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Problem Statement: When I open Datasheet Definer from start menu (Aspen Basic Engineering > Datasheet Definer - ABE Vxx, where Vxx is the version number), Excel opens without the 'Aspen Datasheet Definer' ribbon available at the top.
Note: This knowledge base (KB) article assumes that Datasheet Definer Add-in is not found under the 'Disabled items' as described in KB 48951 (Why does Datasheet Definer Tab disappear in Excel?) | Solution: If you are not able to display the Datasheet Definer tab, there could be two possible reasons:
A. Datasheet Definer Add-in Unloaded: It will display a load behavior as seen below:
To display the load behavior of the image above, follow these steps:
i) Start Microsoft Excel
ii) Go to File > Options > Add-ins
iii) In Excel Options windows choose Add-Ins from left hand side and in Manage drop down box select COM Add-ins as shown in screenshot below and click on Go button. This will show available commercial Add-ins and you can enable it if AZDatasheetDefiner Add-In is in this list.
B. Datasheet Definer Add-in Not Loaded due to runtime error:
This runtime error could happen because the security certificate of the trusted publisher has expired:
Solution
For Issue A:
1. Start Microsoft Excel (Do NOT use the Excel file that was opened during Datasheet Definer ABE - Vxx opening steps)
2. Go to COM Add-ins as previously described
3. Enable 'ABEDefinerAddIn' and hit 'OK'
4. Click Install on the Window that pops up:
Once the ABEDefinerAddIn has been installed, the load behavior will change and Aspen Datasheet Definer ribbon will be available at the top.
For Issue B:
Solution step 1-3 for issue A applies but installation cannot proceed because of the following error:
To avoid a reinstallation of AspenTech products, you can adjust the trusted publisher security settings.
Go to File > Options > Trust Center > Trust Center Settings and uncheck the 'Require Application Add-ins to be signed by Trusted Publisher' as shown below:
Click OK and then follow the steps 1-3 again as described for Issue ASolution and Aspen Datasheet Definer should be available as Ribbon again.
If the above steps do not resolve the issue, please contact AspenTech Support ([email protected]).
Keywords: ABEDefinerAddIn Not Loaded, COM AddIn, Runtime Error, Application-defined or object-defined error, error in AZDatasheetDefiner, application defined error
References: None |
Problem Statement: I created a spreadsheet and added aqueous and liquid phase liquid volume flows at standard conditions from a stream. However, I noticed the values for the phases are reversed on the spreadsheet. Why is this happening? | Solution: This is a known issue which occurs when the variable Phase - Liq Vol Flow @Std Cond is selected for the spreadsheet. Instead, please use Phase Liq Vol Flow @Std Cond (no dash) as a workaround.
Keywords: Liquid, volume, flow, standard, conditions, aqueous, reversed, switched
References: None |
Problem Statement: How to resolve the error, The specified project location does not exist or is invalid? | Solution: This error may occur if the file for logo.bmp is missing from C:\Users\Public\Documents\AspenTech\Shared Economic Evaluation V10.0\Reporter\Database. If logo.bmp is missing from this directory, then it will cause an error when generating the report.
TheSolution is to create a new logo.bmp file at the location. To do so, open Microsoft Paint (or any similar photo editing software), create a new image and save it as logo.bmp. Then put the .bmp in the directory above. Note it doesn't matter what is drawn on logo.bmp because it will be overridden when generating the report, the software simply needs to see the file.
Keywords: Report, error, logo.bmp
References: None |
Problem Statement: What is counter ion and how to apply it to modeling? | Solution: The purpose of counterion is to ensure charge balance of overall exchange process is kept. Take water softening process as an example: (Ca+2) + 2 (Cl-) + 2 (Na+R-) = 2 (Na+) + 2 (Cl-) + (Ca+2)•(R-)2 where (R-) is a cationic exchange resin. In this case, (Na+) is the counterion which is adsorbed in the “clean” resin bed at time zero and will maintain the charge balance during the course of ionic exchange. Once (Ca+2) is adsorbed into the resin R-, Na+ will be desorbed/released and overall charge balance remains. User doesn’t need one counterion for each ionic species to be exchanged / adsorbed. However, user does need one counterion for each type of electrical charge involved in the exchange between ionic species and resin. That says one positive charged counterion for cationic exchange resin or one negative charged counterion for anionic exchange resin is needed. The screenshot below demonstrates specifying Na+ as counter ion for a cationic exchange resin.
Keywords: ionic exchange
counter ion
charge balance
References: None |
Problem Statement: Aspen Basic Engineering (ABE) Explorer says I cannot delete a bridge as it is locked by a user even though I am the only user on that workspace. How do I force it to unlock the bridge so I can delete it? | Solution: Create a new folder on the Explorer and place the Bridge on the new folder. Once bridge is added to the folder you can right click on the bridge and delete it.
Keywords: Bridge, Explorer
References: None |
Problem Statement: Are results in Hydrate Formation based on hydrate formation curve or hydrate dissociation curve? How accurate is the hydrate formation prediction? | Solution: The results in Hydrate Formation are based on hydrate formation curve. On a P-T plot, Hydrate Formation curve sits on the left side closer to the origin where temperature is lower. Hydrate Dissociation curve is to the right of the P-T plot.
To the left of Hydrate Formation curve is the Hydrate Zone (also called Stable Region) where hydrate formation is thermodynamically stable. The region in between of Hydrate Formation Curve and Hydrate Dissociation Curve is called Hydrate Risk Zone (also called Metastable Region). To the right of Hydrate Dissociation Curve is the Hydrate Free Zone.
Hydrate Formation requires low temperature and high pressure to occur. Even in the Hydrate Zone, where the system has crossed the Hydrate Formation curve, hydrate formation is not guaranteed to occur as there is often a time delay. But thermodynamically, hydrate formation is stable within this region.
HYSYS provides two models for hydrate formation study: CSM model and Ng & Robinson model. The base property method also has impact on thermodynamic calculation of the hydrate formation model. User can find an example case study data for some systems in the attachment of this article. The case study data shows the prediction of the two models against experimental data.
Keywords: Hydrate formation, CSM Model, Ng & Robinson, Hydrate Dissociation Curve
References: None |
Problem Statement: What is the reference of higher and lower heating value calculations? | Solution: Gas calorific value (higher heating value and lower heating value) calculations are based on ISO 6976: 1995.Solution document 98758 contains the equations involved in calorific value calculations.
Keywords:
References: , calorific value, higher heating value, lower heating value, HHV, LHV |
Problem Statement: How does HYSYS calculates Lower and Higher Heating Values of a stream? | Solution: HYSYS calculates the lower heating value as the sum of the heat of combustion times the mole fraction for each component in the stream.
LHV = sum(x[i] * Hcomb([i])
The higher heating value is calculated as the lower heating adjusted by the heat of vaporization of water under standard conditions multiplied by the mole fraction of each component and the number of hydrogen atoms divided by 2.
HHV = LHV + sum(x[i] * HvapH2O *Hatoms[i]/2)
This just adjust the heating value by the heat of vaporization of the water formed during combustion, which by definition is the only difference between lower and higher heating values.
HYSYS will therefore report empty if the Heat of Combustion is not specified for one of the components. Hypothetical components by default do not have a value specified.
Keywords: Lower Heating Value, Higher Heating Value, Calorific Value, LHV, HHV
References: None |
Problem Statement: Aspen Properties Database Manager middle pane is coming up blank. See below: | Solution: The missing pane can be resolved by copying the file mmc.exe.config from C:\ProgramData\AspenTech\APED V12.0 (modify the path to match the version you are using) to C:\Windows\SysWow64.
Alternatively, you can add the following lines from the mmc.exe.config file (located under APED folder) into the existing file (under C:\Windows\SysWow64):
<startup useLegacyV2RuntimeActivationPolicy=true>
<supportedRuntime version=v4.0 />
</startup>
Keywords: Missing Pane, Aspen Properties Database Manager middle pane
References: None |
Problem Statement: When a RadFrac column model includes specifications on vaporization stage efficiencies, the liquid composition leaving the tray is not an equilibrium composition. In other words, if the liquid flow from such a stage is flashed at the conditions of that stage, the bubble point temperature is generally higher than the temperature from the RadFrac T-profile. | Solution: The issue with efficiencies is that one composition (liquid or vapor) must be obtained from a flash calculation, in order for the other one to be calculated from the equation which defines the efficiency.
Vaporization efficiency is defined as the ratio of the actual vapor composition of a given component over its equilibrium vapor composition:
Ev = y / y*
Using the definition of the thermodynamic K-value (y* = K*x), we can re-write:
y / Ev = K * x …………………(1)
When vaporization stage efficiencies are used, RadFrac obtains the vapor composition from a flash calculation. Hence, it is a saturated vapor, i.e. when flashed again the state variable values will remain the same. Liquid compositions are obtained by re-arranging the above equation:
y / x = K * Ev
These liquid compositions are non-equilibrium compositions, i.e. when flashed at [P = Q = 0], the state variable values will change.
Effects
As Ev decreases, the vapor pressure must increase which means that the temperature must increase. To understand this, simply consider Raoult's law
x PL = y P
or
K = y / x = PL / P
Using the above definition for efficiency, we get
y = Ev (PL / P) * x
In this equation, the total (stage) pressure is fixed (user input). So as Ev decreases, vapor pressure and thus temperature will increase.
Using vaporization efficiency alters the T profile and this may alter relative volatility.
Symbols
Ev = vaporization efficiency
y = vapor composition exiting tray
x = liquid composition exiting tray
y* = equilibrium vapor composition
K = thermodynamic K-value
P = total or system pressure
PL = pure component vapor pressure
Keywords: vaporization efficiency, Radfrac efficiency, vapor composition
References: None |
Problem Statement: HEATX block is not letting me turn off the henry component for Peng Robinson and shows input incomplete. | Solution: There are two different Right Mouse Button (RMB) clicks for the field for Henry Components. If mouse is hovered over the field and then click right mouse button, it will bring up the below menu items.
If you select the field first then clicking right mouse button, it will bring up another menu items with Clear disabled.
With the first option, you should be able to turn off Henry Components for HEATX block.
Keywords: Henry components, HEATX
References: None |
Problem Statement: How to solve “WARNING: Field name is not liked to a cell/range in the document.”? | Solution: The Field Name exists in Name Manager but it has no reference to a cell/range in the datasheet.
How to fix:
If the Field Name is not associated to an ABE field, then the Field Name can be linked to an empty cell and then deleted using the ABE’s Delete button.
1. Go to Formulas menu > Name Manager button > Name Manager dialog.
2. Identify the field name which should have the “Refers to:” field with the value “#REF!#REF!”.
3. Double click on the field name.
4. In the New Name dialog, set the “Refers to” field to an empty cell (where no ABE field or range name is defined) For example: A1, like this: ='Page 1'!$A$1. Click OK.
5. Verify the field name is available in the Names drop down:
6. Save the file changes.
7. Now to delete the field name, select the cell that was linked to it and click on the Delete button in the Editing group of ABE Datasheet Definer add-in:
The field name Filed2441 will be deleted from the Name Manager’s list.
8. Save the file changes.
9. Validate the datasheet:
10. Confirm in the Validation output that the warning message is not reported anymore.
If there are more fields with the same issue, these fields can be linked to the same empty cell and then be deleted one by one with the Delete button of ABE:
Keywords: Field, Warning, Template, Datasheet Definer
References: None |
Problem Statement: Is the Twu alpha function built in with the Peng-Robinson (PENG-ROB) and/or PR-BM (Boston Mathias) Equation of State (EOS) models? What are the option codes associated with each of these property methods (also called options sets)? | Solution: The Peng-Robinson equation of state is the basis for the PENG-ROB and PR-BM property methods in Aspen Plus and Aspen Properties. The model has been improved with the ability to select different alpha functions and has been extended to include advanced asymmetric mixing rules.
By default, the PENG-ROB property method uses the literature version of the alpha function and mixing rules (Model name: ESPRSTD). The PR-BM property method uses the Boston-Mathias alpha function and standard mixing rules (Model name: ESPR). These default property methods are recommended for hydrocarbon processing applications such as gas processing, refinery, and petrochemical processes. Their results are comparable to those of the property methods that use the standard Redlich-Kwong-Soave (SRK) equation-of-state. SeeSolution 000084485 for more information on SRK.
The new capabilities for PR and PR-BM option sets for version 2004.1 are listed below:
1. New alpha functions for better representation of pure component vapor pressure. In addition to the standard and the Boston-Mathias alpha functions, the Gibbons-Laughton and Twu alpha functions have been added.
2. The Peng-Robinson mixing rules have been extended with an asymmetric term (Lij) based on the work of Mathias-Klotz-Prausnitz. When advanced alpha functions and asymmetric mixing rules are used with the correct parameters, the Peng-Robinson model can be used to accurately model polar, non-ideal chemical systems.
3. Binary interaction parameters (Kij) are temperature dependent, which allows greater flexibility in fitting data over a wider range of temperatures and pressures.
4. Volume translation (volume shift) to empirically improve the prediction of liquid molar volume. A volume shift parameter for each component must be provided by the user.
The Basic Peng-Robinson Model
The equation for the Peng-Robinson model is:
P = RT/((c + Vm) - b) - a/((Vm + c)(Vm + c + b)+b(Vm + c - b))
where:
a = a0 + a1
a0 is the standard quadratic mixing term, where Kij has been made temperature-dependent.
a0 = sumi ( sumj ( xi xj sqrt(ai aj) (1-kij) ))
a1 is an additional, asymmetric (polar/non-linear) term introduced in version 2004.1.
a1 = sumi xi [sumj xj ((ai aj)^0.5 lij)^1/3] ^3
b = sumi xi bi
c = sumi xi ci
ci = 0.40768 (R Tci / Pci) (0.29441 - zRAi)
Please refer to the online help (Physical Property Methods and Models
Keywords: alpha functions property method options sets
References: Manual | Chapter 3 Property model Descriptions | Equation of State Models | Peng-Robinson (alpha functions) for a complete list of equations and alpha function equations.
