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Problem Statement: How to move from a dongle-locked license to a dongle-free license file | Solution: Dongle-free license file request needs to be submitted though our AspenTech Support & Training Website. Once the request has been made, Customer Care will send you a dongle return document which you must sign and return to us to process the request. A dongle-free license file will be sent via email and a dongle return kit will be sent to your address to return the dongle. You have 90 days to return the dongle and should not do so until the dongle-free license file arrives, is installed, and works correctly.
To get started with the process, submit a License Key Request by providing the required information in the form.
Note the case number if you wish to contact us regarding your license key request.
Keywords: Change from dongle to dongle free
How can I change my license type ?
License type change
Dongle free licenses
References: None |
Problem Statement: How to check the start date and expiry date for a license | Solution: There are two ways to check the start and expiry date for a license
Without the SLM manager:
Find the license file and right click on the file.
Choose the Open with Notepad to open the license file.
Then you will be able to see the information of the license, usually you can see the start date on the first row, and the expiry date on the second row. You also can check the corresponding System Name from the license file. The example is shown below:
Using SLM manager:
Open the SLM, go to the License profiler
Choose your license server from the list, and click Load Information, when the loading is finished, click View Licenses button.
License profiler will list information of your license, move the navigation bar to right, you will be able to see the Birth Date and Expiry Date of your license file.
Keywords: None
References: None |
Problem Statement: In the CimIO_msg.log a message is written:
"Maximum Ping Failure set to 3 and pinging frequency to 60"
What does it mean? | Solution: This is not an error message, but a notification.
Aspen Cim-IO will check whether the connection between the Cim-IO server and client is available by pinging every 60 seconds. If this fails three times, Cim-IO concludes that the connection is broken.
These two settings can be optimized using the Cim-IO Interface Manager or Cim-IO IP21 Connection Manager although it is not recommended to change it.
"Maximum Ping Failure" cannot be disabled completely. The range of values allowed for this setting is 1 to 10. Any user value outside this range will cause the value to cap down to the limit.
KeyWords:
Keywords: None
References: None |
Problem Statement: How to create a Custom Material on EDR | Solution: 1. To start, go to the Customize Ribbon and click on Material Database:
If the Private Materials Database is empty, the start screen looks like this:
2. To use an existing material format (gasket, plate, tube, forging, pipe, etc) for your customization of materials, select the Old ASME check box. Then, select the type of material you want to copy (gasket, plate, tube, forging, pipe, etc). For example, material ID 1101 (scroll down on the ASME | Material Name or write the Code Designator).
3. Click the ‘Copy’ button at the bottom of the window and then click on OK on the upcoming window. Go back to the USER section and select ‘Yes’ to add a new record.
4. Accept (click OK) the default number provided:
5. Double click on as many fields as necessary to change the desired properties, such as Material Type, Material Class, Density, etc. After making all the necessary changes, click on Save (NOTE: If the material properties are not changed, the properties will remain the same as the original designated material):
6. The first private material record has been created. You can make further changes to the same material database (it is OK to delete and reenter the same value) and re‐save the record by closing the database (click on the ‘X’ upper right corner) and clicking ‘yes’ to the save record dialog:
7. Your files are saved in the folder pointed to in Program settings (File | Options | Files) Section “Folder for customized database files”.
8. You can create more new materials, all of which will be saved on the same database folder. In order to create new ones, just repeat the instruction 2 and click the Copy button. Now, since the database already has another material, you will require to click the Paste button at the bottom of the USER window. If done correctly, two materials should be displayed on the USER Material window:
9. This can be redone for other materials as well. They will all be saved on the selected location.
Keywords: EDR, Mechanical, Material, Database, Custom
References: None |
Problem Statement: For ACCE's Plant Bulk | Piping, there are allowance options. How can it be used in user's cost model? | Solution: In case of revamping project, complexity of piping route may be high because of interference by existing facility.
So the length of piping can be higher than the direct length of piping. User can use 'Allowance' option to increase the length of piping in a very simple way.
In Library Tab | Fittings, user can specify user's own fitting options. Create new specification and you can find the length options in the bottom.
I set ‘200’ for AGU piping. The equation for length modification is ( LENGTH = (The length you specified * Horizontal Adj/100 * Vertical Adj/100) )
Select fitting file as the file you created in the Library | Fitting. (For this example, it is ‘TEST)
Even if I specified 100m length for the piping, ACCE automatically accounts for 400m. (400 = 100 * (200/100) * (200/100))
Keywords: Piping, Allowance, Vertical, Horizontal
References: None |
Problem Statement: If you follow the wizard to add features in Windows server 2003 to add the .NET Framework 3.5 Features, and you select it and then click on Install button.
But you get the below error:
The feature Installation failed because the source files could not be found! | Solution: Without Internet Connection, you should be aware of the .NET Framework 3.5 feature should be installed from the below sources:
The same Windows media that was used when the Windows is being installed.
The Windows media with the same current installed version.
Eg. If Windows server 2012 R2 has been installed on your machine you must use installation media for Windows Server 2012 R2.
Mount the Windows installation media (ISO/CD) with the same version of the current installed windows.
Specify the alternative source path to U:\Sources\SXS
Note: U:\ is the drive that Windows Server 2012 ISO was mounted.
Directly on the configuration windows, before finishing adding the component, click on the Specify an alternate source path
Specify the source as indicated on the image (The Installation media in this case is located on the U: drive)
Click Install > wait a moment till the feature installed successfully.
This should finish the component installation.
You can use the Deployment Image Servicing and Management (DISM) command-line tool to enables the .NET Framework 3.5 feature without internet connection as the following:
Open Command prompt as Administrator.
Type the following command:
DISM /Online /Enable-Feature /FeatureName:NetFx3 /All /LimitAccess /Source:d:\sources\sxs
d:\ is the drive that the Windows Server ISO has mounted.
/All to enable all parent features of the specified feature.
/LimitAccess to prevent DISM from contacting Windows Update/WSUS.
/Source to specify the location of the files that are needed to restore the feature.
In case you have Internet Connection, You can also use the Deployment Image Servicing and Management (DISM) command-line tool to enables the .NET Framework 3.5 feature as the following:
Open Command Prompt as Administrator.
Type the following command:
DISM /online /enable-feature /featurename:NetFx3 /all
Keywords: None
References: None |
Problem Statement: As part of the configuration of Aspen CIM-IO to get data from an OPC source, a user account with proper privileges is needed. This solution provides overview of how to configure the user and the privileges needed for the Aspen CIM-IO logical device created using the I/O wizard or the Aspen CIM-IO Interface Manager. | Solution: During a logical device creation it is possible to specify a user account; depending of the method you choose (I/O Wizard or CIM-IO Interface Manager) interface will be different:
This information will be used to run asyncdlgp.exe process (by the Aspen CIM-IO Manager service) on the Aspen CIM-IO node which will actually connect to the OPC service. We have three options regarding this user setting:
Option 1: Use a Domain account with Admin privileges on Aspen InfoPlus.21 as well as Aspen CIM-IO server. This is the recommended configuration.
Option 2: If you’re not using a domain, leaving this field empty will make the asyncdlgp.exe process to run with the same user used for the CIM-IO Manager Service (in Windows services). This could be convenient if you’re using local accounts.
Option 3: If you’re not using a domain, you can use a local account with same name and password as an admin account on the Aspen CIM-IO server node.
Whether you’re using a domain account or local account; the recommended permissions for this user are as follow:
1. User should be an administrator of the CIM-IO node.
2. Starting from Windows Server 2003, user should be added to Distributed COM users (use the Windows Computer Management tool to add the user to this group):
3. User should have Access permission as well as Launch and Activation permission on COM security setting (open Component Services using dcomcnfg on a run window, navigate to My Computer and right click / Properties):
Click on Edit Defaults button and ensure that user (or a group which holds the user i.e. Administrators) have permission to activate DCOM services remote or locally depending where the OPC service is running on the same machine as the CIM-IO node or if it is remote to it.
NOTE
Other user settings can be required based of specific OPC configuration that usually changed between providers. If CIM-IO has been installed on the same machine as the OPC service, it is possible to find the OPC as a DCOM service (for example Matrikon OPC Simulation):
Configuration, Access and Launch and Activation Permissions can be changed on it by going to the Properties of the service. The Properties option also let you know the Identity of the OPC Server, this is the user account which is running the OPC server itself, for example:
It is recommended that user running asyndglp.exe should be the same as the user running the OPC Server. Since DCOM applications are executed as called by another application, It is also possible to use The launching user option to let account running asyndlgp.exe run also the OPC server.
Some OPC servers need specific accounts to be used for the server and for the clients (CIM-IO in this case). Please consult with you OPC vendor technical support before doing any change on this service or about specific accounts needed to properly read/write values by OPC.
Keywords: CIM-IO for OPC
DCOM
References: None |
Problem Statement: When configuring an Aspen InfoPlus.21 Database, how can the XOLDESTOK settings be updated to allow aspenONE Process Explorer users to add aspenONE Process Explorer (A1PE) comments for past dates? | Solution: To allow A1PE users to Add Comments to IP.21 Tags for Past Dates, the XOLDESTOK setting for all fields
included in the IP_#_OF_COMMENTS History Repeat Area for the IP_CommentDef Record named “Comments”
should be set accordingly using the following SQLPlus example query:
XOLDESTOK('Comments IP_#_OF_COMMENTS', '01-JAN-18 00:00');
In short, you should change the Date/Timestamp used in the above Query as needed, and then use Aspen SQLPlus to execute it against the Aspen InfoPlus.21 Database(s) that will be used to store A1PE comments.
IMPORTANT: Use of this Solution assumes that you have also completed the following 2 additional requirements:
a.) You must also have 1 or more History Filesets configured and available whose Start and End Dates
encompass the Past Date/Time Range for which the A1PE Users will be allowed to add comments
b.) And the PAST TIME PARAMETER must also be set accordingly for the History Repositories that
are to be used for archiving the comments and any replies which may also be added by the users.
Key Words
Comments
IP_#_OF_COMMENTS
XOLDESTOK
Keywords: None
References: None |
Problem Statement: This knowledge base article contains a query that displays the contents of the file cimio_logical_devices.def for all Aspen InfoPlus.21 nodes available to an Aspen ADSA server. | Solution: Attached to this article is a query named FindCimIONodeNames. For each Aspen InfoPlus.21 node listed in the Aspen ADSA server, the query examines the registry value
HKEY_LOCAL_MACHINE\SOFTWARE\Wow6432Node\AspenTech\CIM-IO\CIMIOETC
for the location of the folder containing cimio_logical_devices.def on the Aspen InfoPlus.21 node.
Then the query displays the contents cimio_logical_devices.def. This allows the Aspen InfoPlus.21 administrator to examine the names of the Cim-IO nodes connected to the various Aspen InfoPlus.21 servers as seen in the following example:
Keywords: Cim-IO logical device
Cim-IO node name
Cimio_logical_devices.def
Cimio_logical_devices
References: None |
Problem Statement: This knowledge base article explains how to resolve the error “APRMODBC::GetAreaList:Unable to write data to the transport” when using the Aspen Production Record Manager add-in to Microsoft Excel. | Solution: This error indicates that the Aspen Production Record Manager add-in to Microsoft Excel cannot communicate with the Aspen Production Record Manager server.
Make sure the port designated for the Aspen Production Record Manager Service in the ADSA server is open both ways between client computer and the Aspen Production Record Manager (APRM) server.
The default port number is 52011.
Keywords: APRMODBC
GetAreaList
References: None |
Problem Statement: We have seen reports of completely unusable Aspen InfoPlus.21 servers - for example, none of the MES tools (IP.21 Administrator, IP.21 Manager, etc) can be opened. The performance is very poor and only a server reboot appears to help get a stable system again. The operating system is Windows Server 10 or higher.
On such a server, it has been noted that Automatic Maintenance feature is enabled and although scheduled to run in the middle of the night, the problem is apparent even during normal work hours. The observation is that the server runs without any performance issues once Automatic Maintenance feature is disabled.
What is AspenTech's recommendation regarding Automatic Maintenance on a Windows server? | Solution: AspenTech recommend turning off Automatic Maintenance or lower the priority of the maintenance task. Go to Task Scheduler in Administrative Tools: Microsoft | Windows | TaskScheduler
Keywords: Slow
Intermittent
Unresponsive
Hang
High CPU
References: None |
Problem Statement: Does Aspen Capital Cost Estimator (ACCE) automatically add the cost of shipping materials to the estimate? | Solution: No. Shipping costs are not automatically added to the estimate. To account for shipping costs, the user could utilize the Contractors forms:
Or, the user could utilize an external Indirects file:
Keywords: freight, charges
References: None |
Problem Statement: Standalone 이나 Network License 설치를 위해 Server 로 활용될 컴퓨터의 Locking Information 을 얻는 방법을 알아봅시다.
This knowledge is based on 136832 article and translated to help the Korean customers. | Solution: 유첨의 SLMLockinfo.zip 를 다운로드받아 압축을 풀어 SLMLockinfo.exe 파일을 실행합니다.
아래와 같은 스크린을 볼 수 있습니다.
우측 하단의 "Copy to Clipboard" 를 눌러 텍스트를 복사합니다.
텍스트 파일을 하나 만든 후 붙여넣기를 합니다. 해당 파일을 저장하신 후 Aspen Technology 담당자에게 송부해주시기 바랍니다.
