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Problem Statement: Some customers report receiving an error within the BCU log:
RetrieveAtTime : SetupForRetrieveAtTime() failed | Solution: This error message can be received when there are communication issues with the Aspen InfoPlus.21 Database, or network issues.
In similar cases deleting and reloading the BCU unit has helped, other times a system reboot can help.
If the BCU is running on the same machine as the Aspen InfoPlus.21 Database, then more likely a unit re-load or restart of the system will help.
Keywords: RetrieveAtTime : SetupForRetrieveAtTime() failed
References: None |
Problem Statement: Which character set should be used in an Oracle installation for Aspen Process Record Manager (APRM) or Aspen Audit and Compliance Manager (AACM)? | Solution: It does not matter what character set is loaded, APRM and AACM do not utilize features that depend on a particular character set. The Aspentech installations do not specify any character set and use what the server has configured. If the client and the server character sets differ from each other, Oracle converts between them during each interaction. Loading unnecessary character sets in a server will only slow it down.
It is the administrator's option to select a character set that is appropriate for their location and language. When migrating the DB it is fine to use the same character set as the original Oracle instance. And for new systems, the Oracle instances can be created with any character set that is appropriate for the customer?s location and language.
Keywords: Oracle
Character set
Installation
References: None |
Problem Statement: Sometimes you may need to retrieve a particular subset of data using the Aspen Batch.21 web service. For example, you may need to retrieve the value of the fourth instance of a characteristic for a given batch. This knowledge base article explains how to generate an XML file which can be used as an example of how to query for a specific set of data using the Aspen Batch.21 web service. | Solution: The Aspen Batch.21 reporting web site is essentially a web interface which allows a user to select data to be returned, generates an XML file for this query, submits the XML to the Aspen Batch.21 server through the Aspen Batch.21 web service then displays the results. You can use the Aspen Batch.21 reporting web site to generate a specific XML query which you can modify further then upload using the Aspen Batch.21 web service. To do this:
1. Create a basic report which specifies the data query using the GUI controls on the Aspen Batch.21 reporting web page.
2. After making sure the data is returned to the report as expected, save that basic report as something identifiable like QueryTest.
3. Go to the Aspen Batch.21 server.
In the folder AspenTech | Batch.21 | Data | Reports you will find the saved basic report xml file which contains the properly formed XML for the query you wish to perform.
4. Use this XML as an example of how to write your own query to query a specific set of data.
Keywords: webservice
References: None |
Problem Statement: How do you specify the Map record in the ATGetTrend function (Excel Add-In)? | Solution: One method is to useSolution ID 103453. However, some customers have reported getting an error (see Defect #CQ00189662). So a workaround is to manually update the formula (in the Excel fx input box) with the MAP record name as the third parameter, then hit Ctrl-Shift-Enter. Note that if you just hit Enter, you will get the following error:
Microsoft Excel
[ ! ] You cannot change part of an array.
[ OK ]
Keywords: excell
addin
References: None |
Problem Statement: How to print VBA form from a command button? | Solution: If you use VBA within Process Explorer, use this code behind the command button for printing the form:
Private Sub CommandButton1_Click()
Application.ActiveDocument.PrintOut End Sub
Keywords: print
form
command
References: None |
Problem Statement: My Aspen Process Explorer Users have noticed a setting labeled Enable Live Preview. How does this
Enable Live Preview setting located in the Process Explorer Options dialog work when it is checked? | Solution: When the Enable Live Preview setting has been checked (enabled), then added preview functionality is turned on when using the changeability settings on the Plot Layout Tab which allows Process Explorer Users to see a Live Preview of changes to things like the Plot Background and Pen Colors plus the Color and Visibility of the Grid Lines and Data Point Markers.
NOTE: This feature is ONLY available when the Ribbon Menus are being used.
The Live Preview functionality is automatically disabled and will not work if the User switches
over to using the Windows Classic Menu Views.
Example Instructions to Test this Live Preview functionality:
1. Open Process Explorer on a selected Aspen Client PC or Server.
2. Open the Process Explorer Options Dialog Box and check the Enable Live Preview checkbox, then click the Apply or OK button at the bottom of the dialog to save this setting change and close the Options Dialog and return to your Trends and/or the Main Application Window.
3. Create or open a New Trend Plot and Add 1 or more Tags.
4. Now assuming you are using the Ribbon based Menus, then Navigate to the Menu Bar at the top of the application window and Click the Plot Layout Menu to switch to that Tab View for the Ribbon Menu.
5. Now using the changeability features located on the Plot Layout menu bar tab, start exploring by clicking into the Plot Background and Pen Color Palettes and/or the Line and Data Marker Style Palettes and then hover your mouse cursor over the different Color, Line, and Marker Style selections and note the Live Preview behavior on the Plot still open in the background.
NOTE: Except for global items like the Plot Background Color or Grid Line Settings, the Enable Live Preview for the Pen, Markers, Scaling, and the Show Data Table button will apply to the Current Tag that is selected in the Legend of your Trend Plot. You can move the mouse back and forth from the Legend to select other Tags to activate for the Live Preview, and when a different selection is made you will see the current settings on the Plot Layout menu bar tab area change accordingly.
Supporting Live Preview Example Screen Shots:
Enable Live Preview checkbox on the APEX Options Dialog:
Plot Layout Menu Area Options for use with Live Preview:
Live Preview showing the Plot Background Color changing to Yellow when Hover over that Color in the Palette:
Live Preview of expected Plot Display Changes if the Line Color and Marker Style were to be selected and applied for the selected Pen (i.e., for the Tag highlighted in the Legend) as shown:
Keywords: Enable Live Preview
Plot Layout
Process Explorer Options
Trend Plots
References: None |
Problem Statement: You may have a situation where some client tools work, like SQLplus, Tag Browser, and the IP.21 Administrator. But, when you attempt to drag a tag from the Browser onto a Process Explorer trend plot, the legend will contain the message Invalid Server in the Value column. | Solution: When a tag is added to the legend of Process Explorer, it attempts to read the historical data from the InfoPlus.21 database. It uses a component called Process Data for IP.21 to read this history. This service component must be listed in the ADSA data source for history to be properly read. The service component looks like:
Aspen Process Data for IP.21
It has been noted that sometimes customers accidently choose the Aspen Process Data Events for IP.21 component.
Keywords: invalid server
adsa
process data
References: None |
Problem Statement: This knowledge base article provides troubleshooting steps for the following error:
Failed to start unit scheduling: 'B21BCU-55031: Unable to access the specified BCU data source: XXXX' | Solution: 1. Ensure that the Aspen Batch.21 data source (in the ADSA Client Config Tool) is configured properly and that a public data source is used. Sometimes deleting then re-creating the ADSA data source (even if no ADSA configuration issues are noticed) resolves the problem.
2. Ensure that the TSK_BATCH21_SERVER task is running in the Aspen InfoPlus.21 Manager.
3. Ensure that the account which starts the Aspen Batch.21 Services and the Aspen Batch.21 BCU Service is a domain account with local administrative rights on the local server.
4. This error has been seen on a system which runs in a cluster environment. In the cluster environment the Aspen Batch.21 Services and the Aspen Batch.21 BCU Service started at the exact same time. If this occurs on your system manually stop both of these services then start them manually (one at a time) then start the Aspen BCU Server.
Keywords:
References: None |
Problem Statement: When connecting to a RDBMS DataSource, Microsoft SQL in this case, and performing searches for tags using the Aspen TagBrowser tool it returns a message: “no record has been found” when searching for tag FI110:
if you try a different type of search, like FI110 Level it returns a number of tags. | Solution: In this case there were a a number of tags in the SQL database whose name started with the characters FI110, 20 of them:
and upon close examination found that there was a null value in the Value Column for one of the tags in the Microsoft SQL table. This was the reason for the error message and prevented the display of the tags found in the Aspen TagBrowser tool.
Once the null value was removed from from the column then the Aspen TagBrowser tool returns the correct number of tags.
Keywords: TagBrowser, RBDMS, search, tag
References: None |
Problem Statement: This Knowledge Base article shows how to resolve the following error message received when opening scheduling tables for all the areas in the system:
Failed while retrying actions in RunUnsyncProc
and the following error message recorded in the Batch.21 Administrator:
Open failed relational database error -2147217900 invalid column name char_value_extended
The above error messages started to appear after the Aspen Production Record Manager V7.2 Cumulative Patch 7, released on March 2012, had been applied to the system. | Solution: Run the Database Upgrade Wizard to update your Aspen Production Record Manager database as described in the Release notes for the patch.
The new database version should be 11.2.1.
Keywords: Patches, error, PRM
References: None |
Problem Statement: This knowledge base article documents the error messages that the Aspen Batch.21 client applications will return if the Aspen Batch.21 server processes or relational database is not running. | Solution: If Aspen Batch.21 Services and Aspen BCU Service are stopped:
Expanding a data source in the Aspen Batch.21 Administrator will result in the message:
The service cannot be started, either because it is disabled or because it has no enabled devices associated with it
Expanding an area in the Batch.21 Administrator may result in the error:
B21BAI-60104: Unknown Exception
Clicking on a batch in the Detail Display will result in the errors:
Invalid area name
Unspecified Error
The Batch Query Tool will display the messages:
DATASOURCE: Unable to retrieve any areas from data source
No batch areas available
The Characteristic Browser will display the messages:
Application error in Method '~' of object '~' failed
Need a batch area to build the tree view
Application error in DialogMgr BuildTree, Element not found
Need a batch area to set up instance tab
The BCU Administrator will display the following messages:
Failed to retrieve batch areas.
Error 80070422 : The BCU data source has not been started
If the relational database is stopped, but the Aspen Batch.21 Services and Aspen BCU Services are running:
Attempts to expand a data source with the Batch.21 Administrator will result in the message:
B21BSC-50002: Relational Database Error ' 2147467259: [DBNETLIB][ConnectionOpen (Connect()).] SQL Server does not exist or access denied.
The Detail Display will return the following messages:
'Invalid area' B21BSC-50002: Relational Database Error ' 2147467259: [DBNETLIB][ConnectionOpen (Connect()).] SQL Server does not exist or access denied.
The Batch Query Tool will display the following messages:
DATASOURCE: Unable to retrieve any areas from data source
No batch areas available
The Characteristic Browser will return the following messages:
B21BSC-50002: Relational Database Error 2147467259: [DBNETLIB][ConnectionOpen (Connect()).] SQL Server does not exist or access denied.
Need a batch area to build the tree view'
Application error in DialogMgr BuildTree, Element not found
Need a batch area to set up instance tab
The BCU Administrator will return the following messages:
Failed to retrieve batch areas. B21BSC-50002: Relational Database Error 2147467259: [DBNETLIB][ConnectionOpen (Connect()).] SQL Server does not exist or access denied
Keywords: Error
Failure
Connection
Connect
Disconnect
References: None |
Problem Statement: When opening the Aspen Production Record Manager Administrator, and then clicking on the Server Administration node, a Catastrophic failure error message is displayed: | Solution: Despite the strong wording of the error message itself, please note this is a client-side only error, and the data stored in the Batch database is not at risk of corruption. This problem can occur if:
1. There is a version mis-match between the Administrator tool on the machine where the error occurs, and the version on the server. Note, the version mis-match is not necessarily a major version, but instead both the server and client are the same version, but a different patch has been installed on either the client or server.
2. Key files related to the Administrator and API need to be registered using REGSVR32.exe
VERSION MIS-MATCH
This typically occurs if the Administrator is installed remotely on a client, and that client has not been patched to the same level as the server. This test is only relevant if the same major version is installed on both server and client. If it is the same major version, but the build number differs (in the example images below, aspenONE V7.2 is indicated by 11.2, and build is 326) then patch the client or server to align them.
To make check this, compare the version of the AtBatch21ApplicationInterface.dll on the client, with the one on the server. The default location is:
C:\Program Files\AspenTech\Batch.21\Client\
An easy way to see versions for all the files in the directory is to right-click in the column header area, choose More,
then add File Version to the column view:
At a glance you can see if all versionable files reflect the version you expect to see based on whatever installation or patch was last applied to the system:
REGISTER FILES
The file versions may be the same, but are not registered correctly.
On the Server, register the following two files:
C:\Program Files\AspenTech\Batch.21\Server\AtBatch21AtlServer.dll
C:\Program Files\AspenTech\Batch.21\Client\AtBatch21ApplicationInterface.dll
For Clients
C:\Program Files\AspenTech\Batch.21\Client\AtBatch21ApplicationInterface.dll
Example syntax for unregistering and re-registering:
C:\Program Files\AspenTech\Batch.21\Server>regsvr32.exe /u AtBatch21AtlServer.dll
C:\Program Files\AspenTech\Batch.21\Server>regsvr32.exe AtBatch21AtlServer.dll
If the Catastrophic error still occurs after these troubleshooting steps, please contact Aspen Support.
