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Problem Statement: Neither Quick Results nor Excel Equipment Contents report includes materials transferred from step1 to step2. | Solution: In a Batch simulation (Run\Simulate Batch), each step is simulated independently. That is, Batch Plus does not use the results from previous steps in a batch simulation.
Example:
Step 1: charge Tank-A with 100 kg of water. Quick Results show Tank-A equipment contents of 100 kg of water.
Step 2: charge Tank-A with 200 kg of water. Quick Results show Tank-A equipment contents of 200 kg (not 300 kg) of water.
In a Production Plan simulation (Run\Simulate Plan), each subsequent step is simulated from the previous steps. The Excel Equipment Contents report of the production plan records materials transferred between steps. In the above example, the water content of Tank-A at the end of Step 2 will be 300 kg.
Keywords:
References: None |
Problem Statement: How does a fill operation handle left-over material? | Solution: When specifying a Fill operation, the user can provide the following input arguments
Filling-Unit
: Equipment used to fill the material.
From-unit
: Equipment unit from which material is transferred.
Packaging-Material
: Packaging material to which material is filled into.
Material-Amount
: Material amount filled into individual container.
To calculate the number of containers, the total amount of material in the From-Unit is divided by the Material-Amount. This can lead to some left-over material, if the result of the division is not an integer. The left-over material will remain in the source vessel.
For example, when specifying 100.5 kg in From-Unit and setting the 'Material-Amount' equal to 1 kg, Batch Plus will report the following:
==> 100 containers are filled, each with 1 kg
==> 0.5 kg are left over in the source vessel
The Fill operation only creates full containers. In other words, FILL does not fill the remaining 0.5 kg into container no. 101.
Keywords: fill, operation
References: None |
Problem Statement: How do you incorporate long chain branching into polymerization reaction? | Solution: To predict long chain branching during polymerization, the BRANCH3 and BRANCH4 segment types need to be defined. To declare certain segments as BRANCH3 or BRANCH4, please go to Aspen Properties > Polymers > Characterization > Segments.
Some common polymers predicted this way includes polyethylene (BRANCH3) and polybutadiene (BRANCH4):
BRANCH3
BRANCH4
Key Words
Polymer, Long Branch, Segment
Keywords: None
References: None |
Problem Statement: How to see the viscosity and the vapor pressure of the fluid loaded within the PUMP-FLO tool? | Solution: PUMP-FLO is a centrifugal pump selection software used by pump manufacturers and distributors around the world and it can work in integration with Aspen Plus. To use it you need to go to the Pump block Setup | Specifications form and click on the Aspen Exchange icon where the PUMP-FLO tool can be downloaded for free from Exchange.
To be able to search for a suitable pump, fluid properties and process data are required ( Head, Flow, inlet temperature, density, viscosity, and vapor pressure)
Process data is and density are transferred automatically from Aspen Plus, but In order to see the viscosity and vapor pressure of a fluid in PUMP-FLO, you need to add these properties in a property set. This can be accomplished with the following steps:
1. Add a new property-set PS-1 and select the following properties with the units that you need.
· RHOMX for mixture density
· MUMX for mixture viscosity
· PBUB for vapor pressure
2. Go to the simulation environment the Setup I Report Options I Stream form and click Property Sets. Add the new PS-1 to the Selected property sets area.
3. Run the simulation.
4. Open the PUMP-FLO tool and you can see the properties loaded within this application.
Once you have all the required process data and properties, you can go ahead and select a manufacturer to perform a pump curve search and selection. The selected pump curve can then be imported into Aspen Plus.
Keywords: PUMP FLO, Fluid viscosity, Vapor pressure, prop-set
References: None |
Problem Statement: Describes how to split Event label in more than one lines in Aspen Petroleum Scheduler and Aspen Refinery Multi-Blend Optimizer | Solution: When create a new Event , enter the label you want to display on the Gantt chart above the event. If you want to display the label on two or more lines, insert a `I?symbol where you want a line break.
Then click OK, now splitted Label is showing in two lines:
Keywords: -Gantt Chart
References: None |
Problem Statement: Explanation of DMC3 features in APC Builder and DMCplus Legacy platform | Solution: - DMC3 is a licensing scheme. We can have a DMC3 controllers built with the legacy DMCplus tools (offline and online). In that configuration, a DMC3 controller has base controller, AspenWatch, SmartStep, Calibrate/Adaptive only. On the other hand, a DMC3 controller built with APC Builder would have the mentioned features along with Robust control (v8.7), SmartTune (v8.8).
- Under legacy tools and APC Builder, the user can build a DMCPlus or DMC3 controller depending on their license scheme. Under the DMCplus licensing scheme, the user will have to manually enable individual features such as AW, SmartStep, etc. Where as, under DMC3 licensing scheme all the features are automatically enabled for the controller.
DMCplus
DMC3
DMCplus Legacy tools
Base control, AW, SS, Calibrate/Adaptive
[Base control, AW, SS, Calibrate/Adaptive]
APC Builder
Base control, AW, SS, Calibrate/Adaptive
[Base control, AW, SS, Calibrate/Adaptive, Robust, SmartTune]
Keywords: DMC3
legacy DMCplus platform
APC Builder Platform
References: None |
Problem Statement: Proware Super-Saddles are not available in pack sizing/rating in Aspen Plus. | Solution: It is not possible to have all packing and tray types in Aspen Plus. We try to add them when we have enough information from the manufacturer. For Proware Super-Saddles, we do not have sufficient data from the manufacturer to add it to the database. Our suggestion is to use the Super Intalox for the calculation (SUPER-INTX) with Vendor=Norton. This should be close enough to make no significant difference to the results.
To add a packing to our database, we need more information than the specific area and void fraction (2.6cm2/cc and 0.77 for super-intelox ceramic 1, compared to 2.55cm2/cc and 0.72 for Proware ceramic Super-Saddles 1). We need also the packing factor or air/water pressure drop curves which are necessary for us to include packings in the database.
About the Norton method, a bit of history is useful to clarify. Norton had its own flooding and pressure drop equations that some people still prefer. While Norton's packing business was acquired by Koch-Glitsch, we still maintain the distinction: Norton packings default to Norton methods, and Kock packings default to Koch methods. NorPro kept the ceramic part of the packing business, but Super Intalox saddles are still in service from the original Norton.
Keywords: compatibility, packing, vendors
References: None |
Problem Statement: How can I use the DOCALL subroutine in a USER2/USER3 user model to call a routine which is not linked in the same dll as the user subroutine code? Can I dynamically link to other dlls? | Solution: This is exactly the purpose of the DOCALL subroutine. Instead of creating a very complex example, let's take a look at this conceptual case:
USRUS2 subroutine implements the USER2 unit operation code, it will be called by Aspen Plus
MYROUT subroutine implements some further calculations, which will be called by the USRUS2 subroutine
We want one dll with the user subroutine USRUS2 (usrus2.dll) and another dll with the additional subroutine MYROUT (myrout.dll). This means that the linking (finding where the MYROUT actual object code is available - also known as resolving the symbols in compilation/linking jargon) will be done dynamically (that means at run time as opposed to static linking, which is done at compilation/linking time - for example if the USRUS2 and MYROUT were in the same dll).
The MYROUT routine name is specified in the USER2 block. Aspen Plus will then try to locate the symbols (the compiled subroutine) MYROUT in the various object/dll supplied (via a DLOPT dynamic linking option file). This ensures that the routine MYROUT will be loaded.
The DOCALL subroutine supplied by Aspen Plus will then allow the USRUS2 subroutine to call MYROUT.
This may look very complex. What is the advantage of calling the routine via DOCALL instead of calling the routine directly? The advantage is that you can supply the name of the routine in the USER2 block. If you were calling the routine directly, then if you want to change and call another routine, you will have to recompile the source code. In other words, this gives us more flexibility.
To run the example, you must have the Intel Fortran compiler correctly installed on your computer.
Task 1 - Compile and create the dlls
1. Open a Aspen Simulation Engine command window.
2. Change to the folder .\libs where the source code is located.
3. Type the commands:
ASPCOMP USRUS2.F
ASPCOMP MYROUT.F
ASPLINK USRUS2.DLL /DLOPT=USRUS2.OPT
ASPLINK MYROUT.DLL /DLOPT=MYROUT.OPT
The first two commands compile the code (from source *.f to object *.obj). The last two commands create the dynamic link libraries (*.dll) based on the commands supplied in the option files (*.opt - the list of object files to include in each library).
Task 2 - Run the simulation
This can be done from Aspen Plus graphical user interface or input file. When developing user models, it is typically more convenient to use the input file and command line interface: you can simply write to the screen (WRITE(*,*)), faster turn around in case of crashes, etc.
1. In the same simulation engine window, change to the parent folder (CD ..)
2. Type the command
ASPEN TEST-USER2 FOO /DLOPT=DLOPT.TXT
This will run the simulation. The DLOPT.TXT file is a dynamic linking option file used for Aspen Plus: in this case it contains the list of dynamic link libraries usrus2.dll and myrout.dll.
The relevant lines in the source code are:
In usrus2.f
-- declarations:
INTEGER IFNCPTR
INTEGER IDUM
DOUBLE PRECISION X, Y
-- code:
X = 42.d0
Y = 0d0
CALL USRUTL_GETSUB(1,IFNCPTR)
CALL DMS_DOCALL(IFNCPTR,X,Y,
* IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,
* IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,
* IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,
* IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,
* IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,
* IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,
* IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,
* IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM,IDUM)
WRITE(USER_NHSTRY,*), Y
The routine myrout.f is a trivial example:
subroutine MYROUT(X,Y)
double precision X, Y
write(*,*) X
Y = X
return
end
The code works fine if you see the value 42 written to the history file (from USRUS2, WRITE(USER_NHSTRY,*) Y).
It is also probably possible to link a library without using the routines supplied by Aspen Plus (calling directly the Windows functions - as a separate process, using COM, etc). These options may be more complex to implement and are outside of the scope of thisSolution.
Keywords: None
References: None |
Problem Statement: Why does #MIX in a weight-based model provide the total volume of a stream or a tank? | Solution: The way #MIX works, for both tanks and streams, is that it is not based on the type of a model but on the keyword
WGT or VOL present as the first property listed in the #RESULTS row of a User Unit.
If the property is WGT the values in the #MIX will be in weight, and if it is VOL (or even any other property) the results of #MIX will be in volume.
Keywords: Â #MIX
#RESULTS
Weight based
Volume based
References: None |
Problem Statement: Is there a reason that Ammonia Carbonate ((NH4)2CO3) is not in our database? And not in the chemistry? | Solution: This compound can exist in crystaline form as a double salt of ammonium bicarbonate (Ammonium hydrogen carbonate NH4HCO3) and ammonium cabamate (NH2COONH4), or it can exist on its own. However, it breaks down very easily when exposed to air. InSolution, it is even more unstable.
We have included an ammonia example with the Aspen Plus installation. The file is located in the \Aspen Plus Vx.x\GUI\App\Ammonia\ directory, or from the User Interface, open to Favorites/Applications/Ammonia.
The pdf file describes that reactions of CO2 with NH3 and water that we think exist. These reactions do not involve Ammonium Carbonate but Ammonium hydrogen carbonate (ammonium bicarbonate). In fact, ammoniun carbonate breaks down into Ammonium bicarbonate & ammonium carbamate.
This can be used as a starting point for users.
Keywords: None
References: None |
Problem Statement: How can I change the routes of an activity coefficient model such as NRTL to use one set of binary interaction parameters for the fugacity calculation for vapor-liquid equilibrium (VLE) and another for the excess enthalpy (HXS)? This may be needed to address the limitation that a single set of binary interaction parameters does not fit both the VLE and enthalpy data. | Solution: Attached is an Aspen Plus V7.1 file which shows how to use a second data set for liquid enthalpy calculations with NRTL.
A number of changes need to be made:
1. A new route for liquid mixture molar enthalpy departure (DHLMX) has been created under Properties | Advanced | Routes. This is a copy of the corresponding NRTL route DHLMX86 where we have set the data set to 2 for the GAMMA model.
2. Another route for liquid mixture molar enthalpy (HLMX), copied from HLMX86 (NRTL) has been created and the route DHLMX has been set to the new route DHLMX.
3. A new property method P-1 has been created under Properties, Property Methods. This is a copy of the NRTL method
4. In this new property method, the route for HLMX has been changed to the new HLMX route.
5. For consistency with other properties, also modify the liquid mixture molar Gibbs free energy (GLMX) route. Create a new route for the liquid fugacity coefficient of a component in a mixture (PHILMX), copied from the NRTL PHILMX86 route, to change the data set for the GAMMA model. Create a new route for the liquid mixture molar Gibbs free entergy departure (DGLMX) to use the new PHILMX route, and finally a new GLMX route to use the new DGLMX route. This will update both the Gibbs free energy and entropy of the liquid phase to use the second set of binary interaction parameters.
The NRTL binary interaction parameters in data set 1 (NRTL-1) are for the vapor-liquid equilibrium and the parameters in data set 2 (NRTL-2) for the enthalpy calculation.
Please note that the regression system in Aspen Plus can only regress the first set of binary interaction parameters, so you may have to create multiple regression files to regress separately enthalpy and VLE data. The modifications above will allow to use two sets of binary interaction parameters for simulation purposes.
For checking purposes, note that Aspen Plus evaluates the excess enthalpy property set correctly with NRTL (HXS) but not the excess Gibbs energy (GXS). This is only a reporting issue but it may still be annoying (e.g. if you want to plot the GXS property - it shows 0). TheSolution is to create a new GLXS route to use the data set 2 for GAMMA. You can create another GLMX-XS route to evaluate GLMX with the method 2. This forces the evaluation of GXS. The property model P-2 is a copy of P-1, with the route for GLMX changed to GLMX-XS. You can see in the property table PT-2 that GXS is zero, but GMX is identical to PT-3 (PT-2 uses P-1 property method, PT-3 uses P-2 property method). This demonstrates that the actual property GMX is calculated correctly, but GXS is only calculated with the method 2 is used for GLMX. There is no such issue for HXS.
A similar approach could be used for other non-electrolyte activity coefficients.
Keywords: None
References: None |
Problem Statement: Where Can I see Unit Operation Summary in Aspen Plus? | Solution: After running the simulation, users can see Unit Operation Summary using one of the following methods listed below:
On Tool Bar select Data Browser | Results Summary | Unit Operation Summary
Click on Check Results short cut icon then select Unit Operation Summary
Click on Block Summary Grid icon
The Block Summary Grid displays a summary of the data for unit operation models, input values are highlighted in blue and results are displayed in black.
