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Problem Statement: How does the “Prevent XLP Solve if Table Load has Errors” option work? | Solution: In PIMS-AO, any table errors detected by PIMS are highlighted when the model is openned and tables are read. These warnings are not repeated when the model is run. Therefore, it is possible that users run without fixing data entry errors such as #REF, #NA in the Excel tables.
Under Model Settings | NonLinear Model (XNLP) | Advanced tab there is an option called “Prevent XLP Solve if Table Load has Errors”. If this is not selected, then PIMS will proceed to run and ignore any bad data. If this option is selected, then PIMS will stop the execution to force the correction of the data. Examples are shown below.
Figure 1 – Messages seen when model was opened
With option unchecked, PIMS proceeds with run and ignores the bad data. In this example of BLNPROP, PIMS will not have a value for PPI of stream HCD. However, if the option is checked, PIMS will stop the execution and provide the message below.
The option is located in the model settings under NonLinear Model (XNLP) | Advanced tab.
Keywords: None
References: None |
Problem Statement: How to set an On-Off controller? | Solution: This can be done adding three digital control point operations and one Boolean latch gate operation.
Open the attached HYSYS case OnOff_starter.hsc.
We would like to control the level of V-100 (height = 1.127 m) through valve VLV-101. If the level is above the maximum level (0.80 m) the desired actuator position is 100%. If the level is below the minimum level (0.20 m) the desired actuator position is 0%.
From the Dynamics tab of the object palette, add three digital point controllers and one Boolean latch gate operation.
Open the first digital point (name it Full Open) and add the following Information:
Connections tab:
Process Variable Source - Object: V-100; Variable: Liquid Level.
Output Target – Object: Latch-1; Variable Set/Reset State.
Parameters tab:
Mode: Auto
Auto Operational Parameters: Latch
Threshold: 0.80 m (2.625 ft)
OP is On when: PV >= Threshold
Faceplate PV configuration:
PV Minimum: 0 m
PV Maximum: 1.127 m (3.698 ft)
In this way, if the Level is higher than the threshold value, the digital point will be ON and will send 1 to Latch-1. If it is equal or lower than threshold value, the current OP state will be OFF and a zero value will be sent to Latch-1.
Open the second digital point (name it Reset) and add the following information:
Connection tab:
Process Variable Source – Object: V-100; Variable: Liquid Level.
Output Target – Object: Latch-1; Variable Set/Reset State.
Parameters tab:
Mode: Auto
Auto Operational Parameters: Latch
Threshold: 0.20 m (0.6562 ft)
OP is On when: PV <= Threshold
Faceplate PV configuration:
PV Minimum: 0 m
PV Maximum: 1.127 m (3.698 ft)
This second digital point will send 1 to Latch-1 when level will be lower than 0.2 and 0 when higher.
Open the Boolean operation Latch-1. In Connections tab | Output Target section, connect the third digital point using Add OP… button.
On Monitor tab, select Set as Prevailing Input to provide this prevailing input to the output of Full Open digital point.
Introduce the following parameters for the third digital point:
Connections tab:
Output Target – Object: VLV-101; Variable: Actuator Desire Position.
Parameters tab:
Mode: Auto
Auto Operational Parameters: Latch
Threshold: 0.5
OP is On when: PV >= Threshold
Faceplate PV Configuration:
PV Minimum: 0
PV Maximum: 1
The third digital point should get 1 or 0 from the latch Boolean operator. If it gets 1, the Digital point will be ON since the PV is higher than the threshold. The control valve was full open and the level would decrease till 0.2 m. At this level, control valve was close. The level would increase till 0.8 m, where the digital point would get 1 again.
Run the case and see the table showing the water vessel results, track the impact on the level in V-100 and the effect of the controllers.
TheSolution of the above steps is attached, please see case OnOff_Result.hsc.
Keywords: On-Off Controller, Digital Point, Latch, Boolean Operator
References: None |
Problem Statement: The Depressuring tool does not initialise or begin calculations. Why is this? | Solution: Such an issue is normally a result of inadequate input values. If the values in Depressuring Utility window look complete (even if not necessarily correct), the program should still attempt to calculate. If this does not occur, navigate to the Dynamics tab, Integrator options:
These options (used in Dynamic simulations) are also used when the Depressuring Utility is run. They should be reviewed. One of the key items to inspect is the End Time. This value should be higher than the end time (as set in the Depressuring Utility). If this value is zero or less than the Depressuring Utility end time value, the utility will not run correctly. The best choice (for steady state based simulations) is usually to clear this number so that it reads <Non-Stop>. In that way, there will be only one 'true' control for the end time (located in the Depressuing Utility window).
Keywords: Depressuring Utility, Initialization, Integrator
References: None |
Problem Statement: How do I know what the minimum required inputs are to calculate a cost for a project component? | Solution: First, open the component in question and view its main form. For many components, but not all, you will notice cells that are bordered in red, yellow, and green.
Cells with a red border are required.
The user has the option to enter data for either the yellow cell(s) or the green cells. However, entering data for both colors is not required. If data is entered for the yellow cell(s), the green cells may be left empty. Alternatively, if data is entered for the green cells, then the yellow cell(s) may be left empty.
For instance, in the screenshot below the Item Description is red and therefore required. The liquid volume is yellow while the vessel diameter and tangent to tangent height are both green. Accordingly, it is acceptable to enter either a liquid volume (single yellow cell) or the vessel dimensions (two green cells). It is not necessary to enter data for all three of the yellow and green cells. After inputting the red cell plus yellow cell or the red cell plus green cells, the component may be evaluated.
Key Words
Required input, red, yellow, green
Keywords: None
References: None |
Problem Statement: What are the different Aspen Properties fluid packages for modelling water-only fluids? | Solution: When modelling pure water systems, it is more accurate to use one of the following models (vs. a general Equation of State model, e.g. Peng Robinson):
STEAM-TA: ASME 1967 steam table correlations
STEAM-NBS: 1984 NBS Steam Table
STEAMNBS2: 1984 NBS Steam Table. The same equations as STEAMNBS, but with different root search method.
IAPWS-95: IAPWS 1995 Formulation for General and Scientific applications
IF97: IAPWS Industrial Formulation, a fast, approximate (but very closely matching) version of IAPWS-95 (available from V10)
IAPWS-95 is the current standard for properties of water and steam and is recommended.
In Aspen HYSYS, these models are available for use via Aspen Properties
Keywords: water only, Steam-NBS, IAPWS, Steam Tables
References: None |
Problem Statement: How does the convective dryer perform the energy balance? | Solution: Heat balance for the gas phase
Here MG is the mass flow-rate of the gas in the dryer, cp,G the specific heat capacity of the dry gas, TG the temperature of the gas, Q the heat flow-rate, NP the total number of particles, z the axial coordinate, L the total length of the dryer, and Q.ind,G the rate of heat transferred to the gas
Heat balance for the solid phase
Here MS is the mass flow-rate of the solids in the dryer, cp,S the specific heat capacity of the dry solids, X the dry-based moisture content of the solids, cp,M the specific heat capacity of the liquid phase (moisture), TS the temperature of the solids, M the evaporation rate of one particle (local evaporation rate), Δhv the enthalpy of evaporation, and Q.ind,S the rate of heat transferred to the solids.
The total number of particles, Np, can be calculated from the particle size distribution with n classes by use of the mean particle diameter dp,I of a particle size class I and the mass fraction of the particles within the class I(xi):
The heat flow rate Q can be determined as follows:
Here αG is the gas-to-particle heat transfer coefficient, and AP the surface area of one particle.
The gas phase heat balance sets, for the sake of simplicity, the local heat flow-rate to the particles equal to the rate of enthalpy change of the dry gas, assuming that evaporation enthalpy rate and the change of vapour enthalpy in the gas are the same. This assumption is equivalent to neglecting vapour superheating.
In the solid phase heat balance, the temperature change of the wet solids is derived from the difference of heat supply and heat consumption for evaporation.
The average surface area of one particle Ap can be calculated based on a given particle size distribution as follows:
Keywords: Energy balance, convective dryer
References: None |
Problem Statement: How is contingency applied in Aspen Capital Cost Estimator? | Solution: The contingency percentage input for a project will not match the final percentage shown on the report. The reason for this difference is explained in the steps below. Please see the attached files.
1) To input a contingency percentage to be applied to the overall project, first go to the Project Basis View tab and open the Contingency and Misc. Project Costs form. Then enter a value for Contingency (default is 10%). In the screenshot below from the attached example file, 16% has been entered. Click the OK button when finished.
2) After the project has been fully input, evaluate the project and open the Interactive Capital Cost Reports. Select the Excel reports option and then the Project Summaries folder. Run the report.
3) In the Excel Report, note that the Contingency listed is 13.8% of TIC (Total Installed Cost) which does not match the original 16% value. In order to understand the difference, please see the attached Excel spreadsheet. It includes an additional table bordered in red and some added color coding. The contingency is being calculated by first adding up the Total Field Costs, Freight, Taxes and Permits, Engineering and HO, and Other Project Costs. These cells have been colored orange. It then takes that summation and multiplies by the contingency percentage (16% in this example) to arrive at the value in cell R30 - these cells are blue. Next, the calculated contingency dollar value is added to the total pre-contingency amount to arrive at the final total (green cells). Finally, it re-calculates the contingency as a percentage of the total installed cost (purple cells). Note this will never equal the contingency value manually entered. For instance, assume the total cost before adding contingency is $100. At 15%, the contingency would be $15. The overall total would then be $115 and the contingency in terms of TIC would be $15/$115 = 13% (instead of 15%).
Key Words
Contingency
Keywords: None
References: None |
Problem Statement: Comparing a single phase fluid flowing in a vertical (upward) pipe vs. a horizontal pipe (of similar geometry), I notice that the frictional pressure drop (in the Pipe Segment) is different. Why is this? | Solution: In the vertical pipe with the upward rising (single phase) fluid, there is a pressure loss due to the elevation change, i.e a reduction in static head. This change in pressure is affecting the Reynolds number (through a reduction in the density and viscosity). The friction factor is a function of the Reynolds number and will be different (when comparing the elevated (rising, vertical pipe) case to the constant level (horizontal) case). As such, the frictional pressure drop (either overall or per unit length) will be different.
Keywords: vertical pipe, horizontal pipe, pressure drop
References: None |
Problem Statement: How do I set up a Case Study in Aspen Plus? | Solution: In this example, we will research a simple heat exchanger where a liquid stream is being heated. Our goal is to observe the effect on the outlet temperature (dependent variable) based on varying the following three manipulated (independent) variables:
1) Process stream flow rate
2) Process stream inlet temperature
3) Heat duty
In a normal Sensitivity Study, varying three independent variables could potentially create a large grid displaying every possible combination of values. In this study, we are assuming there are five real-world operating conditions that need to be evaluated. Therefore, we will only evaluate those specific five scenarios instead of running a full Sensitivity Analysis across the entire range of trials.
Please see the attached example file.
In order to create a Case Study in Aspen Plus, first create a Sensitivity Analysis. From the Simulation Environment Navigation Pane, expand the Model Analysis Tools Folder and then select the Sensitivity Folder. Then click New and enter an ID.
The new Sensitivity Analysis will open and display the Vary tab. Check the box next to Case study. This will unlock the Cases tab. Before leaving the Vary tab, specify the independent variable(s). In this case, we will add the heat exhanger heat duty, inlet stream temperature, and inlet stream flowrate. Note that all three of these parameters are input values in this example. The best practice is to only select inputs as manipulated variables.
Next, go to the Define tab to specify the dependent variable(s). For this example, we will add the outlet stream temperature.
Once complete, go to the Tabulate tab and click the Fill Variables button.
Then, go to the Cases tab to input specific combination of values for the independent variable(s) which were specified on the Vary tab. In this example, we will be studying five possible operating scenarios. Individually set the values for the independent variables on a case-by-case basis.
After setting up the desired cases, run the simulation. The solver will now process the cases by adjusting the independent variable(s) and recording the results of the dependent variable(s). To view the output after the run has completed, click on the Results form under the Sensitivity Analysis from the Navigation Pane.
By default, the base case (the original input values from the main flowsheet) will be reported last.
Keywords: Sensitivity, case study
References: None |
Problem Statement: How do I find iso-hexane, iso-heptane, and iso-octane components in HYSYS databank? | Solution: Components can be found searching by Full Name/Synonym
· Iso-hexane as 2-MethylPentane or as 2-MC5. You can compare the CAS number of this component for iso-hexane: 107-83-5.
· Iso-heptane as 2-MethylHexane or 2-MC6. CAS number: 591-76-4.
