ChE 3G4 HYSYS TUTORIALS pot

Double click on the stream, Feed 1 and enter the temperature –20oC and a pressure of 6000 kPa.. On the window that pops up enter the name of your feed stream into the Inlet, and name y

ChE 3G4 HYSYS TUTORIALS

Tutorial 1: Introduction to HYSYS – Not Graded 1

A Learning Objectives: 2

B Defining the Simulation Basis 2

C Selecting a Unit Set 3

D Adding a Stream 3

E Flash Calculations 4

F Adding Utilities 5

G The Stream Property Value 5

H Customizing the Workbook 5

I Flash Calculations of a Ethanol-Water Mixture 6

J Additional Exercises (For Extra Practice using the GasPlant Example) 7

Tutorial 2: Propane Refrigeration Loop – 15 Marks 8

A Learning Objectives 8

B Base Case (5 marks) 8

C Manipulating the PFD 10

D Manipulating Process Variables (10 marks) 10

E Printing 11

Tutorial 3: Refrigerated Gas Plant - 10 marks 12

A Learning Objectives 12

B Building the Simulation 12

C Adding the Balance Operation 14

D Adding the Adjust Operation 15

E Using the Case Study 15

F Bonus (5 Marks) 16

G Saving the Simulation as a Template 16

Tutorial 4: Recycle Operations - 10 marks 17

A Learning Objectives 17

B Building the Simulation 17

C Installing the Recycles 19

Tutorial 5: Separation Columns – 10 marks 21

A Learning Objectives 21

B Building the Simulation 21

C Column Sub-Flowsheets (Read Only) 26

Tutorial 6: Optimization in HYSYS – 15 marks 27

A Learning Objectives 27

B Building the Simulation 27

C The Optimizer 29

D Bonus ( 3 Marks) 33

Tutorial 1: Introduction to HYSYS – Not Graded

A Learning Objectives:

• Define a Fluid Package

• Add streams and a separator

• Perform simple flash calculations

B Defining the Simulation Basis

1 To start HYSYS go to Course Folders, Chemical Engineering, ceng3g03 and click

on HYSYS.Plant Start a new case by Selecting File, New, Case

2 Select the Components tab This tab allows you to add components to your case

Select these components: N2, H2S, CO2, C1, C2,C3,i-C4, n-C4, i-C5, n-C5, C6 and

H2O You can also add components by typing their names (ie methane rather

then C1) with Match The components should be listed under Component List-1

Minimize the window

3 Select the Hypothetical button under Add Component to add a hypothetical

component to the fluid package These components can be used to model

non-library components, defined mixtures, undefined mixtures or solids In this case it

will be used to model the components in the gas mixture heavier then hexane To

create this component, select the Quick Create a Hypo Comp button

4 On the ID tab type the name, C7+ Move to the Critical tab Enter 110oC for its

Normal Boiling Pt Press Estimate Unknown Props to estimate all the other

properties of the hypothetical component You should get the following base

property values:

Molecular Wt: 111.00 Ideal Liq Density: 745.38

5 Add the hypothetical component to the current component list by

highlighting/selecting it in the Hypo Components group and then pressing Add

Hypo button

6 HYSYS contains various Fluid Packages that contain necessary information for

performing flash and physical property calculations Select the Fluid Pkgs Tab

Create a fluid package by selecting the Add button and choose Peng-Robinson

Equation of State Model (PR)

7 Change the Name from Basis-1 to GasPlant

8 The fluid package is now defined and you can now start a simulation Press Enter

Simulation Environment or the Interactive Simulation Environment in the top

toolbar

C Selecting a Unit Set

The HYSYS edition in the labs should have the default unit set to SI units The unit set

can be changed

1 From the Tools menu, choose Preferences Switch to the Variables tab and click

on Units

2 Highlight the units you wish to work with and close the window

We will use SI units for this tutorial and unless otherwise specified

D Adding a Stream

There are several ways to add a stream We will focus on one and you may try the others

if you have time

Adding a Stream from the Menu Bar

1 Press F11 The stream property view is displayed Change the stream name to

Feed 1

2 Enter the compositions of the components by selecting the Composition Select

Edit Click on mole fraction as a basis Enter the following compositions and

press OK Close the window

The following are other ways to add a stream Move on to Part D Work on these after