The grid allows the user to change the input values in one convenient place.
Keywords: Block Summary, Unit Operation Summary, Block Input, Block Results etc;
References: None |
Problem Statement: How consistent are the results from tray sizing in RadFrac? If I size a tray and then rate it, I get varied results. | Solution: These issues resulted primarily from the complexity of the design equations and the simplifications suggested by the tray design brochures to deal with these complexities. The simplifications were needed because computers had not come into widespread use at the time of the publication of these design procedures.
Trays can either be sized or rated - sizing implies the design of a new tray while rating implies evaluating the performance of an existing tray. Rating is much easier to do than sizing because, in addition to the flows and physical properties of the streams, one knows the detailed geometry of the tray. Sizing is much more difficult. For a relatively complete picture of the tray during sizing, one has to determine not only the diameter, but the widths of all the downcomers, the weir lengths of all the panels, and the flow path length. These calculations involve a number of coupled equations and a fair amount of iteration. In order to avoid this complexity, the design manuals often suggest less complex (and therefore less accurate) methods for sizing a tray. These sizing procedures were meant for initial sizing only...in order to give the designer a feel for the tray. Unfortunately, if you rate the tray you just designed using the detailed (and relatively easy) methods available to you, you often discover that the rating calculations are pretty far off from the sizing calculations. In fact there is no reason to use the simplified design methodology for sizing if you have a computer available. Given that statement, however, the original programming used the simplified methods for sizing and the complete methods for rating.
In V7.2, we have done away with the simplified methods for tray sizing and implemented the exact same set of equations for sizing and rating. Now, when you size a tray in Aspen Plua, and then put the sizing results in a rating block, you'll get back virtually the same performance in both cases. I use the term virtually because Aspen rates a tray on a panel by panel basis, while sizing takes place on the tray as a whole. This is not a problem for 1 an 2 pass trays. It is only a bit noticeable for 3 and 4 pass trays. Further, if you look at the Aspen report file for a column, you'll now find reported the individual downcomer areas, the weir lengths, and the flow path length. The results for rating and sizing are now much more consistent.
Keywords: None
References: None |
Problem Statement: Will Related Equipment effect equipment availability?
Note: related equipment refers to equipment listed on the Related Equipment Tab under the Data/Equipment Dialog. | Solution: Related Equipment will not be used for equipment availability checking. It is only used for documentation. These pieces of equipment are listed in the Equipment Data spreadsheet.
Keywords: Equipment
Availability
Schedule
Releated Equipment
References: None |
Problem Statement: What is the difference between Conventional and Non-conventional Solids? | Solution: Conventional solids are pure materials specified using the Solid component type. These solids may be part of the stoichiometry for simple or kinetic reactions. These solids can be used in the MIXED or in the CISOLID (Conventional Inert Solid) substreams.
Conventional solids are characterized in terms of properties, such as:
· Molecular weight
· Chemical formula
· Vapor pressure
· Critical properties
The solid properties are modeled using solid property models such as Solid Antoine Vapor Pressure, General Pure Component Solid Heat Capacity, and Pure-Component Solid Enthalpy Polynomial. If the component also exists in the liquid or vapor phase, it should be specified as a second component with a type of conventional. The properties for this component will be calculated using the liquid and vapor property models.
Electrolyte chemistry reactions can only be specified using solid salts in the MIXED substream.
EO formulations of Mixer, Flash2, Flash3, Decanter, Pump, FSplit, SSplit, Mult, Dupl, Selector, and Streams support solids in the MIXED substream. Others will issue a warning if they are found, and depending on the properties available for the components in question, may either lead to errors or calculations with wrong results that treat these components as being in another phase.
The SFRAC property will report the fraction of solids, which may include both salts and conventional inert solids, in the MIXED substream.
If a conventional solid is in the CISOLID substream, it does not participate in phase equilibrium calculations or electrolyte chemistry calculations. Conventional inert solids can participate in the equilibrium modeled by the RGibbs unit operation model to predict solid or salt formation from vapor or liquid. None of the other unit operation models handles solid phase equilibrium. Conventional solids in CISOLID substream can participate in kinetic and stoichiometric reactions.
For most blocks, solids will stay in the substream they started in. RStoic can be used to move solids between the MIXED and CISOLID substreams. Solid products of REquil and RGibbs will be placed in the CISOLID substream if it is available, and the MIXED substream otherwise.
Nonconventional Solids
Nonconventional solids are materials characterized in terms of empirical factors called component attributes. Component attributes represent component composition by one or more constituents.
Nonconventional solids do not participate in phase equilibrium. They can be used in an RStoic for chemical equilibrium calculations. Aspen Plus always assigns substreams of type NC to nonconventional solids.
Examples of nonconventional solids are coal and wood pulp.
Keywords: Nonconventional, Solids, Conventional
References: None |
Problem Statement: What are the options to simulate a batch recipe in Aspen Batch Plus? | Solution: Prior to Aspen Batch Plus version V7.2 there were three (3) ways to simulate a batch:
1. Select Simulate Entire Batch from the RUN toolbar, this is equivalent to Simulate Batch, but additional options to choose the specific operations or range of operations. RECOMMENDED method to simulate a batch.
2. Select Simulate Batch from the RUN toolbar. This only simulates operations downstream of any user modification, i.e. it does not simulate the entire batch. (It is equivalent to the play button in earlier versions).
3. Click on the PLAY toolbar button. This button is now mapped to the Simulate Entire Batch run, i.e the ENTIRE batch is simulated.
As of Aspen Batch Plus version V7.2 upwards, the run options changed. There are now two (2) ways to simulate a batch:
1. Select Simulate Entire Batch from the RUN toolbar. This simulates the ENTIRE batch and is the RECOMMENDED method.
2. Click on the PLAY toolbar button. This button is mapped to the Simulate Entire Batch run, i.e the ENTIRE batch is simulated.
The option PLAY toolbar button, sometimes the entire batch is NOT simulated and known to have some issues. If you use this run option, please check the results very carefully.
Keywords: Run
Simulate Batch
Simulate Entire Batch
References: None |
Problem Statement: Where can I find the Aspen Batch Plus Getting Started Quickly Tutorial? | Solution: The Getting Started Quickly Tutorial is included on the installation CD and can also be found via the online help. To access the Getting Started Quickly Tutorial, follow the steps below:
1. Open a blank or any existing Aspen Batch Plus project
2. Go to 'Help' under main menu, then click on 'Help Topics'
3. Under help topics expand Getting Started tree to find 'Getting Started Quickly Tutorial'
An example file also included with the installation CD and can be found in Aspen Batch Plus Installation folder on your system. The corresponding path is typically C:\Program Files\AspenTech\Aspen Batch Plus 2006\Projects\Examples.
In 2006.5, the path to the Examples Project was changed. It is now located in the users' profile, eg: C:\Documents and Settings\All Users\Application Data\AspenTech\Aspen Batch Plus 2006.5\Projects\Examples
Note: You may have to get administrator rights to view and use the folders and files in the Application Data folder.
Keywords: Getting Started Quickly Tutorial, Batch Plus, Getting Started Manual.
References: None |
Problem Statement: What emission models should I use if I have Nitrogen gas sweep
What happens if I have conservation vent
What to do if I have vessel which has sweep going on but no operation is taking place
What does additional Sweep in Advanced button mean | Solution: A1. For everything but MACT, Sweep model should be used. For MACT, MACT Purge model should be used.
A2. If after start sweep, the conservation vent on, or if you set up a blanket pressure, then the sweep emission will be zero. Because the way conservation vent works is that, it is normally closed except when the pressure reaches the blanket pressure you have entered.
A3. If you have sweep going on for multiple vessels, and some of the vessels are idle, that is, although the sweep is generating emission, but since there is no operation going on in the those vessels, there is no way to link the emission model to operation. Here is what you should do: put a parallel keyword for those idle vessels. Then put dummy operation like Age, and get sweep going to mimic the sweep emission.
A4. In Advanced button for Sweep models, there is a fudge factor called addtional sweep. If you leave it blank or put down zero, that means the Sweep emission is as calculated by sweep emission models. Positive number will add to the sweep emission and negative number will take the emssion off.
Keywords: sweep
emission
vapor emission
purge
References: None |
Problem Statement: Custom Excel Report Example | Solution: Custom Report Example: Charges
We will build a custom report that shows a summary of all the input materials for a step.
Here is an example output report, using the Intermediate B (Pilot Plant) step from the Examples project that ships with Batch Plus.
We are not suggesting that one generally wants a finished result with this many different colors and some of the text in italics. We chose a broad range of formatting to show what is possible. You define the formatting in your report template (XLT) file, and it is applied each time you generate a report from that template.
This example shows how to:
- Use the Filtering capabilities in the Report Specification tool.
- Combine information from two different queries from the Report Specification tool into a single result, using Excel's Lookup functions (to get the CAS Numbers).
- A simple way to build a report template with NO Visual Basic programming!
We include the Charges.XML and Charges.XLT files with this document.
The remainder of this document shows how to
- Build the Report Specification (XML) file
- Build the Report Template (XLT) file
- Save the Report Template
- Save the Report Specification
- Use the Report Specification and Template to Generate a Report
Building the Report Specification
We need to build two separate report queries:
1. Step Materials - Retrieve information on all materials in the step, including the material names and CAS numbers.
2. Results Stream Summary - Retrieve information on the ?input streams? to generate the majority of the data items in the table.
Our Excel template will combine information from these two queries.
Step Materials Query
This query uses the following fields from Material List information in the step:
- Name
- Type
- Alias
- CAS Code
Here is an example result in the Report Specification tool:
Note that we really need only the Name and CAS Code. We include the other fields to make the data a little more complete. We will use Excel's Lookup functions to retrieve only the CAS Codes. We need to use a Lookup function regardless of the number of fields we retrieve, so adding more does not hurt.
Results Stream Summary Query
This query uses the following fields from Stream List information in the step results:
- Material
- Volume
- Mass
- Operation Details \ Unit Procedure Sequence Number
- Operation Details \ Operation Sequence Number
We will specify two filters for the list:
1) Select only streams where the Type is Input. Here, we use the Simple Filter.
2) Select only streams where the material is not NITROGEN and not AIR. Note that we use the Free Text Filter for this case.
Here is an example result in the Report Specification tool:
Now we click Export to create the Excel spreadsheet. We choose ?No? when asked if we want to choose an Excel template. We will edit the output spreadsheet to produce a report template to accompany this report specification, then save it.
Building the Excel Template
We would like to create a new sheet, named Charge, and adjust the way information is displayed there.
Here is the Excel output produced by the Export:
Here is the finished template:
To build the template:
We insert a new (empty) worksheet. Change its name to ?Charge.?
We decide that we will allow for 50 charge streams. This lets us keep the process of building the template simple, without resorting to any Visual Basic programming to adjust table sizes, etc. You can see the numbers in column A of the result.
We use the named ranges that Batch Plus automatically defines to reference the information we want.
For example, we concatenate the Unit Procedure Sequence Number and the Operation Sequence Number to get the Operation designator in column B. Here is the formula for all the cells in column B (except the heading in B1):
=IF(ISERROR(_r_QryRptStreamSummary_UnitProcedureSequenceNumber),??,_r_QryRptStreamSummary_UnitProcedureSequenceNumber&?.?&_r_QryRptStreamSummary_OperationSequenceNumber)
Note that we use ISERROR to insert empty strings (??) into the cells after we ?run off the end? of the named range.
To get the range names, we don't type the long text into the formula, we start typing the formula and then choose Insert | Name | Paste from the menu:
Here are the formulas for the remaining columns:
C:
=IF(ISERROR(_r_QryRptStreamSummary_MaterialName),,_r_QryRptStreamSummary_MaterialName)
D:
=VLOOKUP(C2,_s_QryRptStepMaterials_MaterialName:_s_QryRptStepMaterials_CASCode,4,FALSE)
E:
=IF(ISNA(D2),,IF((D2=0),,D2))
F:
=IF(ISERROR(_r_QryRptStreamSummary_Mass),,TEXT(_r_QryRptStreamSummary_Mass,0.00)& &_r_QryRptStreamSummary_MassUOM)
G:
=IF(ISERROR(_r_QryRptStreamSummary_Volume),,TEXT(_r_QryRptStreamSummary_Volume,0.00)& &
_r_QryRptStreamSummary_VolumeUOM)
Column D does the Lookup for the CAS Number. Note the way we specify the range that defines the Lookup Table, using two of the named ranges defined by Batch Plus:
_s_QryRptStepMaterials_MaterialName:_s_QryRptStepMaterials_CASCode
As you can see in the figure, the result = 0 if the material name is valid, but we have not defined a CAS Number (e.g. for the mixtures). The result = #N/A if there is no material in column C. We then ?clean up these two abnormal results in column E.
Finally, we add the formatting to each column and draw the grid. Then we hide column D. So we have:
Saving the Report Template
Note that the default location for report specifications is C:\Documents and Settings\username\Application Data\Aspentech\Aspen Batch Plus 2006\Templates\Reports. However, you can store your report specifications (XML) and templates (XLT) anywhere you wish. You need to put the XLT in the same place where you put the corresponding XML.
We use Save As to create the template.
CAUTION: In Excel's Save As dialog, when you choose XLT as the type, changes the default location to C:\Documents and Settings\username\Application Data\Microsoft\Templates. Be sure you browse to the correct location AFTER you set the file type!
Once you save the XLT, exit from Excel.
Saving the Report Specification
Now that the template is done, we can export the report specification (.XML) file to save it for later use. The reason we save the report specification after the template is that we want to hide the data sheets in the final report. So, we set the Hide Data Sheets option at the lower right of the Report Specification Tool:
Then we export the report specification:
Note that the default location for report specifications is C:\Documents and Settings\username\Application Data\Aspentech\Aspen Batch Plus 2006\Templates\Reports.
Once you export the XML, exit from the Report Specification tool.
Using the Specification and Template to Generate a Report
To generate a report, choose it from Results | Excel Reports | Custom Report.
Choose Open and navigate to the XML.
Remember: the default File Type is BPR, so change it to XML first, then select your report.
Here is the result:
Note that all the tabs except Charges are hidden.
