question
stringlengths 19
6.88k
| answer
stringlengths 38
33.3k
|
|---|---|
Problem Statement: After clicking the ?Config? button on the SLM Configuration Wizard, no system information is provided or the system configuration information dialog box is empty. | Solution: To solve this problem, the solution is to re-register the STRGXI2.dll file:
1. Re-register the STRGXI2.dll and it will re-initialize the SLM Configuration Wizard
2. Click Start | Run and inside the Run box enter: regsvr32 -u "C:\Program Files\Common Files\Hyprotech\Shared\strgxi2.dll"
3. Click OK to accept ??successfully unregistered??
4. Click Start | Run again and enter: regsvr32 "C:\Program Files\Common Files\Hyprotech\Shared\strgxi2.dll" inside the run box
5. Click OK to accept ??successfully registered??
6. Start the SLM Configuration Wizard and click on the ?Config? button. You should see the system information populated.
If the technical tip does not work, contact the AspenTech System Group for further guidance at 888-996-7100 option (2, 1) or submit an incident at www.support.aspentech.com.
Keywords: STRGXI2.dll
SLM Configuration Wizard
References: None |
Problem Statement: Our Korean customers are having some issues getting the locking information required to generate the dongle free license when they purchased the Desktop Engineering Edition for Small to Medium Enterprises. | Solution: To provide a Korean text guide for downloading the SLM tools 7.3 installer and to run it after installation to obtain locking information from SLM configuration Wizard.
See attached Link.
To download our SLM tools 7.3, please refer to solution article "Where can I download the latest version of Software License Manager (SLM)?" 133547
Keywords: SLM Tools 7.3, Desktop Engineering Guide, Dongle Free, SLM Configuration Wizard, Locking Information
References: None |
Problem Statement: From what formula does Aspen HYSYS derive its estimation method for the CH ratio in the Refsys Assay Manager tab? | Solution: If you go to the Basis Manager and then go to the Refsys Assay Manager Tab you can see in the right side the Property Blending Methods, the default for the C to H Ratio is Mass Blend (as you can see below) and the option of User Macro. If you choose the "Mass Blend" option, the equation used to derive the CH ratio is the following:
CtoHratio = 8.7743e-10 *exp(0.007176*Tb + 30.06242*spGr - 0.00735*Tb*spGr) *pow(Tb,-0.98445)*pow(spGr,-18.2753)
So it's dependent of the boiling point (Tb) and specific gravity (spGr).
Keywords: CHratio, estimation
References: None |
Problem Statement: What are the necessary steps to add a user with full access rights in the Aspen Plant Scheduler? | Solution: First the user should have to have a Configurer role to setup new user, below are the steps to add a new user to have SAVE or VIEW access:
· Open the case file, go to Role Based Trees | User Management | Add User tab
o Enter Userid and Description, then select Primary role
o Click the "Add" button
o The information in the lower frame of the Workspace updates to reflect your changes
· Go to the command line and type USERIDS
o This will open the USERIDS set
o Enter User and Description; right click on the set and select "Apply"
· Go to the command line and type USERINFO
o This will open the USERINFO table
o Enter Access Type - this can be only either "SAVE" or "VIEW"; right click on the table and select "Apply"
o Save the case
Keywords: Adding New User
User Management
USERIDS
USERINFO
Superuser
Super User
References: None |
Problem Statement: Aspen Plant Scheduler has 3 tiers: PS, PS-EA, PS-EO. Each of these tiers offer different functionalities and consumes different license keys and tokens. This solution explains how to switch a case file from one tier to another. | Solution: Aspen Plant Scheduler comes in 3 flavors:
· PS: (Plain) Plant Scheduler – for simulation based scheduling
· PS-EA: Plant Scheduler-Enhanced Automation – for simulation + search algorithms based scheduling
· PS-EO: Plant Scheduler-Enhanced Optimization – for simulation + search algorithms + linear programming / optimization based scheduling
Following commands can be executed to convert a model from one tier to another (depending on the requirements). These commands should be entered in the command line, which is found in the Developer tab of the application and executed using the Run button that can be found next to it.
· To convert a case file to PS: TIERPS
· To convert a case file to PS-EA: TIERPSEA
· To convert a case file to PS-EO: TIERPSEO
After running a command, you can call the table called APPDATA from the command line and scroll down to the row called PS_TIER and look at column 1’s value to confirm if the commands indeed changed the model’s tier.
For questions on how many tokens these tiers consume, please refer to your contract.
Keywords: TIER
Plant Scheduler
Enhanced Automation
Enhanced Optimization
Conversion
References: None |
Problem Statement: When I run a simulation in Aspen Petroleum Scheduler (APS) a message pops-up repeatedly:
Unable to open or create Schedule_LOG table
Unable to open or create Model_LOG table
What may be causing this and how to stop these messages from coming? | Solution: This type of error usually happens when working with a model located on a server and the connection is lost. In "User settings" you define the frequency with which you desire APS to check history about event or model modificatiosn and save this information in MODEL_LOG and Schedule_LOG. Some suggestions:
1.- Apply "Reconnect to the Database" option before do the simulation (if server connection failed)
2.- Increase the time in "User settings" for Schedule and Model query frequency. Working alone (not multi-user environment) try increasing the query frequency time , for example, to 10 min (Instead of 1 min) and see what happens.
Keywords: -User Settings
References: None |
Problem Statement: How to use or exclude" OXE"(Aspen Petroleum Scheduler, formally Orion, Excel Emulator) feature in some Excel worksheets? | Solution: Use the #OXE keyword to use OXE in place of Excel to perform user-defined calculations.
Use this keyword in the following worksheet types (Excel): INIT,PREP-POST,UNITS.
To indicate using OXE in place of Excel:
1 Enter the keyword #OXE in column A.
2 Enter a ?Y? or ?N? in column C to turn the OXE processing for the sheet ?ON? or ?OFF?.
Example:
Other option to use or not "OXE" in some excel worksheets is using OXECONFIG worksheet.
The Units workbook can contain an optional OXECONFIG worksheet that contains a list of data sheets for which you do not want OXE to construct internal sheets. OXE constructs (in-memory) internal sheets for all sheets that are referenced in Excel name definitions. This is because the Excel names may be referenced in the formulas or macros. If you are sure the contents of a sheet are not involved in the simulation, you may prohibit OXE from generating the internal sheet.
The example below instructs OXE not to generate in_memory sheet for sheet CRDRUN.
A
B
1
#NOOXE
2
CRDRUN
3
#END
Keywords: -OXE
References: None |
Problem Statement: Assays can now be passed between Aspen PIMS and Aspen Petroleum Scheduler through the use of a service. | Solution: How to use this Feature:
1.- DBUpdate must be completed prior to use this feature: Ensure that your APS database has been updated with the latest table definitions. If the import assay tables are missing, an error will appear and you will not be able to import assay data from PIMS. Run DBUpdate.exe to update your database.
2.- Install PIMS family v7.3 following the normal procedure. Just select "SERVER" installation at Aspen Tech Installer dialog box and select "Aspen Petroleum Scheduler Integration Services" on the Feature Selection dialog box, then complete the installation procedure.
3.- Setting up the services:
3.1.- Launch the APS Integration Services Configuration Tool from the menu. Communication services need to be configured prior to import. You will only need to do this once for each machine. From the Windows Start menu click Start | Programs | AspenTech | APS Integration Services Configuration Tool. This launches the APS Integration Configuration Services wizard.
3.2.- The first step in the services wizard sets up the Assay services. The user will need to input the computer name where the service is located and a port number for this service
3.3.- The second step of the Wizard allows the user to set up the KPI service for sending targets from PIMS to APS (future APS release). The user will assign the machine name where the service is located and assign a port for the service. The port should be different than the port assigned for the assay service.
3.4.- The third step sets up the End Point (or listening) service for the PIMS/APS integration service. The user will assign the machine name where the service is located and assign a port for the service. The port must be different from the KPI and assay service.
3.5.-Step 4 allows the user to dictate which APS model the PIMS data will be sent to. The user can find their database by using the browse button. If the database is a SQL database, a user ID and password must be provided.
3.6.-Step 5 allows the user to test the service configuration. Once the service has been tested, the user must hit finish to save their work.
If the user needs to set up multiple APS database to export to, they will need to set up services on different computers
Keywords: -APS Integration Services Configuration tool
References: None |
Problem Statement: A new option called "Gantt Chart Divider" has been added in Aspen Petroleum Scheduler (APS) and Aspen Multi-Blend Refinery Optimizer (MBO) v7.3.0.2 ,to provide a visual separation between Control variable list. | Solution: An option has been added to the "Selection" dialog box that allows users to add a divider line to the Gantt Chart display. This dialog box is used in multiple locations to allow you to select a property, parameter, component or other object.
Once the divider object has been added, users can use options on the " Control variables" dialog box to position the divider on the Gantt chart. Dividers provide a Visual separation between control variables.
To add a divider:
1. From the ?Control Variable? dialog box, click New Variable. The ?Select?dialog box appears.
2. Click the Displayed Object Types and select Gantt Chart Divider.
3. Click OK to return to the Control Variables dialog box. A DIVIDER row now appears.
4. Click associated with the DIVIDER row to select the row.
5. Click the arrow buttons to position the divider to the correct location.
Note the new "Divider" between THD1 and THCD control variables:
6. Repeat steps 1 to 6 to add additional dividers.
Keywords: Gantt Chart, Control Variable List
References: None |
Problem Statement: Is there a limit to the number of events that can be saved at one time?
There are times when the system goes idle, indicates not responding in Task Manager,and just sits there. | Solution: There is NO limit to the number of events you can save at one time.
These are some things to try to speed up writing and reading of the events table.Try using the BULK_EVENT_WRITE in conjunction with EVENTS_READ_USING_TMP_TBL in CONFIG table.
Also indexing the EVENT_SEQ number of any ATORIONEvent... tables where there are lots of records. The combination of the temp table and indexing should speed up the retrieval of the events from the database. When you save to the database, you always do a read at the end.
Keywords: None
References: None |
Problem Statement: This knowledge base article describes how to globally rename tags in Aspen Petroleum Scheduler, Aspen Refinery Multi-Blend Optimizer and Aspen Olefins Scheduler models. Globally renaming tags is accomplished using the ?Rename Tags Utility?, has been updated to provide easier use and expanded functionality. | Solution: Modifications made to tag names are immediately reflected in the Application database and the Units workbook. Once performed, this operation cannot be undone. Therefore, make a backup of your model before performing this task.
To rename tags in a Model:
1. - Access the program directory for your application (e.g., C:\Program Files\AspenTech\<application name>)
Use this dialog box to perform the following:
? Select the appropriate model database
? Select the Excel Units.xls file
? Log On to the utility
By default, this dialog box displays the last successful log on information.
3. - After click OK, the ?Rename Tags? dialog box is displayed as shown:
Use this dialog box to perform the following:
? Select the desired tag type(s)
? Select the tag(s) you wish to rename
? Enter the new tags
4. - Once a new tag has been entered , the utility will check corresponding Excel file and shows up the Replace Tags in Workbook Dialog Box
Use the Replace Tags in Workbook dialog box to view and confirm the new tags you have entered. This dialog box only appears if the new tags are associated with an Excel Units workbook.
Refer to the Rename Tags Utility online help for additional information on this tool.
For a list of tables that are affected by the rename application, refer to Things You Should Know When using this Utility found in the AtRenameTag help file (click HELP bottom on any of dialog boxes showing above)
Keywords: None
References: None |
Problem Statement: When apply "reload simulator" most the inventory tables are reading , such as: CRDINV,TANK_PROPS,TNKINV,MATERIAL,PARAMINV and also during each simulate ,why is it necessary to read them again every time we simulate all? | Solution: The reason is because there are customers who have external systems that change these tables directly and it is necessary to read these tables to make sure they are using data that are consistent with the database.
Keywords: -Simulation
-Reload Simulator
References: None |
Problem Statement: When you run code that uses the Microsoft Visual Basic for Applications Extensibility 5.3 Library, you may receive the following error message:
Run-time error '1004': Programmatic access to the Visual Basic Project is not trusted | Solution: Microsoft Office Excel 2003 and Microsoft Office Excel 2007 contain a security feature that allows you to choose whether programmatic access to the Visual Basic project is trusted.
The default setting is to NOT trust programmatic access to the Visual Basic project.
To allow programmatic access to the Visual Basic project, follow these steps, as appropriate for the version of Excel that you are running
Excel 2007
1. Click the Microsoft Office Button, and then click "Excel Options"
2. Click "Trust Center"
3. Click "Trust Center Settings"
4. Click "Macro Settings"
5. Click to select the "Trust access" to the VBA project object model check box
6. Click OK to close the Excel Options dialog box.
Excel 2003
1. On the "Tools" menu, point to "Macro", and then click "Security"
2. In the Security dialog box, click the "Trusted Sources" tab
3. Select the "Trust access" to Visual Basic Project check box
4. Click OK.
Keywords: Visual basic
error 1004
References: None |
Problem Statement: The new "Gantt &Trend Chart Options" dialog box has been added with 3 different tabs to meet the needs of the users for event, trend and font sizes views. in Aspen Petroleum Scheduler. | Solution: In addition to this modification, the following options have been added:
- The Hide Crude Runs by Crude Tank option has been added to the Event Filter tab that allows you to hide or show crude runs by crude tanks.