Each property method is assigned a particular list of pure component parameters and binary mixing rule parameters for PENG-ROB and PR-BM according to the following table.
Peng Robinson
TC
PC
Acentric
Zrai
Kij
Lij
Model Name
old PENG-ROB
TCPRS
PCPRS
OMGPRS
PRZRA
see notes 1-3
No term
ESPRSTD/ESPRSTD0
PR-BM
TCPR
PCPR
OMGPR
see note 4
see notes 1-3
see note 1
ESPR/ESPR0
PENG-ROB
TCPRS
PCPRS
OMGPRS
see note 4
see notes 1-3
see note 1
ESPRSTD/ESPRSTD0
Notes
1. In version 2004.1, the PENG-ROB and PR-BM option sets use parameters named PRKBV and PRLIJ.
PRKBV = PRKBV /1 + PRKBV /2 * Temp + PRKBV /3 / Temp
PRKBV /4 and PRKBV /5 provide an indication of the valid temperature range, however the temperature range is not limited to between PRKBV /4 and PRKBV /5.
PRLIJ = PRLIJ /1 + PRLIJ /2 * Temp + PRLIJ /3 / Temp
PRLIJ /4 and PRLIJ /5 provide an indication of the valid temperature range, however the temperature range is not limited to between PRLIJ /4 and PRLIJ /5.
2. In version 12.1, the PENG-ROB and PR-BM option sets used the parameter PRKIJ and no additional asymmetric term was used.
The overall Kij = Kji
3. When 12.1 files containing PRKIJ are opened in 2004.1:
PRKIJ parameters are converted to PRKBV /1 parameters. The temperature-dependent parameters default to 0.
4. ci is only calculated if the Peneloux volume translation is enabled (see below). Peneloux volume translations can greatly increase the accuracy of liquid density calculations. If the option code for these option sets is switched to use volume translation, PRZRA will be used.
Use of Alpha Function Option Codes for Peng Robinson
The alpha functions, model name, and option codes in the PR EOS models are provided in the following table. See Option code definitions section for detailed information on alpha functions.
Alpha Function
Model Name
First Option Code
Standard PR
(PENG-ROB)
ESPRSTD0, ESPRSTD
1
Standard PR\
Boston-Mathias
(PR-BM)
ESPR0, ESPR
ESPRWS0, ESPRWS
ESPRV20, ESPRV2
(default) 0
0
0
Extended Gibbons-
Laughton
ESPR0, ESPR
2
Twu Generalized
ESPR0, ESPR
3
Twu
ESPR0, ESPR
4
Mathias
-Copeman
ESPRWS0, ESPRWS
ESPRV20, ESPRV2
2
2
Schwartzentruber-
Renon-Watanasiri
ESPRWS0, ESPRWS
ESPRV20, ESPRV2
(default) 3
(default) 3
You can verify and change the value of possible option codes on the Properties | Property Methods | Model form. For example, there are two ways to select the TWU alpha function:
1. If using the PENG-ROB, the default model names are ESPRSTD0\ESPRSTD. You will need to change the model names from the model form. Select and modify the PHIVMX and Pure component PHIV to the model names in the table (ESPR / ESPR0). The corresponding model names will automatically change for the properties that are affected. This is now similar to the PR-BM method as the default option codes for ESPR/ESPR0 are 0. The final step is to change the option code by selecting PHIVMX and clicking on the option code. In the first option code, replace 0 with a 4. The pure component properties will automatically change to use the TWU option code.
2. If you start with PR-BM, you only need to switch the option code as above. PR-BM uses ESPR0/ESPR as the default model names.
Option Code definitions for PENG-ROB and PR-BM property methods
Option Code 1 defines the Alpha function used:
0 - Standard (PENG-ROB) Alpha function for PR EOS when Tr < 1, Boston-Mathias (PR-BM) alpha function for Tr>1 (Note - Standard Alpha function is always used for Helium, even if Tr > 1)
1 - Standard alpha function for all components at all temperatures
2 - If PRGLP parameters are present, Gibbons-Laughton alpha function with Patel extension is used for all components. PRGLP-1 are entered in the Data | Properties | Pure Component form. Click New, select T- dependent correlation | Select Alpha function EOS and PRGLP-1.
3 - TWU generalized alpha function (new in 2004.1)
The Twu generalized alpha function is considered the best function as it behaves better than others at supercritical conditions (T>Tc) and at high omega since it does not have a minimum. This is important for high molecular weight pseudo components. L, M, and N parameters vary depending on the EOS and whether the temperature is above or below Tc of component. L, M, N are entered in PRTWUP-1 from Data | Properties | Pure Component. Click New, select T- dependent correlation | Select Alpha function EOS and PRTWUP-1.
4 - Twu alpha function (new for 2004.1)
Same as 3, but L, M, and N are determined from regression of pure-component vapor pressure data or other such data as liquid heat capacity.
Option Code 2 defines the mixing rules for model ESPR, ESPR0:
0 - Standard PR Mixing Rules with symmetric Kij, no Lij (default)
1 - Standard Mixing Rules with asymmetric Kij and Lij
Option Code 3 determines if water is present in the current mixture:
0 - Water is not explicity identified. It is treated as any other component does not use Steam tables (default)
1 - Water is explicitly identified. Water properties (H, S, G, V) are calculated from the steam tables
Option Code 4 defines whether or not the Peneloux liquid volume correction is used:
0 - Do not apply the Peneloux liquid volume correction (default)
1 - Use the Peneloux liquid volume correction (see SRK)
Option Code 5 defines how the cubic equation is solved:
0 - Analytical |
Problem Statement: When making calculations near critical conditions, flash calculations may generate error messages. These messages may be generated not only from a flash block (Flash2 or Flash3), but may happen for any block when a flash is done to set stream conditions, to calculate a prop-set, or during generation of a PT-envelope or other flashcurve. A variety of error messages might indicate similar problems; here are some examples:
FLASH RESULTS ARE WITHIN TOLERANCE, BUT MAY BE UNSATISFACTORY BECAUSE EXTRAPOLATED EOS VAPOR VOLUME ROOT WAS USED FOR PROPERTY CALCULATIONS.
FLASH CALCULATIONS FAILED TO CONVERGE IN 30 ITERATIONS. DEW POINT PRESSURE COULD NOT BE CALCULATED DUE TO FLASH FAILURE.
FLASH CALC CONVERGED TO THE TRIVIAL | Solution: ; RESULTS ARE UNRELIABLE. SPECIFIED TEMP OR PRES MAY BE ABOVE THE MIXTURE CRITICAL POINT. GIVE TEMP AND PRES SPEC AS A WORKAROUND.
ERROR IN PHYSICAL PROPERTY SYSTEM WHILE GENERATING PROP-TABLE: PT1 (LQROOT.1) LIQUID ROOT NOT CONVERGED IN EOS MODEL...
Solution
Often when these messages are generated, the results are completely acceptable, but it is a sign that the user needs to examine the results carefully.
As a first step, the user should figure out how the conditions of this flash compare to the critical region for the mixture. SeeSolution 000082618 for a more detailed explanation of how to determine the true critical point of a mixture. If the flash is failing is at a pressure above the critical pressure, it may be because flash specifications involving Vapor Fraction are used, which are not physically reasonable in that region. (That includes specifying dew or bubble point.) In such a case the user should specify the flash with some other combination of variables (any two of Temperature, Pressure, and Enthalpy or Duty).
If the conditions of the flash are physically reasonable and the results look OK, they probably are OK. The error message can often be avoided by changing the flash specs (often Temperature and Pressure work better than vapor fraction or enthalpy). Increasing the maximum number of iterations or (less desirable) loosening the flash tolerance may allow the Flash algorithm to find aSolution without generating the error messages. Conversely, sometimes tightening the flash tolerance can help avoid infeasible regions. These parameters can be changed globally on the Setup->Calculation Options->Flash Convergence sheet.
On the Setup | Calculation Options| Flash Convergence sheet, you can also change the temperature and pressure limits for the calculations. Typically, changing the limits does not help the convergence though it may speed it up. Occasionally, the limits do need to be extended for some processes involving extreme conditions such as a cryogenic helium system.
Keywords: Flash problems; Convergence; roots;
References: None |
Problem Statement: Is it possible to have different offsets in APS and MBO? For example in APS, if the user wants as 7 hours offset and MBO they want 0 hours offset. | Solution: For an APS/MBO shared database, having different offset hours will cause logic confusion for the tank baseline since APS and MBO share the same baseline for the tanks. Other than that, the simulation results/trend for the same tank in APS and MBO will be inconsistent, for importing APS Run Downs to MBO, it will also cause problem. Overall, the entire integrated APS/MBO workflow will have issues. If APS and MBO databases are different then there will be no issues as it will be as good as two different models. Users of different DBs will not see each other's changes.
Keywords: None
References: None |
Problem Statement: The Keep Only Unique Cases stored procedure doesn't seem to work when transitioning from Access db to SQL | Solution: The “keep unique” stored procedure makes the assumption that the maximumSolution id is the latest execution. This “maxSolution id” is a standard assumption used in other areas of code/logic in PIMS. But because theSolution ids are mixed (using both sql server generated ids and also the original datetime generated ids (which is still used for access databases)), then the maxSolution id is actually the one that starts with “6”. So when the user runs with “keep unique” and there is already a case withSolution id that starts with “6”, then the new case that starts with “498” will be deleted and that is why the user gets the error of “Solution data was not written to the database”. The data was written for the new case but it was then deleted due to the “keep unique” stored procedure. The unique case kept in the sql server database will be the one that starts withSolution id “6”.
The workaround is to clean up the database and remove the data that hasSolution ids that start with “6”.
Keywords: None
References: None |
Problem Statement: Which values in the BCI spreadsheet are multiplied by the scale factor set for a property? | Solution: In the BCI setup, user will put in the min and max constraints in MBO. BCI will process the property from MBO results tables - Specs, GlobalSpecs, etc. When user submits the recipe to generate BCI results, it multiplies BlendValue (blend composition property), PropertySpec (property specification), PropertyLow, and PropertyHigh with the scale for this property. The final submitted recipe in the XML file for BlendValue, PropertyTarget, PropertyLowLimit, and PropertyHighLimit will be scaled regardless of whether the property came from MBO or not.
Keywords: None
References: None |
Problem Statement: Is it possible to create a Non-linear equation using a case in PIMS? | Solution: Currently there's no way to create or modify a NLE in the CASE table. All NLEs attached to the model tree are used in all cases.
One possible workaround could be to divide the cases into 2 spreadsheets - When running the cases with NLEs, enable the spreadsheet with the appropriate cases. When running the cases without NLEs, enable the other spreadsheet with the corresponding cases.
Keywords: None
References: None |
Problem Statement: Is there a way to change the decimalization of the blend recipe in MBO? | Solution: The number of decimal places of composition percentages on a blending event dialog box is hard coded to 3. At present, it is not possible for users to change it in the model settings.
Keywords: None
References: None |
Problem Statement: What could cause the Failed to update the data table: ORION_MGR_ASSAY_IMP_MASTER error message when importing assay data through EIU? | Solution: When importing assay data through EIU, you may get the following error message:
Failed to update the data table: ORION_MGR_ASSAY_IMP_MASTER. Violation of PRIMARY KEY constraint 'PKORION_MGR_ASSAY_IMP_MASTER'. Cannot insert duplicate key in object 'dbo.ORION_MGR_ASSAY_IMP_MASTER'. The duplicate key value is (..., ...,...). The statement has been terminated.
This is casued by duplicate PIMS tags in the assay sheet. Once the duplicate rows are commented out , the error will go away. With this error, no record would be written to table ORION_MGR_ASSAY_IMP_MASTER. The message The duplicate key value is (...,...,...) would point the user to the duplicate entries.
Keywords: None
References: None |
Problem Statement: What is the maximum amount of Properties that we can enter for a Product Receipt in APS? | Solution: There’s no limit as to how many properties you can add in the event. You can select as many defined properties in the dialog box:
Keywords: None
References: None |
Problem Statement: Does MBO support adding Product Purchase price through EIU? If not, what prices does it use for the product receipt? | Solution: MBO supports purchase price only for components and not for products. MBO internally will use the Product purchase price from Product definition dialog.
Keywords: None
References: None |
Problem Statement: What is the impact of the Relax Quality bound setting on the Optimum | Solution: ?
Solution
The Relax Quality Bounds setting allow the bounds on quality variables (except SPG) to be relaxed from their upper and lower bounds during optimization. The user must be careful when turning this setting On for the model, and must check that there's no severe quality bound violations before turning on the setting.
Doing so will make sure that the Objective function is stable and accurately calculated. Below is an example of messages to look out for:
*** Quality variable Qabcxyz solved at -10.1 below its original lower bound of 0
*** Quality variable QPR1str solved at -10.1 below its original lower bound of 0
*** Quality variable QPR1st2 solved at -10.1 below its original lower bound of 0
*** Quality variable QSULabc solved at -10.1 below its original lower bound of 0
*** Quality variable QSULSt3 solved at 0.0383547 above its original upper bound of 0.0101
If there's such messages and the setting is turned on, it is allowing the Quality variables to go below/above their bounds as listed in the execution log messages which allows it to solve to a higher objective function. So it’s not a goodSolution even though it’s higher since it’s violating the Quality bounds.
Keywords: None
References: None |
Problem Statement: When the properties are added to the Assay Manager Property library, why aren't they automatically included in the Property Map section? | Solution: When user adds Properties to the Assay Manager Property library, the Property Map should allow the user to select a custom defined property if they select the 'User Defined' Group. As of now, addition to the Property Map table isn't automatic.
Keywords: None
References: None |
Problem Statement: Why does the Publish-> Export Blends option not publish Blend Rundown events in APS? | Solution: When you use the APS Simulator | Publish --> Export Blends option in APS, it only exports Blend events (type 17) in the model. In MBO, the Events | Publish --> Export Blends will publish both Blend and Blend Rundown events for the current event screen. In APS, user can export individual Blend Rundown events from the Optimize Blend dialog of Event Editor.