Finally, note that once you have Opened a given XML, it will stay on your Most Recently Used Custom Reports list. So, when you open the menu again, it will already be there:
Keywords: Custom
Custom Export
Custom Report
Custom Excel Report
References: None |
Problem Statement: I am running an input file from the Aspen Plus Simulation Engine Window. Is there a way to look at the results that are in the summary (.sum) file? | Solution: Open a new blank simulation.
Go to File Import and then select Summary file in the bottom right for the file type:
Then, the results (including the process flowsheet diagram) will be read into the simulation. There will be lots of red circles to indicate no input, but the results will be there.
You can copy and paste tables or other values to Excel.
Keywords: None
References: None |
Problem Statement: While using certain Operations such as Decant or Separate, the streams that are categorized as a Waste Stream do not appear on the Waste Stream Table Excel report. | Solution: Only output streams that are categorized as a Waste Stream AND sent to an inventory location will be reported in the Waste Stream Table Excel report.
For example, refer to the Pharmaceutical A (Example) Process in the Examples.prj file located in the Batch Plus install directory (default location: C:\Program Files\AspenTech\Aspen Batch Plus 2006\Projects\Examples).
In the Decant Operation (2.9) the Upper Layer Transfer Stream will be reported as a Waste Stream in the Waste Stream Table Excel Report by doing the following:
1. Open the Decant Operation window.
2. Go to the Optional tab and click on the Upper Layer Transfer Stream button.
3. Specify a waste stream category (e.g. High BOD Waste) using the stream category drop down list.
4. Specify equipment (e.g. Storage) from the is sent to drop down list. The equipment MUST be of Equipment Class Inventory Location.
If the user sends this stream to equipment NOT classified as inventory location, then the stream becomes an intermediate stream that remains in the process. As a result, it is not an output stream and will not show up in the Waste Stream Table Excel Report.
Note that if the user leaves the is sent to field blank, then by default Batch Plus will send the waste stream to Unspecified Inventory Location and the stream will be reported in the Waste Stream Table Excel Report.
Keywords: Waste stream report, waste category
References: None |
Problem Statement: Assumptions made in “Fluidbed” for modeling of chemical reactions. An explanation of how to add them to the unit. | Solution: In Aspen Plus, the fluidized bed model considers two different zones: the bottom zone characterized by high solids volume concentrations, and the upper dilute zone in which the solids volume concentration decreases with increasing height. The bottom zone is modeled as a bubbling bed according to Werther & Wein, and the upper dilute zone follows the approach according to Kunnii & Levenspiel. These fluid dynamic models are used with other correlations (see the picture below) to describe the distribution of solids along the fluid bed, and for entrainment considerations.
With regard to chemical reactions, the model makes the following assumptions:
• Gas in plug flow
• Solids ideally mixed
• Each balance cell is considered as CSTR
That is, the fluid bed is discretized in a number of divisions (customizable by the user) along the height of the reactor, with different quantity and profile of solids. In each balance cell, flow conditions are considered as CSTR. The gas going through all this sequence of CSTR cells will show a flow model similar to plug flow.
In terms of reactions, Aspen Plus doesn’t take into account the existence of any bubbling or emulsion phases that are described in the bubbling model whatsoever, just solids and gases perfectly mixed, with homogeneous conditions thorough the whole volume of each balance cell division. Film resistance phenomena between phases is not considered, therefore, user should work with kinetic parameters either based on apparent reaction rate for diffusion-controlled reactions or real kinetics when external and internal transport limitations don’t exist. The fluid dynamic models are considered to obtain the distribution of solids in each cell.
In order to add fluid-solid reactions to a fluid bed, take the steps as follows:
1) Go to Reactions in the left panel and create a new set of reactions.
2) Define stoichiometric coefficients and exponents for your reactions, and use the following criteria for solid components:
• Participate in reactions and control the reaction rate: enter both stoichiometric coefficients and exponents.
• Participate in reactions without controlling the reaction rate: only the stoichiometric coefficients for these solids, without entering exponents.
• Act as catalysts by controlling reaction rates without participating in the reactions: only the exponents for these solids, without entering stoichiometric coefficients.
• Are inert: neither stoichiometric coefficients nor exponents.
3) Enter parameters for the reaction rate expression:
The volume of the reacting phase selected will be taken as the basis of the reaction rate. In solid-vapor reactions, the volume that solid particles occupy is normally insignificant compared to the vapor-phase volume, so that for these reactions select vapor as reacting phase. With liquid-solid reactor you can select liquid & solid or only liquid. Choose the one according with the basis of your kinetic data.
4) When specifying information for reaction expressions, solid components can either be included or ignored in the denominator term of concentrations. To control how these calculations are performed, use the Solids button on the Kinetic sheet of your Reaction ID. Once again, the selection must be consistent with the kinetic parameters of your reaction rate equation.
5) Open the reactions input form of the fluidized bed, select the set of reactions created and add it to the model.
6) The effect of reactions in the particle size distribution can be also specified. Please note that he PSD defined in this form is the PSD of the combined reaction product. The solids with this PSD are subsequently separated by elutriation within the fluidized bed.
The different options are explained in the scheme below:
Blocks / Fluidbed / Input / PSD tab
Keywords: Fluidized bed, fluidbed reactions, solids, gas-solids reactions, liquid-solids reactions, PSD, heterogeneous reactions.
References: None |
Problem Statement: The default format setting that Microsoft uses in ExceI cells is General. The General format automatically converts cell contents that look like dates into Excel's internal date/time format. This not only changes the way that the date looks to users, but it also changes the cell's actual value. Excel internally represents dates as numbers, where a difference of 1.00 represents a difference of one day. January 1, 1900 is represented by 1.00, January 2, 1900 is represented by 2.0, etc.
For example, if you enter 6-1 into an Excel cell (on an English - U.S. system), then Excel will:
1. See the 6-1 and assume that you are entering a date.
2. Excel will then convert the 6-1 text into its own internal date format (for June 1, 2009, the internal representation would be the number 39965.0).
3. Excel will apply the current default date formatting to the cell and display something like 6/1/2009.
This is relevant for ASW because, in rare cases, Excel could make unwanted conversions of your table entries and cause problems. For example, if you have a model variable table which has a name column, and the name of the variable was set to 6-1, then Excel could try to convert the 6-1 to 39965.0 . | Solution: To avoid this, you can manually set the format of the relevant Excel cell(s) to Text format instead of General. This will cause Excel to display the text entered without any conversions. In Excel, you can format a cell to Text format by doing the following:
1. Select the cell(s) in Excel that you want to format.
2. Right-mouse-click the cells and select the 'format cells' option.
3. Select the number tab.
4. Select the 'Text' category from the 'Category' option list box.
5. Click OK.
Keywords: None
References: None |
Problem Statement: While your Aspen Orion-XT Model is running on MS SQL / Oracle Server, how to convert the model in to MS Access Database using Aspen Orion-XT in built feature. MS Access version of Model is highly portable, when sending the model to others or AspenTech support engineer. | Solution: Aspen Orion-XT has Model Archiving feature which creates a MS Access Version of the Model from MS SQL or Oracle Version.
Model Archiving can be accessed through File || Archive Model Option. The output of the Archiving included MS Access version of Model, Units.xls and other optional model files in a ZIP file format.
Keywords: Archive
Model
Database
Oracle
SQL
Convert
migrate
References: None |
Problem Statement: What does Solid Red Circle sign represent in Text Recipe? | Solution: The solid red circle displayed on the Text Recipe is NOT a warning/error message icon/sign.
Under Advanced Simulation (View | Toolbars | Advanced Simulation Toolbar), the user can insert breakpoint(s) in the recipe. A breakpoint in the recipe is indicated by a red dot next to the Operation. When you simulate to a breakpoint, the simulation algorithm simulates all Operations up to and including the Operation just prior to the Operation with the breakpoint. A simulation stopped at a breakpoint is indicated by a yellow arrow next to the red dot. You can search for 'breakpoint' in Help for more details.
Keywords: Red dot, red circle, sign, icon
References: None |
Problem Statement: After reporting the equilibrium constant (Keq) in an REquil block, how can this value be entered in Reactions for an equilibrium reaction to be used in RCSTR? What basis should be used for a liquid phase reaction? | Solution: The internally calculated Keq uses the ideal gas as the reference state, and the reference state fugacity is taken as 1 atm. Hence, for a liquid reaction, there is no corresponding Kbasis since we imply that any such reference state is lumped to the left side, and we then describe how we calculate the right side. The closest would indeed be FUGACITY basis.
To reproduce the same Keq, you need to modify the Keq from REQUIL and add to it sum (stoic_coeff) * ln Pref, where the stoic_coeff is positive for products, negative for reactants, and Pref is 101325 Pa (=1 atm).
So, ln Pref = 11.5261.
Keywords: None
References: : CQ00428374 |
Problem Statement: In RadFrac pack rating and sizing sections, one can specify the type of material. What does STANDARD as a packing material stand for? For example, the BX packing has STANDARD and PLASTIC as the options. | Solution: The STANDARD packing material stands for metal.
Keywords: None
References: : CQ00431013 |
Problem Statement: When salt solubility parameters (K-SALT) are regressed for one solvent, do they apply when other solvents are in the mixture also? | Solution: When K-SALT is used as an adjustable parameter in the solubility calculations, it is directly related to the mole fraction and activity coefficient of the solute at saturation regardless of how many solvents in theSolution. The following paper describes this concept (equations 1-3). It is correct that K-SALT together with NRTL interaction parameters will be able to cover any combination of a defined solute with multiple selected solvents.
From Chau-Chyun Chen and Yuhua Song, Solubility Modeling with a Nonrandom Two-Liquid Segment Activity Coefficient Model, Ind. Eng. Chem. Res. 2004, 43, 8354-8362:
Solubility Modeling
The solubility of a solid organic nonelectrolyte can be described by the expression
(1)
for T <= Tm
(2)
where xiSAT is the mole fraction of the solute i dissolved in the solvent phase at saturation, DfusS is the entropy of fusion of the solute, giSAT is the activity coefficient of the solute in theSolution at saturation, R is the gas constant, T is the temperature, and Tm is the melting point of the solute. Given a polymorph, DfusS and Tm are fixed. At a fixed temperature, the solubility is only a function of the activity coefficient of the solute in theSolution. Clearly, the activity coefficient of the solute in theSolution plays a key role in determining the solubility.
Equation 1 is a simplified expression for solubility. It ignores the contributions due to the difference between solid and liquid heat capacities at the melting point and due to the pressure correction. When the values of DfusS and Tm are not available, the solubility product constant, Ksp, can be introduced into eq 1 as an adjustable parameter for data regression:
(3)
Ksp corresponds to the ideal solubility of the solute.
Keywords: None
References: None |
Problem Statement: When a heat curve is created in a column I get the following warning
COLUMN CALCULATIONS INVOLVE REACTIONS OR EFFICIENCY SPECIFICATIONS HCURVE RESULTS MAY NOT BE CONSISTENT WITH COLUMN RESULTS. | Solution: Heating/cooling curve calculations do not include reactions or column efficiencies that may be specified in the block. When heating/cooling curves are specified in the presence of such features, you may see this warning.
The heating/cooling curve will still calculate results, but because they do not consider the reactions and/or efficiencies, they may not match the results of the block.
Keywords: hcurve,
References: None |
Problem Statement: I like using the shortcut keys rather than the mouse. Are the traditional shortcut keys still available in V7.3.2? | Solution: The traditional shortcut keys (based on key combinations involving Ctrl and/or special keys such as F1 through F12) still exist, and as much as possible are unchanged from previous versions. In the tooltips for ribbon commands, these shortcuts are shown wherever they exist.
See the help topic Using the Keyboard for a list of these shortcuts. From the Help Contents go to Using Aspen Plus | Using the Keyboard. This list is also attached as a .pdf.
Keywords: None
References: None |
Problem Statement: How to create a custom table template in Aspen Simulation Workbook? | Solution: Aspen Simulation Workbook allows to create quick table based on customized pre-configured template. Follow the steps given below to create your own template:
1. Open the Organizer, and then click Create Quick Table button
2. Select <Manage Templates...>
3. Click New on the Manage Table Templates form
4. Give a name for the new template
5. Use the Table format to set the format of this template
6. In the Columns tab click Add button to add the desired Attributes, such as Value, Units
To apply the custom template, click the Create Quick Table button in the organizer and choose the template you have already created.
Note that the templates are saved and accessible within the current ASW file only. If you want to use the custom templates, these must be exported with .ASWTT extension and imported in the new ASW session.
Keywords: Quick Table, Custom Template
References: None |
Problem Statement: Sometimes, a user need to determine if an Aspen HYSYS solve has completed. How can this be done? | Solution: There are three cases to consider:
(1) Performing a Standard Aspen HYSYS Solve (not involving HYSYS Optimizer)
Use the ?SolverIsRunning? property of the simulation object to determine when the solve is completed.
See attached code for examples of how to do this: DetectWhenHysysSolveDone_20110228a.xls (V7.2 ASW Workbook), modCheckWhenHysysSolveDone.bas (code only for earlier versions)
(2) Performing an Aspen HYSYS Optimization Run (V7.2 Aspen HYSYS and earlier)
There is no simple way to find if an optimization has completed. In the attached spreadsheet, you will find the VBA macro IsActiveHysysCaseConverged(). This function polls the active HYSYS simulation and returns when it completes the optimization. The function returns a value of true if the case is converged, and false if some error happened.
A second VBA macro is also presented, IsActiveHysysCaseConverged2(timeOutSeconds As Long, ByRef errorMsg As String). In addition to the above features, this macro will let the user to set a timeout limit on HYSYS optimization, and returns a text description when an error happens.
Attached workbook/code: Hysys_Poll_for_finish_optimize_20110223a.xls (V7.2 ASW Workbook), modFindWhenHysOptimizeDone.bas (code only for earlier versions).
(3) Performing HYSYS Optimization Run in Aspen HYSYS V7.3 or Later
Starting in Aspen HYSYS V7.3, a variable is exposed that describes whether the Aspen HYSYS Optimizer is currently running. The path to this new variables is:
?Top.appmodel.variables.Case Optimizer.Optimizer Is Running?
The value of this variable can be polled to test when the optimization has completed.
Keywords: HYSYS, solve, optimization
References: None |
Problem Statement: In Aspen Batch Plus versions prior to 2006.5, the Aspen Batch Plus Project (example) folder was installed under C:\Program Files\AspenTech\Aspen Batch Plus 2006\Projects.