Keywords: None
References: None |
Problem Statement: When you use a Process Explorer Graphic to display the contents of a field, or use that field in a Process Explorer Adhoc calculation, then the syntax requires you to enter a RecordName followed by a FieldName
e.g. ATCAI IP_VALUE
You can even point to the first occurrence in History via for example
ATCAI 1 Ip_Trend_Value
How can this syntax be used to access the 2nd or 3rd occurance in history? | Solution: In this situation, use the IP.21 Administrator to look at the FIXED area of that record. A fixed area field such as IP_#_OF_TREND_VALUES defines the size of the in-memory history repeat area. Applications such as Process Explorer, Aspen Calc, SQL etc. can only read FieldNames that are in-memory.
Therefore if the History Repeat Area size is set to 1, those applications can read 1 Ip_Trend_Value, but they cannot read 2 Ip_Trend_Value, as it does not exist as an in-memory FieldName.
Setting the repeat area size to 2 means that the first and second occurrence FieldNames can be seen by these applications, but not any higher occurrences. Therefore, increasing the in-memory size of the History Repeat Area will allow more occurrences to be accessed but only up to that size.
Keywords:
References: None |
Problem Statement: Sometimes it is nice to see multiple trend plot blocks on one Process Explorer Display
The very old GUIs that came with CIM/21 and InfoPlus-X/GCS provided these capabilities
Within Aspen Process Explorer it was very difficult, but possible, to simulate this via manipulation of Microsoft Windows features. | Solution: A demo at AspenWorld 2004 displayed the new 9 Block Trend format.
AspenTech now provides a VB form that we distribute as:
?.. AspenTech\APEX\Samples\ProcessExplorer\VBForm\TrendPlots.apx
This form provides the option of 9, 3, 2 or 1 block trends, with or without a legend per block.
Although you may open and use this form in versions earlier than AspenOne, there was a problem in those earlier versions. If you added tags, saved the form, and re-opened it, the tag information was lost.
Keywords:
References: None |
Problem Statement: This knowledge base article provides an example Aspen SQLplus script which shows how to use the Aspen Production Record Manager Application Programming Interface (API) to retrieve the highest instance number of a given characteristic. | Solution: The following query will return the number of instances for a given characteristic. The line which returns the highest instance number is:
batchlist(i).characteristics.item('PRODUCT PLANNED',-2).instance;
When the characteristic is specified there is room for an optional instance number. If the instance number is specified to be -2 then the largest instance is returned.
-----------------------
local data_sources, batch, myarea, myquery, batchlist, i int;
local StartTime timestamp, EndTime timestamp;
data_sources = createobject('AspenTech.Batch21.BatchDataSources');
write 'DATA SOURCE NO: ' || data_sources('hklap').Areas.Count;
myarea = data_sources('hklap').areas('sqldemo');
MyQuery = MyArea.BatchQuery;
-- Clear the query.
MyQuery.Clear;
Myquery.CharacteristicConditions.Add('BATCH NO', 1, atEqual, '4147');
batchlist = MyQuery.get;
for I=1 to batchlist.count do
begin
write 'BATCH NO: ' || batchlist(i).characteristics.item('BATCH NO');
write 'NUMBER OF INSTANCES: ' || batchlist(i).characteristics.item('PRODUCT PLANNED',-2).instance;
write 'START TIME: ' || batchlist(i).characteristics.item('Start Time');
write 'PRODUCT PLANNED: ' || batchlist(i).characteristics.item('PRODUCT PLANNED');
write 'PRODUCT PLANNED: ' || batchlist(i).characteristics.item('PRODUCT PLANNED',2);
write 'PRODUCT PLANNED: ' || batchlist(i).characteristics.item('PRODUCT PLANNED',3);
write 'CHAR: ' || batchlist(i).characteristics.item('CHAR');
exception
write 'No BATCH NO';
end
end
batchlist = null;
batch = null;
---------------------
Keywords: Batch.21
References: None |
Problem Statement: I want to copy the composition from an existing stream to a new stream, but specify the flow of the new stream from a spreadsheet. | Solution: There is a workaround that will enable you to do this:
Create a new stream.
Attach the existing stream to a Balance unit operation. Select the Balance to be a Mole balance so that the composition from the existing stream is passed onto the new stream. Note that this also passes on the Molar Flow to the new stream, but we want to be able to specify the flow of the new stream.
Attach the new stream to a TEE unit operation. Specify 2 outlet streams from the TEE.
In the spreadsheet, export the desired Flow value from the spreadsheet to one of the TEE's outlet streams. You now have a new stream with the same composition as an existing stream, but the Flow of the new stream is specified from the spreadsheet.
Please refer to the attached HYSYS case for a demonstration of thisSolution.
NOTE: Thanks to HYSYS user Keith Henderson for thisSolution.
Keywords: copy of stream, stream, spreadsheet, define flow
References: None |
Problem Statement: This knowledge base article provides troubleshooting steps for the problem in which text within the Aspen Batch.21 web pages does not display properly. An example of this is shown below.
Note: If you experience this problem using Aspen Batch.21 version 6.0.1 please try the steps in knowledge base article 114224 before going through the steps in this article. | Solution: Verify that the local ASPNET account has permissions to these two directories:
C:\Program Files\AspenTech\Batch.21\Locale
C:\Program Files\Common Files\AspenTech Shared\Apex
? Verify that the following file exists:
C:\Program Files\Common Files\AspenTech Shared\Apex\atlocalization.dll
? Verify that the WebDAV web extension has not been set to Prohibited. If the WebDAV web extension has been set to prohibited set it to Allowed through the Web Service Extension list in the IIS Manager MMC snap-in.
? This problem could also occur if the local ASPNET account does not have sufficient privileges. As a test to see if the ASPNET account has sufficient privileges give the local ASPNET account administrative privileges to see if this resolves the problem. If giving the local ASPNET account administrative privileges does not resolve the problem then the ASPNET account likely has sufficient privileges.
? Since the Aspen SQLplus web site also uses ASPNET, if you have the Aspen SQLplus reporting tools installed, you can use the Aspen SQLplus web site as a further test of whether or not other ASPNET applications work correctly on this server.
? When you access the Aspen Batch.21 web page a process called aspnet_wp.exe (on Windows 2000) or w3wp.exe (on Windows 2003) should start on the server which runs the Aspen Batch.21 web site. Does this process start?
? If your site uses a proxy server between the web server and the client machine ensure that the proxy server is not set to prevent Java scripts from executing.
? IIS uses the userName account listed in
C:\Windows\Microsoft.NET\Framework\v1.1.4322\Config\machine.config
to run the ASP.NET worker process (either aspnet_wp.exe or w3wp.exe). This is the process that hosts the Batch.21 reporting web site.
Check to see what the machine.config file has configured to run the asp.net worker process. If the ASP.NET worker process is run as a low privileged account then try giving the account administrative privileges. This would only be done as a test to determine if there is a problem with the account which runs the ASP.NET worker process. (Usually the ASP.NET worker process is run under a somewhat restricted account in case a virus gets control of the ASP.NET worker process.)
Note: On some systems the account which runs the ASP.NET worker process must be changed from the Identity tab of the DefaultAppPool Properties of the IIS Manager.
You could set the ASP.NET worker process to run under the ASPNET account or you could follow the instructions in the following Microsoft knowledge base article which describes how to create a minimum privileged account for the ASP.NET worker process.
http://msdn2.microsoft.com/en-us/library/aa302396.aspx
Keywords: Text
missing
display
blank
gone
labels
References: None |
Problem Statement: This | Solution: outlines the details of new separately installable ODBC Driver for Aspen Production Record Manager (APRM, formerly called Batch.21) starting from V7.2.Solution
Aspen Production Record Manager (APRM) V7.2 now includes an ODBC driver that makes it possible for applications like Microsoft Excel to query data from the APRM server. The ODBC driver is comprised of a server and a client. The server is automatically installed on the same box as APRM server, while the client installs automatically with the APRM Client installation.
The ODBC driver installation is integrated with the Aspen Data Source Administrator (ADSA) service, and can be configured to use specific communications port numbers [default is port number 10016].
The APRM ODBC driver supports a specific subset of SQL syntax. This subset consists of the most frequently used query syntax for acquiring, filtering, and sorting data from the APRM server. Wildcards, UTC time, and support for working with sub-batches and child batches are included.
Keywords: V7.2 Overview
ODBC Driver
Excel
APRM
References: None |
Problem Statement: When stopping and trying to remove units from the BCU Scheduler table, this error appears: | Solution: This error can happen when the Designator structure is not configured correctly. Internally, Aspen Production Record Manager assigns a BatchID to each unique batch. However during configuration a Batch Designator (composed of up to five elements) is also created that becomes the standard way to refer to each batch. This Designator should also be unique for each batch. To avoid this worker thread error, make sure the Designator values for each batch are unique.
Keywords: B21BCU-55066: Unable to stop the unit's worker thread.
References: None |
Problem Statement: Previous versions of HYSYS only allowed display of a single stream variable on the PFD, for instance, one could press Shift-P to show the pressures next to the streams, instead of the stream names. The ability to show more than one process variable next to the stream is desired. | Solution: Attached is a flowsheet level user variable. It updates the stream description variable with useful numbers, such as Temperature, Pressure, Mass Flow, Molar Flow, Vapour Fraction and Heat Flow. On the PFD, you can use the shift-R key to show this description as the stream label.
Note that this user variable is intended to be used permanently in the simulation. Because of this, the code only executes at the very end of the simulation. It also means that if you make your whole simulation and at the end add this code, you will have to force a resolve to get the desired effect.
Directions to import and use the user variable are as follows:
Save the ShowConditionsFlowsheet.huv from thisSolution on your hard drive.
Open your case.
Go to the Simulation menu, and select Import and Export User Variables.
Press the Select file button, and select the ShowConditionsFlowsheet.huv file.
In the 'User Variables in Export File' window, highlight the Flowsheet user variable and press the Import button, then press OK.
Go to the Flowsheet menu and select the Flowsheet User Variables item. Press the Green checkmark, then check the box next to the words 'Code Only' and close the window.
7- Force a resolve of the flow sheet for the User Variable to go through one calculation pass. This is needed to create the stream user variables.
Go to the stream(s) you want to see information for, and switch to the Worksheet tab, User Variables page. Next to the Show Conditions box, input letters for the variables you wish to see on the PFD. For example, enter TPM to show a combination of Temperature, Pressure and Mass Flow for the stream. You can use any combination of the following:
T = Temperature
P = Pressure
M = Mass Flow
F = Molar Flow
V = Vapour Fraction
E = Heat Flow
N = Name
Force a resolve of the flow sheet.
Make the PFD active, and press Shift-R, you will see your combination of variables next to the stream.
Note that the order in which you enter the letters determines the order of appearance of the properties.
There are two more detailed settings in the flowsheet user variable itself: currently it is assumed that the numbers are all 8 characters long to get a nice alignment of numbers and units. the variable NbrLength determines this. Currently the space is used to space the variaous letters and numbers. This is the most logical and nicest, but HYSYS has this bad habbit of word wrapping labels, so you may need to pass through the lables and adjust their size to get a proper display. You could change the variable Spacer to something else than a (a _ for example). This avoids the word wrapping, but it doesn't look as nice.
Keywords: user, variable, stream, description, pfd, condition, display
References: None |
Problem Statement: This knowledge base article describes how to use the Aspen Production Record Manager Application Programming Interface (API) to retrieve the characteristic value of a given instance when more than a single instance exists for a given batch. | Solution: There is an optional parameter after the characteristic name which is the instance number of the characteristic.
.characteristics.item(CharacteristicName,[CharacteristicInstance]);
This parameter allows the user to specify a given instance when more than a single instance exists. When this optional parameter is not specified the data for the first characteristic instance value is returned. If a negative value for the instance number is supplied then the characteristic value corresponding to the largest instance will be returned.
The following example illustrates how to specify the instance number when retrieving a characteristic value. The lines of the code and output where the instance number is specified and returned are highlighted in red.
The following code:
local data_sources, batch, myarea, myquery, batchlist, i int;
local StartTime timestamp, EndTime timestamp;
data_sources = createobject('AspenTech.Batch21.BatchDataSources');
write 'DATA SOURCE NO: ' || data_sources('hklap').Areas.Count;
myarea = data_sources('hklap').areas('sqldemo');
MyQuery = MyArea.BatchQuery;
-- Clear the query.