This functionality is being improved in the V14 release of APS, which will allow to export both Blends and Blend Rundown events from APS as well, similar to MBO.
Keywords: None
References: None |
Problem Statement: How to use the DeltaMinSpec and DeltaMaxSpec columns in the BpcSpecs table in BCI? | Solution: Let's take the example of a blend that has a min and max on a property. We only need the blend to meet the minimum requirement but for the purpose of optimization, we've added a max spec as well in MBO.
In the blend that is exported to BCI, if the property is off-spec, for example above the max, it doesn't matter to us. One way is to manually change the max limit in the BCI blend details.
You can also use the DeltaMaxSpec column in the BpcSpecs table, but when using this, it should be noted that when the property has a Max value defined, and the spec value+ the delta value exceeds the Max value in MBO, BCI will use MBO's Max value. One way to work around this is to modify database AB_BLN_QUALITIES.MAX_SPEC to change the property Max limit to blank.
Keywords: None
References: None |
Problem Statement: What can cause duplicate entries in the PrPurchase table in PIMS? | Solution: In a Global PIMS model, when you run a case, there might be instances where you see multiple entries for the sameSolutionID, CaseID, PeriodID, NodeID, and StreamID, with different descriptions, activity, etc.
These entries are caused by the use of LOCTAGS. In the local model, there are two purchases in BUY: ucc and ucm. In the global model, local tag uccD is mapped to global tag usc and local tag ucmD is mapped to global tag ucc.
Here are the relevant equations on the PURC variables:
VBALuccD: 1.000000 * SCV1uccD +1.000000 * SCV2uccD +1.000000 * SCV3uccD +1.000000 * SCV4uccD -1.000000 * PURCuscD = 0.000000
EPURCusc: 1.000000 * PURCusc -1.000000 * PURCuscD = 0.000000
VBALucmD: 1.000000 * SCV1ucmD +1.000000 * SCV2ucmD +1.000000 * SCV3ucmD +1.000000 * SCV4ucmD -1.000000 * PURCuccD = 0.000000
EPURCucc: 1.000000 * PURCucc -1.000000 * PURCuccL -1.000000 * PURCuccD -1.000000 * PURCuccR = 0.000000
Now the stream in the local model with tag ucc, has two meanings - the purchase of global tag usc and the purchase of global tag ucc, each with the relevant description from the global SUPPLY table. The second one for global tag ucc has the reportgroup=9999. The global tag usc, local tag ucc has reportgroup=1 (from the entry in the local BUY table column GROUP).
This happens because the tag ucc is at two levels for two different purchases. The workaround is to have some naming changes to help minimize the conflicting names.
Keywords: None
References: None |
Problem Statement: What would happen if the license server is restarted when users still have PIMS-AO open? | Solution: When users are working on PIMS and the license server is restarted, if the PIMS AO license becomes unavailable, PIMS will automatically revert to running with DR. This is by design. If the license becomes available again later, the user will need to switch the model back to AO.
Keywords: None
References: None |
Problem Statement: Can the Sub-model calculator files include Non-linear Equations setup in AO? With PIMS-AO, users are able to incorporate non-linear equations to blend qualities, is it possible to create a submodel calculator (SMC) to export those submodels to APS? | Solution: The SMC files that include the non-linear equations cannot be created in this scenario, as the SMCs are strictly linear structures and with the current structure, there is no way to include nonlinear equations.
Keywords: None
References: None |
Problem Statement: Can the Automatically Add Infeasible | Solution: Penalties setting in PIMS-AO be used for Bounds?
Solution
The Automatically Add InfeasibleSolution Penalties setting is used to automatically add infeasibility breakers using built-in penalty structures to solve infeasibility problems.
This setting applies penalties to Capacities, Proclims, Purchases, Sales, and Blend Specs. At present, this setting is not applied to the Variable bounds.
Keywords: None
References: None |
Problem Statement: Is it possible to consolidate APS/MBO databases into one location, when different sites would be on different application versions? | Solution: It is possible to have all your databases in one central database server. For the steps involved, you would have to backup the current database and then restore it in the new server location- you'll need to have Admin access to the server for this step. You can have multiple versions on the server as well, since it’s just a change in shcema and some column orders, that is read by the application.
One thing you’d have to change is the server name that the dsn is pointing to, so that the application can link with the database – this is just a matter of editing the dsn in Notepad and changing the server name.
Keywords: None
References: None |
Problem Statement: How are property calculations handled when tank inventory becomes negative in APS? | Solution: When the tank inventory becomes negative, the simulator will not be updating the property values for those tanks. As such, the property values may not be accurate, as this doesn't reflect the real scenario. When the inventory becomes positive, then the simulator takes up the calculation for the properties again.
Keywords: None
References: None |
Problem Statement: What are the different ways in which PIMS-AO applies the penalties when using the Automatically add Infeasible | Solution: Penalties setting?
Solution
There are two options for selecting how PIMS applies the infeasibleSolution penalties:
1. Apply Penalties to Case Changes Only: Select this option to only apply penalties to all the relevant structures (e.g., limits, blend specs, purchases and sales), that are modified in the current case. Only applies the penalties to the changes in the cases selected for execution, not across the entire model
If not selected, PIMS applies the selected infeasibility penalties, across the entire model to help resolve infeasibilities.
2. Apply Penalties using Marginal Values: If selected, PIMS will automatically apply the Penalty scale factors to specific variables that are at their limit and that show a marginal value that exceeds the internal feasibility objective factor value. Using this option provides another level of infeasibility diagnostics.
Keywords: None
References: None |
Problem Statement: MBO adds additional trend limit with zeroes for Material Pool Trends. The user has a Material Pool trend added to one of the screens, and the Calculate trend limits option is checked.
Now the user navigates to another screen and opens up an Event dialog box, saves and closes the model, and then re-opens it. When looking at the trend, you'll observe that MBO has changed the Trend & if you look at the Trend limits, MBO has added an additional limit with zero's. | Solution: This is a known issue and will be fixed in upcoming patches. The current workaround is to remove trend limits c by deleting it from the TREND_LIMITS table in the db.
Keywords: None
References: None |
Problem Statement: What are some guidelines on Improving model performance in APS & MBO? | Solution: The attached document covers model performance issues, and the settings, keywords, and maintenance tips for improving the model performance.
Keywords: None
References: None |
Problem Statement: What are the model structures to which the Infeasibility breakers are applied using the Automatic Infeasibility breakers setting? | Solution: Using Automatic Infeasibility breakers setting, PIMS-AO automatically adds infeasibility breakers using built-in penalty structures to solve infeasibility problems. It's applied to the following structures:
1. Limits : Applies the indicated factor to capacities and process limits. Specifies the cost of 'buying' additional quantities of the variable or 'selling off' some of the required quantity.
2. Purchases : Applies the indicated factor to purchases. Represents a distressed price penalty. This penalty is applied in situations where it is more profitable to sell a material at a loss than to process it to meet a minimum constraint; when the absolute value of the marginal on the PURCxxx variable or the VBALxxx equation exceeds the feasibility objective function.
3. Sales: Applies the indicated factor to sales. Represents a distressed cost penalty. This penalty is applied when the cost to produce a material is above the associated sales price. Enter a value to use to buy the required material at a loss to meet the production requirements.
4. Blending specifications: Applies the indicated factor to blend specifications. The value must be greater than 0. It is applied when the absolute value of the marginal on the Nxxxyyy or Xxxxyyy row exceeds the feasibility objective factor. Penalties will then be added for all spec equations on property xxx. Penalty can be an up or down penalty.
Keywords: None
References: None |
Problem Statement: How can I import crude assay with crude description using EIU? | Solution: The APS_DESC column in the PIMS_Crude_XREF sheet can be used for importing the crude description using EIU. Once you click Audit Data, make sure you select Yes on “Do you want to load mapping data into database?” message box.After reopening the APS model, we can see the new description on the select crude dialog.
Keywords: None
References: None |
Problem Statement: What are the different possible values for the DBGINFOLEVEL field in the CONFIG table? | Solution: Below are the different values the DBGINFOLEVEL field can have, and the resulting data that is written to the OrionDbg.txt file:
DBGINFOLEVEL
value Debug Information Comments
0 No information is provided If TIMR is set to Y, performance profiling for units will be generated and saved to (WorkingFolder)\(Model ID)\Orion.csv
> 0 During simulation, will Log exceptions in these areas:
Process simulator
ExcelAutomation
On Load Simulator will log:
Name Definitions in Excel workbook
Macro functions exported
Data sheets created
User unit sheets loaded
Elapsed time for recent simulation
OXE or Excel Automation
>=99 On Load Simulator will log:
Unit Array information
Crude Tank Array information
Tank Array Information
Property Array information
Stream Assay information
List of CONSTANT, INPUT and OUTPUT cells in worksheets
Cross-sheet references in worksheets
Index, ID, Tanks, # feeds, and # products
Index and ID
Index and ID
Index and ID
Index and ID
>= 999 OXE verbose mode. Log every cell equation and result at each period simulated. Use with caution; simulate for a day or two at most. The output file can become very large and simulation performance will be impacted.
1001 Will log daily stream values Use with caution.
Keywords: None
References: None |
Problem Statement: Is there a way to read events from an inactive case while the current case is not where the event is defined? | Solution: APS only loads the current case data for the given horizon in the memory. Users cannot directly get case data from another case from automation. The only way would be to publish the event data from the other case so that it's loaded in database tables and query the results directly.
Keywords: None
References: None |
Problem Statement: On the aspenONE Process Explorer, how to display the tag sparkline on the timeline bar? | Solution: Here is the procedure:
1. On a basic trend plot, click the Chart Setting on the top right corner.
2. Uncheck the Optimize Performance, and click OK.
3. The tag sparkline will be displayed on the timeline bar.
Keywords: sparkline
timeline bar
A1PE
References: None |
Problem Statement: How to display the symbol preview on the Aspen Graphic Studio? | Solution: Here is the procedure:
1. Open an existing project.
2. Right-click the symbol library on the and then click Open Palette
3. You will be able to see the preview of all symbols under that symbol library.
Keywords: Graphic Studio
Symbol Preview
References: None |
Problem Statement: When opening the scheduling table, an error message “B21BSC-50002: Relational Database Error -2147217900” appeared. How to troubleshoot? | Solution: The issue is caused by the transaction log for database full, we can free up the log space by shrinking the database log.
Here are the steps:
Launch the SQL server management studio
Right-click the database, select Tasks, select Shrink, select Files.
Select the log you want to shrink, click “OK”.
The transaction log will be shrink, and the error message will be eliminated on the BCU administrator.
Keywords: B21BSC-50002
BCU Administrator
References: None |
Problem Statement: How do I calculate the dew point at different pressures? | Solution: You can use the property Table to calculate the dew point at multiple pressure points. This can be implemented using the Property Table available under Steam Analysis. You can add the Properties Table directly in the stream or via the Navigation Panel. Follow the steps given below:
1. Open the stream where you are interested to know the dew points.
2. Select Analysis under the Attachments tab and click Create
3. Create the Property Table via the Attachments tab
4. For Variable 1, select Vapour fraction mode as state and specify value 1
5. For variable 2, select Pressure and mode incremental
6. Provide the Lower and Upper bounds for pressure and number of increments
7. In the Dep. Prop page, add Temperature as dependent property
8. Click Calculate
9. The results can be viewed in the form of Table or Plots
Key words
Dew Point, Steam Analysis
Keywords: None
References: None |
Problem Statement: Why does the warning “A temperature in stream X is not found at the requested conditions” appear? | Solution: When specifying a stream on Aspen HYSYS using Flow (with its corresponding composition), Vapor Fraction and Pressure, the Warning “A temperature in stream X is not found at the requested conditions” can show up.
When a Vapor Fraction (VF) and the Pressure (P) have been specified, HYSYS will attempt to solve the flash calculations to obtain the Temperature that would satisfy these conditions. When VF is specified as 1, HYSYS will attempt to calculate the Dew Point Temperature of the stream, or when VF is set to 0, HYSYS will attempt to solve for the Bubble point Temperature.
If the value of P is higher than the Critical Pressure (Pc) of the stream and VF is specified, then HYSYS will not be able to find aSolution, since on these conditions, VLE does not apply anymore.
HYSYS V8.8 and above use the following convention when working on supercritical conditions:
When the Pressure (P) is higher than the Critical Pressure (Pc) and the Temperature is lower than the Critical Temperature (Tc), the Vapor Fraction will be specified as 0.
When the Temperature is higher than the Critical Temperature, at any Pressure, the Vapor Fraction will be specified as 1.
When working with Pressures above Pc, the program will not be able to find an Isotherm for a Vapor-Liquid equilibrium or VLE (since you are well above the PH or PT envelope).
If however you specify both Temperature and Pressure, even when working in Supercritical conditions, HYSYS will solve accurately for the Vapor Fraction, based on the convention stated above.
Keywords: Vapor Fraction, Critical, Pressure, Stream not found, Temperature, 0, 1
References: None |
Problem Statement: Why do I have an effect on the sulphur content in distillates when adjusting the overall HDN activity? | Solution: The HDN reaction in the hydrocracker model is exothermic. The reactions will release more heat if you make the overall HDN activity more active. This will raise the temperature in the reactor bed and make HDS reactions also go faster.
Keywords: Hydrocracker, HDN Reaction, HDS Reaction
References: None |
Problem Statement: Aspen Safety Analysis Tool - The Orifice Area on the summary sheet “Calculated Orifice” & the Edit flash table does not match. For example the summary shows value: 4.392 & in flash table its 4.348. | Solution: 1. There is a slight difference in the area calculated in the flash table and the area calculated as the required area in the scenario, because different equations are applied. In both cases, calculated area by calculating the mass flux through the relief valve, then calculating the area required to pass the flow.