Keywords: SLM
Lock info, Locking Info
References: None |
Problem Statement: How to calculate the Mach Number for a multi phase fluid with VBA | Solution: The Aspen HYSYS type library (Hysys.tlb) contains all the objects and parameters associated with the Aspen HYSYS application and accessible via VBA in MS Excel. Users can create variables in VBA that reference these objects in the Aspen HYSYS library.
The example includes an Aspen HYSYS model file, with two different pipe segments and an MS Excel file. The Excel file is calling the Aspen HYSYS file, and calculates the Mach number for the desire pipe segment.
For further information of the equations that were used in the Macro, please refer to the following article How is Mach number calculated in Aspen Flare System Analyzer?
Keywords: Mach Number, Fluid Velocity, Sonic Velocity
References: None |
Problem Statement: This article explains how to import an Aspen Feedstock Assay Manager file (.afam) generated in Aspen HYSYS into PIMS Aspen Assay Management. | Solution: .afam files generated in HYSYS can be opened in PIMS by following these steps:
1) In PIMS go to Aspen Assay Management.
2) Go to Model Assays on the navigation section on the left side.
3) Select the “New Assay” icon on the ribbon. Then select “Import from File”.
4) In Assay data format, select AspenTech and choose the .afam file you want to import.
5) Click on “Import”. After assays have been imported, the following message should appear:
The HYSYS and PIMS version should be the same. When an .afam file created in a newer version of HYSYS is opened in an earlier version of Assay Management, crash or incorrect results may occur. A warning message prompts you to confirm the opening of the file.
Keywords: Petroleum refining, integration
References: None |
Problem Statement: A composite is not showing all Controllers or Sub controllers under the Composite View in the Online Tab of the Production Control Web Server (PCWS). | Solution: Main applications may not be visible in the composite view if the Hostname used in the Data Service connection uses mixed case letters. You can check the definition of the hostname by running a command prompt window on your server and run the command “hostname”. This is a known issue and it will be addressed in future patch releases for V10 CP2 and V11. The proposed fix is to accept the “mixed-case” letters in the hostname. A workaround will be to correct the hostname and avoid mixed case letters.
If sub controllers are not shown, the problem may be caused due to a timing issue for when the Composite variable list is generated. If the constituent applications are not finished loading into the web repository before the composite application completes loading, then this problem occurs. The problem can appear after an upgrade, or a recent restart of the Web Provider Data Service. The current workaround to fix this is to delete and redeploy the composite application from DMC3 Builder.
Both issues are a cosmetic problem of the PCWS website and should not affect the composite operation.
Keywords: Composite
Production Control Web Server
Application
References: None |
Problem Statement: User cannot use zoom in / out by using mousewheel + CTRL on pop-out windows like tower internal data or COA definition. | Solution: It is fixed in V11.
Users will be able to use mouse wheel to scroll vertically, use SHIFT+mouse wheel to scroll horizontally and use CTRL + mousewheel to zoom in/out in forms that pop-out in ACCE UI. NOTE: If all rows/columns in the form are already visible then mousewheel scrolling doesn't do anything. In that case, only CTRL+Scroll can be used.
This fix affects the following forms:
COA Definition
COA Allocation
Reporting COA
Custom Pipe Specs
External Steel File edit form (library mode)
External Civil File
External indirects proratables file
Power distribution - Main Substation
Power distribution - Unit Substation
Power distribution - Transmission line
Power distribution - Sub-unit Substation
Contractor definition form
Conset forms
Indexing: Material, Manhours, Location indexing forms
Craft wage rate and productivity form
Input/Output units of measure specification forms
Currency specification form
Control center, operator center edit forms
Panel board edit forms
External insulation schedule forms (library mode)
APEA: View -> Streams list
APEA: Investment analysis results shown in APEA UI
Fixed in Version
Will be fixed in V11
Keywords: Aspen Economic Analysis, Zoom, ACCE
References: None |
Problem Statement: VSTS 289155: Printing Vessel Dimensions does not retrieve Double Tubesheet calculations | Solution: When running a Shell and Tube Mechanical file with a specified Double Tubesheet (chosen under Exchanger Geometry | Tubesheet | Tubesheet type), the results for Double Tubesheet do show up under Vessel Dimensions | Tubesheet/Tubes/Baffles | Double Tubesheet.
However, when you go ahead and Print the Vessel Dimensions, the Printed Summary does not include the Double Tubesheet results:
Workaround
The calculations for the model Designed are accurate, only the printed values are missing.
Fixed In Version
VSTS 289155: Confirmed and approved for future release
Keywords: Tubesheet, Double, Mechanical, Shell, Tube
References: None |
Problem Statement: VSTS 272163: API Sheet reports Incorrect tube count on Aspen Fired Heater
Applicable Versions
V8.8, V9, V9.1, V10, V10.1 | Solution: For a cabin firebox, you should enter the number of tubes against one wall; hence the default Tube Passes defined for a One Cabin Unit is 2. Same happens for a Twin Box, where the default tube passes are defined as 4.
This would mean the tube count should be multiplied by either 2 or 4, depending on the Fired Heater type specified.
So, if we had a Twin Box Fired Heater and we were to specify 6 tubes on the Roof Rows and 8 tubes on the Main Rows, the correct tube count would be (6 + 8) x 4 = 56 tubes. The tube number at the input only must be specified as 6 Roof Tube Rows and 8 Main Tube Rows:
However, the API sheet displaying the results should consider the No. of Tube Passes for the calculations so that the tube number is 56. Currently, API Sheet does not do that and it simply sums the number of tubes specified on the input:
Workaround
Since the exposed surface is correctly calculated based on the correct tube count, current workaround is just to multiply by either 2 or 4 (One Cabin and Twin Box Fired Heater, respectively) to get the correct No. of Tubes.
Fixed in Version
VSTS 229289: Target for a future release.
Keywords: Fired Heater, Firebox, Number of Tubes, API Sheet
References: None |
Problem Statement: Help does not open after new installation. Why? | Solution: This issue occurs due to a corrupted Aspen HYSYS installation since the help files could not be saved on the right folder. Hence, in order to solve this issue, please checks this directory: C:\ProgramData\AspenTech\Aspen HYSYS VX.X\HtmlHelp. You should find there some files. If you notice that the folder is empty, please repair the installation of Aspen HYSYS.
Keywords: Hysys, Help, Fluid Assistance
References: None |
Problem Statement: This Knowledge Base article provides simple queries for:
1. pulling data from an Aspen InfoPlus.21 tag and storing it in a comma-separated-value format to a .txt or .csv file.
2. inserting CSV repeat-area data from the same flat file to a single InfoPlus.21 tag. | Solution: --Script to write data for one tag from Aspen InfoPlus.21 to a .csv file:
SET OUTPUT 'C:\<path>\<file>';
SET COLUMN_HEADERS = 0;
SELECT IP_TREND_TIME || ',' || IP_TREND_QSTATUS || ',' || IP_TREND_VALUE FROM IP_AnalogDef
WHERE NAME LIKE '<tagname_A>'
AND IP_TREND_TIME BETWEEN '01-JAN-18 00:00:00' AND '31-MAR-18 20:00:00';
--Script to write data from a .csv file into Aspen InfoPlus.21:
INSERT INTO <tagname_B>
(IP_TREND_TIME, IP_TREND_QSTATUS, IP_TREND_VALUE)
SELECT (SUBSTRING(1 OF LINE BETWEEN ',')),
(SUBSTRING(2 OF LINE BETWEEN ',')),
(SUBSTRING(3 OF LINE BETWEEN ','))
FROM 'C:\<path>\<file>';
KeyWords
example
Keywords: None
References: None |
Problem Statement: The standard Aspen IP.21 Process Browser (formerly Web.21) installation does not contain Detail Display pages for records defined by IPAiDef, IPDiDef and IPSetDef. | Solution: Download and unzip the attached file. Place the three asp pages in the \Inetpub\wwwroot\AspenTech\Web21 folder.
Keyword
IP_AiDef
IP_DiDef
IP_SetDef
Keywords: None
References: None |
Problem Statement: What are the network and software requirements for Software License Manager (SLM)? | Solution: aspenONE software utilizes Software License Manager(SLM) for licensing. To be able to use SLM, the following requirement must be met:
Network Requirements:
Ports: You will need to have specific ports open bidirectionally so that the SLM Server can communicate over the network.
· Port Number: 5093 | Protocol: UDP
· Port Number: 5093 | Protocol: TCP
Bandwidth: For the SLM to communicate over the network, you will need to have certain MTU settings to be able to send and receive messages over the network.
· SLM Server 8.4 (aspenONE V8.0 through V8.3) requires the MTU to be set at 7512 bytes
· SLM Server 8.5.3 (aspenONE V8.4 through V8.8) requires the MTU to be set at 1432 bytes
· SLM Server 8.6.1 and higher (aspenONE V9 and higher) has a dynamic MTU, and requires an MTU of about 700 bytes
Ping time: SLM requires a ping of 300 ms or less, with 0% loss.
Operating System Requirements
Visit the AspenTech Plaform Support page for a list of supported operating systems:
https://www.aspentech.com/platform-support
SLM Tools and SLM Server also require:
Microsoft .NET Framework 3.5
Microsoft .NET Framework 4.x
* Review the Platform Support page for the required versions of .NET required for your version of aspenONE.
Keywords: slm network requirements
slm software requirements
slm over vpn
slm over network
References: None |
Problem Statement:
How to transfer a Failure Agent from one Mtell database to another Mtell Database? | Solution: If you have assets which are essentially identical, such as several compressors of the same model running under similar operating conditions, then you can create a Failure Agent on one asset and deploy the Failure Agent on another similar asset.
Export a Failure Agent from an Equipment Set Profile
1. Launch Aspen Mtell Agent Builder and click Machine Learning tab
2. Select a Failure Agent within an Equipment Set Profile
3. Click Export button in the ribbon
4. Provide a location, file name and click Save.
Import a Failure Agent to similar Equipment Set Profile
1. Create a Hidden Failure Detector Agent on the Data Set before importing Failure Agent from another database.
2. Select Data Set and Click Import Machine Learning Agent.
3. Select the Failure Agent exported *.bin file and click Next.
4. Select Failure Signature Recognition Agent and click Next.
5. Select an Asset for Training and click Next.
6. Select Failure Events and click Next.
7. Select Training Date Ranges and click Next.
8. Provide Name, Description and Sensor Group for this Failure Agent and click Finish.
Keywords: Agent Transfer
Export Agent
Import Agent
Failure Agent Transfer
References: None |
Problem Statement: Can I use nonlinear equations to define capacities? | Solution: Yes, non-linear equations can be used to define capacities in PIMS-AO. If the traditional capacity naming is used, then those capacities can be controlled via Table CAPS. The capacities will also be reported in the Capacities section of your reports. However, there is no connection of the capacity to a particular submodel when they are defined this way. Therefore, such capacities will not be reported in the Submodel Summary section of the fullsolution report.
Keywords: None
References: None |
Problem Statement: Does the ADSMALL setting work when using table MICROCUTS? | Solution: The ADSMALL setting is not currently compatible with the use of Shortcut Distillation with Table MICROCUTS. We are investigating the possibility of extending this functionality to Table MICROCUTS in future versions, but as of Aspen PIMS V10.0, it is only compatible with standard distillation using Table ASSAYS.
Keywords: None
References: None |
Problem Statement: Can I customize what is in my reports? | Solution: The PIMS standard reports are partially customizable. Users can deselect various report sections as desired. For example, in the screenshot below, the user is not interested in the details of utilities in the fullsolution report and has de-selected the report sections related to utilities.
When more customization is desired we recommend using reporting tools like Aspen Report Writer or third party tools such as Microsoft Power BI to build the desired reports.
Keywords: None
References: None |
Problem Statement: Should I remove all tiny coefficients from my model? | Solution: Tiny coefficients - smaller than +/- 1e-7 – can be an issue for optimizers and we recommend eliminating them from your model. However, it may not be as simple as finding all such coefficients and replacing them with zero. The issue is whether the coefficient becomes significant in your model optimization. Let’s consider some scenarios.
1. Table Assays has some tiny property values.
This is commonly seen as all assay management tools make correlations about how properties are spread among the various crude cuts. For example, an assay management tool may indicate that there is a very tiny amount of butane in your vacuum bottoms cut. This is unlikely to be the real presence of butane and simply an artifact of the correlations. So numbers like 3.4e-16 for butane in your vacuum bottoms is not a significant coefficient and it could be replaced by zero. PIMS-AO has a setting called ADSMALL that allows you to set a threshold for data in the Assay table and to automatically eliminate any values less than that threshold. We recommend a threshold of 1e-7.
2. A Base-Delta submodel has tiny coefficients in some delta vectors.
This can be trickier to address and requires some further investigation. Most model columns multiplied by tiny coefficients represent flows and are consequently within a range of 0.01 to 1000. Therefore, when they are multiplied by tiny coefficients like 1e-12, the result is still below the threshold of 1e-7 and would not typically be significant to the calculation. However, the delta vectors in Base-Delta models are dimensionless and therefore can be well outside the typical range for “flows”. When this happens, even tiny coefficients may become significant to a calculation and therefore cannot simply be eliminated. When a tiny coefficient is identified in a submodel, the user should investigate what column activity the coefficient if being multiplied by. If the coefficient is 1e-10 and the column activity is 12,000,000 the resulting product is potentially significant for the calculation. In this scenario, instead of eliminating the coefficient, the column and all its coefficients should be re-scaled. For example, a column activity of 1200 and a coefficient of 1e-6 achieves the same mathematical result without violating our recommended threshold of 1e-7. Note that when a column activity is re-scaled then all the coefficients in that column must also be re-scaled.