MyQuery.Clear;
Myquery.CharacteristicConditions.Add('BATCH NO', 1, atEqual, '4147');
batchlist = MyQuery.get;
for I=1 to batchlist.count do
begin
write 'BATCH NO: ' || batchlist(i).characteristics.item('BATCH NO');
write 'START TIME: ' || batchlist(i).characteristics.item('Start Time');
write 'PRODUCT PLANNED: ' || batchlist(i).characteristics.item('PRODUCT PLANNED');
write 'PRODUCT PLANNED: ' || batchlist(i).characteristics.item('PRODUCT PLANNED',2);
write 'PRODUCT PLANNED: ' || batchlist(i).characteristics.item('PRODUCT PLANNED',3);
write 'CHAR: ' || batchlist(i).characteristics.item('CHAR');
exception
write 'No BATCH NO';
end
end
batchlist = null;
batch = null;
Returns the following output:
DATA SOURCE NO: 1
BATCH NO: 4147
START TIME: 21/08/2006 14:02:36
PRODUCT PLANNED: 1
PRODUCT PLANNED: 2
PRODUCT PLANNED: 3
No BATCH NO
The data associated with this batch is as follows:
Keywords: Char
CharInstance
Inst
Batch.21
References: None |
Problem Statement: This knowledgebase article provides an example program which populates a listbox in an Aspen Process Explorer VBForm with the multiple column results of an Aspen SQLplus query. | Solution: The VBA code below calls the following procedure, SelectHistory, to query the SQLplus aggregates table for data. This procedure returns 4 columns of results (avg, min, max & sum.)
Note: In order to call this procedure from a VBA program, the procedure must be saved as a ProcedureDef record.
PROCEDURE SelectHistory
Select avg, min, max, sum from aggregates where name = 'atcai';
END
The VBA program below uses ADO to connect to the InfoPlus.21 database through an Aspen SQLplus ODBC connection. One of the main advantages of storing the actual SQLplus query in a ProcedureDef record is that the 'CommandText' property:
adoCmd.CommandText = selecthistory;
only needs to reference a call to the procedure instead of the full SQLplus query to the aggregates table.
'--------------------
Dim adoCon As New ADODB.connection
Dim adoCmd As New ADODB.Command
Dim adoRS As New ADODB.Recordset
'Will hold concatenated column results
Dim holdme As String
adoCon.Open (YOUR IP.21 ODBC DATASOURCE NAME)
adoCmd.ActiveConnection = adoCon
'Call to the SQLplus procedure
adoCmd.CommandText = selecthistory;
Set adoRS = adoCmd.Execute()
'Clear any contents from the listbox then populate
'the listbox with the query results
ListBox1.Clear
Do While Not adoRS.EOF
holdme = adoRS!sum & : & adoRS!Min
ListBox1.AddItem holdme
adoRS.MoveNext
Loop
adoCon.Close
'----------------
Keywords:
References: None |
Problem Statement: No user - whether or not an administrator - can login to Aspen Collaborative Forecasting (CF).
Getting the following error: | Solution: The user that had this error had Swedish as the language set in the Control Panel.
Officially, CF does not support Swedish language.
The CF create_schema or cf_republish will not work in this case.
TheSolution is then to switch language in the Control Panel | Regional and Language Options to a supported localized language, for example to US English.
CF is also localized in Chinese and Japanese.
Keywords: Collaborative Forecasting
Server Error
Unexpected condition
Fulfilling your request
Please notify the administrator
Language
International
References: None |
Problem Statement: Can I tell if any of the variables in a stream are imported into / exported from a spreadsheet? | Solution: If any of the variables in a stream is an imported variable in a spreadsheet then the Logical Ops table on the Attachments tab ... Unit Ops page of the stream window will show the spreadsheet name and cell reference. (This table also shows the connections to any other logical ops. E.g. Sets, Adjusts ...)
If any of the variables in the stream is exported from a spreadsheet then if you hover over the variable value the yellow tool tip will indicate which spreadsheet and cell reference is setting the value.
Keywords: Spreadsheet, Import, Export, Attachments, Logical Ops
References: None |
Problem Statement: How can I change the number of columns displayed in the Workbook? It is difficult to compare certain stream variables as Hysys wraps the columns depending the size of the workbook window. | Solution: Uncheck the Horizontal Matrix checkbox at the bottom of the workbook window. This will transpose the columns and turn off the column wrapping.
Keywords: Workbook, columns, wrapping
References: None |
Problem Statement: What does ActiveObject refer to? | Solution: The meaning of the object ActiveObject depends on what kind of User Variable / User Unit Operation you are writing:
Unit Op User Variable: ActiveObject = Object variable for whatever kind of operation the user variable is associated with (eg Template = TemplateOp type object, Separator = Separator, ....)
Stream User Variable: ActiveObject = ProcessStream type object
Flowsheet User Variable: ActiveObject = FlowSheet type object
Simulation Case User Variable: ActiveObject is not defined
In all cases the object ActiveCase can be used to return a SimulationCase object for the active case.
What about User Unit Operations?
ActiveObject is an object of type UserUnitOp which refers to the user unit operation.
The best way to see the properties and methods associated with any of these object types is to use the Object Browser included in Microsoft Office. [Go to Tools ... Macro ... Visual Basic Editor. This launches the VBA editor. Go to Tools ...
Keywords: ActiveObject, ActiveCase, User Unit Operations
References: s and then check the HYSYS Type library. Now choose HYSYS in the top left hand drop down box, a list of all the available HYSYS object types should now be visible at the bottom left of the screen.] |
Problem Statement: How do I get rid of the Tray sizing message that asks me if I want to use the vapour leaving tray_ instead? | Solution: On the Design Setup page of the tray sizing utility there is a drop down menu that is by default set on Ask each time. Change it to Always Yes or Always No to avoid the message coming up. Or put your utility on Ignore.
Keywords: vapour to size, tray sizing, column sizing, message
References: None |
Problem Statement: If I have a requirement to have Windows Authentication functionality for the admin users to log into Aspen Collaborative Forecasting, how is this possible? | Solution: We don?t have CF authentication functionality developed for CF admin application at present; this comes under enhancement category. We already had CQ00432963 logged under this category and this CQ deferred until CF 9.0 release.
Keywords: None
References: None |
Problem Statement: Automation example - Creating a case from scratch | Solution: The example code below illustrates this. To use the code: open up HYSYS, paste the code into the VBA editor in Excel, set the code to reference the required case file name, make a reference to the HYSYS type library (Tools ...
Keywords: None
References: s menu option in the VBA editor) and run the procedure. For troubleshooting advice on common HYSYS / OLE Automation errors see Knowledgebase |
Problem Statement: In some of the Logical Operation variable navigators (eg the Set, Adjust and Spreadsheet operations) I see many variables starting with a 'BO' prefix. What does this mean? | Solution: The 'BO' abbreviation within HYSYS stands for Black Oil, the new property package (created by Neotec) offered as an option for Upstream applications. The 'BO' prefix is used because many variables are only specific to this property package.
Keywords: BO, Black Oil, Logical Operation, Set, Adjust, Spreadsheet,
References: None |
Problem Statement: You would like to have multiple instances of Collaborative Forecasting (CF) on one server. | Solution: Please follow these steps in order to create a multi-instance environment.
1. Install BEA Weblogic 10.0 as default configuration.
2. Install CF as default configuration.
3. Check the CF. Entry http://localhost:7001/cf
4. Generate a new domain for another CF.
4.1. Click the menu 'BEA Products -> Tools -> Configuration Wizard'.
4.2. Select 'Create a new Weblogic domain'. Then click 'Next'.
4.3. Use the default configuration. Then click 'Next'.
4.4. Entry the User name and User password. Then click 'Next'.
4.5. Select the 'Production Mode' and 'Jrockit SDK 1.5.0_06@ C:\bea\jrockit90_150_06'.
Then click 'Next'.
4.6. Keep the default configuration. Then click 'Next'.
4.7. Entry the new domain name. Then click 'Create'.
5. Deploy the CF to new domain.
5.1. Copy the folder applications which is under
5.2. C:\bea\user_projects\domains\AspenCFV72 to C:\bea\user_projects\domains\AspenCFV72_2
5.3. Copy the folders rc, logs and file AeBRSSLM.dll Which are under C:\bea\user_projects\domains\AspenCFV72 to C:\bea\user_projects\domains\AspenCFV72_2
5.4. Copy the file CF jms module-jms.xml which is under C:\bea\user_projects\domains\AspenCFV72\config\jms to
C:\bea\user_projects\domains\AspenCFV72_2\config\jms.
5.5. Open the file config.xml which is under C:\bea\user_projects\domains\AspenCFV72_2\config.
5.6. Add the following xml code blocks between '<configuration-version>10.0.0.0</configuration-version>' and '<admin-server-name>AdminServer</admin-server-name>' xml tag elements in config.xml file
Note: Please make sure that <source-path> element should contains the new domain name (AspenCFV72_2)
5.7. Add the following bellow code blocks between
'<name>AdminServer</name>' and
'<listen-address></listen-address>' tags.
The following code can modify the server port number for new CF domain.
<ssl>
<enabled>false</enabled>
</ssl>
<listen-port>7101</listen-port>
5.8. Test the new domain. Go to 'C:\bea\user_projects\domains\AspenCFV72_2'. Run startWebLogic.cmd.
5.9. Check the CF run on 7101. Entry the http://localhost:7101/cf.
Check the CF run on 7001. Entry the http://localhost:7001/cf.
Two CF apps are running in on weblogic server with different domain.
Keywords: None
References: None |
Problem Statement: How is liquid viscosity calculated for an Oil/Water mixture? | Solution: For V(oil) > 0.5
Mu(m) = Mu(oil) * e^[3.6*(1-V(oil)]
For V(oil) < 0.33
Mu(m) = [1 + 2.5 V(oil) ((Mu(oil) + 0.4 Mu(water))/(Mu(oil) + (Mu(water))] Mu(water)
For 0.33 < V(oil) < 0.5, the viscosity is calculated by a weighted average between the equation for V(oil) > 0.5 and for V(oil) < 0.33:
Mu(overall) = Mu(V(oil)>0.5)*(V(oil)-0.33)/(0.5-0.33) + Mu(V(oil)<0.33)*[1-(V (oil)-0.33)/(0.5-0.33)]
where:
Mu(m) = apparent viscosity of the mixture
Mu(oil) = viscosity of hydrocarbon phase
Mu(water) = viscosity of aqueous phase
V(oil) = volume fraction of the hydrocarbon phase in the blended mixture.
Different from the ordinary mixing rule, especially the one used for V(oil) greater or equal to 0.33, this one takes into consideration the emulsion formed in the blended oil-water mixture. Please refer to the Simulation Basis manual, section A.5.4 for more details.
Keywords: liquid viscosity, two liquid phase, immiscible,
References: None |
Problem Statement: Is Aspen Collaborative Forecasting V7.3 compatible with Windows Server 2008 R2 Datacenter? | Solution: Please review the attached installation guide which documents the supported OS?s for CF V7.3. Windows Server 2008 R2 64 bit is not listed, so officially, this is not supported
Keywords: compatibility
References: None |
Problem Statement: Can I access component compositions by name instead of position? | Solution: When the composition of a ProcessStream or Fluid object is obtained via Automation it returns a Variant array containing the compositions. The array runs from zero to one less than the number of components, where the value at the 0th index in the array is the composition of the first component in the component list and so on.
There is no direct way of accessing the composition of a given component by specifying its name. Instead you need to employ an indirect two-step process. First the position of the required component within the component list is determined, then the value at this position within the array of component compositions is accessed. Attached below is some example code that illustrates this. The dblCompbyCptName() function takes two parameters: an object variable for the stream; and the component name. It returns the molar fraction of that component.
To use the code below open up HYSYS with any case, paste the code into the VBA editor in Excel, set the code to reference a stream within the case and a component, make a reference to the HYSYS type library (Tools ...
Keywords: None
References: s menu option in the VBA editor) and run the procedure.
If you are retrieving the same component's composition many times in the same procedure it would not be very efficient to use this function; since each time it is called it determines the position of the component within the component list. Instead you should determine the components position once at the start of the procedure and then use this position whenever you need a composition.
Sub DemoOfCompbyCptName()
'Declare Variables |
Problem Statement: What does the Calculate with Every Solve option do? | Solution: Calculate with every Solve: This option is only available when Read From Flowsheet and MASSBAL are selected. When this checkbox is enabled, the solver behaves like a regular HYSYS case. That is, if there are changes upstream of the MASSBAL op, then it automatically resolves. With the box disabled, the user is required to hit the Calculate button to get MASSBAL to recalculate each time.
Keywords: MASSBAL, Calculate with every solve
References: None |
Problem Statement: I am trying to regress my own data for a component using tabular package. However, Hysys keeps showing Non-Regressable / Cannot Regress Data message. What does this error/warning message mean? | Solution: HYSYS only has a linear regression tool in the Tabular package. Any equation form, which is either linear or can be converted to a linear form, is considered regressable. For example y = a+bx is a linear equation and y = a*x^b can be converted to a linear equation as lny = lna + blnx. Therefore, they are regressable in HYSYS Tabular. On the other hand, y = a + x^b is not a linear equation and cannot be converted to a linear form, hence, considered non-regressable.
There are over 30 equation forms in HYSYS Tabular, which you can use to regress your data. You can select the equation form from the drop down menu by following these steps as shown the the screen shot attached below:
1. Expand the content on the Information page on the Tabular tab.
2. Highlight the property you would like to regress. The window on the right-hand side will display related parameters for all components involved.