2. The mass flux calculation is a direct integration of the nozzle equation assuming a homogeneous fluid. There are at least two ways this can be done. [A] The first is to do a numerical integration (approximate this as a summation) from the relieving pressure until either a maximum is observed in the mass flux or to reach the discharge pressure. [B] The second is to do a thermodynamic transformation of the nozzle equation from an integral over density to a delta enthalpy; then the flow through the valve can be calculated by looking for the maximum change in enthalpy. Although these two approaches are mathematically equivalent, in practice, the density and enthalpy that come from the property packages are fitted independently and so there are small differences in the results of the two methods.
3. We prefer the numerical integration for the required area calculation because we find that in HYSYS and Aspen Plus, it tends to be a little more conservative.
4. We prefer the enthalpy method for the supercritical fire calculation because it requires fewer flashes, and performance is an issue for a large table. Even though the absolute results is a little less conservative, we would expect the trend (thus the selected maximum relief) to exactly follow what we would get if we did a numerical integration instead.
5. This is inherently a dynamic calculation which we approximate as a series of steady-state steps. The results will vary due to discretization.
After all the user will have to use their engineering judgement to determine the appropriate number of steps (and step size) for the table.
Keywords: Orifice Area, Calculated orifice, Edit flash table
References: None |
Problem Statement: How to solve “WARNING: Metadata discrepancy: Field names defined but not as Excel range names.”? | Solution: Cause: This issue occurs if a field name presenting the issue described in WARNING: Field name is not liked to a cell/range in the document. article is deleted from the Name Manager directly, without fixing the link to a cell and then deleting it.
Description: The Field Name does not exist in Name Manager but Excel still knows this name and cannot reference it to a cell/range in the datasheet.
How to Fix:
If the Field Name is not associated to an ABE field, then the Field Name can be redefined, linked to an empty cell and deleted using the ABE’s Delete button.
Select and empty cell (where no ABE field or range name is defined) For example: A1.
Go to Formulas menu and click on “Define name” button.
In the New Name dialog, enter the field name in Name filed: For example: Field2444. Click OK button:
Save the file changes.
Validate the datasheet:
Confirm in the Validation output that the warning message is not reported any more:
Keywords: Field, Warning, Template, Datasheet Definer
References: None |
Problem Statement: How Live Link and Datasheets buttons work in Safety Analysis V12? | Solution: In V12, the ribbon Safety Datasheets was introduced to contain all the commands for the generation of the PSV Datasheets where Live link and Datasheets are two new capabilities in V12.
The Live Link option is a new feature since V12. When activated, the data will be transferred automatically for the mapped objects. This way the objects need to be mapped once and any changes in the simulation will be automatically updated and applied to the Datasheets. If it is disconnected, the data must be transferred from the mapper manually.
Once the Live Link is enabled, the PSV Datasheet can be opened or created without entering into the Explorer. Just move to the PRD Data tab of the specific PSV and click on the button.
Keywords: PSV, Datasheet, Safety Analysis
References: None |
Problem Statement: In the error.log file for a history repository, getting the error:
Save_cache() write data failure 28
What does it mean? | Solution: The above error message means that there is no space left on the hard drive containing archive filesets. The hard drive has filled up to a point where no significant amount of data could be written to the current archive fileset.
First thing to do is to free up some disk space. However, after space on the archive disk has been cleared up, the repositories may not start. At this point the active archive will have to be rebuilt. This is done with the following command.
h21arcck [-r'repositoryname'] (-a'filesetnumber') [-d] [-o]
Example:
h21arcck -rTSK_DHIS -a3 -d -o
This command is documented in the InfoPlus.21 Administrators Manual in the History Utility Programs section. Note that this command is run from a DOS window and it is run from the ..\aspentech\infoplus.21\c21\h21\bin directory.
Once the active archive has been rebuilt, the repository can be started from the InfoPlus.21 Administrator.
Keywords: Save Cache
Write
28
Failure
History
Repository
References: None |
Problem Statement: How to add private timelines to trend plots within Aspen Process Explorer. | Solution: When using Aspen Process Explorer to review multiple trend plots it can be very helpful to give each trend plot a private timeline so that you may review the data within these plots at different time periods for comparative analysis. The example in this knowledge base article will show two trend plots open with the same tags but they will be given private timelines so that the data for these tags can be reviewed for different days. To add private timelines to trends you will first want to open Aspen Process Explorer and add two or more trend plots. Next for comparative analysis it is often best to go to the View button and tile the trends so that you can review them side by side with each filling an equivalent space in the Process Explorer window. The steps to complete this are shown in the image below.
Then to add the private timelines to the trend plots you will simply want to click on and highlight one of the trends at a time and uncheck the 'Global Timeline' and check 'Private Timeline' from within the View button as shown in the following image. Now you will notice that instead of having the timeline bar across the entirety of the Aspen Process Explorer window you will have two timeline bars within the space below each of the trend plots. From there you are able to select individual timespans to compare the data for these tags during different time periods.
After completing these steps it is helpful to save the trends within a workspace so that when you would like to review the trend plots again with their private timelines you can just open the saved workspace and all of the settings configured will be maintained.
Keywords: Private
Timeline
Trend
Process Explorer
References: None |
Problem Statement: When using the Test API utility, GET successful is returned without any data:
Please select device data type for tag 'tagname'
Press RETURN for default:
GET successful
Please press RETURN to continue... | Solution: Perform the cimio_t_api test using Access type Synchronous (1) and list id of -1
Keywords: Test API
CIMIO
Get
Successful
References: None |
Problem Statement: Some sites choose to install the Aspen Cim-IO for OPC interface (acting as an OPC client) on a machine remote from the OPC Server. When using this setup, there are considerations for the DCOM configuration used. | Solution: To get an OPC client talking to an OPC server clients must be able to 'look up' an OPC server:
1. Each OPC server is identified by a GUID - a large hex string stored in the registry.
2. Some OPC clients just scan the local registry and assume that all computers have the same OPC servers installed on them. In this case, you need to install all of the servers you wish to use locally, and then you can remove the OPC server executables if you wish, to save disk space. The installation will modify the registry, which will remain intact even when the executables are removed.
3. Some OPC clients scan remote registries. They need access to the DCOM server 'OPCEnum'.
Treat it just like an OPC server and set it up using the information below:
DCOM communications between client and server must be enabled. DCOM creates 2 one-way barriers between the client and server:
incoming requests to the server can be blocked
incoming replies to the client can be blocked.
You need to make sure that each is allowed to talk to the other.
Both the client and server run under UserIDs. This may be a local user, a domain user, or the system account. If it is a local user, you MUST have the SAME id with the SAME password on the other machine to be able to permit it access to the server or client. If it is a domain user, just give the domain user permissions (thus, domains are MUCH easier for OPC communication.)
To enable the client to talk to the server, run DCOMCNFG on the Server node and select the OPC server's DCOM properties. You can either edit the default properties, or you can set up custom properties for this particular OPC server. In either case, the client's UserID will need LAUNCH and ACCESS permissions.
To enable the server to talk to the client, run DCOMCNFG on the Client node and select the DEFAULT SECURITY settings. The server's UserID must have ACCESS rights in the default settings.
Note: SYSTEM is an individual account on each computer. If you have an OPC server running as a service, you may or may not be able to get the client to talk to the server. You should allow the following system accounts default ACCESS rights on your OPC client's system:
system
network
Network will give access to all users who are on 'trusted' computers (the local Microsoft network).
If you wish to limit access to only the person on that particular computer at that particular time (for example, you have an HMI on the same box as an OPC server, and you want only the HMI, running as the current user, to have access to the OPC server), you should use the INTERACTIVE system id. INTERACTIVE gives access to whoever is currently logged into that particular system.
Keywords: DCOM
CIMIO
OPC
Remote
References: None |
Problem Statement: How do I load a Recload file (.RLD) into an Aspen InfoPlus.21 database? | Solution: A Recload (.RLD) file is a file of records that is loaded into the database. RLD files are loaded into the database to populate the database with records.
The following steps detail how to load a .RLD file into an Aspen infoPlus.21database.
1. Open the Aspen InfoPlus.21 Administrator .
2. Expand the InfoPlus.21 list to view the database names.
3. Right mouse click on the database name that will be modified.
3. From the context menu select Load Record to display the Load Records dialog box.
4. Use the browse button to locate and select the desired .RLD file.
5. Click OK to load the records.
6. A Results List dialog box will appear indicating the the records have been loaded successfully.
Keywords: rld, recload, load, Aspen InfoPlus.21 administrator
References: None |
Problem Statement: Why does my file use a RefSYS license when there is no petroleum refining feature used? | Solution: First, confirm that the file is not using any Petroleum refining features (Petroleum Assays, RefSYS unit ops, etc.). Once this is confirmed, then clear all property slates for petroleum assays. This can be done by pressing Ctrl+M. The window below will pop up:
Select the PV Balance tab, highlight Petroleum Assay Balance, and click Clear All Property Slates.
Keywords: RefSYS
License
Petroleum Assay
References: None |
Problem Statement: Which unit operations use the REFSYS license? | Solution: The REFSYS license is used when HYSYS Petroleum Refining unit operations are present in the simulation environment. Below is a list of these unit operations.
Assay Manipulator
Catalytic Reformer
FCC Reactor
Hydrocracker
Petroleum Distillation Column
Petroleum Feeder
Petroleum Shift Reactor
Isomerization
Hydroprocessor Bed Reactor
Molecule-Based Reactor
Product Blender
Delayed Coker
Visbreaker
Hydrotreater
Alkylation Unit
Catalytic Reformer
Refining Short-Cut Column
HYPlan Model
Some unit operations are not available in all versions of HYSYS. For example, the Refining Short-Cut column was introduced in V10.0. For more information on HYSYS Petroleum Refining unit operations refer to the Aspen HYSYS Petroleum Refining Unit Operations & Reactor Models V12
Keywords: REFSYS
license
xml
References: Guide. |
Problem Statement: How are the various volume flow properties in Aspen HYSYS calculated? | Solution: Density and volumetric flow calculations can be classified in the following three ways: (1) Actual - at flowing conditions - rigorous calculation reflecting non-ideal mixing effects, (2) Standard - at standard reference conditions - rigorous calculation reflecting non-ideal mixing effects, and (3) Ideal - at standard reference conditions - non rigorous calculation not reflecting any mixing effects
Std Ideal Liq Vol Flow
Each component has an ideal liquid density at standard conditions, these are weighted and summed by component fraction to create an ideal liquid density for the stream, and hence a flow rate. For all hypothetical components, the Standard Liquid density (Liquid Mass Density @ Std Conditions) is used in the Ideal Liquid density (Std Ideal Liq Mass Density) calculation. If a density is not supplied, the HYSYS estimated liquid mass density (at standard conditions) is used.
Compositions specified or reported on a liquid volume basis correspond to this Std Ideal Liq Vol Flow. This calculation does not include any mixing effects.
Liq Vol Flow @ Std Cond
This flow is calculated based on a rigorous standard liquid density. This density for every phase, including the overall phase, is obtained by calculating a liquid density using the internal methods of the chosen property package for each phase at standard conditions. Therefore, this includes mixing effects. The standard condition used here depends on the temperature units in use by Aspen HYSYS. If C or K is used, the standard condition is 15C and 1 atm. If F or R is used, the standard condition is 60 F and 1 atm. The reference temperature for standard liquid volume cannot be changed.
The density and flow are reported as <empty> if the pseudo critical temperature of the stream is below 15C (/60F). The pseudo critical temperature is the sum of the component critical temperatures weighted by the component mole fraction and is reported in the Critical Properties utility.
Actual Volume Flow
This is calculated based on a rigorous density at the stream conditions. The method used for the density calculation depends on the property package being used.
Std Gas Flow
This is calculated based on the molar volume of an ideal gas at standard conditions. Again, the standard condition used here depends on the temperature units in use by Aspen HYSYS. If C or K is used, the standard condition is 15C and 1 atm. If F or R is used, the standard condition is 60 F and 1 atm. If you want to change your reference temperature use VVSTDMX or VVSTD in your prop-set, and specify your reference temperature and/or pressure on the Qualifier tab. This is only applicable for standard vapor volume.
Actual Gas Flow
This is calculated based on a rigorous density at the stream conditions for vapor only streams and vapor phases.
Keywords: Volume Flow, Standard, Ideal, Actual, Gas,
References: Temperature |
Problem Statement: What is the phase of a supercritical mixture? Sometimes the phase is listed as Vapor and sometimes the phase is listed as Liquid.
Are liquid density, liquid enthalpy, and liquid heat capacity routes being used to calculate these properties instead of the vapor routes? | Solution: The phase is of a supercritical mixture is not vapor or liquid, it is supercritical. Aspen Plus does not have a designation of supercritical; therefore, the phase can be assigned as either liquid or vapor.
The rough convention for phase designation is:
If the Temperature is greater than the critical temperature (Tc), the phase should be Vapor.
If the Temperature is less than the critical temperature (Tc), but the Pressure is greater than the critical pressure (Pc), the phase should be Liquid.
Tc and Pc of the mixture are not calculated a priori; therefore, the designation is only approximate.
Creating a PT Envelope for a stream using Stream/Analysis is probably the easiest way to tell if a mixture is supercritical. Please seeSolution 000082618 for more information about calculating the true critical point of a mixture (the property sets TCMX and PCMX only give the pseudocritical point which is a mole fraction average of the TC or PC of the individual components).
Since an equation of state (EOS) should be used to calculate both liquid and vapor properties, it does not matter what phase the stream has assigned to it. Activity coefficient (phi/gamma) models should not be used for supercritical mixtures since the vapor and liquid calculations are inconsistent in the critical range. Not all of the EOS property methods use the EOS to calculate every property. For example, a number of EOS Property Methods such as PENG-ROB and RK-SOAVE use Rackett to calculate liquid molar volume. PR-BM and PSRK use the EOS. Check the Properties / Property Methods / Models sheet to see what is being used.
