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Problem Statement: Why is there a difference between the Standard Gas Flow and the Molar Flow in MMSCFD? | Solution: In Aspen HYSYS, all flows are stored in kgmole/s (what we call Internal Units) and converted to the flows displayed on the screen.
If you ask to see your molar flow in MMSCFD or m3/day(gas), the flow is converted using a pre-defined conversion factor that is hard coded into the program. This conversion factor uses an Ideal Gas Molar Volume that is calculated from first principles at standard conditions. The conversion to MMSCFD uses standard conditions of 60 ?F and 1 atm. The m3/day(gas) conversion uses 15 ?C and 1 atm. Since these conversion factors are hard-coded, they do not change with the temperature units used in your simulation.
The Standard Gas Flow displayed on the Conditions Tab is converted on the fly. Again, it uses an Ideal Gas Molar Volume calculated at standard conditions, but the standard conditions used are determined by the temperature units you have chosen to use in your simulation.
For example, if you use ?C as your temperature unit, and display your gas flows in MMSCFD, the flow shown in the Molar Flow cell will be converted using standard conditions at 60 ?F, but the Standard Gas Flow conversion uses 15 ?C as the temperature. The difference in these two standard conditions can lead to a difference of around 0.2% between the two flows.
If you wish the two flows to agree, you need to make sure you are using ?F or ?R for temperature if you are using MMSCFD for gas flows. Alternatively, if you want to see flows in m3/d, you need to ensure that your temperature units are either ?C or K.
Note that even if you are using the correct temperature units, there will still be a small discrepancy between the two values due to round-off error introduced in the two different conversion methods.
Keywords: Standard Gas Flow, Molar Flow, MMSCFD
References: None |
Problem Statement: How do I reset my APS user registry settings? | Solution: Sometimes, there could be some issues with APS (mostly cosmetic issues like dialog box size/Gantt Screen Display changes etc). These can be reset by clearing out the following folder(s) from the user’s registry:
Close any existing APS instances
Open registry editor
Navigate to the following path: HKEY_CURRENT_USER\SOFTWARE\AspenTech\Aspen Petroleum Scheduler\
Rename the folder to another name (Say Aspen Petroleum Scheduler_Old)
Now navigate to the following path: HKEY_CURRENT_USER\SOFTWARE\AspenTech\Orion Scheduling
Repeat the same steps (rename the path)
Now reopen APS.
In the background, APS would have recreated the folders we just renamed. This is equivalent to opening APS for the first time for this user on this machine. This is a measure that should be used only for troubleshooting purposes.
Keywords: None
References: None |
Problem Statement: Should I Use Improve Local | Solution: , Epsilon, or Both?
Solution
In PIMS-AO there are two settings available which are similar: “Improve LocalSolution” and “Epsilon”. Both these algorithms are designed to prevent sub-optimal results caused by the tendency of the optimizer to leave pools which are initialized with zero flow at the rate of zero – even if a non-zero value may be superior. The two options address this problem in mathematically different ways.
Because the two options are addressing the same underlying issue, it is generally best to use one method or the other – not both. We recommend trying the Epsilon algorithm first. Try various values for “Epsilon Value” varying from 0.0001 to 1. The best value is model dependent and should be determined for each model.
If Epsilon does not improve model performance, then try Improve LocalSolution. Vary the “Smallest Initial Pool Collector Column Activity” from 0.0001 to 1 to determine the best value. Again, this is model-specific and should be tested.
In rare cases, we have seen a model perform well with both algorithms active but this should be established by testing.
Keywords: None
References: None |
Problem Statement: Why cannot I set NIST binary databanks as Selected databanks? | Solution: When opening File|Options| Properties Basis table, I selected NIST binary databanks into Searched column.
However, the NIST binary databanks are still not used when I am using an activity coefficient method. Why does this happen?
NIST binary databanks, NIST-RK, NIST-IG, and NIST-HOC, are only on Available databanks; each of them is not implemented/designed for a specific model that contains parameters in the databank. Users have to select it in order to use it.
Key Words
NIST databank binary Aspen Plus
Keywords: None
References: None |
Problem Statement: When launching Aspen SCM, AspenTech Application Exception Message occurs. | Solution: To resolve the error, follow the below steps:
Go to C:\Users\*UserName*\AppData\Local\Aspen_Technology_Inc\AspenTech.SCM.UI.Shell.ex_Url_pxzmw32phcfzwpquginyos4jnepf24fk\21.0.2.0
Delete user.config file
Open SCM. Error should not appear now.
If the above procedure fails to solve the issue, follow the steps below:
Uninstall SCM.
Go to C:\Program Files (x86) \AspenTech (if it is a 32 Bit SCM) or C:\Program Files\AspenTech( if it is a 64 Bit SCM).
Delete all the files/folders.
Re install SCM.
Keywords: None
References: None |
Problem Statement: How can I speed up the loading time of very large case tables? | Solution: In Aspen PIMS V11, there is a new feature that can speed up the loading of large case tables. The option is located on the Reporting | Miscellaneous tab at the very bottom. When selected, PIMS will skip the processing required to generate the W500 warnings related to the case table. W500 is the warning that a case is creating new matrix structure. This option is only available in Aspen PIMS-AO.
Keywords: None
References: None |
Problem Statement: What Is The Enthalpy | Solution: HYSIM and HYSYS use different reference basis for enthalpy (H) calculation. In HYSIM, H=0 at 0 K and 1 atm (ideal vapour); in HYSYS H=heat of formation at 25 øC and 1 atm (ideal gas). For example, if the heat of formation is 1000 kJ/kgmole, the enthalpy at 25 øC is 1000 kJ/kgmole.
For a liquid water stream at 25C, the molar enthalpy of the stream will be the heat of formation minus the heat of vapourization of water. In HYSYS we assume everything is in its ideal gas state. Liquid water is not, so you have have to account for the heat of vapourization to get the real enthalpy of liquid water.
The benefit of using the heat of formation basis is that the heat of reaction is implicitly included in the calculated stream enthalpies, which simplifies the handling of reactions. In practical terms, the HYSYS enthalpy basis results in enthalpies which are large negative numbers, due to the shifting from the heat of formation. The basis offset for a given component is displayed in the fluid package (Component Property View, Point tab).
To determine the enthalpy value of a stream at the operating conditions, HYSYS first calculates the enthalpy change of the stream from 25 øC to the system temperature as an ideal gas. The enthalpy departure is then calculated rigorously using the property package selected. The summation of these terms (H at the reference state, H change from the reference state to system temperature as ideal gas and H departure) will determine the enthalpy value of the stream at the operating conditions.
Keywords: enthalpy, reference, basis, HYSIM, HYSYS
References: Basis in HYSIM and HYSYS? |
Problem Statement: Using Aspen HYSYS Dynamics with Columns | Solution: Columns are an essential part of most processes. Columns can have many variables that rapidly change during plant operation. Utilizing Aspen HYSYS Dynamics, users can set up models to view and control the dynamic response of columns.
Please click the links above to download the Jump Start Guide and example files.
Keywords: Column, operations
References: None |
Problem Statement: Structure related to table PROCLIM can not be applied directly in table ASSAYS, i.e. you can not write ZLIMTAG or ZQQQTAG rows in table ASSAYS as they are not recognized by Aspen PIMS.
What is the work around to use table PROCLIM to control properties in crudes? | Solution: To apply limits using PROCLIM to the crudes mixture going to the crude units you need to do the following:
Define them as deferred cuts in table CRDCUTS (in volume and/or mass, as required)
Define relevant properties in table ASSAYS and recurse on them defining them in PGUESS
Create PROCLIM structure in a dummy submodel
Set limits in table PROCLIM
The example is set up for the crudes going to all the crude units; if you want to set up limits for a specific crude unit, see the note at the end.
The changes required to implement this structure are as follows:
1. Define crude mixture as deferred cuts in table CRDCUTS
In table CRDCUTS, define the deferred crude cut(s). In the example, we define two deferred cuts, one for the crude in volume (CRV) and one for the crude in mass (CRM), because some properties are blended in volume (e.g. SPG) and some in mass (API, SUL).
2. Define relevant properties of deferred cuts in table ASSAYS
In table ASSAYS add the following:
* DBALTAG rows to define the yields for the deferred cuts. For CRM, the Crude Mass deferred cut, the yield coefficient is SPG*VTW (Volume to Weight Conversion Factor), for CRV, the Crude Volume deferred cut, the yield coefficient is 1.
* IQQQTAG rows to define the relevant properties (QQQ) of these deferred cuts (TAG), e.g. IAPICRM.
3. Define properties for deferred cuts in T. PGUESS
In table PGUESS, add initial estimates for the properties of the deferred cuts that need to be recursed:
4. Create PROCLIM structure in a dummy submodel
Create a new submodel (or use an existing one) and add one column per deferred crude tag with the same name (e.g. CRM).
Fix the activity of these columns to a value, for example to 1, by entering a 1 under the column in row FIX.
Set up the PROCLIM structure as shown in the figure. Bear in mind that the TAG used in row ZQQQTAG can not have the same name as the deferred cut. In the example, ZQQQCMR is used for CRM, and ZSPGCVR is used for CRV.
5. Set the limits in table PROCLIM
Set the MIN and MAX property limits for the crudes in table PROCLIM.
6. Results in FullSolution
Look in section Process Limit Summary of the FullSolution for the results.
To set up different limits for different crude units
The example is set up for the crudes going to all the crude units; if you want to set up limits for the crudes going to a specific crude unit, e.g. to unit CD3, in table CRDCUTS enter a 1 only under column CD3.
Use different deferred cut tags for each unit, e.g. CM1, CM2, CM3.
Keywords: None
References: None |
Problem Statement: Simple Heater Unit Operation Extension in C#. | Solution: The attached example illustrates how to create unit operations extension in Aspen HYSYS. The model handles backward and forward calculations and allows for multiple specification sets for flash calculations. Pressure drop in the unit is mandatory so flash calculations are pressure explicit. Duty is optional, PV-flash, TP-flash, PH-flash and PQ-flash types are supported. The extensions includes a worksheet tab where conditions for the streams connected can be directly entered. The class is coded in C#.
Note: these examples are provided for academic purposes only and as such are not subject to the quality and support procedures of officially released AspenTech products. Users are strongly encouraged to check performance and results carefully and, by downloading, agree to assume all risk related to the use of these examples. We invite any feedback through the normal support channel at [email protected].
Keywords: Unit Opration Extensions.
References: None |
Problem Statement: How can a user customize the generation of pseudocomponents in the petroleum characteriztion input formin the petroleum characterization form? | Solution: Quite often the default settings in Aspen Plus will suffice to model petroleum assays in flowsheet simulations. Typically, based on the distillation data provided by the user, a working TBP curve is generated by Aspen Plus engine and the fractions of pseudocomponents are optimized to provide a close match with the input distillation data.
However, in some cases closer match between the input distillation data and the simulated results are required.
In the attached file (characterised.bkp) identical ASTM D2887 data have been provided for the two assays 'cuts' and 'simple'.
The petro characterization solver has optimized the fractions of pseudocomponents as shown in the screen shot below for the 'SIMPLE' assay:
And similarly for the 'CUTS' assay as shown in the screen shot below:
All the default settings in Aspen Plus have been used in the petroleum characterization for these two assays, except that the number of cuts have been specified to be the default 1 cut per temperature interval for the 'SIMPLE' assay :
And 2 cuts per temperature intervals for the 'cuts' assay, as shown in the screen shot below. Needless to say that more cuts will mean more accurate representation of the input distillation data:
The 'SIMPLE' and 'CUTS' assays have been used in streams 'SIMPLE' and 'CUTS' respectively. The PROP-SET D2887CRV has been defined to display the simulated distillation data in the stream results.
In the stream results, the simulated D2887 result by the two assays 'CUTS' and 'SIMPLE' can be compared with the input distillation data and it will be seen that a closer match has been obtained when we define more cuts per temperature intervals.