· Iso-octane as 2,2,4-TrimethylPentane or 224-Mpentane. CAS number: 540-84-1
Keywords: iso-hexane, iso-heptane, iso-octane, component list
References: None |
Problem Statement: What are the different Cp/Cv methods in Aspen HYSYS? | Solution: There are different Cp/Cv values calculated by Aspen HYSYS using different methods:
1. Cp/Cv - This is calculated rigorously based on actual temperature and pressure in the stream. Aspen HYSYS uses this rigorous method for compressor performance & relief valve sizing calculations.
2. Cp/(Cp-R) - This is a semi-ideal calculation where Cp is calculated rigorously which assumes the ideal gas relationship, Cv = Cp-R. This value is available for use with correlations requiring ideal gas relationships, such as industry standards e.g. Relief Valve orifice calculations in API-520/521.
3. Cp/Cv (Ent. Method) - This method calculates Cv as outlined in point 3 of the attached Word document. This method is maintained purely for historical purposes and was initially added to Aspen HYSYS to be an improvement over method 2 above.
Note that because this method (Cp/Cv- Ent.method) is based on a temperature/entropy perturbation, it will not be accurate in the region of a phase change (e.g. bubble point) where the specific entropies at the perturbed temperature may refer to different fluid states (liquid and vapor).
Hence with reference to the above, it is recommended the most appropriate data should always be used where required
Key Words:
Specific Heat, Cp, Cv, Gamma, Heat Capacity
Keywords: None
References: None |
Problem Statement: I would like to change the class of an object already placed on my workspace, and maintain the data of the object. How do I achieve this? | Solution: If you want to change the class of an object, you need to use a KB or query.
Attached is a KB method example.
1. From the Rules Editor, load the attached azkbs file.
2. Replace the Agitator text with the new class.
3. Compile and install the KB
4. From ABE Explorer execute the method on each object to modify the class to the defined on step 2.
As another option, you can use the attached query.
1. Load the attached azq file in the ABE Explorer editor (View tab | Query Editor).
2. Define the OID according to the object you want to change the class.
3. Replace the DrawOffSump text with the new class.
4. Click Submit and refresh the Explorer.
Note: This method and query should only be used by ABE administrators who know the implication of doing this type of operation.
Keywords: Class, Object ID, Local Method, workspace library
References: None |
Problem Statement: How to modify the Binary Interaction Parameters for a number of binary pairs such as H2O-N2, H2O-CO2, H2O-H2S? | Solution: For a number of binary pairs (such as H2O-N2, H2O-CO2, H2O-H2S), HYSYS Peng Robinson (PR) property method does not allow to modify the Binary Interaction Parameters (BIP). HYSYS PR uses T-dependent kij to improve accuracy. These T-dependent kij's are hard-coded and are used automatically. Any user-entered kij (which is a constant) is ignored. After editing the BIP and the case is run in Simulation Environment, when you return to the Properties environment, you will notice that the kij value for these pairs can change. The changed value is that calculated at the last stream or property calculation.
This behavior, while providing the best results out of the box, some users may want to overwrite with their own BIP, they need to follow the steps below.
1. In the Properties Environment, go to the Fluid Packages Folder- Peng Robinson property method Binary Coeffs Tab.
2. On the Binary Coeffs. tab, select Set All to 0.0 radio button and enter the desired values. All kij values that are shown on the form will be used as is. HYSYS will not overwrite them.
Note: The above steps work for Aspen HYSYS V9.0 and earlier only.
This behavior changed in Aspen HYSYS V10 such that user-entered values for these special binary pairs are used and no longer overwritten by HYSYS.
Keywords: Binary Interaction Parameters, Peng Robinson, H2O-N2, H2O-CO2, H2O-H2S
References: None |
Problem Statement: What are the equations used for determining the simple packed column hydraulics in Aspen Plus Dynamics? | Solution: The simple packing hydraulics equation relates the liquid flow rate from a packed section to the amount of liquid in the section as follows:
Where:
IfV =Liquid volume fraction in the packed section
uL= Liquid velocity in the packed section
This is calculated from the volumetric flow rate of liquid and the total cross-sectional area of the section.
KPack= Packing constant
This constant is fitted from the initial volume fraction that you specify and the liquid velocity calculated from the steady-state results.
Keywords: Simple packed column hydraulics, Radfrac, Aspen Technology plus Dynamics
References: None |
Problem Statement: What does the petroleum property correlation ‘Penetration’ measure? | Solution: Starting with V9.0, Aspen HYSYS reports ‘Penetration’. This property correlation is based on the standard test for hardness of wax by ASTM D1321, which measures the depth in tenths of a millimeter that a needle of certain configuration under a given weight penetrates the surface of a wax at a given temperature.
This property correlation may be used either at stream or flowsheet level.
To add this property correlation onto the Properties form of a specific material stream, double-click on the material stream and go to the Properties form. Then, click on the 'Append correlation' button and look for this property under the Petroleum correlations group.
Also, this property correlation can be added to all material streams at once. To do so, click on the 'Correlation Manager' under the Simulation section of the home tab of the ribbon (see image below). Then, look for this property under the Petroleum section and activate it.
Keywords: Penetration, Petroleum, Wax, Depth, Temperature, Petrolatum.
References: None |
Problem Statement: How to change the sequence of parameters/instrument type names displayed in the start and end conditions of an Instrument in AtOMS that need to be rearranged?
Requirement is that it should display in the following sequence: level, temperature, density and so on.
The screen-shot below shows the current configuration: | Solution: This refers the setting of display order of AtOMS Instruments” in the AtOMS Client.
The sequence of parameters can be changed by renaming the Instrument type names in AtOMS Admin tool
Open the AtOMS Admin tool
Go to “Instruments_Type” List in the Model Tree.
Rename the LEVEL Instrument with “1_LEVEL”
Rename the Density Instrument with “2_DENSITY”
And so on, with the order you prefer.
Please Refer the Screenshot.
After the changes save the new configuration,
Refer the screenshot below which shows the expected display of the Instruments order, in AtOMS Client.
Keywords: AtOMS, instrument, name, sequence, client
References: None |
Problem Statement: What is the difference between Sensitivity and Nested Case Study Types? | Solution: The difference between the two Case Study Types is the way the variables are examined and the total number of states.
In a Sensitivity case study, each variable is examined at a time. For example, Variable A changes independently from the other variables. Once the analysis of Variable A is complete, Variable B begins perturbing.
Total Number of States = Sum of # Steps for each variable.
In a Nested case study (default), every possible combination of variable change is examined.
Total Number of States = Product of # Steps for each variable.
Keywords: Case Study, Types, Sensitivity, Nested
References: None |
Problem Statement: What impact does Base Time Unit Offset have on scheduled calcs? | Solution: The calculations will execute at the execution times in the schedule group. When the offset is added, it adjusts the execution time of the schedule group.
Each group has a calculated base time unit of seconds, minutes, hours or days. Groups by default are scheduled to be executed at the top of the base time (seconds, minutes, hours or days.) Adding an offset will cause the group to be executed at the top of its base time unit plus the offset. Aspen Calc evaluates the group and its schedule automatically and adds any offset. A 5 second group by default will execute at 05, 10, 15, 20, etc.; a 5 second group with a 2 second offset will execute at 07, 12, 17, 22, etc.
Keywords:
References: None |
Problem Statement: On the Face Plate of a controller, what does SP:R or L and Exec: Int or Ext mean? | Solution: When a face plate for a controller is selected, user can view the Process Variable (PV), Operating Point (OP), Set Point (SP- Inverted red triangle) and the mode of the controller.
It also displays the two internal setpoints in the controller SP: L (Local) or R (Remote).
The local setpoint (L) is where you can manually specify the setpoint via the property view (interface), and the other is the remote setpoint (R) which comes from another object such as a spreadsheet or another controller cascading down a setpoint. In other words, a master in the classical cascade control scheme.
Apart from that you can also view from where the signal from the controller is sent. Exec: Int (Internal) indicate that the signals are generated to stay within HYSYS. Exec: Ext (External) indicate that the signals are sent to a DCS, if a DCS is connected to HYSYS.
Keywords: Controller, Face Plate, SP, Execution
References: None |
Problem Statement: Suppose the Excel add ins for APS i.e. EIU & Refinery Report Wizard are no longer available in the excel workbook.
On trying to add these Add ins again from the Excel Utilities folder, it gives the below error: | Solution: This Excel ADD in is used for Aspen Petroleum Scheduler and gets installed as a part of the standard installation of the product.This add-in is being used in the application for invoking functionalities provided by APS like EIU & Aspen Refinery Report Wizard.
The issue mentioned in the problem statement can be fixed by updating the machine registry table.
Solution
-
1. Find a machine which has the EIU, Report Wizard add in installed.
2. Export the registry key of the Add-in from the below path: [HKEY_CURRENT_USER\Software\Microsoft\Office\Excel\Addins\AspenTech.Pims.ReportWizard2007]
Open Regedit.exe with Administrator privileges and Import the key file to your registry table.
If the location of your EIU, Report Wizard is different compared to the machine you imported from,
Try modify the key value manually.
OR
You can also double click on the Registry key and it will automatically get copied on the required location i.e.
[HKEY_CURRENT_USER\Software\Microsoft\Office\Excel\Addins\AspenTech.Pims.ReportWizard2007]
Once done, you can refresh the registry table, open Excel and the Add-ins will now be available for your machine.
Keywords: Excel add-in, AspenTech.Pims.ReportWizard2007, EIU add-in, refinery report wizard
References: None |
Problem Statement: Can I perform Column Internals analysis for Side Operations like Side Rectifiers, Side Strippers? | Solution: Yes, the Column Internals analysis can be performed for Side Operations like Side Rectifiers, Side Strippers.
Once the side operations are added and the column is converged. You can select the desired side operation and perform internals analysis.
To view the results, click on View Internals Summary on the Internals tab which will direct you to the Performance Tab-Internals Results Page.
Select the side operation from the dropdown for Tower to view results for the required side operation.
Keywords: Column Internals, Side Operations, Internals Summary
References: None |
Problem Statement: What is the Purpose of “Running Gauge Comp Tanks” option in Blend Optimization Dialog Box in APS ? | Solution: Running Gauge Comp Tanks feature is used to account additional VOLUME of Components generated [or] VOLUME of Component being received during the Blend operation and that VOLUME will be accounted for Blend Optimization process.
In Detail,
Consider a situation, where REF1 ( REFORMATE ) coming from Unit and stored in the COMP TANK TREF, before used for Blending.
In the Begging Time of the Blend EVENT ( 08:00 AM ) the Available component Volume in TREF is 5,000 M3. The Blend Duration is 10 hrs, thus the End time will be 18:00 hrs.
During the Blending duration, the tank TREF is continuously receives rundown from the unit and this additional material VOLUME is say approximately 500 m3.
Enabling “Running Gauge Comp Tank” option account for ,
a). Initial VOLUME 5,000 m3 and
b). the amount of additional component generated during the Blending Process, in this case it is 500 m3.
So in Total 5,500 m3 will be used for Component availability calculation.
Usually this feature should be enabled for the component tanks, which continuously receives streams from the Process units, during Blending Process.
This Difference in Quantity will be noticed when you hit MAX VOL in the Blend Event Dialog box.
Keywords: Running Gauge Tanks
Blending
SBO
MBO
References: None |
Problem Statement: How to specify the time line, multiple tags, etc when calling pbplots.asp from custom application? | Solution: How to specify time line: End time and time span can be specified using the T2 and TimeSpanMilliSeconds query parameters, respectively. T2 is an integer specifying UTC date time in ms from January 1, 1970, e.g., T2=1457165114000 for 05.Mar.16 08:05:14 (UTC). See http://www.unixtimestamp.com/index.php <http://www.unixtimestamp.com/index.php> for more information.
How to specify multiple tags: Multiple tags can be set using a comma delimiter with the Tag query parameter. The Source and Map query parameters can be used wtih Tag to specify the data source and Map for each tag. There is a one-to-one correspondence between lists for these three query parameters. The default will be applied if either the Source or Map is not specified for one of the tags.
For example:
?Tag=fc185,fc183&Source=Source1,Source2 will specify Source1 for fc185 and Source2 for fc183.
?Tag=fc185,fc183,fc180&Source=Source1,,Source2 specifies Source1 for fc185 and Source2 for fc180.
The local data source will be specified for fc183.
How to exclude items from screen:
The OutsideA1 parameter accepts these parameters:
None: standard
Dashboard: no timeline/taginput, user cannot interact with chart (doesn't allow for realtime since we wanted to use common timeline
RBV: same as none, but removes styling from ABar
TabGroup: same as none, but no ABar visible
Graphic: same as none (URL will not be entered into A1PE History Buffer)
Both Get and Post requests are supported. Since tag names may contain characters that require encoding for Get Requests, Post requests may be easier to formulate (all tag names can be sent as is).