- The Max No of open Event views option has been added to the Graphic Features tab that allows you to select or enter the maximum number of event windows to have open at one time. This translates to the maximum number of event window tabs found on the Gantt interface. Default is 10, which is the limit. Opening more than the specified number causes the oldest window tab in the group to close before the newer window is opened.
- The Refresh Trends while Simulating option has been added to the Graphic Features tab that allows you to specify if trends should be updated during simulation and if so, at what frequency using the Min Refresh Frequency, hours option.
Keywords: -Gantt Chart
References: None |
Problem Statement: This knowledge base article describes why you may not be able to find the Report Wizard Add-In in the MS Excel toolbar. | Solution: This problem might have been caused if the Report Wizard was not selected during installation. Make sure that the Report Wizard option is selected under Aspen Refinery Multi-Blend Optimizer and Aspen Petroleum Scheduler during installation as shown in the screen shot:
Keywords: APS report wizard
MBO report wizard
Report wizard installation
References: None |
Problem Statement: When you run code that uses the Microsoft Visual Basic for Applications Extensibility 5.3 Library, you may receive the following error message:
Run-time error '1004': Programmatic access to the Visual Basic Project is not trusted | Solution: Microsoft Office Excel 2003 and Microsoft Office Excel 2007 contain a security feature that allows you to choose whether programmatic access to the Visual Basic project is trusted.
The default setting is to NOT trust programmatic access to the Visual Basic project.
To allow programmatic access to the Visual Basic project, follow these steps, as appropriate for the version of Excel that you are running
Excel 2007
1. Click the Microsoft Office Button, and then click "Excel Options"
2. Click "Trust Center"
3. Click "Trust Center Settings"
4. Click "Macro Settings"
5. Click to select the "Trust access" to the VBA project object model check box
6. Click OK to close the Excel Options dialog box.
Excel 2003
1. On the "Tools" menu, point to "Macro", and then click "Security"
2. In the Security dialog box, click the "Trusted Sources" tab
3. Select the "Trust access" to Visual Basic Project check box
4. Click OK.
Keywords: Visual basic
error 1004
References: None |
Problem Statement: The new "Gantt &Trend Chart Options" dialog box has been added with 3 different tabs to meet the needs of the users for event, trend and font sizes views. in Aspen Petroleum Scheduler. | Solution: In addition to this modification, the following options have been added:
- The Hide Crude Runs by Crude Tank option has been added to the Event Filter tab that allows you to hide or show crude runs by crude tanks.
- The Max No of open Event views option has been added to the Graphic Features tab that allows you to select or enter the maximum number of event windows to have open at one time. This translates to the maximum number of event window tabs found on the Gantt interface. Default is 10, which is the limit. Opening more than the specified number causes the oldest window tab in the group to close before the newer window is opened.
- The Refresh Trends while Simulating option has been added to the Graphic Features tab that allows you to specify if trends should be updated during simulation and if so, at what frequency using the Min Refresh Frequency, hours option.
Keywords: -Gantt Chart
References: None |
Problem Statement: Some questions about Automation routines for Aspen Petroleum Scheduler (APS) | Solution: 1.) Does the automation routine (VB, VBA, etc) need to be launched from an open APS session or can it be run in its separate window? If it can be running in its separate window how to configure the correct application?
Answer:
Automation routines can be launched in a separate vb application , or from within the excel opened as part of APS, as vba code. APS should be active, if it is not the routines can be executed to open model in APS, which will launch and open the model in APS.
2.) Do the automation routines interact with the database table only or can it read/write to/from memory?
Answer:
It really depends on the routine. Most routines are only in memory changes. Most automation routines are the same as what APS does via GUI(Gantt User Interface). If those functions in GUI are only in memory changes then that is how the automation does behave too, if the dialogs write the changes back to the database, then that is how the automation routine will behave. A function like "Addcase", which is available in 7.3.0.2, writes changes to the database. This is how the GUI feature behaves, and the automation will behave similarly. A function like create event and modify event are in memory changes only.
2a. If interaction with in-memory data is possible, do we need connecting string to the database or to the application?
One example :
Saving Events:
- There is a created Blend Event
- Modify it from the Gantt chart, for example, move it forward (change the start time)
- Save the changes (blend event) but in memory, without saving the model
Answer:
There are functions to create "BlendEvent", modify event etc. Once this is executed then the change is in memory only. Unless the model is saved, either from the GUI or via automation. Then the changes are written to the database.
Do not need to know the connection string to the database. All of that is taken care of by APS.
Keywords: -Automation method
References: None |
Problem Statement: New in V7.3 - Create a GOSP Model Using the Conceptual Design Builder - The Basics | Solution: V7.3 introduces the Conceptual Design Builder tool within Aspen HYSYS. The Conceptual Design Builder allows a user to quickly build a steady-state HYSYS model of a gas-oil separation plant (GOSP).
Data for the reservoir fluids and process design preferences are entered in a series of templates within the Conceptual Design Builder. A HYSYS model is then automatically built within minutes based on your selections.
The resulting HYSYS model can then be evaluated for capital and operating costs using the integrated economics workflow available within HYSYS.
The Conceptual Design Builder will build a HYSYS model that utilizes the new Aspen HYSYS Upstream V7.3 black oils functionality to define the reservoir fluids. So, a license to Aspen HYSYS Upstream is required for the Conceptual Design Builder.
This tutorial covers.
Part 1 : The Basics of using the Conceptual Design Builder
Keywords: None
References: None |
Problem Statement: What are the Operating System requirements for Aspen Cim-IO and Aspen Cim-IO Interfaces V7.3? | Solution: The Operating Systems requirements for AspenTech Production Management and Execution Products are found in the Aspen InfoPlus.21 product Family Installation Guide V7.3
Operating System requirements for Aspen Cim-IO and Cim-IO Interfaces V7.3
Windows Server 2003 R2 Standard SP2 (32-bit)
Windows Server 2003 R2 enterprise SP2 (32-bit)
Windows Server 2008 R2 (64-bit)
Windows XP SP3 (32-bit)
Keywords: None
References: None |
Problem Statement: Most virus scanners work by detecting when a file has been modified which may cause unnecessary activity by monitoring Aspen Cim-IO server. | Solution: To avoid unnecessary virus scan activity exclude the following folders from scanning:
..\Aspentech\Cim-IO (including all sub folders)
NOTE: If a custom Store File location was configured then that folder must also be excluded.
KeyWords:
Store and forward
virus
CIMIO
Keywords: None
References: None |
Problem Statement: TSK_M_XXX, the Cim-IO client task running the executable cimio_c_client.exe, starts in the InfoPlus.21 Manager, but does not work and contains this error in the .out file: Unable to read logical device record, retcode=2. | Solution: This error indicates that there is a configuration issue in the External Task record, defined by IOExternalTskDef, in the field IO_DEVICE. It is not pointing correctly to the Device record defined by IODeviceRecDef. In other words, there is most likely a spelling error.
Keywords: Cim-IO client
References: None |
Problem Statement: Main differences of SBO (Single Blend Optimization) in Aspen Petroleum Scheduler (APS) and Aspen Refinery Multi-Blend Optimizer (MBO). | Solution: Here are some differences:
1.-Component handling in Blends :
In SBO/APS blending is done in an approximate way and does not fully account for all the rundown volume and quality changes during the blend. Also the optimization is basically linear with minor corrections and without the MIP capabilities (for manifold component configuration constraints, threshold volume and recipe considerations). Also, the effects of shipments, receipts and transfers are not fully considered / optimized.
If you want more precision in SBO/APS , can simulate to the beginning of the event, then simulate to the end of the event, then subtract the 2 and add back in the amount used by the blend.
In SBO/MBO all the rundown volume and quality changes are taken into account (Component Rundown) and the optimization is truly nonlinear.
2.- Use Trend limit / available volume :
SBO/MBO uses the trend limit min/max (component tank), SBO/APS uses the available Volume to do the Optimization .
3.- MIP (Mixed Integer Programming) capabilities:
SBO/MBO has MIP capabilities. This task is used when the optimal solution contains volumes or recipe percents that are so small that they are impractical (teaspoon blending). All relevant MIP capabilities are enabled for manifold component configuration constraints, threshold volume and recipe considerations. All shipments, receipts and transfers are simultaneously optimized.
SBO/APS does not use MIP capabilities.
Keywords: - MIP
- Single Blend Optimization
References: None |
Problem Statement: What are Tokens? | Solution: A Token is an exchangeable unit of measure for software usage:
? Instead of licensing individual copies of our software, the Customer licenses exchangeable tokens
? The SLM License manager server has a number of products & tokens available for use
? When a product is used, it checks out a specific number of Dynamic Tokens. When the user closes the application, the tokens are returned to the SLM license manager server for other users/products
Keywords: Tokens
References: None |
Problem Statement: Aspen Polymers Example: Styrene-Acrylonitrile (SAN) free-radical polymerization | Solution: This example demonstrates the free-radical polymerization of styrene and acyrlonitrile to form SAN. The example accounts for the main polymerization reactions using the Free-Radical reaction model. A power-law reaction model is used to account for side reactions, including the formation of a volatile dimer and trimer as well as non-volatile waxy oligomers.
This example uses the NRTL property method with monomer/monomer binary parameters from the Aspen Plus databases. The vapor-liquid equilibrium in this sample file is not well validated and should be used with discretion.
This sample model is based on M. Tirrell and K. Gromley, Composition Control of a Batch Copolymerization Reactors, Chem. Eng. Sci., Vol. 36, No. 2, 1981.
Keywords: None
References: None |
Problem Statement: How can a user solve PDE using orthogonal collocation on finite elements (OCFE) in ACM? | Solution: In this article, we use a simple differential equation dy/dx = y as an example for OCFE solver. The important note is that the user need to use a reasonably large number of discretization nodes to get a good prediction.
Keywords: Orthogonal collocation, finite elements, OCFE, PDE, differential equation
References: None |
Problem Statement: Refinery utilties planner demo in Aspen Utilies planner (AUP) V 7.2 | Solution: Please find the attached zipped file with step by step instructions of typical refinery case in AUP V 7.2 demonstrating new features of Excel embedded data editor and marginal cost.
Keywords: Refinery, AUP, Excel, marginal cost
References: None |
Problem Statement: How do I create a single Equipment List for all types of equipment? | Solution: Create a single equipment list for all types of equipment
Many companies produce Equipment Lists that comprise a number of pages for one equipment type, further pages for the next equipment type, and so on. In many cases, a Cover Sheet is attached that displays some high-level project information and the revision history for the Equipment List.
Aspen Basic Engineering V7.2 now supports Equipment Lists that match this style. Attached viewlet explains the procedure to create a combined Equipment List, with a Cover Sheet. The combined Equipment List is truly a single document, with one document number, one revision history, and pages numbered sequentially across all the equipment types.
Keywords:
References: None |
Problem Statement: How to transfer generated standard Excel report data to Aspen Basic Engineering (ABE) using existing bridge.
Assumption: We always receive Excel report in a standard format, format does not change. | Solution: ABE bridge requires excel cells to be a named cells for which you want to transfer data, so our first step after receiving a standard excel report is to make cells as named cells for which you want to transfer data.
It may be time consuming process to name cells if you have many cells data that you want to transfer to ABE and also if you do this process manually then there is always a chance of manual error. To avoid this, you can create an excel macro that will generate named cells. Once you have a macro available this process would be pretty quick and consistent.
Example of excel macro code
Sub Macro1()
[E4].Name = "ItemNumber"
[E5].Name = "Diameter"
[E6].Name = "Length"
[E7].Name = "Volume"
[E8].Name = "Pressure"
End Sub
Above macro code will assign name to cells ?E4?, ?E5?, ?E6? and ?E8?.
Once you have named excel file then you can save that excel file as *.xls file and include it in your pre-configured bridge by replacing the existing excel file inside the bridge.
Now, you should be able to use already existing bridge with newly generated Standard Excel Report.
Please refer to attached zip file for detailed steps by step example files.
Keywords: bridge, use excel file in existing bridge
References: None |
Problem Statement: How do I model multiple service bays in Air Cooled Exchanger? | Solution: Starting with V7.2, Aspen Air Cooled Exchanger can now model the Multiple Services Bay using an Excel Template provided.
For V7.1 and earlier versions, to model multiple services in a bay, user need to set up separate EDR files in Simulation mode for each service, each with the same input bay width and total air flow rate. Enter an estimate of the air flow fraction for each service. Then manually iterate on the air flow fractions by running Air Cooled until the air side pressure drops for each service converge to within a reasonable tolerance. This process can be very time-consuming, so an Excel Template file is provided in V7.2 to:
? Load Air Cooled EDR files
? Interface with Air Cooled User Interface(UI) and Calculation Engine
? Perform iterative calculations to determine the fraction of the total air flow across each tube bundle
? Process and present results.
The following steps will help the user setting up a simulation for modeling Multiple Service Bays using the Aspen Air Cooled Exchanger in conjunction with the Excel Template provided.
Three new input items have been introduced in UI to facilitate the modeling of Multiple Service Bays.