Keywords: critical temperature, critical pressure, PT-envelope, PT envelope, TC, PC, phase
References: None |
Problem Statement: You may have instances where the Aspen Cim-IO server (and OPC for that matter) are located at remote sites with no accessible connection to the corporate network, hence no access to the license server. Will CIMIO server still work after upgrading to the V8 release? | Solution: Cim-IO server does not require a license beginning V11. Prior to that, you may install CIMIO server without a license, but then it will produce the following errors on first attempt to start Cimio Manager service:
Further inspection in Event Viewer will show this:
A new license enforcement scheme was introduced in V8 (for Cim-IO, licensing requirement was ended with introduction of V11). Some products implement it differently, for example, CIM-IO runs its license enforcement only ONCE - the first time CIMIO Manager service is started after a new installation.
In other words, you can install a CIM-IO server without a license but the CIM-IO Manager service won't start until you setup a network connection between you CIM-IO server and SLM server so its license can be validated.
After this first license validation, you can setup your CIM-IO server back to its usual network setup. CIM-IO will still try to check for a license everytime the service restarts but if it fails to find the SLM server it won't prevent the service from running, it will just log a message in the event viewer and start normally.
Keywords: CIM-IO License Enforcement
SLM
CIM-IO Manager Service
Error 1067
References: None |
Problem Statement: Example: Carbon Emissions Modeling for Refinery Planning Using Aspen PIMS | Solution: This Aspen PIMS example model captures the carbon emitted in a refinery plantwide optimization model. It covers two main sources of CO2, mainly the Fluidized Catalytic Cracker (FCC) plant and the Fuel Gas system. With ongoing focus of refiners to include sustainability aspects into their planning and scheduling models, this model can be used as a starting point for including CO2 emission modeling in Aspen PIMS refinery planning models.
Please see the attached PDF for steps on how to create the model.
Key Words
Aspen PIMS, Carbon Emissions, Refinery Planning
Keywords: None
References: None |
Problem Statement: Carbon Emissions Modeling for Olefins Planning Using Aspen PIMS | Solution: The Chemical and Petrochemical sector is one of the largest greenhouse gas (GHG) emitting industrial sector among stationary sources such as Power Plants, Petroleum and Natural Gas Systems. The chemical and petrochemical industry accounts for 30% of global industrial energy use and 16% of direct CO2 emissions. This Aspen PIMS Planning example model captures the carbon emitted in a sitewide olefins optimization model. It covers two main sources of CO2, mainly the Furnaces and Boilers. With ongoing focus of global majors to include sustainability aspects into their planning and scheduling models, this model can be used as a starting point for including CO2 emission modeling in Aspen PIMS olefins planning models.
Please see the attached PDF for steps on how to create the model.
Keywords: Aspen PIMS, Carbon Emissions, Modeling
References: None |
Problem Statement: Carbon Emissions Modeling for Refinery Planning Using Aspen Unified PIMS | Solution: This Aspen Unified PIMS Planning example model captures the carbon emitted in a refinery plantwide optimization model. It covers two main sources of CO2, mainly the Fluidized Catalytic Cracker (FCC) plant and the Fuel Gas system. With ongoing focus of refiners to include sustainability aspects into their planning and scheduling models, this model can be used as a starting point for including CO2 emission modeling in Aspen Unified PIMS refinery planning models.
Please see the attached PDF for steps on how to create the model.
Key Words
Aspen Unified PIMS, Carbon Emissions, Refinery Planning
Keywords: None
References: None |
Problem Statement: Can HYSYS envelope analysis plot the hydrate dissociation curve? | Solution: The HYSYS envelope analysis for hydrates will only plot the hydrate formation curve. It will not plot the hydrate dissociation curve. HYSYS hydrate formation analysis utility only calculates hydrate formation, not hydrate dissociation.
Keywords: Hydrate formation, hydrate dissociation, envelope analysis
References: None |
Problem Statement: How to export a list of OPC UA Browse paths or node id’s that can be imported into an OPC UA client application using the Aspen OPC UA Explorer? | Solution: Open the Aspen OPC UA Explorer.
Connect to the OPC UA server.
Select the desired tags so the details are displayed on the “Variable Details” tab.
Select all the lines containing the tags.
R-Click and Copy
Paste to a notepad and save as a *.CSV file. the file will contain all the variable details.
If needed the file may be edited to remove unnecessary columns using Excel or an editor.
For Example; the CSV file can be edited so it contains only the Display Name and OPC Browse Path or Node Id.
Keywords:
References: None |
Problem Statement: Do we have any typical mechanical arrangement for deresonating baffles!! | Solution: Application of Deresonating Baffles
An acoustic type of vibrations may observed in the heat exchangers. In such cases to avoid acoustic resonance issues, deresonating/ detuning baffle could be the best choice.
There are several means available to correct resonating vibration issues. The other modifications may have some effect on the exchanger performance, or in some cases may need to modify geometry as well & could have some effect on exchanger performance.
The simplest method would be to install deresonating baffle in the exchanger to break the wave’s at or near the antinode. The advantage of using deresonating baffle is “without significantly affecting the shell side flow pattern” vibration issues would be resolved.
Articles on Deresonating Baffles
Below are some of the important articles available on deresonating baffles:
If deresonating baffles are used in designing a heat exchanger, how is an external user informed of the deresonating baffles?
https://esupport.aspentech.com/S_Article?id=000055072
How do I add tube supports to deresonating baffles?https://esupport.aspentech.com/S_Article?id=000077380
Deresonating baffles
https://esupport.aspentech.com/S_Article?id=000091433
Typical De-resonating Baffles mechanical arrangement is shown in attached pdf file.
Keywords: Deresonating Baffles, Mechanical arrangement of deresonating baffles, Vibrations
References: None |
Problem Statement: How to create a new Project in OptiPlant? | Solution: Procedure to create a new OptiPlant project.
Select a location in the folders and create one with the name of the project.
In OptiPlant go to File | Open.
In the File Name field, enter the file name.
Important Note: The folder and file names must not contain spaces and should not have any special characters like ?, /, \, <, etc. Only hyphen (-) and underbar (_) are allowed.
Go to the new folder and give a name. A new PPL file will be created
In the containing folder the following structure should be created:
Keywords: Create, Project, OptiPlant
References: None |
Problem Statement: Why is there no heat transfer calculated in the Convective/Economizer zones of a Fired Heater? | Solution: Fired Heaters give the user the option for specifying stream connections in three different heat transfer zones: Radiant, Convective and Economizer. On the Design/Connections page, multiple inlet and outlet streams can be defined and it is possible to assign a zone of the exchanger to each of the streams. It is important to notice that if the simulation is run in steady state mode, the heat transfer calculations will only be applied to the Radiant zone. If there is need to make heat transfer calculations in the Convective and Economizer zones, the simulation must be evaluated in Dynamic mode.
Keywords: Furnace, heat transfer, zones, steady state, dynamics
References: None |
Problem Statement: Using Aspen Hydraulics and dynamic simulation to study pigging operation in a pipeline | Solution: Pig can be used to clean and inspect the pipeline. A pig is launched from a certain location along the pipeline and is pushed down the pipe until it reaches the receiving trap. Pigging operation can help to achieve environmental benefit by avoiding the use of cleaning agent, solvent, or water to clean the pipeline. Before each pigging operation, an engineer needs to plan and study the effect of the operation on pipeline and production downstream.
This application example will show how to plan a Pigging Operation using Aspen Hydraulics and HYSYS Dynamics.
Using Aspen Hydraulics model in Dynamics, the user can:
· Simulate the pigging operation across the pipeline
· Evaluate the effect of liquid front at the pipeline outlet by monitoring liquid level in the slug catcher, performance of pressure control valve and flow control valve, and loss through pressure relief valve
You will learn to:
· Leverage rigorous dynamic modeling capabilities of Aspen Hydraulics
· Monitor pigging operation using tools within Aspen Hydraulics
· Use dynamic tools such as strip charts to monitor behaviors at the pipeline outlet
Keywords: Pipeline Hydraulics, HYSYS Dynamics, Pigging
References: None |
Problem Statement: What year DIPPR databooks were used to build Aspen Plus databanks? | Solution: The PURExx databanks are based on the public version of the DIPPR database.
The PURE39 databank in Aspen Plus V12.1 is from 2019
The PURE38 databank in Aspen Plus V12.0 is from 2019
The PURE37 databank in Aspen Plus V11.0 is from 2018
The PURE36 databank in Aspen Plus V10.0 is from 2016
The PURE35 databank in Aspen Plus V9.0 is from 2015
The PURE32 databank in Aspen Plus V8.6 and V8.8 is from May 2013
The PURE28 databank in Aspen Plus V8.2 and V8.4 is from January 2012
The PURE27 databank in Aspen Plus V8.0 is from January 2011
The PURE26 databank in Aspen Plus V7.3.2 is from January 2011
The PURE25 databank in Aspen Plus V7.3 is from January 2010
The PURE24 databank in Aspen Plus V7.2 is from January 2009.
The PURE22 databank in Aspen Plus V7.0 and V7.1 is from January 2007.
The PURE20 databank in Aspen Plus 2006 is from January 2006.
The PURE13 databank in Aspen Plus 2004 and 2004.1 is from January 2003.
The PURE12 databank in Aspen Plus 12.1 is from January 2002.
The PURE11 databank in Aspen Plus 11.1 is from April 2001.
The PURE10 databank in Aspen Plus 10.0-1, 10.1, and 10.2 is from April 1997.
Keywords: reference date
References: None |
Problem Statement: Why am I unable to estimate properties for a certain component? I get the following warning:
* WARNING IN PHYSICAL PROPERTY SYSTEM
FUNCTIONAL GROUP GENERATION FOR THE XXX METHOD CANNOT BE COMPLETED
FOR COMPONENT XXX. THE FOLLOWING ATOMS WERE NOT MATCHED:
SI 2 SI 4 | Solution: The Aspen Physical Property System uses the molecular structure information to build the required functional groups for all estimation methods used in the run. Not every group is available for every method. If the component contains atoms or groups that are not available in a method, it is not possible to use that group contribution method. This is a limitation of the method itself and not of the product.
The available estimation methods have a limited number of groups and cannot predict properties for every molecule. In general, the estimation methods support the following atoms: C, O, N, S, B, Si, F, Cl, Br, I, Al, P, Zn, Ga, Ge, As, Cd, Sn, Sb, Hg, Pb, and Bi; however, every estimation method does not include all of these atoms or combinations of atoms. See the Help under Aspen Plus
Keywords: Estimation, troubleshooting
Ambrose
Benson
Bondi
Joback
UNIFAC
References: -> Physical Property Data Reference Manual -> Group Contribution Method Functional Groups -> Overview -> PCES Functional Groups for the lists of groups that each method includes. The group definitions for most methods are obtained from literature. The references for the different methods are in the help. |
Problem Statement: The bubble point calculated using PT-Envelope in Analysis is completely different from that estimated using a bubble point property calculation (Tbub) using Generic Analysis. The overall valid phases has been set to use Vapor-Liquid-Liquid (VLL); however, the PT-Envelope only ever shows one liquid phase. | Solution: PT-Envelope Analysis was originally only designed to work with vapor-liquid systems and was not designed to detect two liquid phases. Starting in V11, a new method, the density marching method (Venkatarathnam, 2014) is available for use in computing P-T Envelope analysis. The new method also supports vapor-liquid-liquid systems. In earlier versions, for two-liquid systems, another analysis type such as Properties | Analysis | Generic needs to be used.
The original standard phase envelope starts calculations from a low pressure and moves up to the critical point marching along a constant vapor fraction branch (dew, bubble, or intermediate vapor fraction). This method supports only vapor-liquid calculations and may fail to close the phase envelope when approaching the critical point, in particular with systems which exhibit multiple stationary points.
The density marching method makes use of the density of one phase as the independent variable along which it computes the saturation point, and thus the temperature and pressure. This method can march from low density (vapor) through the critical point to high density (liquid), covering the whole PT space without the computational difficulties around the critical point which the standard method may encounter. However, this method may require more points than the standard method to draw the entire curves,
Keywords: PT-envelope
CQ00348268
References: G. Venkatarathnam, “Density Marching Method for Calculating Phase Envelopes”, Ind. Eng. Chem. Res. 2014, 53, 3723−3730. |
Problem Statement: The 64-bit compilation of zetoolkit.dll provided with Aspen Plus/Properties V11 works fine in VBA macros with 64-bit Excel; however, there can be problems with 32-bit Excel. Is it possible to get the inclusion 32-bit version of zetoolkit (e.g. zetoolkit32.dll)? | Solution: Zetoolkit.dll is the summary file toolkit dynamic-link library. This file is stored in the Engine\xeq subfolder of the APrSystem installation, typically C:\Program Files\APrSystem <version>\Engine\xeq\zetoolkit.dll
It is used as a standalone tool and has no dependency on other Aspen Plus dlls; therefore the 32-bit verison from V10 can be used in applications.
Attached is the last version of zetoolkit.dll compiled in 32-bit from V10. This file can be placed in a new directory and the path can be referenced in VBA script.
Keywords: None
References: : VSTS 539408 |
Problem Statement: I am using an oil assay library and components are listed as PC66F etc. How can I interpret these PC components and relate it with carbon hydrocarbon (CxHx) components. | Solution: ATOMNO and NOATOM, which combine to form the chemical formula, are estimated from the molecular weight and carbon-to-hydrogen (C/H) ratio. The C/H ratio is estimated using the procedure in Technical Data Book - Petroleum Refining, vol. 2, fig. 2B6.1, American Petroleum Institute, 1983. These components are assumed to contain no atoms but carbon and hydrogen, and the carbon and hydrogen numbers are adjusted to meet the molecular weight and C/H ratio. As a result, H and C may be fractional.
If you click Retrieve Parameters in the Tools section of the Home ribbon, the properties for all of the components will be retrieved.
On the Methods | Parameters | Results | T-dependent sheet the ATOMNO (atomic number - e.g. 6 for carbon and 1 for hydrogen) NOATOM (the number of that atom) will define the molecule.