Where is this Project folder in Aspen Batch Plus version 2006.5? | Solution: In Aspen Batch Plus version 2006.5 the Project (example) folder is installed under C:\Documents and Settings\All Users\Application Data\AspenTech\Aspen Batch Plus 2006.5\Projects.
This change was made for Microsoft Vista compatibility.
Keywords: None
References: None |
Problem Statement: Is it possible to specify a different heat of combustion value (HCOMB) for a non-conventional component for each stream? | Solution: No, the value of HCOMB is specified for a given non-conventional component model-wide. You can specify different attributes for the component in each stream, but only one value of HCOMB can be specified. If you have different coals or components with different values of HCOMB, you must specify them as different components, e.g. COAL1, COAL2, etc. Alternatively, it is possible for the heat of combustion to be calculated from the component attributes using one of the built-in models.
The general coal model for computing enthalpy in the Aspen Physical Property System is HCOALGEN. This model uses the non-conventional (NC) attributes defined under form Properties | Advanced | NC Props.
To use the attributes, it includes a number of different correlations for the following:
Heat of combustion
Heat of formation
Heat capacity
You can select one of these correlations using an option code in the Properties Advanced NC-Props form. Each element in the option code vector is used in the calculation of a different property. See Aspen Plus online manual and pdf files for further details. For example, specifying option code 1 to be a value of 6 enables the user-entered value of HCOMB to be used for the heat of combustion rather than one of the correlations. The input value of the heat combustion, HCOMB, is specified under Properties | Parameters | Pure Component and creating a non-conventional type parameter HCOMB.
Since HCOMB is defined against individual NC components model-wide, while on the other hand, the NC attributes for feed streams are defined on Input | Component Attr form at stream level, users should make sure the involved NC components only be filled at most in 1 material stream. Otherwise a stream containing NC components with different component attributes could have same HCOMB specification, which leads to potential inconsistency.
Keywords: HCOMB, HCOALGEN, Non Conventional, Attributes, Coal
References: None |
Problem Statement: How do you model a co-current tower? | Solution: The rigorous distillation model RadFrac cannot handle a co-current tower. The work around is to use a series of flash or CSTR blocks. The only limitation is that you cannot enter an efficiency.
Keywords: RadFrac
column
References: : CQ00107185 |
Problem Statement: The user specified the default vapor emission model for a particular operation (e.g. React) under File | Preferences | Vapor Emission but failed to see the vapor emission calculation for that operation in the Vapor Emission Stream Table or Vapor Emission Detail reports. | Solution: There are MULTIPLE pieces of equipment for the same operation listed on the File | Preferences | Vapor Emission | Vapor Emission Models tab. The user has to ensure that vapor emission models are specified for the correct pieces of equipment for the vapor emission calculation to be performed.
For example, for the React operation, a vapor emission model has to be specified for the MAIN Equipment Unit under File | Preferences | Vapor Emission | Vapor Emission Models (even though the emission model for the Receiver may already be specified). Be aware that due to the window size limitation, the user may have to SCROLL DOWN the window to see all the related pieces of equipment.
Similarly, the vapor emission model for the relevant equipment can also be specified on the React Operation | Model tab.
Keywords: vapor emission model, operation, equipment, preferences
References: None |
Problem Statement: Converting PROII input file into Aspen Plus file using PROII to Aspen HYSYS Converter | Solution: 1. Browse for PROII to Aspen HYSYS Converter, go to Start | All Program | Aspentech | Process Modelling V7.2 | Aspen HYSYS | ProII to Hysys Converter
2. Once the converter has been opened, on the upper left hand toolbar, change Hysys to Aspen Plus(1). Similarly on the right side page, select Aspen Plus tab instead of HYSYS(2). Finally click the run button(3).
3
1
2
3. A command window will appear during conversion.
4. Once the conversion is complete, an Aspen Plus file will automatically open and saved in a temp folder where the PROII input file is located.
In V7.3 and higher, there will be a PROII to Aspen Plus option in the Aspen Plus folder from the Start Menu,
e.g. Start | All Program | AspenTech | Process Modelling V7.3 | Aspen Plus| PROII to Aspen Plus Converter
Keywords: ProII converter, input file converter
References: None |
Problem Statement: I have a components 5-HYDROXY-3-HEXANONE (CAS number 33683-44-2). The simulation worked fine for V7.1 and found the necessary parameters in the NIST-TRC databank. However, there were missing parameters with V7.2.
Why were the data removed between V7.1 and V7.2?
Is it possible to get the NIST V7.1 pure database with V7.2 as it is possible for the other Aspen databases?
Are the pure data available from NIST defined somewhere? | Solution: The NIST database is constructed based on pure data information stored in files send from NIST. AspenTech does not have control on how these files are generated. For this particular component, there is very little data stored in files NIST sends for use in V7.2 compared with V7.1/V7.3. The reason might be some file writing error when NIST generates these files. NIST is improving their automations progressively to prevent such errors in the future.
There are a few ways to get the data from NIST in one release to another.
1. Copy and paste the parameter from one version to another. SeeSolution 131414 for details.
2. Export a project (PRJ) report file with the data for that component. SeeSolution 110445 for details.
3. Add the NIST V7.1 database to a later version such as Aspen Plus V7.2.
To add the NIST V7.1 database to a later version such as V7.2:
1. Open Start->All Programs->AspenTech->Process Modeling V7.2->Aspen Properties->Aspen Properties Database Manager.
2. Right click Aspen Physical Properties Database V7.2, select Register Databases...
3. Type apeduser in Login Name, type Aprop100 in Password.
4. In Database:, select NISTV71. and click OK. Close the manager.
5. Start the Aspen Plus V7.2. On the Enterprise Database tab, user can select NISTV72 NIST-TRC databank now.
It is also possible to use NIST TDE to dynamically retrieve parameter and experimental data for this component. To do that, execute the following steps:
1. Open a blank simulation, select this component.
2. On the toolbar, click TDE icon (NIST Thermo Data Engine).
3. On the pop up form, select Select this component and click Evaluate now button.
4. After few seconds, a result form will show up, hosting many properties with parameters and experimental data.
5. Users can then save these information to the Aspen parameter form or data form.
Keywords: None
References: None |
Problem Statement: What is the difference between the Harwell spline fitting method and the Hermite method? | Solution: You can specify the spline fitting method for distillation curves. Spline fitting is used for interpolation of the curves.
The Harwell method is the default. The Hermite method enforces monotonicity between points, and prevents the minimum/maximum from falling between points, as occurs for the Harwell method above. The Linear method uses linear interpolation between the points on the distillation curves, and is recommended when the distillation curves contain many closely-spaced points. Hermite is recommended for most assay analysis cases.
In the compressor block (Compr), the methods are the same ones available for assay analysis. The Hermite method, which enforces monotonicity between points, is the default.
Keywords: compr, assay
References: : CQ00705378 |
Problem Statement: Why DPN (Number Average Degree of Polymerization), DPW (Weight Average Degree of Polymerization) and PDI (PolyDispersity Index) are calculated twice in Cumulative Chain Length Distribution curve? | Solution: To see the Chain length, please select the product stream > Chain Size Distribution
The figures on the right are calculated from method of moments, the ones on the left are calculated numerically from the MWD curve. They should match reasonably well (these do) but not exact because there is round off error from discretization. If there is a big difference it may mean the MWD curves are not valid because some assumption is violated. For example high levels of branching or cross linking or random scission reactions can cause discrepancy. Moments values are more correct. The area under the curve should be near 1.0 as a secondary check.
Key Words
Chain, Moments, Distributions
Keywords: None
References: None |
Problem Statement: Is it possible to perform emission calculations for operations such as Distill/Concentrate, where the contents are at its boiling point? | Solution: The emission equations should all fail when you are at or above the boiling point of the vessel contents. This is one of the reasons for the process condenser designation. If the vessel is at the bubble point then every condenser up to the one which lowers the temperature below the bubble point, or all condensers before vacuum devices can and should be designated as a process condenser. The condenser temperature is then used in the uncontrolled emission calculation to calculate the saturation level of VOC's in the uncondensable stream. This prevents failure of the equation by eliminating the term in the denominator of system pressure minus the sum of component partial pressures.
It is possible in Batch Plus to specify a condenser as a process condenser in the properties of the emission control device. This condenser though is then always used as a process condenser instead of only the cases where the operation requires boiling. It is better practice to let Batch Plus dynamically decide in which operations a condenser is a process condenser. This can be done by specifying the Process Condenser Determination as Automatic in Preferences | Vapor Emission | Model Parameters. The setting will overide any designation on an individual condenser as a process condenser and use the necessary EPA rules to apply the designation per operation.
The user should also note that when a condenser is used as a process condenser it is considered to be a part of the vessel. If the emission control path assigned to ST-A includes condenser1 followed by scrubber1 and ST- is involved in a concentrate operation (vessel at the boiling point), then the emission streams will be shown as ST-A to scrubber1 and scrubber1 to nothing/atmosphere/vent-ID. The first emission stream, uncontrolled emission, will take into consideration the condenser and be at the temperature specified in the condenser emission control detail dialog, but is not individually reported as an emission control device for this operation because it is acting as a part of the vessel.
Keywords: Vapor Emission
References: None |
Problem Statement: What does Aspen Batch Plus do with the density supplied for a predefined mixture. | Solution: The density of a predefined mixture is only used when charging the mixture to a vessel using the Charge operation. The density is used to convert the charge amount, if specified on a volume basis, to a mass and mole basis. The predefined mixture density will only show in the charging stream. Once the mixture is in contents, the density will be calculated based on mixing rule and the pure component densities. In other words, the mixture density supplied will be lost.
Keywords: density
pre-defined mixture
References: None |
Problem Statement: How do I run Aspen Plus with DLLs generated by Intel Visual Fortran (IVF) Composer XE (IVF 12) on a computer with no IVF compiler and Microsoft Visual Studio installed? | Solution: In order to run .dlls compiled using a program such as Intel Visual Fortran, you need to have the runtime or redistributable libraries installed in the system directories. Generally, these libraries are installed with Aspen Plus; however, sometimes for newer versions of programs, it may be necessary to download and install these libraries (which are typically available on the website for that program, e.g. Microsoft or Intel).
Intel Visual Fortran Composer XE (IVF 12) has a different structure of runtime library compared to previous versions, such as IVF 9, 10 or 11. The runtime library Aspen Tech delivered with Aspen Plus which works with IVF 9, 10 and 11 does not work with the DLLs generated by IVF Composer XE. The following workaround can be used to enable your Aspen Plus (e.g versions V7.3, V7.2, and etc.) work with the DLLs generated by IVF Composer XE without having IVF compiler and Microsoft Visual Studio installed on your computer:
1. Install IVF 12 runtime library. This can be downloaded from their website: http://software.intel.com, by searching for redistributable libraries for Visual Fortran Composer XE. Attached zip file w_fcompxe_redist_msi_2011.1.104.zip is from their website with runtime libraries for both 32 bit and 64 bit machines. Double click on either of them to install the package.
2. Copy the files from \Program Files\Common Files\Intel\Shared Libraries to \Windows\system32 for a 32-bit machine,
or, from \Program Files (x86)\Common Files\Intel\Shared Libraries to \Windows\SysWOW64 for a 64-bit machine.
3. Install Microsoft Visual Studio 2010 C++ runtime library. It can be downloaded from the Microsoft downloading center. Attached zip file vcredist_x86.zip is from their website. Double click on the .exe file to install the package.
Fixed in Version
These libraries will be installed automatically during installing in the next version of Aspen Plus.
Keywords: Intel Visual Fortran Composer XE
References: None |
Problem Statement: MS Excel fails due to Aspen Simulation Workbook (ASW) plug-in - Need to disable Aspen Simulation Workbook for all users on a shared system | Solution: For a single user do the following:
There will be keys starting with ASWXLAddinLoader under:
<>HKEY_LOCAL_MACHINE\SOFTWARE\Microsoft\Office\Excel\Addins
The above keys should be deleted.
To remove ASW for all users on a machine do the following:
You have to delete the ASWXLAddinLoader key for all users under HKEY_USERS as follows:
HKEY_USERS\*\Software\Microsoft\Office\Excel\Addins that should be deleted.
Keywords: Excel
Addins
ASW
References: None |
Problem Statement: How to restore windows opened on a disconnected secondary display to the primary display. | Solution: When working with APC software on a computer with two or more displays, the user might have opened various windows from the APC software on either displays. If the second display is removed, it is possible that some of the windows may still be opened on the removed display thus not being accessible from the primary window.
To bring back the orphaned window, either:
·  Right click on the task bar and click on cascade windows. This would put all the opened windows in cascaded.
·  or, Select the orphaned windows in the task bar. Press Alt+Space and then M to access the move command for the orphaned windows and use the arrow keys to it back to the primary display.
This also work if the windows is internal to the main application (such as DMCplus Build entry editor).
Keywords: Disappeared windows, Multiple displays, APC offline tools
References: None |
Problem Statement: When you start Excel you receive a message that the Aspen Simulation Workbook (ASW) Add-in failed to connect to Excel.
One thing that can cause the ASW Add-in to fail to connect to Excel, is if version 1.1 or an earlier version of the .NET Runtime is loaded by Excel. ASW versions 2006.5 and later require version 2.0 or later of the .NET Runtime to run. The .NET 2.0 runtime files are installed with ASW, and normally Excel uses the latest version of the .NET Runtime which is installed on the PC, so normally this shouldn?t be a problem. It is possible to have an Excel application configuration file setup on your PC which can specify which version of the .NET Runtime Excel should load. If you have this file on your PC and it specifies that the 1.1 .NET Runtime should be used, then ASW will fail to connect. Excel can only load one version of the .NET Runtime, so if a version which is earlier than 2.0 is specified then ASW will fail to connect. | Solution: The Excel application configuration file will be named Excel.exe.config and will be in the same directory as the Excel.exe file. To enable ASW to work properly, you need to remove the file or remove the line of the configuration file which specifies which version of the .NET Runtime to load.
The following link explains what the different lines in the Excel application configuration file mean:
http://msdn.microsoft.com/en-us/library/1fk1t1t0.aspx
Here is an example of an application configuration file which specifies that the v1.1 .NET Runtime be used (this will cause ASW to fail to connect):
<configuration>
<startup>
<requiredRuntime version=v1.1.4322 safemode=true/>
</startup>
</configuration>
Note: You might also want to investigate what application placed that restriction in the Excel application configuration file because changing this restriction might affect that application.