1. Multiple services in bay: Under Input | Problem Definition | Application Options, specifies whether the current EDR file defines a service that shares a fan bay with one or more other services.
2. Flow fraction of air to this service: Under Input | Problem Definition | Process Data | Outside Stream, specifies the air flowrate that applies to the service defined in the current EDR file.
3. Bay width: Under Input | Exchanger Geometry | Unit Geometry | Unit Geometry, specifies the plenum dimensions and provide a reference dimension for the fan size.
Setting up the Excel Utility:
1. Make copy of the Excel Utility provided in this solution or from the installation directory.
2. Develop EDR files for each of the services. The tube lengths of each of the bundles must be identical.
3. The utility Edits the EDR files and Save the changes. So make a back-up copy of the original files in another folder or create a new folder and reference the folder name in the field Folder for EDR files with results.
4. Open the Excel Utility - AirCooled_Multiple_Service_Analysis.xls
5. Decide on the units of measure for the sheet, by clicking on the button for SI or US
6. Go to the Tab named Calculation Sheet and enter the folder where the EDR files are located
7. Enter the filenames in the row headed "EDR filename"
8. Enter the total air flowrate and air inlet temperature
9. Enter the bay width, fan diameter and number of fans
10. Press the button titled "Import Data from Files"
11. Press the button titled "Run Multi-Service Analysis"
12. When the calculation is complete, scroll down to check the progress of the Iterations. The tube bundle pressure drops
13. Also examine the Calculation Results displayed for each service and check that the calculated duty for reach service
14. Guidelines are also listed in Tab named Instructions.
In the attached file, three different service bays are simulated with Excel utility and Aspen Air Cooled Exchanger program and presented with the results.
Note: To run the attached file, Download and save the files to your local drive and change reference folder name to Air Cooled exchanger files to match the location on your machine.
Troubleshooting: If utility does not work as expected check the following.
1. Make sure the macros are enabled. In Office 2003, go to Tools | Macros | Security and set it to Low. In Office 2007, Click on the Office Button at left hand top corner and go to Excel Options | Trust Center | Trust Center Settings | Macro Settings | select Enable All Macros and click OK.
2. Since this utility works only with EDR V7.2 and later versions, and if you happen to have multiple versions installed on your machine, then run the Version Control Utility from Start | Program (All Programs) | AspenTech | Aspen Exchanger Design and Rating V7.2 and fix the version to V7.2. To run the Version Control utility, user needs administrative rights on the machine.
Keywords: Multiple Service Bays, Mutliple Service, Bays, Air Cooled, Air-Cooled.
References: None |
Problem Statement: How do I calculate the final pressure in a closed vessel when temperature changes? | Solution: The easiest way to simulate this is using a RBATCH block. In the example attached a tank with a mixture of n-pentane and n-butane is simulated. Specify final temperature, tank volume and select to calculate reactor pressure:
Since this a non-reactive system, uncheck the box ?reactive system? in the reactions tab:
Specify a stop criteria for the simulation:
Alternatively you can model this with a Heater block. Specify the final temperature and an estimated final pressure. The final pressure will be varied by a design spec to ensure that the volume flow does not change. Note that the two approaches yield similar calculated pressures.
Keywords: isolated, unsteady
References: None |
Problem Statement: Example for modeling an A or V frame in Aspen Air Cooled Exchanger | Solution: See attached "A Frame Simulation.EDR" for details on modeling the A frame using Aspen Air Cooled Exchanger.
When modeling an A or V frame, the following steps need to be followed:
- Select the Rating/Checking or Simulation mode (Input | Problem Definition | Application Options)
- For an A-frame with the tubeside flow downward as shown:
- Under Input |Exchanger Geometry | Unit Geometry select the following options
According to the frame that you require to model against Exchanger Frame type:
a) A Frame - Select 'Forced draught'
b) V Frame - Select 'Induced draught'
In Exchanger Geometry |Unit Geometry | Unit Geometry tab, enter the Angle of outside flow. This is used to determine the direction of the X-side flow:
0? is set for vertically upward flow
90?C for horizontal flow
180?C for vertically downward flow
For the case above the outside flow will be directed at 60?to the vertical and perpendicular to the tubes.
To show that the tube side flow is downward in the tubes we set the ?Tube side flow direction? to: Downward (any angle).
For an A-frame with the tubes horizontal as shown below:
The following settings would be appropriate:
Although you may specify A & V frame exchangers and the program will rate or simulate these geometries, at present the AirCooled setting plan can only render illustrations of conventional exchanger geometry.
Keywords: A and V frame
Air Cooled Exchanger
Example
References: None |
Problem Statement: New Feature in Aspen Plus V7.2 - New scaling examples | Solution: These files describe Aspen Plus models for predicting scaling potential of sulfate minerals and carbonate minerals in complicated brine at 0.1 MPa. Solids NaCl, NaCl?2H2O, Na2SO4, Na2SO4?10H2O, BaSO4, CaSO4, CaSO4?2H2O, SrSO4, BaCO3, SrCO3, CaCO3, MgCO3?3H2O, MgCO3?5H2O, and Mg(OH)2 are included in this model. These models consist of a flash block to estimate the liquid-solid equilibrium for this systems. The thermophysical properties are studied, and wherever possible, model parameters have been estimated and validated against experimental data from open literature.
The model includes the following key features:
? True species including ions
? 2009 electrolyte NRTL activity coefficient model for liquid phase nonideality and PC-SAFT equation of state for vapor phase
? Thermodynamic equilibrium between solid and liquid phase
Keywords: None
References: None |
Problem Statement: New Feature in Aspen Plus V7.2 - New and updated amine examples | Solution: Aspen Plus has a number of rate-based models of the CO2 capture process using different amines. In V7.2, a new example using aqueous solutions of mixed piperazine and methyl-diethanolamine (PZ+MDEA) was added. In addition, the examples using ammonia (NH3), methyl-diethanolamine (MDEA), monoethanolamine (MEA), 2-Amino-2-Methyl-1-Propanol (AMP), and piperazine (PZ) were revised and updated. See the PDF documents accompanying each one for more details about the processes.
These new example simulations are included in the C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\App\Amines directory and are attached to this solution document.
NOTE:
The Rate-Based PZ+MDEA Model shipped with V7.2 is missing some parameter values. The file attached to this solution document has been modified to include the following parameter values:
? The IONMUB parameter for HCO3- and CO3-3 should be 0.09469 cum/kmol and 0.5641 cum/kmol respectively.
? The VLQKIJ for MDEA and H2O is -0.1106115180 and that for PZ and H2O is -0.1980222.
? The MUKIJ for H2O and MDEA is Aij = 0.1902388020, temperature is given in Kelvin.
? The MULIJ for H2O and MDEA is Aij = 1.41596620 and Aji = -1.41596620, temperature is given in Kelvin.
? The IONMUB for MDEAH+ is 0.50940199 cum/kmol.
Keywords: None
References: None |
Problem Statement: How do I model removal of sulfur from coal? | Solution: Coal can be modeled as nonconventional (NC) solid in Aspen Plus. A RSTOIC reactor can be used to remove the moisture content to dry the coal (refer to Aspen Plus Getting Started Modeling Processes with Solids). The simulation of removing non-moisture content from coal is more complicated than removing water only, because all the NC attributes need to be updated, e.g. the ones included in PROXANAL, ULTANAL, and SULFANAL.This solution provides an example of removing non-moisture attribute from NC component, such as removal sulfur from coal. The details are documented in the attached word file and Aspen Plus backup file.
Keywords: Coal, sulfur
References: None |
Problem Statement: The hypothetical components in Aspen HYSYS do not have any chemical formula. A gross estimation for the chemical formula can be useful if the simulation requires chemical reactions. The formula can be estimated from molecular weight of hypothetical components with certain assumptions. | Solution: This solution provides a macro which splits the components into carbon and hydrogen assuming that the hydrocarbons have a gross formula as
C(n)H(an+b).
The sample code given below sets a = 2 and b = 2. This effectively represents the paraffinic components. The code below can be modified if necessary.
========================================================================================
'Macro Description start
' Estimates the gross formula hydrocarbons
' It is assumed that the hydrocarbons have a gross formula that is
' Cn H an+b
' the code sets a=2 and b=2, for other values, change code below
'
' Written by: Wim Van Wassenhove, E-mail [email protected]
' Version info
' Date: 13/11/1999
' Version 1.0
'
'Macro Description end
Sub Main
Dim a As Double
Dim b As Double
Dim tvar As Variant
a=2
b=2
Dim hpgr As Object
Dim hpcmp As Object
Set MyCase=ActiveCase
MyCase.BasisManager.StartBasisChange
If MyCase.BasisManager.HypoGroups.Count <> 0 Then
For Each hpgr In MyCase.BasisManager.HypoGroups
For Each hpcmp In hpgr.HypoComponents
If hpcmp.Class=200 Then
HCMW = hpcmp.MolecularWeight
CAtom = (HCMW-b)/(12+a)
HAtom = a * CAtom + b
Dim ff As Double
Dim fformula As String
If CAtom > 0 Then
fformula = "C" + Format(CAtom, "0.000")
End If
If HAtom > 0 Then
fformula = fformula + "H" + Format(HAtom, "0.000")
End If
hpcmp.Formula = fformula
tvar = hpcmp.GibbsCoeffs.Values
tvar(1)=0
tvar(2)=0
tvar(3)=0
hpcmp.GibbsCoeffs.Values=tvar
End If
Next
Next
End If
MyCase.BasisManager.EndBasisChange
End Sub
=========================================================================================
Refer solution ID 109174 for using a macro in Aspen HYSYS.
To test the above macro follow the steps given below:
1. Down the macro and HYSYS files.
2. Open the HYSYS file. This file contains a stream and the component list contains pure as well as hypothetical components.
3. From the menu bar select Tools and then Macro Language Editor.
4. From the Macro Language Editor open the file with extension WWB.
5. Now click the Start/Resume button in the Macro.
The macro will run and create gross formula for the hypothetical components.The screenshot below shows the chemical formula for a component.
Keywords: Macro, Gross Formula
References: None |
Problem Statement: Examples for the new electrolyte models in V7.2 | Solution: Three examples are attached:
1) enthalpy.bkp: Calculate the enthalpy using ENRTL-RK, ELECNRTL, and NRTL-RK for non-electrolyte systems.
? The analysis "ELECNRTL" is to show ELECNRTL is not entirely self-consistent
? The analysis "ENRTL-RK" is to show ENRTL-RK is fully self-consistent
? The analysis "ELEC-2" is to show ELECNRTL is not entirely consistent with the standard NRTL-RK when compared to the analysis ?NRTL-2?
? The analysis "ENRTL-2" is to show ENRTL-RK is entirely consistent with the standard NRTL-RK when compared to the analysis "NRTL-2"
.
2) multiple_electrolyes_drs.bkp: Data Regression for multiple electrolyte systems using ENRTL-RK and ELECNRTL. The electrolyte-electrolyte pair parameters and equilibrium constants are determined by data of the solubility of salts in the aqueous solution. The solvent-electrolyte pair parameters are the same in both ENRTL-RK and ELECNRTL and retrieved from Aspen database. Due to different mixing rules used, the electrolyte-electrolyte pair parameters and equilibrium constants are different. Both models are able accurately to correlate data but ENRTL-RK does a slightly better job
3) non_aqueous_solution_ENRTL-SR.bkp: Data Regression for non-aqueous solutions with ENRTL-SR. The solvent-electrolyte pair parameters and equilibrium constants are determined by data of the solubility of salts in mixed-solvent solutions
Keywords: solubility, salts, benzene
References: None |
Problem Statement: How do you set up a number of sensitivity case scenarios in Equation Oriented (EO) Mode as you do in Sequential Modular (SM)? | Solution: Solution 125039 A procedure of how to set up and perform a sensitivity analysis in EO mode shows a procedure to set up a sensitivity analysis in EO mode. Unfortunately there is no functionality in the Graphical User Interface to run several EO cases automatically in a similar fashion as in SM mode. A script can be used to run several cases automatically in EO mode.
Here you can find an example were a script is used to solve various EO cases and tabulate the results in a text file. The script varies the temperature of the inlet stream to a column and the mole fraction of C2H4 in the bottoms; the dependent variables are the distillate mass flowrate and the reboiler duty. The script modifies the variables in a way such that all possible combinations of the variables are considered.
To reproduce these results, load the BKP file into the Aspen Plus Graphical User Interface, solve the simulation in SM mode, switch to EO in Simulation mode and invoke the script by typing INVOKE SMSENSEO at the command line. The script will drive the problem through a series of Simulation solutions and write the resuls to results.txt.
Keywords: Case study, scenario, multiple cases.
References: None |
Problem Statement: How can I model the heat transfer in the reactor as a function of the driving force (temperature in the medium) | Solution: Use a Design-spec where you specify the reactor duty to be QR=hA(T-To) where hA is the heat transfer coefficient multiplied by the contact area (considered constant in this example), T is the reactor outlet temperature and To is the temperature of the medium. The reactor duty is fed to a heater block where it exchanges heat with the medium. The design-spec varies the reactor heat duty in order to match the required Q=hA(T-To).