So PC120F has 5.69313 Carbons and 12.7151 Hydrogens.
An example file that can be opened in V9 and higher is attached.
Keywords: None
References: None |
Problem Statement: How should the retention vector (RETN and IRETN) be defined in a call the physical property flash in a user model? | Solution: The retention vector can be used to initialize the flash. RETN is the Real retention vector and IRETN is the Integer retention vector. The retention vector needs to be set properly and be large enough or other variables in memory can be overwritten in an unpredictable manner. This is true even if it is not used to initialize the flash.
JRES is the integer restart flag that specified how the retention vector is used.
JRES Simulation restart flag
0=Do not use retention. Initialize with default values
1=Do not use retained values but retain values for subsequent runs
2=Use retained values and retain results for subsequent runs
3=Use guesses from STWORK and STWKWK and save retention
4=Use retained values but do not retain results for subsequent runs.
For more information on JRES see knowledgebase document 85066
For FLSH_FLASH, call FLSH_FRETN to find the size required for the real and integer retention vector (RETN and IRETN). For FLSH_RFLASH, call FLSH_RFRETN to find the size required for retention.
Calling Sequence for FLSH_FRETN
SUBROUTINE FLSH_FRETN(NR,NI)
Calling Sequence for FLSH_RFRETN
SUBROUTINE FLSH_RFRETN(NR,NI)
NR Number of real retention values
NI Number of integer retention values
The safest method to set the retention vector size in a new temporary area using DMS_ALLOCM.
In this example (RETN is set to B(LRTMP) and IRETN is set to IB(LITMP):
C ------GET INTEGER AND REAL SIZES FOR FLASH RETENTION
CALL FLSH_FRETN(NRTN, NITN)
C
C ------ALLOCATE INTEGER VECTOR AND REAL VECTOR FOR RETENTION
CALL DMS_ALLOCM(NITN, NRTN, NBTMP, LITMP, LRTMP, LTMPOFF)
CALL FLSH_FLASH(SOUT,NSUBS,IDXSUB,ITYPE,NBOPST,
+ 2,1,1,USER_IUMISS,USER_RUMISS,
+ 737.15d0,201325.0d0,
+ 0.0d0,4,4,0,1,B(LRTMP),IB(LITMP),FLASHFLAG)
C
C ------DO NOT FORGET TO RELEASE THE ALLOCATED VECTORS
CALL DMS_ATFREE(NBTMP)
It is also possible to use the location of the flash work common area STWKWK array to set the retention size.
The real work area for FLSH_FLASH or FLSH_RFLASH starts at B(STWKWK_LRSTW+1) in COMMON /DMS_PLEX/. This area also contains workspace of the correct size for real retention, pointed to by STWORK_MRETN. Thus, the user model can pass B(STWKWK_LRSTW+STWORK_MRETN) to FLSH_FLASH or FLSH_RFLASH for RETN.
The integer work area for FLSH_FLASH or FLSH_RFLASH starts at IB(STWKWK_LISTW+1) in COMMON /DMS_PLEX/. This area also contains workspace of the correct size for integer retention, pointed to by STWORK_MIRETN. Thus, the user model can pass IB(STWKWK_LISTW+STWORK_MIRETN) to FLSH_FLASH or FLSH_RFLASH for IRETN.
If you do this:
If you set JRES to 0, retention is not used to initialize the flash from retention variables.
Retention values are not saved.
If you are calling the flash utility from a User or User2 block, you can use the real and integer arrays to save the retention values. To do this:
Set the integer and real arrays to large values on the User | Input | Specifications sheet or User2 | Setup | User Arrays sheet.
If you need LR real parameters and LI integer parameters for other purposes, pass REAL(LR+1) and INT(LI+1) to FLSH_FLASH or FLSH_RFLASH as RETN and IRETN.
Call FLSH_FRETN or FLSH_RFRETN once, to get the sizes required for retention.
Set the real and integer array sizes to LR+NR and LI+NI.
See the Aspen Plus User Models
Keywords: None
References: Manual for details.
See knowledgebase document 000055620 for an example of how the physical property flash monitor is called in a user model. |
Problem Statement: How do you find out what streams are tear streams in a flowsheet? | Solution: A tear stream is a stream in a flowsheet with recycle which is torn by the sequential modular convergence routine. The tear removes the recycle by guessing an initial value for this stream where it enters a block, and allows the solver to progress through the flowsheet. Eventually a result is calculated for the stream, and this is compared with the guess. To resolve the tear, a new guess is made, gradually converging on the correct value for the stream.
There are a few ways to find the tear streams in a simulation.
In V9 and higher, in the Results Summary | Streams, you can select Tears as a Stream Group on the Stream Summary Ribbon.
You can go to the Convergence | Tear Stream Summary to see the Tear stream ant their Status, Variable with maximum error, Maximum error / Tolerance, Maximum relative error, Absolute error, and Convergence block.
Tears and their convergence blocks are also listed at the top of the Control Panel. The Sequence follows.
If you export the Run messages (.cpm) file, you can search for Flowsheet Analysis to find this section of the Control Panel messages.
Following is an example of the Flowsheet Analysis for a flowsheet.
In this example, there are three tear stream convergence blocks to converge three sections of the flowsheet.
$OLVER01 converges tear streams BFW3 and STEAM2.
$OLVER02 converges tear streams SCRUBBER and 7.
$OLVER03 converges tear streams Z34 and Z61.
The other convergence blocks ($OLVER04, $OLVER05, etc.) are used to converge the design specifications (DS-1, DS-2, etc.).
Flowsheet Analysis :
Block $OLVER01 (Method: BROYDEN ) has been defined to converge
streams: BFW3 STEAM2
Block $OLVER02 (Method: BROYDEN ) has been defined to converge
streams: SCRUBBER.7
Block $OLVER03 (Method: BROYDEN ) has been defined to converge
streams: 234 261
Block $OLVER04 (Method: SECANT ) has been defined to converge
specs : DS-1
Block $OLVER05 (Method: SECANT ) has been defined to converge
specs : DS-2
Block $OLVER06 (Method: SECANT ) has been defined to converge
specs : DS-3
Block $OLVER07 (Method: SECANT ) has been defined to converge
specs : DS-4
Block $OLVER08 (Method: SECANT ) has been defined to converge
specs : DS-7
COMPUTATION ORDER FOR THE FLOWSHEET:
$OLVER01 HRSG-RAD HRSG-STM HRSG-BFW STMDRUM B4
(RETURN $OLVER01)
$C-2
$OLVER02 SCRUBBER.B1 SCRUBBER.SCRUBBER SCRUBBER.B3
(RETURN $OLVER02)
SCRUBBER.B2 $C-3 $C-4 B11.B1 B11.B2 B11.B3 $C-7 LOCAT $C-8
C-STAGE1.B1 C-STAGE1.B2 C-STAGE1.B3 DMDSPUMP DMDSHX DMDSH2S
$C-5 TRTR-1 TRTR-2 TRTR-3 B10
$OLVER03 PROD-SEP SEPAREX B3 PRG-SPL B9 RG-COMP B5 H2O-RO
| PLETDOWN HVY-DIS ME-ETDIS B6 B7 B8 MEOHPUMP B2 ATREFORM
| $OLVER05 RCYHX1
| (RETURN $OLVER05)
| ATR-KO-1 FEED-MIX $C-1 K-STAGE1.K5
| $OLVER06 K-STAGE1.K5HX
| (RETURN $OLVER06)
| K-STAGE1.K5B $C-12 $C-13 K-STAGE2.K7
| $OLVER07 K-STAGE2.K7HX
| (RETURN $OLVER07)
| K-STAGE2.K7B $C-14 $C-6 K-STAGE4.K9 $C-18 FD-RGMIX
| FDSTMOH TRIM-HX H2S-MIX B1 REACTOR RXT-HX RXEFFHX1
| $OLVER04 RXEFFHX2
| (RETURN $OLVER04)
(RETURN $OLVER03)
ETH-DRY
$OLVER08 ME-COND
(RETURN $OLVER08)
ME-REB1 ETOHREB1 ETOHCOND STMGEN RXT
->Calculations begin ...
Convergence time can be improved by adding estimates for the condition and flow of tear streams.Solution 102354 tells how stream results be copied to input forms to be used as tear estimates.
Keywords: None
References: None |
Problem Statement: How are Gross and Net Heating value (QVALGRS and QVALNET) prop sets calculated in Aspen Plus? | Solution: Gross and Net Heating value should be accessed using the property sets QVALGRS and QVALNET respectively. The property sets HHVxxx and LHVxxx are from the Aspen HYSYS Refining Correlation Manager.
Net Heating Value (QVALNET) - API Low Heating Value (LHV)
In Aspen Plus the Net Heating value is the property set property QVALNET. Net Heating value is calculated as follows:
QVALNET = SUM [-HCOM*RATES(i)]
where HCOM(i) is the molar standard heat of combustion at 25C of the component i
RATES(i) is the component mole fraction
This heat of combustion calculation is the change in enthalpy when the substance reacts with oxygen to produce these combustion products (vapor, except where noted): CO2, H2O, F2, Cl2, Br2, I2, SO2, N2, P4O10 (crystal), SiO2 (crystobalite), and Al2O3(crystal, alpha).
Gross Heating Value (QVALGRS) - API High Heating Value (HHV)
In Aspen Plus, the Gross Heating value is the property set property QVALGRS. You can calculate the Gross Heating value for a component using the following formula:
QVALGRS = SUM [-HCOM*RATES(i)]
+ 0.5 * (Number of H atoms) * Hvap of Water at 25 C
+ (number of Chlorine atoms) * (DHFORM of HCl ideal gas - 0.5 * DHFORM water)
+ (number of Fluorine atoms * (DHFORM of HF ideal gas - 0.5 * DHFORM water)
In this calculation, ΔHvap(water, 25°C) is set to 43998034 J/kmol, a value prescribed by API procedure 14A1.1. This is within 0.01% of the value predicted by STEAM-TA at these conditions.
The last part of the formula is a correction for the latent heat of water where it is assumed that two hydrogen atoms will form one molecule of water except for those that form HCL or HF at combustion.
If water is not formed in the combustion, QVALGRS is not valid.
For pseudocomponents, the QVALNET and QVALGRS property sets are estimated based on the API gravity value for each pseudocomponent using API Data Book procedure 14A1.1 (based on API gravity value) to get the value at 60°F and linear extrapolation is used for other temperatures.
Heating values are reported in Aspen Plus on a mass basis so the above results need to be divided by the average molecular weight of the stream.
The difference between QVALGRS and QVALNET is due to the gross heating value being defined to use combustion products including liquid water rather than water vapor, HCl instead of Cl2, and HF instead of F2. If, for certain components, there are not enough hydrogen atoms to convert the fuel to HCl and HF, then water will appear as a reactant in this calculation. For such components, an information message will be generated indicating that QVALGRS may not be valid. To determine its validity, the hydrogen content of the whole mixture must be considered.
Despite the names, it is possible for the gross heating value to be less than the net heating value, especially for components with many Cl atoms and few or no H atoms, such as C2Cl4.
Keywords: heating values
heat of combustion
properties
LHV
HHV
QVALGRS
QVALNET
VSTS 592961
References: None |
Problem Statement: You cannot connect to the Rockwell FactoryTalk historian. When testing the connection in the Rockwell FactoryTalk adapter, you may get the following error message:
Connection test failed.
[PI SDK] Unable to open a session on a server. [-10734] PINET: Broken Connection.
If you get the following error message, you need to get a license for PIEOLEDB in Rockwell:
PISDK Registry item not found in the collection. | Solution: Prior to setting up the historian connection, the following prerequisites must be completed:
PIOLEDB Enterprise and Provider have to be installed
A connection has to be done in the application
After these steps are completed, you must do the following:
1. Log into PI OLEDB MMC Snap-in.
2. Right click on the server where the historian is located and click Connect.
3. A pop will appear and 2 different methods have to be tested:
Checking the Windows NT Integrated security
Using a user ID and Password (look at file How to Troubleshoot PIOLEDB connection problems it recommends using piadmin user)
You will finally need to configure your sensor data source in Aspen Mtell System Manager:
1. Open Aspen Mtell System Manager.
2. Open the Configuration tab.
3. In the left sidebar, select Sensor Data Sources.
4. In the top ribbon, select Add Data Source.
5. Name the data source whatever you want.
6. Leave the default Source as Plant Historian.
7. For the Historian, use the drop down to select Rockwell FactoryTalk.
8. Leave both User Name and Password blank.
9. For Connection Data, enter the following text: Data Source=[IP address or server name*]; Provider=PIOLEDB;
*Note: Enter your IP address or server name in place of the bracketed text. Remove the square brackets.
10. Press Save in the top ribbon.
Keywords: Rockwell FactoryTalk historian adapter
sensor data source
References: None |
Problem Statement: When importing date and time data into Aspen Mtell, what formatting should be used? | Solution: Aspen Mtell follows the standard Microsoft date and time formats when importing CSV files
When using Aspen Mtell, the Microsoft formats should correctly represent the date and time data being imported.