Keywords:
References: None |
Problem Statement: How do I change the High Time (maximum time on the X-axis) on a Strip Chart in Aspen HYSYS? | Solution: The high time of the strip chart cannot be changed initially before the case has been run. The software will not allow this value to be modified if there is no data in the graph.
After running the simulation, the graph will progressively begin to fill in as data is generated. After completing the run, it is now possible to change the High Time via the following steps:
Right click the plot and select Graph Control…
In the Time Axis tab, you can now double click the High Time value and change it. Note only a value less than or equal to the maximum final run time may be entered. You can also change the time units by clicking the drop-down box (minutes shown below). The Low Time may be modified from this screen as well.
Keywords: Strip Chart, High Time, Aspen HYSYS, X-axis, time axis, Low Time, Graph Control
References: None |
Problem Statement: I want to convert my HYSYS file to xml. file. However, there is no choice for xml. file when trying to save it. I need the xml. file to convert a file from the new version of Aspen HYSYS into an older version. What could I do? | Solution: When you use Petroleum Assays in HYSYS simulation, you could not save the hsc. file to xml. file. If you go to “File” – “Save As”, you will not find the choice of xml. file when trying to save it:
In some cases, there is a workaround. Try to manually input “.xml” after the file name and save it (just neglect the “Save as type” box):
But in general, when you have Petroleum Assays in the simulation, there is no guarantee that you could save it in xml file. Even if you could save it, there may be convergence issues in the simulation. So always double check before you use the file. If thisSolution does not work, then you need to delete the Petroleum Assays from Property. You also need to delete any streams with Petroleum Assays attached from the flowsheet.
Keywords: xml
hsc
conversion
backwards compatibility
References: None |
Problem Statement: How to resolve Permission Denied error being received while operator/user is trying to activate a movement in AtOMS? | Solution: This error shown in the problem statement screenshot is for a user log in configured for ATOMS.
Please find the cause for this issue and the reSolution for fixing this problem,
Cause: DCOM settings not being configured for the user’s login resulting in an error while activating the movement.
It is essential to have the DCOM Settings configured with access rights for all Domain users.
Solution
Configure the DCOM security from the dcomcnfg.exe tool and enable the security/access rights for all Distributed Com users.
Once done, using computer management tool add all the domain users in the DCOM group and provide them access to perform various AtOMS functions like activating a movement, closing the movement , etc.
Keywords: AtOMS, permission, denied, activating, movement
References: None |
Problem Statement: How to model a rupture disk in Aspen Flare System Analyzer | Solution: In Aspen Flare System Analyzer (AFSA), rupture disks may be modeled with control valves or pressure relief valves.
Both types of source have a user specified flowrate and do the same rigorous energy balance. A maximum allowable backpressure must be specified, but it can be either entered by the user or calculated by AFSA.
If modeling the rupture disk with a control valve, then the maximum allowable back pressure would be the maximum pressure at the outlet of the rupture disk which would not hamper the relieving capacity of the rupture disk significantly.
The pressure drop across the rupture disk may be included by adding a pipe with a very short length and a specified fitting loss (some known value) downstream of the rupture disk.
Keywords: Rupture Disk, Control Valve, Pressure Relief Valve, Backpressure, Pressure
References: None |
Problem Statement: What are the differences between the two Beggs & Brill methods 1973 and 1979 for pipe segment correlations? | Solution: The differences between the two Beggs & Brill methods are:
Beggs & Brill (1973):
Includes Flowmap correction by Payne et al.[1977]
Does not Include Frictional Pressure drop correction for rough pipes by Payne et al.[1979]
Does not include Liquid Holdup Correction for uphill & downhill pipes by Payne et al.[1979]
Gives an option on whether to include Beggs & Brill model acceleration pressure drop in the calculation or not.
Beggs & Brill (1979):
Includes Flowmap correction by Payne et al.[1977]
Includes Frictional Pressure drop correction for rough pipes by Payne et al.[1979]
Includes Liquid Holdup Correction for uphill & downhill pipes by Payne et al.[1979]
Gives an option on whether to include Beggs & Brill model acceleration pressure drop in the calculation or not.
Keywords: Beggs & Brill, Method, Pipe Segment.
References: None |
Problem Statement: How do I control the data transferred between Aspen Capital Cost Estimator and Aspen Basic Engineering? | Solution: Options for import can be accessed directly from the Cost Mapper window by clicking on Tools | Options, to control the data imported and specify whether input values are overwritten.
Keywords: Zyqad, costing data, Icarus import, Cost Estimator Interface
References: None |
Problem Statement: How does EDR Mechanical determine the Hydrostatic Test Pressure? | Solution: To calculate Hydrostatic Test Pressure. Exchanger Design & Rating uses code rules UG-99(B), which dictate that vessels designed for internal pressure must be subjected to a Hydrostatic Test Pressure. This value will be equal to 1.3 times the Design Pressure multiplied by the Lowest Stress Ratio (LSR):
Hydrostatic Test Pressure = 1.3 * Design Pressure * LSR
All these values are reported by EDR Mechanical in the MAWP/MDMT/Test/PWHT section:
Keywords: Hydrostatic test pressure, LSR, lowest stress ratio, UG-99
References: for the 1.3 factor is reported in the Code Calculations: |
Problem Statement: What are the advantages of using New Equation Oriented (EO) Subflowheet and Modeling capabilities in Aspen HYSYS V10? | Solution: Aspen HYSYS V10 features a new, revolutionized Equation Oriented Sub-Flowsheet. Equation Oriented Solving is an alternative method used for solving flowsheets in HYSYS, which normally uses Sequential Modeling. EO technology collects the model equations and derivatives for selected operations in the flowsheet and solves them simultaneously, using a nonlinear sequential quadratic programming (SQP) solver. This improves the convergence and optimization of complex flowsheets that contain recycle streams and complex control strategies (specifications).
The advantages are detailed below:
Allows nested loops to solve simultaneously.
Uses a single model for both calibration and optimization with flexible variable specification.
Provides optimizations that are feasible.
Provides aSolution in minutes.
It is easy to validate Equation Oriented input.
Keywords: EO, HYSYS EO, Equation Oriented
References: None |
Problem Statement: When trying to configure a CIM-IO Interface, the user might get the following message-
Creating Cim-IO for OPC SERVERNAME...
Failed create SERVERNAME
CIMIO_MGMT_PROCESS_EXECUTABLE_INEXISTANT, Process executable does not exist
Please check if Aspen CIM-IO Manager service is running | Solution: 1. Check if the Aspen CIM-IO Manager service is running.
2. If the service is running and the problem persists. This is typically because different executable interfaces are not found on the Cimio directory.
All different interfaces need to be in the following folder.
C:\Program Files (x86)\AspenTech\CIM-IO\io
If executable files are missing, the Aspen software needs to be uninstalled and reinstall on the system.
The below screenshot contains the executable folders.
Keywords: CIMIO_MGMT_PROCESS_EXECUTABLE_INEXISTANT
References: None |
Problem Statement: How do I create a brand new blank APS database in SQL? | Solution: After setting up an SQL instance, open SQL Management Studio and create a new blank database. (This is done from the SQL interface)
Right click against the instance name and select New Database
Name the database that is being created.
Next, go to the application install folder (Default location: C:\Program Files (x86) \AspenTech\Aspen Petroleum Scheduler\)
There will be a SQL script by the name: SQLServer_Create_Tables.sql
Run this script against the database just created.
This SQL script will populate the required database tables required by APS, with the latest database schema of the current version.
This would be the first step to starting to build an APS model.
In order to open this blank database in APS, there is some initial data that has to be filled in to tables:
- Table CASES: add a case ID (usually BASE)
- Table USERS:
- CASE table ; Create a new case, say BASE
- GROUPS table: Create a Group with all privileges, say ADMIN. Add '1' to ADDSCRN and EDITMODEL fields
- USERS table ; Users ID with ADMIN as GROUP_
Keywords: None
References: None |
Problem Statement: Why is pressure increasing instead of decreasing in my pipe segment when a swage fitting is added? | Solution: When a swage is added as a fitting in a pipe segment to model and account for the diameter change between to pipes of different sizes (diameters), there will be a pressure increase instead of a decrease.
The reason why pressure increases in the pipe is due to the diameter increase across the swage between pipe segments of different sizes. Fluid flow across an expansion results in a decrease in fluid velocity and hence a recovery of velocity head as pressure head occurs. This can be explained with the following equations: the Mass conservation (continuity) equation and Bernoulli’s equation.
Starting with the Mass conservation (continuity) equation (for steady state):
And now Bernoulli’s equation (in terms of pressure energy):
For a horizontal pipe:
Where:
- Q1 and Q2 = Mass flow rate
- Qv1 and Qv2= Volumetric flow rate
- ρ, ρ1 and ρ2 = Mass density
- V, V1 and V2 = Velocity
- A, A1 and A2 = Flow area
- D, D1 and D2 = Diameter
- P1 and P2 = Static pressure
- g = Acceleration due to gravity
- z1 and z2 = Height
Considering a very small or null change on density due to temperature and pressure:
At the end these two equations describe the fluid flow through the piping:
Aspen HYSYS calculates and reports static pressure, including momentum contribution in a flowing system. When a flowing fluid expands, a pressure increase occurs as the fluid slows or a pressure loss can occur if the fluid accelerates. Removing swage fittings, for the sake of demonstration, will make it possible to notice that the overall pressure in the pipe segment will decrease.
The attached example file (‘Swage_Pressure increase example.hsc’) contains a pipe segment for which a swage fitting was added, so pressure is increasing and it can be seen on the Worksheet | Conditions window, as well as another pipe segment (with the same input) for which no swage fitting was added and for which pressure is decreasing instead of increasing.
Keywords: Pipe Segment, Swage, Diameter, Pressure, Pressure Drop, Pressure Increase.
References: None |
Problem Statement: How to model a vacuum pump in Aspen HYSYS | Solution: Pump calculations are performed by Aspen HYSYS with the assumption that the liquid going trough is incompressible; that is, density is constant (liquid volume is independent of pressure). This is the usual assumption for liquids well removed from the critical point.
In summary, to model vacuum pumps in Aspen HYSYS users may use a compressor to represent a vacuum pump, this will allow to simulate pressure changes to affect density.
Keywords: Vacuum Pump, Pump, Compressor, Density, Pressure
References: None |
Problem Statement: How are Pseudo and True Critical Properties of material streams calculated in Aspen HYSYS? | Solution: (1) The Pseudo Critical Properties of material streams calculated by the Critical Properties Utility, are calculated by a linear mixing rule.
For example:
Where:
is the composition (mole basis) of component ‘i’
is the critical temperature of component ‘i’
Therefore, the pseudo critical properties of any material stream will be calculated if is available for all components in the mixture.
(2) The True Critical Properties of material streams calculated by the Critical Properties Utility, are determined thermodynamically by satisfying both the quadratic and cubic forms in the expansion of the Helmholtz free energy mathematical expression as a function of composition (mole basis) at critical point conditions.
Details of critical point calculation can be found in the paper by Heidemann and Khalil, AIChE Journal, Vol. 26, No.5, p769-779, 1980.
For some cases/conditions, the calculation of True Critical Properties will not be converged, so the utility will return ‘<empty>’ on the UI form.
Keywords: Pseudo Critical Properties, True Critical Properties, Critical Properties Utility, Critical Point.
References: None |
Problem Statement: Are there velocity values recommended for a Plate exchanger as there are for a S&T exchanger? | Solution: Fluid velocity in a heat exchanger is an important variable to keep track of in order to control pressure drop or effects of fouling, erosion, etc. Unlike tubular exchangers such as Shell & Tube or Air Cooled exchangers, Plate heat exchangers are compact equipment. The velocities for the port and plate channel are directly related to pressure drops over the port and plates or plate wall shear stress that may affect plate exchanger operations.
Pressure drops over the port and plates or plate wall shear stress are calculated in terms of the velocity and plate geometries. There are recommendations in API 662 for pressure drops over the port and plates or plate wall shear stress, but not for the velocity.
Keywords: Plate exchanger, velocity recommendation, pressure drop
References: None |
Problem Statement: How do I add a component if it is not available in Aspen HYSYS? | Solution: On the navigation pane of the Properties environment, select a component list. The Component List property view appears.
In the Component List property view, select Hypothetical in the Select field.
Click the New Hypo Group. The Hypo Group property view appears.
Open the Hypothetical Manager and click the Settings tab.
Select the class type you want to assign to this group of hypo components from the Component Class field. You can only have one class type per group. You must create a new hypo group to contain components of a different group. The class type has no effect on the values calculated for the solid hypothetical components. Close the Hypotheticals Manager when finished.