Keywords: Heat transfer, ambient, jacket
References: None |
Problem Statement: How do you set up a sensitivity case scenario in Equation Oriented Mode? | Solution: Solution 125039 A procedure of how to set up and perform a sensitivity analysis in EO mode shows a procedure to set up a sensitivity analysis in EO mode. Unfortunately there is no functionality in the Graphical User Interface to run several EO cases automatically in a similar fashion as in SM mode. A script can be used to run several cases automatically in EO mode.
Here you can find an example were a script is used to solve various EO cases and tabulate the results in a text file. The script varies the temperature of the inlet stream to a column and the mole fraction of C2H4 in the bottoms; the dependent variables are the distillate mass flowrate and the reboiler duty.
To reproduce these results, load the BKP file into the Aspen Plus Graphical User Interface, solve the simulation in SM mode, switch to EO in Simulation mode and invoke the script by typing INVOKE SMSENS3 at the command line. The script will drive the problem through a series of Simulation solutions and write to temp.txt.
Keywords: Case study, scenario, multiple cases.
References: None |
Problem Statement: The number of stages and feed stage location cannot be a VARY (manipulated variable) within RADFRAC. However, both number of stages and feed stage location can be manipulated with a Sensitivity Analysis and an external Design-Spec provided the manipulated value is an integer value. In a Sensitivity Analysis, the user can specify integer values to by evaluated by either listing the values or specifying the upper/lower bound and number of points or increment. However, in a Design-Spec, the convergence algorithm determines the next guess between iterations. How do you make sure the number of stages being manipulated is always an integer value when using a Design-Spec. | Solution: To insure the number of stages is an integer value, the Design-Spec manipulates a global Parameter which in turn is processed by a Calculator block that uses the Fortran function INT (returns the integer value of a real number) to set the number to an integer value. The Calculator block then sets the next guess for number of stages in the RADFRAC block. An example of this application is shown in the attached BKP file. In the example, a Design-Spec is varying the number of stages to obtain a specified mass flow of water in the distillate stream.
There are a couple of considerations to be noted:
1) The upper bound for the number of stages in the Design-Spec should not be higher than the base number of stages set on the RADFRAC Setup | Configuration sheet. When varying the number of stages Aspen Plus will not allow a value larger than the base value.
2) Convergence of the Design-Spec may be somewhat difficult. Since the number of stages has to be an integer, there is a good possibility that the next guess and previous guess from the convergence algorithm could be the same value. Therefore the objective function will show no response. This can usually be alleviated by using the "Bracket" or "Check Bounds" option for the Secant convergence algorithm.
3) Be careful setting the tolerance used for the Target for the Design-Spec. Again since the number of stages has to be an integer, a tight tolerance may result in the Design-Spec not converging.
Keywords: RadFrac, number of stages, NSTAGE
References: None |
Problem Statement: How can I simulate an isothermal column? | Solution: Here is an example on how you can include design specs in a column to achieve isothermal conditions.
To set the temperature on a stage, you need to add or remove heat. This is done by including a heat stream for each stage with a corresponding design specification (on the RadFrac column's Design Specs form) that sets the stage temperature to a certain value by varying the heat stream duty. The heat stream is included on column's Vary form. In the example, the column has three stages; therefore, three heat streams need to be specified.
Keywords: isothermal, RadFrac,
References: None |
Problem Statement: Rate-based coal gasifier examples | Solution: There two rate-based coal gasifier examples shipped with Aspen Plus. One is for an entrained flow coal gasifier and one is for a moving bed coal gasifier. Both simulation files and a PDF file describing the details of the model are included.
These files are located in the following location:
V9 and earlier: C:\Program Files (x86)\AspenTech\Aspen Plus Vx.x\GUI\Examples\
V10 and later: C:\Program Files (x86)\AspenTech\Aspen Plus Vx.x\GUI\Examples\Power\Coal Gasification
Aspen Plus Model for Entrained Flow Coal Gasifier
File: Aspen_Plus_Model_for_Entrained_Bed_Coal_Gasifier.apwz
This file describes an Aspen Plus kinetics-based model for Texaco down-flow entrained flow gasifiers. The model follows the modeling approach proposed by Wen and Chaung.
The model includes the following features:
The model is a steady-state model.
The model accounts for major physical and chemical processes occurring in the gasifier, i.e. coal pyrolysis, volatile combustion, and char gasification.
The reaction kinetics for char gasification is considered.
The hydrodynamics to calculate solid residence time is taken into account.
The gas phase is assumed to be instantaneously and perfectly mixed with the solid phase.
The pressure drop in the gasifier is neglected.
Coal particles are assumed to be spherical and of uniform size.
The ash layer formed remains on the particle during the reactions based on the unreacted-core shrinking model.
The temperature inside the coal particle is assumed to be uniform.
Aspen Plus Model for Moving Bed Coal Gasifier
File: Aspen_Plus_Model_for_Moving_Bed_Coal_Gasifier.apwz
This file describes a comprehensive Aspen Plus model for countercurrent moving bed coal gasifiers.
The model includes the following features:
The model is a steady-state model.
The model considers all the processes occurring in the gasifier, i.e. coal drying, coal pyrolysis, char gasification, and char combustion.
The kinetics for char gasification and combustion are included.
Coal drying and pyrolysis take place instantaneously at the top of gasifier.
The variable bed voidage throughout the gasifier is taken into account.
The solid and gas phases flow in a plug-flow pattern.
The pressure drop in the gasifier is neglected.
The solid and gas temperatures are equal inside the gasifier.
Keywords: None
References: None |
Problem Statement: New Feature in Aspen Plus V7.2 - New and updated CO2 capture process examples using the physical solvent DEPG | Solution: Aspen Plus has a number of rate-based models of the CO2 capture process using different physical solvents. In V7.2, the DEPG example was completely revised. See the attached documentation for more information.
This example simulation is included in the C:\Program Files\AspenTech\Aspen Plus V7.2\GUI\App\Physical solvents directory and is attached to this solution document.
The simulation is an Aspen Polymers model of the CO2 capture process with physical solvent DEPG from a gas mixture of CO, CO2, H2, H2O, N2, Ar, CH4, NH3, and H2S generated from gasification of Illinois No. 6 bituminous coal.
DEPG is a mixture of the dimethyl ethers of polyethylene glycol with formula CH3O(C2H4O)nCH3 where n ranges from 2 to 9. This model treats each DEPG component as a compound made up of a CH3OCH3 end segment and n C2H4O repeat segments. Aspen ideal gas heat capacity parameters for CH3OCH3 and C2H4O segments are regressed against ideal gas heat capacity data generated from DIPPR correlation for individual DEPG components (n=2 to 5). The literature data of individual DEPG components (n=2 to 5) for vapor pressure, liquid density and liquid heat capacity are used to determine parameters for CH3OCH3 and C2H4O segments of the copolymer PC-SAFT equation of state. The available vapor-liquid equilibrium data for selected gas components in DEPGs are further used to identify the PCSAFT
binary interaction parameters for various gas and segment pairs.
The model is validated with the literature data on vapor pressure, liquid density and heat capacity for DEPG solvent, relative solubilities of gas components in the DEPG solvent and commonly accepted design cases for CO2 capture with the DEPG solvent.
The operation data for the CO2 capture process from an engineering evaluation design case by Energy Systems Division, Argonne National Laboratory (1994) are used to specify the feed conditions and unit operation block specifications in the process model. The designed packing information from the literature is also included in the process model. Since only the equilibrium stage results are available in the literature, the process model developed here is based on the equilibrium stage distillation model instead of the more rigorous rate-based model.
The model includes the following key features:
? Copolymer PC-SAFT equation of state model for calculating vapor pressure, liquid density, heat capacity, and phase equilibrium
? Equilibrium distillation model for absorber with designed packing information from the literature.
Keywords: None
References: None |
Problem Statement: Sample file to illustrate the use of the integrated costing and sizing functionality with Aspen HYSYS | Solution: This example Aspen HYSYS file is design to assist you in exploring and understand the integrated economics capability in Aspen HYSYS, which will enable you to launch Aspen Process Economic Analyzer from within HSYSY and to run an economic calculation transparently. For additional details on the use of the integrated economics capability, we have also posted a self learning tutorial at:
https://www.brainshark.com/aspentech1/HYSYS_Costing
Keywords: costing, sample
References: None |
Problem Statement: Column - Feed Tray Optimization using Automation | Solution: There are 2 versions included here:
? Old version allows to perform case study and the feed location is varied for single feed only.
? New version which deploys takes advantage of the OLE capabilities of HYSYS. This allows to find the ideal location of a Distillation column feed. This algorithm uses a Newton's method with a line search to calculate the optimum feed location based on the column's heat duty in a distillation column with up to 4 feeds. It has been tested with columns that have few stages to super-fractionator.
Instructions:
1. Open HYSYS and load the simulation file
2. Open the Excel file "Column Stage Optimization.xls"
3. Click on "Initialise Case" to link Excel with Aspen HYSYS.
4. Select the column Name, Tray Section name as well as the feeds name.
5. Enter the bounds as a fraction of the total number of trays of the tray section.
6. Enter the relative location as a starting value estimate. I haven't found a way to determine the current feed location, so that will be ignored for now.
7. Select Total energy consumption (ie the sum of all the energy streams heat duties) or just for one stream. The feed location will be calculated to minimize the energy.
8. Click on "Run Case"
Note: If there is a crash during calculation, clicking the "Run case" from Excel should re-load the simulation file correctly as file name and location as already shown in the spreadsheet.
Limitations / Recommendations:
? It has been tested in HYSYS v7.1 and v7.2
? The optimizer seeks to minimize either all the energy streams or a selected energy stream. However, if you have a heat exchanger as a reboiler or condenser this will not be taken into account.
? All the feeds must be attached in the same tray section.
? The feed stream name must be the same in the main flowsheet and the column's flowsheet. If the configuration is different then you can fix this problem by disconnecting and reconnecting the feeds from the column flowsheet.
? If you seek to optimize more than 3 feeds it is recommended to provide a good estimate, otherwise the optimizer may not be able to find the global minimum for the correct tray locations. .
? It is recommended to start with 1 or 2 feeds first, run the optimizer and then add the remaining feeds and perform the final optimization.
? It is recommended to provide a good starting point for the feed location.
An updated version has been posted (1.4.1), this is the change log:
? Fixed an off-by one error on the final solution (the solution at times was off by one stage)
? Added a reset button.
? Added the option to hide Aspen HYSYS. This can increase the performance by at least 15% for some cases with frequent automation calls.
? fixed an error where the Aspen HYSYS type library features weren't recognized for some computers
Keywords: column feed tray optimization
References: None |
Problem Statement: Fired heater example in Steady State. | Solution: The attached example file illustrates a simple fired heater model to heat the atmospheric crude column feed to desired inlet temperature. To setup the Fired Heater in steady state mode, the following parameters must be specified.
1. Components O2, N2, CO, CO2, H2O must be added to your component list.
2. Air should be defined as N2/O2 mixture. Do not add Air as separate component.
3. Make sure the feed, air(N2+O2) and fuel stream are fully defined and connected to the Fired heater.
Note: If you have multiple passes for feed in the radiation zone, then specify the # of external passes and then split the feed into that many feed streams and add the respective number of product streams.
In the attached example, Preflash liquid crude is passed through fired heater. The fired heater uses the Natural gas a fuel and the air(N2+O2) is used for O2 supply for combustion.
4. Enter the Efficiency (Only SS) on the Parameters Tab of the Fired heater property interface. In general fired heater efficiency usually fall in the range of 60-80%, so an efficiency of 75% is used in the model.
5. Add the Flue Gas outlet stream and Process Outlet stream.
As of HYSYS V7.2, fired heater calculations are limited to Radiation zone only in Steady State mode. It is recommend to perform Convective and Economizer zone calculations separately. Though the program lets you specify the feed streams and product streams in Convective and Economizer zones, no calculations will be performed in these zones and simply feed conditions will be passed onto product streams.
Note: Combustion Options such as Flame status, combustion boundaries are a dynamic simulation parameter.
Keywords: Fired heater, Steady State, Sample
References: None |
Problem Statement: Example of CO2 removal process by DEPG. | Solution: The attached file is an example of CO2 removal process by DEPG solvent. Most of the gas sweetening processes have similar process flow-sheet.
In this example PC-SAFT is used as property method. It is accessed from Aspen Properties.
New EO Subflowsheet is used to simulate this process.
If you are in the main PFD, you will see an icon of a subflowsheet only. Double click on it and enter subflowsheet environment.
The PFD is shown below.
All of the specifications and process conditions are arbitrarily chosen.
Note: The file was created in Aspen HYSYS version V7.2 CP1. An older version can not open it. You may need license of Aspen Properties and New EO Subflowsheet.
Keywords: DEPG solvent, CO2, removal
References: None |
Problem Statement: How to get simulation status using VBA (Visual Basic for Applications)? Do you have any example? | Solution: For an example refer to attached excel file.
We have used statement,
go_Simulation.Tree.Data.AttributeValue(HAP_COMPSTATUS) in a public function in module and then we have called it after simulation run from Private worksheet code.
You should also refer to solution ID: 110783 and 130369 for more detail information on Status code.