Keywords: None
References: None |
Problem Statement: Aspen Process Controller new feature: Import Vectors.
DMCplus Model imports the following data files: Collect files *.clc, Vector files *.vec, Extended Vector files *.dpv and Vector Import List files *.lst.
APC Builder has imported the following data files: APC Dataset files *.apcdataset, CLC files *.clc and TXT files *.txt.
Now, APC Builder V8.0 also imports: Vector files *.vec, and Extended Vector files *.dpv. | Solution: To import Vector *.vec and Extended Vector *.dpv files:
1. From the main menu, click File | Import | Vectors. A Browse for Folder dialog box is displayed.
2. Use the Browse for Folder dialog box to locate and select the folder that contains one or more vector (*.vec and/or *.dpv) files.
3. Click OK, and if vector files are found in the folder, the following message is displayed: n extended vector files (dpv extension) were found. n vector files (vec extension) were found. Do you want to import these files? [Yes] / [No].
4. Click Yes. A Dataset Name dialog box is displayed.
5. In the Dataset Name dialog box, accept the default value, which is the name of the folder you selected in step 2, or enter the desired name for the new dataset, and then click OK.
Keywords: Aspen Process Controller Builder, APC, V8.0, Import, Vectors
References: None |
Problem Statement: Why does the controller application generate No responses in gain matrix for an MV message? How to resolve this issue? | Solution: The No responses in gain matrix for an MV error message is typically generated when the controller model has one or more MVs that have all their model with zero or near zero gain values (10 to power -7 or lower in magnitude). The controller engine recognizes this when performing the control calculations (either online or in simulate) and reports that there are MVs with near zero models. The reSolution for this issue is to open the model for the controller and fix any variable (independent or dependent) that has only zero or near-zero model curves associated with it.
It is not recommended to build a controller application with blank variables (variables without any model) or variables with only zero or near-zero gains.
Keywords: APC Builder
MV responses
References: None |
Problem Statement: How can I use a Macro/VBA to enable ASW? | Solution: See the code in the attached workbook. You need to add two Aspen references to the vba project when you do this (already added in the workbook attached):
The code is attached here as well.
'--------------Code starts---------------
Sub EnableWorkbook()
Dim a As AspenOSEWorkbook.OSEApplication
Call GetASWApplication(a)
a.ExecuteCommand (AspenTech.ASWXL.Commands.EnableCommand)
End Sub
'--------------Code Ends---------------
Keywords: Macro, OLE, VBA, Enable, ASW, Disable
References: None |
Problem Statement: Links between Excel and Aspen HYSYS broken when the Aspen HYSYS simulation is renamed | Solution: When you change the name of the AspenHYSYS file or change the location of the file on the PC and then open the active simulation case then the links between Excel and Aspen HYSYS get broken. You can use a different file name located in a different directory with your Aspen Simulation Workbook (ASW) excel file. The steps you should consider are listed below:
1. Open the ASW excel file.
2. Select Manage Simulation by clicking the down arrow with the simulation file name. This will bring the File Properties window.
3. Select Change case link to navigate the location of the correct Aspen HYSYS file and then select the Aspen HYSYS file you want use. You can also use the File Name under the configuration page to navigate the new file.
4. You can now activate the simulation and display the case using the Show/Hide button.
The above procedure will now allow to use the new file with the current ASW provided the mapping with variables remains the same as in the original file.
Keywords: ASW, HYSYS link
References: None |
Problem Statement: How do I change the font size of the variables in a Gantt chart? | Solution: Click on the Green button at the corner of the Gantt chart, the following dialog pops up
Select the Graphic Feature tab
Adjust the font size by specifying values in the Control variable box. Furthermore this dialogue gives the flexibility to change other graphic options like: font size of Event Labels, Gantt bar thickness etc.
Keywords: Gantt chart
Gantt chart graphics
Gantt chart font
Event views
Gantt bar thickness
References: None |
Problem Statement: We have an Aspen Plus model that uses a .dll file (via an opt file specification in the .bkp file).
Aspen Simulation Workbook (ASW) can never find the .opt (or the .dll) file since they are not part
of the embedded .bkp file. How does one do this? | Solution: Embed the compound file (.apwz) when the Aspen Plus bkp model requires external files such
as Fortran objects (.obj), DLLs (.dll), apmbd (binary embedded component from Excel calculator
blocks), and exchanger design EDR files. The Aspen Plus compound file should have embedded
all the necessary files to run (dll, opt, etc). See Figure 1.
Figure 1. Embedded file on Aspen Plus compound library file ammonia.apwz
C:\Program Files\AspenTech\Aspen Plus V7.3\GUI\App\Ammonia
When compound files are run locally with ASW, the embedded files into compound file are
extracted into a temporary folder under your profile when the simulation is activated in ASW.
The simulation runs in this temporary directory. The embedded file is updated at the end of the run.
Temporary files are deleted when the simulation is deactivated.
See attached example built with the library model ammonia.apwz that works in ASW following the
above methodology.
Keywords: External files, dll, opt, apmbd, EDR, apwz.
References: None |
Problem Statement: How do you import a dataset, in a text file format, to DMC3 Builder? | Solution: In order to import data from a text file in DMC3 Builder you have to put the information in a tab delimited format. The information in the text file should follow the following order:
(1) In the first line you can put a description of the data set.
(2) In the second line the name of the vectors (time and name of the tags).
(3) In the third line a brief description of the tag.
(4) In the fourth line the engineer units.
Note the time format should follow mm/dd/yyyy hh:mm:ss format.
Attached to thisSolution is a fire heater data set example so you can import it in DMC3 Builder. Note that if you have the information in Excel you can save the file as Text(Tab delimited)(*.txt) format.
Then open a new project and follow this steps to access the import text file dialog:
1
In the Datasets view go to the top left menu.
2
Click Import | Dataset. In the Import Dataset dialog, change the format to Text Files (*.txt) and select the text file with the data.
3
In the Import TXT File menu review the number of tags, sample period and data range.
4
If the Interpolate bad/missing samples checkbox is selected the import operation will use the desired interpolation span.
You can verify the information in the import text file dialog correspond to the information you introduced in the txt file.
Then hit the import button and start the interpolation. You will have the new data set in the project, select the tags to display in the workspace. At this point you should be able to plot the data.
Keywords: DMC3 Builder
Dataset
TXT file
References: None |
Problem Statement: What could prevent me from importing a dataset? | Solution: Working on a system that is using Portuguese local settings, dataset import fails.
The root cause is an issue with the date format. In Portuguese the format is dd-mm-yyyy, instead of the English standard format of mm-dd-yyyy. Inverting the position of month and day in the dataset corrects this issue when using Portuguese settings.
Keywords: localization, regional settings, date, time
References: None |
Problem Statement: How do you incorporate cross linking in polymerization kinetics? | Solution: Crosslinked polyemrs usually involve reactions with pendant double bonds. Pendant double bonds (vinyl segments) resulting from the propagation of diene monomers such as 1,3-Butadiene can generate cross links between polymer chains.
The polymer attributes XLFLOW and XDENSITY are used to track the mole flow of cross links and the cross linking density. Please make sure to include XLFLOW and XDENSITY attributes from Aspen Properties > Polymers > Characterization > Attribute List
Key Words
Double Bond, Cross-Link, Attribute
Keywords: None
References: None |
Problem Statement: For a metallocene copolymerization reaction of monomers M1 and M2, can we determine the fraction of active catalyst that have M1 as the last inserted monomer? | Solution: Polymer attribute “LSEFLOW” needs to be included in the list of attributed calculated during polymerization process.
LSEFLOW will track the flow rate of live end segments for each type of active site. With calculated LSEFLOW, the catalyst flow rate and maximum active sites we should be able to work out the fraction or concentration of M1 as the last inserted monomer (e.g., the end of the chain).
Key Words
Metallocene, Monomer, Catalyst
Keywords: None
References: None |
Problem Statement: I'm trying to load an old simulation (created with Aspen Plus 2006.5 or older) with Aspen Plus V7.0 (or higher). I get a ID Conflict window such as shown below.
Why am I getting this window? What should I do? | Solution: The documentation mentions in the What's new in V7.0:
IDs for Design Specs, Calculators, Transfers
Design Spec, Calculator, and Transfer blocks may now be placed on the flowsheet. A side-effect of this is that they must have unique IDs. When opening backup files from previous versions where Design Specs, Calculators, Transfers, and unit operation models do not all have unique IDs within a hierarchy level, the Resolve ID Conflicts dialog box will appear to let you rename the conflicting items.
You get this window because in version v7.0 we changed the rules for object names: you may not have two objects with the same name, such as a block, a calculator block and a design spec. This change has been implemented to allow users to display design specs and calculator blocks on the flowsheet. As another side effect, the change also prevents users getting another error message when they want later to turn their simulation to the equation oriented mode. In the graphical user interface of v7.0 or higher, the user gets a message that the object name is already in use. The issue applies only to old simulations in which the user was allowed to use such names.
The onlySolution is to resolve those ID conflicts. You need to make sure the names are unique: you can click the block name, then the button Change Name and enter a new name.
Keywords: ID Conflict
References: None |
Problem Statement: Which emission model to use for Purge Operation? | Solution: In Purge operation, if you go to Model tab, take a look at the emission models available to this operation, you will see Purge, Sweep, Depressurization and other emission models are available to this operation.
Although this is confusing, one should NOT use Purge or Sweep emission model for Purge operation. Otherwise you will see the following message, Warning: Purge operation emissions should be calculated with evacuation instead of gas sweep/purge equations.
The emission model one should use for Purge operation is evacuation model, such as ACT Evacuation, CTG Evacuation or MACT Depressurization model. The reason being that, Purge operation has nothing to do with a high flow gas sweep. It is a pressurization with gas (usually non condensable) followed by an evacuation and repressurization. The depressurization equation is calculated using this pressure range.
Purge/Sweep emission models were retained for upward compatibility.
Keywords: Emission
Purge
References: None |
Problem Statement: HP announced in June 2005, they would stop selling their Fortran Compiler, HP Visual Fortran 6.6 on December 1st, 2005. HP also advised users to migrate to Intel Fortran Compiler version 9. | Solution: Currently, the following Aspen Tech products allow compiling user routines using HP Visual Fortran:
? Aspen Plus
? Aspen Properties
? Aspen Dynamics
? Aspen Custom Modeler
? Aspen Adsim and Chromatography
Attached PDF file (Japanese) is a summary of the compatibility of the various versions of our products with both compilers.
Keywords: Japanese
Intel Visual Fortran
Compaq Visual Fortran
HP Visual Fortran
CVF
compiler
References: None |
Problem Statement: Shortcut to access the hierarchies and variable names in Aspen Plus, so that they can be easily used in your ActiveX Visual Basic code. | Solution: The Variable Explorer is important to the Automation user because it shows the names and the structure of the variables which may be accessed through the Automation interface.
Go to your simulation, browse through the navigation panel and do right-click in any of the parameters you want to control via ActiveX.
Select “copy� in the drop-down menu.
Then go to customize on the application ribbon, and click on “Variable Explorer�.
Right click on the variable tree and select on the drop-down menu “Find Clipboard Variable�. The program will automatically take you to the corresponding entry showing you the name and the structure of the variable, so that you can easily use it in your code:
Â
Keywords: ActiveX, VB, VBA, Visual Basic, Automation Server, variable explorer, variable name and structure.
References: None |
Problem Statement: How to modify the number of valid phases in a node through Automation. | Solution: The following code demonstrate how to do it. You can make the specification for the stream or block node as follows:
myNode.FindNode('\Input\NPHASE\MIXED').Value = 1
myNode.FindNode('\Input\PHASE\MIXED').Value = V
Where '\NPHASE\MIXED' node values are: 1 (1-phase), 2 (2-phases), 3 (phases); and if NPHASE.MIXED.value = 1 then \PHASE\MIXED node values can be: V (vapor only), L (liquid only), S (solid only). In the example above sets the number of valid phases to one and specifies only vapor is allowed.
You can also modify the default global settings for streams and blocks with the same logic. This way you can save some lines of code:
Data\Setup\Sim-Options\Input\NPHASE
Data\Setup\Sim-Options\Input\PHASE
Keywords: Automation, VB.NET, VBA, valid phases.
References: None |
Problem Statement: Aspen Plus stream summary is not in the order specified in the customized .TFF
title=yes
stream-id-label=yes
display only substream=Mixed substream-header=yes pb-header=NO
prop temp prop-label=Temperature substream=Mixed &
format=%10.1f
prop pres prop-label=Pressure substream=Mixed &
format=%10.1f
prop massflmx prop-label=Mix MassFlow substream=Mixed &
format=%10.1f
display only substream=CIPSD substream-header=yes pb-header=NO
prop massflmx prop-label=CIS MassFlow substream=CIPSD &
format=%10.1f
display only substream=$total substream-header=yes pb-header=NO
prop massflmx prop-label=Tot MassFlow substream=$Total &
format=%10.1f
The results show up in the following order [Mixed, CIPSD and $Total], but they in the results $total is shown before CIPSD. | Solution: Put abeglooop and endloop around each display solves the issue.
Attached is a sample tff file.
Keywords: TFF, Begloop, Endloop
References: None |
Problem Statement: Why do I get an unknown bead number error? | Solution: When you get a message about unknown or undefined bead number, it indicates a problem with accessing some information from the vector. If this happens reproducibly in a simulation, it is a defect. Please set the file to customer support.
If the simulation contains user fortran, check that all variables are dimensioned and accessed properly.
Keywords: Fortran, corrupt
References: None |
Problem Statement: After installing Visual Fortran VS2015 Professional with Update1, there was a dialog telling me VS 2015 with Update 1 is installed successfully. However, when trying to set the compiler for Aspen Plus, the VF16_VCX14 reports ERROR. | Solution: By default, the Visual Fortan VS 2015 Update 1 does NOT install Visual C++ (and associated tools) by default as in earlier versions. You now have to select the Custom installation option and then check Visual C++ (under Programming Languages). Visual C++ is needed to use Fortran with Aspen Plus.
Keywords: None
References: None |
Problem Statement: How to model Tank to Tank transfer in a PPIMS model | Solution: Following is the example about how to model Tank to Tank transfer in a PPIMS model. For example, Crude ANS, NSF and TJL are pooled into Tank 01 and then transferred to Tank 02. Sample model can be downloaded from this article.