To add a hypothetical component to your group, first select Create and Edit Hypos in the Method field. Then, click New Hypo (or you can click New Solid to add a solid hypothetical component if you selected Hypothetical Solid).
A new Hypo component will be added. In the table listing all the hypothetical components in the current selected hypo group, specify values for normal boiling point, molecular weight, liquid density, critical temperature, critical pressure, critical volume, and accentricity. Solid hypothetical components do not require values for critical properties.
Optional: On the Type field, select Vapour Pressure. Specify values for minimum temperature, maximum temperature and the Antoine Coefficients.
Notes:
You do not need to specify all the component properties. By supplying a minimum amount of information* and clicking Estimate Unknown, HYSYS will estimate the critical properties as well as the all the variables used to calculate vapor pressure.
*For HYSYS to estimate the component's critical properties, the following information must be supplied:
Normal Boiling Point Minimum Required Information
< 700 °F (370 °C) Boiling Point
> 700 °F (370 °C) Boiling Point and Liquid Density
Unknown Molecular Weight and Liquid Density
The Vapour Pressure is calculated using the Modified Antoine equation. The units used for Pressure and Temperature are kPa, and degrees Kelvin respectively.
You may also specify the UNIFAC structure to estimate properties. First, open the Hypo by double-clicking its name. From the ID tab, click Structure Builder to open the UNIFAC Component Builder property view.
You can view more information about Hypotheticals from the Aspen HYSYS Help Menu.
Keywords: Hypothetical, hypo, hypo group, unknown component
References: None |
Problem Statement: How to change the fluid package for a single or multiple trays in a column? | Solution: A column can use different fluid packages for different stages, including the condenser and the reboiler. The Parameters tab | Fluid Pkgs page property view lets you change the fluid package for each stage. Use the Change Fluid Pkgs button to change the fluid packages for a range of stages in one click.
Note: Multiple fluid packages must be assigned the same component list to be substituted within the column
Key words
fluid package for trays, column, trays, fluid package, multiple fluid packages
Keywords: None
References: None |
Problem Statement: I want to perform a Vapor-Liquid-Liquid separation, then I need to use a Flash3 block instead of the Decanter, since I want to take into account the vapor separation. However, I would like to consider that a part of L1 is entrained in the L2 and viceversa. This is possible when using a Decanter block from the Block | Input | Efficiency sheet: it allows to adjust the decanter results to match experimental data.
How can I realize something analogue when having the need of using the Flash3 block, because of the presence of vapor and light gases? | Solution: In order to take into account the entrainment of the 2nd Liquid in the 1st one and viceversa, one can use a sequence of Splitter and Mixer blocks, as shown in the image below:
- the splitter SP1 allows to separate a fraction of the 1st liquid from the B1 Flash3 block and mix it with the 2nd Liquid stream through the mixer MX2;
- the splitter SP2 allows to separate a fraction of the 2nd liquid from the block B1 and mix it with the 1st Liquid stream through the mixer MX1.
For avoiding that this operation occupies a large part of the flowsheet, one can create a Hierarchy that contains the Flash3 and the splitter+mixer blocks required for considering the liquid entrainment. In this way in the main flowsheet, one will see only a block that represents the 3phase separation unit; when double-clicking on it, one can access into the hierarchy and see all the blocks created for simulationg the liquid entrainment.
As one can see in the example file attached, in the main flowsheet one can see the 3-phase decanter represented by 1 block only (the hierarchy B1H, as per the image below), with contains all the block necessary for considering the liquid entrainment. The Hierachy block can be represented with different icons: the Flash3 in this case is considered.
Keywords: Flash3, Decanter efficiency, entrainment
References: None |
Problem Statement: Failure library does not list an equipment set recently added in the machine learning tab even after running machine learning training over the equipment. | Solution: Changes made to the database on the Machine Learning section are saved into the Mtell database, and can be accessed from the Failure Library section. However, the display for each section does not automatically refresh when user makes changes to the database from another section. To get the Failure Library to display the new changed to the database, the user will have to manually click the Refresh button located in top left corner of the Failure Library tools ribbon.
Keyword:
Database
Refresh
Missing Equipment
Keywords: None
References: None |
Problem Statement: What are the different dynamic initialization modes for a vessel in Aspen HYSYS? | Solution: Using the different initialization modes, you can determine the composition and amount of each phase in the vessel holdup. Whenever the initialization mode is changed, HYSYS forces the simulation case to re-initialize. There are three options available on the Specs page of the Dynamics tab of the vessel.
When Initialize from Products option is selected, the composition of the holdup is calculated from a weighted average of all products exiting the holdup (this is the default option). A PT flash is performed to determine other holdup conditions. The liquid level is set to the value indicated in the Liq Volume Percent field.
When Dry Startup option is selected, the composition of the holdup is calculated from a weighted average of all feeds entering the holdup. A PT flash is performed to determine other holdup conditions. The liquid level in the Liq Volume Percent field is set to zero.
When Initialize from User option is selected, the composition of the liquid holdup in the vessel is user specified. The molar composition of the liquid holdup can be specified by clicking the Init Holdup button. The liquid level is set to the value indicated in the Liq Volume Percent field.
Keywords: Vessel, initialization modes, Dynamics
References: None |
Problem Statement: Which files need to be preserved for modeler products file archiving? | Solution: During dynamic run of modeler products, multiple files are created in the working folder. For file archiving purposes and compatibility issues related to future versions, the following file types should be saved:
1. For any of the Modeler products, the primary file .acmf, .dynf, .ada, .bspf etc should be saved.
2. For future version compatibility purpose, the .bkp or .aprpkp file that generates the .appdf or .aprpdf file, needs to be saved. If needed, saved .bkp or .aprbkp file can opened in future versions to generate .appdf or .aprpdf files.
3. To save the exact state of the simulation and snapshots, save any file with a .snp extension created in the working directory.
Key Words
File, Properties, Back up, Snapshot
Keywords: None
References: None |
Problem Statement: How to Use Workbook Backup Utility? | Solution: You have several options for configuring automated backups of internal Aspen Simulation Workbook data.
To configure backups:
In the Model Variable Organizer, navigate to Configuration | Application.
Choose the location where you would like to store the backup files.
If enabling automatic backup, set the options for User Interaction and Backup Time Interval.
You can also perform an interim backup by clicking the Backup button on the Aspen ASW tab.
Key words
Backups of ASW, Backup button, backup files, backup folder
Keywords: None
References: None |
Problem Statement: On launch, Mtell View may return the following SQL Authentication error:
Server Error in ‘/AspenTech/AspenMtell/MtellView’ Log in Failed for user ‘xx/xx’.
Exception-An unhandled exception occurred during the execution of the current web request. Please review the stack trace for more information about the error and where it configured in the code’
Exception Details: System data SqlClient SqlException log in failed for user ‘xx/xx’
Cause
The Authentication Mode in the Registry entry for the Aspen Mtell configuration is incorrectly set to ‘Integrated’ | Solution: Change the registry entry for Authentication from ‘Integrated’ to ‘SqlServer’:
Invoke the Windows registry editor regedit.exe. This is typically found in the folder C:\Windows.
Navigate to the following key: Computer->HKEY_LOCAL_MACHINE->SOFTWARE->AspenTech->Aspen Mtell->Suite->Configuration.
Select “AuthenticationMode.
Right click and select Modify…
Change the ‘Value Data’ field from ‘Integrated’ to ‘SqlServer’
Click on OK.
Exit the registry editor.
Keywords: Registry Entry
Authentication Mode
Mtell View
SQL Server
References: None |
Problem Statement: How to resolve Broken Variable Links? | Solution: When you activate a simulation it is possible (perhaps because of the simulation being modified outside of ASW) for some links to be broken. When this happens, Aspen Simulation Workbook will inform you of this.
If you click OK, ASW will open the organizer to a filtered view of the model variables, showing only the broken links. You can also reach this view by clicking Check Links on the Organizer toolbar from the Model Variables view.
You can fix these links individually by right-clicking the variable in the Organizer toolbar and selecting Find Variable in Browser, then locating the desired variable within the tree of model variables.
You can click Find and Replace to open a panel allowing you to search for and replace specific strings within the names and/or paths of model variables.
In this panel:
Type a string in the Find box and click Find Next to highlight the next variable matching the string, or Find All to further filter to variable list to show just the matching variables.
Type a string in the Find box and one in the Replace with box, and click Replace Next to replace this string in names and paths one at a time, or Replace All to replace the string everywhere. When you use Replace All, you will be informed of the number of changes and given the option whether to make the changes. If the number of matches seems too large, check what variables are matching before you make the change.
Use the Name and Path checkboxes to control whether the find and replace actions act on the variable name, path, or both. These boxes are both checked initially.
If other filters have been applied, the find and replace actions only apply to the variables visible with these filters.
Key words
Broken variable links, connection with ASW, check links, the variables linked to the simulation, find variable
Keywords: None
References: None |
Problem Statement: Can I combine different objects on the flowsheet into a sub-flowsheet and assign a specific fluid package? | Solution: User can combine different objects on the flowsheet by just highlighting all required objects, then right click and choose “Combine into Sub-Flowsheet” option.
Once the new Sub-flowsheet is created you can assign a specific fluid package using Fluid Package Associations. Go to Home Ribbon, Simulation Section, Fluid packages Associations button. When Fluid Package Manager opens, you can notice created sub-flowsheet. Navigate to default “Basis-1” and select desired Fluid Package from drop down list.
Key words
Sub-flowsheet, Fluid Package Associations, specific fluid package
Keywords: None
References: None |
Problem Statement: User is unable to use the sensor prediction rank button when working with anomaly view. | Solution: The Sensor Prediction Rank becomes available for Failure Agents, while the Operating States option becomes available for the other types of agents. This is mainly because Failure Agents are looking for patterns of failure in specific sensors of the data being processed; while the Anomaly Detection agent is looking at what operating state is currently active and if there is any unusual behavior (not necessarily failure type issues) in the process.
Keywords: Anomaly Detection
Sensor Prediction Rank
References: None |
Problem Statement: After using a petroleum assay in my simulation, I notice the calculated saturated vapour pressure is not similar to my plant/lab data. Why? | Solution: Provided that the petroleum assay data has been correctly input (i.e. appropriate basis, e.g. mass or volume; appropriate standard, e.g. TBP, ASTM D86, etc), ensure that the light ends have been included in the data input prior to assay characterisation.
It is also very important to include the water content (if applicable) in the stream (from the simulation environment) as the assay characterisation will not generate this cut. Depending on the process (P, T) conditions, this cut can significantly contribute to the vapour pressure of the mixture.
Keywords: Petroleum Assay, Water cut, characterisation, vapour pressure
References: None |
Problem Statement: How can user model blocking the bypass of Baffle hole to Tube OD and Baffle OD to Shell ID in Aspen Shell and Tube Program? | Solution: In Aspen Shell and Tube Program, the user can reduce clearance, even to zero to model such situation. If the exchanger is later cleaned and the clearances open up. The original clearances can be input.
Keywords: Blocking the Bypass, baffle clearance
References: None |
Problem Statement: Why do I get different Enthalpy and Entropy values reported in Aspen HYSYS and Aspen Flare System Analyzer similar? | Solution: Properties like Molar Entropy and Molar Enthalpy are measured from a particular reference point (Pressure / Temperature) which is assumed to be zero. This reference point is different between Aspen HYSYS and Aspen Flare System Analyzer. That is why the values of Molar Entropy and Molar Enthalpy reported for the same stream by Aspen HYSYS and Aspen Flare should not be directly compared. For example, look at the images below which illustrate the difference between the values calculated for Entropy for the same stream in Aspen HYSYS and Aspen Flare.
In the case that a model includes hypothetical components, the properties estimation methods for such components is not the same for Aspen HYSYS and Aspen Flare.
Also, Aspen Flare has its own separate property packages which are different from those in Aspen HYSYS.
Keywords: Enthalpy, Entropy,
References: , Properties, Pressure, Temperature. |
Problem Statement: How can I set an On-Off controller using digital control point and Boolean latch gate operations together? | Solution: This can be done adding three digital control point operations and one Boolean latch gate operation.
Open the attached HYSYS case “OnOff_starter.hsc”.
We would like to control the level of V-100 (height = 1.127 m) through valve VLV-101. If the level is above the maximum level (0.80 m) the desired actuator position is 100%. If the level is below the minimum level (0.20 m) the desired actuator position is 0%.
From the Dynamics tab of the object palette, add three digital point controllers and one Boolean latch gate operation.