Keywords: simulation status
References: None |
Problem Statement: Paste links no longer work after V7.2 | Solution: OLE paste links (the live, updating link to a data value in Aspen Plus created when it is copied and pasted into an application which can support such links, such as Microsoft Excel) are discontinued after V7.2. It will still be possible to copy and paste data, but without the live link. This mechanism has been the source of problems, including slow copy and paste of large amounts of data. There are other techniques (OLE automation and Aspen Simulation Workbook) to link models to Excel and other applications, and these techniques will remain available.
Keywords: None
References: : CQ00405763 |
Problem Statement: When trying to import a XML file using ImportBatchDataXMLForScripting() you get the following result in the xmlResult file:
<Description>
Relational Database Error: Relational Database Error -2147217887: Invalid character value for cast specification.
</Description> | Solution: Timestamps should be specified when importing XML into V7.1.x.
Here is an example format:
2010-01-14T14:43:00
Batch example:
<BatchData xmlns="Aspentech.Batch21.BatchData">
<Area name="Demo2">
<Batch>
<Designator name="Batch No">976</Designator>
<Characteristic name="Batch Cost" instance="last" forceOverwrite="1">
<Value>1510</Value>
<Timestamp is UTC="1">2002-10-07T23:01:25</Timestamp>
</Characteristic>
</Batch>
</Area>
</BatchData>
Note: In V7.2 timestamps are allowed to be missing (default to NOW.)
Keywords: XML
Import
ImportBatchDataXML
References: None |
Problem Statement: For version 5.0 the Batch.21 Definition XML schema was altered to include security descriptors. But because the schema was designed with all closed elements, this means that different versions of the schema are not interoperable. In addition, since there is no version information, the schemas are indistinguishable. This breaks backward compatibility. There needs to be a method for determining the version of the XML schema, if it is altered. In addition, having an open model would permit better compatibility between versions (and tools built against a particular version). | Solution: The API no longer validates against the schema for version 6.0, which eliminates inadvertently denying XML submittal that will function. Extra non-relevant elements are ignored. If you pass in "acceptable" XML then it will be handled appropriately. No alterations to existing elements or attributes have been made -- however additional elements and attributes have been added. In addition, XDR schemas are being phased out, and no XSD schema is currently being developed or supported.
KeyWords
Batch.21, XML, Schema
XSD file
Keywords: None
References: None |
Problem Statement: As listed in the Release Notes, a new feature in V7.2 is an ODBC driver (CQ00245995). This key enhancement adds a whole new level of accessibility to Production Record Manager data, however the documentation on how to configure and use the driver is not included in the V7.2 Help files. | Solution: Attached is a Word document covering the configuration and usage of the Production Record Manager ODBC driver. The information will be incorporated into the Help files for V7.3 (CQ00413280.)
IMPORTANT NOTES:
1. The attached documentation refers to V7.1, however please note that the ODBC driver was in fact not included with any general patch for V7.1. The Documentation is intended as a help to configure and use the ODBC driver for aspenONE V7.2, the first aspenONE release to include the ODBC driver.
2. The Documentation refers to an ODBC Test application. That Test application did not ship with aspenONE V7.2, but is available from KB 130987.
Keywords: batch
batch.21
data access
References: None |
Problem Statement: What's New in Aspen Supply Chain Connect (ASCC) V7.2 | Solution: Aspen Supply Chain Connect is an enterprise-level solution that seamlessly integrates the aspenONE? Planning and Scheduling suite with ERP solutions. It has the ability to rapidly move very large quantities of real-time data from multiple sources through a relational database repository, providing the foundation for multi-user collaborative planning and scheduling, web-based reporting and analytics.
Informatica Upgrade to 8.6.1
Aspen Supply Chain Connect includes an important upgrade to Informatica from v 8.1.1 to v8.6.1. This upgrade provides compliance for the product running on Foreign OS, Windows Server 2008 and a full support for the following foreign languages: German, Japanese, and Chinese.
Quality Improvements
A major focus of the release was addressing a backlog of less severe product defects that had accumulated over the past few releases. Approximately 25 such defects have been fixed in this version.
For more information on some of the defects please refer the Release Notes
Keywords: Informatica 8.6.1
Localization
ASCC V7.2
References: None |
Problem Statement: What databases are supported for Aspen SCM V7.2 on Windows 2008 Server R2 (64-bit) operating system? | Solution: Aspen SCM V7.2 supports Oracle and SQL database servers.
The supported servers are:
? Microsoft SQL Server 2005 SP3 (Standard Edition)
? Microsoft SQL Server 2005 SP3 (Enterprise Edition)
? Microsoft SQL Server 2008 SP1 (Enterprise Edition)
? Oracle 9i Database Release 2
? Oracle 10g Database Release 2
However, Oracle Client 10.2.0.4 is required for Windows Server 2008 to function properly.
Keywords: Database
Data Base
References: None |
Problem Statement: What happens if you SELECT against TCHOSEN ?
What does MIMI SWITCH 66 do?
If you have the following SELECT statement on the TCHOSEN table in your code, it will work with MIMI versions earlier than 7.2, but it will cause erroneous results with MIMI 7.2 and later. You will not have an error, just bad data.
/* This doesn't work */
AMPSET &8 = CX
SELECT TCHOSEN(*&8,*) | Solution: The syntax used here is:
SELECT table(rowmask,colmask) [{CO|DE}[{CO|DE}]]
rowmask: (Required) Indicates which rows you want to select. Can include masks.
colmask: (Required) Indicates which columns you want to select. Can include masks.
In the example the user would like to select all the rows of table TCHOSEN whose rowset's code ends by the string CX (* is a wildcard representing any number of characters).
When the user replaced this line with the following ones, he got the expected results. Why?
/* This fixes it */
AMPSET &8 = CX
COPY TCHOSENC INTO ZCHOSENC
COPY TCHOSENC INTO ZCHOSENR
SELECT ZCHOSEN(*&8,*)
MIMI cannot guarantee you will get the results that you expect if you use SELECT like this, where TCHOSEN is at the same time the input and the output of your selection. The fix above worked because it avoided this situation.
In MIMI7.2 we have a new implementation of SELECT which greatly reduces the memory consumption and improves the performance in the execution of the command. The new implementation doesn't allow the user to do a select against TCHOSEN. Therefore, you should consider revising your MIMI code to avoid doing things like SELECT TCHOSEN(*&8,*).
Fortunately there is an alternative to solve the problem in the short term. If you really don't want or you have big difficulties to modify the MIMI model right now, you can turn switch 66 on to use the old implementation of SELECT.
Use either of the following syntaxes:
SWITCH 66 = ON
SWITCH 66 = YES
KeyWords
SELECT
TCHOSEN
SWITCH 66
Keywords: None
References: None |
Problem Statement: When opening case user gets message stating that case is dependent and cannot find references. It mentioned that if continued it would initialize several sets to blank | Solution: This problem is due to you not having the libraries the case expects in the location set in $TCASES.
To resolve this, please do the following:
1. In SCM, choose View / command line toolbar or hit F3
2. Type $TCASES
3. The following is an example and is not representative of what you will see in your environment. However, you must ensure you either have the files in the location designated by $TCASES or you manually change the path to the location of the files:
4. When completed with changes, close the table, you will be prompted to save the changes to the table. Choose Yes
5. Save the case
6. Reload the case
Keywords: None
References: None |
Problem Statement: The ONTOP style indicates that you want the dialog to remain on top of other MIMI windows, even when another window has focus. Displaying more than one dialog window with this ONTOP attribute defined produces unpredictable results. | Solution: To ensure the correct window appears on top, it is recommended that only one dialog at a time have the ONTOP Style defined.
KeyWords
Dialogs
Stay-on-Top Feature-
Keywords: None
References: None |
Problem Statement: How do I remove workstations from all standard Plant Scheduler configured application (PS CAP) structures via a macro routine? | Solution: The script below will remove workstations from all standard Plant Scheduler configured application (PS CAP) structures via a macro routine. The list of workstations to be removed will be in CHOSEN.
GETCAT &RETURN = CHOSEN COUNT
IF &RETURN = 0 THEN GOTO NOSEL
SELECT FSEI > 0
TCHOSENR = TCHOSENR * CHOSEN
GETCAT &RETURN = TCHOSENR COUNT
IF &RETURN > 0 THEN GOTO SCHEDULES
(* Save schedule to text
M SAVSCH RMFAC_&CASENAME.SCHD
FAC = FAC - CHOSEN
ALL = ALL - CHOSEN
PBFACSEL = PBFACSEL - CHOSEN
FTFR = FTFR - CHOSEN
CALMAPR = CALMAPR - CHOSEN
CAP = CAP - CHOSEN
RES = RES - CHOSEN
TMPSET1 = NULL
TMPSET1 = CHOSEN
DO FAC_LOOP &1 = TMPSET1
SQUEEZE &1
SELECT BOMID(*.&1,C)
BOMID = BOMID - CHOSEN
DO FAC_LP1 &2 = CHOSEN
SELECT IBILLMAT(*,BOMID) = &2
IBILMATR = IBILMATR - TCHOSENR
SELECT IBOMEFF(*,BOMID) = &2
IBOMEFFR = IBOMEFFR - TCHOSENR
SELECT CALPM(*,RESOURCE) = &2
CALMPR = CALMPR - TCHOSENR
FAC_LP1
ENDDO
SELECT OPR(*.&1,C)
OPR = OPR - CHOSEN
DO FAC_LP2 &2 = CHOSEN
SELECT IOPRMAP(*,OPR) = &2
IOPRMAPR = IOPRMAPR - TCHOSENR
FAC_LP2
ENDDO
SELECT RTGID(*.&1,C)
RTGID = RTGID - CHOSEN
DO FAC_LP3 &2 = CHOSEN
SELECT IROUTING(*,RTGID) = &2
IROUTNGR = IROUTNGR - TCHOSENR
SELECT IRTGEFF(*,RTGID) = &2
IRTGEFFR = IRTGEFFR - TCHOSENR
FAC_LP3
ENDDO
SELECT IRESMAP(*,RES) = &1
IRESMAPR = IRESMAPR - TCHOSENR
FAC_LOOP
ENDDO
GETCAT &RETURN = IBILMATR COUNT
IBILMATR = &RETURN
GETCAT &RETURN = IBOMEFFR COUNT
IBOMEFFR = &RETURN
GETCAT &RETURN = IOPRMAPR COUNT
IOPRMAPR = &RETURN
GETCAT &RETURN = IROUTNGR COUNT
IROUTNGR = &RETURN
GETCAT &RETURN = IRTGEFFR COUNT
IRTGEFFR = &RETURN
GETCAT &RETURN = IRESMAPR COUNT
IRESMAPR = &RETURN
<MACFAC
(* Get schedule back
M GETSCH RMFAC_&CASENAME.SCHD
WSYS launcher cmd /c DEL RMFAC_&CASENAME.SCHD
(* Rebuild Process data
>ROPRDATA
>RPRDDAT
>RRESDAT
>RPRODATA
>RTEOPR2
M RESET 0
M SIM
INFOMSG RESET
INFOMSG Selected Facility(s) Removed.
GOTO END
END
NOSEL
(*
INFOMSG RESET
INFOMSG No facilities selected for removal
GOTO END
SCHEDULES
(*
INFOMSG RESET
INFOMSG Facilities can't be removed.
INFOMSG First delete all activities on them.
GOTO END
END
(*
WINFO MESSAGE "Facility Removal Status" 200 200 INFO
END
Keywords: Facility removal
Line removal
Work Center
References: None |
Problem Statement: MIMI 7.2 requires the orientation property to display the tabs on the Workspace properly. | Solution: It is now mandatory to specify the ORIENTATION property when displaying the TABS control in a dialog. The valid values are TOP, BOTTOM, LEFT and RIGHT depending how the TABs are displayed.
Find the dialog set name.
At the TAB section of the dialog set, type ORIENTATION <values>.
Keywords: None
References: None |
Problem Statement: On Windows 7, we must run Business Process Explorer (BPE) as Administrator to prevent retrieve model from failing. How can this be remedied? | Solution: The problem is due to the following statement in the VBA code:
Set Bpe = CreateObject("bpe.application")
If you run BPE as administrator at least once, CreateObject runs properly.
The Type Lib called RepositoryClient.tlb is not properly registered upon install. When running BPE as a regular user, BPE can't create the object. When running BPE as an andministrator, the object can be created and BPE appears to register the type lib on its own.
To resolve this once the install is complete, open a DOS window by launching it as Administrator. Run the command "C:\Program Files\AspenTech\BPE\BPE.EXE" /REGSERVER.
Keywords: None
References: None |
Problem Statement: How do I resolve the error "M0026: Table row not found in set" in Aspen SCM V7.2? | Solution: The problem was caused because of the following snippet of code in $SIMEND$:
AMPSET $9 = CNTL(LSTIND,1)
IF $9 <= 0 THEN GOTO FIN
AMPSET $5 = MAKI($9,LEV)
There were two different situations where CNTL(LSTIND,1) was set to an IND value that was greater than the current max count of the IND set. In one situation the plant shut down and there was almost nothing on the planning board anymore and in the second situation we were sharing schedule files between a case using M GETSCHA and the value of CNTL(LSTIND,1) was inconsistent with the merged schedule files. This made the AMPSET $5 = MAKI($9,LEV) fail in both situations and you receive the error. You must change the code to the following:
AMPSET $9 = CNTL(LSTIND,1)
ON ERROR FIN
IF $9 <= 0 THEN GOTO FIN
AMPSET $5 = MAKI($9,LEV)
Adding the ON ERROR FIN will resolve the issue.