3. Select a component by clicking any cell under its name and press the Cmp. Prop. Detail button to open up the detailed PropCurve view.
4. Select the equation form from the drop down menu on the Variables or Coeff tab page:
If the equation form you have selected (or HYSYS default) is regressable and HYSYS is failing to calculate the coefficients while regressing, HYSYS will display a Can not regress message. In that case, if you have your own coefficients, you can enter them manually on the Coeff tab, after checking Do Not Regress check boxes for the coefficients.
If you do not have the coefficients, try another equation form, which can regress the data. Please note that if you select a Non-Regressable equation form, you will NOT be able to check the Do Not Regress boxes and enter any coefficients of your own.
If you have selected an equation form, which is non-regressable or using which HYSYS is unable to calculate the coefficients, you will not be able to save the case or go to simulation environment, because the component data (in Tabular) are not complete. In that case, you will have to make sure that the data are regressed or Tabular is disabled.
Keywords: Tabular package, non-regressable, Cannot Regress Data
References: None |
Problem Statement: What are the Dynamic Specs? | Solution: These are specs that need to be defined for the pressure solver to work. They are mainly pressure and/or flow specs on boundary streams. Other specs are also needed in most unit operations, but these differ based on the type of operation. For example a compressor needs two dynamic specs (similar to the steady state degrees of freedom), these can be efficiency and pressure rise, or Compressor curves and speed, etc..
Many combinations of Dynamic specs can be used and work, the decision on which to use is case specific and depends on what the model is intended for.
Keywords: Pressure, Flow, Specs
References: None |
Problem Statement: Can I access the Optimiser via Automation? | Solution: The Optimiser does not yet have an object in the HYSYS Object Hierachy so can't be accessed via normal OLE Automation methods. However it can be accessed via a 'Backdoor' variable method.
The attached Excel file contains a VBA macro that will link to the currently open HYSYS case, it allows the Optimiser parameters to be set and the Optimiser to be started and its progress monitored.
The code contained in this file is also attached below.
NB Backdoor methods are only recommended when there is no other alternative, the internal HYSYS monikers may not remain constant between versions so care should be exercised when upgrading.
'Note: HYSYS Type library must be referenced under Tools ...
Keywords: None
References: s
'Require explicit variable declaration
Option Explicit
'API Function Declarations
Private Declare Sub Sleep Lib kernel32 (ByVal dwMilliseconds As Long)
Public Sub AccessOptimiser()
'
'Description: Demonstrates how to access the Optimiser via back door variable methods
'
' NB Backdoor methods are only recommended when there is no other alternative, the internal
' HYSYS monikers may not remain constant between versions
' so care should be exercised when upgrading
'
' Modified from code from MGreaves Incident #411554/H16067
'
'Declare Variables |
Problem Statement: When I tried to re-upload a previously uploaded override file into Aspen Collaborative Forecasting (CF), I received an error message stating the file was uploaded before. | Solution: CF functionality is not designed to support repeated uploading of the same file multiple times due to data integrity constraints.
The user must download the file again by enforcing new override session and creating a new file name. Once the override changes have been made the file can be upload back to CF.
You cannot change the name of a previously downloaded Excel file and upload it again into CF. You must first download from CF, create unique file name, do the overrides, and then upload the file to CF.
Keywords: None
References: None |
Problem Statement: When I import the PIPESYS flow regime variable into the databook or the spreadsheet all I see is a number. What flow regime does this number represent? | Solution: 0 Unknown
1 Elongated Bubble
2 Plug
3 Stratified
4 Wave
5 Slug
6 Annular Mist
7 Dispersed Bubble
8 Single Phase
9 Intermittent
10 Froth
11 Bubble
12 Error
13 Undefined
14 SP-Laminar (single phase - laminar)
15 SP-Transitional (single phase - transitional)
16 SP-Turbulent (single phase - turbulent)
Keywords: PIPESYS, flow regime
References: None |
Problem Statement: How do I determine if an object reference actually points to an object? | Solution: When an object reference is made, the reference may point to an object which does not exist. For example, when FindVariable is used to set an object reference to an object in the EDF. If there is no object (for example, when a feed stream has not been attached), then the reference points to nothing. Use the Is keyword to compare the object reference to Nothing. The following code demonstrates this:
Set hyFeed = hyContainer.FindVariable(FeedStream).Variable.object If hyFeed Is Nothing then Exit Sub
Keywords: Object reference Nothing
References: None |
Problem Statement: When logging into Aspen Collaborative Forecasting(CF) as admin and clicking on tab User manager why am I getting the following error message:
Error 404--Not Found
From RFC 2068 Hypertext Transfer Protocol -- HTTP/1.1: 10.4.5 404 Not Found The server has not found anything matching the Request-URI. No indication is given of whether the condition is temporary or permanent. If the server does not wish to make this information available to the client, the status code 403 (Forbidden) can be used instead. The 410 (Gone) status code SHOULD be used if the server knows, through some internally configurable mechanism, that an old resource is permanently unavailable and has no forwarding address. | Solution: In the CF database; in table cf_user_manager; in manager_id column had values 16,17 and 30 and there are no corresponding user_id?s which exists in cf_user table; this means that there were manager_id?s(16,17 and 30) but not existing user_id?s (Ex: Manager exists without exists as a employee in real life)
User_Manager_id
user_id
manager_id
155
19
30
156
20
30
157
18
30
158
15
30
159
14
30
160
13
30
161
12
30
162
10
30
164
19
16
165
20
16
166
18
16
167
15
16
168
14
16
169
13
16
170
12
16
171
10
16
172
19
17
173
20
17
174
18
17
175
15
17
176
14
17
177
13
17
178
12
17
179
10
17
To resolve this apply the following bellow SQL in Aspen Collaborative Forecasting(CF) database to correct the issue
delete from cf_user_manager a where a.manager_id not in (select b.user_id from cf_user b where b.user_id = a.manager_id)
Keywords: Manageusers
References: None |
Problem Statement: How do two contractors combine their work on a heat exchanger or an air cooler if one has access to the Aspen HYSYS program only and the other has access to the STX or ACX programs only? Is there a way that they can send each other files to be incorporated into the software? | Solution: Yes, there are utility programs created for this reason.
The attached STX or ACX utility program queries a Aspen HYSYS case and writes the HOT and CLD files for any of the exchangers or a HOT file for any of the coolers in the case. As there is no need for HYSYS-STX Link to use it, anyone with Aspen HYSYS can create the HOT and CLD files even if he doesn't have STX or ACX.
NOTE: The ACX utility program does not recognize air coolers in a Aspen HYSYS case as the Air Cooler icon is a new feature that was added to Aspen HYSYS after this utility was created. Therefore, if the data of an air cooler is needed to be transferred to ACX, a dummy cooler should be created for this purpose.
Keywords: Link, Heater
References: None |
Problem Statement: Does Aspen HYSYS support CAPE-OPEN Thermo 1.1 interface standards? | Solution: New in Aspen HYSYS 2006.5, the new CAPE-OPEN Thermo 1.1 interface standards are supported. This support includes both plug and socket capabilities; namely a CAPEOPEN Thermo 1.1 property package can be exported from Aspen HYSYS so that it can be used in any 3rd party CAPE-OPEN Thermo 1.1 compliant Process Modeling Environment (plug) and any CAPE-OPEN Thermo 1.1 property package can be used in Aspen HYSYS for process calculations (socket). As with version 1.0 of the CAPE-OPEN Plug, the 1.1 CAPE-OPEN Plug uses Aspen COMThermo as the physical property engine.
Note that the CAPE-OPEN Thermo 1.0 interface continues to be supported in Aspen HYSYS 2006.5.
Keywords: CAPE-OPEN, thermo, interface, standard, standards
References: None |
Problem Statement: I am upgrading HYSYS to a new version. I have property correlation sets defined and saved in the current version and I don''t want to lose them after the update. How can I migrate the correlation sets to the new version for reuse? | Solution: Property correlation sets are saved in an XML file named CorrelationSets.xml in HYSYS 3.1 or StreamCorrSets.xml in HYSYS 3.2 and 2004. The file is located in the HYSYS Support directory. If you have a new version of HYSYS installed, the file will not exist until you actually save a set.
To migrate the property correlation sets used in the old version of HYSYS to the new version, you need to copy and paste the XML file to the Support directory for the new version of HYSYS. If you copy the file from version 3.1 to version 3.2 or 2004, remember to change the file name from CorrelationSets.xml to StreamCorrSets.xml. The correlation sets saved in the file are now available for reuse in the new version.
For information on how to apply a correlation set to streams, please refer to the Correlation Manager section of the HYSYS User Guide.
Keywords: Property Correlation Set, Correlation Manager, Migration Issues
References: None |
Problem Statement: Why does my Automation code fail when I try to link to PFD objects I have just created?
If you use code like:
Set hyPfditem = hyPfditems.Item(An Object Name)
to link to a stream or operation that you have just added to a case, then your Automation code may fail with an error code -2147467259. | Solution: This is because each time any objects are added to the PFD, HYSYS then redraws it. If code tries to link to a PFD object before HYSYS knows where it is then an error occurs.
The way to prevent this is to check for this error, and if it occurs to wait and try again until an object is successfully obtained. The following sub procedure does this:
Private Sub GetPFDItem(ByVal strName As String, ByRef hyPFDitems As HYSYS.PFDItems, ByRef hyPFDitem As HYSYS.PFDItem)
'Returns the named item from the collection hyPFDitems into object hyPFDitem
'Normally this can be done just by using Set hyPFDitem = hyPFDitems.Item(Name)
'However this line can cause a runtime error -2147467259 if HYSYS is still redrawing the PFD
Dim intCount As Integer
intCount = 0
On Error Resume Next
Set hyPFDitem = Nothing
'Ensure code doesn't go on looping forever
Do Until intCount > 25
'If HYSYS hasn't finished redrawing the PFD then this line can cause an error
Set hyPFDitem = hyPFDitems.Item(strName)
'If now got the item then get out of this procedure
If Not hyPFDitem Is Nothing Then Exit Sub
'Wait 50 ms by using the API Sleep function
Sleep 50
intCount = intCount + 1
Loop
End Sub
In order to use the Sleep API function, the following line must be placed in the Declarations section of the code module:
Private Declare Sub Sleep Lib kernel32 (ByVal dwMilliseconds As Long)
The code below illustrates how the GetPFDItem() procedure could be used. For more basic information on manipulating PFD objects seeSolution #112354.
Private Sub DemoGetPFDItem()
'HYSYS Type Library reference required
Dim hyApp As HYSYS.Application
Dim hyFlowSht As HYSYS.Flowsheet
Dim hyCase As HYSYS.SimulationCase
Dim hyPFD As HYSYS.PFD
Dim hyPFDitems As HYSYS.PFDItems
Dim hyPFDitem As HYSYS.PFDItem
Dim hyBD As HYSYS.BackDoor
Dim hyStream As HYSYS.ProcessStream
'Link to objects - visible ops (and streams) collection of active PFD of main flowsheet of active case
Set hyApp = GetObject(, HYSYS.Application)
Set hyCase = hyApp.ActiveDocument
Set hyFlowSht = hyCase.Flowsheet
Set hyPFD = hyFlowSht.PFDs.ActivePFD
Set hyPFDitems = hyPFD.Items(pfdOperation, pfdVisible)
'Make sure the PFD is showing - if this is not done the following two code sections will fail
'(SeeSolution 112359 for full details of this workaround)
Set hyBD = hyFlowSht
hyBD.SendBackDoorMessage CreatePFDAndView
'Create a new stream
Set hyStream = hyFlowSht.MaterialStreams.Add(New Stream)
'Link to it
GetPFDItem New Stream, hyPFDitems, hyPFDitem
'Could have used
'Set hyPFDitem = hyPFDitems.Item(New Stream)
'but this might have failed if HYSYS was still redrawing the PFD
End Sub
Keywords: Automation PFD Error -2147467259
References: None |
Problem Statement: How do I update or create a sales profile in Aspen Collaborative Forecasting? | Solution: You must update / add to the subroles.txt file. The subrole.txt file defines sub-roles and the attribute values associated with each one. This file consists of four columns, which you populate as follows:
1) Sub-role Code: Can be any desired text
2) Sub-role Description: Can be any desired text
3) Attribute set name in DM: The attribute set for which you are creating sub-roles.
4) Attribute value: An entry from the attribute set listed in the previous column. This entry specifies an attribute value which the current sub-role can access.
Example:
This example defines three sub-roles: See screen shots below:
1 JONESM
2 SMITHJ
3 EPS
The JONESM and SMITHJ sub-roles can each access one attribute value from the REP set. The EPS sub-role can access five attribute values from the REP set.
NOTE: All value entries must be valid. I.e.- in order to assign a value it must be a valid entry in the attribute table. If you do not use a valid attribute and attempt to upload the new subrole, it will fail.