Format specifier Description Examples
d The day of the month, from 1 through 31. M/d/yyyy H:m:s
5/2/2020 0:0:0
dd The day of the month, from 01 through 31. M/dd/yyyy H:m:s
5/02/2020 0:0:0
M The month, from 1 through 12. M/d/yyyy H:m:s
5/2/2020 0:0:0
MM The month, from 01 through 12. MM/d/yyyy H:m:s
05/2/2020 0:0:0
MMM The abbreviated name of the month. d-MMM-yyyy H:m:s
2-MAY-2020 0:0:0
yy The year, from 00 to 99. M/d/yy H:m:s
5/2/20 0:0:0
yyyy The year as a four-digit number. M/d/yyyy H:m:s
5/2/2020 0:0:0
h The hour, using a 12-hour clock from 1 to 12. M/d/yyyy h:m:s AM
5/2/2020 1:0:0 AM
hh The hour, using a 12-hour clock from 01 to 12. M/d/yyyy hh:m:s AM
5/2/2020 01:0:0 AM
H The hour, using a 24-hour clock from 0 to 23. M/d/yyyy H:m:s
5/2/2020 1:0:0
HH The hour, using a 24-hour clock from 00 to 23. M/d/yyyy H:m:s
5/2/2020 01:0:0
m The minute, from 0 through 59. M/d/yyyy H:m:s
5/2/2020 0:1:0
mm The minute, from 00 through 59. M/d/yyyy H:mm:s
5/2/2020 0:01:0
s The second, from 0 through 59. M/d/yyyy H:m:s
5/2/2020 0:0:1
ss The second, from 00 through 59. M/d/yyyy H:m:ss
5/2/2020 0:0:01
f The tenths of a second, from 0 through 9. M/d/yyyy H:m:s.f
5/2/2020 0:0:0.1
ff The hundredths of a second, from 00 through 99. M/d/yyyy H:m:s.ff
5/2/2020 0:0:0.01
fff The thousandths of a second (milliseconds), from 000 through 999. M/d/yyyy H:m:s.fff
5/2/2020 0:0:0.001
. The separator between the seconds and milliseconds of the time portion. M/d/yyyy H:m:s.f
5/2/2020 0:0:0.0
: The time separator. M/d/yyyy H:m:s
5/2/2020 0:0:0
/ The date separator. M/d/yyyy H:m:s
5/2/2020 0:0:0
Keywords: Aspen System Manager / Agent Builder
datetime
AM PM
sensor data historian
work order
date format
timestamp
CSV import date
References: None |
Problem Statement: When trying to train agents, the job in the job queue gets stuck at Loading Data and Creating Exemplars.... | Solution: The indices in certain SQL tables became fragmented, which slowed down the training of agents. The tables affected are
1. RCM.tbl_SensorGroupSensorRoleMappings
2. RCM.tbl_TrainingSetProfileData
3. RCM.tbl_TraningSetProfileTagMappings
Caution! This procedure should be followed by Database Administrator after taking database backup
To resolve this, do the following:
1. Open SQL Server Management Studio.
2. Expand the Tables folder in the Mtell database.
3. Expand one of the above tables.
4. On the Indexes subfolder, right click and select Rebuild All.
5. Repeat steps 3 - 5 for the other tables above.
Keywords: Aspen Mtell Agent Builder
retrain agents
References: None |
Problem Statement: How to assign FMEA codes to Live agents in Aspen Mtell | Solution: FMEA codes can be assigned to Live Deployed agents from Aspen Mtell System Manager. These codes will then also be a part of the Email alert if the template consists of the macro for these codes. Code assignment can be done by the following:
1. Open Aspen Mtell System Manager
2. Click on Equipment [1] tab
3. Select the Asset in consideration (here Compressor 1 [2] )
4. Click on the Agents [3] option under Health Monitoring
5. Select the Agent [4] that FMEA codes need to be assigned to
6. Enter the FMEA codes [5] selection in the Reliability Row of the Agent Settings tab
7. Select the FMEA Code Source (here User defined [6])
8. Click Refresh [7] to load the respective codes
9. Select the respective level of Problem/Cause/Remedy Code to be assigned (here Bearing/Wear/Replace[8])
10. Click OK [9] to firm up your selection
This should assign the respective codes to Live Agent.
Keywords: FMEA Email
Cause Code
Problem
Remedy
Failure mode
References: s
How to change/edit email notification settings after the agent has been deployed live |
Problem Statement: How to change the Aspen Mtell Database Recovery Model to Simple mode to manage Log files growth rate | Solution: Changing the Aspen Mtell Database Recovery Model to Simple mode is recommended if you don't want your logs to grow as fast as they currently are. Risks of doing so should be weighed by the Database administrator based on how often Database backups are conducted.
In order to shrink logs, open SQL Server Management Studio (SSMS) and connect to the SQL server hosting Aspen Mtell Database
1) Locate the Aspen Mtell Database in SQL server and right click on it (MtellSuite here) [1]
2) Select Properties [2]
3) Open Options [3] and select Simple from the Recovery Model Dropdown [4]
4) Confirm the setting by clicking OK [5]
This should change the Recovery Model of the Database to Simple and reduce Log File size growth rate.
Please refer to the Microsoft document related to Recovery mode of Database to understand further.
https://docs.microsoft.com/en-us/sql/relational-databases/backup-restore/recovery-models-sql-server?view=sql-server-ver15 [docs.microsoft.com]
Keywords: Fast growth
Log size growth rate
Space management
Data settings
References: s
How to shrink Mtell SQL Database logs |
Problem Statement: How to train a Machine Learning Agent on CSV Historian Data and deploy it live on another Historian? | Solution: When the Aspen Mtell user has imported their historian data using CSV files and their historian does not contain much history data, they can train the agent on the CSV data and then switch the historian to connect to the live historian.
1. Setup CSV Historian on Aspen Mtell System Manager
To setup CSV Historian refer to How do I create a CSV-based historian sensor data source?
2. Import the CSV Historian Data using CSV files.
To import CSV historian refer to How do I import historian data available in CSV file format into Aspen Mtell?
3. Launch Aspen Mtell Agent Builder and Import the data into TDS
4. Train your agent within the TDS you imported. When training the agent, it will use CSV Historian data.
5. Once the Agent training is completed, Change Sensor Data source to the live Historian you intend to connect to by selecting the respective Historian [1] from the dropdown as below (Aspen InfoPlus.21 here)
6. Fill in the respective adapter configuration details [2] and make sure the Connection Test is successful
7. Save [3] the changes to lock the information in.
7. Deploy Trained agents Live
Mtell will process new data from the Live Historian at set Processing schedule and TDS granularity. The system is now being fed by Live Historian data for monitoring.
Note: While doing this, please make sure the tag names on CSV files and historians are identical. Also, make sure that Sensor Data Source name remains unchanged (Here it is an example CSV).
Keywords: Offline data
CSV Historian
Train Agent Offline
Deploy Live
References: None |
Problem Statement: How do I create high frequency agents using Aspen Mtell System Manager?
High frequency agents are a subset of rule agents that are processed by agent services on a smaller time interval to get a higher frequency of results | Solution: 1. Open Aspen Mtell System Manager
2. Select the Equipment [1] tab
3. Navigate the Asset Hierarchy [2] to find the asset of interest
4. In the health monitoring sub section, select the Agents[3] option
5. Select the Add agent [4] option from the ribbon and choose rule agent in the drop-down menu.
6. Refer to kb article on How do I create Rule Analysis Agents?
7. Once the Rule Agent is created you will be able to edit the Agent Settings
8. Check the box with Use high Speed Processor in order for this agent to be processed as a high frequency agent
9. These agents will now process at a frequency setup in the Scheduling Configuration as the below tab (here every 1 minute)
Keywords: High speed
Fast Rule
Instantaneous
Mtell scheduling
Processing Frequency
References: How do I change Agent Processing frequency in Aspen Mtell System Manager? |
Problem Statement: How to create a trend that updates dynamically with new tag data using the MES Excel Addins. | Solution: A dynamically updating trend can be created using the MES Excel Addins. To complete this process you will first want to go to the Aspen Process Data tab within MS Excel and then select the 'Historical Values' function. Next you will need to enter the Tag name and Map record for the tag/s that you are desiring to create a trend for. Since this process will require data that is being updated you will then need to select a 'Relative Day and Time' for the start and end times. In the example shown below the start time has a 1 hour offset and the end time is current because all of the offset selections are zero.
Next you will need to add a Timer to the spreadsheet which will request data for the period specified by the start and end time selections at the interval chosen in the Timer settings. It is also important to select the checkbox to automatically start Timer when Workbook is Reopened. This will ensure that next time the spreadsheet is reopened it will continue updating with current data. After adding the Timer you will now have a data set that is updating with the most current values for that tag for the period specified.
Lastly you will want to insert a scatter plot into the spreadsheet and right click on the newly created plot and choose select data. From there you can add a data series where you can give your plot a name within the Series name field and select the data columns you will be using for the x and y axes. In this case you will want to select the timestamps column as the x axis and the data values column as your y axis. After completing this process you will now have a data trend for a tag over the period specified that is updating with new data at the interval chosen with the Timer.
Note: This process could also be completed by using the 'SQLplus Query' function instead of the 'Historical Values' function. For example you can achieve similar results by using a script written to return the last 1000 values and timestamps for a tag. This would then provide you with a dynamically updating trend showing data for the most recent 1000 values.
Key Words
Excel
trend
dynamic
tag
Keywords: None
References: None |
Problem Statement: Is it possible to find the source of pure component parameters? | Solution: You can often see the references in the Aspen Properties Enterprise Database (APED) Manager. Many parameters have citations available in the NIST-TRC and in PURE38 and higher.
After opening the Aspen Properties Database Manager, add the desired component.
The citation will show in the bottom pane when you click on the Citation cell for a Parameter.
Keywords: None
References: None |
Problem Statement: There is a difference between Move Suppression parameter in GDOT compared with APC. | Solution: The ‘Use Move Suppression’ option in console is limited to Infeasible problems. This option tells the optimizer to use Move suppressions or not if the problem is Infeasible, there is no such option if the problem is feasible.
If you would like to test the optimizer without move suppressions you would have to set move suppressions to 0 for the MVs you are interested in.Directional test with no move suppressions gives a linearSolution at constraints for one cycle. However, the finalSolution may lie at unconstrained optimum depending upon how non-linear the model is and the optimizer configuration.
It is not expected to use the optimizer online without move suppressions. The reason is that since we are using linear gains every cycle the optimizer will be calculating a linearSolution that may not be representative of where the finalSolution will end to be and typically it would make extreme MV moves and may become unstable. The optimizer may be affected by any small/numerical inconsistencies, somewhat analogous to collinearity issues in DMC.
Keywords: Aspen GDOT, GDOT console, Move Suppression, infeasible
References: None |
Problem Statement: There is a difference between for the Aspen Unified GDOT Builder in the Hydrotreater unit type Standard VS Diesel.
The Standard type shows the Feed Sulfur property but for the diesel hydrotreater, but for the Diesel type it removes that parameter. | Solution: Consider the HDS1 the Hydrotreater unit and the service specified as “Diesel”.
When the hydrotreater type is Diesel, the residual of row HDS1_PROD_SULFUR_BAL depends on HDS1_FEED_VAR1 and not on HDS1_FEED_SULFUR. Since HDS1_FEED_SULFUR does not contribute to any residual, the variable does not exist.
When the hydrotreater type is Standard, the residual of row HDS1_PROD_SULFUR_BAL depends on HDS1_FEED_SULFUR.
The fact that the hydrotreater is underspecified when you switch from Standard to Diesel type is not a defect either since you can bring the system to be squared by pressing Reset specification.
Use “Diesel” type when you are processing a diesel feed. Use standard for everything else.
Keywords: Aspen Unified, Unified GDOT Builder, hydrotreater, diesel
References: None |
Problem Statement: The CCP report is the standard Aspen Capital Cost Estimator evaluation report, but sometimes it can be hard to be read because it is unaligned. | Solution: To make the CCP look aligned, the font needs to be changed to the following:
Font: Courier New
Font Style: Regular
Size: 7
Keywords: ACCE, CCP, reports, unaligned, mess, disorganized
References: None |
Problem Statement: How can I see a list of the Codes of Account (COA) used in the project? | Solution: In order to see all of the COAs that are being used in the project follow the steps below:
1. Evaluate the project
2. Run the Interactive Reports selecting Excel as the report type
3. Select the Combined – Overall report, this can be found in the following path: Full Import > Capital Cost Reports > Direct Costs > COA Summaries > Combined – Overall
4. The report will display a full list of the COAs used in your project
Keywords: COA, full, complete, list, all
References: None |
Problem Statement: Creating custom Excel reports in the New Reporter (SQL Server database) for the interactive reporter | Solution: The attached PDF file covers the following topics in the creation and use of custom Excel reports in the New Reporter for the interactive reporter in the Economic Evaluation products:
Define report information in the database
Install Microsoft SQL Server
Connecting to LocalDB
Including report and query information in Icarus_User.mdf
Migrating an Access Database query to the SQL Server database query
Detach the Icarus_User Database from SQL Server Management Studio
Create an Excel Template for the New Reporter
Understanding Project Properties
Add headers and format the template
Insert a logo for the report
Replacing the logo for the report
Adding a configuration sheet to the report
Define name ranges for the report
Define column names
Sort the data
Adding a macro to the report
Merging macro sub-routing with the main ST.xlsm template
Running the new custom report
Keywords: Custom reports, custom, reports, Excel, SQL, New reporter
References: None |
Problem Statement: Fortran subroutine flash has a parameter called JRES for retention. What does retention mean?
Do I get the same results with JRES at 0, 1 or 2 ?
Does the code execute more efficiently if I set JRES correctly ? | Solution: JRES is the integer restart flag that specified how the retention vector is used.
JRES Simulation restart flag
0=Do not use retention. Initialize with default values
1=Do not use retained values but retain values for subsequent runs
2=Use retained values and retain results for subsequent runs
3=Use guesses from STWORK and STWKWK and save retention
4=Use retained values but do not retain results for subsequent runs.
When a user-written subroutine calls FLSH_FLASH, pass JRES=2 or 3 to tell FLASH whether to restart the calculations from the previousSolution. This should result in faster flash calculations.
The first time a user subroutines calls FLSH_FLASH, pass a value of JRES=0 or 1 (it doesn't matter which is used) to tell FLASH to generate initial guesses.
Also, if you want to use JRES=2, you must save the retention arrays that are passed to FLASH. These are described in the User Models manual.
The value of JRES does not affect the answer, only the speed of calculations.
The effect of using retention (JRES=2) has an effect on several levels. Each level requires more work on the part of the person writing the user model:
Inside the user subroutine. FLASH can be called more than one time, for example if it is doing iterative calculations. Setting JRES=2 will cause subsequent flash calculations to converge faster. The subroutine writer needs to save the arrays IRETN and RETN between calls to FLASH.