Keywords: Petroleum Characterization, number of cuts, pseudocomponents
References: None |
Problem Statement: This | Solution: provides an Aspen SQLplus query to return all the references to a manually-entered tag name in the Aspen InfoPlus.21 database.Solution
procedure findchar24 (char24 char(24), qname record)
local i,j,k int;
local c char(80);
j =(select #QUERY_LINES from QueryDef where name = qname);
for i=1 to j do
c=(select query_line[i] from QueryDef where name = qname);
c=upper(c);
k=POSITION(upper(char24) IN c);
If k > 0 then
write char24 ||' was found in line of ' || i ||' in '|| qname;
end
end
end
local filename char(256), s string, r record, found_field field, ref_type char(20), dummy char(20),tname char(24);
macro sqlfileslocation = 'C:\ProgramData\AspenTech\InfoPlus.21\db21\group200\sql\';
s = PROMPT('Enter tag name');
macro searchstring = s;
r = s;
Write '&searchstring'||' appears in the following CompQueryDef records:',' ';
for (select name as QueryName from compquerydef where queryname||'.sql' in (select line from system 'dir/b &sqlfileslocation')) do
filename = '&sqlfileslocation'||queryname||'.sql';
select QueryName, linenum from file(filename) where position(upper('&searchstring') in upper(line)) <> 0;
set column_headers=0;
end
Write ' ','&searchstring'||' appears in the following ProcedureDef records',' ';
for (select name as QueryName from compquerydef where queryname||'.sql' in (select line from system 'dir/b &sqlfileslocation')) do
filename = '&sqlfileslocation'||queryname||'.sql';
select QueryName, linenum from file(filename) where position(upper('&searchstring') in upper(line)) <> 0;
set column_headers=0;
end
Write ' ','&searchstring'||' appears in the following QueryDef records:',' ';
FOR (Select name nym from QueryDef) DO
tname=nym;
findchar24 (s,tname);
END
Write ' ','&searchstring'||' appears in the following non-Query references: ',' ';
found_field = nxtrefer(NULL, r);
while found_field is not null do
ref_type=(select Definition from All_Records where Name=substring(1 OF found_field));
write found_field, ref_type;
found_field = nxtrefer(found_field, r);
end
Keywords: SQLplus
Show references
References: None |
Problem Statement: Are there any plans to match the SI units set in Aspen Plus to the standard SI? | Solution: The SI units in Aspen Plus use the following units of measure:
Length is in meters
Mass is in kilograms
Time is in seconds
Moles are in kgmol
Combinations of the above units are used for all other derived units.
In the SI units set in Aspen Plus or Aspen Properties, molar properties are defined using kmoles rather than moles (standard SI), to correspond with the mass unit of kilograms. This ensures that molecular weight has the same value for all units sets, without the need for a conversion factor (1 lb/lbmol = 1 kg/kgmol).
We have no plans to change the SI unit set to use mole instead of kg-mole since it would break all existing files.
Keywords: unit-sets
units-sets
References: None |
Problem Statement: How do I create and distribute a unit set to be used by others? | Solution: You can create your own customized units sets and distribute it to others by creating a template. Create a new simulation case using General with Metric or English units templates depending on your needs. Then, go to Unit sets at top under Home ribbon and create New . Then, modify the units as desired.
Â
Once you have finalized the units, save this file as a template file (.apt) format.
Distribute the template file to the end users.
Keywords: Company Units sets, Template file, .apt format
References: None |
Problem Statement: It is possible to publish standard Process Explorer plots to aspenONE Process Explorer.
This Knowledge Base article shows how it is done. | Solution: · In Aspen Process Explorer click the Tools tab
· Select Plot Utility icon in the Ribbon
· Plot Utility dialog box opens
· Define File or Folder path to where your Process Explorer plot files are saved
· Define the Destination path – Public or Private
· Click Export XML to publish the plot to aspenONE Process Explorer
The value that goes into the Destination field in the above dialog box will vary according to the following four scenarios:
Aspen Process Explorer and aspenONE Process Explorer (A1PE) web server version 8.8 and older on the same system: C:\inetpub\wwwroot\AspenTech\ProcessExplorer\Files\Public
Aspen Process Explorer and aspenONE Process Explorer web server version 8.8 and older on different systems: the path in the Destination field should be a UNC path similar to \\CastleBlack\c$\inetpub\wwwroot\AspenTech\ProcessExplorer\Files\Public where CastleBlack is the name of the A1PE server
Aspen Process Explorer and aspenONE Process Explorer (A1PE) web server version 9.0 and newer on the same system: C:\ProgramData\AspenTech\A1PE\Files\Public
Aspen Process Explorer and aspenONE Process Explorer web server version 9.0 and newer on different systems: the path in the Destination field should be a UNC path similar to \\CastleBlack\c$\ProgramData\AspenTech\A1PE\Files\Public where CastleBlack is the name of the A1PE server
Keywords: None
References: None |
Problem Statement: What is the use of table _BIASRESULTS in APS? | Solution: This table contains the biased and unbiased simulation results for a stream property. The following are the steps on how to configure and work with this table:
1. Add a keyword PUB_BIAS_RESULTS in CONFIG table, and set it as Y;
2. Set scheduled bias for any stream property in screen “Simulator \ Schedule Property Bias…”;
3. Add trend for this stream property to trend list
4. Publish all results. There should have the data in that table
Keywords: Simulation, Stream property, Property Bias
References: None |
Problem Statement: This Knowledge Base article shows how to resolve the following CIMIO timeout errors that occur when DCOM configuration is used.
CIMIO_USR_GET_RECEIVE, Error receiving a GET reply from device
CIMIO_MSG_RECV_TIMEOUT, Time-out trying to receive a message | Solution: There should be a user account on the OPC server machine which has the same name and password as the user account which started the OPC client (Asyncdlgp.exe). User name and/or password mismatch causes the above error.
To fix this problem, create or modify a user account on the on the OPC server to match the username and password on the OPC client.
Keywords: DCOM
timeout
time out
References: None |
Problem Statement: How will PIMS calculate property values of blended crude defined in table CRDBLEND while in Table ASSAYS, property values are entered for this blended crude? | Solution: CRDBLEND table is used to create a new crude from a blend of one or more crudes. PIMS will calculate the property values for the new blended crude linearly based on the fractions of the component crudes entered in table CRDBLEND, even if properties for the new blended crude are also defined in the ASSAYS table. Any such data in T. ASSAYS for new blended crude will be ignored.
For example, MX1 crude is a new blended crude which has 40% of ARL and 60% of AHV. The property value of MX1 will be calculated by property of ARL *40% + property of AHV *60%. The data in the MX1 column shown below will be ignored.
Keywords: CRDBLEND
ASSAYS
References: None |
Problem Statement: Known Issue: In which case does the “Do not allow overlapping crude run events” setting fail?
CQ00769845 | Solution: There is a setting called “Do Not Allow Overlapping Crude Run Events” in Model Settings-> Advanced. As it states, it prevents the overlap of crude run events against a crude unit. However, I noticed that even though I had this setting checked ON, my crude run events could overlap. What could be the reason?
The one case where this setting would fail is when the crude unit has no parameters defined. This can be verified on the flowsheet when you go to the crude unit definition.
If the crude unit has no parameters, like the following screenshot, then the setting will not be obeyed.
The workaround for now is to bring in parameters to the crude unit.
This is targeted to be fixed in upcoming releases of APS.
Keywords: None
References: None |
Problem Statement: I have this parameter unit which tracks cut points of my process unit. What are the different methods by which I can change them? | Solution: Method 1: Using the Gantt Screen and Unit Operation Event
Add PM1 to the corresponding event screen’s control variable list
2. Add a unit operation event on PM1, and change the cut points as per the time stamp
Method 2: Using Excel Units Workbook
The only challenge with this approach is to make sure the bias is applied in the right excel worksheet (to make sure the bias is applied in the right time)
When you identify the right worksheet, you can insert a row in the #RESULTS section of the sheet
Since in this example, the unit PM1 has 4 parameters, you can have your biasing calculation in the 4 highlighted cells (column D for parameter 1, column E for parameter 2 and so on)
This is the more dynamic approach, as this process can be automated. You can bring in the inputs for calculating this bias either in the #INPUT section (if it is an APS variable) or below the #END of the corresponding worksheet.
Keywords: None
References: None |
Problem Statement: How do I seclude the APS excel instance as a separate instance? | Solution: APS, as already known, always opens with an excel instance. If you open the excel units workbook when APS is open, the title bar will say Excel for APS as per the following screenshot
In v8.8 and above, any external excel files opened will also be tied to the excel for APS (by default)
For example, if the user opens APS, and five other excel sheets, in the task manager there will still be just one instance of excel.
This is default behavior. On some occasions this can impact simulation speeds, and could interfere with the wrong instances of excel while executing a user-calc.
To separate the APS excel instance from the rest of the excel workbook instances, use the following keyword in the CONFIG table: IGNORE_REMOTE_REQ and set this keyword a value of 'Y'
When APS is loaded the next time onwards, all other external excel instances will be created separately. For example, if the user opens APS and another external excel sheet, the task manager will now show two separate instances of Excel, one for APS and the other for the external workbook.
Keywords: None
References: None |
Problem Statement: Why am I unable to run a distillation column without a condenser?
There is a Completion Status message: Feed (or pumparound stream) to the top stage must be specified when Condenser=None or Condenser Duty=0 (Specifications | Setup | Configuration sheet) | Solution: If there is no condenser and no liquid stream to a column top, the top stage will dry up, which is not allowed in RadFrac. Either a liquid feed stream in stage 1 or a pumparound to the same stage is a required input for the model.
If you define a liquid feed stream on the top stage of the column, remember to go to RadFrac | Setup | Streams Feed streams to select the stream location at the stage 1.
If you decide to add a pumparound, you must go to RadFrac | Configuration | Pumparounds to enter all pumparound specifications, in the same way, remember to specify the pumparound return to stage 1 to ensure that the top of the column does not have any dry stages.
For additional information, please refer to the followings Knowledge Base articles:
Severe error in distillation columns without a condenser: a liquid feed/pumparound to the top stage is required
What happens if there is no reboiler and no vapor stream to the column bottom?
Keywords: RadFrac, Condenser=None, Condenser Duty=0, feed (or pumparound stream) to the top stage must be specified.
References: None |
Problem Statement: How does HYSYS calculate the Enthalpy of a stream? | Solution: The enthalpy reference state used in HYSYS is the heat of formation of an ideal gas at 25 C. You can view this value in the Basis Environment, Point tab page of a pure component as Heat of Form (25 C). For a stream made up of multiple components, the reference state will be the sum of the individual heats of formation of the components multiplied by the mole fraction of the component in the stream. The heat of formation is usually in large negative numbers. That is why the stream molar enthalpies are large negative numbers.
Then, there are basically three parts to the enthalpy calculation in HYSYS.
1. Ideal Gas Enthalpy: If a stream were in its ideal gas state at 25C, then its molar enthalpy would be exactly equal to the ideal gas heat of formation at 25C. But, if the stream were at any other temperature, its Ideal Gas Enthalpy change caused by the change in temperature will be determined using the equation on the Tdep tab page of the pure component view (a+bT+cT^2+...+fT^5).
2. Enthalpy Basis Offset: The reference basis for the Ideal Gas Enthalpy equation is Ideal Gas at 0 K and therefore must be converted to the enthalpy reference state used in Aspen HYSYS (i.e. Ideal Gas at 25?C). For that purpose there is the Enthalpy Basis Offset which can also be found on the Point tab of a pure component. We call this term Hoffset. Therefore, the ideal gas enthalpy at a given temperature (Hid) can be expressed as Hid = Hoffset + (a+bT+cT^2+...+fT^5).
3. Enthalpy Departure: This term accounts for the enthalpy departure of the fluid from ideal gas behavior at the same temperature and pressure, including latent heat, as well as heat of mixing if an equation of state model is used. It is determined by the property package being used. The exact equations used are those published in the Aspen HYSYS Simulation Basis Guide Appendix A. Let us call this term Hdep.
Therefore, answering the above question: StreamEnthalpy = Hoffset + (a+bT+cT^2+...+fT^5) + Hdep
Keywords: Enthalpy, reference state, enthalpy departure, ideal gas
References: None |
Problem Statement: How to Create a Memory Dump for 32bit AspenTech Applications | Solution: Step 1.
For Orion, MBO and Olefins, you may see a dialog showing the reason why the application is crashing. Press the PrtScn key to caputure a screen shot to record this information, and the application window.
Click on OK, and you will see the following window. For some other applications, you do not see the above window.
Step 2.
You need to start Task Manager at C:\Windows\SysWOW64\taskmgr.exe. This is a 32bit program better for dumping our 32Bit applications. Do not use the one from Taskbar or Ctrl+Alt+Del.
Step 3.
Right-mouse-click your application and then Create dump file.
Step 4.
Send the screen shot, and the dump file to us to analyze the crash.
Keywords: None
References: None |
Problem Statement: What is the significance of Time Period Settings in an APS/MBO model? | Solution: APS will calculate material/property balances at every time period that it creates. With more time periods, there are more balance equations, and therefore more detail. However, more periods have a negative impact on simulation speed. The challenge is to leverage the amount of detail and the simulation speed.