Keywords: None
References: None |
Problem Statement: What tools can help improve my matrix initialization in PIMS-AO? | Solution: In Aspen PIMS-AO the matrix is initialized in one of two ways:
No input solution file. In this scenario, the properties are initialized using Table PGUESS values and columns are initialized to the Default Initial Value designated in the model settings as shown below.
The recommended alternative is to designate an input solution file. This can be done on the Run Execution Dialog box or via the LOADSOL keyword in Table CASE.
Whichever method is used, it is possible that some of the initialization values are not very good for the current case. PIMS-AO has some tools available that can minimize the impact of poor initialization including:
Hybrid Quality Initialization
Epsilon
Improve Local Solution
Fix Qualities of Zero Flow Pools to Initial Values
Hybrid Quality Initialization
This is a setting on the XNLP | General tab. When this is activated and an input solution file is being used, PIMS-AO will identify property values in the input solution that are at their bounds. Such values are then replaced with the corresponding property in Table PGUESS.
Use Epsilon
This setting is on the XSLP | Advanced 1 tab. It is a proprietary algorithm that reduces local optima. The epsilon value is model-specific but is usually between 1 and 0.0001. The Max iteration is recommended to be around 6 to 8. When a matrix has poor initialization, this feature can be helpful in avoiding local optima
Improve Local Solution
This setting on the same tab as shown above for Epsilon. It is typically not used at the same time as Epsilon although it is possible. The Improve Local Solution algorithm forces pools to have some activity for a few iterations so they are not prematurely turned off. This can be helpful if matrix initialization involves some streams being turned off.
Fix Qualities of Zero Flow Pools to Initial Values
This setting is on the XSLP | Advanced 2 tab. When the activity of a pool goes to zero, the properties of that pool tend to drift toward the upper or lower bounds. This feature sets the property values of a stream with zero flow to the value those properties had when the stream last had flow. This ensures that properties stay in a reasonable range and prevents poor data in any input solution created from a case where a pool was off in the solution.
Keywords: None
References: None |
Problem Statement: How do I enable .NET Framework 3.5 / 4.5 within Windows OS? | Solution: .NET Framework 3.5 / 4.5 is built into the Windows OS has a Windows Feature. To install .NET Framework 3.5 / 4.5 follow these steps:
Non-server Windows OS:
Open the Control Panel and click Programs and Features.
Once the Programs and Features window displays, click Turn Windows features on or off.
Expand and check all features from .NET Framework 3.5 and .NET Framework 4.5 and click OK.
.NET Framework 3.5 / 4.5 will install. Once the installation is finished, the Windows Feature window should close.
Server Windows OS:
Open the Server Manager and click Manage > Add Roles and Features.
Continue to click Next until you feature the Features section.
Expand and check all features from .NET Framework 3.5 and .NET Framework 4.5 and click OK.
NET Framework 3.5 / 4.5 will install. Once the installation is finished, the Windows Feature window should close.
Note: If there are any error while installing .NET Framework 3.5, then please contact your IT team or Microsoft to resolve .NET Framework installation issue.
Keywords: .NET Framework 3.5, aspenONE, AES, MSC
References: None |
Problem Statement: Common cause of RadFrac column failure during dynamic run? | Solution: One of the most common reasons of column failure is significant shift in column stage pressure profile during dynamic run. If for some reason, column feed stage pressure is considerably different than that of feed pressure during dynamic run, failure can occur. This may happen for many reasons including rapid change in condenser/reboiler duty, reflux ratio or feed pressure.
One common strategy is to make any change of operating conditions slowly using a ramp or task option, rather than using direct step change.
Key Words
Column, Pressure, Dynamic
Keywords: None
References: None |
Problem Statement: Each batch generated in the Aspen Production Record manager Database has a system generated Batch ID and a Serial Number associated with it.
Aspen Production Record manager uses the Batch ID to link all supporting variables and parameters. For example, a Batch SPC variable defined for the Area gets updated with the Batch ID.
This KB provides a query to obtain the Batch ID using the serial number. | Solution: This query uses the Batch.21 API Object module in Aspen SQLPlus.
Note: The Aspen Batch.21 Application Interface library needs to be added as a reference before running this query
LOCAL BatchDataSourcesOrig;
LOCAL BatchDataSources;
Local BatchDataSource;
Local BatchQ;
Local Area;
Local Desigval;
Local Batch;
Local BatchID;
Local BatchList;
-- declare batch Data source
BatchDataSourcesOrig = createobject('AspenTech.Batch21.BatchDataSources');
BatchDataSources = BatchDataSourcesOrig.New;
BatchDataSource=BatchDataSources.Item(1);
-- Select the Area based on the Index
Area=BatchDataSource.Areas.Item(1);
BatchQ = Area.BatchQuery;
-- query by designator value
Desigval ='16400';
BatchList = BatchQ.GetByDesignatorValues(DesigVal);
-- get the BatchID of the batch
Batch= BatchList.Item(1);
BatchID=Batch.ID;
Write BatchID;
Designator Value(DesigVal) here is the Serial Number that can be changed.
Keywords: Batch ID
Serial Number
API
Query
References: None |
Problem Statement: My PIMS opens up solutions of each case at the end of run. How can I disable this? I've checked all the settings and don't see it anywhere. | Solution: The run dialog box contains an option: "Open Report Windows". This option needs to be de-selected.
Keywords: Open Report Windows,
References: None |
Problem Statement: In the EDR program, how can I select different methods for calculationg mixture surface tension in Aspen Properties? | Solution: Surface tension is an important parameter in the design and rating of shell and tube exchangers and therefore accurate estimation will be of fundamental importance.
In the EDR program there is now the option to use Aspen Properties in which there are a variety of methods available for the estimation of mixture properties.
After selecting Aspen Properties for the required stream, in the Advanced Options there is the option to import Aspen Property file (with extension aprbkp) into the EDR program.
Prior to opening the EDR simulation file, the Aspen Properties program can be run from the Windows start. .In the Aspen Properties we need to select the required components and a suitable property method
And subsequently in the folder for the method selected in the Tab called Routes we can see the different methods available for calculating the surface tension. The property parameter that we should be checking is called SIGLMX.
Further help and information can be found in the online help for the Aspen Properties.
KeyWord: EDR, Surface Tension, Aspen Properties
Keywords: None
References: None |
Problem Statement: We have built a lot of structure in local PIMS model to constrain our loading unloading possibilities. We would like to be able to use this structure in global XPIMS or MPIMS models. We have built the structure using tables ROWS/BOUNDS | Solution: Though making a global version of ROWS/BOUNDS by appending or changing the structure of the keywords using Excel functions like CONCATENATE is a viable option we do understand that it is indeed easier to just keep exactly the same structure present in the local models. This makes maintenance easier and also shortens the time it takes to switch between global and local run. One distinct advantage is also that keeping exactly the same structure reduces possibilities of human error while toggling between local and global runs.
The way to achieve this is to enable setting KEEPLOCL in the global model.
To access this option:
Expand the Model Settings branch on the model tree, and then double-click General to display the General Model Settings dialog box, and then click the Miscellaneous tab.
This option will preserve any local model structure that intersects with local model purchase and sales vectors in the local table ROWS, RATIO or MIP. This is for M-PIMS and X-PIMS only. The purpose of this feature is to keep any linear-programming structure, with some exception, that you have added to local PURC and SELL vectors in table ROWS. The system still strips from the local model PURC and SELL columns any entries pertaining to group limits. All column entries are retained except entries in OBJFN, MINOBJ, VBAL, WBAL, ABUY, and ASELL.
This way the columns will function properly in the global model but still be part of local constraints, at least those related to ROWS, RATIO or MIP. Entries related to local table GROUPS are not kept and it is important to stress this.
Effectively this will enable you to keep local constraints of buying and selling such loading and unloading constraints and to have the applied to global tables SUPPLY and DEMAND in an equal way as they have been applied to local BUY and SELL entries.
Keywords: KEEPLOCL, MPIMS, XPIMS, ROWS, BOUNDS, RATIO, MIP
References: None |
Problem Statement: How do I resolve the error "Could not Create PropertiesDialog Check that AtProperties.dll is registered" when opening an Aspen Process Explorer plot? | Solution: Try re-registering the following files located in the folder C:\Program Files (x86)\Common Files\AspenTech Shared\Apex:
1. AtPECoreCtls.ocx
2. AtPEGuiCtls.dll
3. AtSamples.ocx
4. AtTime.dll
Also, re-register AtProcessdata.dll located in the folder C:\Program Files (x86)\AspenTech\ProcessData.
Keywords:
References: None |
Problem Statement: Why can’t I see wires smaller than 12 AWG for Low Voltage in the Electrical items report of Aspen Capital Cost Estimator V10? | Solution: In V9.1, a bug fix allowed the spec in Project Basis | Electrical Specs | LV minimum wire size to be read correctly. See article 000045643 for more info.
The default value for this field is 12 AWG, meaning that no smaller wires will be calculated in the program.
If the user wishes to consider smaller wire diameters in the estimation, this value can be manually entered in the LV minimum wire size field on the Project Basis | Electrical Specs form:
This change will allow the program to estimate the values of smaller wires, making the results comparable to those generated by previous versions.
Keywords: LV, Wire, AWG, Electrical, 14, Size.
References: None |
Problem Statement: How do I resolve the error "Could not Create PropertiesDialog Check that AtProperties.dll is registered" when opening an Aspen Process Explorer plot? | Solution: Try re-registering the following DLLs located in C:\Program Files (x86)\Common Files\AspenTech Shared\Apex
1. AtPECoreCtls.ocx
2. AtPEGuiCtls.dll
3. AtSamples.ocx
4. AtTime.dll
Also, re-register AtProcessdata.dll located in the folder C:\Program Files (x86)\AspenTech\ProcessData
Keywords:
References: None |
Problem Statement: How do I import the Air Cooled exchanger fan power in Spreadsheet? | Solution: Fan power for air coolers is calculated by EDR Air Cooled and available through Aspen HYSYS. To test this:
Load the attached case.
Add a spreadsheet to the flowsheet.
Open the spreadsheet form, select a cell and click Add Import.
Select the air cooler AC-100 and wait for variables to populate.
Scroll down to variable "xEDRr: Brake power for all fans" and select. Click OK.
On spreadsheet tab note the value of this variable which populates the cell.
To verify the number, open the form for AC-100. Go to Rigorous AirCooler tab and click model details which launches the EDR browser.
In the EDR browser, navigate to Results|Mechanical Summary|Exchanger data and go to Fan Details. Confirm "Total brake power (winter)" is the same as the value in step
Keywords: Fan Power, Air Cooled Exchanger
References: None |
Problem Statement: What equations are used in the Heat Exchanger model in Aspen HYSYS to calculate shell side and tube side heat transfer coefficients? | Solution: When the user does not specify heat transfer coefficients, the simple steady-state rating model uses different equations depending on certain characteristics of the flow. The equations are given below:
Tube HTC, Single Phase Flow:
Re > 10000: h = 0.023*Re^(-1/5)*Pr^(-2/3)*Cp*massFlux
2100 < Re < 10000: h = 0.116*((Re^(2/3)-125)/Re)*(1+(D/L)^(2/3))*Pr^(-2/3)*Cp*massFlux
Re < 2100: h = 1.86*Re^(-2/3)*Pr^(-2/3)*(L/D)^(-1/3)*Cp*massFlux
Tube HTC, Condensing Flow:
Vertical: h = 1093.28*thermalConductivity*(density^2/viscosity/tubeLoading)^(1/3)
Horizontal: h = 898.2634*thermalConductivity*(density^2/viscosity/tubeLoading)^(1/3)
Tube HTC, Boiling Flow:
h = 1800*(.577789*thermalConductivity)^(0.6)*(0.2388459*Cp)^(0.4)/viscosity^(0.4)/0.04891946
Shell HTC, Single Phase Flow:
Cross flow: h = 0.198*Re^(-0.4)*Pr^(-2/3)*Cp*massFlux
Parallel flow: h = 1.3*0.023*Re^(-0.2)*Pr^(-2/3)*Cp*massFlux
Shell HTC, Condensing Flow:
Vertical: h = 1093.28*thermalConductivity*(density^2/viscosity/tubeLoading)^(1/3)
Horizontal: h = 898.2634*thermalConductivity*(density^2/viscosity/tubeLoading)^(1/3)
Shell HTC, Boiling Flow:
h = 1800*(.577789*thermalConductivity)^(2/3)*(0.2388459*Cp)^(1/3)/viscosity^(0.267)/0.04891946
Note:
Re = Reynolds number
Pr = Prandtl Number
Cp = Mass heat capacity (kJ/kg*C)
h = heat transfer coefficient (kJ/m2*C*h) D = tube inner diameter L = total tube length viscosity (cP) thermal conductivity (W/m*C) density (kg/m3) Thermal conductivity/viscosity/heat capacity are for the liquid phase in multiphase flows
Keywords: Heat Exchanger, Heat Transfer Coefficients
References: None |
Problem Statement: What is Exchanger Effectiveness and how can this be used in Aspen Shell & Tube Exchanger? | Solution: The effectiveness of a (two-stream) exchanger is the exchanger heat load as a fraction of the maximum possible heat load. The maximum possible heat load for a given set of process inlet conditions occurs either when the hot stream is cooled to the cold stream inlet temperature, or when the cold stream is heated to the hot stream inlet, whichever of these gives the lower heat load.