Open the first digital point (name it Full Open) and add the following Information:
Connections tab:
Process Variable Source - Object: V-100; Variable: Liquid Level.
Output Target – Object: Latch-1; Variable Set/Reset State.
Parameters tab:
Mode: Auto
Auto Operational Parameters: Latch
Threshold: 0.80 m (2.625 ft)
OP is On when: PV >= Threshold
Faceplate PV configuration:
PV Minimum: 0 m
PV Maximum: 1.127 m (3.698 ft) In this way, if the Level is higher than the threshold value, the digital point will be ON and will send 1 to Latch-1. If it is equal or lower than threshold value, the current OP state will be OFF and a zero value will be sent to Latch-1.
Open the second digital point (name it Reset) and add the following information:
Connection tab:
Process Variable Source – Object: V-100; Variable: Liquid Level.
Output Target – Object: Latch-1; Variable Set/Reset State.
Parameters tab:
Mode: Auto
Auto Operational Parameters: Latch
Threshold: 0.20 m (0.6562 ft)
OP is On when: PV <= Threshold
Faceplate PV configuration:
PV Minimum: 0 m
PV Maximum: 1.127 m (3.698 ft)
This second digital point will send 1 to Latch-1 when level will be lower than 0.2 and 0 when higher.
Open the Boolean operation Latch-1. In Connections tab | Output Target section, connect the third digital point using Add OP… button.
On Monitor tab, select Set as Prevailing Input to provide this prevailing input to the output of Full Open digital point.
Introduce the following parameters for the third digital point:
Connections tab:
Output Target – Object: VLV-101; Variable: Actuator Desire Position.
Parameters tab:
Mode: Auto
Auto Operational Parameters: Latch
Threshold: 0.5
OP is On when: PV >= Threshold
Faceplate PV Configuration:
PV Minimum: 0
PV Maximum: 1
The third digital point should get 1 or 0 from the latch Boolean operator. If it gets 1, the Digital point will be ON since the PV is higher than the threshold. The control valve was full open and the level would decrease till 0.2 m. At this level, control valve was close. The level would increase till 0.8 m, where the digital point would get 1 again.
Run the case and see the table showing the water vessel results, track the impact on the level in V-100 and the effect of the controllers.
TheSolution of the above steps is attached, please see case OnOff_Result.hsc.
Keywords: On-Off Controller, Digital Point, Latch, Boolean Operator
References: None |
Problem Statement: What's the maximum temperature supported Non-Ferrous material plates in ACCE? | Solution: Below is a table listing all Non-Ferrous materials available on ACCE and the maximum temperatures they withstand.
System Material Internal Pressure Max Temp External Pressure Max Temp
° F ° C ° F ° C
A1100 400 204 400 204
A3003 400 204 400 204
A5052 400 204 400 204
A5083 150 66 150 66
A5086 150 66 150 66
A6061 204 204 400 204
CA464 400 204 350 177
CU 400 204 150 66
CA110 400 204 150 66
CA655 350 176 350 176
CA122 400 204 150 66
CA715 700 371 700 371
HAST 800 426 800 426
HASTB 800 426 800 426
HASTC 1000 537 1000 537
I800 1500 815 800 426
I825 1000 537 700 371
C 20 800 426 800 426
INCNL 1200 648 800 426
I600 1200 648 800 426
NI 600 315 600 315
NI200 600 315 600 315
NI201 1200 648 1000 537
MONEL 900 482 800 426
M400 900 482 800 426
TI35A 600 315 600 315
Tl 600 315 600 315
TI50A 600 315 600 315
Keep in mind that entering a component with a design temperature above the material maximum temperature listed previously, will result in an error for the component. If a component has an error while evaluating, no price will be calculated.
Keywords: Maximum, Temperature, Non-Ferrous, Material
References: None |
Problem Statement: What's the maximum temperature supported Heat-Treated Steel material plates in ACCE? | Solution: Below is a table listing all Heat-Treated Steel materials available on ACCE and the maximum temperatures they withstand.
System Material Internal Pressure Max Temp External Pressure Max Temp
° F ° C ° F ° C
A353 250 121 900 484
A353 250 121 900 484
A553 250 121 900 484
A517A 650 343 650 343
A517B 650 343 650 343
A517E 650 343 650 343
A517F 650 343 650 343
Keep in mind that entering a component with a design temperature above the material maximum temperature listed previously, will result in an error for the component. If a component has an error while evaluating, no price will be calculated.
Keywords: Maximum, Temperature, Heat-Treated, Steel, Material
References: None |
Problem Statement: How can I set the Aspen Inferential Qualities debug switches without reloading the application? | Solution: You can set the debug switches for Aspen Inferential Qualities from the Production Control Web Server (PCWS), if you are using 2006.5 or newer, which does not require reloading the application.
Procedure is as below:
1. Go to the PCWS home page.
2. Go to the Configuration tab, select AspenIQ under column Sets
3. Make sure P1DBGLVL and P1DBGSW along with P2DBGLVL and P2DBSW are in the Selected list on the right. If not, find them in the Available list on the left and add them.
Go to the Online tab, Expand the Aspen IQ Application, and select the Aspen IQ application name in the navbar to open the application display to the right.
Click on the application name (on right side of the navbar) to open the Details page. The Details page provides a list of parameters (selected to appear in the column set). Here you will look for Debug Level for Prediction Process and Debug Switch for Prediction Process and also Debug Level for Update Process and Debug Switch for Update Process. Help is available to assist in setting these values, either from the web page or from the Aspen IQ Help tool found where the Aspen IQ Desktop tools are installed.
In general the Switches are set to equal to the number of cycles debug information is to be collected. Setting the value to 0 stops the debug logging. Level determines the amount of debug information you generate, 5 is a common setting.
The debug files will be found in the C:\ProgramData\AspenTech\APC\Online\app\{iq name} folder for the application.
You will want to send the debug files, along with the iqf and a confirmation of the version of iqp_main.exe found in the C:\Program Files (x86)\AspenTech\APC\Online\bin directory.
Keywords: Debug switch
PCWS
Aspen IQ
References: None |
Problem Statement: Aspen Process Explorer has the ability to store FREE or FIXED Comments for pre-configured Q records on Statistical Process Control(SPC) Charts such as an XBAR chart. These can be viewed in Aspen Process Explorer, aspenONE Process Explorer ,SQLPlus etc..
A FREE Comment is any text string that an operator may want to enter on the chart usually to indicate something unusual has happened such as a sudden Power Loss due to maybe a Thunderstorm . A FIXED Comment is a comment chosen from a Standard list of comments that has been setup by the Database Administrator. These would be for expected events such as a product change.
Configuration of Free or Fixed Comments are ONLY available with pre configured Q records. This feature is not available with AdHoc tags added to the plot.
This | Solution: provides the configuration that needs to be done for the Q record.
Solution
The pre-configured list of FIXED Comments is defined using a Q_FIXEDCommDef record. A default records is provided with the standard InfoPlus.21 snapshot called Q_Fixed. You may use & configure that record or else build yourself another one. You would then go to the Q record(s) where the Fixed area of Q records has a field called Q_FIXED_COMMENTS. In that field of your Q record you would enter the name of your Q_FixedCommDef record (such as Q_Fixed) that would be relevant for that Q record.
As far as FREE Comments are concerned, you need to configure a Q_FREECommDef record. AspenTech provides one of these records called Q_Free. You may use & configure that record or else build yourself another one. The link between the Q record and the Q_FREECommDef record is through the Q_FIXEDCommDef record. You need to edit the relevant Q_FIXEDCommDef record (such as Q_Fixed) because it has a Fixed Area field called Q_FREE_FORM_COM_REC. It is in this field that you need to enter the name of your Q_FREECommDef record (such as Q_Free)
Now, where are the Comments actually stored in the database ?
FIXED Comments, entered from Process Explorer, are stored in the Q records themselves. There is a Field called Q_FIXED_COMMENT in the Q_Sbgrps_In_Memory Repeat area where these are stored.
As far as FREE Comments entered from Process Explorer, there is another field in the Q_Sbgrps_In_Memory Repeat area of a Q record, called Q_FREE_COMM_TIME. This field stores the Time that a Free Comment was generated. The actual Free Comment is stored in the Q_FreeCommDef record (such as q_free ), inside the History Repeat Area Q_#0f_Free_Form_Coms
Keywords:
References: None |
Problem Statement: Error Access denied: No license code is available for the specified feature on this host. when using Aspen Licensing Dashboard. | Solution: Aspen Licensing Dashboard requires SLM_RN_FNC_LICDSHBRD license key in your license file. If this license key is missing you will get Error Access denied: No license code is available for the specified feature on this host. when using Aspen Licensing Dashboard.
Using SLM License Profiler check and verify if your license server have SLM_RN_FNC_LICDSHBRD license key.
Refer article for using SLM License Profiler: What is the SLM License Profiler and how do you use it?
Place a license key order to get a latest license file with SLM_RN_FNC_LICDSHBRD license key.
Keywords: SLM_RN_FNC_LICDSHBRD
Access Denied
References: None |
Problem Statement: What's the maximum temperature supported Low Alloy Steel material plates in ACCE? | Solution: Below is a table listing all Low Alloy Steel materials available on ACCE and the maximum temperatures they withstand.
System Material Internal Pressure Max Temp External Pressure Max Temp
° F ° C ° F ° C
A202A 1000 537 900 482
A 202 1000 537 900 482
A202B 1000 537 900 482
A203A 1000 537 900 482
A203B 1000 537 900 482
A203D 1000 537 900 482
A203E 1000 537 900 482
A204A 1000 537 900 482
A204B 1000 537 900 482
A 204 1000 537 900 482
A204C 1000 537 900 482
A302A 1000 537 900 482
A 302 1000 537 900 482
A302B 1000 537 900 482
A302C 1000 537 900 482
A302D 1000 537 900 482
A387A 1000 537 900 482
A387G 1000 537 900 482
A387B 1200 648 900 482
A387H 1200 648 900 482
A387C 1200 648 900 482
A387J 1200 648 900 482
A387D 1200 648 900 482
A387K 1200 648 900 482
A387E 1200 648 900 482
A387L 1200 648 900 482
A387F 1200 648 900 482
A387M 1200 648 900 482
A533A 1000 537 650 343
A533B 800 426 650 343
A533C 800 426 650 343
Keep in mind that entering a component with a design temperature above the material maximum temperature listed previously, will result in an error for the component. If a component has an error while evaluating, no price will be calculated.
Keywords: Maximum, Temperature, Low, Alloy, Steel, Material
References: None |
Problem Statement: The Aspen Manufacturing Suite (AMS) of products includes the database (Aspen InfoPlus.21) as well as the many other products that can be used with the database, such as Aspen Cim-IO, Aspen SQLplus, Aspen Process Explorer and Aspen InfoPlus.21 Administrator..
There already exists a few AspenTech knowledge-base articles relating to highly specific features within the AMS products on what to do when Daylight Saving Changes occur (commonly known as DST changes).
This article attempts to give a much better overview of the effect of DST changes on the AMS products, with a few links to some of the above mentioned articles. | Solution: The Short answer is that very little, if anything at all, needs to be manually performed at a DST change.
The important thing to realize is that our software assumes that all data that is stored in the IP.21 Database historian has an internal timestamp that is actually in Coordinated Universal Time (UTC).
UTC is sometimes referred to as Zulu time (Z) or Greenwich Mean Time (GMT)
When Cimio ( Or SQLplus, Or Process Explorer ) writes to an IP.21 database, API routines are called to convert the associated Local times to UTC.
Similarly, retrieval of data from the historian by clients such as Process Explorer, SQLplus or IP.21 Administrator, will convert the times from UTC for display purposes only.
This is performed via more API routines which examine the Timezone settings of the client PC, and adjust from UTC to Local times.
A feature of UTC timestamps is that they are continuous every day of the year. There is no impact from a DST change. Meaning that as far as IP.21 internal time storage there is NO overlap and NO gap - it is totally continuous.
However, in most parts of the world 'Local' times are affected by DST changes. Therefore the API conversion routines need to look at the Timezone setting, as well as the check-box Automatically Adjust for daylight Savings, and of course the date. All conversions are then performed with regards to all 3 criteria.
Therefore, viewing data across a DST change will automatically result in either a Gap or an Overlap of 1 hour depending which direction the Local clocks have changed. This means that the displayed local times will be exactly what they were when the data was stored in the historian.
All of the above of course assumes that
- Both the IP.21 Server PC and the (PE, SQL, Administrator) Client PC are correctly configured with regards to both Timezone, and adjust for DST changes.
- The Cim-IO Server is on a PC also configured for the correct Timezone and to adjust for DST changes.
If the Cim-IO Server is a VMS or Unix box rather than a PC then the administrator may need to manually reset those boxes at a DST time change.