The number of time periods created by APS is what you control in set period settings.
Initially, APS constructs the time periods, which are event start or stop times, based on the settings on the top half of the set periods tab.
Then it evaluates the minimum period lengths, as per the settings in the second half of the tab.
From the above, it filters the time periods it creates from the first tab. It doesn’t look at event start/stop times. However, there are mandatory periods created by APS, regardless of these settings for:
- The 12 AM midnight (or whatever the beginning of day offset is)
- For crude run events
Keywords: None
References: None |
Problem Statement: Is it possible or advisable to run two different versions of APS/MBO against the same DSN? | Solution: This scenario will not be possible if:
- One of the two versions are after v8.7, and the other version is before 8.7 AND
- The model has pipelines
If the model does not have pipelines, an APS/MBO database is backward compatible (meaning a v9 database can be opened successfully in v7)
Though from the database side, this may sound feasible (because for a model with no pipelines, a v9 database can be opened in v7.3 and the user can still navigate around), we would still not recommend this from the software behavior’s side. Especially with functionality changes/ bug fixes on a specific feature, the same database is now subject to two different behavior from two users on different APS versions, and this could lead to confusion in results and usability.
Keywords: None
References: None |
Problem Statement: An error is received after selecting the Test Connection button on the AFW Security - Configure Data Source screen
The main screen displays the status:
Error number: 80040e4d
Authentication failed. | Solution: AFWDB data source missing. Please create it manually.
1. Go to ODBC Data Source Administrator(32-bit)
2. Click on System DSN tab
3. Click on “Add” button to create new data source
4. Select Microsoft Access Driver(*.mdb) and click on “Finish” button.
5. Type a Data Source Name, i.e. AFWDB
6.Click on “Select…” button , locate to C:\Program Files (x86)\AspenTech\Local Security\Access97
7.Select AFWDB.mdb, then click on OK
8.Click on OK, you will see a new data source AFWDB has been created.
9.Test connection again
Keywords: 80040e4d
Authentication failed
References: None |
Problem Statement: A user does not wish to display certain stream components in the Composition page of the Workbook. However, if these columns are deleted, the calculated compositions for all other components appear as <empty>. | Solution: If the user chooses to delete a stream column in the Compositions page of the Workbook, This will be deleted in the main flowsheet Thus, the flowsheet will be unable to solve completely. This is not a defect, but the way the Workbook is implemented.
User should select the option ‘Hide object’ instead. This makes the column disappear in the workbook, while retaining the values for the non-displayed stream in the flowsheet.
Keywords: Workbook, composition, stream, page, hide, delete
References: None |
Problem Statement: How do I model pipeline pressure surge analysis using Aspen HYSYS | Solution: 1. The Pipe Segment model (part of standard HYSYS) has a slug analysis section on the Flow Assurance tab. This capability will analyze the potential flow conditions (flow, pressure drop, amounts of liquid and vapor, elevation changes) and predict if slugging could occur and how big the slugs may be.
2. To do a proper job of modeling the actual slugs and their impact dynamically, one can model the pipeline using dynamic simulation capabilities of Aspen Hydraulics (a part of Aspen HYSYS Upstream).
3. Aspen HYSYS Hydraulics capabilities estimates the performance and slugging behavior of pipelines. However, users can model using OLGA from SPT Group. This is also tool for slug prediction and modeling of multiphase pipelines that are common in off-shore oil & gas production. Aspen HYSYS Upstream Dynamics has an old link (OLGA 5.3.2) that allows an OLGA model of the pipeline to work with an Aspen HYSYS Dynamics model of the rest of the gas-oil production process.
The sample files are attached.
Note: OLGA needs license for Aspen HYSYS Hydraulics and license from OLGA (SPT group) to run in Aspen HYSYS. Also we have tested the above feature in OLGA 5.3.2. If you are using later versions and find any issues, report it to AspenTech Support.
Keywords: Slug flow, pressure surge, Flow surge
References: None |
Problem Statement: A customer is developing a custom portal view with all the input boxes and display elements of a standard aspenONE Process Explorer plot hidden except for the trend plot itself once called.
This knowledge base article shows how to format a URL that will hide different display elements of A1PE plot and display just the trend plot. | Solution: aspenONE Process Explorer supports the following URL settings/switches:
ShowLegend=0 or 1 (no or “yes”)
ShowTimeline
ShowChart
ShowTagInput
Below is a usage example that will display only the following trend plot: A1113D.appid-1.pt-1.cat-1.def-0.s-a.xml
http://localhost/ProcessExplorer/WebControls/PBPlots.asp?outsidea1=graphic&PlotFile=Public/A1113D.appid-1.pt-1.cat-1.def-0.s-a.xml&ShowLegend=0&ShowTimeline=0&ShowTagInput=0
Keywords:
References: None |
Problem Statement: Couldn’t be able to run the PIMS model under Chinese character folder with the following error: | Solution: Problem could be resolved in the following way:
1.Change the system locale to Chinese on the Administrative tab. Then restart the machine.
2.Set the Format to Chinese on the Format tab.
Both DR and AO would be able to read the Excel tables from PIMS model with Chinese character, and the Chinese characters would show up in the FullSolution reports.
Keywords: Chinese character, PIMS model
References: None |
Problem Statement: How do I regress Activity Coefficient data? | Solution: In this example, NRTL will be used as the base property method. Two components were selected for which the database does not contain binary interaction parameters. They were chosen arbitrarily to illustrate the results of this exercise.
The first step is to create a mixture Data Set and input the Activity Coefficient data. Select Gamma as the Data type. Select the two components by moving them to the list on the right. Inputting a value for constant temperature or pressure is optional.
Click the Data tab and input the Activity Coefficient data.
After the Activity Coefficient data has been input, the next step is to regress the data. First, go to the Home tab in the ribbon if not already there. Then, switch the Run Mode to Regression. Create a new Regression and select the previously created Data set.
Go to the Parameters tab and select Binary parameter for the type and NRTL for the name. For the element, please see the table below. Normally elements 1 or 2 are regressed, and sometimes both if necessary. Element 1 refers to aij and aji, element 2 refers to bij and bji, etc. Note that each element must be listed twice with the components reversed to regress both the ij and ji parameters.
After the regression setup is complete, click the Run button in the top ribbon. You can now view the results of the Regression. Also, by default, the parameter values are written back to the NRTL-1 form and will be used in calculations using the NRTL property method.
Key Words
Activity Coefficient, gamma, regression, regress, binary interaction parameters, NRTL, data set
Keywords: None
References: None |
Problem Statement: When using a Data fit block, how would you deal with the situation where one of the Input variables is a spec variable in a Design- specification? | Solution: If an input variable is the spec in a design specification, you will need to switch the Input/Result label in the Data Fit. In the attach example, a heat exchanger block is used to regress the value of the
Keywords: regression fit design-spec target goal manipulated
References: Heat transfer coefficient (U-REF) by tracking the value of the inlet flows and the outlet vapor fractions. The model with just the heat exchanger would have the following structure:
Where the blue values are specified (Input) and the red values are calculated by the model (Result).
However, when you apply a design spec (e.g. manipulating the FWATIN until a certain VF MEOH is achieved), what was originally a specified value becomes a result and vice versa:
Therefore, in the Data Fit block you can would need to specify the FWATIN as a Result variable and VF MEOH as an Input. You may run into the situation where the target variable of the design spec is not directly accessible in the variables tab of the Data Fit block (like in this case, where you cannot specify the target value of VF MEOH directly as a value). To overcome that problem, you would need to use a global parameter variable (In this case Parameter 1 is used) so that you can access the DS spec from the Data fit block.
Also, on the calculation sequence you will notice that the Data Fit regression steps are solved on the upper level and the design spec solver is nested inside. This means that the design spec block is solving completely every time the Data Fit is doing a Flowsheet pass. |
Problem Statement: When a simulation file that includes a Excel calculator block is saved as a *.bkp file, another embedded file will be generated (*.apmbd). When a special character such as ä, ö or similar, are present in the path where the file is located (for example: C:\Users\mayordom\Desktop\Temporär), the software cannot read the embedded file as the presence of these characters is not compatible with the Fortran language used in Aspen Plus (please refer to the | Solution: ID 144587). Thus, the following error message is displayed:Solution
Avoid the use of special characters in the file name or any folder included in the path. If the file is saved as a document file *.apw or as a compound file *.apwz, then the error is not reproducible as the embedded file is not created separately.
Keywords: Excel calculator, error.
References: None |
Problem Statement: This article discusses how to configure InfoPlus.21 to use OPC server time stamp for get records. | Solution: User can follow below manual steps to change existing records in case IP.21 server time is used for IO time stamp by default.
1, In InfoPlus.21 Administrator, Cim-IO, IO_Timestamp_SRC, we can specify whether timestamp comes from Cimio Client (IP.21 server), or Cimio Server.
2, User will need choose from ‘Cimio Server’, then go to C:\Program Files (x86)\AspenTech\CIM-IO\io\cio_opc_api\OPCProperties.exe, choose ‘OPC server time’.
3, 2nd step can also be done by selecting ‘OPC Server Time’ in CimIO Interface Manger.
Keywords: OPC server time
IO time stamp
IP.21 server time
References: None |
Problem Statement: The default pump unit operation in Aspen HYSYS is based on a centrifugal pump. In the industrial environment, reciprocating pumps are used in many cases. So, how can reciprocating pumps be simulated using Aspen HYSYS? | Solution: Aspen HYSYS does not differentiate between centrifugal or reciprocating pump during simulation when calculating theoretical power requirement. You can supply a Q vs H as a vertical line as Q is independent of the required pump head in case of reciprocating pump simulation. Note that Aspen HYSYS has more flexibility on centrifugal pump than reciprocating pump as in Dynamics- you are allowed to include NPSH curve. For simulating reciprocating pump in dynamics refer toSolution id: 000029305.
How to setup reciprocating pump or positive displacement pump
https://esupport.aspentech.com/S_Article?id=000029305
Keywords: Pumps, Reciprocating, Centrifugal, Head, Flow rate
References: None |
Problem Statement: This article provides you a way to display current time in a Graphic designed by Aspen Process Graphic Editor. You can adjust the timestamp format by changing the SQLplus query if needed. | Solution: 1- Go to Aspen SQLplus, Create a query
WRITE CAST(CURRENT_TIMESTAMP AS CHAR FORMAT 'DD-MON-YY HH:MI:SS')
2- Click on the Menu Record | Save As...
3- Type a name such as My_Clock , select QueryDef, click on Create
Select TSK_IQ1, click on OK
4- Go to Infoplus.21 Administrator, search for the record My_Clock ,set #SCHEDULE_TIMES and #OUTPUT_LINES to 1
5- Double click on #SCHEDULE_TIMES, SET SCHEDULE_TIME to a future timestamp, for example: after 5 minutes. set RECHEDULE_INTERVAL to 1 sec.
After five minutes, you should be able to see the current timestamp in #OUTPUT_LINES
6- Go to Aspen Process Graphic Editor, add a Data field object, double click on it, go to Data Source tab,
type Tag Name: My_Clock, Attribute: OUTPUT_LINE, click on Apply | OK.
you will see the current timestamp and it updates every 7 seconds by default.
Keywords: Current timestamp
timestamp
process explorer
graphic
References: None |
Problem Statement: How do I enable Extrapolate for Aspen Calc calculations' parameter using an Aspen InfoPlus.21 query? | Solution: In Aspen SQLPlus, use View /
Keywords: Aspen Calc
Aspen SQLPlus
Extrapolate
References: s... menu option to add references to the CalcScheduler and Aspen Calc Components:
Click on the Ok button and copy the following code into the query writer:
LOCAL CALCCMD, CALCNAME, CALCULATION, FOLDERNAME,GROUPNAME, APARAMETER, NEWPARAM, NEWTAGNAME;
CALCCMD = CREATEOBJECT('CALCSCHEDULER.CALCCOMMANDS');
FOLDERNAME = 'folder1'; --CHANGE FOLDER NAME AS NEEDED
FOR EACH CALCNAME IN CALCCMD.GETCALCULATIONLIST DO
IF CALCNAME LIKE '%'||FOLDERNAME||'%' THEN
CALCULATION = CALCCMD.GETCALCULATIONOBJECT(CALCNAME);
FOR EACH APARAMETER IN CALCULATION.PARAMETERS DO
IF APARAMETER.SOURCE LIKE '%'||'IP21'||'%' THEN
WRITE 'CALCULATION_NAME: '||CALCNAME;
WRITE 'SOURCE: '||APARAMETER.SOURCE;
APARAMETER.SETUSINGDATASOURCEANDMAP('NODE01', NEWTAGNAME, ''); --NODE01 IS DATA SOURCE
APARAMETER.EXTRAPOLATE = -1; --ENABLE EXTRAPOLATE SET TO -1 AND DISABLE EXTRAPOLATE SET TO 0
CALCCMD.SAVECALCULATIONOBJECT(CALCULATION);
END;
END;
END;
END;
Leaving the FolderName blank (FolderName='';) will changes all Aspen Calc calculations. Enable Extrapolate set to -1 , Disable Extrapolate set to 0 |
Problem Statement: How can I quickly create a new SQL database for PIMS results? | Solution: In Aspen PIMS V11, there is a new feature that allows users to perform many tasks related to their SQL database. The new feature can be accessed within PIMS by going to TOOLS | SQL Server Management Tool as shown below.