The input value of effectiveness is essentially an alternative way of specifying the exchanger duty. It is not needed if the actual exchanger duty is specified. In Simulation calculations, the input value of effectiveness, like that of exchanger duty is simply an initial estimate.
The value for the effectiveness lies between 0 and 1. A value of 1 can nominally only be obtained using a pure countercurrent exchanger of infinite area. Multi-pass exchangers, even with a very large area excess, will usually have an effectiveness well below unity. Effectiveness is valuable as an input in Simulation if you only know the stream flows and inlet conditions. This is specified in the Process Data form as highlighted below.
The program also calculates the exchanger effectiveness, based on the calculated exchanger duty. Using the output Effectiveness from one run can provide a good initial guess for a subsequent run in which flows or inlet conditions have changed slightly. The calculated effectiveness is available in the Heat Transfer Page under Thermal / Hydraulic Summary.
Keywords: Exchanger Effectiveness, Shell and Tube Exchanger
References: None |
Problem Statement: How do I customize the Fly by window in Aspen HYSYS? | Solution: When a user hovers over the stream in Aspen HYSYS this displays the values of the variables specified in the Fly by setup. The default variables are Temperature, Pressure and Molar Flow. The default variable can be changed in the “File | Options” in Aspen HYSYS. Select “Simulation” in the “Options” page and move to the Tool tips section as shown below.
Now click on “Specify Fly by”. This will open a window where you can select the variables wish to display for the material stream and energy stream.
Keywords: Fly by, Variables
References: None |
Problem Statement: How to specify the relative humidity of a process stream in Aspen HYSYS? | Solution: The extension "Saturate with Water" can be used to specify the relative humidity of a process stream. In the newer versions this and some other commonly used extensions are installed with Aspen HYSYS. The extensions are available in the Custom group of Object Palette.
In the Saturate with Water extension, you can specify the relative humidity. The default value is 100%. You only need to specify the component mole fraction of water in the water stream. By default, the extension uses the temperature and pressure as specified in the Process stream. The flow rate for water is calculated based on the specified relative humidity.
There is a simple example case attached with this solution which illustrates how to specify the relative humidity with "Saturate with Water" extension.
In Aspen HYSYS V10 a new unit operation named “Stream Saturator” has been added. This provides the same functions as in “Saturate with Water” extension. In addition this calculates the temperature of water stream to meet the humidity conditions in the process stream.
Keywords: Relative Humidity, Saturate with Water
References: None |
Problem Statement: How to configure flow splits in Aspen HYSYS Hydraulics? | Solution: Attached is an example case which explains to configuration for flow splits in Aspen HYSYS Hydraulics. The hydraulic solver can calculate the flow based on pressure drop in each branch and the specified constraints in the boundary streams.
The constraints can be either flow or pressure. The constraints can be accessed and changed from any of the boundary streams. The screenshot below shows that all the boundary streams have pressure specification.
The constraints can be changed from Pressure to Flow or vice versa for any stream from the nod.
Keywords: Upstream, Flow Splits, Constraints
References: None |
Problem Statement: Why do I see an inconsistency between the user input and calculated light ends in Petroleum Assay? | Solution: In Petroleum Assay, The light ends are extra data in addition to cut yield data.
Let’s take a simple example. If there are 5 hypo in a case, hypo1-hypo5, user specified 5 light gases(C1-C5) with 1% composition for each. If hypo1 is IBP-38C and its composition is 5%, the calculation needs this extra information to determine how to distribute 5% among light gases.
However, user may see a large composition gap between the input and calculated pure components as above when light end data is incorrect.
Here the steps to illustrate this:
User specify light end data in IBP -15C but this range could not cover both iC5 and nC5. Thus Assay manager cannot handle these two components.
To resolve this, user can remove iC5 and nC5 then he needs to renormalize the light ends input so all are added up to 100% to ensure material balance.
After entering these values in IBP-15C and re-characterized the assay, the light ends results in this cut matches input exactly. Please refer to related case file(Assays_sample.hsc)
KeyWords
Petroleum Assay, light end gas, IBP,
Keywords: None
References: None |
Problem Statement: How to model a Flame Arrestor on Aspen Flare System Analyzer? | Solution: Aspen Flare System Analyzer’s palette does not have a Flame Arrestor operation. However, there is an alternative to add the pressure drop caused in this operation by using a FlowBleed unit.
The Flow Bleed is a simple calculation block that can be find on the model palette and allows the customer to:
• Specify a fixed pressure drop
• Specify a constrained flow offtake where the flow offtake is calculated from the following equation
• Offtake = Multiplier x Inlet Flow + Offset
The calculated Offtake is constrained to maximum and minimum values.
The FlowBleed can be used to model a Flame Arrestor by accepting a pressure drop input that can be manually calculated.
Keywords: Flame Arrestor, Model, FlowBleed, Flow Bleed, Pressure Drop
References: None |
Problem Statement: How can I backcalculate compositions of a stream in a Mixer block in Aspen Plus? | Solution: Aspen Plus doesn’t have the ability to backcalculate properties for a stream as Aspen HYSYS does. However, there is an easy workaround for this by using a Calculator block. We will use a water/ethanol system for this example.
Once the Unit Op where you want the backcalculation to be done is set up (the Mixer block was selected for this example), two inlet streams need to be set; the known stream is fully specified, the unknown one with Temperature and Pressure specified and some initial estimates for composition; and the outlet stream fully specified.
It is easier to work with Flows rather than Fractions, because you don’t have to normalize them once you want to export them as values for the stream. It is not necessary for the outlet stream to have inputs.
Now you can create the Calculator block. In it, you need to define variables for components 1 and 2 (water and ethanol in this case) as Mole-Flows per component on the known inlet stream; while define them as Parameters | Mole Flow for the unknown inlet stream and for the outlet stream as well. Both the known inlet and outlet streams are defined as Import Variables, while the unknown inlet is defined as Export variable.
You can now set up the Component Mass Balance (for both water and ethanol) equation on the Calculate tab, using the same names you used for variable definition:
It is important to notice that the Initial Value for the Parameters for the outlet stream are the desired outlet stream conditions, so A+ knows this value is the Target Value, while the Initial Value for the unknown stream is just an initial condition for the calculation.
Once this is correctly set up, run the simulation. The results displayed on the Calculator block | Results | Define Variable will show the value read and the value written, where the value written is the value calculated for the unknown stream. These results are only displayed and calculated for the Calculator block, NOT for the simulation’s mass balance:
Now that the values have been calculated, you can even go further and transfer them to the streams, in order to be used as variables on the simulation. Go back to the calculator block and change the Defined variable for the previously unknown stream from Parameter type to Mole-Flow type, specifying the Stream and Component to calculate (do this again for the other component on the previously unknown inlet stream).
Run the simulation again. You will see the Mole Flows are now the mole flows referred to the previously unknown inlet stream on the Results of said stream. You can see the difference between these values and the ones you originally used as inputs on the stream.
Keywords: backcalculation, calculator
References: None |
Problem Statement: How can I refer a calculated stream already connected to a Unit Operation from a Subflowsheet to another flowsheet? | Solution: The correct workflow to refer one calculated stream from a Subflowsheet and use its results to define another stream on another flowsheet without having to manually copy from the original stream every time is the following:
1. Make sure the subflowsheet with the original stream is fully converged.
2. Go to the Parent flowsheet and add a Spreadsheet. In this spreadsheet, on the Connections tab, select the Subflowsheet where the original stream is located and browse through the streams that show up on the Objects section.
3. Select the Variables you want to refer from the Stream. Typically for streams, the main variables to specify are Temperature, Pressure and Molar/Mass Flow Rate. These variables MUST be specified as Import Variables.
4. Select those same Variables as Exported Variables, but now for the stream you want to transfer those values to.
5. On the Exported variables cells on the Spreadsheet, specify the equations as equalities, where the cells with the Export variables are defined as equalities for the cells with the Import variables. Keep in mind if the stream where the variables are exported has input values, the simulation will not converge. You need to delete the input values first and then specify the spreadsheet equalities.
NOTE: As with any variable calculated by a spreadsheet, this transfer can ONLY be performed to a stream with USER SPECIFIED variables. If you try to transfer the variables to a stream with CALCULATED values, the simulation will have convergence issues.
NOTE: This workflow was developed only for Operating Conditions (Temperature, Pressure, Flow). The same worflow can be applied to transfer Compositions from one stream to another.
Keywords: Subflowsheet, Spreadsheet
References: None |
Problem Statement: Why does the Overall Heat Transfer Coefficient increase when using a high viscosity fluid? | Solution: The Heat Transfer Coefficient (HTC) is a proportional function of both Reynolds and Prandtl numbers:
Where: the Prandtl number (Pr) is directly proportional to the viscosity of the fluid
and the Reynolds number (Re) is inversely proportional to the viscosity of the fluid
Hence, the HTC is expected to have both increasing and decreasing behaviours when the viscosity increases/decreases:
1. If viscosity (µ) increases, Re decreases and Prandtl increases
2. If viscosity (µ) decreases, Re increases and Prandtl decreases
In most applications, the Reynolds number is dominant for the HTC, so the HTC value decreases when the viscosity increases (and viceversa).
The reason for the HTC increase with a high viscosity is that the contribution of the obtained Prandtl number becomes more significant than the Reynolds number. Pr has an increasing linear behaviour with increasing viscosity, while Re has an asympotic decreasing behaviour with increasing viscosity; when the viscosity tends to zero, Reynolds tends to infinite. As the viscosity increases and tends to infinite, the Reynolds tends to zero. Considering just the viscosity dependance, the Prandtl number is at a fixed slope. Therefore, at low viscosities, the Reynolds number is the greater contributor, whereas the Prandtl number becomes the greater contributor at high viscosities.
This means that the overall HTC for the high viscosity case ends up being higher (see equation 13 on SM4):
αc = crossflow HTC; HTC in this case
Note: We do have considerations in the code for such low Re cases, but even so, the range of applicability and the obtained results may treated with caution at these low Re numbers.
Keywords: EDR, viscosity, Prandtl, phi
References: None |
Problem Statement: Even if .json files and accompanying .jpeg files or subfolders exist in C:\inetpub\wwwroot\AspenTech\Process Explorer\Files\Public, the public folder within the navigation pane of AspenONE Process Explorer still does not expand when clicking on it and behave as if there were no files within the public directory. | Solution: This most commonly occurs when AspenTech files are installed on a drive other than C: even though IIS is installed on the C: drive. To resolve this issue, look for a file named "default__.tls" and migrate all graphics and trends into the folder containing the "default__.tls" file instead. Upon doing so, the graphics should show up in the navigation pane.
Keywords: Graphics
navigation pane
References: None |
Problem Statement: If feed contains trace-level-concentration of light impurity whose relative volatility is higher than that of light key component, it can be accumulated in the dead zone of piping / equipment and can cause operating problem like localized corrosion and operating condition upsets. These impurities also lower the quality / purity of product.
For example, Hydrogen / Methane impurities in Ethane / Ethylene splitting process and O2 / N2 impurities in CO2 liquefaction process.
Pasteurization column is good protection for these problem. There are some distillation column which has zero or very low distillate flow rate (top flow rate) and has side-draw as a main light-key product. Pasteurization section means the tray section between top-distillate and side-draw for main light-key product. Top side is usually operated as a full reflux with normally closed vent-valve after the condenser. This valve is opened occasionally when the temperature condition of top section is changed. | Solution: HYSYS can model pasteurization section as a steady state, one important thing is user shall input non-zero flow rate for distillate flow even if operating column has zero-flow rate.
If user input '0' as a distillate flow rate, column will not converge with error message.
Please input low number of distillate and change the solving method to 'Modified HYSIM inside-out' which is fit for the column that has side-draw.
Please refer to the attached simulation file to compare the result between normal distillation column and pasteurization column for C2 splitter process.
Keywords: Pasteurization, zero flow rate, no flow
References: None |
Problem Statement: How can I solve O2 mole fraction convergence issues when working with an incinerator? | Solution: When working with an incinerator, you may encounter some convergence issues when changing the Target Outlet O2 Mole Fraction.
The simulation may be behaving correctly and converging at a low value, but encounter convergence issues when this value is increased.
Here are two recommendations to choose from:
Decrease the Target incinerator Exit Temperature. To decrease the temperature you need a larger Air flow to the incinerator which will cause the remaining oxygen at the end will increase (target oxygen increases).
Change the Natural Gas composition. Specify a greater composition for heavier hydrocarbons. Heavier hydrocarbons require more oxygen to be combusted than lighter hydrocarbons (like Methane), so the Air flow rate will be increased as well which will cause the remaining oxygen at the end will increase (target oxygen increases).
Try either of these 2 options and specify your Target Outlet O2 Mole Fraction to a greater value. You should be able to get the simulation converged.