To reach this purpose, we can create submodel ST12 and use T.CRDTANKS and T.PGUESS to force recursion.
1) Create a submodel ST12 to transfer Tank 01 to Tank 02.
mf2
2) As Tank 02 did not include the crudes in Tank 01, so in order to create the necessary recursion rows, a small amount of the Tank 01 crudes are added to the Tank 02 as initial composition in T.CRDTANKS. And initial guess for these crudes in Tank 02 are also added entries in T. PGUESS.
Keywords: TANK TRANSFER
PPIMS
References: None |
Problem Statement: How are some common chemicals used in pharmaceutical and biotech processes listed in the Batch Plus database? | Solution: Below is a list of common chemicals used in pharmaceutical and biotech processes and their more exact names. \
Common Name MW Technical/Other Names In Batch Plus Database?
Tris 121.14
Tris (hydroxymethyl) amino-methane
or trimethamine or C4H11NO3
No
Dithiotheitol 154.3
DTT or Cleland's Reagent or
C4H10O2S
No
EDTA
Ethylendiamine tetraacetic acid or
Ethylenedinitrilo-tetraacetic acid or
C10H16N2O8
Yes, as
EthyleneDiamineTetraAcetic-Acid
Aminoacetic Acid
Glycine
Yes, as Glycine
Carbamide
Urea
Yes, as Urea
ACN
Acetonitile
Yes, as Acetonitrile
HCL
Hydrochloric acid
Yes, as Hydrogen-Chloride
NAOH
Caustic, Sodium Hydroxide
Yes, as Sodium-Hydroxide
Tricine
N-tris (hydroxymethyl) methyl glycine or
C6H13NO5 or CAS 5704-04-1
No
Keywords:
References: None |
Problem Statement: Why does the temperature of water increase when the pressure decreases? | Solution: The Joule–Thomson coefficient is defined as the change in temperature with respect to an increase in pressure at constant enthalpy.
At room temperature for most vapors (including steam), Joule-Thomson expansion lowers the temperature. Some notable exceptions are hydrogen, helium, and neon. However, for liquids at temperatures well below their critical temperature, the Joule-Thomson coefficient is typically negative, meaning that a decrease in pressure actually raises the temperature.
Because liquid water has a negative Joule–Thomson coefficient at low temperatures (below approximately 250C), the water cools as it compresses and heats as it expands.
Keywords: Water, depressuring, Joule-Thomson
References: None |
Problem Statement: I am attempting to see if Aspen Plus correctly predicts the solubility of oxygen in water. To do this I flash a mixture of oxygen and water and take the concentration of oxygen in water for the liquid outlet. I use UNIFAC as property
method and Oxygen as Henry component. However, based on Aspen reports, I get ~39 mg/l but literature reports 8.3 mg/l for oxygen solubility in water (@ 25 ?C and 1 atm). | Solution: Water solubility of Oxygen at 25 ?C and 1 bar is calculated by Aspen Plus as 39.3 mg/l. In air with a normal composition at sea level, the Oxygen partial pressure is 0.21 bar. This results in disSolution of 39.3 * 0.21 = 8.3 mg Oxygen/l in water that comes in contact with air, which is the value reported on literature.
Keywords: Oxygen solubility, property values reported on literature, discrepancies.
References: http://water.usgs.gov/owq/FieldManual/Chapter6/table6.2_6.pdf |
Problem Statement: The user would like to generate a summary of all waste streams and the net costs relating to the disposal of these streams. | Solution: Batch Plus can report a summary of all waste streams and their costs. To generate this summary:
Define new waste stream categories and associated costs under File, Preferences, Stream Categories. It may be advantageous to define multiple Stream Categories that represent different concentrations and their relative costs when appropriate.
To be included in the Waste stream cost summary, the waste material must be transfered to an Inventory Location. To define a location select the Facility tab on the Project Builder window. Select a facility, add an Inventory Equipment Type and assign a name (i.e. Disposal).
Finally, add a Transfer operation to send the appropriate material to the Inventory location. Double click on the operation, set the Destination, select the Optional tab and the Transfer Streams button to set the stream name and category.
NOTE: Only waste streams sent to inventory locations are included in the waste stream summary report. Waste streams transferred to equipment of other types, such as a tank, are not considered as disposal and will not be included in the waste stream summary report.
Keywords: Costing
Waste
Disposal
Streams
References: None |
Problem Statement: What is the validity range of PC-SAFT data in terms of temperatures and pressures for the data against which the parameters were regressed? | Solution: PC-SAFT parameters stored in Aspen database are mainly from papers by Sadowski and her co-workers. Here is a list of references:
Gross, J., & Sadowski, G. Perturbed-Chain SAFT: An Equation of State Based on a Perturbation Theory for Chain Molecules. Ind. Eng. Chem. Res., 40, 1244-1260 (2001).
Gross, J., & Sadowski, G. (2002a). Modeling Polymer Systems Using the Perturbed-Chain Statistical Associating Fluid Theory Equation of State. Ind. Eng. Chem. Res., 41, 1084-1093 (2002).
Gross, J., & Sadowski, G. Application of the Perturbed-Chain SAFT Equation of State to Associating Systems. Ind. Eng. Chem. Res., 41, 5510-5515 (2002).
Dominik, A., Chapman, W. G., Kleiner, M., Sadowski, G. Modeling of Polar Systems with the Perturbed-Chain SAFT Equation of State. Investigation of the Performance of Two Polar Terms. Ind. Eng. Chem. Res., 44, 6928-6938 (2005).
Keywords: None
References: None |
Problem Statement: When ideal gas enthalpy (HIG) is calculated based on saturated liquid reference state, how are ideal gas Gibbs free energy and entropy (GIG and SIG) calculated? | Solution: When H*,ig (HIG) is calculated based on saturated liquid reference state, ideal gas Gibbs free energy and entropy (GIG and SIG) are also calculated based on saturated liquid reference state to maintain thermodynamic consistency, and liquid Gibbs free energy and entropy are also calculated based on saturated liquid reference state since they are calculated based on departure from the ideal gas values.
Keywords: None
References: None |
Problem Statement: Equipment is not showing up in the Equipment diagram | Solution: Check to see that the operations that use these pieces of equipment simulated correctly. If there are no vessel contents or the inlet stream is of zero flowrate, then there are no stream results and Batch Plus will omit the equipment from the Visio Equipment diagram.
Correct the recipe so that the vessel contents are not zero and rerun the simulation. Create the Equipment diagram and the equipment should be visible.
Keywords: None
References: None |
Problem Statement: When plants are added directly into the equipment database, they do not show up on the facilities list in the Batch Plus GUI. | Solution: In the equipment database, the new facility has to be entered in two places, the Plant Table and the Plant-to-Project Table. At least one piece of equipment must be added to the facility in the ActualEquipmentCommon Table or else the facility will be deleted from the list in Batch Plus.
To add a facility in the Batch Plus database,
Copy the file //Batch Plus/bin/ProjectEquip.tmp to a temporary or working directory.
Open ProjectEquip using MS Access. (You may need to rename the file ProjectEquip.mdb).
In the Plant Table, enter the Plant ID No. for your new plant and the Name. This can be the next sequential number in the list.
In the Plant-to-Project Table, enter the same Plant ID No. and Name as well as a Project ID No.
To add a piece of equipment to the facility,
Open the ActualEquipmentCommon Table
Enter a new equipment item by giving it a unique Actual Equipment ID, Equipment Class ID, Plant ID and Batch Plus (BP) Tag.
Keywords:
References: None |
Problem Statement: After moving to a new computer user fortran .dll files cannot be linked. | Solution: The problem is could be due to missing fortran link libraries DFORRT.DLL and DFORMD.DLL files (located in \ \windows\system32) for the older Compaq Visual Fortran.
TheSolution is to copy those two DLLs from the old computer to the new computer.
Keywords: None
References: None |
Problem Statement: Is there an assumption of a constant flow in the RPlug reactor on the energy balance? | Solution: The variables that appear in integrations:
1. For each substream: the effective (involving reactions) components flow and enthalpy flow
2. For each component: effective component attributes
3. Pressure: if pressure is not assumed constant or defined (profile)
4. Resident time: at each step (indirectly volume flow)
There is no assumption for constant flow. There is a mass balance in the reactor.
F(out) = F(in) + rate*area*dz, or dF/dz = rate*area
There is a similar equation for the heat balance.
The solver integrates component flow (DF/dz = rxn rate) and enthalpy (with dH/dz = Heat transferred out or in) with dz, with an convergence loop to ensure the integration is converged to corrected component flow and enthalpy.
The heat of reaction is not needed because Aspen Plus calculates component enthalpies based on the enthalpy of formation of the compounds at the referred state. So heat of reaction is included in the enthalpy difference over dz.
In this way, temperature, Cp and overall flow are not directly integrated but are implied since all state variables and property values (Cp, T, P etc) are temperature and thus z dependent. No additional constants are assumed.
Keywords: RPlug, flow, energy balance
References: : CQ00689680 |
Problem Statement: When using the NIST ThermoData Engine (NIST TDE) for a Pure Component, some of the properties are for Liquid vs. Gas. For example, There is Density (Liquid vs. Gas) and Heat Capacity (Liquid vs. Gas). What does this mean? | Solution: This generally means saturated liquid. For example, Saturated Density (Liquid) and Saturated Heat Capacity (Liquid). In general, properties indicated as applying to Liquid vs. gas, or Crystal 1 vs. gas, etc. apply to the first phase at its equilibrium with the second. This information is taken directly from NIST.
Here is more information on the NIST equations and definitions:
http://trc.nist.gov/TDE/Equations/FEquations.html
Keywords: None
References: : CQ00585117 |
Problem Statement: The pressure in a vessel or reactor is increasing unexpectedly. | Solution: A common reason for the pressure to increase unexpectedly is that a vent is closed unexpectedly.
If the pressure is increasing through the Charge or other operations, first check the Run History (under NotePad Results) for operations occurring earlier in the recipe to see if the vent on a vessel was closed as part of an operation.
For example, the vent on a vessel will be closed if a blanket of gas is specified on the Optional form of the Purge operation.
Also check for a Open-Close vent operation in the recipe.
Keywords: Vent
Purge
Pressure
References: None |
Problem Statement: Why does the objective function keep decreasing past the value reported on the Column | Analysis | NQ Curves | Summary sheet? | Solution: The traditional NQ curve is a plot of heat load (Q) against total number of stages (N). However, the concept of NQ curves is not restricted to just heat load. These curves can be used with any objective function.
The NQ Curves feature in Aspen Plus determines the curve by performing calculations at different numbers of stages. The optimum location for the main feed stream is determined for each number of stages. The locations of product streams, other feeds, pumparounds, and decanters are determined from the feed location and number of stages for each run; there are several methods available which can be chosen independently for each stream. The NQ curves analysis records the detailed results of column simulation for each number of stages. A variety of other variables, such as reflux ratio, are available for plotting.
Generally, the heat load continues decreasing as you increase the number of stages, but after a point, the improvement diminishes to the point where it becomes negligible. NQ Curves will stop increasing the number of stages when it reaches that point (or else at the maximum number of stages you specify). In either case, the finalSolution uses the optimum feed location for the number of stages it determines. In V8.8 and earlier, FinalSolution results were called Global optimum results which was unclear since the heat load continues to decrease as you add stages, but very slowly, or it may stop at the stage limit you specify, when adding stages could reduce the heat load further.
Keywords: nqcurves
References: : CQ00614001 |
Problem Statement: Aspen Plus 10.1 should be loaded and run before you attempt to use it with Batch Plus. | Solution: Batch Plus will not recognize that Aspen Plus has been installed until it has been run once. You can run the Testprob.bkp found under the \Program Files\AspenTech\Aspen Plus 10.1-0\Favorites folder.
Note that Aspen Plus 10.0 is not supported in Batch Plus 2.0b.
Keywords: Installation
Aspen Plus
Batch Plus
References: None |
Problem Statement: What happens if more than one outlet stream is denoted as the key step output? | Solution: Batch Plus will use the first occurrence of this specification.
Keywords: BATCH PLUS
Key
Step
Output
Product
References: None |
Problem Statement: How to report molar properties for a polymer in the stream report? | Solution: Aspen Plus includes in its property sets two properties to report the true molecular weight and the true molar flowrate of a polymer.
For V9, the process to add those values in the stream report is as follow:
1. Go to the stream that you want to review and select the results tab.
2. Click on add properties at the bottom of the screen
3. Type Polymer in the search form. Select TRUEFLOW and TRUEMW and click ok
4. Expand the Mixed Substream form to reveal all the properties in the report. You will find the new properties added at the bottom. If results do not appear, run the simulation again.
Keywords: True molecular weight, molar flow, polymer properties
References: None |
Problem Statement: Is it possible to define Utility (heat transfer fluid) as mixture? | Solution: Currently, you cannot use a mixture to create a utility; only pure components are allowed. You have to create a new pure component with the physical properties that the mixture would have to simulate similar heat transfer activities. Then, create a new utility based on the pure component.
Keywords: Utility, Heat Transfer
References: None |
Problem Statement: What version of Visio is required for Batch Plus 2.x? | Solution: Batch Plus 2.0, 2.0b, 2.1 and 2.2 require Visio Technical or Pro version 5.0c or higher.
Keywords:
References: None |
Problem Statement: The average molecular weight is needed to calculate equivalent and bill of material. How is it calculated for a mixture in Route Selection? | Solution: If you specify the active ingredient in a mixture, then the molecular weight should be: (active ingredient MW)/(mole fraction of active ingredient in the mixture)
If you did not specify the active ingredient, then the molecular weight should be the average MW based on mole fraction
The molecular weight in the Route Selection Results/Process Route Detail sheet is wrong. However, this MW is not used in equivalent or cost (bill of material) calculation. The MW used in the equivalent calculation is described above in (1).
Fixed by
The problem will be fixed in version 2006. - CQ205134
Keywords: Molecular weight
MW
equivalent
cost
bill of material
References: None |
Problem Statement: Installation and configuration issues may lead to problems launching Visio Equipment or Block diagrams. | Solution: Either Visio Professional or Visio Technical is required to generate Equipment or Block diagrams in Aspen Batch Plus. Visio Viewer cannot be used to generate diagrams. However, once Visio diagrams are generated, one can use the Visio Viewer to browse the diagrams.