To create a new SQL database simply click on the + icon.
In the Database Name window, type the desired name for the new database.
In the Server Name window, use the drop down arrow and select the appropriate SQL server
Click Create.
Once the database is created, you will see it added to the list. You can now configure PIMS to output results to this SQL database via the PIMS model settings.
Keywords: None
References: None |
Problem Statement: When starting the aspenOne Process Explorer, the following error message may sometimes appear:
The file Templates/Basic/Trend no longer exists. If it is in your home page preferences or as a Tile then please update those settings.
How can this be resolved? | Solution: This issue is caused by the Trend plot template missing or corrupted. Download the attached trend plot template and paste it into the following directory: C:\ProgramData\AspenTech\A1PE\Files\Templates\Basic . This will overwrite the damaged or corrupted template and resolve the issue.
The name of the Trend plot template is Trend.appid-1.pt-1.cat-1.def-1.s-a.tmpl. It is attached to this KB.
Keywords: aspenOne Process Explorer
Templates/Basic/Trend no longer exists
Trend plot template
References: None |
Problem Statement: How can I perform an isentropic flash in the V-L region? | Solution: A Design Spec block can be used to vary the temperature of a stream to achieve a desired entropy (or keep entropy constant). However, this will not work for all cases.
Consider you are working with a pure component (rather than a mixture) and the desired entropy lies inside the V-L region. For pure components at a fixed pressure, phase transitions are isothermal. This means that Aspen Plus, at any given temperature will assume the stream is either completely a liquid, or a vapor, so changing the temperature of the stream will not help reaching the desired entropy.
Instead, enthalpy (which does change in the V-L region) can be adjusted to achieve the specified entropy.
This example attempts to do the following: Keep the entropy of a stream constant by adjusting the duty (enthalpy) in a heat exchanger. The initial conditions of the stream were selected on purpose to fall inside the V-L region.
Description:
The model only contains water. The initial conditions are VF=0.5 and 1 bar
A HEATER block is used to change the enthalpy of the stream (Duty). Outlet pressure is 0.5 bar
A DESIGN SPEC is used to calculate the enthalpy change (Duty) needed to keep entropy constant
The example file is attached
Keywords: Entropy, isentropic, enthalpy.
References: None |
Problem Statement: How to regress PSRK parameters from Liquid Vapor Pressure data. | Solution: In general for Equation of State methods, the model specific critical constants and ideal gas heat capacity (CPIG) parameters can be regressed to fit pure component data. The pure component behavior and parameter requirements used by the PSRK method are described in the help topic Aspen Plus
Keywords: PSRK, Liquid Vapor Pressure, regression, DRS, TCRKS, PCRKS, OMGRKS
References: -> Physical Property Methods and Models -> Physical Property Models -> Themodynamic Property Models -> Equation of State Models -> Redlich-Kwong-Soave and in Soave Alpha Functions. Based on those equations, one should select the specific TC (TCRKS), PC (PCRK) and Omega (OMGRKS) parameters in order to regress Liquid Vapor Pressure data. Remember one should provide initial guesses for the parameters before running the regression.
Attached to this article you will find a regression example for the Vapor Pressure Regression of N-Hexadecanoic Acid (Palmitic Acid) based on experimental data extracted from the NIST ThermoData Engine v8.2 (TDE Wagner 25 liquid vapor pressure). For detailed information on how to access to the TDE data, refer to the article How do I review NIST TDE data from within Aspen Plus? |
Problem Statement: How to Unmatch Imported Events from Existing Events? | Solution: This Tech Tip explains what does it mean to unmatch internal events from existing events, what tables are involved in this process and what is the recommended workflow to use Application ID.
When you unmatch an internal event from an imported event, you are actually deleting the values in columns MOVEMENT_ID and APPLICATION_ID of the application database for the selected event so that the system no longer recognizes the events as matched.
In the attached file you can find further details on this process.
Keywords: None
References: None |
Problem Statement: When using electrolytes is GAMMA on a mole fraction or on a molality basis? | Solution: There are a few prop-set properties that report activity coefficient for an electrolyte mixture.
GMTRUE is the Activity coefficient of a true species (molality scale)
GXTRUE is the Activity coefficient of a true species (mole fraction scale)
GAMMA is the Activity coefficient of a species (mole fraction scale)
The species reported for GAMMA are either the true or apparent species as specified by the property method.
Attached is an example (a modified version of the elec1.bkp file in the Examples directory) that reports GAMMA, GMTRUE, and GXTRUE. If you look at the stream results, the value of GAMMA matches the value of GXTRUE which is the Activity coefficient of true species on a mole fraction scale.
Units HCL LIQUID MIXED NAOH
Description
From FLASH MIX
To MIX FLASH MIX
Stream Class CONVEN CONVEN CONVEN CONVEN
GAMMA_Activity coeff of true species, molality scale
WATER 0.661488 0.725059 0.894435 0.699744
HCL 0.008912 0.033624 0.084196
NAOH
H3O+ 1.482626 0.835058 0.546605 0.782798
NA+ 0.867506 0.720734 0.945549
NACL(S)
CL- 1.482626 0.896695 0.738323
OH- 0.897726 0.478966 0.415875 0.945549
GAMMA_Activity coeff of true species, mole fraction scale
WATER 0.808486 0.915467 0.988137 0.853688
HCL 0.010892 0.042453 0.093017
NAOH
H3O+ 1.812098 1.054354 0.603869 0.955013
NA+ 1.095322 0.79624 1.153569
NACL(S)
CL- 1.812098 1.132176 0.815671
OH- 1.097221 0.604748 0.459442 1.153569
GAMMA_Activity coefficient
WATER 0.808486 0.915467 0.988137 0.853688
HCL 0.010892 0.042453 0.093017
NAOH
H3O+ 1.812098 1.054354 0.603869 0.955013
NA+ 1.095322 0.79624 1.153569
NACL(S)
CL- 1.812098 1.132176 0.815671
OH- 1.097221 0.604748 0.459442 1.153569
Keywords: None
References: None |
Problem Statement: Can I run Multi-Start in a Multi-Plant Model? | Solution: This Tech Tip gives a brief description of how to run Multi-Start Analysis in Multi-Plant Models.
Multi-Start is one of the different methods of comparison of Global Optimization and is one of the feature available in the Aspen PIMS Advanced Optimization package (PIMS-AO), it is available for Multi-Plant model. Mutli-Start is a one step automatic process that can work with any model with any type of nonlinearities
This tool will allow you to test theSolution by starting from different initial points. All you have to do is turn on Global Optimization to run the exceuction Dialog box.
While most users keep the default settings, if you want to change some of the default Multi-start options, those can be accessed as follows:
1. Expand the Model Settings branch of the model tree, and double-click XNLP to display the XNLP Settings dialog box.
2. Click the Global Optimization tab.
3. Select Perform Global Optimality, and then click Multi Start Only.
4. Click Multi Start.
Multi-Start Results
You can observe the results that were obtained by testing different initial points by case, in this example we ran Case1 and Case 6
Keywords: None
References: None |
Problem Statement: aspenONE Alerts is a web application that provides an easy way to subscribe to the alarm states of various tags. When the tag reaches that alarm state, it will be added to the Alerts page in aspenONE Process Explorer, allowing for easy monitoring.
When e-mail alerts are enabled for an alert subscription, you will receive an email each time the subscribed tag reaches an alert state.
However, some users prefer to receive an SMS message on their phones rather than getting an email message.
This knowledge base article shows how to configure the Alert application to send SMS messages instead of email notifications. | Solution: To designate a phone number for alert subscriptions:
From the Alerts application, click the envelope icon on the aBar. The Alert Subscription dialog box opens.
In the E-mail box enter the phone number syntax instead of the user's email address. An example of such a syntax is shown below. (Note: The syntax will be different for different phone service providers. Please contact your phone service provider for the exact syntax.)
To enable SMS alerts, select the ‘Receive e-mails when an alert is issued’ check box on the Alerts tab of the Tag Detail dialog box or on the Multiple Alert Subscription Settings dialog box, as shown below:
Note: If there are issues sending the SMS messages from the Alerts page, please make sure your SMTP server is configured to allow SMS messages to pass through. See the following article for more details:
https://www.digitaltrends.com/mobile/how-to-send-a-text-from-your-email-account/
Keywords: Text messages
References: None |
Problem Statement: Would like a list of all Standard CIMIO Interfaces(Sold by AspenTech and supported by Aspen Tech Support). | Solution: Standard CIM-IO Interfaces (Effective July 1th 2006).
*** IMPORTANT NOTICE ****
This list contains standard interfaces, in the sense that they are sold by Aspen and supported by our support team.
CIM-IO FOR DOW MOD DCS via MIF is no longer supported a supported Interface and is no longer included in this list.
CIM-IO for Bailey semAPI
CIM-IO for Fisher-Rosemount CHIP
CIM-IO for Fisher-Rosemount RNI
CIM-IO for Foxboro FoxAPI
CIM-IO for Measurex ODX
CIM-IO for OPC
CIM-IO for PI
CIM-IO for RSLinx
CIM-IO for Setcim/InfoPlus-X/InfoPlus.21
CIM-IO for Westinghouse
CIM-IO for Yokogawa ACG
*** IMPORTANT NOTICE ****
This list contains standard interfaces, in the sense that they are sold by Aspen and supported by our support team.
Keywords: CIMIO
Interface
References: None |
Problem Statement: How do I resolve the error when Excel does not load COM Add-ins, even after they have been enabled? | Solution: Check the registry key:
HKEY_CURRENT_USER\Software\Microsoft\Office\Excel\Addins\ AspenTech.PME.ExcelAddin.Process Data\LoadBehavior
It should be set to 0x0000003(3). This directs Excel to load the Add-Ins when starting. If it is not then change it to a value of 3.
If this does not resolve the problem then to be able to troubleshoot, add an environment variable to the user session, the variable name is VSTO_SUPPRESSDISPLAYALERTS. Set its value to 0.
Once this variable is declared, next time Excel is started a pop-up message should appear that will give a detailed version of error it encountered while trying to load the COM Add-in. You may then forward this output to AspenTech Support for further analysis.
Keywords: Failed to load
Addin
Disabled
References: None |
Problem Statement: What is the difference between static pressure and total pressure? | Solution: Starting with version 3.0 of FLARENET, the static pressure is shown by default rather than velocity (dynamic) pressure or total pressure. If you select the Display total pressure check box on the General tab of the Preferences Editor, the total pressure is displayed instead.
Static pressure (Ps) is the pressure acting equally in all directions at a point in the fluid. Physical properties are calculated at the static pressure condition.
Velocity pressure (Pv) (also known as kinematic pressure or dynamic pressure) is given by the term:
Pv = (rho * V^2) / 2, where
rho = fluid density
V = fluid velocity
Using SI units (kg/m3 for density and m/s for velocity), velocity pressure is calculated in Pascal.
In FlareNet outputs, the (rho * V^2) term is reported. Pv is half this value(corrected by the appropriate unit conversion factors).
Total pressure (Pt) is the sum of the static and velocity pressures.
so Pt = Ps + Pv
Keywords: Static pressure, Total pressure, Dynamic pressure, Kinematic pressure, Velocity pressure
References: None |
Problem Statement: How can I manage the cases in my Aspen PIMS SQL database? | Solution: In Aspen PIMS V11, there is a new feature that allows users to perform many tasks related to their SQL database. The new feature can be accessed within PIMS by going to TOOLS | SQL Server Management Tool as shown below.
When the SQL Database Management Tool opens, make sure you are displaying the desired database. If your database is not shown in the upper left section, then click the magnifying glass icon to find and select the desired database.
Once your desired database is listed, you can see the contained cases in the right side panel.