Keywords: Incinerator, sulfur, recovery, unit
References: None |
Problem Statement: A dynamic utility is available for solving known Security Server configuration problems. This utility can be used with both Aspen Framework and Local Security.
Local Security users should run this utility before installing or upgrading their Aspen Local Security server to determine if the ALS version will have a problem with ADSI on the new server. The ADSI problem should be corrected before upgrading. | Solution: The utility, SSTest.hta, can be used to diagnose and solve common Security Server configuration problems. SSTest is an HTML application with embedded JavaScript to progressively test the role-based security client/server interface. Possible solutions for failed tests are returned in HTML format. Links to appropriate Aspen Tech and Microsoft Knowledge Base documents are also provided. This utility can also be used to measure the time required to complete key functions.
To run the utility, go to C:\Program Files (x86)\AspenTech\BPE on your current security server and double-click on the html application (SSTest.hta) or download the attached version. If moving to a new security server, place this file in any folder on the target system and double click. All tests will be performed under the current user's login context.
KeyWords:
diagnostics
run-time
dynamic
NTFS privileges
connection problems
anonymous user rights
sstest
Keywords: None
References: None |
Problem Statement: How to use Aspen Process Data Add-in to Retrieve Compliance.21 Data | Solution: The Process Data Attribute Values dialog box can be used to retrieve data from Compliance.21. To display the Attribute Values dialog box select the Aspen menu from the Excel menu bar. Choose Process Data, select Get Data, then select Attribute Values.
In the Attribute Values dialog box:
1. Use the Tag Browser to search for the desired Compliance.21 tag, and drag the into the Tag field.
2. Select a cell range to display the output for the selected tag.
3. Click on the Attributes List button to display the "Select Attribute List" dialog box.
4. Add the desired fields to the Selected list for display in the Excel spreadsheet.
An example showing the results when retrieving data for the Compliance.21 tag CM3-133.
Keywords: Compliance.21;
Process Data Add-in;
Excel;
Attribute Values;
References: None |
Problem Statement: An RTE controller loaded but won't run. The run time is not updating and the WHYOFF message remains as Application Starting. | Solution: When the RTE controller loaded but won't run is likely a result of an erroneous input calculation. When a input calculation failed, the controller cycle is aborted and the controller will try to run again the next cycle. Unfortunately there is no message to indicate the error. In order to troubleshoot the problem, follow this KB articles, https://esupport.aspentech.com/S_Article?id=000045896 to turn on diagnostic for the controller.
If using DebugView is not possible, go back into the DMC3 Builder and use the test function in the calculation section to catch any error. You may have to manually input the current DCS values in order to catch the error.
Keyword:
RTE controller
loaded but won't run
Keywords: None
References: None |
Problem Statement: Some of literature provides UNIQUAC parameters of TAU as △Uij while Aspen Plus is using different polynomials for TAU.
> Literature, other source
> Equation of Tau used in Aspen Plus | Solution: Aspen Plus uses polynomial equation to calculate Tau for activity coefficient while UNIQUAC equation originally developed from Tau only with energy interaction parameter △Uij.
If user want to input △Uij parameters, user can use "Enter Dechema Format" to input this.
If user input △Uij parameters, Aspen Plus is automatically converting these parameters to Aspen parameters form.
Keywords: UNIQUAC, △Uij, binary parameter
References: None |
Problem Statement: When user adds 'Catalytic Converter' in sulsim, there are 2 types of catalyst selection in Design > Paramters tab of 'Catalytic Converter' Block.
User needs to choose the catalyst either between 'Alumina' and 'Titania'. | Solution: When acid gas is burned in reaction furnace, some undesirable reactants like COS and CS2 are created due to the side reaction between CO2, Hydrocarbon and H2S. Hydrolysis is the reaction between COS and H2O, or CS2 and H2O which is turning back those reactant to H2S. H2S is then can participate Claus reaction which is a desired main reaction in the sulfur reactor.
Titania catalyst (>25% mixed bed with titania) generally offers better performance in Hydrolysis reaction compared with Alumina catalyst.
In order to achieve equivalent level of hydrolysis with Alumina catalyst, reactor temperature shall be raised about 40 ~ 60 ℃ which in turn may increase the loss of energy (steam in heater) and decrease the rate of claus reaction (which is a desired main exothermic reaction).
Titania catalyst is generally placed as the first stage reactor then used to minimize by-products (COS and CS2) and will enhance the performance of entire sulfur plant.
HYSYS - Sulsim offers approach to equilibrium of Hydrolysis as percentage, please compare the below results between Alumina catalyst and Titania catalyst.
It is a mandatory for user to specify 'Space velocity' or 'Catalyst bed volume' when user apply 'Titania catalyst' as option. Titania catalyst shows higher approach of Hydrolysis ,less amount of COS/CS2 and higher amount of H2S in outlet stream.
> Alumina Reactor
> Titania Reactor
Keywords: Sulsim, Titania, Alumina, Claus reactor
References: None |
Problem Statement: How can I enable or disable the SLM “Network Broadcasting” option from the Windows registry? | Solution: This Knowledge Base article describes how to change the SLM “Network Broadcasting” option in the Windows Registry. This option allows SLM clients to automatically search for other available SLM Servers in their networks in case the Servers or Licenses on the specified SLM Server list (configured by the SLM Configuration Wizard or during the installation of any AspenTech product) are not available. While having this option checked could be a benefit to some users, it could also cause delays with the license checkout process or result in licenses being unintentionally consumed from a different SLM Server.
The recommended way to change this setting is through the SLM Configuration Wizard. However, it is also possible to quickly change this setting through the Windows Registry by following these steps:
Open the registry window from Start > Run > type REGEDIT
Go to HKEY_LOCAL_MACHINE\SOFTWARE\WOW6432Node\AspenTech\SLM\Configuration
3. Set the value for the key named “SuppressBroadcasts” (type REG_DWORD) to 1 (enable) and 0 (zero) to disable.
Keywords: SLM Configuration Wizard, SLM TOOL, Network Broadcasting, script, & registry
References: None |
Problem Statement: This is article explains how to fix the error 'The procedure entry point libm_sse2_exp2 could not be located in the dynamic link library libmmd.dll ' when opening Aspen DMCplus Model. | Solution: 1, find libmmd,dll from "C:\Program Files (x86)\Common Files\Intel\Shared Libraries\redist\ia32\compiler"
2, copy it to "C:\Windows\SysWOW64"
This should make DMCplus Model work again
KeyWords
DMCplus Model
libmmd
dll
Keywords: None
References: None |
Problem Statement: There are times that a tag existed in the CLE file but would not extract its data from the BIN file. The extract programs marked the line in the CLE file as such
N~~~Modeltagname~~~DCStagname~~~
every time it runs | Solution: If the CLE file is not generated automatically (due to a lack of description and engineering units), the tag in the CLE file has to match exactly as it appears in the collection list. If not, the extract program would mark it N~~~ in the CLE file after it run and it would not extract the data. For examples, if the tag exist in the collection list as "FIC101 ":DBVL: (with a space), then the CLE line should read
Y~~~FIC101~~~"FC101 ":DBVL.
Keywords: COLLECT
CLE EXTRACT
References: None |
Problem Statement: Intro:
When dealing with predicting properties of blends in PIMS and APS we usually work with either linear or linearized property contributions. Sometimes we also model the impact of components on each other, either using tables PBONUS or INTERACT which are well explained in PIMS help. In essence PBONUS will add or deduct a certain figure from the neat property of a certain component in a certain blend. E.g Alkylate may have RON 95 and PBONUS may add 0.5 to that figure for 95 RON MOGAS while it may deduct 1 for blending to 98 RON MOGAS. Table INTERACT is much more sophisticated since it defines the impact of one component on another. It does require a large amount of measurement data and may can impact convergence performance.
Problem:
It is fairly well known that some blending components may exhibit unusual property bonus behaviour with sometimes adding to a property of the entire blend up until a certain concentration and afterwards subtracting from it and then usually in anon-linear fashion. One such example is the ethanol RVP impact – do note that here we are talking about the bonus impact on the rest of the blend, not the absolute impact of the component. With ethanol at the beginning of the blending we exhibit a certain level of impact while it reverses after a certain concentration level. The question is how to model this. Let’s imagine a refinery PIMS model in which PBONUS was used to model DON (delivered octane number) and a new blending component XXX was modelled, coming from a brand new unit: APS tables would be the same here.
*TABLE PBONUS
*
TEXT DON
*
LCNURG LCN in URG -0.7
HCNURG HCN in URG 0.3
RFTURG RFT in URG -0.8
XXXURG XXX in URG 0.6
***
Now, after the new unit came on stream we have realized that the new component XXX is reducing the octanes if added in small amounts and increasing it after going through a certain threshold. | Solution: To begin with we will switch over to the use of table INTERACT. One might argue that we do not have enough data to use INTERACT but we will show that INTERACT can be used to deliver same effect as PBONUS which in itself would have been superfluous but serves as first step towards modelling this problem. First let’s see how PBONUS works:
PBONUS calc:
Comp: DON: DON-BONUS: DON calc: vol%:
LCN 75 74.3 14.86 0.2
HCN 80 80.3 24.09 0.3
RFT 100 99.2 34.72 0.35
XXX 95 95.6 14.34 0.15
We have assumed above certain DON levels of neat components and certain blending ratios. Afterwards we have applied the bonuses and calculated the DON of the blend. Now we can show that with a setting of uniform INTERACT coefficients the INTERACT would calculate the same.
Before we show that method let’s show how INTERACT works. The calculation happening in the background is:
P = Pixi + Aijxixj
Where:
P – is the average property of the blend
Pi – are the pure component property values
xi – is the volume fraction of component i in the blend
xj – is the volume fraction of component j in the blend and
Aij – is the interaction coefficient between components i and j
With typical usage the matrix [Aij] is a lower rectangular, that is, coefficients on or above the diagonal are all zero, however if we wish to mimic PBONUS we ought to use a full matrix with uniform indices, as shown here:
*TABLE INTERACT
*
ROWNAMES TEXT LCN HCN RFT XXX
*
DONLCN -0.7 0.3 -0.8 -3
DONHCN -0.7 0.3 -0.8 -3
DONRFT -0.7 0.3 -0.8 -3
DONXXX -0.7 0.3 -0.8 9
This way the calculation will lead to the same results as PBONUS. This can be proven by following the P = Pixi + Aijxixj formula.
Now we want to show that for XXX the contribution is negative up until a certain point where it turns zero and then the contribution becomes positive.
We will achieve this by having one set of (negative) coefficients for the interactions between XXX and the rest of the blend and then we will have a (positive) coefficient for interactions between XXX and itself.
To start with we first need the zero point, let’s say that it occurs at 25%. We need to make sure that the relation between one of the negative coefficients (assuming they are all the same) and the positive coefficient, in absolute terms, is 1 to 3 (equal to the ratio of component percentage with negative bonus vs the component percentage with positive bonus).
Now we can use the weight of the coefficients to adjust the impact. E.g if we chose -3, -3, -3 vs 9 the neutral point will be at 25% XXX and the impact of XXX on the total Octanes will be as following, example below showing results for 15% and the calculation following the “P = Pixi + Aijxixj” formula:
ROWNAMES TEXT LCN HCN RFT XXX
* -0.3825
DONLCN -0.028 0.018 -0.056 -0.09
DONHCN -0.042 0.027 -0.084 -0.135
DONRFT -0.049 0.0315 -0.098 -0.1575
DONXXX -0.021 0.0135 -0.042 0.2025
We can work it out further to what it looks like as “pseudo PBONUS” on the examples of ratios -3/-3/-3/9 and -2/-2/-2/6:
09:03
vol% XXX Bonus/Blend Bonus/XXX
0.01 -0.0288 -2.88
0.05 -0.12 -2.4
0.1 -0.18 -1.8
0.15 -0.18 -1.2
0.2 -0.12 -0.6
0.25 0 0
0.3 0.18 0.6
06:02
vol% XXX Bonus/Blend Bonus/XXX
0.01 -0.0192 -1.92
0.05 -0.08 -1.6
0.1 -0.12 -1.2
0.15 -0.12 -0.8
0.2 -0.015 -0.075
0.25 0 0
0.3 0.285 0.8
We can work out such “response calculation tables” to fine tune the coefficients to be close enough to the data so they can be used in LP.
One caveat of the above approach is the fact that there will be a certain amount of bonus present at very low levels, those close to and approaching a zero, of presence of the component XXX – e.g. -0.3825 for the -3/-3/-3/9 and -0.255 for -2/-2/-2/6. Depending on the exact situation we can devise several strategies to deal with this, using PBONUS additional to INTERACT – something that can work in AO but not in DR. Adjusting the BLNPROP entries is an option in case of components with hardwired properties such as ethanol. For some other instances minimum content of the component can be set in BLNSPEC or teaspoon blending can be prevented via BLNSPEC.
KeyWords
INDEX
RVP
Blending
Ethanol
PBONUS
Keywords: None
References: None |
Problem Statement: How does Production Control Web Server (PCWS) implement a WRITE to the DCS when a change is made through a web viewer | Solution: When any APC application (DMCPlus, DMC3, IQ) runs for the first time, CIM-IO READ and WRITE lists are built based on the configuration in the application (READ, RDWRT, WRITE, ...). These lists are maintained as long as the application is running.