Keywords: sub-role, update sales profile, attribute
References: None |
Problem Statement: Can I use Automation to access user variable values? | Solution: The .GetUserVariable method of the ProcessStream object can be used to access a user variable attached to a stream. Simply pass the user variable Tag as a parameter, and take the Variable property to return a Real Variable object. The user variable Tag is entered on the user variable code editing window and can be different to the name.
For example, paste the following code into Excel's VBA editor, set a HYSYS type library reference, and press the Run button. It links to a user variable with tag MyUV on stream Example Oil that has temperature units.
Private Sub GetUserVariable()
'Description: Uses the GetUserVariable() method of the stream to return a Real Variable
' for a user variable attached to the stream
'Declare Variables
Keywords: None
References: None |
Problem Statement: I get Windows Installer Error 1406 when installing the application. What do I do? | Solution: Error 1406 results from a problem with the Windows Installer Service, a Microsoft Windows feature involved with program installation. The best wyay to solve this problem is to download version 2.0 of the Windows Installer Service.
For Windows 95 & 98 machines, go to: http://www.microsoft.com/downloads/details.aspx?displaylang=en&FamilyID=CEBBACD8-C094-4255-B702-DE3BB768148F
For Windows NT 4 & 2000 machines, go to: http://www.microsoft.com/downloads/details.aspx?displaylang=en&FamilyID=4B6140F9-2D36-4977-8FA1-6F8A0F5DCA8F
Click on the *.exe file you downloaded from the Microsoft website to run it. After the Windows Installer Service installation is complete, try re-installing Ground Loop Design.
Usually this problem occurs during the installation of the Sentinel System Driver. Just click on Ignore when this message comes up and the installation will re-start itself. You may have to click on Ignore a second time if the message comes up again. The installation should then proceed to completion.
For more information about this error, please refer to the following website: http://support.installshield.com/error_central/
Keywords: Error 1406; installation error 1406; installation error; windows install error;
References: None |
Problem Statement: Aspen Collaborative Forecasting (CF) offline loading may take a long time if the file is large and possibly could return with a Weblogic Server Error. | Solution: The default transaction timeout in Weblogic server is 30 seconds. This may be changed to 90 seconds as a recommendation.
1. Login to Weblogic Admin tool:
http://<yourHost>:<yourPort>/console
Login/password as what you saved them to be when you created the domain. (This has nothing to do with CF and is configured when you installed Weblogic.)
2. In the Admin page, on the left navigation panel, click: Services ->JTA, and the transaction timeout is shown as follows:
Change the value in seconds and Apply. This setting is saved permanently.
Keywords: Weblogic 8, 9, 10
Transaction Timeout
Collaborative Forecasting (CF)
Java Transaction API (JTA)
References: None |
Problem Statement: Any roles that are set up manually in Aspen Collaborative Forecasting (CF) get deleted from CF by the next publish/republish from Aspen Demand Manager (DM). | Solution: This is indeed working as designed. In the 2006.1 release, any roles that are set up manually in CF and are not set up in DM get deleted from CF by the next publish/republish from DM.
This is a different behavior from previous versions. Previously roles could be manually set up in CF and they would persist after a publish/republish even if they were not setup in DM.
Therefore, theSolution is to make sure that CF roles are also added in DM. In fact each repub shall synchronize roles configured in DM and those in CF. Any role created in CFAdmin but absent from DM will be wiped out upon repub.
This synchronization was not controlled in previous version (e.g. 2006) as it is now controlled in 2006.1. Any role created in CFAdmin must exist in DM. If you need a new role, first define it in DM, then create it in CFAdmin. It will persist upon repub.
Keywords: REPUBLISH
PUBLISH
ROLES
DISAPPEAR
DELETED
References: None |
Problem Statement: How can I use my favorite Workbook setting for all of my simulation cases? | Solution: Once you have setup the Workbook the way you want for one simulation case file, you don't have to do it again for other cases. All you need to do is to save this setup and use it repeatedly for other cases. Here is the procedure to follow:
Open the case file with your favorite Workbook setting. Let's call it case A.
Make sure the Workbook view is active. If not, press Ctrl-W to Open/View it.
From the top menu bar, select Workbook and then Export.
Provide a name for the .wrk file and save it.
Open the case file where you want to use the same Workbook setting. Let' call it case B.
Again, make sure the Workbook view is active. If not, press Ctrl-W to Open/View it.
From the top menu bar, select Workbook and then Import. It will bring the same Workbook format you have in case A into case B.
Keywords:
References: None |
Problem Statement: How do I set up a Fired Heater in dynamics? | Solution: Typically the hardest part when setting up a fired heater in HYSYS dynamics is to get the operation to initialize on the first integration time step. The procedure outlined below will help ensure that the fired heater will initialize. Since the fired heater operation is for dynamics only, it is assumed that all the steps below are followed after the case has been switched to dynamics mode. It is expected that valves, controllers and other ancillary equipment required will be added after the fired heater has initialized and been run for several time steps.
Additional information on the theory used for the fired heater can be found in the Heat Transfer Equipment section of the HYSYS Operations Guide.
Create all the streams that will be attached to the heater first. If the desired feed streams already exist in the simulation these may be used. It is recommended however to create new process streams and leave them disconnected from the main process as the fired heater will go through an initial transient period as it heats up. Feed and product streams include: all process streams connected directly to the fired heater in the radiant zone, convective zone, and economizer zone, the fuel/fresh air stream and flue gas stream. The number of process streams required will depend on the number of external passes connected to each zone.
For all product streams initially use a dynamic pressure specification. If the feed stream is a boundary stream (only attached to the furnace) a flow specification should be used.
Product streams do not need to be initialized with expected values. The default values provided by HYSYS for composition, flow and pressure are acceptable; only pressure needs to be specified. If adding the fired heater in steady state mode you will need to ensure that the product streams have fully solved before switching to dynamics.
Ensure that the air contains oxygen and nitrogen components. Do not use the HYSYS Air component.
Ensure that the fuel gas stream contains HYSYS library components of type CxHy.
The fresh air stream and fuel gas stream need to be mixed into a single stream which will be attached to the fired heater.
Install the fired heater. From the Design tab, Connections page of the fired heater enter the number of external passes for each zone and attach the required feed and product streams created in the first 4 steps. If a zone is not used enter zero (0) for the number of external passes. The number of external passes per zone should match the number of process feed and product streams created in step 1. Note: Once any streams have been connected to the fired heater if the number of external passes is changed it may be necessary to delete the fired heater and add a new one.
On the Ratings tab, Sizing page ensure that all the physical sizing information for the three zones is entered. Data can be entered for the three zones by using the radio button at the top of the page to switch zones. As a first guess the default data supplied by HYSYS can be used, however you need to check that the total volume of the tubes is less than the total volume of the shell. If using multiple external passes it is possible the default HYSYS tube values will produce a tube volume larger than the shell volume. If the tube volume is larger than the shell volume the fired heater will not initialize and run in dynamics.
On the Ratings tab, Heat Transfer page ensure that all the heat transfer information for each external pass for the three zones is entered. As a first pass the default values provided by HYSYS can be used and then tuned to match actual temperature profiles.
On the Dynamics tab, Tube Side PF page enter the expected fixed pressure drops or size the k values for each external pass. As a starting point either fixed pressure drops or k values are acceptable, however, once the fired heater has started running and temperatures have stabilized fixed pressure specifications should be replaced with k value specifications for more realistic pressure/flow behaviour. Ensure that the Use Delta P or Use K's boxes are checked, depending on which method is used.
On the Dynamics tab, Flue Gas PF page enter the expected fixed pressure drops or size the k values for each zone. Ensure that the Use Delta P or Use K's boxes are checked, depending on which method is used.
The fired heater should now be ready to run in dynamics. If when the integrator is started the fired heater fails to initialize, go back and make sure all the information is entered from steps 6, 7, 8, and 9. Please note that if the number of external passes for any zone was changed after any streams were connected to the fired heater it may be necessary to delete the fired heater and start over from step 5.
Once the fired heater has been run for several time steps additional fidelity can be entered:
If fixed delta P specs (tube and flue side) were initially used, these should be changed to 'k' value specs and 'k' reference flows added.
Fixed heat transfer coefficients can be changed to scaled values and reference flows added.
Valves added (with controllers as required) so as to remove the fixed flow specifications from feed streams.
Additional air side equipment as required.
When adding additional equipment try to ensure that the original streams connected to the fired heater are not disconnected as this may cause the fired heater to fail and require a new heater to be installed.
Keywords: Fired heater, dynamics
References: None |
Problem Statement: Can I bring an open case to the front within HYSYS using OLE Automation? | Solution: In the HYSYS interface if a case is open but not showing, it can be activated (brought to the front) by using the Load Workspace option on the Window menu. It is also possible to activate the case through OLE Automation.
The Excel VBA code below illustrates a function that will activate (i.e. bring to the front within HYSYS) a particular case.
To use the code open up HYSYS with any case, paste the code into the VBA editor in Excel, make a reference to the HYSYS type library (Tools ...
Keywords: None
References: s menu option in the VBA editor), change the case name and path as appropriate and run the procedure.
Public Sub CaseToFrontContainer()
BringCaseToFront C:\Program Files\Hyprotech\HYSYS 3.2\Samples\G-1.hsc
End Sub
Private Function BringCaseToFront(ByVal strCaseName As String) As Boolean
'
'Description: Links to the currently active HYSYS instance and brings the specified case to the front
' Returns True if the case was found and activated, False if not
'
'Declare Variables |
Problem Statement: Can Aspen HYSYS calculate the Methane Number of a stream? | Solution: Aspen HYSYS has no built in feature to calculate the Methane Number of a stream. The user should use a spreadsheet to calculate the methane number from an appropriate equation. If you want to calculate this number for many streams in a simulation, we would recommend programming a user variable for it (seeSolution ID 111460 for some training on how to program a user variable).
You can find an equation to calculate the Methane Number at the following internet address:
http://www.arb.ca.gov/regact/cng-lpg/appd.PDF
However, you might want to do a search of your own to determine what equations would be best to calculate the methane number for your streams.
Keywords:
References: None |
Problem Statement: Why is mixer outlet stream temperature higher (or lower) than the maximum (or minimum) of its inlet streams temperature, even when all the inlet and outlet streams are at the same pressure? What did I do wrong or is it a bug in HYSYS? | Solution: The mixer outlet stream temperature can be higher (or lower) than the maximum (or minimum) of its inlet streams temperature depending on the phase equilibrium achieved after mixing the inlet streams i.e. the distribution of components in different phases at the given conditions or, in other words, on the composition, temperature and the relative flowrates of inlet streams, at a given pressure of all the streams. Normally the observation has been made for systems with Hydrogen and Helium component involved.
Please see the attached HYSYS 3.0.1 cases. In one case, the mixer outlet temperature is higher than the maximum of the inlet streams temperature and in the other, the mixer outlet stream temperature is lower than the minimum of the inlet streams temperature.
In the case mixer-HIGH-OUTLET, pure n-Butane (only vapor) is mixed with pure n-Decane (only liquid) at the same pressure. If you look at the outlet stream (two phase) composition of liquid and vapor phases, you will see that vapor phase (still) has mainly n-Butane (mole fraction: 0.9958) with some n-Decane and n-Butane's mole fraction in liquid phase is 0.266. This means that some n-Decane has vaporized (absorbing heat) and some n-Butane has condensed (releasing heat). The final equilibrium temperature will depend on the relative amounts of different components being vaporized /condensed and their heat of vaporization.
Heat of mixing of components may also have some effect on the equilibrium temperature.
Keywords: Mixer outlet temperature
References: None |
Problem Statement: How can I model a total condenser with a water (or second liquid) draw stream? The only condenser with two liquid outlets available on the object palette of the Column Environment is a 3-phase condenser which also has a vapour outlet stream. | Solution: A total condenser with a water draw can be modelled simply by using a 3-Phase Condenser and leaving the Vapour connection empty. The attached HYSYS 3.2 case (a modification of the R-1.hsc sample case) shows this.
This approach can be useful if you have a total condenser with two liquid outlets and you want to use the Subcooling option (on the Design\Subcooling page of the column properties view). The reason is that subcooling is not supported if there is a nonzero vapour flow and a very small (but nonzero) vapour flow can arise even with appropriate column specifications due to the solver tolerances.
Keywords: total condenser, water draw, two liquids, subcooling, 3-phase condenser
References: None |
Problem Statement: How do I load the subrole file?
If this file is not loaded correctly you may have problems like some particular users not seeing any data in the View Data filters tab, as shown in the picture below: | Solution: In theory there are two ways available to load the subrole file (subrole.txt):
1. Using the CFAdmin user interface (UI)
2. From the DOS command line, via CF Integration
Due to some stability issues, it is advisable to stop using the CFAdmin UI to load the subrole file. The only way to load it should be via the DOS command line in CF Integration.