Use the lower left section to apply filters for the cases you want to delete from the database. You can filter by Date Range of the run,Solution ID, Case ID, Model Directory, User name, and Machine name. The example below shows dates and case numbers as the filter criteria. Once your criteria are set, click the filter icon (see red box) to apply them and the right side panel will update accordingly.
Once you have selected the desired cases by checking the corresponding box on the left, you can apply one of the 3 icons at the top. The options are:
Delete the selected cases (red box)
Export the selected cases to a different database (blue box)
Export the selected cases to Excel (green box)
Keywords: None
References: None |
Problem Statement: Overview of Firewall security, Antivirus scanning and Windows permission requirements for APC Products | Solution: Follow our permission checklist to make sure machines and networks are configured with required permissions.
Windows Permission requirement
APC Server applications requires service account during installation. This service account needs to have local and domain administrative privileges.
Aspen Process Control Desktop Application user's needs to have read privilege to the system registry while using the application. Admin privileges will only be required during application installation and configuration.
Windows and Network Firewall requirement
Windows and Network firewall needs to be configured to allow specific ports communication for our application. View KB: 20700 for detailed firewall ports requirement.
Give exception to AspenTech Support website and support email address to use our support resources. View KB:45773 to give exception to access AspenTech Web Content.
Anti Virus Scanning requirement
Antivirus software scanning APC Server and Desktop applications can affect the performance of our application. Giving exception to Anti Virus software will optimize the performance. View KB:47912 for giving exception to application files and folder.
Keywords: security configuration
security requirement
References: None |
Problem Statement: Aspen Tag Browser on a workstation gives error No data sources found. Please check ADSA configuration and it won't show any servers, while the Aspen Process Explorer and the Process Data Add-in work fine along with the ADSA test. | Solution: The issue occurs when the user has configured the Aspen Tag Browser to connect through the MES Web Server.
You can fix this in Aspen Tag Browser | View | Options | MES Web Server, and uncheck the Use MES Web Server option. The error message will disappear after you uncheck the option.
Keywords: Configuration
No data sources found
Tag Browser
Uncheck
References: None |
Problem Statement: What is the time span (t1 and t2) meaning in the aspenOne Process Explorer (V11) page saving URL?
In the aspenOne Process Explorer V11, after we saved a trend/plot, we are able to copy the URL of the trend/plot and share it to the A1PE in the other machines.
Here is a sample of the saved URL: http://vmhongya1/processexplorer/aspenONE.html?ProcessExplorer?nav=true&file=Public%2Furl%20testing.appid-1.pt-1.cat-1.def-0.s-a.xml&t1=1567696324794&t2=1567703524794.
What is meaning of t1=1567696324794&t2=1567703524794 ? | Solution: The time span t1 and t2 in the aspenOne Process Explorer page saving URL is the Unix Epoch Time.
For the URL sample above:
t1=1567696324794 = Thursday, September 5, 2019 10:12:04.794 AM GMT-05:00 DST
t2=1567703524794 = Thursday, September 5, 2019 12:12:04.794 PM GMT-05:00 DST
Here is a link you could convert the Unix epoch time to the readable time: https://www.epochconverter.com/
Keywords: aspenOne Process Explorer
Page saving URL
Unix Epoch Time
References: None |
Problem Statement: What is the best way to control the composition or quality of a recursed pool? | Solution: In the past some have used the PIMS blending tables to setup and control the properties of a pool such as a reformer feed pool. While this is possible, it is not ideal. The best way to control properties of a recursed pool, is to create the recursed pool in a submodel and use Process Limits (defined in Table PROCLIM) to define the constraints.
The example below shows a simple recursed pool (RFP) being created from 3 naphtha streams. There are 2 qualities that need to be controlled (N+2A and the % of NA1 in the pool). Recursion rows have been defined to calculate these 2 qualities. In order to apply minimum and maximum constraints, corresponding process limit rows are also defined. The desired limits are then defined in Table PROCLIM as shown.
Note that when calculating a composition such as the % NA1, it is important to put zeros for the other components of the pool in the process limit row in the submodel. This directs PIMS to include those column activities in the denominator, even though they are not in the numerator. This is not needed in the recursion row.
Keywords: None
References: None |
Problem Statement: How do I suppress the message box: Do you want to save changes to Units.xls? | Solution: There is a setting keyword DO_NOT_SAVE_EXCEL that can be used in the CONFIG table, with a value of Y.
This keyword can be used for both APS and MBO.
From the next launch, APS/MBO will suppress the excel save dialog prompt while closing the software.
Keywords: None
References: None |
Problem Statement: How do I use the Spot Crude Evaluation feature in PIMS Assay Management? | Solution: 1. Start Assay Manager
2. Click on the Spot Crude Evaluation button on the ribbon
3. Find and select the desired crude, then click on “Use Selected Assay”
4. On the “Setup Evaluation” tab fill in the appropriate data. Typically, we would use case 1 (Base Case) for the reference case and run the analysis for the desired quantity of the selected crude and also specify the cost of the crude. Then select the crude units that this crude can charge, which will make the necessary entries in the CRDDISTL table.
5. Hit on Run Evaluation. If we notice, in the background PIMS will run a new case with this crude. Review the results. PIMS will evaluate the break even price for the crude, the new crude slate and the major constraints. A chart similar to the following figure will be generated, and we can choose to abort this case, or save it for future reference.
Keywords: Assay Manager, Spot Crude Evaluation
References: None |
Problem Statement: There are so many parameters used in UNIQUAC activity coefficient model in Aspen Plus. How should I understand them, and how does Aspen Properties regress these coefficients? | Solution: Aspen uses the normal UNIQUAC equation:
Where
Although this UNIQUAC equation looks a little complex, it only has 2 adjustable parameters: τij and τji. They are the binary interaction coefficients, and are dependent of temperature. In real simulations, only τij and τji need to be regressed using experimental data.
All the others are constants of pure chemicals which you cannot adjust or regress. They are already in Aspen databank. ri is the relative Van der Waals volume, and qi is the surface area. They are related to the molecular structure of the pure species. Z is the coordination number, i.e. the number of close interacting molecules around a central molecule. Z is frequently set to 10.
You see 7 coefficients in the Aspen Plus UNIQUAC model parameter UNIQ:
UNIQ/1 to UNIQ/7 are all used to regress τij as a function of temperature by the following equation:
with T upper bound and T lower bounds.
You could use experiment data (such as vapor-liquid and liquid-liquid equilibrium data at different temperatures) to regress UNIQ/1 to UNIQ/7. In many cases, you could leave cij, dij, eij, T_lower and T_upper as the default, and only regress aij, aji, bij, and bji . It is important to regress both the ij and ji parameters since they are generally correlated.
Keywords: None
References: None |
Problem Statement: This Knowledge Base article shows how to delete a graphic or a trend published to aspenONE Process Explorer. | Solution: Before MES V9.0
When a graphic or a trend is published to aspenONE Process Explorer, it appears in the Menu Tree but there is no obvious way to delete it from the tree as there is no recycle bin to drag it to or a context menu with the Delete option.
The proper way to delete a graphic or a trend from the aspenONE Process Explorer Menu Tree is to navigate to the aspenONE Process Explorer directory
C:\inetpub\wwwroot\AspenTech\ProcessExplorer\Files\Public
or
C:\inetpub\wwwroot\AspenTech\ProcessExplorer\Files\Private\<username>
and delete the file(s) representing the graphic or a trend.
The graphic files (two per graphic) will have extensions .jpg and .json. The trend file will have an .xml extension.
Then go to the Manage Search Data page, click the Files tab and click Remove Deleted Files. The Manage Search Data administration page can be accessed by entering the following in the browser's address bar:
http://<servername>/ProcessExplorer/WebControls/PBItemDetails.asp?admin=true
After MES V9.0
When a graphic or a trend is published to aspenONE Process Explorer, it appears in the Menu Tree. Right click the graphic name and click Delete option, the trend plot will be deleted.
Keywords: aspenONE Process Explorer
Delete trend plot
References: None |
Problem Statement: It is not always known which Aspen Manufacturing Suite Applications are eligible to have security set in the AFW Security Manager.
Nor is it easy to locate the respective XML files to be imported into the AFW Security Manager. | Solution: Here is the list of Aspen Manufacturing Suite applications eligible to have security set in the AFW Security Manager. Also included is the default location for each XML file:
Process Explorer: C:\Program Files (x86)\AspenTech\APEx\Pe\pe.xml
Process Graphics Editor: C:\Program Files (x86)\AspenTech\APEx\GE\graphic.xml
Aspen Process Graphic Studio: C:\Program Files (x86)\AspenTech\Web21GraphicStudio
AFW Security manager: C:\Program Files\AspenTech\BPE\AfwSnapin.xml
SQLPlus: C:\Program Files\AspenTech\InfoPlus.21\db21\sql\SQLplus_base_security_install.xml
Aspen Production Record Manager (Batch21): C:\Program Files\AspenTech\Batch.21\Server\Setup\Batch21.xml
AspenCalc: C:\Program Files\AspenTech\Aspen Calc\bin\AspenCalc_base_security_install.xml
Advanced Process Control: C:\Program Files\AspenTech\ACOView\
Aspen Audit & Compliance Manager: C:\Program Files\AspenTech\AuditAndCompliance\Server\setup\AuditAndComplianceManager.xml
MES Client Applications (Excel Add-in, aspenONE Process Explorer):
C:\Program Files (x86)\AspenTech\ProcessData\AspenMESClientApplications_AFW.xml
For Aspen Production Execution Manager (AeBRS), no XML file exists. Instead, to add an AeBRS system to an AFW server first check AFW Tools on the AeBRS server to make sure you are pointed to the correct security server, and then double-click on the AFWCreate.cmd file typically located at: C:\Program Files\Aspentech\AeBRS\AFWCreate.cmd
This will create the AeBRS application in AFW, along with a pre-existing set of Roles and Permissions.
Keywords: Applications security
AFW Security Manager
XML
Process Explorer
Process Graphic Editor
AFW Security manager
Batch21
AspenCalc
Advanced Process Control
Aspen Audit & Compliance Manager
SQLPlus
References: None |
Problem Statement: This Knowledge Base article shows how to change the timeline span from within the graphic and be able to get, as variables, the beginning and end timelines. | Solution: In order to be able to change the timeline span from within the graphic, the following java script functions were added to the aspenONE Process Explorer (a1PE) graphics page and are now supported in graphic script actions for a1PE:
setTimeWindow(millisec_T1, millisec_T2)
Description:
The setTimeWindow() method sets the start & end times for the graphic's main timeline.
Parameter Values:
millisec_T1 Required. Start time as number of milliseconds since midnight Jan 1, 1970.
millisec_T2 Required. End time as number of milliseconds since midnight Jan 1, 1970.
getTimelineT1()
getTimelineT2()
Description:
The getTimelineT1() and getTimelineT2() methods get the start & end times for the graphic's main timeline as number of milliseconds since midnight Jan 1, 1970.
Examples:
var dateNow = new Date();
var msNow = dateNow.getTime();
var msYesterday = msNow - (86400 * 1000);
var msTwoHours = (2 * 60 * 60 * 1000);
// pass in T1 and T2 as no. of milliseconds since Jan 1, 1970, 00:00:00 GMT
setTimeWindow(msYesterday - msTwoHours, msYesterday);
// these return the number of milliseconds since Jan 1, 1970, 00:00:00 GMT
var dateT1 = new Date(getTimelineT1());
var dateT2 = new Date(getTimelineT2());
alert(T1 is now: + dateT1.toLocaleString());
alert(T2 is now: + dateT2.toLocaleString());
A timewindowchange event was also added that can be used for custom scripts, to be notified whenever the graphic time window changes. To use, register for it in java script by calling addTimeWindowChangeHandler and passing in your handler function.
Example: Place the following code in the graphic's OnLoad event:
addTimeWindowChangeHandler(handleTimeWindowChange);
function handleTimeWindowChange() { // a test function
var dateT1 = new Date(lastTimelineT1);
var dateT2 = new Date(lastTimelineT2);
alert(T1 = + dateT1.toLocaleString() + T2 = + dateT2.toLocaleString());
}
Also note in the above example the lastTimelineT1 and lastTimelineT2 variables are now available to the a1PE graphics page. These are updated to reflect the current times whenever the timewindowchange event occurs.