If the user model is in a flowsheet inside a convergence loop, using retention can cause the flash to converge faster when the unit operation model is executed. In this case, the user needs to retain IRETN and RRETN between calls to the block. The subroutine can check the value of USER_IRESTR in COMMON / PPEXEC_USER/ . If the user wants to take full advantage of retention and has coded the subroutine correctly, USER_IRESTR can be passed to FLASH as JRES.
If a user saves as an .apw file and re-opens the run, it should behave as if the user never closed the simulation. If the user has JRES=2 and has saved IRETN and RETN, FLASH will restart from the previousSolution. This means that IRETN and RETN have to be part of the INT and REAL array for the user model.
1 & 2 are independent of how the user saves the run or whether they are running from input file or from the GUI.
The easiest thing to do is to set JRES=0. This will take a bit longer in the simulation, but it is the easiest to implement.
The next more difficult option (not too much more work) is for the user to create arrays for IRETN and RETN (or use STWKWK_LRSTW and STWKWK_LISTW as described in the User Models Manual). The user would set JRES=0 (or 1) on the first call to FLASH within the user model. On subsequent calls, set JRES=2. Obviously, if the user model only calls FLASH once (not iteratively), there is no reason for this level of complication.
For more information on setting IRETN and RETN see knowledgebase document 97760.
Keywords: flash
flsh-flash
user subroutine
References: None |
Problem Statement: Why Aspen Properties and Aspen Simulation Workbook Add-In cannot be added to Microsoft Excel? | Solution: If the user is working with a 32 bit version of Microsoft Excel, this issue could be caused as the Add-Ins were not register properly during the installation; so the user can perform the following steps to manually re-registered the Add-Ins.
For Aspen Properties Excel Add-In:
Open command prompt with Admin Rights.
Un-register the Excel Add-In running this command line:
regsvr32 /u “C:\Program Files\AspenTech\Aspen Properties V11.0\Engine\Xeq\APXLAddinLoader.dll”
Re-register the Excel Add-In running this command line:
regsvr32 /s “C:\Program Files\AspenTech\Aspen Properties V11.0\Engine\Xeq\APXLAddinLoader.dll”
For Aspen Simulation Workbook Excel Add-In:
Open command prompt with Admin Rights.
Un-register the Excel Add-In running this command line:
regsvr32 /u “C:\Program Files (x86)\AspenTech\Aspen Simulation Workbook V11.0\ASWXLAddinLoader.dll”
Re-register the Excel Add-In running this command line:
regsvr32 /s “C:\Program Files (x86)\AspenTech\Aspen Simulation Workbook V11.0\ASWXLAddinLoader.dll”
Notes:
The re-register step command works in a silence mode so the user won't see any confirmation message; only will see a message if the command fails
During the re-register step, if a message appears saying it cannot find the dll use the same commands but without the (x86).
i.e. regsvr32 /u “C:\Program Files\AspenTech\Aspen Simulation Workbook V11.0\ASWXLAddinLoader.dll”
For other versions locate the dll and paste the path in the command above.
i.e regsvr32 /u “C:\Program Files (x86)\AspenTech\Aspen Simulation Workbook V10.0\ASWXLAddinLoader.dll”
Keywords: Excel Add-In, Aspen Properties, Aspen Simulation Workbook, Microsoft Excel, ASWXLAddinLoader, APXLAddinLoader.
References: None |
Problem Statement: Aspen Plus implements an automation interface, which enables you to create unique | Solution: s to accomplish things that the software is not natively designed to do. To illustrate, a program that prints stream results to Excel 365 is presented. The example utility program runs as a standalone exe file, and does not require installation.
Solution
After three simple steps, the utility program can print stream results for any open Aspen Plus file to Excel, and it does not require any complex variable linking like ASW does.
Step 1: Select a simulation to report.
When the program is running it continuously looks for any open Aspen Plus files, no matter the version. All open files will be listed. Select the file you would like to print the stream summary for.
Step 2: Select a workbook and worksheet to report to.
Like in the previous step, all open and available Excel workbooks will be listed. When you select a workbook, the worksheets for that item will be listed in the table below. Select or add a sheet to report the stream summary to. You can also double-click on the sheet name or press F2 to rename the sheet:
Step 3: Select the report options.
You can report flow rates and/or contents in moles or mass, including the option to report any Property Sets listed in the Setup > Report Options > Streams > Property Sets of the file. You can print a summary, or you can include report results for each substreams.
When you Run the report, the results will be printed to your selected Excel workbook and sheet. Stream summary information (description, classification, scope and status) will always be listed at the top, with all remaining selections printed below this. Note: results are printed in the selected global units of the flowsheet:
By default, the Excel sheet that is reported to will be wiped clean before printing the results. If you want to limit what is deleted from the sheet (e.g., formatting) then you can modify this under Settings:
Keywords: None
References: None |
Problem Statement: Aspen Plus generates and uses many ASCII file types (*inp, *bkp, *his, *rep, *var...), which means that custom programs can be created to read and edit these types of file. To illustrate, a simple program that can convert Aspen Plus file to function between versions is presented. | Solution: The utility program automates the procedure from the followingSolution article:
How do I open a higher version of an Aspen Plus backup (.bkp) file from a lower version?
Please NOTE the following limitations:
Column Analytics defined V9+ cannot be back converted to earlier versions without error, but offending blocks can be re-defined after conversion.
Stream-Groups for Aspen Batch Modeler were added in V10 (Boundary and Charge), and will have to be deleted after conversion.
The available download runs as a standalone *.exe file, no installation required. It can convert *.inp, *bkp, *apw and *apwz files types. Double-click the Aspen Plus File Version Converter.exe to launch the program:
You can either browse to select a file or files, or you can simply drag-and-drop files(s) onto the form (including folders).
After reading the current files version, you will be able to select the new target version... then click Convert. You can also right-click items to launch them in Aspen Plus, which will attempt to open the files in their own version if installed (if not installed, it will attempt to open the files in the latest installed version).
The source file will remain. The converted file will be the parent name appended with the target version number:
Keywords: None
References: None |
Problem Statement: How can I provide limits on values so model end users are only able to enter values within a specified range in Aspen Simulation Workbook? | Solution: Users may use the data validation tool to enforce limits on which values may be entered in ASW tables.
1. Select the appropriate cell and go to Data | Data Validation
2. Select the type of values to allow and enter appropriate limits
3. If the user enters a value outside the limit an error message will pop up telling them it is not allowed.
4. Optionally, provide minimum and maximum values or allowed types, to provide guidance to model end user on acceptable inputs.
Key Words:
Aspen Simulation Workbook, model end user, values, limits, specified range, data validation
Keywords: None
References: None |
Problem Statement: Is it possible to configure bi-directional replication? | Solution: If it is required to send values from the InfoPlus.21 Subscriber Server to the InfoPlus.21 Publisher Server, bi-directional replication is possible but it is required to be careful while configuring it.
Before enabling replication for the desired tags, make sure that on the other InfoPlus.21 Server the tags selected to receive information do NOT have replication enabled (Only in one server this option must be checked for every tag).
Not following this step will result in an infinite loop of information going back and forth once the second replication gets started.
KB article mentioning all the steps to configure Replication: How do I configure Aspen InfoPlus.21 V8.0 (and above) Data and Tag Replication?
Keywords: Replication
References: None |
Problem Statement: On a Cim-IO connection with Yokogawa, the following error appears on the Get Transfer:
ACG10S Data Could Not Be Converted To Client Datatype | Solution: What this error means is that ACG10S is sending the information in a different format than REAL. Verify that the occurrences associated with this error are set up to Default in IO_DATA_TYPE in the Repeat Area of your Get Transfer.
Also, verify that the Yokogawa DCS is sending values in Real Format.
Keywords: Cim-IO
Yokogawa
References: None |
Problem Statement: This Query gets information for each Aspen InfoPlus.21 tag within a Transfer Record such as: Name, Type (if it is Analog, Text, Discrete), Plant Area, Value Format, ENG-Units, Description, Low Limit, High Limit, and the information of its Transfer Record (Get, Put, Unsolicited). | Solution: For this query you inly have to enter 2 values: the name of the output file and the name of the Transfer Record.
This query can set a .CSV file or a .TXT file output in the command line set output 'C:\Temp\infotags.csv'; just change the extension of the file and give the name that you want.
SET Column_Headers 0;
SET Value_between ',';
set output 'C:\Temp\infotags.csv';
select substring(1 of IO_Value_Record&&Fld) as Tag Name,
Case substring(1 of IO_Value_Record&&Fld) -> Definition When 'IP_AnalogDef' then 'Analog' when 'IP_textDef' then 'Text' When 'IP_DiscreteDef' then 'Discrete' When 'IP_TextDef' then 'Text' Else Null end as Type,
substring(1 of IO_Value_Record&&Fld) -> IP_Plant_Area as Plant Area,
substring(1 of IO_Value_Record&&Fld) -> IP_value_format as value format,
substring(1 of IO_Value_Record&&Fld) -> IP_eng_units as Units,
substring(1 of IO_Value_Record&&Fld) -> IP_Description as Description,
substring(1 of IO_Value_Record&&Fld) -> IP_low_limit as Low Limit,
substring(1 of IO_Value_Record&&Fld) -> IP_high_limit as high Limit,
IO_frequency,
IO_Main_Task -> IO_Device as IO Device NAme,
IO_TagName,
case when definition in ('iogetDef', 'iolongget', 'iollget') then 'Get'
when definition in ('IOputDef','IoLongPut', 'iollput') then 'Put'
when definition in ('IOunsolDef','IoLonguns', 'iolluns') then 'Uns'
when definition in ('IoPutOnCosDef','IoLongPOC', 'iollpoc') then 'PutCOS'
else null end
as Type of transfer record
from getmatrikon
Keywords: Query
SQLplus
Trasfer Record
References: None |
Problem Statement: This Query gets information for each Aspen InfoPlus.21 tag within a Transfer Record such as: Name, Type (if it is Analog, Text, Discrete), Plant Area, Value Format, ENG-Units, Description, Low Limit, High Limit, and the information of its Transfer Record (Get, Put, Unsolicited). | Solution: For this query you inly have to enter 2 values: the name of the output file and the name of the Transfer Record.
This query can set a .CSV file or a .TXT file output in the command line set output 'C:\Temp\infotags.csv'; just change the extension of the file and give the name that you want.
SET Column_Headers 0;
SET Value_between ',';
set output 'C:\Temp\infotags.csv';
select substring(1 of IO_Value_Record&&Fld) as Tag Name,
Case substring(1 of IO_Value_Record&&Fld) -> Definition When 'IP_AnalogDef' then 'Analog' when 'IP_textDef' then 'Text' When 'IP_DiscreteDef' then 'Discrete' When 'IP_TextDef' then 'Text' Else Null end as Type,
substring(1 of IO_Value_Record&&Fld) -> IP_Plant_Area as Plant Area,
substring(1 of IO_Value_Record&&Fld) -> IP_value_format as value format,
substring(1 of IO_Value_Record&&Fld) -> IP_eng_units as Units,
substring(1 of IO_Value_Record&&Fld) -> IP_Description as Description,
substring(1 of IO_Value_Record&&Fld) -> IP_low_limit as Low Limit,
substring(1 of IO_Value_Record&&Fld) -> IP_high_limit as high Limit,
IO_frequency,
IO_Main_Task -> IO_Device as IO Device NAme,
IO_TagName,
case when definition in ('iogetDef', 'iolongget', 'iollget') then 'Get'
when definition in ('IOputDef','IoLongPut', 'iollput') then 'Put'
when definition in ('IOunsolDef','IoLonguns', 'iolluns') then 'Uns'
when definition in ('IoPutOnCosDef','IoLongPOC', 'iollpoc') then 'PutCOS'
else null end
as Type of transfer record
from getmatrikon
Keywords: Query
SQLplus
Trasfer Record
References: None |
Problem Statement: How to get Java Runtime Environment (JRE) 32 & 64 Bit pre-requisite during aspenONE Installation pre-requisite validation? | Solution: During aspenONE installation pre-requisite validation whenever it asks for 32 and 64 bit Java Runtime Environment one of the simplest and easiest way to get this is via directly visiting below links for 32 & 64 bit JRE and downloading it. We just need to visit these sites and load these pre-requisites from below links rather keep on searching for different links to download it. These pre-requisite are not available on Aspen third party redestributables folders as well. The above screenshot is during the installation of Aspen Web server and IP21.
Link for downloading 32 bit Java Runtime Environment (JRE):
https://www.filepuma.com/download/java_runtime_environment_32bit_8.0.1620.12-17918/download/
Link for downloading 64 bit Java Runtime Environment (JRE):
https://www.java.com/en/download/manual.jsp
Click on the one highlighted in yellow to download 32 & 64 bit JRE.
Once downloaded and run the .exe files will install these pre-requisites and the installation should now proceed successfully.
Key words:
Java Runtime Environment
32 & 64 Bit
Keywords: None
References: None |
Problem Statement: What is the REFPROP version used in Aspen Plus? | Solution: In Aspen Plus V12.1, the REFPROP is version 10.0.0.02.
In Aspen Plus V12, the REFPROP is version 10.0.0.02.
In Aspen Plus V11, the REFPROP is version 10.0.0.02.
In Aspen Plus V10, the REFPROP is version 9.1102.
In Aspen Plus V9, the REFPROP is version 9.1102.
In Aspen Plus V8.6 and V8.8, the REFPROP is version 9.1.
In Aspen Plus V8.4, the REFPROP is version 9.1.
In Aspen Plus V8.2, the REFPROP is version 9.0.
In Aspen Plus V7.3.2 and aspenONE V8.0, the REFPROP is version 9.0.
In aspenONE V7.3, the REFPROP is version 8.01c.
Key Words
REFPROP
Physical properties
Keywords: None
References: None |
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