If you encounter difficulties while trying to generate Visio Equipment or Block diagrams using Visio Professional or Visio technical, it is likely that Visio was installed after Batch Plus. Try the following steps to update the path:
1. Go to File | Preferences | Equipment Diagram
2. Check the box Check this box if you are encountering problems generating a diagram
3. Close Preferences and run the Visio Diagram.
4. You should be told that the Visio add-on path has been updated and that you should close Visio for the change to take effect.
5. Close Visio
6. Go back to preferences and uncheck the check box Check this box if you are encountering problems generating a diagram
7. Close preferences
8. Run the Visio diagram again
If the problem persists, try to change the security settings of Visio :
· Launching Visio
· Go to Tools | Macro | Security
· Change the security to Low
If the above steps fail to resolve the issue please contact AspenTech Support.
Keywords: Visio
Equipment Diagram
Block Diagram
References: None |
Problem Statement: How can I retrieve r, q and q' Uniquac parameters? | Solution: The Uniquac r, q, and q' parameters are scalar parameters for each component.
To review parameters, from the main menu, select Tools and Retrieve Parameters Results. The values for r, q and q' will be reported as GMUQR, GMUQQ and GMUQ1 respectively on the Properties | Parameters | Results | Pure Component | Scalar sheet.
Keywords: None
References: None |
Problem Statement: Why do I get large, unexplained time gaps in the simulation results? | Solution: The facility for the step is can use a non-24 hour calender where certain dates are marked non-working or exception.
Check two places:
The calender assigned to the facility. Go to the Facility tab in the project builder, select the facility and click Edit.
Preferences. If a calender is not specifically assigned, the default calendar in the Preferences will be used.
Keywords:
References: None |
Problem Statement: What are the different batch movement operations available in Aspen Batch Process Developer (ABPD)? | Solution: Following are the different batch movement operations used in ABPD:
1. Charge: Charge raw material to a unit which may include pure component, a pre-defined mixture or pre-defined cells.
2. Charge-To-Amount: Charge raw materials to an equipment unit, to a certain amount of pure Component, pre-defined mixture or pre-defined cells.
3. Line-Blow: Blow a line with gas following the transfer of material between units to remove any remaining material in the line.
4. Line-Flush: Flush a line following the transfer of material between units to remove any remaining material in the line.
5. Multiple-Transfer: Transfer material from many equipment units to a single equipment unit, or from a single equipment unit to multiple equipment units.
6. Pressure Transfer: Transfer liquid and/or solid contents from a source unit to a destination unit.
7. Transfer: Transfer the full or partial contents of a unit to another unit.
8. Transfer-Through-Heat-Exchanger: To transfer the full contents of a unit to another unit through a heat exchanger.
Keywords: definitions, operations
References: None |
Problem Statement: Not able to run the Custom (Example) process in the Examples project. | Solution: Make sure that the file path and name of Excel/VBA mode is specified correctly in each Operation it is used. The path and name set by the installation is
G:\Program Files\AspenTech\Batch Plus 2.1\Projects\Excel Models\MaintainComponentAmountv1.xls
You should change it accordng to your installation. To do this, open the text recipe. Go to Operation 1.3 specification, click Model and then Advanced. Browse to locate MaintainComponentAmountv1.xls in \Batch Plus 2.1\ Projects\Excel Models directory. Select it. Repeat for Operations 1.5 and 1.6.
Check MaintainComponentAmountv1.xls in Visual Basic Editor. Make sure that Batch Plus 2.1 Object Library is referenced. See theSolution to Problem-1 above for details.
Keywords: v2.1, version 2.1, installation, automation, Exel/VBA model, user model, Excel Model, BatchPlusAutomationExample, MaintainComponentAmountv1, Run-time error 9:, Run-time error 429
References: None |
Problem Statement: Besides molar flows, what parts of SVEC(*) must be defined calling the FLASH utility in user fortran? | Solution: Specifications for the flash are taken from a combination of values in SVEC, SPEC1, and SPEC2. The component flows and total flow are always used, and the following table shows the additional specifications:
KODE
SPEC1
SPEC2
Additional specifications
1
P
Q
P in SVEC(NCOMP_NCC + 3) if SPEC1 <= 0, H in SVEC(NCOMP_NCC + 4)
2
T
P
P in SVEC(NCOMP_NCC + 3) if SPEC2 <= 0
3
P
V
P in SVEC(NCOMP_NCC + 3) if SPEC1 <= 0
4
T
Q
H in SVEC(NCOMP_NCC + 4)
5
T
V
none
Indices in SVEC are for the MIXED substream. For the CISOLID substream, add NCOMP_NCC + 9 + NCOMP_NVACC. For the NC substream, add NCOMP_NNCC + 9 + NCOMP_NVACC plus an additional NCOMP_NCC + 9 + n if there is a CISOLID substream. See the Aspen Plus User Models reference manual appendix C for details.
Keywords: user fortran utility
References: None |
Problem Statement: Are there any new examples available for Aspen Plus V7.2? | Solution: A number of examples have been added or updated for V7.2.
Amines
MDEA+PZ
Aspen Plus simulation model and doc
Add
C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\App\Amines
NH3
Aspen Plus simulation model and doc
Update
Physical
Solvents
DEPG
Aspen Plus simulation model and doc
Update
C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\App\Physical solvents
MeOH
Aspen Plus simulation model and doc
Update
Alternative
energy
Entrained flow coal gasifier
Aspen Plus simulation model and doc
Add
C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\App\Entrained Flow Coal Gasifier
Fixed-bed coal gasifier
Aspen Plus simulation model and doc
Add
C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\App\Fixed-bed Coal Gasifier
Oil shale retorting
Aspen Plus simulation model and doc
Add
C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\App\Oil Shale Retorting
Scaling
Scaling
Aspen Properties backup files and docs
Add
C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\Datapkg\Scaling
Industrial
packages
H2SO4
Aspen Properties backup files and docs
Add
C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\Datapkg
These are added to the existing examples. The online applications library now includes the following files:
File(s)
Description
Aspen Plus features demonstrated
3phase.bkp
Reactive Distillation production of methylchlorate by esterification of chloroacetic acid with methanol.
Reactive distillation
Three-phase distillation
Column with total boilup (i.e. zero liquid bottoms flow rate)
Internal column specification with feed flow manipulation
Use of Decanter model
Alternative Energy\Entrained-flow coal gasifier
Texaco down-flow entrained flow coal gasifiers
HCOALGEN and DCOALIGT for nonconventional component properties
RYield for coal pyrolysis and pressure correction
RStoic for volatile combustion
RStoic, RPlug, and Fortran Calculator blocks for char gasification
Alternative Energy\Moving-bed coal gasifier
Countercurrent moving-bed coal gasifiers
HCOALGEN and DCOALIGT for nonconventional component properties
RYield for coal drying and coal pyrolysis
RStoic, RCSTR, and Fortran Calculator blocks for char gasification and combustion
Alternative Energy\Oil Shale Retorting
Fluidized-bed oil shale retorting process
Preheat, retort, combusion, and separation sub-processes
RK-SOAVE property method for conventional components
ENTHGEN and DCHARIGT models for nonconventional solids
Reaction model for pyrolysis of kerogen
Ammonia\ ammonia.apwz
Ammonia production using natural gas
Desulfurization with Sep2 and RStoic
Reforming using RStoic and RPlug
Carbon monoxide conversion with RPlug, FSplit, and Heater
Carbon dioxide removal with Flash2
Methanation with RPlug and Sep2
Synthesis with RPlug, FSplit, and Heater
Refrigeration with Valve and HeatX
Design Spec and Calculator blocks
bayer.apwz
Bayer digestion circuit where gibbsite (Al[OH]3) is removed from bauxite.
Hydrometalurgy uses of simulator
Design specifications
In-line Fortran
Sensitivity analysis
Stream report format customization
biodiesel\ biodiesel.apwz
Alkali-catalyzed production of biodiesel from vegetable oil, including transesterification, methanol recovery, water washing, FAME and glycerol purification, and catalyst removal.
See the PDF document in this project folder for more details.
RadFrac models for purification operations and methanol recovery
Extract model for water washing
RStoic and Sep models for catalyst removal
RCSTR model for transesterification
Design specification and Calculator block
Detailed modeling of the reactions
In-line Fortran
Bioethanol from corn\ bioethanol_from _corn.apwz
Production of bioethanol from corn, including saccharification, fermentation, distillation, dehydration, dewatering, evaporation, and drying.
See the PDF document in this project folder for more details.
RadFrac model for distillation
Design specifications
Excel Calculator blocks
This model does not perform detailed modeling of the reactions.
Bioethanol from Corn Stover\ corn_stover_to _ethanol.apwz
Production of bioethanol from corn stover, including feed handling, pretreatment and conditioning, saccharification, fermentation, enzyme production, product purification, water treatment, storage, and utilities.
See the PDF document in this project folder for more details.
SSplit, Sep, Flash2, RStoic, and RadFrac models for core units
User model for anaerobic digestor
Pump, Compr, and Heater models
Design specifications
In-line and compiled Fortran
Detailed modeling of the reactions
Excel user interface
cdu.bkp
Atmospheric crude tower.
PetroFrac model
Tray-sizing and Tray-rating
Tray property reporting
Cogeneration\ cogeneration.apwz
Integrated cogeneration process using the internal energy of the natural gas to generate electrical power, burning the gas to generate power with a turbine, and recovering the heat from the hot gas to generate steam and electrical power.
HeatX shortcut heat exchanger
Flash2 for rigorous vapor-liquid equilibrium
Compr for compressor/turbine to calculate electrical power required or produced
IGCC.apwz
Integrated coal gasification combined-cycle power process, including coal crushing, screening, gasification, dust removal, coal gas purification, water-gas shift, methane and ammonia production, and combined cycle power generation.
See the PDF document in this project folder for more details.
Crusher and Screen models to reduce coal particle size
Flash2, Sep, Compr, HeatX, MHeatX, RadFrac, and Heater to separate air
RStoic, RGibbs, HeatX, Sep, Flash2, Heater to produce coal gas
RadFrac, Flash2, HeatX, Sep, Compr, Heater to remove corrosive components from raw syngas
RStoic, RGibbs, Flash2 for desulfurization
Compr, Mixer, Heater, Flash2, HeatX, Pump to generate electrical power from the coal gas
Mixer and REquil to produce methane
REquil, Flash2, HeatX, and RadFrac to convert carbon monoxide to carbon dioxide, then capture carbon dioxide
RGibbs, HeatX, Sep, Mixer, Heater, Flash2 to produce ammonia
Design specifications
Excel Calculator block
pen.bkp
penext.f
penfrm.f
This flowsheet models a penicillin recovery system using a Podbielniak extractor.
In-line Fortran
Sensitivity Analysis
PipelineGas\ pipelinegas.apwz
Manufacturing pipeline gas from coal, including coal crushing and screening, gasification, purification, shift reaction, methanation, and power generation.
See the PDF document in this project folder for more details.
Crusher, Screen, Sep, and Flash2 models for coal processing
Compr model to calculate required power for compression
HeatX and MHeatX models to simulate the generation of high pressure steam in a boiler
Compr model to simulate a turbine and calculate power produced
Design specifications
In-line Fortran
Scaling\
Prediction of scaling by NaCl, NaCl?2H2O, Na2SO4, Na2SO4?10H2O, BaSO4, CaSO4, CaSO4?2H2O, SrSO4, BaCO3, SrCO3, CaCO3, MgCO3?3H2O, MgCO3?5H2O, and Mg(OH)2 in water at various pressures. Besides the main model, there are also models here implementing various subsets of these scales.
Electrolyte NRTL for liquid modeling
RK equation of state for vapor
Extended Antoine equation for vapor pressure of water
Chemistry models for solid-liquid equilibrium
Flash2 model for setting pressure and temperature
solvent.bkp
Separation of acetone and methanol using water to break the azeotrope.
sour.apwz
Removal of hydrogen sulfide, ammonia, and carbon dioxide from water.
Electrolytic distillation
SulfuricAcid\ sulfuricacid.apwz
Production of sulfuric acid from sulfur in a typical double-absorption plant
RadFrac for drying and absorbing towers
Compr for blower
HeatX and MHeatX for boiler, superheater, economizers, and gas-to-gas heat exchangers
Industrial Packages\Aspen_Plus_ H2SO4_Model.bkp
Thermodynamic modeling of the H2SO4-SO3-H2O system
Symmetric electrolyte NRTL for modeling of electrolyte systems even in the absence of water
Flash2 model to simulate SO3 absorption by water
teg.bkp
Sensitivity analysis of gas drying with TEG.
SR-POLAR equation of state - application in high pressure non-ideal system
Urea\urea.apwz
High-pressure synthesis of urea
RadFrac for CO2 stripper and scrubber
RPlug for urea reactor
RStoic for CO2 condenser
The following additional application examples model CO2 removal from flue gas and similar mixtures. See the PDF documents accompanying each one for more details about the processes.
File
Description
Aspen Plus features demonstrated
Amines/Rate_Based _AMP_Model.apwz
CO2 capture from flue gas, using AMP
Aspen Rate-Based Distillation model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _DEA_Model.apwz
CO2 capture from flue gas, using DEA
Aspen Rate-Based Distillation model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _DEA+MDEA_Model.apwz
CO2 capture from flue gas, using DEA and MDEA
Aspen Rate-Based Distillation model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Physical solvents/Aspen_Plus_DEPG_Model.apwz
CO2 capture from flue gas using DEPG
RadFrac equilibrium stage model for absorber (high and low pressure cases)
PC-SAFT liquid and vapor properties
Transport property parameters fit to literature data
This model was prepared using the equilibrium stage model in order to provide a valid comparison against the literature case which was based on equilibrium stage calculations. Transport and packing data are included to allow you to use the more rigorous Aspen Rate-Based Distillation model.
