Double click E-102. Create an Inlet stream called Feed-1,1,2, an Outlet stream called 1,1,2-Out, and an 
Energy stream called Q-1,1,2. 
 
4.12. In the Worksheet tab, for the feed stream enter a Vapour Fraction of 0, a Molar Flow of 1 kgmole/h, 
and a Pressure of 100 kPa. In the Composition form, enter a Mole Fraction of 1 for 1,1,2-
trichloroethane in the feed stream. Lastly specify the outlet conditions of 100 kPa for Pressure and a 
Vapour Fraction of 1. Note the Heat Flow of the energy stream. 
 
 
Thermo-004H Revised: Nov 6, 2012 
 7 
5. Conclusions 
Although water has small molecular weight, its heat of vaporization is large. Heat of vaporization for water is 
about 18% higher than that of 1,1,2-trichloroethane and about 30% higher than that of 3-methylhexane. Of the 
three options, 3-methylhexane has to lowest heat of vaporization and would require the least amount of energy 
as a solvent in a distillation. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Therm-005H Revised: Nov 6, 2012 
 1 
Simulation of Steam Engine with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Learn how to simulate a steam engine with Aspen HYSYS 
 Learn how to specify pumps, heaters, coolers, expanders 
2. Prerequisites 
 Aspen HYSYS V8.0 
 Introductory thermodynamics 
3. Background 
A steam engine consists of the following steps: 
 Water is pumped into a boiler using a pump. 
 Water is vaporized in a boiler and becomes high temperature and pressure steam. 
 Steam flows through a turbine and does work. The pressure and temperature go down during this 
step. The steam is also partially condensed. 
 The steam is further cooled to be condensed completely. Then, it is fed to the pump mentioned in 
the first step to be re-used. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Aspen HYSYS Solution 
4.01. Create a new simulation in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component Lists folder, select Add. Add Water to the component list. 
 
Therm-005H Revised: Nov 6, 2012 
 2 
4.03. Create a fluid package. In the Fluid Packages folder, select Add. Select NBS Steam as the property 
package. 
 
4.04. Go to the simulation environment by clicking the Simulation button in the bottom left of the screen. In 
the Home ribbon, select EuroSI as the Unit Set. 
 
4.05. Enter the simulation environment. Add a Heater, a Cooler, a Pump and an Expander as shown in the 
flowsheet. 
 
Therm-005H Revised: Nov 6, 2012 
 3 
 
4.06. Double click the pump (P-100) to open the pump specification window. Create an Inlet stream called 
Liq-Water, an Outlet stream called ToBoiler, and an Energy stream called Q-Pump. 
 
4.07. In the Worksheet tab, specify an outlet Pressure of 1.2 bar. 
 
Therm-005H Revised: Nov 6, 2012 
 4 
 
4.08. Double click the heater (E-100). Select ToBoiler as the Inlet stream, create an Outlet stream called 
HPSteam (high pressure steam), and create an Energy stream called Q-Heat. 
 
 
4.09. In the Worksheet tab, specify an outlet Pressure of 40 bar, and a Temperature of 460°C. 
Therm-005H Revised: Nov 6, 2012 
 5 
 
 
4.10. Double click the expander (K-100). Select HPSteam as the Inlet stream, create an Outlet stream called 
LPSteam, and create an Energy stream called Q-Expand. 
Therm-005H Revised: Nov 6, 2012 
 6 
 
4.11. In the Worksheet tab, specify an outlet Pressure of 1 bar. 
 
Therm-005H Revised: Nov 6, 2012 
 7 
 
4.12. Double click the cooler (E-101). Select an Inlet stream of LPSteam, an Outlet stream of Liq-Water, and 
create an Energy stream called Q-Cool. 
 
 
Therm-005H Revised: Nov 6, 2012 
 8 
4.13. In the Worksheet tab, specify an outlet Vapour Fraction of 0 and a Pressure of 1 bar. 
 