Here are detailed steps on how to load subrole.txt via CF Integration:
1. Verify the file's location and name
File name: subrole.txt
File location: <CF_INTEG>\dm\control
Note: It is advisable to always make file extensions visible in Windows Explorer (Tools menu | Folder Options... | View tab | Hide extensions for known file types setting unchecked)
2. Open a DOS prompt (Start | Run... | type command CMD) then change directory to the <CF_INTEG> folder
3. Type the following commands:
intra_repub control
return
Keywords: roles
subroles
empty
filter
References: None |
Problem Statement: Two distinct liquid phases (liquid and aqueous) are sometimes observed for lower concentrations of TEG in water when using the PR property package in HYSYS. | Solution: The interaction parameters for TEG and water in the PR and PRSV property packages are based on data from the Union Carbide glycol handbook at 1 atm. Although the entire composition range was used in the fit, these Property Packages are more applicable to higher glycol concentrations (glycol > 80 mass%) and higher temperatures. At lower glycol concentrations (< 80 mass%), phase splitting is sometimes observed with PR property package - this phase splitting is likely caused by the model and not a reflection of what happens in practice.
If this problem happens in a TEG regenerator, you can select No 2 Liquid Check for the Two liquids Check Based On field (Column Property View, Parameters tab, Solver page).
Alternatively, PRSV or NRTL can be used when the concentration of TEG is lower than 80 mass%. With NRTL however, the missing LLE interaction parameters must be provided or estimated by UNIFAC and as always, validation is required to ensure that the estimated parameters give realistic results.
Keywords: TEG, glycol, water, mixture, concentration, composition, phase, liquid, split, splitting, flash, stability, aqueous, separate, distinct, property package, PR, PRSV, NRTL.
References: None |
Problem Statement: How do I deal with multiple open cases / opening cases / closing cases via Automation? | Solution: The HYSYS Application object has an ActiveDocument property which gives a SimulationCase object for the currently active case in HYSYS (i.e. the one being displayed within the program). The SimulationCases property of the Application object gives access to a VB collection of all the currently open cases within HYSYS. You can also open any other cases by using the Open method of the SimulationCases object. To close an open case use the Close method of the SimulationCase object for that case.
Once the required case has been accessed, via the ActiveDocument property or via the SimulationCases collection, it can then be used as a top level object for all the other objects within the case. For example hyCase.Flowsheet.MaterialStreams gives access to a collection of all the Material streams in the main flowsheet.
The following VBA code example gives a procedure that will check whether HYSYS already has a particular case open. If it's the currently active one then it just displays a message to that effect, if it's open but not currently active then it asks the user if they want to reopen the file from disk, if it's not open then the file is opened. This illustrates most of the relevant properties and methods in this area.
To use the code below: open up HYSYS, paste the code into the VBA editor in Excel, set the code to reference to the required case name (strCaseFN = ...), make a reference to the HYSYS type library (Tools ...
Keywords: None
References: s menu option in the VBA editor) and run the procedure.
Public Sub OpenCase()
'
'Description: Attempts to open a specified HYSYS case
'
'Declare Variables |
Problem Statement: When using the OLI property package, the solid unit operations palette is all greyed out, except for the simple solid separator. | Solution: This is a limitation of the OLI package, it does not currently support the solid unit operations' functionality (other than the simple solid separator). Until this functionality is added, you must use a subflowsheet approach, where the subflowsheet has a different simulation basis than the main environment. The solid unit operations can then be added to the subflowsheet.
Keywords: solid, OLI, rotary filter, cyclone, hydrocyclone, rotary vacuum filter, baghouse filter.
References: None |
Problem Statement: Do we have any report or interface in Aspen Collaborative Forecasting (CF) to find out how many users performed Forecast Signoff during a forecast horizon? | Solution: We don't have any report or interface in CF to view how many users performed forecast signoff. The only available option is manually querying CF database table.
I.e. someone who acts as administrator would able to query against Collaborative Forecasting database using CF_Forecast_SignOff table.
Keywords: forecast
CF_Forecast_SignOff table
forecast horizon
users
References: None |
Problem Statement: I presently have two roles in Collaborative Forecasting (CF), Sales and Admin, which write to two different data sets; Sales writes to Sales Rep Forecast data set and Admin writes to Admin Forecast data set. I would like to add a third role, Forecaster, and have that role write to the Sales Rep Forecast data set. | Solution: There can be multiple data sets and roles established in Demand Manager/Collaborative Forecasting but a user can only have one of these roles and that one role can only write to one data set. A user cannot have multiple roles, thus he cannot write to multiple data sets.
For example; in the standard CAP case for CF there are 3 roles, Sale Rep, Customer, and Admin. A user can only have one of these roles. A role writes to a data set, for example the role Sales Rep writes to the Sales Rep data set, and the Customer role writes to the Customer data set. So 1 role, 1 data set.
If you want to create a new role, you will have to create a new data set for that role.
Keywords: CF
DM
References: None |
Problem Statement: Can I access the Stream Description property via OLE Automation? | Solution: Yes, the Stream Description property (on the Worksheet / Notes page of material streams in HYSYS 3.2+) can be accessed via Automation, however not yet via a standard property of the ProcessStream object. Currently the only way to retrieve the stream description is via a Backdoor method, this is illustrated in the VBA code below. Backdoor methods allow access to features not yet wrapped for access by normal OLE methods.
Public Sub GetStreamDescription()
Dim hyApp As HYSYS.Application
Dim hyCase As HYSYS.SimulationCase
Dim hyStream As HYSYS.ProcessStream
Dim hyBD As HYSYS.BackDoor 'Must be of type Backdoor, Object is not good enough
Dim hyDesc As HYSYS.TextVariable
Dim strStrmDescription As String
'Link to the currently active document within HYSYS
Set hyApp = GetObject(, HYSYS.Application)
Set hyCase = hyApp.ActiveDocument
'and a named stream on the main flowsheet
Set hyStream = hyCase.Flowsheet.MaterialStreams.Item(Feed)
Set hyBD = hyStream
Set hyDesc = hyBD.BackDoorVariable(:Notes.401).Variable
strStrmDescription = hyDesc.Value
MsgBox strStrmDescription
End Sub
For an example of this being used in practice see KnowledgebaseSolution 112556 where a HYSYS user variable is used to allow multiple stream variables to be displayed on the HYSYS PFD. See alsoSolution 109203 which describes how Object notes can be accessed via OLE Automation.
Keywords: Stream Description, Backdoor
References: None |
Problem Statement: How do I fix the File Not Found error when installing Oracle for Aspen Collaborative Forecasting?
File not found C:\app\Administrator\Products\11.2.0\dbhome_1\oc4j\j2ee\oc4j_applications\applications\em\em.ear. File not found | Solution: This problem is caused when you are not using the Oracle CD, but instead are using two .zip files. When you unzip the archives, you must ensure they are unzipped into one folder before installation is started. Example: Unzip files into c:\oracle\database as opposed to c:\oracle\part1\database and c:\oracle\part2\database.
Keywords: None
References: None |
Problem Statement: How to model a vertical vessel with weir in dyanmics? | Solution: Horizontal separators have the option of a weir, unfortunately vertical ones don't. Although vertical separators with weirs are not common, weirs and partitions are more common in column sumps, which are modeled as vertical separators in HYSYS. This article is intended to show you how to model a separator with weir using some simulation tricks that were used before the weir option was added in HYSYS. The method described here works for both vertical and horizontal separators.
In future versions of HYSYS this functionality will be implemented within the separator operation. For versions 3.2 and earlier, read the attached document and see the sample cases.
Keywords: separator, weir, wier, vertical, horizontal, how, hysys, works, dynamics, francis, abouelhassan
References: None |
Problem Statement: Why am I getting a consistency error when I specify the inlet distribution parameters for the Horizontal Vessel Carry Over Correlations? | Solution: When specifying the d95 inlet distribution parameters you are only required to specify the following parameters: Inlet droplet, Light Liquid in gas, Heavy Liquid in gas, Gas in Light Liquid and Gas in Heavy Liquid. The Heavy Liquid in Light Liquid and Light Liquid in Heavy Liquid are calculated by HYSYS using the following method.
First the amount of water that is in the stream is determined from:
Water% = WaterFlow / (OilFlow + WaterFlow)
If water is the continuous phase then:
Water in Oil = Inlet Droplet * (WaterDensity / OilDensity)^0.6 Oil in Water = Inlet Droplet
If water is not the continuous phase then:
Water in Oil = Inlet Droplet
Oil in Water = Inlet Droplet * (OilDensity / WaterDensity)^0.6
Keywords: d95, Inlet Distribution Parameters, Real Separator
References: None |
Problem Statement: What does the RTI Server do? | Solution: Beginning with HYSYS 3.0, the RTI Server can be used for case linking and collaboration.
Multiple HYSYS Cases can now be linked across multiple machines on a LAN or WAN. This is accomplished by linking the appropriate streams in a case with the streams of other cases. These links can be Live which means changes in the source stream are immediately and automatically transferred to the destination stream. Alternatively, the source stream changes can be manually transferred to the destination stream when the user requires the new information.
This new capability relies on the use of the Run-Time Integration (RTI) Server which is installed with HYSYS 3.0. The RTI Server is the conduit through which the linked streams exchange data. Large plant wide HYSYS cases can now be broken into smaller, more manageable cases and distributed to the engineers with expertise on the individual plant units. The entire model can then be linked together at the appropriate time to see the overall effect of the unit changes.
Keywords: RTI Server, Case Collaboration, Case Linking
References: None |
Problem Statement: In Aspen Collaborative Forecasting (CF) User Manager, there is an issue with user id being deleted when user manager is deleted. The following script is being used to create user_manager table.
CREATE TABLE ASPENCMCM.CF_USER_MANAGER
(
USER_MANAGER_ID NUMBER(10),
USER_ID NUMBER(8) NOT NULL,
MANAGER_ID NUMBER(8) NOT NULL,
TIME_STAMP DATE DEFAULT sysdate
)
TABLESPACE CFDATA01
PCTUSED 0
PCTFREE 10
INITRANS 1
MAXTRANS 255
STORAGE (
INITIAL 64K
NEXT 1M
MINEXTENTS 1
MAXEXTENTS UNLIMITED
PCTINCREASE 0
BUFFER_POOL DEFAULT
)
LOGGING
NOCOMPRESS
NOCACHE
NOPARALLEL
MONITORING;
CREATE OR REPLACE TRIGGER ASPENCMCM.cf_user_manager_id_gen BEFORE INSERT ON ASPENCMCM.CF_USER_MANAGER for each row
begin select cf_user_manager_id.nextval into :new.user_manager_id from dual; end;
/
ALTER TABLE ASPENCMCM.CF_USER_MANAGER ADD (
PRIMARY KEY
(USER_MANAGER_ID)
USING INDEX
TABLESPACE CFDATA01
PCTFREE 10
INITRANS 2
MAXTRANS 255
STORAGE (
INITIAL 64K
NEXT 1M
MINEXTENTS 1
MAXEXTENTS UNLIMITED
PCTINCREASE 0
));
ALTER TABLE ASPENCMCM.CF_USER_MANAGER ADD (
CONSTRAINT CFC_UMU_R_U
FOREIGN KEY (USER_ID)
REFERENCES ASPENCMCM.CF_USER (USER_ID)); | Solution: You are missing one more important constraint on CF_USER_MANAGER table and needs to be added to resolve the issue.
ALTER TABLE ASPENCMCM.CF_USER_MANAGER ADD (
CONSTRAINT CFC_UM_MGR_R_U
FOREIGN KEY (MANAGER_ID)
REFERENCES ASPENCMCM.CF_USER (USER_ID) ON DELETE CASCADE ENABLE);
The problem was caused due to the Alter statement which was ran below. It is highly advised you do not perform any backend database updates / alterations, inserts, etc as you can cause problems such as what you are seeing.
It should look like this:
Keywords: None
References: None |
Problem Statement: What does Aspen HYSYS do with the reference flows on the Dynamics tab | Model page of the Heat Exchanger? | Solution: The reference flows are used to change the actual UA value of the heat exchanger. The change follows a power law equation:
UAdynamic = F * UAsteadystate
Where:
UAsteadystate = the UA value entered on the Parameters page of the Design tab.
F = (2 f1 f2) / (f1 + f2)
where:
f1 = (mass flowrate / reference flowrate) ^ 0.8 (for fluid 1)
f2 = (mass flowrate / reference flowrate) ^ 0.8 (for fluid 2)
Note that if you leave the reference flow blank, no scaling is done. That is, the UA remains constant (= steady state value).
Keywords: reference flows; UA scaling
References: None |
Problem Statement: What is a radio button in HYSYS? | Solution: A radio button in HYSYS is one of those little black dots that you can check (toggle). For example, in the Fluid Package view on the Components tab, there are radio buttons for Library and Hypotheticals.