When an user is looking at an APC application on the PCWS through a web browser, any changeable field would be in Blue font. If that field has a DCS connection, the PCWS would use the existing list to write that change to the DCS. When the change is made through the PCWS, it does not discriminate whether that parameter is READ only, RDWRT, and WRITE in the application, it would trigger the WRITE to the DCS. Moreover, there is a temporary lock to the list during the WRITE so it would not interfere with the WRITE from the application.
Keyword
PCWS
READ WRITE list
Keywords: None
References: None |
Problem Statement: Aspen Watch (AW) reports are generated and stored in the AspenWatch (AW) server in the folder C:\ProgramData\AspenTech\SQLplus\Output. How do they get copied to the Aspen Production Control Web Servers so that they can be viewed. | Solution: Once the reports are stored in the output folder, the Querydef record AWPCWSReports is run on a regular interval to scan the output folder and generate a command file that pushed the reports to the C:\inetpub\wwwroot\AspenTech\ACOView\Reports using the WCF (Windows Communication Foundation) protocol. Only files with extension .htm will be copied. The record AW_WEB_SERVERS list the Web Server(s) that the reports will be copied to. To initiate a new copy cycle, blank out the parameter AW_LASTUPDATETIME for the corresponding web device.
Keywords: WCF
AW reports
References: None |
Problem Statement: How to build a rolling average calculation in Aspen DMC3 Builder | Solution: In order to build a rolling average, we need to have a stack equal to number of cycles in the rolling average. Below is the sample of calculation that calculate a 10 cycles rolling average of an input.
'Initialize the stack
'
if (fistrun=1 or ctl_init=1 or var_init=1) then
Input_avg = Raw_input
stack1 = Raw_input
stack2 =Raw_input
stack3 =Raw_input
stack4 = Raw_input
stack5 = Raw_input
stack6 = Raw_input
stack7 = Raw_input
stack8 = Raw_input
stack9 = Raw_input
stack10 = Raw_input
count = 1
End if
'Fill the stack with raw input
'
Select case count
case 1
stack1 = Raw_input
case 2
stack2 = Raw_input
case 3
stack3 = Raw_input
case 4
stack4 = Raw_input
case 5
stack5 = Raw_input
case 6
stack6 = Raw_input
case 7
stack7 = Raw_input
case 8
stack8 = Raw_input
case 9
stack9 = Raw_input
case 10
stack10 = Raw_input
End Select
'Update the counter
'
Count = count + 1
If Count > 10 then
Count =1
End if
'Calculate the average
'
Input_avg = (stack1+stack2+stack3+stack4+stack5+stack6+stack7+stack8+stack9+stack10)/10
Stack1 through Stack 10 are user-defined variables. Raw_input is mapped to the DCS measurement where Input_avg is the rolling average of Raw_input
Keywords: Rolling average
AspenCalc
References: None |
Problem Statement: Attached to this article is a sample query that displays the active file set number of a repository, the number of tags being written to the active file set, and the list of tags with their definition records stored in the file set. | Solution: The query prompts for a case sensitive repository name.
Using the object AtIP21HistAdmin, the query finds the active file set number of the repository.
Next, the query issues a system command to run the Aspen InfoPlus.21 utility h21summary. The query parses the the output of h21summary to retrieve the number of tags stored in the file set and the tags themselves.
The query assumes h21summary is stored in the folder C:\Program Files\AspenTech\InfoPlus.21\c21\h21\bin. Edit the macro h21summaryPath if the utility is stored in a different location on your Aspen InfoPlus.21 server.
Keywords: h21summary
AtIP21HistAdmin
References: None |
Problem Statement: ** Courtesy Magnetol international
Wave radar type level instrument requires dielectric constant information. It sends high-frequency electromagnetic pulses to downward and it measure the discontinuity of dielectric constant between vapor and liquid to indicate exact level. This level instrument generally does not affect by density, temperature and pressure changes.
Aspen Plus can calculate dielectric constant of mixture, but it is risky when we use dielectric constant calculated from Aspen Plus to radar type instrument directly. | Solution: The reason is that Dielectric constant of Aspen Plus is mainly used for electrolyte system phase-calculation and might not accurate for plant instrumentation.
Aspen Plus does not rigorously calculates mixing effect of dielectric constant. Moreover, dielectric constant information of many components may be missing if the component is not generally used in electrolyte mixture calculation. (i.e. Ethane, Propane) This can be a significant issue if user want to install radar type instrument for 2-phase liquid system. In general, dielectric constant gap between 2 liquid phases is smaller than air-liquid phases.
User can use Aspen Plus's dielectric constant, however, calibration work after the installation is necessary. Also, please check if components has CPDIEC parameters carefully, otherwise it is using "2" as default value.
Keywords: Dielectric Constant, Electrolyte, GWR, Radar
References: None |
Problem Statement: There are 2 tuning factors for rate-based column simulation.
Heat transfer factor and interfacial area.
Interfacial area is used to adjust mass and heat transfer while heat transfer factor adjust heat transfer between liquid and vapor phase.
If user has operation results from real plant or experiment, user can use 'Data-Fit' feature to tune those 2 factors. | Solution: Basis : Assume that user has input all the internal information and done the rate-based simulation.
Heavy key entrainment to the top and light key entrainment to the bottom is 582 kg/hr respectively.
Assume that the user has entrainment data and temperature profile from real operation.
1. Create Data-Fit case from Model Analysis Tool | Data Fit
2. Input data type in 'Define' Tab
3. Input experimental / operation data in 'Data' tab
4. Go to Model Analysis Tool | Data Fit | Regression, choose 'heat transfer factor' and 'Interfacial area' and regress them simultaneously.
Choose appropriate range for those parameters, parameter can exceeds 1 which means more heat / mass transfer is occurred in your data.
5. We can find the result that now the simulation well fit to the real operation results. We can take these 2 factors for future simulation.
Keywords: Rate-Based, Radfrac, Data Fit, Tune
References: None |
Problem Statement: When user choose feed convention as 'Above-Stage' in Streams (Tab) | Feed streams | Stage, user can input NS+1 stage which is not existing in the column. (NS: Number of Stage)
If user choose other feed convention like 'On-Stage', NS+1 stage shows consistency error. | Solution: For example, let's say the number of stage is 20 and there is vapor inlet stream at the bottom.
- If user input vapor stream to 20 stage with Above-Stage. Vapor is fed to 19 stage and column cannot converge.
- In this case, user can input vapor stream to 21 (NS+1) stage with Above-Stage. Then vapor is fed to 20 stage.
- This is basically same as input stream to 20 (NS) stage with On-Stage.
Any liquid in an above-stage 21 feed enters stage 20 (as in an on-stage 20 feed, since there is not actually a stage 21).
Keywords: RadFrac, Feed Stage, Convention, NS+1
References: None |
Problem Statement: Pure analysis in electrolyte system does not matching with the parameter (i.e PLXANT). | Solution: The reason is that the 'Chemistry' of electrolyte simulation and its chemical equilibrium is applied even if user use pure (or mixture) analysis.
For example, even if you want to see CH4O2 component's vapor pressure, it finds chemical equilibrium and not a pure component anymore.
So when user wants to analyze pure component's property, user need to remove chemistry.
Keywords: Electrolyte, Pure analysis, vapor pressure
References: None |
Problem Statement: Excess enthalpy cannot be calculated when user regresses only Aij / Aji parameters. | Solution: As excess enthalpy of mixing is calculated by differentiation of activity coefficient,
User need to regress Bij / Bji parameters together as it affect temperature term. (Bij/T)
If we see the Aij / Aji parameter, we can find that there's no temperature effect.
When user have excess enthalpy data, regression of 4 parameters (Aij / Aji / Bij / Bji) is recommended for the mixture.
When the mixture includes water, user may need to consider to include Eij and Fij as well to get the better results.
Keywords: NRTL, excess enthalpy of mixing, regression
References: None |
Problem Statement: High Performance Tray has special type of internal dimension. Aspentech provides various types of conventional tray, but no options for this special tray.
Now most of vendor provides high performance tray (or sometimes, high capacity tray) that can have 5 to 15 % capacity advantages over conventional trays. | Solution: Not exactly, user need to adjust the model to achieve this.
There are 3 adjustment factors provided for column hydraulic. User need to understand these factors to model his/her own proprietary column.
Please go to Radfrac | Internal | Design Paramters
System Foaming Factor : This factor adjust flooding limit (Csf) that decide vapor flowrate limit.
Overdesign Factor : This factor will directly applied to vapor / liquid flowrate both.
Aeration Factor Multiplier : This factor adjust pressure drop through the tray.
(For detailed equation and description, please see the Online help)
For example, if user is using high performance tray that can achieve 10% more liquid load / and 20% more vapor load over conventional tray.
Overdesign Factor : 1 / 110% = 0.909 (Liquid 110% / Vapor 110%)
System Foaming Factor : 1 * 120% / 110% (adjusted by overdesign factor) = 1.09
Aeration Factor also need to adjusted as per the pressure drop.
For real operation, it is always good to adjust those 3 parameters to fit to the real operation.
Keywords: Radfrac, Column Hydraulic, High performance tray
References: None |
Problem Statement: Which pressure is used if you specify both the global pressure and system back pressure in Aspen Flare System Analyzer? | Solution: In Aspen Flare System Analyzer the user can specify the Atmospheric pressure in the Calculation Settings Editor as shown below.
The user can also set the System back pressure in the scenario editor. System back pressure refers to the static pressure at the outlet of the flare tip. By default, this is set to atmospheric
pressure.
The System back pressure is scenario specific. The Flare System Analyzer uses this as the flare tip pressure for the specific scenario. If this value is left empty then the atmospheric pressure is used for all the scenarios.
Keywords: Atmospheric pressure, System back pressure
References: None |
Problem Statement: I have imported a template in my flowsheet but the fluid package in the imported template is different from the main-flowsheet. How do I change the fluid package for the template imported in the flowsheet? | Solution: The template inherits the fluid package used to create the template flowsheet. The user has the option to change the fluid package after importing this into the current simulation. The option is available in the Home page under Fluid Package menu as highlighted below.
The Fluid Package Manager will open when you click on Fluid Package menu.
The user can then change the fluid package (Basis-1) for the imported template to the fluid package used in the main simulation (GasPlant). In the above screenshot the template name is FLOW-1.
Keywords: Fluid Package Association, Fluid Package Manager
References: None |
Problem Statement: How do I exclude the height restriction in depressuring study when using Fire API521 equation? | Solution: The Fire API521 Operating Mode uses the heat flux model described in Section 4.4.13 in API Standard 521. Three coefficients: C1, C2, and C3 must be specified. The equation used by the Depressuring Utility is an editable form of the empirically-derived API 521 heat flux equation for a liquid-containing vessel.
The vessel wetted area is used to calculate the heat flow; in accordance with API 521, this heat flow is applied directly to the liquid in the vessel (as opposed to the vessel wall).
The following equations are based on conditions where there is adequate drainage and firefighting for the depressuring system.
API Equation
(field units)
Q = 21000 x F x A0.82
Q = total absorption to wetted surface (BTU/h)
F = environmental factor
A = total wetted surface (ft2)
API Equation
(metric units)
Q=43.116xFxA0.82
Q = total absorption to wetted surface (kJ/s
F = environmental factor
A = total wetted surface (m2)
According to API521, for equipment containing liquid, the depressuring rate is governed by the rate at which vapor is formed due to the liquid inventory boiling. To determine this vapor generation rate, API recommends that you only take into account only the portion of the vessel that is wetted by liquid up to 7.6 m (25 ft) above the source of the flame. Individual companies may deviate from this figure, so make sure that this is accurate for your situation. This usually refers to ground level, but it can be any level capable of sustaining a pool fire.
If any user requires a deviation of 7.6 m height restriction then this can be achieved by changing the base elevation of the vessel relative to ground level. By default this is set as 0.00 m. You can open the depressuring sub-flowsheet and change the base elevation available under Rating | Nozzles page of the vessel.
Keywords: Depressuring, Fire API521
References: None |
Problem Statement: How do I view the phase properties for the various headers and tailpipes? | Solution: It is possible to view the phase properties of the fluid within the various headers and tailpipes within the flare system. To do so, you must first ensure that the "Save Phase Properties" check box is checked off in the Preferences. To verify if the box is checked, access the Preferences view via the File menu. If the box is not checked, check it off and then re-run the calculations. This is necessary to obtain the actual phase properties. Once the calculations have been successfully completed with the aforementioned check box active:
Go to the View menu, select Results and then Physical Properties. If each pipe segment appears to have only one row associated with it and only lists "F" in the Phase column, double click anywhere on the view. The view will expand and the individual phase properties will be displayed.
The phases are denoted using the following legend:
F = bulk fluid
V = vapour phase
L = hydrocarbon liquid phase
W = aqueous liquid phase
M = mixed liquid phase
If the phase properties have been saved for a particular calculation, they will be printed when the results are directed to a printer or flat file format regardless of what is displayed on the screen.
Keywords: phase properties
References: None |
Problem Statement: How do I use the TEE in Dynamic mode? | Solution: In Dynamic mode the flow rates of the exit streams from the TEE are determined by the pressure flow solver. This gives the realistic flow behaviour in the dynamic simulation.
The user can also consider "Use Splits as Dynamic Flow Specs" in the TEE as shown below.