you have completed the rest of the tutorial

Adding a Stream from a Workbook

1 To open or display the workbook, press the Workbook icon on the top toolbar

2 Enter the stream name, Feed 2 in the **New**

Component Mole Fraction Component Mole Fraction

N2 0.0025 I-C4 0.0115 H2S 0.0237 N-C4 0.0085 CO2 0.0048 I-C5 0.0036

C2 0.1920 C6 0.0003 C3 0.0710 C7+ 0

3 Double click on the Molar Flow cell and enter the following compositions and

click OK

Component Mole Fraction Component Mole Fraction

N2 0.0002 I-C4 0.0150 H2S 0.0405 N-C4 0.0180 CO2 0.0151 I-C5 0.0120 C1 0.7250 N-C5 0.0130 C2 0.0815 C6 0.0090 C3 0.0455 C7+ 0.0252

Adding a Stream from the Object Legend (F4 if it is not available)

1 Double click on the materials stream (blue) and change the name to Feed 3

Enter the following compositions

E Flash Calculations

In this section, simple vapour-liquid equilibrium flash calculations from ChE 3D3 will be

performed HYSYS can perform three types of flash calculations on streams:

Pressure-Temperature, Vapour fraction-Pressure and Vapour fraction-Temperature Once the

composition of the stream and two of either T, P or vapour fraction are known, HYSYS

performs a flash calculation on the stream

Try these on Stream Feed 1

1 P-T flash Set P = 7500 kPa and T = 10oC The calculated vapour fraction should

be 0.9879

2 Perform a dew pt calculation by setting P =7500 kPa and vapour fraction to 1.0

The dew pt should be 11.43 o C

3 Perform a bubble pt calculation by setting P = 7500 kPa and vapour fraction to

0.0 The bubble pt should be –34.32 o C

Component Mole Fraction Component Mole Fraction

N2 0.0050 I-C4 0.0041 H2S 0.0141 N-C4 0.0075 CO2 0.0205 I-C5 0.0038

C2 0.2545 C6 0.0060 C3 0.0145 C7+ 0.0999

F Adding Utilities

The utilities available in HYSYS is a useful tool that interact with your process and

provide additional information or analysis of streams or operations

1 Double click on stream Feed 1

2 Select the Attachments tab and then select Utilities Press Create to access the

utilities window

3 Select envelope and press Add Utility The Envelope utility should be displayed

4 The critical temperature, -12.06 o C, and pressure, 8980 kPa, for the stream should

be displayed

5 Select the Performance tab and the Plots tab to view the envelope By pressing

Table, you can view the envelope data in tabular form

6 You can also add a utility using the Menu Bar – Menu, Utilities

G The Stream Property Value

It is possible to view the properties of the individual phases for any stream

1 Double click on the stream, Feed 1 and enter the temperature –20oC and a

pressure of 6000 kPa Move the cursor to the left of the view until the cursor

changes the resizing arrows

2 Drag the edge of the view until all the phases can be seen (Feed 1, Vapour Phase,

Liquid Phase)

H Customizing the Workbook

HYSYS will allow you to customize the workbook You can add additional pages,

change the variables that are displayed on current pages, or change the format of the

values which are displayed

In this exercise, a new workbook tab containing stream properties, Cp/Cv, Heat of

Vapourization and Molar Enthalpy will be added

1 Open the workbook by pressing the Workbook icon button on the top toolbar

2 Select Workbook and Setup from the main menu and the setup window will appear

Under Workbook Tabs, press Add and in the view which appears select Stream+

and OK

3 A new workbook tab, Streams2 will be listed in the workbook pages group

Highlight this tab Change the name to Other Properties

4 In the Variables group, press the Delete button until all the default variables are

removed Click the Add button to add a new variable to the tab

5 From the Variables list, select Cp/Cv and click OK Repeat by adding Heat of

Vaporization and Molar Enthalpy Press the Close button to return to the

workbook

6 The workbook now contains the tab Other Properties which shows the value of

Cp/Cv, Heat of Vaporization and Molar Enthalpy If there are no values for these

numbers go back to the Stream tab and enter a temperature and pressure for

stream Feed 1

7 To print a workbook specsheet just right click and select Print Specsheet

8 Save this file if you wish to try the other methods of adding streams

I Flash Calculations of a Ethanol-Water Mixture

In this exercise, we will take the flash calculations from Part D a step further by adding a

separator To install a flash separator, the following steps need to be performed:

1 Start a new case Choose a fluid package Choose UNIQUAC

2 Select the components ethanol and water You will learn later on in the course

that the type of fluid package must be appropriate depending on your flash

components This means that it might happen that one or some of the desired

components do not appear in the list for a certain fluid package For

ethanol-water mixture the UNIQUAC fluid package is appropriate

3 Create a feed stream and name it For flash calculations we need to fix the

required degrees of freedom (4) A liquid-vapour mixture is necessary to allow

separation We therefore need to find the dew and bubble points, between which

the 2 phases exist Select P = 100 kPa, F = 100 kgmol/h and 50-50 mole fraction

for each component Then to calculate the dew point, set the vapour fraction to

1.0 A green OK should appear which indicates the degrees of freedom have been

specified and a converged solution has been found You should get Tdew =

84.03oC Now change the vapour fraction to 0.0 to get a bubble point, which is

Tbubb = 79.41 oC Remove the specification of the vapour fraction and select a

temperature between the dew and bubble point The vapour fraction should be

between 0.0 and 1.0

The following table shows dew and bubble points for the feed stream at different

pressures Verify these with your case

Pressure (kPa) T bubb ( o C) T dew ( o C)

100 79.41 84.03

150 90.09 94.79

200 98.13 102.9

250 104.7 109.5

4 Press F12 We want a separator Choose vessel and then separator On the

window that pops up enter the name of your feed stream into the Inlet, and name

your vapour and liquid outlet and energy streams (ie Vap, Liq, Q)

5 A yellow warning should appear indicating unknown duty We will ignore duty

in this case Select Parameters and enter 0 for the duty A green OK should now

6 Try these examples for pressure and temperature and verify these results with

your case To view the properties of the inlet and outlet streams double click on

the separator and choose the Worksheet tab To view the composition of the

liquid and vapour streams select Composition

P = 150 kPa, T = 92oC, F = 100 kgmol/h

Liquid Flow: 28.53 kgmol/h

Ethanol mol fraction (liquid) 0.3013

Water mol fraction (liquid) 0.6987

Ethanol mol fraction (vapour) 0.5793

Water mol fraction (vapour) 0.4206

P = 250 kPa, T = 105oC, F = 100 kgmol/h

Liquid Flow: 78.63 kgmol/h

Ethanol mol fraction (liquid) 0.4628

Water mol fraction (liquid) 0.5372

Ethanol mol fraction (vapour) 0.6368

Water mol fraction (vapour) 0.3632

J Additional Exercises (For Extra Practice using the GasPlant Example)

Try these exercises, the answers are in bold You will need to add the other streams in

order to answer some of these questions

1 The critical pt of Feed 2 -1.11 o C, 14431 kPa

2 Cricondenbar (max pressure) for Feed 2 16292 kPa

3 Bubble Pt Temperature for Feed 3 at 6000 kPa -53.57 o C

4 Dew Pt Temperature for Feed 2 at 4000 kPa 98.12 o C

5 Vapour fraction for Feed 1 at 5oC and 8000 kPa 0.9487

6 Vapour fraction for Feed 2 at 32oF and 10 bar 0.9245

Note: when entering the pressure and temperature click on the unit drop down box

for the correct units HYSYS will convert these to the default units

Tutorial 2: Propane Refrigeration Loop – 15 Marks

Refrigeration systems are commonly found in the natural gas processing and petroleum

refining industry Refrigeration is used to cool gas to meet a hydrocarbon dewpoint

specification and to produce a marketable liquid In this tutorial you will construct, run,

analyze and manipulate a propane refrigeration loop

A Learning Objectives

• Adding and connecting unit operations to build a flowsheet

• Adding tables to the PFD

• Printing procedures

B Base Case (5 marks)

Answer the questions that appear as bold and boxed

1 Start a new case and add the components and fluid package: propane and ethane

and Peng Robinson (Equation of State) Enter the simulation environment

2 Install a stream Double click on the stream and enter the following information

3 Add a second stream and enter the following properties:

4 There are a variety of ways to add unit operations in HYSYS Last tutorial we

used F12 and the Unit Operations window to install a separator In this case you

will add the following operations: valve, chiller, compressor, condenser The

following are alternate ways to install a unit operation Use the one you feel most

comfortable with These instructions will use F12

Name 1 Vapour Fraction 0.0

Temperature 45oC

C3 Mole Fraction C2 Mole Fraction

1.0 0.0

Name 3 Vapour Fraction 1.0

Temperature -15 oC

What is the pressure of stream 1 in kPa?