The one other thing you may need to consider is the Rescheduling of things such as Reports, SQLplus Queries etc.
For example do you want a report to be generated every day at 7am whether it is Summer or Winter, OR do you want something scheduled on a daily basis where there will always be 'exactly' 24 hours between activations.
For more details on Rescheduling around DST changes please refer to Knowledge-base articles:
103559 - Daylight Savings time change - Why might my Schedule_Time appear wrong by one hour?
111140 - How to configure ScheduleActDef records to automatically account for daylight savings changes.
Another article of interest may be :-
110546 - Inserting values into history over Daylight Savings time change
Keywords: None
References: None |
Problem Statement: I have selected my external file under Customer External Files | Steel Material on my project basis view, however when I evaluate my project, there are no changes on the steel price. | Solution: Unlike most external files such as Civil Material or Indirects - Proratables, for Steel Material indirect file must be selected from Steel Material | Select and then applied to the project under Civil/Steel Specs | Steel material external file or apply to a specific area under Area Steel | Steel material external file.
You can even select more than one external steel file and apply different files to different areas.
Keep in mind that if you apply a steel file for the whole project and then select a different one for an area, the file selected for the area will override the one selected at project level.
Once you have selected the external file on a project level or area level, you can evaluate your project and the price changes will be applied.
Keywords: Steel, external, file
References: None |
Problem Statement: Can the fin alloy ratio be defined in Aspen Plate Fin Exchanger? | Solution: The fin alloy ratio cannot be defined directly. As an option, the fin thermal conductivity value can be specified in Program Options | Thermal Analysis.
Keywords: Fin alloy ratio, Fin thermal conductivity, alloy ratio
References: None |
Problem Statement: What's the maximum temperature supported Non-Ferrous material plates in ACCE? | Solution: Below is a table listing all Non-Ferrous materials available on ACCE and the maximum temperatures they withstand.
System Material Internal Pressure Max Temp External Pressure Max Temp
° F ° C ° F ° C
A1100 400 204 400 204
A3003 400 204 400 204
A5052 400 204 400 204
A5083 150 66 150 66
A5086 150 66 150 66
A6061 204 204 400 204
CA464 400 204 350 177
CU 400 204 150 66
CA110 400 204 150 66
CA655 350 176 350 176
CA122 400 204 150 66
CA715 700 371 700 371
HAST 800 426 800 426
HASTB 800 426 800 426
HASTC 1000 537 1000 537
I800 1500 815 800 426
I825 1000 537 700 371
C 20 800 426 800 426
INCNL 1200 648 800 426
I600 1200 648 800 426
NI 600 315 600 315
NI200 600 315 600 315
NI201 1200 648 1000 537
MONEL 900 482 800 426
M400 900 482 800 426
TI35A 600 315 600 315
Tl 600 315 600 315
TI50A 600 315 600 315
Keep in mind that entering a component with a design temperature above the material maximum temperature listed previously, will result in an error for the component. If a component has an error while evaluating, no price will be calculated.
Keywords: Maximum, Temperature, Non-Ferrous, Material
References: None |
Problem Statement: What's the maximum temperature supported Heat-Treated Steel material plates in ACCE? | Solution: Below is a table listing all Heat-Treated Steel materials available on ACCE and the maximum temperatures they withstand.
System Material Internal Pressure Max Temp External Pressure Max Temp
° F ° C ° F ° C
A353 250 121 900 484
A353 250 121 900 484
A553 250 121 900 484
A517A 650 343 650 343
A517B 650 343 650 343
A517E 650 343 650 343
A517F 650 343 650 343
Keep in mind that entering a component with a design temperature above the material maximum temperature listed previously, will result in an error for the component. If a component has an error while evaluating, no price will be calculated.
Keywords: Maximum, Temperature, Heat-Treated, Steel, Material
References: None |
Problem Statement: How to change the fluid package of single or multiple objects in Aspen HYSYS V10.0 | Solution: You can change the fluid package for a single or multiple objects using “Change Fluid Package” option. To use this approach user should select a stream or highlight several objects on PFD, right click and choose “Change Fluid Package”.
Note, if you change the fluid package of the stream, the package properties will be changed for all downstream elements after this stream.
There some articles that also can be useful for you:
How to change the fluid package for a single material stream?
Can I combine different objects on the flowsheet into a sub-flowsheet and assign a specific fluid package??
How to change the fluid package for a single or multiple trays in a column?
Key words
Change Fluid Package, Fluid Package Associations, Fluid Package of multiple objects, Fluid Package of the object.
Keywords: None
References: None |
Problem Statement: How to change the fluid package for a single material stream ? | Solution: Go to simulation environment, select and click on the stream, for which you want to modify the fluid package. Once the Stream Window appears, go to Worksheet tab/Conditions.
Navigate to Fluid Package Row and select from drop down list the desired fluid package.
Note, if you change the fluid package of the stream, the package properties can be changed for downstream elements after this stream
Key words
Change the fluid package, the fluid package of the stream.
Keywords: None
References: None |
Problem Statement: How do I create insert library file(*.ILB) by using insert file(*.INS)? | Solution: An Insert Library is a convenient tool that provides large amounts of fixed data, such as physical property data, to all users in a group. Please go through the procedure below.
Create a working directory for storing all insert files(*.INS)
Open “Customize Aspen Plus V8.X”
Provide working directory path in command prompt of Aspen Plus
Then type command “MAKEINS” for creating the user Insert Library called USER.ILB in working folder. You can see following messages in command prompt window
You can able to see the USER.ILB file created in the working director
This user.ilb file you can connect to your Aspen Plus. bkp file to do the calculations. (Run Settings | Provide the User.ilb file path)
Keywords: Insert file (*.ins), Insert User Library file (*ilb), Run Settings, Customize Aspen Plus, Command Prompt
References: None |
Problem Statement: How does EDR Mechanical determine the Lowest Stress Ratio? | Solution: In general, the Stress Ratio for a specific material is calculated as the stress at the Test Temperature divided by the stress at the Design Temperature. The Design Temperature is specified by the user, while the Test Temperature is, by convention, 70 F or 20 C. To retrieve values at design and test temperatures, EDR looks up the stresses using internal tables that come from ASME Section II, Part D.
Since the vessel is constructed using different materials, EDR needs to determine which will be the Controlling Component for both shell and tube side, selecting the component with the Lowest Stress Ratio (when two or more components have the same stress ratio, any of them can be selected).
EDR reports the Controlling Component under Results | Design Summary | MAWP/MDMT/Test/PWHT | Test Pressure tab:
In addition, under Results | Code Calculations | MAWP/MDMT/Test P/Static P | Hydrostatic Test Pressure sheet, EDR reports all the stress ratios for the different materials, in case user wants to verify the selection made by the program:
Keywords: Lowest stress ratio, LSR, Test pressure, hydrostatic test pressure
References: None |
Problem Statement: In the Pipe Segment unit operation, the user can choose the Aziz, Govier & Fogarasi correlation for modelling vertical 2-phase flow. The flow regime is based on the modified superficial velocities of the vapour and liquid phases. What are the definitions of these terms? | Solution: The modified superficial velocities are defined as follows:
Further information on this correlation can be found in the original reference: Aziz, K., Govier, G.A., and Fogarasi, M., Pressure Drop in Wells Producing Oil and Gas, Journal of Canadian Petroleum Technology, July-September 1972, pp 38-48.
Keywords: Pipe Segment; 2-ph correlation; flow regime; modified superficial velocity; Aziz, Govier & Fogarasi
References: None |
Problem Statement: The IF statement within the Spreadsheet unit operation does not appear to compare numerical values correctly. For instance, when 'identical' values are compared, the IF statement states that they are not equivalent. | Solution: This behaviour is because that the values being compared may not be truly identical (though with the number of significant figures shown, they may appear equal). Such discrepancies can occur for a number of reasons but the most common ones are due to unit conversion.
Keywords: Spreadsheet, IF statement, unit conversion
References: None |
Problem Statement: During the execution of your MS Excel VBA code, you get a VBA Run-time error 70 (Permission denied). | Solution: Though there are many methods that can lead to this issue, the general philosophy behind this error is that your VBA code is trying to write (i.e. input) to a variable that is considered output or locked (by another process).
A typical example would be trying to modify segments within the pipe segment model. Some segments within this block can have a length / equivalent length input (e.g. Pipe), whereas the length / equivalent length variable in other segments (e.g. elbow or valve) are locked and unable to accept a length input.
Keywords: VBA, Run-time error 70, Permission Denied
References: None |
Problem Statement: Is it possible to calculate the Research Octane Number (RON) for a pure known (i.e. not hypothetical) component in Aspen HYSYS? | Solution: For the calculation of the Research Octane Number (RON) in Aspen HYSYS, the stream should have AT LEAST three (3) components with non-zero composition. A workaround to roughly estimate pure component RON in non-petroleum assay stream is to create a stream with three components and set mole fraction for the desired component close to 1.
Furthermore, the RON calculation is limited to components with molecular weights greater than 70.
Keywords: RON, pure components
References: None |
Problem Statement: Currently in Aspen HYSYS, it is not possible to back calculate the composition of an unknown feed stream to a mixing point (Mixer, Balance, Separator or Tank unit operation) if the mixed product stream is defined as a Petroleum Assay (and all the other feed streams are fully defined). | Solution: It is helpful to think of this as the mathematical equation: A + B = C (where A, B are the feed and C is product). In this case, A and C are known, but not B. This equation requires 'back-calculation' to solve in its current form. The workaround is provide a 'forward calculating' input for the solver to use. To accomplish this, this equation can be equivalently represented as C - A = B, in which case, A and C are known and B can be 'forward calculated'.
Returning to the actual problem statement, to solve the unknown feed stream (Feed B), it will require the negative flow of the known feed (Feed A) flow to be used.
If after applying this workaround, there is a consistency error for the total flowrate, it is likely that the component balancing of the system is resulting in negative composition values. In this case, the assay characterisation input should be checked and/or modified.
Keywords:
References: None |
Problem Statement: How do I get a collections of utilities of a certain type in Aspen HYSYS through VBA Automation? | Solution: The property UtilityObjects from HYSYS.SimulationCase can be used to retrieve the collection of all utilities in a simulation case. However this property doesn't take an indexer to narrow by type the elements like the HYSYS.Flowsheet.Operations does (seeSolution 144577).
This simple piece code illustrates how to create an array of utilities filtered by type:
Dim hyApp As HYSYS.Application
Dim hyCase As HYSYS.SimulationCase
Dim hyUtil As Object
Dim utilCol() As Object
Set hyApp = CreateObject(HYSYS.Application)
Set hyCase = hyApp.ActiveDocument
Dim count As Integer: count = 0
For Each hyUtil In hyCase.UtilityObjects
If hyUtil.TypeName = htfsplusdesignutil Then
ReDim Preserve utilCol(count)
Set utilCol(count) = hyUtil
count = count + 1
End If
Next
Note: utilCol contains all the shell&tube sizing utilities
Keywords: VBA, HYSYS, Utilities
References: None |
Problem Statement: During the execution of your MS Excel VBA code, you get a VBA Run-time error 70 (Permission denied). | Solution: Though there are many methods that can lead to this issue, the general philosophy behind this error is that your VBA code is trying to write (i.e. input) to a variable that is considered output or locked (by another process).
A typical example would be trying to modify segments within the pipe segment model. Some segments within this block can have a length / equivalent length input (e.g. Pipe), whereas the length / equivalent length variable in other segments (e.g. elbow or valve) are locked and unable to accept a length input.
Keywords: VBA, Run-time error 70, Permission Denied
References: None |
Problem Statement: When Aspen Audit and Compliance (AACM) is installed in the MS Cluster environment, it may not work correctly after a failover.
This KB Article shows how to properly configure AACM in an MS Cluster environment. | Solution: Make sure that the AACM Extractor Service is not running on the inactive node. This service must be stopped and disabled both on the active and inactive node because it is not part of the failover process.
Furthermore, do not run the AACM manager console (MMC) on either node while making a failover switch because AACM Admin tool will try to start the AACM Server service on the inactive node before the failover process is complete.
Symptoms of misconfiguration
AACM Server will not record any events until the AACM Server service is restarted.
Keywords: AACM is not working in a cluster environment after a failover
References: None |
Problem Statement: How to import symbols from AutoCAD to Graphics Definer? | Solution: To import symbols from AutoCAD to Aspen Basic Engineering (ABE) | Graphics Definer follow the next steps:
1) Start Graphics Definer from the Start menu: Start | Aspen Basic Engineering | Graphics Definer.