With this specification active, the user can define the flow of each stream by entering the valve openings for each exit stream. This configuration is not generally recommended since the flow from the TEE is determined from the split fractions and not from surrounding pressure network in the simulation. If this option is used, the number of dynamic specification will increase by one. The user will need to remove one specification, for example, the pressure-flow specification from one of the valves in the downstream of the TEE.
There are two HYSYS cases attached for illustration purpose: one without the split specification and one with TEE split specification.
Keywords: TEE, TEE Split Dynamics
References: None |
Problem Statement: How is the k value calculated for LNG exchangers in Dynamic mode? | Solution: The k value in the LNG exchanger is calculated based on laminar flow or by the flow equation.
Laminar flow
If the laminar option is checked the k value is calculated as:
k = SQRT(massFlow/(massDen * dP))
Flow Equation
If the flow equation is checked then the k value is calculated as:
k = massFlow/SQRT(massDen * dP) as the initial value
The k value is then improved iteratively with the equations given below:
rhs = moleflow * (moleflow + k) - moledensity * (k) * (k) * dP;
drhsdk = 0.5 * moleflow * 0.02 / SQRT(k) - 2.0 * moledensity * (k) * dP;
dk = rhs / drhsdk;
k = k - dk;
The iteration is continued until dk is very small or reached 500 iterations. If no improvement is found then the original k value is used.
Keywords: LNG Exchanger, Dynamic, k Value
References: None |
Problem Statement: Simple Partial Differential Equation modeling in Aspen Custom Modeler | Solution: Here is a simple PDE model to illustrate the below equation, example file is attached.
Equation for linear heat transper, v is heat transfer coefficient.
CODE
Model PDE
Axis as LengthDomain (length:8,HighestOrderDerivative:1,spacingpreference:0.5);
// 8m X-axis, 0.5m discretization, so 16 point.
T as Distribution1D (XDomain is Axis) of temperature;
// Declare T as function of x : T(x,t)
v as realvariable (fixed);
// Constant v
$T = -v*T([1:16]).ddx;
// Partial differential equation
T(0) : 25, fixed;
// initial conditions
T([1:16]) : 25, rateinitial;
// boundary condition
End
When user initialize the dynamic simulation, user can find that all temperature in the X-axis are equalized at 25 degC in temperature profile plot.
Let's add the task to change the inlet temperature,
Task T_Change runs at 1
ramp (B2.T.value(0),50,0.1);
Wait 5;
ramp (B2.T.value(0),0,0.1);
End
User can find that the temperature profile is changing as per the inlet temperature change.
Keywords: Partial Differential Equation, Aspen Custom Modeler, Heat transfer equation
References: None |
Problem Statement: What are the required steps for upgrading an SLM server running on an InfoPlus.21 machine? | Solution: Before following these steps, it is recommended to schedule an InfoPlus.21 downtime window, as InfoPlus.21 functionality may get affected. To read more about the different InfoPlus.21 license states and behavior, refer to KB 18640.
Go to C:\Program Files (x86)\Common Files\Safenet Sentinel\Sentinel RMS License Manager\Winnt and backup your license file “lservrc” and move it to a safe folder.
Go to the Control Panel > Programs and Features and uninstall “Sentinel RMS License Manager 8.x”.
Download the latest SLM software from the Download Center.
Install SLM server by following the KB 22399.
After SLM server is installed, install the network license by following KB 22408.
Verify the license is loaded by using the SLM License Profiler. For instructions on how to use the SLM License Profiler, refer to KB 22014.
Note: You will be required to stop and start the InfoPlus.21 Database if InfoPlus.21 could not regain the license.
Keywords: IP.21, SLM, MSC, MES, Manufacturing
References: None |
Problem Statement: How to interpret temperature profile of Absorber column? | Solution: Absorber column for gas solute that is absorbed to liquid solvent usually shows temperature increase within the column.
This is because of the absorption heat (Vapor Solute changes to Liquid Solute, similar to heat of vaporization) and heat of mixing between Solute and Solvent. (i.e. CO2 solute absorption to Amine solvent)
In industry, we usually call the highest temperature point as 'Temperature Bulge'.
Solvent flowrate need to be decided by the solute fraction in outlet gas which is usually the target of unit operation.
But the temperature bulge helps interpretation of the column.
Bulge in Bottom Zone
Bulge in Top Zone
Case file is attached for the above column temperature profiles.
If we decrease the flowrate of solvent. We can observe that the bulge goes up to the top. It means most of absorption occurred in the top side and the bottom side doesn’t active. Because there’s no driving force between vapor solute to solvent.
If we increase the flowrate of solvent, the bulge will goes down to the column. This is the desired condition which means your whole column stages are active for absorption.
Rule of thumbs is to achieve target spec. of outlet gas while maintaining the bulge in the bottom zone.
Keywords: Absorber, Solute, Solvent, Temperature Profile, Temperature Bulge
References: None |
Problem Statement: What is Criss-Cobble equation and how it calculates aqueous phase heat capacity at infinite dilution (CPAQ0) ? | Solution: For Ion type components in electrolyte simulation, thermodynamic properties like entropy, enthalpy and Gibbs energy information are required.
If those information are missing, Aspen Plus use Criss-Cobble correlation to estimate those properties.
The Criss-Cobble model is based on a model that the standard partial molal entropy of an ion at a given temperature is based on the reference temperature entropy using an equation of the form S = (e T + f) + (g T + h)*S_ref. There are five different sets of e, f, g, h coefficients for the different classes of ions. You can find the coefficients in Studies of Redox Equilibria at Elevated Temperatures I. by Derek Lewis, 1969.
For the details of the correlation parameters, please find it in Online Help documents as below.
Keywords: Criss-Cobble, Ion, IONTYP, S025C
References: None |
Problem Statement: There are a lot of questions regarding if a SQL server database is supported in certain versions of PSC products from V8.8 to V11. This article is a quick reference on the list of supported database versions. | Solution: Version Number Database Servers
V8.8 Microsoft SQL Server 2012 SP1 Standard & Enterprise
Microsoft SQL Server 2008 R2 SP2 Standard & Enterprise
Oracle Database 12.1.0.2 (Only supported in MES and SCM)
Oracle Database 11.2.0.4 (Only supported in MES and SCM)
Oracle Client 11.2.0 or 12.1.0 (32-bit) must be installed to access data available from a compatible Oracle Server 11.2.0 or 12.1.0. Supported Web Server
V9 Microsoft SQL Server 2014 SP1 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO
Microsoft SQL Server 2014 SP1 (Express Edition) PIMS, APS, MBO
Microsoft SQL Server 2012 SP2 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO
Microsoft SQL Server 2012 SP2 (Express Edition) PIMS, APS, MBO
Microsoft SQL Server 2008 R2 SP2 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO
Microsoft SQL Server 2008 R2 SP2 (Express Edition) PIMS, APS, MBO, PSCP,
Oracle Database 12.1.0.2 APS, MBO, AFO(Retail)
Oracle Database 11.2.0.4 APS, MBO, AFO(Retail)
V10 Microsoft SQL Server 2016 SP1 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO, AUP
Microsoft SQL Server 2016 SP1 (Express Edition) PIMS, APS, MBO, AUP
Microsoft SQL Server 2014 SP2 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO, AUP
Microsoft SQL Server 2014 SP2 (Express Edition) PIMS, APS, MBO, AUP
Microsoft SQL Server 2012 SP2 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO, AUP
Microsoft SQL Server 2012 SP2 (Express Edition) PIMS, APS, MBO, AUP
Microsoft SQL Server 2008 R2 SP3 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO, AUP
Microsoft SQL Server 2008 R2 SP3 (Express Edition) PIMS, APS, MBO, AUP
Oracle Database 12.1.0.2 APS, MBO, AFO(Map Monitor Server)
Oracle Database 11.2.0.4 APS, MBO, AFO(Map Monitor Server)
V11 Microsoft SQL Server 2017 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO (Retail), AUP, AUS
Microsoft SQL Server 2017 (Express Edition) PIMS, APS, MBO, AUP, AUS
Microsoft SQL Server 2016 SP1 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO (Retail), AUP, AUS
Microsoft SQL Server 2016 SP1 (Express Edition) PIMS, APS, MBO, AUP, AUS
Microsoft SQL Server 2014 SP2 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO (Retail), AUP, AUS
Microsoft SQL Server 2014 SP2 (Express Edition) PIMS, APS, MBO, AUP, AUS
Microsoft SQL Server 2012 SP3 (Enterprise/Standard Edition) PIMS, APS, MBO, PSCP, AFO (Retail), AUP, AUS
Microsoft SQL Server 2012 SP3 (Express Edition) PIMS, APS, MBO, AUP, AUS
Oracle Database 12.2.x 64-bit APS, MBO, AFO(Web Server & Retail)
Oracle Database 11.2.x 64-bit APS, MBO, AFO(Retail)
Keywords: None
References: None |
Problem Statement: When trying to save a plot on the Production Control Web Server (PCWS) site, operation is not successful, and the following error shows up.
“Permission denied – No account was found: Launch browser using ‘Run as Administrator’ or contact your administrator” | Solution: First try to run the PCWS site as an administrator as indicated on the pop-up message.
If the above does not work, on the web server, check that the following folders have Write permissions (NTFS file security system) for the username you use to log on to the Production Web Control Web Server site:
C:\inetpub\wwwroot\AspenTech\Web21\Plots
C:\inetpub\wwwroot\AspenTech\Web21\WebControls\Plots
Go back to PCWS and try to save the plot again.
The location of these folders is currently fixed and cannot be changed due to security reasons.
If the above steps do not work. Please contact Aspentech Support.
Keywords: : Production Control Web Server, Plot.
References: None |
Problem Statement: DMC3 Builder would crash upon open an existing project. This is largely due to corrupted file(s). | Solution: DMC3 Builder stores the project as a series of files or folders. Most of the datasets and applications are stored under the APC folder. In case of a corrupted project where you can't open it, it is largely due to one or more corrupted files (hopefully it is not one of the dataset or applications). To fix a corrupted project the first thing you can try is:
Open DMC3 Builder and create a brand-new project. Save it and Close DMC3 Builder.
Open the folder contents of the old project and find the “APC” folder.
Copy the APC folder from the old project to the new project, overwriting the new project’s APC folder.
Now use DMC3 Builder and try to open the newly created project.
If the problems persist, it means something under the APC folder is corrupted. The next step is to inspect the project.contents file. This file must reflect the same folder structure inside the APC folder. If not, you can repair it following the steps below.
Look at the following example for project structure:
Your project.content file should look like the following:
1 <- version number
3 <- number of datasets
dataset0 <- name of dataset
dataset0 <- directory name
dataset1
dataset1
dataset2
dataset2
2 <- number of applications
application2 <- name of application
application2 <- directory name
application3
application3
You can create this file and save it under the project folder and try to open your DMC3 project again. Note: DO NOT include the comments on the right when creating the project.content file.
If fixing the project.contents file does not solve the issue, please go to the APC folder and delete the _scrnsttngs.dat_ and project.content files. Close the file explorer and open the new DMC3 Builder Project.
If the above steps fail to recover your project, it is most likely due to a corrupted dataset or application. To fix a corrupted dataset or application please follow the procedure on KB48360 or contact Aspentech support.
Keywords: DMC3 Builder
corrupted project
References: None |
Problem Statement: Trouble enabling ASW V10.0 in Excel | Solution: If you have trouble getting the V10.0 ASW add-in enabled in Excel:
1. first, try to activate the add-in through the option in Excel (refer to the article “How to enable ASW in MS Excel?” for more details https://esupport.aspentech.com/S_Article?id=000046735 ).
2. if it is without success, then perhaps the problem is related to compatibility of the installed Microsoft Office and the ASW version. Please, pay attention that 64-bit Office is not support in V10 Engineering. That’s why it’s needed to install V10.1 Aspen Engineering on above existing version V10.0.
Aspen Engineering V10.1 supports 64-bit Excel for ASW. Users can download Aspen Engineering V10.1 from esupport website / My Download Center
Key words
ASW V10, enable ASW, COM Add-Ins
Keywords: None
References: None |
Problem Statement: How to changed default first result displayed after run in EDR? | Solution: By default Aspen Exchanger Design and Rating (EDR) program will display warning/messages page after run, but program will allows the user to change first displayed result page after run.
To change default first result displayed after run, please go to File and then click on Options page to open Program settings window.
In Program settings window go to UI options 2 page and select desired option by clicking the pull-down arrow next any program for that you want to change the default first displayed result page and Click OK to save the changes.
Please find below screenshot for your reference.
Keywords: Display result
References: None |
Problem Statement: Installing the Aspen Microsoft Excel Add-ins from the Aspen IP.21 Process Browser may fail due to permission errors or an internal security policy. This solution explains has to install the Aspen Microsoft Excel Add-ins (both the COM and legacy add-ins) directly with the files used by the Aspen IP.21 Process Browser home page links. | Solution: Use the file [Disk drive]\inetpub\wwwroot\AspenTech\AspenCUI\ExceladdinSetup.exe on the Aspen IP.21 Process Browser server to install the COM-based ribbon add-in. This file installs the proper add-in based on the system architecture (32-bit or 64-bit). The setup program opens and closes a command window without displaying a success message because the setup program is designed to be run from the Aspen IP.21 Process Browser home page. To confirm a successful installation, open a new spreadsheet Microsoft Excel and verify the Aspen Process Data ribbon appears.