Workbook Select Tools, Workbook and select View

Open the workbook and go to UnitOps tab page then click on Add UnitOp

button The UnitOp window will be displayed

Object Legend You can select the unit from the icon of

the operation If this legend is close press F4 and it will appear You can either double click on the appropriate operation

or right click on it and drag it over to the simulation environment (PFD)

5 Press F12 and click on Piping Equipment Select Valve and press the add button

The valve property window should be displayed For the Feed stream select 1

and for the Product stream type 2 A J-T valve is being modeled so type J-T as

the Name of the valve Close the window

6 The chiller operation in the loop is modeled in HYSYS using a heater operation

The outlet of the chiller will be at its dewpoint Press F12 and select Heat

Transfer Equipment Select Heater and Add In the property window name the

operation Chiller The inlet is stream 2 and the outlet is stream 3 Name the

energy stream Chill-Q

7 Select Parameters Enter the values 1.50e+6 kJ/h and 5.0 kPa for the Duty and

Pressure Drop of the chiller A green OK should appear Close the window

8 The compressor is used to increase the pressure of the inlet gas stream Press F12

and select Rotating Equipment Select Compressor and add it On the property

view window enter the Name of the unit as Compressor the Inlet stream is 3,

Outlet stream is 4, and Energy stream as Compressor-Q

9 Select Parameters Enter the Adiabatic efficiency as 75%

10 To complete the loop we will add a condenser It is placed between the

compressor and valve and is modeled as a cooler operation Press F12 and Heat

Transfer Equipment Select Cooler and Add

11 In the property view window enter the Inlet stream as 4, the Outlet stream as 1,

the Name of the unit as Condenser and the Energy stream as Condenser-Q

12 Select Parameters and enter the Pressure Drop: 30 kPa

13 If your PFD diagram appears to be small you can zoom in on the PFD by

selecting the magnify glass icon and drawing a box around your PFD

W What is the flow rate of propane in kgmol/h?

What is the valve pressure drop in kPa?

What is the temperature of the valve outlet in o C?

What is the compressor duty in hp?

Note: 1 J/s = 1.341 x 10 -3 hp

C Manipulating the PFD

HYSYS allows users to view properties and tables and print information for the PFD,

unit operations and streams Try these exercises to get accustomed to these options

1 For the PFD, right click the mouse and select Add a Workbook Table Streams

should be highlighted and click on Select Material and energy data for all

streams should be displayed in the table on the PFD You can remove the table

by selecting the table, right click the mouse and select Hide

2 Add a table for stream 4 Select stream 4 and right click on the mouse Select

Show Table from the menu You can remove the table in the same manner as

above

3 Add a table for the valve Select the valve using the mouse Right click on the

mouse and select Show table from the menu

Each workbook has a unit operations page by default that displays all the unit operation

and their connections in the simulation You can add additional pages for specific unit

operations to the workbook

1 Open the workbook In the Menu bar, select Workbook and then Setup

2 Highlight Unit Ops and press the Add button in the workbook pages group From

the New Object Type view, double click on Unit Operations and then select

Compressor Click Ok A new page, Compressors, containing only compressor

information is added to the workbook

D Manipulating Process Variables (10 marks)

Save your base case using File, Save, Case After manipulating variables of the base case

for Question 1, you may want to re-open the base case and use it for Question 2

1 In reality, a plant would not have a pure propane refrigeration cycle There will

always be a small fraction of impurities Suppose the plant has a 96/4 (mole %)

propane/ethane blend What effect, if any, does this new composition have on the

refrigeration loop? Use the base case for comparison

Base Case: 100% C3 New Case: 4 % C2, 96% C3

Flow (kgmol/h)

Valve Pressure Drop (kPa)

Valve Outlet Temp (oC)

Condenser Q (kJ/h)

Compressor Q (hp)

2 In the plant there is no instrumentation that can measure or calculate the chiller

duty However, you know that the compressor is rated for 250 hp and that it is

running at 90% of maximum and 70% adiabatic efficiency Assume a pure

propane refrigeration cycle What is the chiller duty in kJ/h? What is the propane

flow rate in kgmol/h Explain how you solved this problem

E Printing

You can print results through the menu bar, from the PFD and using the report manager