Amines/Rate_Based _DGA_Model.apwz
CO2 capture from flue gas, using DGA
Aspen Rate-Based Distillation model for absorber
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _DIPA_Model.apwz
CO2 capture from flue gas, using DIPA
Aspen Rate-Based Distillation model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _K2CO3_Model.apwz
CO2 capture from flue gas, using K2CO3
Aspen Rate-Based Distillation model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _MDEA_Model.apwz
CO2 capture from flue gas, using MDEA
Aspen Rate-Based Distillation model for absorber
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _MDEA+PZ_Model.apwz
CO2 capture from flue gas, using MDEA and piperazine
Flash2 model for absorber
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _MEA_Model.apwz
CO2 capture from flue gas using MEA
Aspen Rate-Based Distillation model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _MEA+MDEA_Model.apwz
CO2 capture from flue gas, using MEA and MDEA
Aspen Rate-Based Distillation model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Physical solvents/Rate_Based_MEOH_Model.apwz
CO2 capture from flue gas using Methanol
Aspen Rate-Based Distillation model for absorber
PC-SAFT liquid and vapor properties
Wilke-Chang and DIPPR transport properties, matching literature data
Amines/Rate_Based_NaOH_Model.apwz
CO2 capture from flue gas, using NaOH
Aspen Rate-Based Distillation model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _NH3_Model.apwz
CO2 capture from flue gas, using NH3
Flash2 model for absorber and stripper
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Physical solvents/Aspen_Plus_NMP_Model.apwz
CO2 capture from flue gas using N-methyl 2-pyrrolidone
RadFrac equilibrium stage model for absorber
PC-SAFT liquid and vapor properties
Transport property parameters fit to literature data
This model was prepared using the equilibrium stage model in order to provide a valid comparison against the DEPG case which was based on equilibrium stage calculations, since there is no adequate literature case for NMP. Transport and packing data are included to allow you to use the more rigorous Aspen Rate-Based Distillation model.
Physical solvents/Aspen_Plus_PC_Model.apwz
CO2 capture from flue gas using propylene carbonate
RadFrac equilibrium stage model for absorber
PC-SAFT liquid and vapor properties
Transport property parameters fit to literature data
This model was prepared using the equilibrium stage model in order to provide a valid comparison against the DEPG case which was based on equilibrium stage calculations, since there is no adequate literature case for propylene carbonate. Transport and packing data are included to allow you to use the more rigorous Aspen Rate-Based Distillation model.
Amines/Rate_Based _PZ_Model.apwz
CO2 capture from flue gas, using piperazine
Flash2 model for absorber
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _PZ+MEA_Model.apwz
CO2 capture from flue gas, using piperazine and MEA
Flash2 model for absorber
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
Amines/Rate_Based _TEA_Model.apwz
CO2 capture from flue gas, using TEA
Aspen Rate-Based Distillation model for absorber
Electrolyte NRTL liquid properties
RK vapor properties
Transport property parameters fit to literature data
ElectrolyteSolution chemistry and kinetic reaction model
The following additional application examples (in the Polymers subfolder) use features of Aspen Polymers:
Files
Description
hdpe.apwzSolution polymerization of ethylene.
ionicSB.bkp
Ionic polymerization of styrene butadiene rubber in a batch reactor.
ldpe.apwz
This flowsheet models a high-pressure LDPE tubular reactor flowsheet with four sections, two initiator injection points, and high and low pressure separators.
nylon6.bkp
This is a model of a NYLON-6 process VK column reactor.
pmma.bkp
Polymerization of methyl methacrylate (MMA) in a batch reactor.
pp.bkp
Ziegler-Natta gas-Phase polymerization of propylene.
ps.bkp
Styrene polymerization in two CSTR's followed by a plug flow reactor.
psea.bkp
Regression of propagation and termination rate constants for a styrene-ethyl acrylate batch reactor.
sbd.bkp
Copolymerization of styrene and butadiene in a batch reactor.
sty_dist.bkp
Optimization of inhibitor concentration to suppress formation of polystyrene in a column reboiler.
SuspensionEPS.apwz
Expanded Polystyrene Suspension batch polymerization rigorously accounting for 2 liquid phases with reactions occuring in organic phase
Keywords: None
References: None |
Problem Statement: I have installed some Aspen Plus emergency patches using the .exe file. How do I know what fixes have been installed? | Solution: Go to the Help menu and select View Update Readme to see a list of the fixes addressed in the installed emergency patch.
This list is contained in a file named readme.htm located in the ..\AspenTech\Aspen Plus V7.x folder.
Keywords: None
References: None |
Problem Statement: How is it possible to change icons in Visio for Batch Plus Equipment Diagram? | Solution: You can change the icons used in Visio. Refer to the online help under User Manual/Equipment Diagram/Custom Equipment Stencil. There is one icon for each equipment class.
You can replace the icon with a bitmap of a box or create a new icon in Visio. The stream ports are called connection points. To assign a connection point, use the Blue X icon that is on the Visio Toolbar under the Connector Tool (looks like two boxes connected by a line). Because the order is important you may want to check the order under Window/ View ShapeSheet. There is a Connection Point category. If you tile the windows to see both the Stencil and the ShapeSheet you can identify the order by selecting the connection point on the ShapeSheet.
For other icons there are several Process stencils within Visio (Valves, Pipes, Instrumentation, Pumps, Compressors, Heat Equipment, Equipment and Vessels).
You may define a custom equipment stencil to be used in place of the standard Batch Plus equipment stencil. Please refer to your Visio documentation for instructions on creating stencils and masters. The file User.vss is now called BPUser.vss.
To be compatible with Batch Plus:
Name your stencil User.vss and place it in the Templates sub-directory of your Batch Plus installation directory (e.g. Batch Plus 2.2\Templates\Visio). A starter BPUser.vss stencil has been placed in the \Templates\Visio directory by the Batch Plus installation. You may use this stencil as a starting point for your own custom stencil.
Name your equipment masters after Batch Plus Equipment Classes. The starter stencil has a complete list of valid Equipment Classes. If an Equipment Class is missing from your custom stencil, Batch Plus will use the standard master for the missing Equipment Class.
Include 7 connection points for each equipment master. Batch Plus will use these connection points to attach streams. The seven connection points are (in order):
Alternate input port (not used, reserved for future use) Main input port
Top output port
Bottom output port
Vapor Emission port
Main utility port
Alternate utility port (not used, reserved for future use)
Keywords:
References: None |
Problem Statement: How do I define the stream class for a solid if I want to model it using a Crusher block? | Solution: The Solids unit operation blocks such as CRUSHER require a Conventional (CI) or Nonconventional (NC) solid substream with a particle size distribution (PSD). The stream classes that include these substreams are either CIPSD or NCPSD.
The stream class is specified as MIXCIPSD (or NCPSD) on the Setup | Specifications form:
The component(s) defined as solid will be available on the CIPSD substream and those defined as nonconventional will be available on the NCPSD substream.
In the feed stream, specify the input for the CIPSD substream for the inlet stream:
After specifying the flow for the solid components the PSD tab will activate to fill in the weight fraction for the solid particles:
For the CRUSHER block, specify the power at which the particles will be grinded (in the Grindability tab):
This way, the simulation is ready to run.
Keywords: Stream class, CIPSD, crusher, solids
References: None |
Problem Statement: Is there a way to know what changes have been made in a simulation file? | Solution: There is no built-in functionality that would allow you to look for modifications in the simulation in Aspen Plus. On the other hand, there is a procedure that would allow you to know if there are any differences between two input files from Aspen Plus. First of all, the input files are summaries of the different data used by Aspen Plus during the simulation, and they can be exported at any time directly from Aspen Plus by following this procedure:
1. Go to File -> Export.
2. Select Input file (.inp) as the file type and name the file.
3. Click on Save.
Now, you could compare 2 input files created at different times with the Windiff utility from Microsoft. It usually is included in the Visual Studio installation and is commonly located in C:\Program Files\Microsoft Visual Studio X\Common7\Tools\Bin where X is the version you have. Now you can compare the two input files with the following procedure:
1. Start Windiff.exe.
2. On the File menu, click Compare Files.
3. In the Select First File dialog box, locate and then click a file name for the first file in the comparison, and then click Open.
4. In the Select Second File dialog box, locate and then click a file name for the second file in the comparison, and then click Open.
5. The information in the right pane indicates whether there is a file difference.
6. To view the actual file differences, click the first line in the Windiff.exe output results, and then on the Expand menu, click Left File Only, Right File Only, or Both File. (More information on Windiff is available at http://support.microsoft.com/kb/159214)
Keywords: Windiff flowsheet change input
References: None |
Problem Statement: After checking Estimate missing parameters by UNIFAC on the NRTL or UNIQUAC binary parameter form, the parameters are not estimated for my components that are only in the NIST-TRC databank even though there should be UNIFAC groups for them. Why not? How do I get them to be estimated? | Solution: The UNIFAC groups (UFGRP) are part of the PURExx databanks, but they are not part of the NIST databank. In order to estimate the NRTL or UNIQUAC parameters, the UNIFAC groups need to be entered or generated from the General structure of the component.
To have Aspen Plus attempt to generate the UNIFAC groups:
1. Go to the Properties | Molecular Structure | Structure sheet.
2. Click on the Calculate Bonds button.
3. Click on the Ok button to generate the General structure.
4. Re-run.
If UNIFAC groups can be matched to the structure, they will be used to estimate NRTL or UNIQUAC binary parameters.
Keywords: None
References: None |
Problem Statement: How is the Heat of Reaction calculated in Batch Plus? | Solution: Users can use the Calculate button on the Batch Plus Reaction dialog to calculate heat of reaction. This heat of reaction is calculated as the sum of the IDEAL GAS heat of formation for the reactants and products; therefore, it might be far from the actual heat of reaction at given reaction condition.
Consider the following example:
2 H2 + O2 -> 2 H2O Hydrogen and Oxygen are in the gas phase.
Water is in the liquid phase.
The reaction takes place at 25 C, 1 atm.
The heat of reaction calculated by Batch Plus is 2.412E+5 J/mol, assuming water is ideal gas at 25 C, 1 atm. However, in actuality, water at standard condition is in the liquid phase; therefore, the heat of reaction differs by heat of vaporization for water at 25 C, 1 atm, which is 4.4E+4 J/mol.
Keywords:
References: None |
Problem Statement: Where do the vapor emission models in Batch Plus come from? | Solution: Vapor emission calculation in Batch Plus are adapted from the EPA Guideline Series:
Control of Volatile Organic Emissions from Manufacture of Synthesized Pharmaceutical Products, December 1978. EPA Publication No. EPA-450/2-78-029
Control of Volatile Organic Compound Emissions from Batch Processes, February 1993. EPA Publication No. EPA-450/R-94-020.
Federal Register EPA 40 CFR Parts 9 and 63, National Emission Standards for Source Categories: Pharmaceuticals Production; Final Rule, September 1998. EPA Publication Nos. EPA-453/R-94-026 and EPA-456/R-97-003
Keywords: vapor, emissions, EPA, CTG, ACT, MACT, model
References: None |
Problem Statement: Estimated parameters for liquid heat capacity (CPLDIP) are lost when switching the Run type option in Setup/Specifications from property estimation to Flowsheet. | Solution: Most property methods do not use a liquid reference state or hence the CPLDIP equation for the liquid enthalpy calculations. Therefore, when you switch from Property estimation to Flowsheet the CPLDIP form disappears as it will not be used in the calculations. The easiest way to change this is by making sure that CPLDIP is used by at least one property method referenced in the flowsheet calculations.
To use the liquid reference state for a Property Method, go to Properties | Specifications| Global sheet and check the box ?Modify property models? and ?Use liq. reference-state enthalpy?. When you modify the property method, give it a new name.
Now the liquid reference state will be used for this property method, and the CPL property on Properties | Estimation | T-dependent sheet will be enabled:
Alternatively, you can go to Properties | Property Methods | Routes, change the Property route to subordinate property and change the route ID for property DHL to DHL09:
By doing this change, you will not lose the estimated parameters CPLDIP when you switch your run type from Property Estimation, to Flowsheet.
You can see more information on using the liquid reference state inSolution3100 How to use liquid heat capacity parameters directly in a simulation.
Keywords: CPLDIP, cp, estimate
References: None |
Problem Statement: New Feature in Aspen Plus V7.2 - Physical Property Improvements | Solution: The following enhancements were made to the physical properties in V7.2.
New Electrolyte Models
The Symmetric Electrolyte NRTL activity coefficient model has been added, with corresponding property method ENRTL-SR. This model calculates activity coefficients based on a symmetric reference state for ionic components of pure fused salts. This model possesses several advantages over the original Electrolyte NRTL model:
In non-aqueous systems it removes the need to introduce water where there would otherwise be none.
For mixed-solvent systems, this is more convenient than the reference state of infinite dilution in pure water used by the original Electrolyte NRTL model.
This model calculates the Gibbs free energy and enthalpy from the same thermodynamic framework as the activity coefficient, rather than using mixing rules in systems with multiple electrolytes, as the original Electrolyte NRTL model did. This is more thermodynamically consistent for systems with multiple electrolytes, and in systems with no ions it is identical to NRTL-RK.
This model can handle zwitterions when they are designated by parameter ZWITTER = 1 and PLXANT/1 less than -1.0E10 (to make them nonvolatile).
The Unsymmetric Electrolyte NRTL activity coefficient model has been added, with corresponding property method ENRTL-RK. This model uses the same reference state for ions (infinite dilution in pure water) as the original Electrolyte NRTL, but uses the more consistent methods for calculating Gibbs free energy and enthalpy of the Symmetric Electrolyte NRTL model, as well as its new zwitterion feature. For systems with a single electrolyte, this should be identical to Electrolyte NRTL.
These new models require new electrolyte interaction pair parameters, since the parameters may be regressed from data associated with the reference state for ions. The new models can use existing NRTL binary parameters for molecule-molecule interactions and the same parameters for dielectric constant and Born radius as the original Electrolyte NRTL model.
New
Keywords: None
References: State
Additionally, a new option for the reference state for the activity coefficients of ionic components has been added to the Setup | Simulation Options | Reactions sheet. This must be set to Symmetric when using ENRTL-SR and to Unsymmetric when using ENRTL-RK or ELECNRTL. This is necessary to ensure consistency across the simulation, since this basis affects the equilibrium constants of electrolyte chemistry. It is not possible to combine symmetric and unsymmetric reference states for ions in the same simulation.
The electrolyte wizard has been updated to honor this new option. When using the symmetric reference state it will set the property method to ENRTL-SR. When using the unsymmetric reference state it will allow you to choose between ELECNRTL and ENRTL-RK.
New and Improved Property Models
The NRTL-SAC activity coefficient model has been updated with an extension to handle electrolytes. This is useful for systems where you would have used NRTL-SAC in the past if it were not for the presence of electrolytes. When no electrolytes are in the system, the results should be unchanged from past versions. An option code allows you to select either the symmetric (pure fused salts) or unsymmetric (infinite dilution in aqueous |
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