Use the file [Disk drive]\inetpub\wwwroot\AspenTech\AspenCUI\AddinControls.cab on the Aspen IP.21 Process Browser server to install the legacy add-in. This .cab file contains all the files needed by the legacy Excel Add-in and is usually extracted on a default windows folder (like in C:\Windows). To install you will need to open Excel and go to Options/Add-ins, click on the Go button and browser for the AtWebData.xla or AtWebData.xlam depending on your Excel version (see solution 128239).
Keywords: Excel
Add-in
ExceladdinSetup.exe
AddinControls.cab
References: None |
Problem Statement: Problem Statement:
How can I manually secure an individual Aspen IP.21 Process Browser page? | Solution: Adding a few simple lines of code to a page can secure the page from being viewed by members not in the specified role.
In the following file example (PEXYPlot.asp), the highlighted added code will allow only the AFW roles of "Aspen Web.21 Administrators" and "Aspen Web.21 Users" to view the page:
Notes:
? The securing of ASP Pages is Case sensitive.
? Individual pages can also secured by using NTFS File Permissions by Windows group or users.
KeyWords:
Securing Aspen IP.21 Process Browser
Roles
ASP code
custom
Keywords: None
References: None |
Problem Statement: During the installation of Aspen InfoPlus.21 Server you can select a different drive for the aspenONE products rather than C drive. The group200 folder should be installed under the specified folder. If, instead, you had installed to the C drive but later want to move it to a different drive you will need to make several manual changes.
This knowledge base article describes how to change the location of the group200 files to a drive other than "C". | Solution: To achieve this change, follow the steps below:
1. Stop the Aspen InfoPlus.21 database
2. Stop the Aspen InfoPlus.21 Task Service
3. Move the group200 folder from its current location - by default,
%ProgramData%\AspenTech\InfoPlus.21\db21\
- to its new location - for example,
D:\AspenTech\InfoPlus.21\db21\
4. You will need to change the value of the IP21GroupFolder parameter in the IP21Profiles.xml file to reflect the new location of the group200 folder. You can edit the IP21Profiles.xml file directly using a text editor. Since V8.0, a utility program called the System Profile Manager can be run from the Actions menu of the Aspen InfoPlus.21 Manager. Use this tool to show you the Root Folder containing the IP21Profiles.xml file itself. After making the changes required to the IP21Profiles.xml file use System Profile Manager to confirm the updated location of the InfoPlus.21 group files.
5. In Aspen InfoPlus.21 Manager make the following changes to the TSK_DBCLOCK task:
a. Double click TSK_DBCLOCK task in the Defined Tasks area, so you can see its definition information in the NEW TASK DEFINITION area.
b. Correct the Command line parameters field with the full path to the relocated snapshot,
eg. SNAPSHOT="D:\AspenTech\InfoPlus.21\db21\group200\InfoPlus21.snp". Click the UPDATE button.
c. Double click TSK_DBCLOCK task in the Defined Tasks area again and click Snapshots Button.
d. In the Configure Snapshot List correct the full path of any relocated snapshots. Click the OK button.
6. The TSK_OPCUA_SVR external task reads in xml configuration files when it starts up. By default, the location of the InfoPlus21.Opc.Ua.Server configuration file is in the group200 folder. You will now need to correct the file location parameter. To do this, edit the InfoPlus21.Opc.Ua.Server section of the \AspenTech\InfoPlus.21\db21\code\IP21OpcUAServerHost.exe.config file. Save your changes.
7. Reboot the server and start the InfoPlus.21 database. Confirm to yourself that no errors have occurred.
8. Finally, run the Aspen InfoPlus.21 Administrator and make sure you are not using an incorrect full path for the any records defined by DataBaseSaveDef.
Keywords: Installation
Group200
TSK_DBCLOCK
Root folder
move
References: None |
Problem Statement: What is this warning and how this can be eliminated? | Solution: This warning message will appear if you select “TEMA F and F EJ Line Element FEA interface� option expansion joint calculation as shown below.
TEMA F and F EJ Line Element FEA interface EDR now interfaces to the TEMA flanged-and-flued (thick wall) expansion joint Line Element Finite Element Anaylsis software, obtained directly from TEMA. The FEA analysis results can now be obtained much faster than with traditional FEA tools. The program provides and receives all the required data to design the expansion joint and the tubesheet-shell-tubes assembly.
The TEMA Line Element FEA is a DLL created by Paulin Research in Houston. To perform this calculation, the users need a DLL file to be used together with EDR, the warning is present when this DLL is missing.
TEMA is working with Paulin Research to market the DLL. Please contact TEMA directly regarding this DLL.
Keywords: Expansion Joint, TEMA, Flanged and Flued Joint
References: None |
Problem Statement: Why do I get an error message in Aspen Asset Analytics when cloning a model or build? | Solution: In Asset Analytics you can clone or copy a model/build that you have already created.
When copying a model you select the 'Copy' (fig 1) icon
Figure 1
You then receive an error message.
"Error Cloning Root Cause Model in DAWS Response from DAWS:
The model could not be saved because it does not exist"
This issue occurs as after the latest patch is applied the models that were created before the patch cause this error.
Note that the case has been copied and works as before. To resolve this issue you will need to create a new case.
Keywords: None
References: None |
Problem Statement: A new Aspen InfoPlus.21 HPT Search Data Management page was added to Aspen IP.21 Process Browser in V8.0. Using the management tools it is now possible to completely purge the HPT search index or simply update/remove tags from the index by specifying the individual data source they belong to.
On clicking the Purge Data Source button an Error dialog box may immediately appear stating that the function is invalid or violates the same-origin security restriction: | Solution: This error is likely to occur if your server has Internet Enhanced Security (IE ESC) enabled for Administrators. This feature needs to be disabled for High Performance Trend operations to work correctly. To disable this feature see How to correct the messsage "zoom control unable to create canvas element"on Tag search ?
Note, a similar error is also likely if you attempt to update/delete indexed tags on the management page using the Update or Delete buttons.
Keywords: High Performance Trend
Purge Update Delete Index
solr tag_datasource_nav
References: None |
Problem Statement: This knowledge base article documents why users attempting to open the Aspen Audit & Compliance Manager webpage via IP.21 Process Browser are seeing the error message:The certificate used to identify this application has expired. | Solution: This happens because the Rsproxy.jar certificate expired on the 19-June-2017. Customer may update the jar file with the attachment to this article. Please carry out the following when updating the jar file location.
Create a copy of the old file as backup file as there may be a chance that the file is corrupt when downloaded from the attachments.
Copy and paste the new file to the following location.
<Root drive>\inetpub\wwwroot\AspenTech\AuditAndComplianceManager\_ScriptLibrary
NOTE: You may need to clear the web browser’s cache before testing and may require a server restart.
Keywords: AACM
SHA256
Certificate Exipry
References: None |
Problem Statement: If there are V8.x 64-bit products installed in a non-default installation folder, after upgrading to V9.x, some of the product installation files are moved to the default installation location (C:\Program Files\Aspentech), instead of remaining in the non-default installation folder.
This is caused by the V8.x 64-bit installer not creating the ASPENROOT64 registry key during the installation of V8.x. | Solution: Before upgrading to V9.x, you will need to add the ASPENROOT64 registry key. To do this, follow the steps below:
Open the Windows Registry by typing regedit.exe in the Start Menu Search Box. Right-click it and select Run as Administrator.
Expand HKEY_LOCAL_MACHINE\Software\ApenTech\Setup.
In the right pane, right-click and select New > String Value and name it ASPENROOT64.
Set the Value to the non-default location you originally installed. Please DO NOT miss the “\” at the end of the folder path (ie: “X:\XXX\”.)
Continue with the V9.x upgrade. Your files will be installed to the location you selected.
Keywords: aspenONE, V9, upgrade, install, 64-bit
References: None |
Problem Statement: Does Aspen Air Cooled Exchanger calculate the liquid level on the headers? | Solution: Aspen Air Cooled Exchanger does not explicitly calculate the liquid level in the header box based on pressure drop through the return passes and the necessary static head from condensate level in that header box required to remove the accumulating condensate.
However, we can use the Phase Separation option (Input | Program Options | Methods/Correlations | Tube Side | Tube side flow distribution) to calculate the steam process conditions of each tube row for a given tube pass, which gives an approximated liquid level in the header box in terms of tube row.
The user can observe the flow distribution for each row by viewing vapor fraction versus tube distance plot from Results | Calculation Details | Interval Analysis - Tube Side | Plots tab.
For full details of the method please see the HTFS Research Report RS1057 (1999) by P E Farrant.
Keywords: Header box, liquid level, phase separation.
References: None |
Problem Statement: Is there a JDBC driver for Aspen InfoPlus.21? | Solution: Historically, there has not been an AspenTech provided JDBC driver for Aspen InfoPlus.21. You have been able to use the Oracle JDBC-ODBC bridge included in JDK up to version Java SE 7. You then specify AspenTech SQLplus as the ODBC driver.
Starting with Java SE 8, the JDBC-ODBC Bridge will no longer be included with the JDK. This is described in the Oracle tech notes:
https://docs.oracle.com/javase/7/docs/technotes/guides/jdbc/bridge.html
If you were previously making use of the Oracle JDBC-ODBC bridge and now wish to move to Java 8+, one suggestion would be to use a third party JDBC-ODBC Bridge replacement to continue to connect to the AspenTech SQLplus ODBC driver.
If possible, as an alternative you could make use of the Aspen Process Data REST Service. See Knowledge Base article 138723-2 for more information regarding Aspen Process Data REST Service.
Note, it is worth pointing out that the Aspen Role-Based Visualization (RBV) Dashboard (RTView) requires a JDBC driver to connect to Aspen InfoPlus.21. However, since the Oracle JDBC-ODBC bridge has been removed from Java 8, we now provide an Aspentech driver as a replacement (starting with RBV V9.0). To make use of that in RBV please refer to the Aspen Role-Based Visualization Implementation Guide (Chapter titled "Aspen Operations Dashboard Configuration"). As explained in the Guide, the name for the JDBC Driver Class would be: Aspentech.JdbcOdbc.JdbcOdbcDriver
With Aspen Production Execution Manager (APEM) the AspenTech's JdbcOdbc bridge driver contains the following two parts:
AeBRSJDBC.jar: installed in the folder: %TOMCAT_HOME%\lib
AeBRSODBC.dll: installed in the AspenTech shared folder: %ProgramFiles(x86)%\Common Files\AspenTech Shared
For APEM, Aspen's JdbcOdbc bridge driver is only designed to be used to connect to Aspen Production Record Manager (APRM) and InfoPlus.21 database (it has only been tested for AspenTech's Production Record Manager and SQLplus ODBC driver). It is used to replace Java's JdbcOdbc bridge driver.
Keywords: interface
development
java.sun.com
sun.jdbc.odbc.JdbcOdbcDriver
java.lang.ClassNotFoundException
References: None |
Problem Statement: Are there any Rules of Thumb while choosing a Statistical Data Distribution Type in AFR? | Solution: Following are some Rules of Thumb while choosing a Statistical Data Distribution Types in AFR
Weibull betas - If it is greater than 2.5, double check your data
Log Normal distributions - Only use with 20+ data points
Number of Data Points - If Less than 4, then use Exponential
Normally Use Weibull or Exponential for Failures
Normally Use Normal or Triangular for Repairs
Keywords: Statistical Data Distribution, Rules of Thumb
References: None |
Problem Statement: When running a query in the Batch Extractor you get an error:
Error using SQL:Query timeout expired select * from vBDIS_INTERFACE_Subbatch where end is not null | Solution: This message can occur when you have entered a SQL query that either:
1. Is over 100 characters long.
2. The query involves too much data.
To resolve this issue you will need to shorten the query to resolve less data or you can increase the SQL timeout (see article 000044724):
https://esupport.aspentech.com/S_Article?id=000044724
Be careful not to set the timeout too high to cover up a query that could be creating performance issues. It is better to have multiple queries that are smaller.
Keywords: Batch Extractor
Interface
vBDIS
Query timeout
References: None |
Problem Statement: How can I solve the error ERROR> 'CD - 1' TOTAL INDIRECT WAS SPECIFIED - ITEMIZED INDIRECT IGNORED? | Solution: The cause of this error is an over specification for the Indirect Costs data for one or more contractors.
The user can choose to either specify the two fields in the INDIRECTS TOTAL section, which will affect all the indirect items.
Alternatively, if different specifications are known and wished to be entered for these indirect items (such as burdens, travel, etc.), instead of specifying a total cost, the user should fill the fields under INDIRETS ITEMIZED section.
However, note that if there is information for INDIRECTS TOTAL, the itemized section will be ignored, triggering the error. Make sure that only one of this options is entered to avid this error message.
Keywords: Indirects, Total, Itemized, Contractors, Error> 'CD.
References: None |
Problem Statement: While working in Visio I encountered an Illegal Connection error. Even after resolving the error, the enlarged pipe widths of the pipes in question do not revert to the original state. Is there a way to restore the original width? | Solution: There is no button of reverting the enlarged pipe in Visio. You will have to manually change the width of the pipe to match the standard. A quick way to do it is to Right click on the pipe à Styles à Line à Weight à 1.5 pt as shown in the following screenshot:
Keywords: Visio, Illegal Connection error, pipe width
References: None |
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