You do not have to print any tables or PFD for this tutorial Read these procedures only

to become familiar with the printing procedures

1 To print from the menu bar select File, Print All worksheets will be printed

2 To print your PFD, right click on the PFD and select Print PFD

3 You can also print worksheets for specific streams or unit operations Select the

unit operation or stream you wish to have information printed Right click the

mouse and select Print Datasheet You can view a Preview of the printout as

well

4 To print using the report manager, select Tools, Reports Press Create to add a

new report and open the Report Builder Press Insert Datasheet to add specsheets

to your report You can add single or multiple unit operations specsheets to the

report

Tutorial 3: Refrigerated Gas Plant - 10 marks

In this simulation, a simplified version of a refrigerated gas plant is to be modified The

purpose is to find the LTS (low temperature separator) temperature at which the

hydrocarbon dewpoint target is met The Sales Gas hydrocarbon dewpoint should not

exceed –15oC at 7000 kPa The incoming gas is cooled in two stages – first by exchange

with product Gas Sales in a gas-gas exchanger and then in a chiller A Balance operation

will be used to evaluate the hydrocarbon dewpoint of the product at 6000 kPa

A Learning Objectives

• Install and converge heat exchangers

• Understand Logical Operations (Balances and Adjusts)

• Use the Case Study tool to perform case studies on your simulation

• Saving the simulation as a template

B Building the Simulation

Answer any questions that appear in bold and boxed

1 Start a new case Enter the following components: N2, H2S, CO2, C1, C2, C3,

i-C4, n-i-C4, i-C5, n-C5, C6, H2O and a hypothetical component C7+ For the

hypothetical component, choose 110oC for its normal boiling point and select

Estimate Unknown Parameters to determine all other parameters Use

Peng-Robinson EOS as a fluid package Enter the simulation environment

2 Add a stream Fill in the following values:

Name: To Refrig Pressure: 6500 kPa

Temperature: 15oC Flow Rate: 1500 kgmole/hr

Name: Inlet Gas Sep Vapour Outlet: Inlet Sep Vap

Feed: To Refrig Liquid Outlet: Inlet Sep Liq

The heat exchanger performs two-sided energy and material balance calculations The

heat exchanger is capable of solving for temperatures, pressures, heat flows, material

stream flows and UA

4 Add a heat exchanger Select F12, Heat Transfer Equipment and Heat

Exchanger Enter the following information

Name: Gas-Gas Shell Side Inlet: LTS Vap

Tube Side Inlet: Inlet Sep Vap Shell Side Outlet: Sales Gas

Tube Side Outlet: Gas to Chiller

The heat exchanger models are defined as follows:

Weighted – The heating curves are broken into intervals, which then exchange energy

individually A log mean temperature difference (LMTD) and UA are calculated to each

interval in the heat curve and summed to calculate the overall exchanger UA The

weighted method is available only for counter current exchangers

Endpoint – A single LMTD and UA are calculated from the inlet and outlet conditions

Can be used for simple problems where there is no phase change and Cp is relatively

constant

5 Switch to the Parameters tab Under Heat Exchanger Model, select Exchanger

Design Weighted Under Individual Heat Curve Details, change the number of

intervals to 10 for both streams Under Exchanger Parameters enter a Tubeside

Delta P of 30 kPa and Shellside Delta P of 5 kPa

In order to solve the heat exchanger, unknown parameters are manipulated by the solver

Each parameter specification will reduce the number of degrees of freedom by one Two

specifications are needed for this exchanger:

Heat Balance = 0 : this is a duty error specification and is needed to ensure that the heat

equation balances HYSYS will supply this specification by default

Min Approach = 5oC – this is the minimum temperature difference between the hot and

cold stream

6 On the Design tab, select Specs Deactivate the UA specification Click on the

Active check box for the specification (the X means the specification is active)

7 To add a specification, press the Add button In the display window enter the

following Close the window once entering the information

Name: Temp Approach Type: Min Approach

Pass: Overall Spec Value: 5oC

8 Add a cooler to the simulation F12, Heat Transfer Equipment, Cooler Enter the

following information:

Name: Chiller Energy Stream: Chiller Q

Feed Stream: Gas to Chiller Product Stream: Gas to LTS

Under the Parameters tab, add a pressure drop of 40 kPa

9 Add a separator and provide the following information

Vapour Outlet: LTS Vap Liquid Outlet: LTS Liq

10 Specify the temperature of the stream Gas to LTS to be –25oC

C Adding the Balance Operation

The balance operation provides a general-purpose heat and material balance facility

There are different balances available in HYSYS:

Mole: an overall balance is performed where only the molar flow of each component is

conserved Outlet streams will have the same molar flow rate and composition as

the inlet stream, but will contain no vapour fraction, temperature or pressure

values

Mass: Same as above but only the mass flow is conserved

Heat: Same as above but only the heat flow is conserved

Mole and Heat: the mole and heat flow are conserved

Look at the parameters for Sales Gas The stream parameters are calculated so

there is no way to force the stream to calculate a dewpoint temperature at 7000 kPa