 
4.14. The flowsheet is now ready to solve. All that is left to do is to specify the composition and flowrate of a 
stream within the loop. Double click on stream Liq-Water and specify a Mole Fraction of 1 for Water 
and a Mass Flow if 10,000 kg/h. 
Therm-005H Revised: Nov 6, 2012 
 9 
 
 
 
Therm-005H Revised: Nov 6, 2012 
 10 
4.15. The flowsheet should now solve. 
 
5. Conclusions 
The steam engine system can be simulated using Aspen HYSYS. This flowsheet clearly shows where energy is 
being input to the system and where energy is being released. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Thermo-006H Revised: Nov 6, 2012 
 1 
Illustration of Refrigeration with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Learn how to specify compressors, heaters, and valves in Aspen HYSYS 
 Understanda refrigeration loop 
2. Prerequisites 
 Aspen HYSYS V8.0 
 Introductory thermodynamics 
3. Background 
In a typical refrigeration system, the refrigerant starts at room temperature and ambient pressure. It is 
compressed, which increases the refrigerant’s temperature and pressure so it is a superheated vapor. The 
refrigerant is cooled by air with a fan so that it is close to room temperature. At this point, its pressure remains 
high and the refrigerant has been condensed to a liquid. Then, the refrigerant is allowed to expand through an 
expansion valve. Its pressure decreases abruptly, causing flash evaporation, which reduces the refrigerant’s 
temperature significantly. The very cold refrigerant can then cool a fluid passed across a heat exchanger (e.g., 
air in an air conditioner). Of course, for an AC unit to work, the air that is used to cool down the super-heated 
refrigerant must be air outside of the room; the air that is cooled by the cold refrigerant is the air inside the 
room. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Aspen HYSYS Solution 
Problem Statement 
Determine the cooling capacity of 300 kgmole/h of CFH2-CF3 when allowed to expand from 10 bar to 1 bar. 
Thermo-006H Revised: Nov 6, 2012 
 2 
Aspen HYSYS Solution 
4.01. Create a new simulation in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component Lists folder select Add. Add 1,1,1,2-tetrafluoroethane to 
the component list. 
 
4.03. Create a fluid package. In the Fluid Packages folder, select Add. Select NRTL as the property package. 
 
4.04. Move to the simulation environment. Click the Simulation button in the bottom left of the screen. In 
the Home ribbon, select EuroSi as the Unit Set. 
 
4.05. Add a Compressor, a Cooler, a Heater, and a Valve to the main flowsheet. 
Thermo-006H Revised: Nov 6, 2012 
 3 
 
4.06. Double click on the compressor (K-100). Create an Inlet stream called Vapor, an Outlet stream called 
SuperHeat-Vapor, and an Energy stream called Q-Comp. 
Thermo-006H Revised: Nov 6, 2012 
 4 
 
4.07. In the Worksheet tab, specify an outlet Pressure of 10 bar. 
 
Thermo-006H Revised: Nov 6, 2012 
 5 
 
4.08. Double click the Cooler (E-100). Select SuperHeat-Vapor as the Inlet stream, create an Outlet stream 
called Liquid, and create an Energy stream called Q-Cool. 
 
4.09. In the Worksheet tab, specify an outlet Temperature of 30°C. In the Parameters form under the Design 
tab, enter a Delta P of 0. 
Thermo-006H Revised: Nov 6, 2012 
 6 
 
 
4.10. Double click the valve (VLV-100). Select stream Liquid as the Inlet stream and create an Outlet stream 
called LowP. 
Thermo-006H Revised: Nov 6, 2012 
 7 
 
4.11. In the Worksheet tab specify an outlet Pressure of 1 bar. 
 
Thermo-006H Revised: Nov 6, 2012 
 8 
 
4.12. Double click on the heater (E-101). Select stream LowP as the Inlet stream, select stream Vapor as the 
Outlet stream, and create an Energy stream called Q-Heat. 
 