2) Go to File | Open. On the Open window, browse to the location of the AutoCAD drawing file (either *.dwg or *.dxf) and change the ‘Files of type’ filter from default *.sym to either *.dwg or *.dxf. Next, click on ‘Open’.
3) After opening the AutoCAD drawing file, select the symbol you want to save in order to use it further in ABE. Once it is highlighted, click on the ‘Extract’ button. The Extract button will save the selected AutoCAD symbol on *.sym form, so it can be read by ABE. Save it on the correct symbols group folder of the proper Workspace.
4) Finally, before opening the Drawing Editor, open the Administration tool and reload the Workspace by right-clicking on it and selecting ‘Reload Workspace’. The new symbol created from the AutoCAD drawing will be then available in the Drawing Editor.
Keywords: Graphics Definer, Drawing Editor, AutoCAD, Symbols, Extract.
References: None |
Problem Statement: How does multi-valve analysis work in Aspen Plus/HYSYS PSV Sizing? | Solution: When sizing a relief valve, the capacity used is equal to the required orifice area divided by the available orifice area. This figure should not exceed 100% because that indicates the valve is undersized for the given scenario. On the other hand, grossly oversizing the valve is also not recommended because this can lead to chattering that can damage the valve.
In V8.8 and before, the program will generate a warning if the capacity used drops below 60%.
In V9.0 and above, the user can adjust the minimum value for capacity used that will trigger this warning by going to Preferences Manager | General Setup and checking the box labeled Warn when required flow is less than... of rated flow. The default value is 30%. Note that there is a lack of industry consensus on what is an acceptable capacity used. The user should use discretion and engineering judgment to decide.
For some valves, the various relieving scenarios may result in a wide range of required orifice areas. This can make it impossible to select a single orifice area that satisfies the constraints for capacity used. In that case, it may be necessary to consider a system where the flow is split between two or more valves. For a scenario requiring a smaller relieving flow, the flow only exits through the primary valve. The secondary valve will only open in scenarios requiring larger relieving flows.
This works because the secondary valve has a higher set pressure than the primary valve. API guidelines recommend increasing the set pressure of the secondary valve by 5% over the primary valve. During an emergency scenario, relieving material first opens the primary valve due to the lower set pressure. When the primary valve reaches 100% capacity, pressure rises in the system, which causes the secondary valve to open.
When performing a multi-valve analysis, the user can select the orifice sizes for the two valves. This will affect the calculated percentage orifice area used for both valves for each scenario. The idea is to employ a trial-and-error process to find a combination of orifice sizes where the constraints on capacity used are satisfied for every scenario.
In the example screenshot, the minimum capacity used is taken to be 30%. Scenarios 102, 103, and 104 only open the primary valve PSV 001 A. Scenario 101, representing a larger required relieving flow, will run PSV 001 A to 100% capacity, and the remaining flow will relieve out of PSV 001 B.
Keywords: Aspen Plus HYSYS PSV sizing multiple valves
References: None |
Problem Statement: How does multi-valve analysis work in Aspen Plus/HYSYS PSV Sizing? | Solution: When sizing a relief valve, the capacity used is equal to the required orifice area divided by the available orifice area. This figure should not exceed 100% because that indicates the valve is undersized for the given scenario. On the other hand, grossly oversizing the valve is also not recommended because this can lead to chattering that can damage the valve.
In V8.8 and before, the program will generate a warning if the capacity used drops below 60%.
In V9.0 and above, the user can adjust the minimum value for capacity used that will trigger this warning by going to Preferences Manager | General Setup and checking the box labeled Warn when required flow is less than... of rated flow. The default value is 30%. Note that there is a lack of industry consensus on what is an acceptable capacity used. The user should use discretion and engineering judgment to decide.
For some valves, the various relieving scenarios may result in a wide range of required orifice areas. This can make it impossible to select a single orifice area that satisfies the constraints for capacity used. In that case, it may be necessary to consider a system where the flow is split between two or more valves. For a scenario requiring a smaller relieving flow, the flow only exits through the primary valve. The secondary valve will only open in scenarios requiring larger relieving flows.
This works because the secondary valve has a higher set pressure than the primary valve. API guidelines recommend increasing the set pressure of the secondary valve by 5% over the primary valve. During an emergency scenario, relieving material first opens the primary valve due to the lower set pressure. When the primary valve reaches 100% capacity, pressure rises in the system, which causes the secondary valve to open.
When performing a multi-valve analysis, the user can select the orifice sizes for the two valves. This will affect the calculated percentage orifice area used for both valves for each scenario. The idea is to employ a trial-and-error process to find a combination of orifice sizes where the constraints on capacity used are satisfied for every scenario.
In the example screenshot, the minimum capacity used is taken to be 30%. Scenarios 102, 103, and 104 only open the primary valve PSV 001 A. Scenario 101, representing a larger required relieving flow, will run PSV 001 A to 100% capacity, and the remaining flow will relieve out of PSV 001 B.
Keywords: Aspen Plus HYSYS PSV sizing multiple valves
References: None |
Problem Statement: What is “Wall Specification” when defining tubes in exchanger geometry? Is there any difference by choosing “Average” or “Minimum”? | Solution: When you define the tubes in exchanger geometry, you will find two choices for “Wall specification”: “Average” and “Minimum”:
The choice of tube wall specification usually has no impact on the heat transfer performance. It is used to aid the purchase specifications.
Minimum Wall requires that the tube thickness shall not be less than the specified thickness. Average Wall permits the tube thickness to vary above or below the specified thickness. This variance or tolerance may be up to 12% of the specified thickness.
When ordering tubes, it is necessary to state whether the specified wall thickness is the average or the minimum required. This distinction is not usually considered to be significant as far as thermal design is concerned.
Keywords: Wall specification
Heat exchanger
Tube wall
References: None |
Problem Statement: How does heat transfer occurs in cross flow exchanger in presence of Distributors? | Solution: Distributors can be specified for axial flow streams in crossflow exchangers. In this case there is a two dimensional grid covering the exchanger. Distributors are, however, modeled using the same assumptions as for pure axial flow. The distributor heat transfer and geometry is averaged across the distributor width. The effective heat transfer coefficient is thus essentially the same for all transverse locations. No allowance is yet made for distributor area being concentrated on one side of the exchanger, or for there being components of both axial and transverse flow within the distributor.
Keywords: Cross Flow Exchanger, Distributor, Plate & Fin, Heat Transfer
References: None |
Problem Statement: The Wobbe Index can be calculated from the HHV (higher heating value). However, one may observe that the 'hand calculated' Wobbe Index (using the Heating Value reported in Aspen HYSYS) is not the same as the reported Wobbe Index (as calculated by the program). | Solution: Aspen HYSYS follows the ISO 6976 procedure for calculating the higher and lower heating values (HHV and LHV respectively) used in the Wobbe calculation. This procedure utilises heating values tabulated for different hydrocarbons.
In the stream property calculation (where the LHV and HHV values are calculated and reported), the heating values are calculated using the number of hydrogen atoms in each component. The HHVs / LHVs from these two sources can be different.
As such, there can be a discrepancy (reasonably small, in most cases) between the user-calculated Wobbe Index (using the HHV values reported in Aspen HYSYS) and the reported Wobbe Index (as calculated by Aspen HYSYS).
Keywords: Higher Heating Value (HHV), ISO 6976, Wobbe Index
References: None |
Problem Statement: How is the liquid holdup defined in the Pipe Segment? | Solution: The liquid holdup is defined as the ratio of the volume of a pipe segment occupied by liquid to the volume of the pipe segment, at a given point in the pipe segment. It is a fraction (no units) which varies from 0 (for all gas flow) to 1 (for all liquid flow).
The remainder of the pipe segment is, obviously, occupied by gas, which is referred to as gas holdup or gas void fraction.
The calculation of the liquid holdup will depend on the correlation you are using (Beggs & Brill, etc.). It is different than the volume fraction at the inlet of the pipe segment because of the slippage between liquid and vapour phases, meaning that the vapour will travel through the pipe at a higher velocity than the liquid. The slip velocity is defined as the difference in the actual gas and liquid velocities.
The no-slip liquid holdup, sometimes called input liquid content, is then defined as the ratio of the liquid volume to the pipe segment volume which would exist if the gas and the liquid traveled at the same velocity (no slippage). It can be calculated directly from the known gas and liquid flow rates.
The liquid holdup is used to calculate the pressure gradient in two-phase pipe segments, also using different correlations depending on the method used (Beggs & Brill, etc.).
Keywords: Pipe Segment, Liquid Holdup
References: None |
Problem Statement: For the characterization of solids, one approach is to define a mesh of particle size distribution (PSD) and specify the PSD mass fractions. Is there a model in Aspen Custom Modeler to replicate the PSD options available in Aspen Plus? | Solution: The attached model replicates the options available in Aspen Plus solid options.
PSD Mesh
- user: the user specifies the upper size for each class
- equidistant
- geometric
- logarithmic is not implemented
PSD distribution
- user
- normal
- log normal
- RRSB
- GSS
Keywords: PSD, derf, distribution, model
References: None |
Problem Statement: For the characterization of solids, one approach is to define a mesh of particle size distribution (PSD) and specify the PSD mass fractions. Is there a model in Aspen Custom Modeler to replicate the PSD options available in Aspen Plus? | Solution: The attached model replicates the options available in Aspen Plus solid options.
PSD Mesh
- user: the user specifies the upper size for each class
- equidistant
- geometric
- logarithmic is not implemented
PSD distribution
- user
- normal
- log normal
- RRSB
- GSS
Keywords: PSD, derf, distribution, model
References: None |
Problem Statement: This knowledge base article documents example Visual Basic for Applications (VBA) code needed to open a saved Aspen Process Explorer document via a Click event. | Solution: Aspen Process Explorer VBForm allows the user to include Visual Basic controls and associate VBA code with certain events. The following code sample would launch a new instance of Aspen Process Explorer with document file C:\temp\Document1.apx
Private Sub CommandButton1_Click()
RetVal = Shell(C:\Program Files (x86)\AspenTech\APEx\Pe\ProcessExplorer.exe C:\temp\Document1.apx, 1)
End Sub
Keywords: VB-Forms
References: None |
Problem Statement: ERROR: Invalid value in schedule_time
when trying to make records unusable that contain a Schedule_Time field, like scheduleactdef and others. | Solution: Field must be undefined before making the record unusable. To make it undefined, remove/delete any value present in the field, do this by typing a question mark character and press the RETURN key to commit the change.
Keywords: Invalid value
schedule_time
Databasesavedef
References: None |
Problem Statement: Is Aspen Flare System Analyzer applicable for design of low pressure flare system, like continuous vents (not emergency)? | Solution: Yes, Aspen Flare System Analyzer (AFSA) would be able to model continuous flares as it is a steady state simulator.
You can run the Design mode as it has three different calculation modes as explained in Article ID 000031924
Keywords: Low Pressure Flare, Continuous Vent
References: None |
Problem Statement: When I run the diagnostic described in | Solution: How do I troubleshoot the error message Unable to load simulation engine. Probable cause: Insufficient disk space or memory.?, I get the error, the program cannot start because ntvdm.exe is missing from your computer. How can I fix this issue?
Solution
This error is most likely due to a conflicting or missing file in the Windows operating system. There is a file named ppmon.dll in the C:\windows\syswow64 directory which is conflicting with the ppmon.dll required in the AspenTech Install folder. Aspen Properties is calling up the other version of the file in the windows directory, rather than the correct one in the AspenTech folder.
TheSolution is to rename the ppmon.dll file in the windows directory. This file is from a third-party and should not be in the Windows folder.
Keywords: ntvdm.exe, Aspen Properties Error, Unable to load simulation engine, Insufficient disk space or memory
References: None |
Problem Statement: How do you Implement Composition Delay behavior ? | Solution: Delay or lag time in dynamics is almost obvious. Here are the typical delay or dead time one would expect in different control operations
Pressure sensor: < 0.2 seconds
Thermocouple with thermo well: 6 to 20 second
Resistance temperature device (RTD) with thermowell: 6 to 20 seconds
Differential pressure level indicator: < 1 second
Control valve: 3 to 15 seconds
Control valve with valve positioner: 0.5 to 2 second
In most cases transfer Function block can be used implement delay behavior in Hysys dynamics.
Keywords: Composition Delay behavior, Dynamics
References: None |
Problem Statement: Aspen Production Record Manager (APRM) aliases provide an easy way to make a more user-friendly name for an InfoPlus.21 tag, like this:
Once the Alias has been created, then in a Aspen Process Explorer trend the alias can be added to a (APRM) plot instead of the related InfoPlus.21 tag.