It is also necessary to clear up the registration of the event when the graphic is unloaded. Place the following code in the graphic's OnUnload event to unregister the example function:
//--- this will remove the time change handler defined in OnLoad assuming function name handleTimeWindowChange
try {
if ( timeWindowCustomEvent ) {
document.body.removeEventListener(timewindowchange, handleTimeWindowChange, false);
}
else {
timeWindowFunctions[timeWindowFunctionsI] = null; timeWindowFunctionsI--;
}
} catch (twhX2) {}
Keywords: None
References: None |
Problem Statement: Is it possible to simulate the pyrolysis of high density polyethylene (HDPE)? What thermodynamic model should be used? | Solution: Attached is a model of HDPE pyrolysis in Aspen Plus.
Open a new file and start with polymer template.
Add PC-SAFT to the database on the Components | Specifications | Enterprise Database sheet.
Specify HDPE to have a type of oligomer and ETHYLENE-R as segment on the Components | Specifications | Selection sheet. Include any other components desired in the simulation such as PROPANE, PROPYLENE, ETHANE, ETHYLENE, METHANE, HYDROGEN, and ACETYLENE.
On the Components | Polymers | Characterization form, specify that the ETHYLENE-R segment is of a type REPEAT on the Segments sheet and specify that there are 1000 ethylene repeat units on the Oligomers sheet.
Specify atom number NATOM on the Parameters | Pure Component form for HDPE as C=2, H=4 (repeat unit basis)
Set the property method to PC-SAFT on the Methods | Specifications | Global sheet.
In the Simulation Environment on the PFD, add an RGIBBS with one feed and one product.
Specify polymer feed rate and thermodynamic conditions for the feed stream.
Enter the RGIBBS temperature and pressure on the block's Setup | Specifications sheet. Define RGIBBS products on the Setup | Products sheet explicitly as all components except the polymer.
The Model shows reasonable product distribution which depends on temperature
Temp Deg C
500
600
700
800
900
1000
PROPANE
0.012
0.017
0.019
0.016
0.011
0.006
PROPYLEN
21.168
18.211
13.958
9.234
5.29
2.73
ETHANE
0.038
0.09
0.155
0.205
0.212
0.181
ETHYLENE
3.271
6.297
9.711
12.19
12.744
11.598
METHANE
0.343
1.206
3.08
6.017
9.296
11.808
H2
< 0.001
0.002
0.021
0.131
0.571
1.864
ACETYLEN
0.394
1.315
3.275
6.368
10.09
13.859
The pyrolysis model has been extended with version 11 to include a wider product slate as well as steam and combustion air injection with heat integration (the hot effluent gas is used to generate steam and pre-heat the combustion air).
The new version of the model includes a sensitivity study (deactivated) which can be used to evaluate how the air/polymer and steam/polymer ratios influence the product gas composition and temperatures.
Keywords: None
References: None |
Problem Statement: I can't delete pipeline route from APS. There is a message: At least one entity (Inv 25549) has used this route thus it cannot be deleted now. | Solution: Routes without any pipeline events can be deleted. If a route has been used by other entities, it should not be deleted and you should get the following message:
To delete a pipeline Route, you can use the following script:
Delete FROM [DBNAME].[dbo].[PLINV_DEST] where PLINV_XSEQ in (SELECT [X_SEQ] from [DBNAME].[dbo].[PIPELINE_INV] where ROUTE_XSEQ IN (1,54,55))
go
Delete FROM [DBNAME].[dbo].[PLINV_COMP] where PLINV_XSEQ in (SELECT [X_SEQ] from [DBNAME].[dbo].[PIPELINE_INV] where ROUTE_XSEQ IN (1,54,55))
go
Delete from [DBNAME].[dbo].[PIPELINE_INV] where ROUTE_XSEQ IN (1,54,55) go Delete from [DBNAME].[dbo].[ROUTE_PLS] where ROUTE_XSEQ IN (1,54,55)
go
Delete from [DBNAME].[dbo].[ROUTES] where X_SEQ IN (1,54,55)
go
The numbers 1, 54, 55 will change based on the user's model.These statements will delete a route from APS that does not have any events associated with it. If any events are associated with that route then those need to be deleted before running the above mentioned script.
We recommend running it when no users are using APS with that model.
Keywords: None
References: None |
Problem Statement: How do I make sure the SQL Database Management Tool is showing the most current data in my database? | Solution: In Aspen PIMS V11, there is a new feature that allows users to perform many tasks related to their SQL database. The new feature can be accessed within PIMS by going to TOOLS | SQL Server Management Tool as shown below.
If this tool is open while you are executing more PIMS runs, the screen data may need to be refreshed. To do this, right click on the database name and select Refresh.
Keywords: None
References: None |
Problem Statement: what is the rules of generating Cable trays for Electrical cable and Instrumentation cable? | Solution: Cable tray type can be selected at area and/or project level. If you don't set the tray length, ACCE system will create E&I cable tray lengths equal to the distances from the area to the motor control and control centers. If the number of runs to the centers require more than one tray, the system will generate multiple tray. Then how does system generate multiple cable trays?
The system increases the number of trays as the tray gets filled with cable.
System will fill cable tray
- One layer
- 80% full, 20% spare
Width can be defined by user
- Default width is 18 inches
- May specify from 6 to 36 inches
The total number of trays needed depends upon the various loads in the area and the cable size required for that load. For each cable size a specific capacity in the tray is filled. As each tray fills up, extra trays of the specified width are estimated. So the total length of the area level cable tray depends on the (number of trays needed) x (Distance to MCC).
Key Words
Cable trays, Electrical cable, Instrumentation cable
Keywords: None
References: None |
Problem Statement: How to add and customize a stream properties table on the PFD? | Solution: The attached pdf document illustrates how to customize the workbook. The attached HYSYS file (openable in V8.8 or later) is used to generate the illustrations.
Keywords: Stream, Table, Worksheet, Workbook, Properties, Variables, sort, hide, display, reveal
References: None |
Problem Statement: How to model a simple reactor for biomass digestion without knowing specific reactions sets and kinetics.
In this situation, when you are building a larger model of installation using biomass combustion products and you don't want to concentrate on complex digestion process, you can simplify that part using RYield reactor. This will allow you to have a working biomass digestion reactor without going into details of reactions kinetics. | Solution: In order to model a simple reactor for biomass combustor, you will need to have data to specify the composition of inlet and outlet stream and properties of biomass (for example laboratory analysis results).
This example is based on the Solids Getting Started Example. This example uses COAL; however, the Ultimate (ULTANAL), Proximate (PROXANAL), and Sulfur (SULFANAL) Analysis is often used to describe biomass. This example is described in the Help under Getting Started with Aspen Plus -> Tutorials -> Modeling Processes with Solids. The completed files can be found in
..\AspenTech\Aspen Plus Vxx\GUI\Examples\GSG_Solids
Steps:
1. Create a new simulation using NRTL or SOLIDS method.
2. Define all biomass as non-conventional components and desired products as conventional components.
3. Specify enthalpy and density property models for each of the non-conventional components. Depending on chosen property model you will need to use different component attributes but there is a possibility to choose additional attributes. Please refer to Help for a detailed explanation of component attributes.
4. Go to the simulation environment and create a RYield reactor model with one inlet and one outlet stream.
5. Specify the feed stream. In order to input biomass properties data go to NC Solid / Component Attribute and enter elements values for all attributes.
6. Specify the RYield reactor. In the Yield tab enter composition of the outlet stream.
7. Add a Calculator to make sure that the mass atomic balance from the Ultimate Analysis is preserved. This Calculator is modeled after the COMBUST Calculator in the Solids Getting Started Example file solids2.bkp, but it has been extended to handle multiple nonconventional components.
8. Run the simulation.
Keywords: Biomass, nonconventional, RYield
References: None |
Problem Statement: How can I automate pump or compressor shutdown during HYSYS dynamic simulation? | Solution: In the attached case Shut down pumps AT.hsc, a spreadsheet Pump control is included which acts as an On/Off switch for each of the two pumps, P-100 and P-101. If a value of 0 is entered in cell B1 or B2, it will shut down pump P-100 or P-101, respectively, via the output from C1 or C2.. To start it up again, enter a value of 1 in B1 or B2. When running the case, turn on the sequence in the Event Scheduler and start the integrator.
In this example, the Event Scheduler waits for 3 hours of elapsed time and then shuts off P-101 by setting the cell B2 to 0 in the Pump control spreadsheet. C2, which equals B2, takes this 0 and exports it to the pump control, effectively disabling it. The effect of turning off the pump may be seen by observing the flow and discharge pressure.
Note that even when the pump is off, in certain circumstances there may still be flow through the line if there is still a significant enough pressure gradient.
In the second attached case Compressor shut down.hsc, the flow controller (IC-100) manipulates the compressor speed. The face plate of this controller is open; to shut down the compressor, enter 0 as the OP value (corresponding to zero speed). To restart the compressor, enter an OP value of 85%. Note that one could also automate the speed changes using the Event Scheduler and the spreadsheet, as in the previous example.
Keywords: automate, pump shutdown, shutdown, compressor shutdown
References: None |
Problem Statement: Occasionally, users have issues when exporting tag data from aspenONE Process Explorer (A1PE) to a CSV file and then importing the CSV file into MS Excel.
This Knowledge Base article shows how to properly import A1PE generated CSV files into Excel. | Solution: Here are the steps to properly import A1PE generated CSV files into Excel:
1. In aspenONE Process Explorer click the Export to CSV icon
2. When prompted by the Internet Browser to open or save the CSV file, choose to save it
3. Next, in MS Excel, click From Text in the Excel Data tab, browse to the file, and click Open
4. A 3-step wizard will appear. Choose the appropriate delimiter, e.g., comma or semicolon (can see delimiter in wizard with preview on how the data will look after import). Also, please note that the CSV file is downloaded as UTF-8. When importing data via the Excel Text Import Wizard, ensure that UTF-8 encoding type is selected in the File Origin list box (see below).
5. The CSV file is successfully imported into Excel.
Note: If Excel automatically opens, close it, and import file following the above instructions.
Note: For MS Excel Office 365, this option is called Text to Columns under Data.
Keywords:
References: None |
Problem Statement: How viscosity of multiple polymer component mixture is handled by Van Krevelen model? | Solution: In Aspen polymer, the van Krevelen binary polymerSolution viscosity model treats a multicomponent polymer mixture as a quasi-binary system consisting of a pseudo-polymer component and a pseudo-solvent component. It takes the average of properties of polymer species and solvent species, respectively.
Pseudo-polymer component is treated as a blend of all polymers and oligomers in the mixture that possesses properties averaged across the components present.
On the other hand, pseudo-solvent component is composed of all present non-polymeric species. The properties of the pseudo-solvent are averaged across the conventional species in the system.
Key Words
Van Krevelen, Viscosity, Polymer
Keywords: None
References: None |
Problem Statement: How to view the equations and coefficients used in Aspen Inferential Quality files, in case of working with an old/ previous IQF or IQM file? | Solution: The inferential sensing application is used to infer the value of a critical process variable or product property, from the values of other process variables and their relationships, which are continuously measured.
This inference yields a model whose corresponding stream of data values simulates the expected behavior of a sensor monitoring the critical variable or property
Thus, IQ model is created as the starting point of building an inferential sensor. The model is built with using the continuous process (temperature, pressure, flow etc.) data & laboratory or analyzer data, both as input data.
Many equations or formula are also used in the
If there is any formula used in the inferential, it can be checked through the path below:
Aspen Inferential quality model-> Open .IQM file-> Build Inferential sensor-> Model statistics (at right hand drop down)
NOTE: Equations/ formula are available for old files, only if model type is PLS Model.
Keywords: Equations used in IQM
IQF
Formula in IQM
References: None |
Problem Statement: This Knowledge Base Article answers the following question:
Can existing Process Graphics that have links to other displays and files on the network (such as Excel files) be published to aspenONE Process Explorer and maintain this linking functionality? | Solution: Currently this is a manual process - neither Aspen IP.21 Process Browser Graphic Studio nor Aspen Process Explorer Graphics Editor will publish Excel files to the web server based on links in a graphic.
The Excel files must be manually copied to the desired destination on the web server, such as
C:\ProgramData\AspenTech\A1PE\Files\Public\Book1.xls
Excel files can then be opened with a custom line of script such as:
window.open(/ProcessExplorer/Files/Public/Book1.xlsx);
So for example in Process Browser Graphic Studio you can create buttons with custom OnClick actions that execute such script and open the desired Excel or PDF files from the browser.
In PE Graphics Editor, there is currently no way to specify custom javascript and do this - the hotlink buttons when clicked in a1PE will attempt to open the spreadsheet as if it were a .json file.
The workaround for this in PE Graphics Editor is fairly involved - creating a graphic in IP.21 Process Browser Graphic Studio that automatically loads the desired Excel file, then linking the PE hotlink to that graphic would work.