Keywords: None
References: None |
Problem Statement: Is SCM V7.2 supported on Microsoft Windows Server 2008 64-bit? | Solution: SCM V7.2 is supported on Microsoft Windows 2008 Server R2 64-bit. Below is a list of supported server platforms for SCM V7.2:
Server Operating System
? Microsoft Windows Server 2003 R2 Standard SP2 (32-bit)
? Microsoft Windows Server 2003 R2 Enterprise SP2 (32-bit)
? Microsoft Windows Server 2008 R2 (64-bit)
Keywords: 64 bit
32 bit
Windows 2008
References: None |
Problem Statement: Aspen Plant Scheduler or Aspen Supply Chain Planner has returned a solution as infeasible. | Solution: Aspen Plant Scheduler or Aspen Supply Chain Planner uses XPRESS version 18.00.04 and the floating point control for ELIMTOL setting is too aggressive. The floating point setting for ELIMTOL in XPRESS version 18.00.04 should be 0.999.
When the setting is not set for 0.999 the variable eliminations in the presolve are too aggressive. These eliminations cause a cascading effect causing some coefficients to explode to 1e8.
The following work around is specific to version 18.00.04 and not to later versions (20.00.21 or later). Later versions avoids this cascading problem.
The work around sets the floating point control ELIMTOL to 0.999.
Setting this control in C/C++ looks like the following:
XPRSsetdblcontrol(prob, XPRS_ELIMTOL, 0.999);
Keywords: Optimizer
References: None |
Problem Statement: What is the meaning of the set or table that begins with '$' in SCM?
Example: $ESCAT and $CASES | Solution: In SCM, system reserved Sets and Tables always begin with '$'
$ESCAT is an Expert System Set and $CASES is a Database Manager Set.
Caution: Do not use any of these reserved words as names for your own sets, tables, etc.
Keywords: Set
Table
$ESCAT
$CASES
References: None |
Problem Statement: The user will receive an error "cannot create MIF file" while trying to install SCM 7.2 on a machine running Microsoft Windows 2003. | Solution: If the user is attempting to install Aspen SCM 7.2 on Windows Server 2003 (Standard or Enterprise), during the installation, you will receive an error:
"Unable to create MIF file. The filename, directory name, or volume label syntax is incorrect. Error : 123"
All of the common core components as well as the product install create a small file with the MIF extension. There can be 12 or more steps. These MIF files are written to the Windows directory. The user receives this error as there is a special CD installation Family 4.1 (SCM 7.2) Sever 2003. The standard CD does not come with installation support for Windows 2003.
Please contact Aspen Technical Support for ordering instructions for the CD.
Keywords: Installation
References: None |
Problem Statement: In the V7.2 release, the only way to get Chinese characters to work is by changing localization settings. You have an end user who has raised the question is does SCM not support Unicode input? | Solution: Aspen SCM is not UNICODE enabled. The only method for inputting Chinese characters is to change the language settings / Regional settings as discussed previously.
Keywords: None
References: None |
Problem Statement: You are trying to send production order changes to SAP during which the transfer fails intermittently. You recently updated SAP_BASIS and AP_ABA to 7.02 SP8; SAP_APPL is 605 SP5; Kernel is 720 patch 222. | Solution: The root cause of the problem was some additional authorization checks are being done when updating released process orders in the new version of SAP that you are running. You must ensure you have the proper access added in SAP. After running an authorization trace there are failures on authorization object L_LGNUM is missing,
If you review SAP Note 1418766 - Authority check on warehouse number ignored in LT26 and LT27 which indicates that "Transaction LT26 can be run even though users do not have the authorization for the warehouse number. The same behaviour can be experienced with transaction LT27."
Keywords: None
References: None |
Problem Statement: When there is a requirement of connecting a USB dongle in order to license SCM on a Hyper-V server, how can you set it up to do so? | Solution: Hyper-V currently does not support direct pass through connection to the USB port. There is one way to get this to work, though. If you connect to your VMs using RDP (rdp 6.1) you can enable PnP device redirection at your client that will resolve this.
Follow these steps when at your client:
? Open Remote Desktop Connection | Options | Local Resources tab | More button.
? Select 'Supported Plug and Play' Devices.
Keywords: None
References: None |
Problem Statement: Is Windows 7 a supported environment for V7.2 Aspen Manufacturing Master Data Manager? | Solution: Yes, as per the V7.2 Aspen Manufacturing Master Data Manager Installation Guide, this is supported:
Keywords: None
References: None |
Problem Statement: The Giveaway cost by property for each Blend product was defined in PROP_GIVEAWAY_COST table. However when you run Aspen Refinery Multi-Blend Optimizer(MBO) and after apply "Export Blend" option to populate the selected blend information in AB_BLN_QUALITIES table, column called GIVEAWAY_COST appears totally empty even the information really exist in PROP_GIVEAWAY_COST table. | Solution: MBO works as designed. The concept of "Giveaway cost" is only in Single Blend Optimization (SBO) not for Multi-Blend Optimization.
If you were to Optimize and Export blend from the SBO dialog you will get the cost in the AB_BLN_QUALITIES table. Note that this identifies the cost associated with the quality giveaway,not the actual penalty (cost * deviation).
Example with RVP for a product (type of Gasoline):
a) Fill out PROP_GIVEAWAY_COST table with cost associate with RVP property:
b) Go to a SBO (Blend Event) for U91 product and apply "Optimize LP" button:
c) If you want to "Export" this Blend information to AB_BLN_QUALITIES table, apply "EXPORT" option
Keywords: .
- Giveaway Cost
- SBO
References: None |
Problem Statement: Why can't the function ubml_GetPropID retrieve a UBML or ABML property (pcPropId)? | Solution: Use UBML General automation functions to perform the following:
? Initializing UBML parameters
? Freeing the allocated memory
? Handling error codes
? Passing in a product ID string to be used in an UBML correlation
If ubml_GetPropID function is not retrieving property ID main reason should be the fact "Property ID has a limit of 4 characters. This limit was recently updated in the documentation Help file for Petroleum Scheduler y Refinery Multi-Blend Optimizer, topic called "ubml_GetPropID".
Keywords: -Automation
References: None |
Problem Statement: When Exclude Heels option is turned "ON" in MBO/Orion when Publishing | Export Blend, the tank heel information is still included with the heel quantity and property values in AB_TANK_QUALITIES table. Since the heel does not contribute to the blend quality calculations, this is not proper and causes errors on the blend control side. | Solution: Added a CONFIG flag in Aspen Petroleum Scheduler and Refinery Multi-Blend Optimizer in V7.2 to supress the TANK_SPEC column in the AB_TANK_QUALITIES tables.
CONFIG table:
OMITHEELPUBLISH , VALUE_ : Y
Set the OMITHEELPUBLISH TO N :Do a Simulate / Publish /Export blend, then open the AB_BLN_QUALITIES db table. TANK_SPEC should not be blank, as following:
Set the OMITHEELPUBLISH TO Y :Do a Simulate / Publish /Export blend, then open the AB_BLN_QUALITIES db table. TANK_SPEC should be blank, as following:
Keywords: -AB_TANK_QUALITIES table
- TANK_SPEC field
- CONFIG table
- Exclude Heels
References: None |
Problem Statement: Is there a way to set a default value for the "Exclude Heels" option that will be used for all newly created blends? | Solution: A new Config switch has been added and this can be changed using the "Exclude heel" checkbox under Settings -> Blending Page in version V7.2 (build 11.4.9 and higher). All new blends being created will automatically use the value designated in the Settings -> Blending page for "Exclude Heels". Existing events are not affected by the flag. The following information has been added into the Aspen Petroleum Scheduler and Refinery Multi-Blend Optimizer Help files:
1. Added documentation of new keyword EXCL_HEEL to the
Keywords: associated with CONFIG table.
2. Added description of Exclude Heel option to the Blending Tab associated with Settings dialog box.
3. Modified description of option Exclude Heel on the Optimization tab of the OPtimize Blend dialog box.
Keywords
Exclude Heel
CONFIG table
Settings
References: None |
Problem Statement: It would be very useful if the users could use the Component Rundown trend charts to monitor how their rundown qualities are behaving. | Solution: Since version V7.2, Aspen Refinery Multi-Blend Optimizer (MBO) has the ability to trend component rundown flow rates (also properties) .
Here a screen shot showing when you add a new trend list, have the option available for "Streams" for Component rundowns (created the flow rate trend for ALK stream):
Keywords: - Trend Chart
- Component Rundown
References: None |
Problem Statement: Aspen Refinery Multi-Blend Optimizer V7.2 has improved its capability of handling physical blender constraints while creating optimal recipes through the improvement of MIP (Mixed Integer Programming). | Solution: Refineries are often presented with the issue of more blending components than physical controllers on the blender. This leads to components sharing a controller. The previous method for modeling these constraints called for the optimization of all available components. The user would then go through a trial and error method of eliminating components until a satisfactory solution was reached. When dealing with multiple blends over a period of time, this was time consuming and complex to handle.
With MIP capability, the optimizer can now consider all components for the blend and select components based on blender constraints. The user can then set the time frame for when the constraints should be applied allowing the optimizer to ignore the constraints in later periods.
The MIP capability is controlled through configuration tables:
? CMPMIPGRPDEF-defines the group, maximum number of active components, and a flag to indicate the constraint should be considered when optimizing
? CMPMIPCNSTRNT-defines the components in the group and a flag to indicate whether the component is active
? Users can control the number of days to apply the constraints thru the Blending Configuration parameter -Number of MIP Recipe Days- (Blending Tab- Settings)
Keywords:
References: None |
Problem Statement: The following issues have been resolved in this patch:
Issue ID
Headline
CQ00438436
Issue Publishing Master Data Updates from ODM
This issue has been observed at customer site when master data updates for pipelines were sent from ODM to IMOS. The outcome was XML validation errors visible in the IMOS Integration view and IPL.
This issue is due to ODM classes for IMOS missing fields (specifically the IMOSPipelineSegmentClass) and is often symptomatic of not installing ODM 2006.5 Patch 6.0
The customer had already installed the above mentioned patch but was still experiencing Master Data publication issues, this is due to the OdmIncrementalPublishProcessor being disabled. After enabling it, ODM will be able to publish messages normally. | Solution: Follow these steps to resolve the publication issues:
1. From the machine where ODM is installed, Select ?Start?, ?Programs?, ?AspenTech?, ?AspenONE Infrastructure?, ?Aspen ODM Administrator 2006.5?
2. If the Automated ?Aspen ODM Getting Started Wizard? pops up, Click the Cancel button
3. From the Configuration Option list, Tick the ?Incremental Updates? option. Note that the status could be already set to ?Enabled?. Ignore it and Tick the checkbox anyway. Then Click the ?Configure?? button.
4. The Aspen configuration wizard dialog will appear. Ensure the ?Enable Incremental update processing on this computer? checkbox is ticked, then click on ?Next?
5. If the status of the Incremental publish had already been set to ?Enabled? as shown in Step 1, the Wizard will inform that no configuration changes occurred, select finish anyway, to complete the procedure and then close the Aspen ODM Administrator 2066.5.
Keywords: None
References: None |
Problem Statement: How to use the fields penalties and inventory increment price and inventory decrement price in tank definition dialog box? | Solution: Here the meaning of Penalties in Tank dialog box:
. Begin (Deficiency)
Enter the penalty factor for infeasibility breakers on tank deficiency at the beginning of the schedule.
. Begin (Excess)
Enter the penalty factor for infeasibility breakers on tank excess at the beginning of the schedule.
. End (Deficiency)
Enter the penalty factor for infeasibility breakers on tank deficiency at the end of the schedule.
. End (Excess)
Enter the penalty factor for infeasibility breakers on tank excess at the end of the schedule.
. Inventory Increment Price
Enter the price for crediting any increase in the tank inventory from the beginning of the schedule to the end.
. Inventory Decrement Price
Enter the price for debiting any decrease in the tank inventory from the beginning of the schedule to the end.
The Penalties field only apply if you select "Planning Objective function Formulation" to do the Optimization. If you check the equation using by Aspen Refinery Multi-Blend Optmizer (MBO) to calculate the objective function, it considers the Inventory buildup and drawdown cost you defined. Operational Objective function does not care about these penalties. See help file for more details related to this equation and each term.
A.-Economic Objective Contribution:
The formula for the economic portion of the objective function is as follows:
Regarding to INVENTORY Increment Prices, they apply for both Planning and Operational, and are using to calculate the Infeasibility break contribution to global function (fp):
To calculate the first part of this equation (Inventory Infeasibility breakers), the following variables are using:
-Penalty for inventory excess in tank i at time t,
-Penalty for inventory deficiency in tank i at time t,
-Inventory excess & deficiency for tank i at time t
For more details, review MBO Help file: Planning (Operating) objective function formulation items.