4.13. In the Worksheet tab, specify an outlet Temperature of 25°C. In the Parameters form under the Design 
tab, specify a Delta P of 0. 
Thermo-006H Revised: Nov 6, 2012 
 9 
 
 
We must now specify the molar flowrate and composition of the refrigerant. Double click any stream, 
for example stream Liquid. Enter a Molar Flow of 300 kgmole/h. In the Composition form specify a 
Mole Fraction of 1 for the refrigerant. 
Thermo-006H Revised: Nov 6, 2012 
 10 
 
4.14. The flowsheet will now solve. 
 
Thermo-006H Revised: Nov 6, 2012 
 11 
4.15. Check results. To view the cooling capacity of this refrigeration loop, double click energy stream Q-Heat. 
The stream is removing 1.26e006 kcal/h, or approximately 350 kcal/sec. 
 
 
5. Conclusions 
Refrigeration is a process where heat moves from a colder location to a hotter one using external work (e.g., a 
compressor). We know that vaporization of a liquid takes heat. If there is no external heat available, the heat 
will come from the liquid itself by reducing its own temperature. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Thermo-007H Revised: Nov 6, 2012 
 1 
Maximum Fill up in Propane Tanks with Aspen HYSYS® V8.0 
Using a Spreadsheet 
1. Lesson Objectives 
 How to calculate the maximum liquid level in propane tanks 
 How to access stream variables in Aspen HYSYS 
 How to configure a heater block 
 How to use the Spreadsheet tool to perform customized calculations 
2. Prerequisites 
 Aspen HYSYS V8.0 
3. Background 
When a propane tank is filled at 25°C, we need to leave enough volume for liquid propane expansion due to an 
increase in temperature. The hottest weather ever recorded is about 58°C. In real life practices, propane tanks 
are only filled up to 80-85% of the tank volume. Why? We know that propane expands when it is heated up. 
However, why 80-85%? 
We can answer this question by using a simple flash calculation in Aspen HYSYS. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Problem Statement and Aspen HYSYS Solution 
Problem Statement 
Propane tanks are filled at 25°C with liquefied propane. These tanks will be stored and used in an environment 
at 1 bar and ambient temperature. How much, in terms of volume %, can each tank be filled up to? 
Thermo-007H Revised: Nov 6, 2012 
 2 
Aspen HYSYS Solution 
4.01. Create a new simulation in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component Lists folder select Add. Add Propane to the component list. 
 
4.03. Create a fluid package. In the Fluid Packagers folder, select Add. Select Peng-Robinson as the property 
package. 
 
 
4.04. Go to the simulation environment. Click the Simulation button in the bottom left of the screen. 
 
4.05. Add a Heater to the flowsheet. 
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4.06. Double click on the heater (E-100). Create an Inlet stream, an Outlet stream, and an Energy stream, 
named 1, 2, and Q, respectively. 
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4.07. Define feed stream. Go to the Worksheet tab. For the feed stream, enter a Vapour Fraction of 1, a 
Temperature of 25°C, and a Molar Flow of 1 kgmole/h. In the Composition form, enter 1 for Mole 
Fraction of propane. 
 
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4.08. Specify outlet conditions. For the outlet stream, enter a Vapour Fraction of 0, and a Temperature of 
58°C. The heater should solve. 
 
 
4.09. Add a Spreadsheet to the flowsheet to calculate the maximum percent to fill the propane tank to allow 
for expansion when heated. 
Thermo-007H Revised: Nov 6, 2012 
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4.10. Double click the spreadsheet (SPRDSHT-1). Go to the Spreadsheet tab and enter the following in cells 
A1, A2, and A3. 
 
 
Thermo-007H Revised: Nov 6, 2012 
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4.11.Now we will link flowsheet variables to the spreadsheet. Right click on cell B1 and select Import 
Variable. Make the following selections to import the Molar Density of stream 1. Click OK when 
complete. 
 
 
4.12. Right click on cell B2 and select Import Variable to import the Molar Density of stream 2. Make the 
following selections and click OK. 
 
Thermo-007H Revised: Nov 6, 2012 
 8 
4.13. The spreadsheet should now look like the following. 
 
4.14. Next, click cell B3 and enter “=(B2/B1)*100”. This divides the molar density at 58°C by the molar density 
at 25°C. The resulting number is the percentage that a propane tank should be filled at 25°C to allow for 
thermal expansion up to a temperature of 58°C. 
 