Keywords: radio button
References: None |
Problem Statement: Are the components of Aspen Collaborative Forecasting v2006.6 suite compatible with the new version of WebLogic 10gR3 or 11gR1? | Solution: AspenTech doesn't support WebLogic Application Server versions either 10gR3 or 11gR1 for Collaborative Forecasting v2006.6 application
AspenTech Collaborative Forecasting does support WebLogic Application Server version 10.0 starting from v2006.6 until V7.3
Keywords: Collaborative Forecasting
WebLogic 10.0
WebLogic 10gR3
WebLogic 11gR1
WebLogic Support
References: None |
Problem Statement: For some systems, the shape of the phase envelope is often characterized as strange or unusual since it shows only a dew point line and no bubble point line and no critical point (see attached case Unusual_Shape_Env.HSC). | Solution: This shape of phase envelope is entirely expected for a system consisting primarily of non-condensable components (e.g. more than 90% C1, C2, N2, and CO2) with non-negligible amounts of heavier hydrocarbons. During the calculation of the phase envelope via the Michelsen scheme, the critical point essentially disappears and only a dew point line is traced eventually going off to infinite pressure. According to the original Michelsen paper (Michelsen, M. L., 1980, 'Calculation of Phase Envelopes and Critical Points for Multicomponent Mixtures', Fluid Phase Equilibria, 4; 1-10), this behavior will arise but is typically accompanied with a two liquid region below the dew point line (sometimes multiple critical points can be found as well). Since the HYSYS Phase Envelope Utility is designed to deal only with the VLE phase envelope (not VLLE), we observe that the dew point line going off to infinity.
Although this explains the fact that the mathematical calculation demonstrates this phase behavior, only experimental data can confirm it. However, the critical points for systems of this nature are notoriously difficult to measure and the experiments can be inconclusive.
Another fact to consider is that these envelopes are quite sensitive to the pure component properties and the interaction parameters. For example, the interaction parameters between C1 and heavy components will control the bubble point line. This can have a significant impact for hypothetical components, for which the properties and interaction parameters are estimated.
Keywords: Phase, Envelope, Strange, Unusual, Bubble, Dew, Point, Critical, Line, Utility, Typical, Weird, Unexpected.
References: None |
Problem Statement: HYSYS has given me the message A math error has occurred in the math library, Math overflow error or A numerical error of some sort has occurred. What does this mean? | Solution: The message A math error has occurred in the math library, Math overflow error or A numerical error has occurred is shown when HYSYS has encountered some kind of numerical difficulties during calculations, for example a division by zero, square root of negative number or any other type of mathematical error. Unfortunately, HYSYS knows that a mathematical error has occurred but is unable to tell the user what the specific cause of the error is. (This limitation has been addressed for HYSYS 3.2+ - see below)
After such a warning is displayed, HYSYS will try to converge the calculation one more time using a different route. If the calculation succeeds, the complete results will be displayed. If the calculation does not succeed, HYSYS will display only the results that could be successfully calculated.
When you encounter this problem, we advise that you check the results carefully using your engineering judgement. The program will only report results from converged calculations. If the results are reasonable, then you can continue your simulation.
Relevant Preferences Settings
Displaying Errors in the Trace Window
HYSYS can be set to display error messages in the Trace window (white panel at bottom right of HYSYS screen) instead of popping up a message box. This will eliminate the need to manually acknowledge numerical errors.
In HYSYS versions prior to 3.2 this is accomplished by using the Tools / Preferences menu option and ticking the 'Display Numerical Errors in Trace Window' checkbox on the Simulation tab Options page. In HYSYS 3.2 there is a new Errors page on the Simulation tab that contains the same checkbox.
Identifying Sources of Numerical Errors
HYSYS 3.2 includes a new feature to identify the source of Numerical errors. This is activated by ticking the 'Identify Source of Numerical Errors' checkbox on the Errors page of the Preferences window.
Keywords: numerical error occurred, math error, math overflow error, math library
References: None |
Problem Statement: Does Aspen Collaborative Forecasting accept custom attribute tables other than ATT1-5? | Solution: Yes Demand Manager includes six additional attribute sets that you can use as needed including standard attribute sets.
Additional Attribute Sets
The Demand Manager includes six additional attribute sets that you can use as
needed. You might use the additional attribute sets for attributes such as
product family, package, region, market, or industry. These attribute sets are
named as follows: ATT1, ATT2?ATT6.
If desired, you can add any number of additional attribute sets, or delete any
of the ATTn sets.
Keywords: ATT
Additonal Attributes
ATTCFG
CFATT
References: None |
Problem Statement: Why is my valve size in HYSYS not matching the Cv provided by my vendor for the same valve? | Solution: There is a very strong probability HYSYS and your valve vendor use totally different equations for Cv calculations. This is not a problem, as long as you keep in mind that the valve in your simulation and the real valve should match in terms of performance and not Cv. (ie. for the same flow and valve openings the two valves should calculate the same DP. Each valve will have its own Cv value, but they perform the same way.)
In order to understand why the Cv calculation in HYSYS would differ from the vendor, one must keep in mind that HYSYS is merely a calculation engine, whereas your vendor needs to account for how they manufacture the valve and its mechanical characteristics. In other words, the Cv equation in HYSYS is a best-fit representation of a fisher valve, while your vendor would be basing their calculations on a specific valve they build and guarantee.
As for the specifics of the equation used in HYSYS, please refer to the Operations Guide manual (supplied on the Documentation CD/DVD and on the support web site).
Keywords: valve, cv, dynamic, fisher
References: None |
Problem Statement: For a liquid stream of liquid and aqueous phases present at stream conditions, HYSYS calculates the Liq Vol Flow @ Std Cond of the overall stream, which is not equal to the sum of the liquid and aqueous phases. Why? | Solution: All calculations for volumetric stream flows are based on density. For Liq Vol Flow @ Std Cond, the density basis is Liq Mass Density @ Std Cond.
The traditional HYSYS thermo always uses the COSTALD liquid density model to calculate Liq Mass Density @ Std Cond, regardless of the property package you have chosen (provided you are below the critical point). However, if you use COMThermo in HYSYS 3.0.1 or above, you have choices of liquid density models for the calculations.
No matter what density model is used for a multiple phase stream, the standard liquid density of individual phases and the overall stream is calculated as follows.
For individual phases:
The standard liquid density of each phase is calculated by the density model with the phase composition of the stream at the flowing conditions and the reference temperature and pressure of standard conditions.
For the overall value:
The standard liquid density of the overall stream is not calculated as a weighted average of the individual phases. Instead, the bulk composition of the stream is used in the density model to calculate the standard liquid density of the overall stream. The Actual Liquid Density value is calculated as the weighed average of the individual phases.
Since the standard liquid density of the overall stream is not calculated as a weighted average of individual phases, the standard liquid volume flow of the overall stream does not equal to the sum of the individual phases for a multiphase stream.
The standard liquid volume flow of the overall stream is just a theoretical value for a multiphase stream. It does not change with stream conditions, so long as the stream's overall composition does not change. However, the standard liquid density and flow of each phase will change because the phase fraction and composition will change with stream conditions.
Keywords: volume flow, liquid density, Liq Vol Flow @ Std Cond, Liq Mass Density @ Std Cond
References: None |
Problem Statement: How does Aspen HYSYS calculate friction factor and pressure drop for single phase flow in a pipe? | Solution: Aspen HYSYS uses the Fanning Friction Factor in the Darcy equation for calculating pressure drop in single phase flow.
To calculate the friction factor for both laminar and turbulent flow, the full-range, smooth-transition, direct calculation method by Churchill (Chem. Eng., p.91, Nov. 7, 1977) is used in HYSYS. The Churchill equation adequately represents the Fanning friction factor over the entire range of Reynolds numbers within the accuracy of the data used to construct the Moody diagram.
The Churchill equation and Darcy equation are described in detail in the attached Word document. The Excel file shows the manual calculation. The case file shows the manual calculation in an Aspen HYSYS spreadsheet and compares it to what Aspen HYSYS calculates. Cell B7 is the Aspen HYSYS result, cell B8 is the manual result and cell B9 is the relative error caused by rounding and machine precision.
Keywords: pipe segment, single phase, pressure drop, Darcy, Fanning, friction factor
References: None |
Problem Statement: This knowledge base article explains why BEA WebLogic Server 10.0 uninstalls when upgrading from Collaborative Forecasting (CF) 2006.6 and older versions to V7.3 and how to request BEA WebLogic Server 10.0 from AspenTech. | Solution: BEA WebLogic Server was distributed as part of the Aspen installation media through the distribution of CF V7.1, so when you uninstall a CF application older then CF V7.2, BEA WebLogic Server 10.0 will also uninstall. As of CF V7.2, BEA WebLogic Server 10.0 is no longer distributed with the AspenTech installation media.
When upgrading from a CF version V7.1 and older, the upgrade process will uninstall the BEA WebLogic Server. Your BEA license will not uninstall.
Existing CF customers who are current on support can request a download of BEA WebLogic Server 10.0 directly from AspenTech. New customers using CF are required to purchase BEA WebServer 10.0 directly from Oracle.
To obtain BEA WebServer 10.0 from AspenTech, the customer must submit a request from the AspenTech Support web site http://support.aspentech.com/ using the Upgrade, Media or License? link, found on the left-hand side of the screen.
Select Request an AspenTech Software Upgrade or Media and complete the form, including the system name and the request for the electronic media. Complete the comment section stating your request is for BEA WebLogic Server 10.0.
When approval is granted, the user will receive an email from AspenTech Customer Care with a user specific link for the download.
Keywords: None
References: None |
Problem Statement: After installing CF (Collaborative Forecasting), the user is unable to start the Weblogic service. | Solution: This is due to a bug with the installer adding a space to the configuration file for the Weblogic service. The user must delete the added space, save the file, and restart the service.
Example.
Expected: WLS_PW=password
Found: WLS_PW= password
Keywords: Weblogic10
References: None |
Problem Statement: How do I model a thermosyphon reboiler in Steady State? | Solution: The default reboiler configuration in HYSYS is a kettle-type reboiler, however, many columns use thermosyphon reboilers in place of kettle reboilers. A thermosyphon reboiler returns a two-phase stream to the bottom of the column, and the bottoms product is drawn from the same location as the reboiler feed - the bottom of the tray section. The document and sample case will show you how to convert the default kettle reboiler to a thermosyphon one.
Keywords: thermosyphon, thermosiphon, reboiler
References: None |
Problem Statement: I am trying to install HYSYS and I get Error 1311. Source file not found:.... What does this mean and how can I get around it? | Solution: Error 1311 is a Windows Installer problem. Basically, there is restricted access to the installation CD and so you're not able to access the file, even though it's there.
To get around this, you'll have to copy the contents of the installation CD onto the computer harddrive (create a folder and copy the contents to that folder), and then run the setup.exe file from the new folder on your computer.
Keywords: Error 1311, Windows Installer
References: None |
Problem Statement: How may I calculate the pH in HYSYS? | Solution: The pH is directly available in HYSYS only when the OLI-Electrolyte Property Package is used.
With any other Property Package, the pH is not one of the variables available in HYSYS. As a possible workaround, the pH may be calculated in the HYSYS Spreadsheet using some assumptions. For example, theSolution pH can be calculated based on its acid content (only when these acids are completely in ionic forms):
pH = - log[H+]
In that case, the concentration of the hydrogen ion could be determined based on the concentration of the related acids. In the case where weak acids are involved, it would be difficult to get the [H+] values.
Alternatively, a User Variable could be used for the same purpose. The detailed instructions on how to create a User Variable can be found in the HYSYS Customization Guide (chapter 5), which is available on our support website.
Keywords: pH,
References: None |
Problem Statement: Why can I not put the Tray Sizing utility into rating mode? | Solution: The calculation mode of the Tray Sizing utility (Design or Rating) is displayed in two places - On the Design tab / Setup page and on the Design tab / Specs page. In order to change the mode to rating you need to go to the Design / Specs page. Here you can also enter the geometry information needed for the rating calculations.
Keywords: Tray Sizing Utility, Rating Mode, Design Mode
References: None |
Problem Statement: Why won't my stream User Variable work in dynamic mode? | Solution: In steady state mode streams have two available methods (PreExecute and PostExecute) to which user variable code can be attached. These methods are NOT called when the Integrator is running in dynamic mode.
Operations also have PreExecute and PostExecute methods which are called in steady state, however they have two additional methods (DynPressureFlowPreStep and DynCompositionPreStep ) which are called in Dynamics. (Before each Pressure/Flow and Composition step respectively.)
Hence if you want to write user variable code that will run in dynamics you MUST place it in an operation. If required a user variable attached to an operation can reference the attached streams.
In the attached HYSYS (2.2) case the mixer operation has User Variables (Steady State and Dynamic) that calculate the stream temperature if it were flashed at the same pressure to have a vapour fraction as specified in the Vapour Fraction user variable.