Adding a mole balance allows you to create a second steam with the same molar

flowrate and composition but no vapour fraction, temperature or pressure

11 Select F12, Logicals and Balance Add the following information:

Inlet stream: Sales Gas Outlet Stream: HC Dewpoint

Select the Parameters tab For the Balance Type, click on Mole

12 Specify a pressure of 7000 kPa for the stream HC Dewpoint Set the vapour

• What is the pressure of stream “Sales Gas” in kPa?

• What is the temperature of stream “Sales Gas” in o

C?

• What is the current available UA for the Gas-Gas exchanger in kJ/ o

Ch?

D Adding the Adjust Operation

The adjust operation is a logical operation It will vary the value of one stream

variable (independent variable) to meet a required value or specification (dependent

variable) in another stream The current HC dewpoint does not meet the

requirement of –15 o C

13 Select F12, Logicals and Adjust On the display window, press Select Var in the

Adjusted Variable group From the Object list select Gas to LTS From the

Variable list, select Temperature Press Ok to accept the variable and return to

the Adjust property view

14 Press the Select Var button in the Target Variable group Select HC Dewpoint

Temperature as the target variable Enter the value of –15oC in the Specified

Target Value box

15 Switch to the Parameters tab When considering step sizes, use larger rather then

smaller sizes The Secant method works best once the solution has been

bracketed by using a larger step size and a converged solution will be found

faster For this case leave parameters at the default values

16 Go back to the Connections tab and press Start to begin calculations To view the

progress of the Adjust, go to the Monitor tab

E Using the Case Study

The case study tool allows you to monitor the steady state response of key process

variables to changes in your process You select independent variables to change and

dependent variables to monitor HYSYS varies the independent variables one at a time

and the dependent variables are calculated Instead of using the Adjust to find the LTS

feed temperature required to achieve the hydrocarbon dewpoint, you can use the Case

Study to examine a range of LTS temperatures and dewpoints

17 Open the Adjust view Check the ignore box in the bottom right hand corner

This turns off the Adjust function which is required for the Case Study function to

be used

18 From the Tools menu select Databook On the Variables tab, press the Insert

button Select the Gas to LTS Temperature as the first variable Press the Add

button to add the variable

What is the dewpoint temperature in o C?

Assuming the pressure is fixed, what other parameter affects the dewpoint?

How can we change the dewpoint in the simulation (Hint: Keep reading on)?

What is the chiller outlet temperature to achieve the dewpoint specification in

o

C?

19 Add a second variable Select the HC Dewpoint Temperature and press the Add

button Press the close button to return to the Databook

20 In the Databook, switch to the Case Studies tab Press the Add button to add a

new case study Select the Gas to LTS Temperature as the independent variable

(Ind) and HC Dewpoint Temperature as the dependent variable (Dep.)

21 Press the View button to setup the case study Enter the values for Low Bound,

High Bound and Step Size of –25oC, 5oC and 5oC respectively Press the Start

button to begin the calculations

Reactivate the Adjust operation by unchecking the ignore box

SAVE THIS CASE ON A DISK

F Bonus (5 Marks)

What is the log mean temperature difference (LMTD) for the exchanger with an

minimum approach temperature of 5oC? Double Click on the heat exchanger to find this

information

Suppose now the available UA for the Gas-Gas exchanger is only 1.5 x 105 kJ/oC h

Make the necessary modifications to your exchanger design to achieve this UA What is

the affect on your LMTD and minimum approach temperature? Describe the steps you

took to solve this problem in HYSYS

G Saving the Simulation as a Template

HYSYS allows the user to save a simulation as a template A template is a complete

flowsheet that has been stored to disk with some additional information included that

pertains to attaching the flowsheet as a sub-flowsheet operation Typically, a template is

representative of a plant process module or portion of a process module The stored

template can be read from disk and installed as a complete sub-flowsheet operation any

number of times into any number of different simulations The main advantage of a

template is it can link two or more cases together

22 Choose Main Properties from the Simulation menu

23 Press Convert to Template button Press Yes to convert the simulation case to a

template Answer No to the question “Do you want to save the simulation case.”

Name your template file

What Gas to LTS temperature range will satisfy the HC Dewpoint specification

(-15 o C)?