 
4.15. The maximum fill % of propane at 25°C is 87.86%, as seen in the spreadsheet. 
 
Thermo-007H Revised: Nov 6, 2012 
 9 
5. Conclusions 
The calculation shows that the maximum fill up is 87.8% if the ambient temperature doesn’t exceed 58 °C. To 
accommodate special cases, typically, propane tanks are filled up to 80-85%. After completing this exercise you 
should be familiar with how to create a spreadsheet to perform custom calculations. 
It is important to note that, in real life, the content in a filled propane tank is typically a mixture instead of pure 
propane. In addition to propane, the mixture also has a few other light components such as methane and 
ethane. Therefore, to carry out calculations for a real project, we need to know the compositions of the mixture 
we are dealing with. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Thermo-013H Revised: Nov 7, 2012 
 1 
Generate PT Envelope with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Learn how to generate PT envelopes in Aspen HYSYS 
2. Prerequisites 
 Aspen HSYSY V8.0 
3. Background 
It is very important to know the phase conditions of a mixture at a given temperature and pressure. For 
example, the phase conditions of a fluid in a heat exchanger have an impact on the heat transfer rate. 
Formation of bubbles (vapor phase) in inlet streams can also be very damaging to pumps. The phase conditions 
of a fluid in a pipe can impact pipeline calculations. 
The PT envelope for a given mixture provides a complete picture of phase conditions for a given mixture. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Aspen HYSYS Solution 
4.01. Start Aspen HYSYS V8.0 and start a new simulation. 
4.02. Create a component list. In the Component Lists folder select Add. Add Ethane and n-Pentane to the 
component list. 
 
Thermo-013H Revised: Nov 7, 2012 
 2 
4.03. Define property package. In the Fluid Packages folder select Add. Select Peng-Robinson as the 
property package. 
 
4.04. Go to the simulation environment by clicking the Simulation button in the bottom left of the screen. 
 
4.05. Add a Material Stream to the flowsheet. To create a PT Envelope we must perform a Stream Analysis, 
and in order to perform a Stream Analysis we need a material stream. 
 
 
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 3 
4.06. Double click the material stream (1). Enter a Molar Flow of 100 kg/h. In the Composition form enter 
Mass Fractions of 0.5 for each component. 
 
 
 
4.07. Right click on the stream and select Create Stream Analysis | Envelope. 
Thermo-013H Revised: Nov 7, 2012 
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4.08. In the Envelope window, go to the Performance tab. Here you will see a PT Envelope. Note that you 
can change the Envelope type using the radio buttons in the bottom right corner of the window. On the 
graph, the blue line represents the dew point and the red line represents the bubble point. The area 
between the lines represents the 2-phase region. 
Thermo-013H Revised: Nov 7, 2012 
 5 
 
5. Conclusions 
With the PT envelope of a mixture, we can determine its phase conditions for a given temperature and pressure. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied with or for use with, 
this work. This work and its contents are provided for educational purposes only. 
 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Thermo-014H Revised: Nov 7, 2012 
 1 
Retrograde Behavior Illustrated with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Observe retrograde behavior 
2. Prerequisites 
 Aspen HYSYS V8.0 
 Completion of teaching module Thermo-013 
3. Background 
For a mixture, the amount of liquid (liquid fraction) increases as pressure increases at constant temperature. 
However, in the retrograde region near the critical region, we may see some interesting behavior—vapor 
fraction increases as pressure increases (at constant temperature). 
Many mixtures have retrograde behavior near the critical region. In this example, we will examine the 
retrograde behavior using a binary mixture of ethane and pentane. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Problem Statement and Aspen HYSYS Solution 
Problem Statement 
Retrograde behavior can be observed in the mixture of ethane and pentane. In Aspen HYSYS, use PT Envelope to 
determine the critical region of the mixture. Then, use a Property Table to examine the retrograde behavior near 
the critical region. 
Thermo-014H Revised: Nov 7, 2012 
 2 
Aspen HYSYS Solution 
4.01. Open the file titled Thermo-14H_Retrograde_Behavrior_Start.hsc. This is identical to the file that was 
created in lesson Thermo-013H_PT_Envelope. 
4.02. In the PT Envelope that appears in the Performance tab of the Envelope window, notice that there is a 
region near the critical point where the vapor fraction will increase as pressure increases while 
temperature is held constant. 
 