To see this in operation:
Switch to Dynamics mode
Start the Integrator A new user variable called Vapour Fraction is created in the mixer - by default this is set to 1 to give a dew point temperature. Adjusting this value sets the vapour fraction in the flash (e.g. changing it 0 would give a bubble point temperature).
More technically, the mixer product stream is duplicated into a Fluid object which is then flashed to a different vapour fraction. The temperature of the resultant fluid is then reported.
Keywords: User variable Stream Dynamics DynPressureFlowPreStep DynCompositionPreStep Dew Point
References: None |
Problem Statement: What is COMThermo? | Solution: Starting with HYSYS 3.0, you will find an option in HYSYS on the Fluid Package view (Set Up page) under Advanced Thermodynamics.
COMThermo is a thermodynamic calculation framework, which makes it possible to develop independent, extensible, customizable, and encapsulated thermodynamic calculation modules.
COMThermo allows the use of a single thermodynamics engine in all major engineering applications, including in-house tools.
Its key benefits include providing consistent results across applications; and its ability to mix and match best-of-breed components, either from third parties or in-house, to accurately represent the system/process you are simulating.
Keywords: COMThermo, new 3.0 features
References: None |
Problem Statement: How do I implement a Ratio Controller in Aspen HYSYS? | Solution: A ratio controller is used to maintain the ratio between two process variables fixed. For example, if you have two streams, one that is controlled (A) and the other that is uncontrolled (B). You may want to use a ratio controller to fix the ratio between A and B.
The following steps illustrate how to set up a simple ratio controller:
1. Press the Select PV button and choose the first process variable (A), in this case it is the controlled flow.
2. Press the up arrow to activate the second process variable selection. The PV window should show a number two and the Process Variable Source fields should be blank.
3. Press the Select PV button and choose the second process variable (B), in this case it is the uncontrolled flow.
4. Press the Select OP button and chose the control element to be used to control process variable A.
5. Go to the Parameters -> Configuration tab and enter the maximum and minimum values for the two process variables.
6. Go to the Parameters -> Operation and select the Enable Ratio Control check box.
7. Enter the desired ratio. Note that this number will be the value of the first process variable divided by the value of the second process variable.
8. Enter the desired tuning parameters.
9. Change the Controller Mode to Automatic.
10. Start the Integrator.
A simulation case built in Aspen HYSYS v3.2 is attached to illustrate the set up of a ratio controller (S109680.hsc)
Keywords: dynamics; controller; ratio control
References: None |
Problem Statement: You would like to know if you can install CF on Vista SP2, using IE8. Is this supported? | Solution: As per the Installation guide, Vista is not supported. We do support IE8, though.
Keywords: None
References: None |
Problem Statement: Do I still need recycle operations in Dynamics? | Solution: Recycle operations are not required in dynamics because the solver is completely different than the one available in steady state and will automatically calculate any required information for recycled streams. However, if you happen to have any recycle operations left over from the steady-state case, they will simply be ignored with the stream composition and conditions being passed directly through the recycle operation.
Keywords: recycle, dynamics
References: None |
Problem Statement: The on/off checkbox in my pump in Aspen HYSYS is greyed out. How do I turn my pump on/off in Dynamics? | Solution: The check box is only applicable if you are using one of the following:
Electric motor
Speed spec
Power spec
If you are using the electric motor option on a pump then the only specs active should be Use characteristic curves and Electric Motor - speed will be a calculated value.
The speed of the pump will be determined based on the information provided on the Ratings tab | Electric motor page.
Keywords: pump, dynamic, on, off, switch
References: None |
Problem Statement: How does the MASSBAL solver compare to the normal HYSYS Solver? | Solution: HYSYS solves using a sequential modular solver. Unit operations must have specific degrees of freedom satisfied (specified) in order for the unit operation to solve.
MASSBAL uses a simultaneous solver. In MASSBAL, a completely specified problem requires that there be no degrees of freedom remaining for the flowsheet. However, the specifications are not restricted on a unit by unit basis. They can be specified anywhere in the flowsheet.
Keywords: MASSBAL, solver, sequential modular, open equation, degrees of freedom
References: None |
Problem Statement: Why does the forecast only show through June 2013 in Aspen Collaborative Forecasting? | Solution: This is caused when the weblogic server is hanging on a thread and not accepting any more new requests at that juncture. To resolve the problem, restart the weblogic service.
Keywords: None
References: None |
Problem Statement: Calculation of Integral and Differential Condensation Curves in HYSYS | Solution: [Based on HTFS Handbook Datasheet CP13 Vapour Liquid Equilibrium in Condensers]
Integral Condensation
To calculate an integral condensation curve the bulk vapour phase at any point is considered to be in equilibrium with all of the previously formed bulk condensate.
To calculate such a curve in HYSYS there are two approaches. Either a property table utility is used to vary the temperature between the dew point and the bubble point at a given pressure, or a series of coolers is used to drop the stream temperature by a small temperature decrement. In either case the total mass enthalpy of the system is recorded and then subtracted from the mass enthalpy at the dew point to give a heat released value.
[In the attached case both approaches to calculate the Integral condensation curve for a 50% molar mixture of n-Butane and n-Pentane are used. See Property Table utility 'Property Table Integral Condensation' and spreadsheet 'Integral Condensation Results (Prop Table)' and also spreadsheet 'Integral Condensation Results (Flowsheet)'. The temperature difference across each Cooler is set by a Set operation. The spreadsheet 'Set Delta Ts Integral' sets the offset in each of the Sets.]
Differential Condensation
For differential condensation the bulk vapour at any point is considered to be in equilibrium only with the newly formed condensate. Any previously formed condensate is not considered to take any part in the vapour/liquid equilibrium.
To calculate such a curve in HYSYS a series of condensation steps is used. At each step the vapour from the previous step is cooled to a given small temperature decrement below the local dew point. The liquid that condenses is then mixed with the liquids from previous stages which has also been cooled to the same temperature.
The heat released is calculated by finding the total 'mass enthalpy' at each stage. This is calculated by adding together the total heat flows of the vapour and combined liquids at each stage and dividing by the total mass flow.
Since the vapour phase becomes richer in the more volatile components, the equilibrium temperature tends to fall more rapidly than for integral condensation.
[In the attached case see spreadsheet 'Differential Condensation Results' and spreadsheet 'Set Delta Ts' which is used to set the delta temperature at each stage. The attached case requires the virtual stream extension to be registered (see KnowledgebaseSolution #110889. Also included is an Excel spreadsheet that includes a plot of both the integral and differential condensation curves.]
Keywords: Integral, Differential, Condensation Curve, Condenser
References: None |
Problem Statement: My Gibbs Reactor cannot solve and I get the error unknown chemical formula. Why? | Solution: The HYSYS Gibbs reactor requires known chemical formulas for all of the components involved in the simulation. This error message usually means that the atom matrix needs to be filled (Gibbs Reactor Property View, Reactions tab, Details page, Atom Matrix radio button).
If you are simulating a fuel containing hypothetical components with unknown chemical formulas, you cannot use the Gibbs reactor unless you can specify the atomic makeup of each of the participating species.
Keywords: Gibbs, reactor, unknown, chemical, formula, error, warning, atom, matrix, hypotheticals, pseudo.
References: None |
Problem Statement: How does the Forecast SignOff feature works in Collaborative Forecasting? | Solution: Detailed instructions about Forecast Signoff feature: The My Preferences: Forecast Signoff feature enables you to manually sign off on a forecast when you have completed the collaborative forecast process for the current business cycle, or time period. The Forecast Signoff option runs independently of override creation. You can perform a signoff even if you have created overrides or not. Period Type The Period Type field displays the type of time period. Currently, month is the only period type available. Current Period The Current Period field displays the current working forecasting cycle, generally a description of month and year. Period Start/End The Period Start and End fields display the time period in which you are permitted to perform signoffs. Once the Period End date is passed, you can no longer sign off on a forecast from this time period. Signoff Status The Signoff Status field displays No if have not signed off during the current time period and Yes if you have signed off during the current time period. Sign/Signing Date Click the Sign checkbox when you are ready to sign off on a forecast. After you check the Sign checkbox, the checkbox is removed and replaced by the Signing Date field. The Signing Date field displays the date that you signed off on the forecast. After initial sign off, you can still update comments and the signoff date until the current time period ends. Comment The Comment field is where you enter comments about the forecast signoff. You can continue to update comments to this field as long as you are still in the current time period. To sign off on a forecast: 1Review your unconstrained forecast data. 2Click the Sign checkbox. 3Enter comments in the Comments box, if necessary. 4Click OK. Note: This process is irreversible. Once you sign off on a forecast, you cannot revert back to an unsigned state. To update forecast comments: 1Add additional comments in the Comments box. 2Click Update. In addition to overriding forecasts, CF users now have the option to approve and signoff forecasts for each forecasting cycle after they have reviewed them. The Forecast Signoff submenu is located under the My Preferences tab. For each forecasting cycle, each web client user can sign off once irreversibly. However, the comment can be updated until the end of the forecasting cycle.
Keywords: Signoff Forecast Signoff Signoff Status
References: None |
Problem Statement: Aspen Collaborative Forecasting (CF) does not immediately release Tokens after logging out and closing the web client. | Solution: You must change the properties.ini on the CF server having the issue and then restart your services.
## Session timeout in minutes. Setting is valid if it is a number greater than 0.
## Anything else will be ignored and the timeout will be Weblogic's default of 60 minutes.
SESSION_TIMEOUT=5
In this example, after 5 minutes, the license will be released.
Keywords: None
References: None |
Problem Statement: HYSYS is predicting two liquid phases in my stream having only hydrocarbons components, why? | Solution: One of the technical difficulties associated with flash calculations is the fact that the number of equilibrium phases is not known in advance. Unless there is a strong evidence for 3 phases, HYSYS performs a 2 phase flash calculation. The resulting phases are then tested for stability using the stability test of Michelsen (Michelsen, M. L., The Isothermal Flash Problem. Part I. Stability, Part II. Phase Split Calculation, Fluid Phase Equilibria, 9, 1-19; 21-40. (1982)). This test is based on the tangent plane criterion put forth by J. W. Gibbs. For an unstable system, this test provides the composition of a new phase that could be split off to decrease the overall Gibbs free energy of the mixture.
If you would like to have control over the flash convergence methods used by HYSYS, you can modify the stability test parameters (found on the StabTest tab of the Fluid Package property view) to instruct HYSYS to perform phase stability calculations using a different route. For example, you can limit the maximum number of phases allowed to 2 in order to avoid searching for a second liquid phase, or use HYSIM flash if you do not want HYSYS to perform a phase stability test at all. The details of the stability test parameters are provided in the Simulation Basis manual of the HYSYS documentation CD (Section 2.4.4 in Hysys 3.2).
As far as the validity of the results are concerned, only a comparison of the results with experimental/plant data would be able to provide an accurate assessment.
Keywords: two liquid phases, stability test, flash, stability test of Michelson
References: None |
Problem Statement: Do you have a step-by-step procedure for creating a Hypothetical component? | Solution: Please review the attached document for a detailed description of creating a Hypothetical component.
Keywords: Hypothetical, create
References: None |
Problem Statement: I'm trying to add a component and I can't find it in the component library list. What should I check? | Solution: If components are not compatible with certain property packages, Hysys will, by default, not display them. For example, if you are trying to add a ketone to a Fluid Package where you have chosen the Property Package to be the Peng Robinson equation of state, the component filter for ketones is empty. This is because ketones are highly non-ideal liquids and they are best simulated by the Activity Models (such as NRTL and UNIQUAC) rather than Equations of State (EOS) like Peng Robinson. If you had chosen the NRTL model as the property package and used the ketones filter, all would be listed there. Please be aware that Activity models should only be used at low pressure, far below the critical pressure of the system you are dealing with.
An alternative to Activity models is to use the Property Package called PRSV. It is an EOS which can account for the non-idealities of certain components. Moderately non-ideal liquid and vapours at high pressure are best simulated with this property package. More detailed information can be found in the HYSYS documentation (Simulation Basis Appendix A). If using PRSV you can add components such as ketones and alcohols to your simulation.
If you want to model a non-ideal liquid using the Peng Robinson model (non-recommended however), you can add a fluid package with the property package set at None and choose any component you want. Then go back and choose the PR model. HYSYS will present a message warning you that the component is not suitable for that property package. Choose the Keep Components radio button.
If you wish to see the full list of library component in HYSYS, you can toggle the radio button Full Pure Component Library (Including Non-Recommended Components) in the Component Selection Control group (Prop Pkg tab of the Fluid Package Property View). Non-recommended components for the selected Property Package will then appear with an X beside them in the list.
Keywords: non-compatible component
References: None |
Problem Statement: When will Aspen Collaborative Forecasting support Oracle 11g? | Solution: We are currently working to supporting Oracle 11g upgrade to CF. We expect to be able to support that in the next major release.
Generally, we have been issuing quarterly supplemental product releases and we typically anticipate having a major release each year for the aspenONE suite.
Keywords: None
References: None |
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