But how can aliases be used in a more powerful way, making it easier to trend information in plots when each batches may be routed through different physical plant equipment? | Solution: The first step to take advantage of the aliasing capability of APRM is configuration, which has a couple of parts. This Knowledgebase article uses the example of the AspenChem demo. This simple process ends with three storage tanks. Each batch can finish by storing its product in any one of the storage tanks.
CONFIGURATION IN THE BATCH ADMINISTRATOR
These tanks exist -- in Aspentech terms -- as Units defined in the Batch Administrator. They are S401, S402 and S403. Each tank has a tag which reports back level. The tags are unique to each tank, and are ATCL401, ATCL402, and ATCL403.
Without using aliasing, the user would have to always know, for a given batch, what tank was being stored, and then trend the correct Infoplus.21 tag (ATCL401, etc.)
With aliasing though, we have decided on an alias named LEVEL, which is then tied to each unique tag for each unit, as shown here:
CONFIGURATION IN THE BCU ADMINISTRATOR
The second part of the configuration is that, as each batch runs, it is necessary to store the Unit name as a characteristic. In the Batch Conversion Utility (BCU), we have a BCU unit for each Storage tank. On the General tab for the Unit, we associate the BCU script with its Unit (all units must be previously defined in the Administrator):
Next, in the script itself we need to record the Unit characteristic itself when the trigger fires. The trigger for each storage unit is the valve for that tank being turned on (ATCV401, ATCV402, ATCV403). At that point we know which tank the batch is using for its Dump phase. This screen capture shows how the Unit characteristic is included for batches that store to tank S401:
VIEWING A BATCH READY FOR ALIASING
By looking in the Detail Display area we can see for example, that during the run of Batch 109, Storage tank S401 was used, since we see that Unit characteristic recorded:
Now that all of that configuration is done, we can use aliasing in a Aspen Process Explorer Batch plot (in the Batch Overlay plot, three batches have been added. Then using the Alias Browser, we choose the alias we defined for the DUMP Phase):
The final result in Process Explorer:
The demo triggered valve ATCV401 for all three of these batches, so, as it is shown in the Legend, all three aliases resolved back to tag ATCL401. The key point is the user does not have to be concerned with what tag is involved at all, regardless of the storage unit used in the Dump Phase.
Keywords: None
References: None |
Problem Statement: When attempting to add a role to the database permissions of the Aspen InfoPlus.21 Administrator, the user is unable to retrieve (or view) the Security Roles that have been defined (and are visible) in the AFW Security Manager. The following error message is received:
failed with an empty roles list when getting local roles list | Solution: This problem can be resolved by refreshing the AFW Security cache files and the Aspen InfoPlus.21 AFW cache file.
Stop Processing and clear cache files
1. Stop the Aspen InfoPlus.21 Database
2. In Control Panel services (services.msc) stop the following services:
AFW Security Client Service
Aspen InfoPlus.21 Task Service
3. Delete the local database cache file (IP21AFWCACHE.dat) from the group200 folder:
%ProgramData%\AspenTech\InfoPlus.21\db21\group200\
4. Delete the four AFW Security cache files
To locate the AFW Security Cache files see the CachePath found under the Server Registry Entries tab of the AFW Tools application. Usually, the four cache files listed below are located here: C:\ProgramData\AspenTech\AFW
aclcache.xml; AfwCache.txt; ApplCache.xml; rolecache.xml
Restart Processing
5. Start the AFW Security Client Service
Check the cache file location shown in the previous section to see that the four AFW Security cache files have been created
6. Start the Aspen InfoPlus.21 Task Service and the AFW Security Client Service
Check for the creation of the local database cache file (IP21AFWCACHE.dat)
7. Restart the Aspen InfoPlus.21 database (however note that if your InfoPlus.21 Manager already has STARTUP @ BOOT option checked, then the start-up of the Task Service will cause InfoPlus.21 to start up automatically).
Keywords: Client application
Process Explorer
References: None |
Problem Statement: When I try to launch any of the Economic Evaluation programs from the Windows taskbar, an error reading Error initializing Aspen - will appear and the application will not launch. | Solution: The root of this error is the way in which the shortcuts were added to the Windows taskbar.
When any of the Economic Evaluation products (Aspen Capital Cost Estimator, Aspen Process Economic Analyzer and Aspen In-Plant Cost Estimator) UI is open, the customer can right click on the taskbar icon and choose to pin the application to the taskbar.
This is a non-supported workflow that will not link correctly the application. If the user tries to open a link created this way, the error will pop up.
The correct way to create a shortcut to the taskbar is to browse for the applications from the Windows menu. These can be found on All Programs | AspenTech | Economic Evaluation V8.X or for V9 and above in All Programs | AspenTech | Aspen Economic Evaluation.
Once the application has been located, right click the application and select “Pin to Taskbar”.
A link created with this workflow will not show up the error and will open correctly.
Keywords: Error, Initializing, Taskbar, Pin.
References: None |
Problem Statement: Why are the stream properties of my external stream different from those of my internal stream? | Solution: If you are using a different property package for the column than for the rest of the simulation, there is a risk that the internal streams have different properties than the corresponding external streams. This is due to the fact that different property packages perform flash calculations differently. Aspen HYSYS requires the stream composition, a flowrate and two other values to perform a flash calculation. As an example, with a Pressure-Enthalpy (P-H) flash, Aspen HYSYS carries pressure and enthalpy across the flowsheet boundary and refreshes the stream.
If there is a big discrepancy, it is a good idea to:
1. Check the Transfer Basis in the Column View | Flowsheet | Setup. Pressure-Temperature or Pressure-Enthalpy flash are usually the best options.
2. Make sure that both property packages are applicable for the given set of components at the given operating conditions.
3. Do not use the subcooling option for a condenser with non-zero vapour flow.
Keywords: Column, Transfer Basis, T-P Flash, P-H Flash, Property Package.
References: None |
Problem Statement: What is the recommendation to handle the Bromine Number for the HBED and the Hydrocracker reactors? | Solution: In Aspen HYSYS Petroleum Refining, the recommendation is to specify the Bromine Number in the HBED reactor instead of letting the model to calculate it. For the Hydrocracker, this is not a limitation.
The difference between the HBED and the Hydrocracker is that the HBED does all its calculations in Equation Oriented mode (EO), whereas the Hydrocracker feed blender is part of the Sequential Modular (SM) HYSYS calculations before sending the information to EO. Therefore, for the Hydrocracker, it is fine to estimate a Bromine Number as it will automatically limit the olefin content.
For the HBED, you have the option of entering the Bromine Number or the olefin content. It would be find to estimate the Bromine Number, but the user should pay attention to what olefin content is being calculated. If it is approaching to zero, then it would probably be better to just enter the olefin content directly, otherwise that could cause the olefin number to be negative.
Keywords: Olefin Content, Bromine Number, HBED, Hydrocracker
References: None |
Problem Statement: When using Acid Gas – Chemical Solvent property package with MDEA in Aspen HYSYS V9 or prior, the regenerator heat duty predicted when specifying lean H2S loading may be too high. How shall a user improve the calculation results? | Solution: The root cause is that the electrolyte model parameters related to MDEA-H2O-H2S in V9 or prior were determined using VLE data of Jou et. al, 1982, which are inconsistent with accepted GPA data.
Aspen HYSYS V10 contains a revised set of electrolyte model parameters that better match the plant performance. The parameters were tuned using VLE data of GPA and selected plant data. When upgrading from models built in Aspen HYSYS V9 or prior, click the Upgrade Parameters button on the Acid Gas – Chemical Solvent property package | Set Up tab to use the updated parameters.
Keywords: None
References: s
1. Bullin, J. A., Davison, R. R., Rogers, W. J., The Collection of VLE Data for Acid Gas – Alkanolamine Systems Using Fourier Transform Infrared Spectroscopy, GPA Report, RR-165, 1997.
2. Huang, S. H., Ng, H. -J., DB Robinson Research Ltd., Solubility of H2S and CO2 in Alkanolamines, GPA Report, RR-155, 1998.
3. Jou, F. -Y., Mather, A. E., Otto, F. D., Solubility of H2S and CO2 in Aqueous Methyldiethanolamine |
Problem Statement: By default Aspen Custom Modeler uses the density to identify the second liquid phase in vapour-liquid-liquid equilibrium. There are, however, cases where the user would prefer to identify the phase by one or more key component(s). | Solution: The attached zip file contains a document that explains how to use the key components to identify a second liquid phase. The physical properties is embedded in the simulation file. The code is in the model vlle2. The parameter liqIDMethod is used to specify the method to identify the second liquid phase. If it is set to Key components, the user can select the key components.
pflash3 as Props_flash3 (T=T, P=P, z=z, x1=x1, x2=x2, y=y, lf1=lf1, lf2=lf2, vf=vf,
hv=hv, hl1=hl1, hl2=hl2, rhov=rhov, rhol1=rhol1, rhol2=rhol2, liqIDMethod:liqIDMethod,
KeyComps : AllKeyComps);
Let's take a look at the following declaration:
PARAMETER KCparameter uses stringparameter
valid as stringset;
END
The list of key components is declared as:
LiqIDMethod as LiqIDMethodParam (Description: Liquid phase identification method, value: Density);
AllKeyComps as StringSet (Description: All Key components);
nKC as integerparameter (Description: Number of key components, 0);
keycomp([1:nKC]) as KCparameter (Description: Key component, valid: componentlist);
This is done so that the user can select in the array keycomp the key components from the list of components due to valid : componentlist which specifies the valid component set. Specifying the list of valid values for a string parameter cannot be done on the generic stringparameter. This is why we declare KCparameter as a new stringparameter type.
Keywords: props_flash3
References: None |
Problem Statement: You may need to backup, archive or even purge data from the Aspen Production Record Manager database. | Solution: There are three options to be ale to work with your batches or data.
The administrator will allow you to:
1. Backup
The Production Record Manager Administrator allows you to allows you to export historic batch data for a single batch area to a single data file or across multiple batch areas to multiple data files. Multiple areas require one data file per area. Backing up historic data is useful if you want to copy data from an online system to an offline system for testing purposes. The file can be restored using the restore task.
2. Archive
Archiving is used to save online data for long-term storage. When data is archived, a single data file for a single area is created and the state for each piece of batch data is set to archived thereby allowing that data to be purged from the system.
3. Purge
Purge allows the removal of orders to keep clean and tidy system. Permanently removes the batches.
To do this follow these steps:
Right Click your Area and select Database
Select the Option you wish do run. For example Backup.
Select the Type drop down menu under Criteria and choose either 'Time Range' or ' Batch Range'
You can select a Time Range or a range of batches using the BatchID.
Once you have made selection then choose Browse to save your data to a location on your hard disk.
Press the Backup/Restore or Purge button button to continue.
NOTE: The Ignore Archive flag is for the Purge option. If you have already archived the data and want to purge you can do this.
Note: Purging is Permanent so make sure you backup first.
Keywords: None
References: None |
Problem Statement: It is observed that a rather large simulation using partial differential equations is solving slowly. Is there any setting that could improve the speed? | Solution: You could give a try to the transpose option in the Run, Solver Options, Linear Solver, with M48 solver.
When checked, MA48 uses a transpose of the matrix instead of the original matrix when solving linear systems. This has the effect of changing the direction in which MA48 searches for pivots. For some models, using the transpose will be faster than using the original matrix. You may wish to use this option if your simulation is very slow (particularly if each nonlinear iteration is taking a long time) to improve performance.
Note that in this case, the improvement is both in terms of speed and memory requirement.
Keywords: linear, MA48, options
References: None |
Problem Statement: What is the difference between the hydrocracker product transition and the hydroprocessor product transition? | Solution: The standard hydroprocessor product transition was designed to map from HCRSRK to the petroleum assay directly. This is better than the petroleum transition since the kinetic lumps have large gaps in boiling ranges. For this reason, the standard hydroprocessor product transition has become the default transition for the hydrocracker since V8.6.
The hydrocracker product transition is not recommended to be used in the hydrocracker reactor. This transitions was created to map the HCRSRK to the larger HCRSRKEXT which could then be mapped to an assay basis using a petroleum transition. The HCRSRKEXT just makes the case larger and requires two transitions.
Keywords: hydrocracker product transition, standard hydroprocessor product transition
References: None |
Problem Statement: What might be done when this error message is produced when accessing the Aspen Production Record Manager Batch Query Tool or a similar error is produced when using another AspenTech application?
Text of the error:
BatchQueryTool
Run-time error '6':
Overflow | Solution: In at least one instance the application was being run not locally on a user's system but rather by the user accessing it through a Citrix server. That particular situation was solved by having the user log out of the Citrix server and then their user profile was deleted by someone who administers the server. When the end user logged in again with a fresh (undamaged) user profile the problem went away.
Keywords: None
References: None |
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