 
Thermo-014H Revised: Nov 7, 2012 
 3 
4.03. We can demonstrate this behavior by creating a property table in HYSYS. In the Stream Analysis folder 
in the Navigation Pane, click the dropdown arrow next to Add and select Property Table. Select stream 
1 and click OK. 
 
 
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 4 
4.04. Double click Property Table-1. Select Temperature for Variable 1 and select State for Mode. Enter a 
State value of 115°C. SelectPressure for Variable 2 and Incremental for Mode. Enter a Lower Bound 
of 60 bar, an Upper Bound of 69 bar, and a # of Increments of 20. 
 
 
4.05. In the Dep. Prop form under the Design tab click Add. Select Vapour Fraction and click OK. 
 
 
Thermo-014H Revised: Nov 7, 2012 
 5 
4.06. Click Calculate. Once complete, go to the Performance tab. Here you can view the results in either table 
or plot form. Go to Plots and select View Plot. 
 
 
4.07. From the plot you can clearly see the region where increasing the pressure will cause the vapour 
fraction to increase. 
5. Conclusions 
For the binary mixture of ethane and pentane (50% each on mass basis), we observed that vapor fraction 
increases from 0.701457 to 1 as pressure increases from 65.22 bar to 66.78 bar, which is a retrograde behavior. 
This retrograde behavior can be a source of multiple solutions to process simulation. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
Thermo-014H Revised: Nov 7, 2012 
 6 
liable to you for damages, including any loss of profits, lost savings, or other incidental or consequential 
damages arising out of the use of the information contained in, or the digital files supplied w ith or for use with, 
this work. This work and its contents are provided for educational purposes only. 
AspenTech®, aspenONE®, and the Aspen leaf logo, are trademarks of Aspen Technology, Inc.. Brands and 
product names mentioned in this documentation are trademarks or service marks of their respective companies. 
Thermo-019H Revised: Nov 7, 2012 
 1 
Remove Hydrogen from Methane, Ethylene and Ethane 
with Aspen HYSYS® V8.0 
1. Lesson Objectives 
 Learn how to remove bulk of hydrogen using a cooler and a vapor liquid separator 
 Learn how to use adjust block and spreadsheets 
2. Prerequisites 
 Aspen HYSYS V8.0 
 Introduction to vapor-liquid equilibrium 
3. Background 
In an ethylene plant, we have a feed stream containing hydrogen, methane, ethylene, and ethane . Before this 
stream can be fed to the demethanizer, hydrogen must be removed so the volumetric flow is less, which 
decreases the required size for the demethanizer column. Because hydrogen has a much higher vapor pressure 
than the other components, one or more flash drums can be used for hydrogen removal. 
The examples presented are solely intended to illustrate specific concepts and principles. They may not 
reflect an industrial application or real situation. 
4. Problem Statement and Aspen HYSYS Solution 
Problem Statement 
The feed stream is a combination of 6,306 lb/hr of hydrogen, 29,458 lb/hr of methane, 26,049 lb/hr of ethylene, 
and 5,671 lb/hr of ethane. The mole fraction of hydrogen in the feed stream is greater than 0.51, indicating a 
large volume of hydrogen in the feed stream. There are two goals for this section of the process: 
 After bulk of hydrogen is removed, the stream contains less than 0.02 mole fraction of hydrogen 
 Loss of ethylene to the hydrogen stream should be less than 1% 
Thermo-019H Revised: Nov 7, 2012 
 2 
Aspen HYSYS Solution 
4.01. Create a new simulation in Aspen HYSYS V8.0. 
4.02. Create a component list. In the Component Lists folder select Add. Add Hydrogen, Methane, Ethylene, 
and Ethane to the component list. 
 