Keywords:
References: None |
Problem Statement: Received Not Authorized error when opening ODM Advanced Editor and ODM BPCManager pages. | Solution: The user is not authorized to open the URL's required by ODM. This is not an ODM specific problem because other users can view these pages. To resolve the "web page permissions" issue by first try opening the pages from other computers where other users are able to log in. Resolve the user permissions problem will resolve the viewing problem.
Keywords: None
References: None |
Problem Statement: What is the minimum version of .Net Framework required by Aspen Refinery Multi-Blend Optimizer? | Solution: The Automation feature allows the program (Aspen Refinery Multi-Blend Optimizer) to serve as an automation server. Use the type library (OrionMBO.tlb) to reveal the complete interface so that VB and other compiled languages can bypass the slower dispatch interface calls.
The recommended version is .NET FRAME work 3.5 SP1.
Keywords: - .NET Framework
- Automation
References: None |
Problem Statement: After running the token conversion tool, DMCplus Composite still looks for the DMCplus_Composite key. This key is used in the perpetual schemes. Token scheme uses APC_Comp key.
How to force Composite to check the right key after changing to the token scheme? | Solution: After using the Token Conversion tool to change the mark on the machine, use the APC License Scheme selector to set the value of the APC License scheme. You can find this tool in the Start menu. Use this tool to set the license Scheme to APC or APC olefins. It may be necessary to select one or the other more that once to get the appropriate value.
The value that is being changed with this tool is in the registry SOFTWARE\\Aspentech\\Setup\\APCLIC
The value is either blank, SLM_APC_Inst, or SLM_APC_Olefins_Inst. If this is left blank then Composite will still attempt to check out a perpetual license even when the machine is marked Token.
You will have to restart the Composite after making this change.
Keywords: Composite, DMCplus_Composite, APC_Comp, Token conversion utility
References: None |
Problem Statement: I need to design a shell side reflux condenser (knockback condenser) for direct mounting on my distillation column.
Aspen Shell & Tube Exchanger only appears to permit tube side reflux condensers to be designed, rated or simulated. | Solution: Starting with Aspen Shell & Tube Exchanger V7.2, users may specify a condenser operating in reflux on the shell side (shell side knock-back condenser).
Simple specify what you require in Input | Problem Definition | Application Options.
Set the location of the hot fluid to = Shell side and
The Hot Side application will be specified as Condensation. Set the Condenser type = Knockback reflux as shown.
In addition to the tube side knockback units which could be designed and modelled in Aspen Shell and Tube Exchanger V7.1 and earlier, with V7.2 you can now model and design units configured as follows:
Note: The example case included with this solution is a vertical stab-in exchanger corresponding to arrangement 3 above.
Note: Knockback condensers have the condensate returning to the unit from which the vapor stream originates. This differs from conventional condensers in the sense that the vapor enters the heat exchanger from the bottom instead of from the top. As the condensate forms, it drains down flowing counter to the hot vapor stream. Thus the condensate cannot get subcooled. Furthermore, if the vapor velocity is very high, it can result in the liquid being carried out with the vapor and unable to flow in the desired downward position. Aspen Shell & tube has invoked a more restrictive maximum velocity to avoid the flooding, but does not reduce the heat load for any subcooling of the condensate, nor take into account the impact on the vapor liquid calculations of separation of the liquid and vapor phases.
Note: It is now very easy to compare tube side and shell side knockback condensers to explore the most cost effective configuration for your application:
Keywords: Reflux condenser, knockback condenser, knock-back condenser, Shell side, Tube side.
References: None |
Problem Statement: How do I install the new Aspen Exchanger Design and Rating V7.2.1? | Solution: Aspen Exchanger Design and Rating V7.2.1 applications, which include the following can be installed by obtaining the 7.2 Release of aspenONE V7. To request the DVD Click Here
Aspen Air Cooled Exchanger (AirCooled)
Aspen Shell & Tube Exchanger (Shell&Tube)
Aspen Shell & Tube Mechanical (Shell&TubeMech)
Aspen Fired Heater (FiredHeater)
Aspen Plate Exchanger (Plate)
Aspen Plate Fin Exchanger (PlateFin)
Note: Each Emergency Patch posted for V7.2 Exchanger Design and Rating has been included in the appropriate product in the V7.2.1 release of Exchanger Design and Rating. Aspen Shell and Tube Mechanical has new features in V7.2.1; the remaining Exchanger Design and Rating applications have only bug fixes in V7.2.1.
V7.2.1 Exchanger Design and Rating (EDR) will not co-exist with the V7.2 version of Exchanger Design and Rating. This means installing V7.2.1 EDR will ?upgrade? the V7.2 version if it was installed previously. V7.2.1 EDR can also be installed on a machine where V7.2 EDR was never installed.
The installer therefore functions in 2 modes:
Mode 1 (?Upgrade? Installation): if V7.2 EDR has been installed, the installer will detect this and upgrade the V7.2 EDR installation to V7.2.1.
Mode 2 (?Full? Installation): if V7.2 was not previously installed on a machine, the installer will detect this and perform the necessary functions to complete a full V7.2.1 installation.
In order to activate the V7.2.1 EDR installation, please select the following option within the Aspen Tech Installation Browser - ?Aspen Engineering (for Upgrade)?:
For further instructions on installing AES V7.2 and EDR V7.2.1 please refer to the Installation Guide provided with the DVD.
Keywords: EDR V7.2.1, new, V7.2, installation
References: None |
Problem Statement: Why I am seeing different vibration analysis results between Aspen Shell & Tube Exchanger V7.1 and V7.2 | Solution: One of the major enhancement in Aspen Shell & Tube Exchanger V7.2 is to re-structure the vibration analysis.So the cases created prior to V7.1 version will show some difference in results as compared to the Aspen Shell & Tube Exchanger V7.2 version.
The flow-induced vibration calculations (HTFS Methods) have been completely re-structured and modularized. This will allow future developments and improvements such as extending the number of representative tubes. Improvements have been made to the methods for fluid-elastic instability and tube natural frequencies and to the integration process along the tube length. The full HTFS vibration methods are now available for TEMA G- and H-shells.
All cases will show some difference in results from V7.1. However an E-shell with end spaces equal to the baffle spaces, several baffles, 25-30% baffle cut, and single phase flow should show only small differences. Other geometries can show more significant differences, and known instances are as follows:
? X, K-shells - More accurate natural frequencies, especially for a small number of supports.The re-structured method gives higher values of W/Wc, i.e., the ratio (mass flowrate)/(critical mass flowrate for FEI).
? Split-Flow Shells - There can be significant differences in W/Wc, especially for small number of baffles.The new method generally gives lower values.
? U-bends - Natural frequency method updated, and there are different results when there are no U-bend supports or one U-bend support.
? F-shells with U-bends, Multi-Tube Hairpin - The entire tube is analyzed instead of each leg separately, so there will be different results with shell side phase change. The V7.2 method will give lower values of W/Wc.
? Velocity on top tube row - The bundle entrance velocity is always used in the re-structured analysis, whether or not there is an impingement plate present. Previously, it could be replaced by the nozzle velocity if there was no impingement plate.
? Vertically cut baffles - In Shell&Tube V7.1, it was assumed that the mid-space velocity over a tube in the top or bottom row is near zero. This assumption is not made in the re-structured method. The re-structured analysis might therefore give higher values of ratio W/Wc and different vortex shedding and turbulent buffeting frequencies.
? Velocity calculations - Shell&Tube V7.1 applied a single average crossflow fraction in calculating the shell side velocity for the vibration analysis. In Shell&Tube V7.2, local velocities are used in the vibration analysis and these are the same as are used in the heat transfer and pressure drop calculations. The V7.2 values more accurately represent changes in shell side geometry and fluid properties along each representative tube.
Keywords: vibration, difference, enhancement, results, V7.1, V7.2
References: None |
Problem Statement: I would like to ensure that my tube layout is designed with complete symmetry.
This will allow baffles to be easily replicated on automated drilling processes and ensure the bundle can be rotated if required during maintenance operations. | Solution: Starting with Aspen Shell & Tube Exchanger V7.2, users may specify symmetry options which include the handling of clearances under the shell side nozzles (bundle limits).
By default a design may result in an arrangement like that shown below:
With a left mouse click and drag you can zoom in to any area of the tube layout.
Looking more closely at the centre of the bundle it is clear that there is no symmetry about the horizontal centre line. How can we design a fully symmetric bundle?
1. Go to Exchanger Geometry | Bundle Layout | Layout Parameters: Set the Tube layout symmetry = Full Symmetry. Set the Bundle limit symmetry = Limits must be equal.
2. Run the design optimization with this new specification. Go to Results | Mechanical Summary | Setting Plan & Tubesheet Layout | Tubesheet Layout
This is now a fully symmetric arrangement. You may like zoom in and verify using the left click & drag function.
3. To check the comparison between these two designs. Go to Results | Results Summary | Recap of Designs
We can see that the original design had 1363 tubes and with an area ratio of 1.01 and was 1% over surface. Our symmetrical design has 1334 tubes and has an area ratio of 1. This final design has no over-surface.
Note: The general approach to design optimization in Aspen Shell & Tube Exchanger is to find an arrangement with the maximum number of tubes in a given shell. Typically more clearance will be required under an inlet nozzle than an outlet nozzle - to avoid erosion problems. This means that non-symmetric arrangements may be expected to give a ?better? optimum in terms of surface area for a given shell diameter.
You can now use the symmetry options to get the degree of symmetry you require.
Keywords: Tube Layout, Bundle Layout, Layout Parameters, Symmetry, Bundle Limits.
References: None |
Problem Statement: In Aspen Olefins Scheduler (AOS) the PIONA (molecular composition of feedstock) of a feed can only be entered in mass percentages, but not in volume percentages. Both options are displayed, however volume percentages can not be selected since the radio button is grayed out and therefore can't be checked. Feed suppliers and laboratories usually provide the PIONA of feeds in volume percentages only. | Solution: This behavior is by design. Spyro (by Technip) does the volume to weight calculations so Spyro must be present on the machine for these radio buttons to be active.
Please, check if the required file references to the Spyro folder in AOS were correctly set.After doing so both radio buttons can be selected.
PIONA:
When you click the Convert Entered PINA to MC button the system calculates the molecular composition and then recalculates the PINA values from the calculated molecular composition and displays the calculated PINA values in the Calculated column. Since the conversion of PINA to molecular composition is an approximation, seeing the calculated PINA values give you a sense for how accurately the molecular composition was calculated.
Spyro:
Spyro is a third party application available from Technip. The Aspen Olefins Regression Calculator calls Spyro, which uses the simulation inputs to generate the simulation model (simulation results). You must have Spyro installed and a valid Spyro SPSL license to use Spyro and generate the simulation models.
Keywords: -Feedstocks
References: None |
Problem Statement: In a Swedish system, the colouring and highlighting options are missing from Scheduling Insight - Planning Board and User Preferences screen as below: | Solution: This error is due to the fact that the Internet Explorer language setting for the Aspen Scheduling Insight user is different from English. It must be reset to English. To do this, open Internet Explorer, go to the menu "Tools" | "Internet Options", select the "General" tab, click the "Languages" button under "Language Preference" and make sure that "English" is selected
Keywords: Color By, Highlight, Internet Explorer, IE, foreign languages, language, Swedish
References: None |
Problem Statement: What's New in aspenONE V7.2 - Supported Platforms | Solution: aspenONE V7.2 introduces changes to the operating systems, databases, web browsers and Microsoft Office versions that have been tested as compatible with aspenONE applications. The supported platforms and changes from aspenONE V7.1 are summarized below. Consult the installation guide for your product to see any additional system requirements.
Client Operating System
Windows Vista Ultimate SP2 (32-bit)
Windows Vista Business SP2 (32-bit)
Windows 7 Ultimate (32-bit)
Windows 7 Professional (32-bit)
Windows XP Professional Edition SP3 (32-bit)
? Dropped
? Microsoft Vista SP1
? No change from V7.1
? Microsoft Windows XP SP3
Server Operating System
Windows Server 2003 R2 Standard SP2 (32-bit)
Windows Server 2003 R2 Enterprise SP2 (32-bit)
Windows Server 2008 R2 (64-bit)
? Dropped
? Microsoft Windows Server 2008 (32-bit)
? No change from V7.1
? Microsoft Windows Server 2003 R2 SP2
Databases
Microsoft SQL Server 2005 SP3 (Standard Edition)
Microsoft SQL Server 2005 SP3 (Enterprise Edition)
Microsoft SQL Server 2008 SP1 (Enterprise Edition)
? Dropped
? Microsoft SQL Server 2005 SP2
? No change from v7.1
? Oracle 10g Release 2 (10.2.0.4)
? Oracle 9i Release 2 (9.2.0.1)
Microsoft Office
Desktop:
Windows XP: Office 2003 SP3
Windows Vista: Office 2007 SP1
Windows 7: Office 2007 SP1
Server:
Windows Server 2003: Office 2003 SP3
Windows Server 2008: Office 2007 SP1
? Dropped
? Microsoft Office 2007 SP1
? No change from v7.1
? Microsoft Office 2003 SP3
Web Browsers
? Added
? Microsoft Internet Explorer 8
? Dropped
? Microsoft Internet Explorer 6 SP2
? No change from v7.1
? Microsoft Internet Explorer 7
Microsoft .NET Framework
.NET Framework 3.5 SP 1
Keywords: V7.2 Platforms
Supported
Overview
64-bit operating system
References: None |
Problem Statement: You have a requirement to install and configure ASCC with Informatica Powercenter and SAP. Is there any documentation to help with this? | Solution: Please refer to the Implementation,
Keywords: None
References: , Installation, and Release Note guides attached to this |
Problem Statement: I tried to install Process Modeling V7.1( HYSYS ) in a Windows 7 x 64 machine, which is not a supported environment of AES v7.1, and the installation gets corrupted. Process Modeling HYSYS is not working and I can not un-install the software getting a generic MS installer error 1722.