For example, create and publish a blank graphic name OpenBook1 in PB Graphic Studio adding an OnLoad action to that graphic with the script: window.open(..\\..\\Files\\Public\\Book1.xlsx); graphicBack(); then change the hotlink in PE Graphics Editor to open the OpenBook1 graphic rather than the Excel file directly.
Keywords: None
References: None |
Problem Statement: How to input NC Solid stream component attributes? | Solution: For a Non-conventional Solid stream, following Component Attributes are mandatory & should be consistent with each other:
PROXANAL
ULTANAL
SULFANAL
PROXANAL:
Enter the component attribute for the solid component in NC Solid stream as weight % on a dry basis, except for moisture. PROXANAL values for FC, VM and ASH should sum to 100.
Example PROXANAL input attribute for Coal (Non-Conventional Solid):
ULTANAL:
ULTANAL values for Ash, Carbon, Hydrogen, Nitrogen, Chlorine, Sulfur and Oxygen should sum to 100 (weight %)
ULTANAL value for ash should equal the PROXANAL value for ash
Example ULTANAL input attribute for Coal (Non-Conventional Solid):
SULFANAL:
SULFANAL values should sum to the ULTANAL value for sulfur (weight %)
Example SULFANAL input attribute for Coal (Non-Conventional Solid):
Keywords: NC Solids, Component Attribute, PROXANAL, ULTANAL, SULFANAL, Coal
References: None |
Problem Statement: How to apply the ABML correlation for a submodel stream. | Solution: ABML is applicable to BLENDS property only, not for submodel stream property. If you want to also use the ABML correlation for a submodel stream property, then you need to introduce the Table AMBLSUBF.
Use table ABMLSUBF to invoke ABML correlations that convert properties “created” in a submodel table (SXXX) to indices or blend values so that the stream can then be blended.
In our example, there is recursion structure for both TRN and TNM in Table SREF. If there are no entries in Table ABMLSUBF, then the recursion will be obeyed and both will be calculated by volumetric average of the components. As the example was provided, there are an RTRNRFT and RTMNRFT entries in table ABMLSUBF. This tells PIMS to ignore the recursion for TRN and TMN of RFT and instead calculate it by the ABML correlation.
If there is no ABMLSUBF entry for TRN of RFT, the TRN will be calculated by volumetric average of the components as defined in SREF.
Keywords: ABMLSUBF
ABML
Blending
References: None |
Problem Statement: When cimio_msg.log reaches 1 mb, the log file is copied to cimio_msg_backup.log, and a new version cimio_msg.log is created. This process is repeated each time the log file reaches 1 mb, and the previous log file is lost.
How to collect more information in the log file if needed? | Solution: The size of the log can be configured using the following settings.
Open the Cim-IO Interface Manager and select Cim-IO Interfaces, or
the Cim-IO IP21 Connection Manager and select Cim-IO Connections.
Edit the field Max log size (Mb) to set the desired log size.
You must restart the CIM-IO Client and/or Server for the change to take effect.
Keywords: CIMIO_MSG.LOG
Backup log
References: None |
Problem Statement: In short, what are the steps to be using the ‘new’ pipeline functionality in APS, post v8.7? | Solution: The following steps summarize how to use the new pipeline functionality in versions 8.7 and above:
Note: If you have pipelines in your existing model, you will be forced to go through the following steps by the DBUpdate tool
Define Locations (Model-> Pipeline -> Location)
Assign Tanks at locations (Optional Step) Go to Model-> Tanks, and you can see there is a location dropdown box in the dialog
Assign each pipeline with a source and destination location (Model -> Pipeline -> Segments)
Populate Routes of Pipeline Segments between source and destination (Model -> Pipeline -> Routes)
The concept is that the pipeline is always full. Every day, add beginning line fill to each pipeline segment (Events-> Beginning Linefill -> Crudes/Products) This defines what is in the pipeline at the start of the model horizon.
Add pipeline events to the Gantt Screens
Visualize pipeline events on the pipeline fill dialog screen (Simulator -> Pipeline Fill Dialog) This screen must be configured from Model -> Pipeline -> Pipeline Fill Dialog Configuration
Keywords: None
References: None |
Problem Statement: Can I set a time limit on my Aspen PIMS runs? | Solution: In PIMS-AO there is an option to set time limits on individual cases of a multicase run. This is available in the model settings under Non-Linear Model (XNLP) | General tab as shown below.
When this is activated, PIMS will stop any individual case whose optimization time exceeds the specified limit.
Keywords: None
References: None |
Problem Statement: APS Error “compile error the variable is not defined” | Solution: When selecting edit in excel, the error appears “compile error the variable is not defined”.
Please follow the steps below to fix the problem.
Open Excel file (any file is fine)
Press Alt + F11 key Microsoft Visual Basic for Applications is launched.
Go to the menu [Tool] –[Option]
Select the option “Require Variable Declaration” and check OFF the option
Click OK button to save the change.
Keywords: Compile error
Excel
Aspen Petroleum Scheduler
References: None |
Problem Statement: How to add penalties to OBJFN from Non-Linear Equations? | Solution: In some scenarios, we may want to add penalties for capacity and process limits when it reaches certain thresholds. There are multiple ways to add penalties to OBJFN row and non-linear equation dialog has the function to add penalties.
Let’s take capacity threshold penalty for an instance. Firstly, one new penalty variable should be defined, e,g Pxxxyyy. And a new E row should be introduced to calculate this penalty column. At the bottom of the dialog, we can decide whether to add this penalty value to objective function calculation. The coefficient entered under OBJFN usually represents the penalty cost.
Keywords: None
References: None |
Problem Statement: Is there any way to use a different mix of nitrogen and oxygen, or even include other inerts like oxygen or argon inside the FCC? | Solution: Currently when the user works with the FCC, the composition for the air is fixed (79% N2 and 21% O2). The only way to change this is through the EO variables (AIRPLTP.BLK.DRYAIR_N2_MOLPCT and AIRPLTP.BLK.DRYAIR_O2_MOLPCT) corresponding to those, since those are currently connected to Aspen HYSYS otherwise.
Also, the user can change the O2/N2 mix by using Enrich O2 and what is reported on the results tab is the mixture of the air and the enrich O2. So if the user has enrich O2, the O2 composition will be higher and the N2 composition will be lower.
Note: The user can treat any CO2 or argon in the air as nitrogen since that will be inert.
Keywords: FCC, N2, O2, Composition, Custom
References: None |
Problem Statement: How is the LHSV (liquid hourly space velocity) calculated for Hydrocracker Reactor in Aspen HYSYS Refining? | Solution: LHSV for Hydrocracker Reactor is calculated as follows:
LHSV = Feed Volumetric Rate/Total Catalyst Volume.
Where, Feed Volumetric Rate is user specified the flow rate and Total Catalyst Volume is calculated from the user specified deails for the the catalyst weight, catalyst density and void fraction for each reactor bed. We use this information to calculate the catalyst volume for each bed:
Catalyst Volume = Catalyst Weight * Catalyst Density / (1 – Void Fraction)
So, the catalyst volume for each reactor is just the sum of the catalyst volume for each reactor bed in the reactor.
Keywords: LHSV, Hydrocracker, Catalyst Volume
References: None |
Problem Statement: How is Enthalpy calculated in Aspen Plus? | Solution: The enthalpy of a compound at a given temperature and pressure is calculated as the sum of the following three quantities:
DHFORM: This is the Ideal Gas Heat of Formation and refers to the enthalpy change involved in reacting the elements at 298.15 K and 1 atm at their reference state (vapor, liquid or solid) conditions to form the compound at 298.15 K and ideal gas conditions.
Integral CPIG: This is the integral of the ideal gas heat capacity (parameters CPIG or CPIGDP) and refers to the enthalpy change involved in taking the compound from the reference state (298.15 K and 1 atm) to system temperature still at ideal gas conditions.
DH: This is the Enthalpy Departure (parameters DHV for vapor state, DHL for liquid state, or DHS for solid state) and refers to the enthalpy change involved in taking the compound to system pressure and state; is symbolically shown as the difference in the enthalpies, such as (Hi*,l - Hi*,ig) for liquid enthalpy departure. The method of calculation of this value varies depending on the thermodynamic model used to represent the vapor and liquid phases.
These three steps are shown graphically in the diagram below:
Keywords: Enthalpy, H, DHFORM, CPIG, DH, DHVL
References: State Notes
The enthalpy reference state used by the Aspen Physical Property System for a compound is that of the constituent elements in their standard states at 298.15 K and 1 atm. Because of this choice of reference state, the actual values of enthalpy calculated by the Aspen Physical Property System may be different from those calculated by other programs. All enthalpy differences, however, should be similar to those calculated by other programs.
Aspen Plus uses the constituent elements at 298.15 K (25 C) as an ideal gas for the enthalpy reference state for a component. In other words, the ideal gas enthalpy for a component at 25 C is equal to the heat of formation at 25 C (DHFORM). When DHFORM is retrieved from pure component databank, the value is typically a large negative number, so the value of vapor and liquid enthalpies will often be large negative numbers.
Aspen Plus uses a different reference state than the ASME steam tables; however, calculated heat capacities and enthalpy differences from the Aspen Plus STEAM-TA property method and the ASME Steam tables are comparable.
In Aspen Plus, you can use other reference states for activity coefficient property methods. These reference states allow the use of a saturated liquid reference state or an ideal gas reference state. These methods (such as option sets WILS-LR and WILS-GLR) optimize the accuracy tradeoff between liquid heat capacity, heat of vaporization, and vapor heat capacity.
For more information refer to the Help Guide topic “Enthalpies Based on Different Reference States”
Enthalpy Departure Notes
The vapor enthalpy departure (DHV) represents the difference between the ideal gas enthalpy and the enthalpy of the real gas. The vapor enthalpy departure is generally calculated using the equation of state. The vapor enthalpy departure is zero for activity coefficient property methods that use the ideal gas law (like NRTL). Other activity coefficient property methods use Redlich-Kwong (like NRTL-RK), Hayden O'Connell (e.g. NRTL-HOC) or Nothnagel (e.g. NRTL-NTH).
The liquid enthalpy departure (DHL) represents the difference between the ideal gas enthalpy and the liquid enthalpy and includes the heat of vaporization. When using an equation of state property method, the liquid enthalpy departure is calculated by using the equation of state model. When non-electrolyte activity coefficient property methods are used, the default calculation method is:
DHL = DHV + DHVL + DHLPC
DHV is the vapor enthalpy departure evaluated at the system temperature and the component's vapor pressure
DHVL is the heat of vaporization. This term is calculated by the DIPPR or Watson Heal of vaporization model; it is the largest contribution to liquid enthalpy departure.
DHLPC is a correction between the component's vapor pressure and the system pressure. DHLPC will be small for incompressible fluids or if the density model is not dependent on pressure.
DIPPR Liquid Heat Capacity Option
Most option sets default to calculate liquid enthalpy (HL) using the ideal gas enthalpy and the heat of vaporization (DHVL).
You can also modify a property method to calculate the liquid enthalpy from the DIPPR liquid heat capacity model (CPLDIP parameters). Use this option when more accurate liquid heat capacities are required, and the default enthalpy departure method is insufficient. For more information about this option see the article How to use liquid heat capacity parameters directly in a simulation
This method should not be used when using an equation of state property method because more extensive modifications are required. |
Problem Statement: How can I create a new user-defined unit from APS flowsheet? | Solution: We can directly create a new user-defined unit in APS flowsheet. The unit information will be saved to database tables.
By clicking Update Excel, the corresponding excel spreadsheet will be generated in the Units workbook.
Keywords: None
References: None |
Problem Statement: How do I enable HTML reports with frames in PIMS? | Solution: To enable the frame in the HTML reports, using which you can easily navigate through the different sections of the report, follow the below steps:
Go to Tools-> Program Options-> Report tab and check the “Launch HTML reports with Frames” option. When you run the model after doing this, the report will launch with frame enabled.
Keywords: None
References: None |
Problem Statement: Aspen PIMS will handle one additive for each specification blend. There may be scenarios when multiple additives are required. | Solution: Special thanks are extended to Sr. Rodrigo Favela of Pemex who authored this paper for the 1995 PIMS User's Conference in Florence, Italy. There are situations that may exist where a client model requires more than one additive in a specification blend. PIMS currently only allows for one additive, therefore, if additional additives are required, the user must accommodate them outside of the normal PIMS structure. It is possible to model additive addition in a submodel. The structure is different than the PIMS-built specification blending structure.
Please find sample model enclosed to the article.