4.03. Define property package. In the Fluid Packages folder select Add. Select Peng-Robinson as the 
property package. 
 
4.04. Go to the simulation environment. Click the Simulation button in the bottom left corner of the screen. 
 
4.05. Add a Cooler block to the flowsheet from the Model Palette. 
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 3 
 
 
4.06. Double click the cooler (E-100). Create an Inlet stream called Feed, an Outlet stream called ToSep, and 
an Energy stream called Q-Cool. 
Thermo-019H Revised: Nov 7, 2012 
 4 
 
4.07. In the Parameters form, enter a Delta P of 0, and a Duty of 0 kcal/h. We will create an adjust block to 
vary the duty to reach the desired specifications. 
 
 
Thermo-019H Revised: Nov 7, 2012 
 5 
 
4.08. Define feed stream. Go to the Worksheet tab. Enter a Temperature of -90°F (-67.78°C), and a Pressure 
of 475 psia (32.75 bar). 
 
4.09. Define composition. Go to the Composition form and enter the following Mass Flow rates in kg/h. 
 
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 6 
4.10. Add a Separator to the flowsheet from the Model Palette. 
 
4.11. Double click the separator (V-100). Select stream ToSep as the Inlet stream, and create Outlet streams 
called Vap and Liq. 
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4.12. Go to the Worksheet tab to view the separation results. You can see that the liquid stream has a 
flowrate of 0. We must now add an adjust block and a spreadsheet to find the cooler duty required to 
limit the loss of ethylene to the vapor stream to less than 1%. 
 
 
Thermo-019H Revised: Nov 7, 2012 
 8 
4.13. Add a Spreadsheet to the flowsheet from the Model Palette. 
 
 
4.14. Double click on the spreadsheet (SPRDSHT-1). In the Spreadsheet tab enter “Ethylene flow in Feed” in 
cell A1, and “Ethylene flow in Liq stream” in cell A2. Right click on cell B1 and select Import Variable. 
Select the Master Comp Molar Flow (Ethylene) in the Feed stream. Right click cell B2 and select Import 
Variable. Select the Master Comp Molar Flow (Ethylene) in the Liq stream. 
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4.15. Enter the text “Fraction Ethylene Lost” in cell A3. In cell B3 enter the following formula: = (B1-B2)/B1. 
 
4.16. You can see that right now we are losing 100% of the Ethylene to the vapor stream. We will now add an 
adjust block to vary the cooler duty in order to limit the fraction lost to under 0.01. Add an Adjust block 
to the flowsheet from the Model Palette. 
Thermo-019H Revised: Nov 7, 2012 
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4.17. Double click on the adjust block (ADJ-1). Specify the Adjusted Variable to be the Duty of cooler block E-
100. Specify the Target Variable to be cell B3 of SPRDSHT-1. Enter a Specified Target Value of 0.01. 
Thermo-019H Revised: Nov 7, 2012 
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4.18. In the Parameters tab enter a Step Size of 1e+005 kcal/h and change the Maximum Iterations to 100. 
Click Start to begin calculations. 
 
Thermo-019H Revised: Nov 7, 2012 
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4.19. The fraction of ethylene lost in the vapor stream will now be less than 1%. We must also make sure that 
the Mole Fraction of Hydrogen in the liquid stream is less than 0.02. Double click the Liq stream and go 
to the Composition form under the Worksheet tab. 
 
 
4.20. The Mole Fraction of hydrogen in the liquid stream is 0.0172, which is less than the specified value of 
0.02. 
 
 
 
 
Thermo-019H Revised: Nov 7, 2012 
 13 
5. Conclusions 
The vapor pressure of hydrogen is much higher (6,600 times higher than methane at -150 °C) than the vapor 
pressures of the other components in the feed stream. We used the adjust block and a spreadsheet to 
determine a good value for the heat duty of the cooler block to remove the bulk of hydrogen from the feed 
stream through a separator block. 
6. Copyright 
Copyright © 2012 by Aspen Technology, Inc. (“AspenTech”). All rights reserved. This work may not be 
reproduced or distributed in any form or by any means without the prior written consent of 
AspenTech. ASPENTECH MAKES NO WARRANTY OR REPRESENTATION, EITHER EXPRESSED OR IMPLIED, WITH 
RESPECT TO THIS WORK and assumes no liability for any errors or omissions. In no event will AspenTech be 
liable to you for damages,