How can I remove the installation of Process Modeling v7.1 (HYSYS) from my machine ? | Solution: The installation can not roll back because Process Modeling V7.1 installer calls an executable "REGEXTN.EXE" during the installation which can not run successfully under Windows 7 x64. This executable is responsible of stopping the installation roll back.
The work-around which enables the roll back of the corrupted installation is to replace the mentioned executable with the file attached with this solution.
"C:\Program Files (x86)\AspenTech\Aspen HYSYS V7.1\regextn.exe"
Keywords: Supported Environments, MS Installer, Error 1722, "Windows 7 x64" HYSYS
References: None |
Problem Statement: Using the AspenSCConnectV7_2-Inst.pdf guide to install the web applications, under Editing the web.config file: section on page 104 the instructions say to
Set VSSWorkDirTop to the path to the working folder created in the ?Creating a Working Folder for File Transfers? section on page 101.
For example:
<add key=?VSSWorkDirTop?,
value="\\YourVSSMachine.YourDomain.com\ModelMngmtShare">
and also to
Set VSSWebDirTop to the web share folder created in the ?Creating a Working Folder for File Transfers? section on page 101.
If the Impersonate account is a local account, use a Web Syntax as shown below:
<add key=?VSSWebDirTop?,
value="http://YourVSSMachine.YourDomain.com
/ModelMngmtWebShare">
Both of these instructions point to the VSS server.
However, on page 101, when you create the working folder and the web share folder, you create them on the .NET server, not the VSS server as shown from the instructions below.
To set up the working folder:
1 Create a folder on the .NET server to correspond to the project root folder created above.
For example:
C:\ASCC\ModelMngmtShare
and
Enable web sharing on the ModelMngmtShare folder. When you enable Web Sharing, modify the alias to be different from your network share.
For example, ModelMngmtWebShare.
I have not been able to find anywhere in the Model Management installation instructions where it says to create either of these folders or a ModelManagement folder in VSS.
My root folder in VSS that the working folder points to is Error! Hyperlink reference not valid. server>\ASCC as the instructions state on page 100.
Using Visual SourceSafe Explorer, create a root project folder for ASCC.
For example, ASCC.
Where should the VSSWorkDirTop and the VSSWebDirTop keys point in the web.config file? | Solution: Make sure you have web-shared ModelMngmt folder and ModelMngmtShare folder in previous step.
On Web.config file which is under ModelMngmt folder,
1. For VSSWebDirTop, it shows:
Set VSSWebDirTop to the web share folder created in the ?Creating a Working Folder for File Transfers? section on page 101.
For example:
<add key=?VSSWebDirTop?,
value="http://YourVSSMachine.YourDomain.com/ModelMngmtWebShare">
Answer:
YourVSSMachine means your machine name which you have installed VSS.
YourDomain.com means the Domain name your VSS machine in.
Then for example, the VSSWebDirTop value can be: http://shtest.dev.aspentech.com/ModelMngmtWebShare
2. For VSSWorkDirTop, it shows:
Set VSSWorkDirTop to the path to the working folder created in the ?Creating a Working Folder for File Transfers? section on page 101.
For example:
<add key=?VSSWorkDirTop?,
value="http://YourVSSMachine.YourDomain.com/ModelMngmtWebShare">
Answer: This is similar to VSSWebDirTop, for example, the VSSWorkDirTop value can be: http://shtest.dev.aspentech.com/ModelMngmtShare
Keywords: None
References: None |
Problem Statement: In the"AspenSCConnectV7_2-Installation Guide", under step 3, 'Installing ASCC Web Applications', both step 5: 'Configure Administration Management' and step 6: 'Configure Data Management', require the installer to verify ASPNET permissions.
The guide says that if you installed Admin Management or Data Management on Windows Server 2003, then you need to skip these steps.
It also says that the ASPNET account was automatically installed when Microsoft.NET was installed on the server.
Your user, however, installed Admin Management and Data Management on Windows Server 2008 R2, but the ASPNET account does not exist on this machine. Microsoft.NET Framework 3.5 was installed on this machine, but the ASPNET account was not created at that time.
Since Admin Management and Data Management were installed on a Windows Server 2008 server, should they skip these steps as well?
Here is the text of Step 5:
Here is the text of Step 6: | Solution: For Windows Server 2008 R2 and Windows Server 2008, we haven?t an ASPNET account, because it does not install IIS by default. Therefore, it is our recommendation to not skip this check. You should make sure IIS installed before installing ASCC web application. However, you can skip the check on verifying permissions.
Keywords: None
References: None |
Problem Statement: During the installation of AES v7.2 Windows installer shows the following form requesting the original installation
disk of the "Shared Add-in support Update for Microsoft .NET Framework 2.0 ( KB908002 )".
The installer enters an endless loop preventing the installation of AES v7.2. Trying to remove the referenced package from the control panel is not successful either. | Solution: 1. Download and extract the attached file "MSICUU2.zip" to a temporary folder of the machine showing the problem.
2. Launch "MSICUU2.EXE" and browse for the package corresponding to the referenced KB908002.
3. Click on the "Remove" button to delete the package information from your machine.
4. Accept the MSICUU2 utility's confirmation message and click OK
5. Launch AES v7.2 Installer to install your licensed products.
Note the MS KB 908002 installer is available from the AES v7.2 installation media:
"<Drive>:\aspenONEV7.2dvd1\aes72\aspenonev7.2dvd1\core\MSUpdate\lockbackRegKey.msi"
Keywords: MS KB908002, MS Installer, AES v7.2
References: None |
Problem Statement: You have an end user who would like to install Informatica Power Center x64 on Windows Server 2008 x64 (GERMAN), using Oracle 10g x64 on Windows 2003 (GERMAN). Is this supported? | Solution: PowerCenter 8.6.1 is supported in Windows 2008 64 bit OS and also MS SQL SERVER 2008 in GERMAN.
PowerCenter 8.6.1 is supported in Windows 2008 64 bit OS with Oracle 10G in GERMAN.
Oracle 11g and 9i not supported in any language
Keywords: None
References: None |
Problem Statement: You are currently installing the AspenTech Supply Chain Connect 7.2 web applications. According to the AspenSCConnectV7_2-Inst.pdf guide, according to step number 4, on page 101, you are supposed to enable web sharing and modify the alias to ModelMngmtWebShare. Next, You cannot find where you are supposed to select None for application permissions as stated in step number 6. Do you know if this step is no longer required when using IIS 7.5? | Solution: For Windows Server 2003
4) Right click ModelMngmtShare folder, select ?Properties??
5) Select ?Sharing? tab, and select ?Share this folder? option. Add ASPNET, Everyone and web application user (In this example, it is qapart). Give them Full Control permission.
6) Select ?Security? tab, add ASPNET, Everyone and web application user (In this example, it is qapart). Give them Full Control permission.
7) Select ?Web Sharing? tab, select ?Share this folder? option. Then modify alias, it should be different from the name you share in 5). In this example, modify the alias to ModelMngmtWebShare. Give Read and Write access permissions. Select None for application permissions.
[For 2008 server, go to IIS->Machine name->Sites->Default Web Site, right click Add Virtual Directory, set Alias=ModelMngmtWebShare, Physical patch=C:\ModelMngmtShare (for the address you configure), this is the way for configure web-sharing]
Keywords: None
References: None |
Problem Statement: "IDocListener_17601_1762 : [ERROR] Received a call to an unsupported function [IDOC_INBOUND_ASYNCHRONOUS?????]" running a BCI Listener workflow in Informatica while receiving an IDOC message.
The BCI Listener workflow aborts with the following sequence of error messages in the session log:
IDocListener_17601_1762 : [ERROR] Received a call to an unsupported function [IDOC_INBOUND_ASYNCHRONOUS?????].
IDocListener_17809_1762 : [ERROR] Message from SAP LastError: RfcDispatchFUNCTION_NOT_FOUND raised by external server.
IDocListener_17656 : [ERROR] The Integration Service failed to process the IDoc packet for transaction ID = [0A2102300D5C4A9C318B0567].
This is caused by RFC destination running in non-Unicode mode on a Unicode SAP system. | Solution: To resolve this issue do the following:
1. Go to transaction SM59 in SAP.
2. Select the appropriate Logical System.
3. On the tab Communication Type with Target System set it to Unicode when the PowerCenter Repository is running in UTF-8 mode.
Keywords: None
References: None |
Problem Statement: You have an end user who would like to install Informatica Power Center x64 on Windows Server 2008 x64 (CHINESE), using Oracle 10g x64 on Windows 2003 (CHINESE). Is this supported? | Solution: PowerCenter 8.6.1 is supported in Windows 2008 64 bit OS and also MS SQL SERVER 2008 in CHINESE.
PowerCenter 8.6.1 is supported in Windows 2008 64 bit OS with Oracle 10G in CHINESE.
Oracle 11g and 9i not supported in any language
Keywords: None
References: None |
Problem Statement: The V7.2 documentation is incorrect in relation to Windows Server 2008 running IIS 7.x.
Currently, page 97 Heading Configuring IIS Security states the following:
To configure IIS security:
1 Open Internet Services Manager.
2 Right-click on Administration Management's virtual directory,
AdminMngmt, and select Properties.
3 Select the Directory Security tab.
4 Click Edit for Anonymous access and authentication control.
5 Select Basic authentication. Clear Anonymous access.
6 Click OK to complete security setup. | Solution: The following should be added regarding Windows Server 2008 as IIS 7.x has changed drastically.
To configure IIS security:
1. Open Server Manager
2. Expand Roles
3. Expand Web Server (IIS)
4. Click on Internet Information Services Manager
5. Expand your hostname (the Server which IIS is running on)
6. Expand Sites
7. Choose Default Web Site
8. Double Click Authentication
9. Right Click on Anonymous Authentication
10. Choose Disable
11. Right Click Basic Authentication
12. Choose Enable
Keywords: None
References: None |
Problem Statement: You are attempting to configure Aspen Supply Chain Connect with Informatica and SAP. Your SAP Administrator set up your account with a mixed case password. The only way you can connect is by using all upper case letters. | Solution: SAP does not support mixed case. See SAP Note 930833 for clarification.
Keywords: None
References: None |
Problem Statement: The PowerCenter 8.6 installation fails in the final steps of as shown in the installation debug log:
Output of execution
-------------------
Output: [ICMD_10133] Command [ping] failed with error [[ICMD_10053] Node [node01_adminmsas06] Domain [Domain_Dev] Host:Port [adminmsas06:6001] has failed to ping back.].
Error:
ExitCode: -1
When attempting to start the Informatica Services 8.6.0 the following errors appear.
Node.log:
2008-11-20 18:55:04,515 FATAL [main] [PCSF_10420] Failed to initialize the repository utility with native code because: [no pmjrepn in java.library.path].
java.lang.UnsatisfiedLinkError: no pmjrepn in java.library.path
Catalina.out:
java.lang.UnsatisfiedLinkError: no pmjrepn in java.library.path
at java.lang.ClassLoader.loadLibrary(ClassLoader.java:1682)
at java.lang.Runtime.loadLibrary0(Runtime.java:822)
at java.lang.System.loadLibrary(System.java:993)
at com.informatica.powercenter.sdkint.repository.ILocaleManager.<clinit>(ILocaleManager.java:38)
at com.informatica.pcsf.common.utilities.RepositoryUtility.init(RepositoryUtility.java:59)
at com.informatica.pcsf.adminconsole.app.config.ApplicationLoader.init(ApplicationLoader.java:161)
Cause
This error occurs when the PowerCenter Services installation directory has not been added to the Windows PATH environment variable. | Solution: To resolve this issue, add the <PowerCenter_Home>\Server\bin directory to the Windows PATH system variable.
To modify the PATH in System Variables do the following:
1. On the Windows desktop right-click My Computer and select Properties.
2. Select the Advanced tab.
3. Click Environment Variables
4. Under System Variables, scroll to and select "Path".
5. Click Edit.
6. Add the full path for \server\bin separated by a semi-colon from the other paths.
After making this change, start the Informatica Services.
Note:
You may continue with the PowerCenter installation program, if the window is open. However at this point, the installation has finished and the Install Program is only verifying a successful install. The same results can be achieved by starting the service and opening the administration console http://hostname:6001.
Keywords: None
References: None |
Subsets and Splits
No community queries yet
The top public SQL queries from the community will appear here once available.