Keywords: additive
submodel
submodels
addition
Applications
applications
References: None |
Problem Statement: The Aspen Physical Property System has several submodels for calculating vapor pressure of a liquid. Antoine vapor pressure model is one of them. Is there any easy way to get Antoine equation constants of pure component from Aspen Plus? | Solution: In Aspen Plus, the equation for the extended Antoine vapor pressure model is illustrated in Help manual (screen shot showed in figure 1). In this equation, nine parameters are used and called PLXANT. First seven parameters are equation constants and last two parameters are temperature bounds.
Figure 1. Extended Antoine Equation in Aspen Plus
The detailed extended Antoine equation parameters gain procedure is listed below and demonstrated in figure 2-3:
1) Click the ‘Review’ button in Aspen Plus Property Enviroment --> Components | Specifications | Selection sheet.
2) The Review result is popped out, which located at Methods | Parameters | Pure Components | REVIEW | Input sheet.
3) Select the PLXANT-1 folder located at Methods | Parameters | Pure Components.
4) In the Input sheet, table shows extended Antoine Equation parameters of pure components.
Figure 2. Extended Antoine equation parameters gain procedure (step 1)
Figure 3. Extended Antoine equation parameters gain procedure (step 2-4)
Keywords: Aspen Plus, Antoine Equation, Pure Component, PLXANT
References: None |
Problem Statement: How to use Dirty-Water option to simplify the phase calculations | Solution: In applications where the hydrocarbon solubility in the water phase is of great concern (such as in an environmental study), you can use the Dirty-Water method to calculate the valid phases. Dirty-water calculation uses special methods to compute the solubility of organic compounds in the water phase. It’s always faster than rigorous three-phase calculations and require minimal physical property data preparation.
You can turn on the dirty-water calculation by 2 ways:
(1). To enable global setting, check the “Use free water calculations” box on the Setup | Specifications | Global sheet.
(2). For a block, specify Vapor-Liquid-DirtyWater (or Liquid-DirtyWater for decanters) in the Valid phases field:
The minimum of water composition in water phase is 0.98. If your water composition is lower than 0.98, you should change this setting on the Setup | Calculation Options | Calculations sheet.
However, for chemical systems such as water-higher alcohols, dirty-water calculations do not apply. Solubility of the organics in the water phase is significant. Rigorous three-phase calculations are required.
Keywords: Dirty-Water
Three-phase calculations
References: None |
Problem Statement: Which property packages can be used to model rate based columns in Aspen HYSYS? | Solution: In Aspen HYSYS, Aspen Rate-Based Distillation can be used to model columns when one of the following property packages is selected in your case:
Acid Gas - Chemical Solvents
Acid Gas - Liquid Treating
Extended NRTL
Keywords: Rate Based Column
References: None |
Problem Statement: Are there any Excel templates to extract data from Excel to Aspen Energy Analyzer? | Solution: You can use specifically formatted excel spreadsheets to import stream information, or complete heat exchanger network designs with splitters and utility heat exchangers, into an Aspen Energy Analyzer case.
You can find empty templates for these data transfer formats as well as complete examples of each type under the Samples directory of your installation: C:\Program Files (x86)\AspenTech\Aspen Energy Analyzer Vx.x\Samples\Excel Test Cases
The empty templates are attached to this article as well:
HEN_Transfer_Template.xls: to extract both heat exchanger and stream data
Stream_Data_Transfer_Template.xls: to extract stream data only
Keywords: Data Transfer, Excel, Template, Data, HEN
References: None |
Problem Statement: Through the | Solution: article (KB 000025309: How do you enter Fisher data for a control valve?), user knows the possibility of customizing Aspen Plus User Interface so that additional series of valve data information can be added into the library of Aspen Plus Valve block. However, the steps described in KB 000025309 is not so clear. Can AspenTech provide step by step instruction on thisSolution?
Figure 1. The final desired effect of KB 000025309 knowledgeSolution
The step by step instruction with customized 'valve.dat' file have been uploaded in Attachments. Please refer to 'KB 000025309 step by step instruction.pdf' document for reproducing the KB 000025309 knowledge.
Keywords: Customize, Aspen Plus User Interface Table Building System (MMTBS), Valve, Fisher data
References: None |
Problem Statement: If the user is using a fluid package from the Aspen Properties Databank in Aspen HYSYS, where are stored the Henry's constants? | Solution: As mentioned in the How to find Henry coefficients in Aspen HYSYS? article, Henry's Law cannot be selected explicitly as a property method in Aspen HYSYS. However, Aspen HYSYS uses Henry's Law when an activity model is selected and non-condensablecomponents are included within the component list.
If the user is using an Aspen Properties Databank, Henry's constants are available for all activity coefficient property methods such as Wilson or NRTL. Henr'ys constants appear on Fluid Package | Binary Coeffs | Binary Vector | HENRY, as shown below.
Keywords: Henry's constant, Fluid package, non-condensable, activity model, binary parameters
References: None |
Problem Statement: How can I specify heat transfer in a Aspen HYSYS pipe segment? | Solution: There are 4 ways of defining heat transfer in Aspen HYSYS pipe segment.
1. Heat Loss : User need to manually enter the heat loss to the surrounding. Program will not calculate the heat loss and use the user entered value.
2. Overall HTC : Enter ambient temperature and overall heat transfer coefficient; heat transfer is calculated on each increment.
3. Segment HTC : Enter unique ambient temperatures and heat transfer coefficients for each piping increment.
4. Estimate HTC : Overall HTC can be calculated based on individual contributions: convective effects inside the pipe, outer medium convective/conductive effects, and conductive effects of the pipe wall and any insulation. Under this option HYSYS will estimate the HTC for the user.
If you choose above option, HYSYS will look into the following for overall heat transfer coefficient calculations:
a) If you check, 'include pipe wall button it will estimate the conductive heat transfer based on the pipe material you specify.
b) If you check, 'include inner HTC button, it will estimate the convective heat transfer due to fluid movement
c) If you check, 'include insulation button it will estimate the conductive heat transfer based on the insulation material you specify
d) If you check, 'include outer HTC button it will estimate the convective / conductive heat transfer to the surrounding. --> Outer heat transfer
Notes:
1. If you select By Segment radio button for the Estimate HTC option, user needs to specify segment ambient temperature value in the Segment HTC option, if not the pipe segment wont solve.
2. You can either use the option 1 or 2 or 3 or 4. If you specify parameters in multiple options then Pipe segment will not solve.
Key words
Pipe, heat transfer, Overall heat transfer coefficient, heat loss.
Keywords: None
References: None |
Problem Statement: Which method is used by EDR to calculate lifting lugs? | Solution: Lifting lug design is not included in the ASME Code Section VIII Division 1, the default design code used by EDR. Instead, EDR uses a different standard.
Attached to this article you will find a PDF document with the standard being used (variables, equations and example).
Keywords: Lifting lugs, EDR, mechanical
References: None |
Problem Statement: What is the Purpose of #AUTO with UNITS.XLS in Aspen Petroleum Scheduler? | Solution: Aspen Petroleum Scheduler, Units.XLS supports many # Commands and #AUTO is one among them.The Purpose of this Command is, to execute excel Macro, when the user hits “OK” button in the Event Dialog box. In other words, while SAVING the event, the Macro gets executed in the background.
The MACRO may be a SIMPLE one to Automate something in the event dialog box or it may be a COMPLEX one to Perform Database functions as well
In brief, this kind of automation is, used to improve the productivity of the scheduler by minimizing the manual task with event dialog box.
Example Automatically changing the EVENT COLUR from the Default color option.
The #AUTO command should implemented as follows. The below example is used for changing the default color options , through a Macro.
Sample code to change the Event Colour in APS
The above Macro can be used in the Units.xls to change the color for Crude Run event, means Different crude Unit Run event will have different color.
To complete the configuration, below option must be set to in the settings tab
Keywords: #AUTO
Changeeventcolor
Macro
Units.xls
References: None |
Problem Statement: How can I view two tabs at once in Aspen Plus? | Solution: Often it is useful to be able to view two tabs at the same time. For instance, having two tabs open can make the process for setting up Design Specs or a Sensitivity Analysis easier. As another example, it is possible to leave Stream Results open while still making changes to the main flowsheet without having to switch back and forth.
In order to view two tabs simultaneously, right-click directly on the title of the second tab and select New Vertical Tab Group.
The main view will now split 50/50 and the second tab will display on the right half.
When finished, simply click the X on the second tab group to close it and restore the original tab group to full screen. Alternatively, right-click directly on the title of the second tab and select Move to Previous Tab Group to return to the original view.
Key Words
New vertical tab group
Keywords: None
References: None |
Problem Statement: How do I copy record security permissions using IP.21 administrator and then paste them to another record? | Solution: Make sure you have Change Security user rights.
Right click and select copy permissions from the source record.
Then right click on the database (first branch in the administrator) and choose paste permission. A pop-up screen will appear, into which you can drag & drop the destination records to which you want to paste the permissions.
More information can be found in the IP.21 Administrator help file: Assigning a Security Setting to Selected Records.
Keywords: copy
paste
security
permissions
References: None |
Problem Statement: What is the Difference Between a Hypocomponent and a Hypogroup in HYSYS? | Solution: A Hypocomponent is a single pseudocomponent. A Hypogroup is collection of individual Hypocomponents. Hypogroups are useful because the Hypocomponents within the Hypogroup can be edited all at once using the Hypotheticals Manager (accessed from the Home ribbon). For example, the Heat of Vapourization method used for all Hypocomponents in a given Hypogroup can be set (as Default, Chen, Pitzer, etc.) in one step. Additionally, a large group of Hypocomponents contained in a single Hypogroup can be imported to or exported from a HYSYS simulation.
Keywords: None
References: None |
Problem Statement: What are the new external tasks added to Aspen InfoPlus21 Manager starting from V9.1?
TSK_ALRT
TSK_PMON
TSK_ROOTCAUSE | Solution: The tasks TSK_ALRT, TSK_PMON, and TSK_ROOTCAUSE are added starting from V9.1 are related to the Alerts, Pattern Matching, and Persistent alarm functionality respectively which provides added functionality to aspenONE Process Explorer. For more information related to these tasks refer to Aspen InfoPlus.21 Manager help file.
Keywords: new tasks
TSK_ALRT
TSK_PMON
TSK_ROOTCAUSE
References: None |
Problem Statement: How do I delete an ABE workspace? | Solution: Delete the workspace from the AdminTool using the right-click menu on any workspace. Please note, this is only recommended to be performed by ZyqadAdministrators.
If the workspace just deleted connects to either a SQL Server or Local DB Server, please use the SQL Management Studio to delete the actual database instance as well. (This should always be the second step, and might require assistance from DBA to do so). The recommendation is that a user create a new DB for every new workspace, for ease of use and fewer database corruptions issues, if any arises, and if that procedure is followed, you will be required to delete only a single specific database. For any ABE workspace, you will see a DB Table list similar to image below. This can be used as a step to identify the ABE database that needs to be deleted. For Oracle, please use the management tool as is specified for its usage, to do the same.
Locate the workspace libraries folder installed on the ABE Server. The folder is called AspenZyqadServer and within the folder navigate to AspenZyqadServer| Basic Engineering19.1|Workspaces (Please not the version number depends upon the version of software that is installed. Here in the example, we have used a V10 example). Navigate to the folder for the deleted workspace. The folder name is usually the same name as the workspace. Delete this folder and its contents.
Keywords: Cleanup workspace
References: None |
Problem Statement: Can DMC3 Builder import .prd file (DMCPlus Model prediction file)? | Solution: No. DMC3 Builder cannot import a .prd file.
However, DMC3 Builder can import .cas file (exported cases from DMCplus Model) and these cases after import in DMC3 Builder can be run to get predictions.
Keywords: .PRD
.CAS
Predictions
References: None |
Problem Statement: Can I add new CVs to the controller without revising the Foxboro bridge database and the DMC DCS graphics? | Solution: New CVs can be added to the controller if the CV measurements can be read directly from the OPC server using Cimio for OPC instead of using the FoxBridge interface.
It is also important to note that adding a CV to a controller without updating the FoxBridge and DCC Graphics is not recommended. This is because the new CV will not be displayed on the DCS graphics (as it is not a part of FoxBridge) and therefore the operators would not be able to monitor and maintain the CV (limits) using the DCS graphics. They may however still interact with the new CVs using the Aspen Web Interface (PCWS).
MVs would need additional interface parameters and logic that are part of FoxBridge and therefore cannot be added to the controller without changes to the FoxBridge and DCS graphics.
Keywords: Foxboro Bridge
References: None |
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