question
stringlengths 19
6.88k
| answer
stringlengths 38
33.3k
|
|---|---|
Problem Statement: I have a weight based model but I want to add a constraint for a certain feed to my submodel to be in volume. How can I do this?
|
Solution: Add an E row for SPV to convert each stream in volume. Then, sum the new columns and put a constraint. An example is shown below. This is a small excerpt from a SCCU submodel in our Weight Sample model. Notice the two ESPV rows transfer the weight activity into columns BP1 and BP2 using the SPV's and the Volume to weight conversion (VTW) of 0.1587. Columns BP1 and BP2 now carry the volume activity of the feeds and can contribute to the desired volume-based capacity (CCAPCCU).
Keywords: volume, weight, capacity, conversion
References: None
|
Problem Statement: How is the PrUnitOperationUtility table's FeedFlag field in the PIMS output DB is generated? In other words, how does PIMS decide which Utility in the unit is a feed or a yield when writing Results.mdb?
|
Solution: The feed flag is calculated based on the balance in a submodel for the result.mdb of the given run. The setting will imply whether the stream is consumed or produced in the given submodel. If it is consumed than the flag is 1 (feed), otherwise it is 0.
For detailed calculation please see enclosed excel example.
NOTE: In case of zero activity the flag will be also marked as 1.
Keywords: Result.mdb
Feed flag
References: None
|
Problem Statement: What does function NLUNKOWN mean in Matrix
|
Solution: In the Matrix Analyzer, the function NLUNKNOWN(variable1, variable2,…) indicates that this is a non-linear equation with unknown definition. In other words, the exact formulation of the equation (variable1*variable2 or Variable1^3+Variable2^3).
To get the definition, PIMS needs to make an external call, e.g. from an external model. PIMS knows the variables associated with the equation and finds the equation non-linear, although without exact definition for the function. If the external model is a dll file, PIMS will flag all equations as non-linear and feed in variables to do the optimization without direct access to the equations. In other words, PIMS will give the input variables values to the external model and use the result from the external model to do the optimization.
Keywords: NLUNKOWN
Matrix
References: None
|
Problem Statement: I see ABML correlations to go from D86 percent off values to TBP temperatures, but how can I convert from D86 percent off to D86 temperatures?
|
Solution: Using the ABML correlation called ABML_D86FROMPERCENTOFF, allows the user to select the method used for converting D86 to TBP. However if no such conversion is desired, the method NONE may be specified. In this case, the correlation will generate D86 temperatures, not TBPs.
Keywords: distillation, D86, TBP
References: None
|
Problem Statement: When you try to commute a license, you get the message window below. However, you are commuting from a physical machine on which Window 2008 Server is installed. Why is this message appearing?
The licensing system is unable to commute a license to a standalone machine while running a Citrix or Terminal server application. Click OK to exit.
|
Solution: Just as the message indicates, by design, you are not allowed to commute a license from a terminal server.
A terminal server could be a physical machine which has terminal service installed. Windows 2008 Server comes with terminal service installed. Thus, SLM commute detects the system as a terminal server.
You have to be continuously connected to the license server in order to run Aspen applications on a Window 2008 Server OS machine.
Keywords: standalone machine, citrix, Win 2008
References: None
|
Problem Statement: Ranging Analysis is one of the features in the Aspen PIMS Advanced Optimization package (PIMS-AO). It is a tool to analyze the minimum and maximum range for feeds/products/capacities at or near optimal
|
Solution: .
The first step is to establish a base. Once we have the optimalSolution for this base case, we set the allowable percent giveaway in the objective function. During the Ranging Analysis, PIMS will minimize the lower bound for each selected variable and maximize the upper bound for each selected variable while keeping theSolution within the designated percent change in objective function.
The combination of the Utility Index and the Flexibility Index provides the maximum operational range under optimality conditions for each feedstock.
Utility Index (Maximum Feedstock Addition)
For a given feedstock, this metric is defined as the fraction of the remaining total feed that this particular crude can displace for a predefined marginal drop in the economic objective function (typically 1%). This index ranges from 0 to 1. The formula for this is:
In other words, the Utility Index tells how much of a particular Feedstock/Product/Capacity can be added to theSolution.
0 : No additional quantity can be added (at maximum)
0.5 : It can replace 50% of all the other items at theSolution
1 : It can replace all of the other items
Flexibility Index (Maximum Feedstock Removal)
For a given feedstock, this metric is defined as the fraction (in terms of the total feed) of the optimum amount that can be displaced for a predefined marginal drop in the economic objective function. This index ranges from 0 to 1.
In other words, the Flexibility Index tells how much of a particular Feedstock/Product/Capacity can be removed from theSolution.
0 : It cannot be removed (at minimum)
0.5 : Half of it can be removed
1 : All of it can be removed (minimum zero)
Where:
Xi, MAX : the maximum fraction of the total feed this feedstock can reach at or near optimal conditions,
Xi, MIN : the minimum fraction of the total feed this feedstock can reach at or near optimal conditions.
Xi, BASE : the fraction of total feed this feedstock represents at the base optimalSolution,
Fi, MAX : the maximum of this feedstock can reach at or near optimal conditions,
Fi, MIN : the minimum of this feedstock can reach at or near optimal conditions,
Fi, BASE : the base value of this feedstock represents at the base optimalSolution
N : the total number of feeds used for range analysis
Note:
If the particular crude constitutes the ENTIRE optimum feed, i.e., Xi, BASE = 1, the index is by definition 1.
If the particular crude is NOT part of the optimum feed, i.e. XBASE = 0, the index is by definition 1.
Solution
In the attached model, we use feed analysis as an example to perform Ranging Analysis.
Procedure to run Ranging Analysis,
1. Use a model setup with PIMS-AO,
2. Run a Base case
3. From Menu Run | Advanced Optimization | Range Analysis | Perform,
Here we select 2 feed stocks AHV and ANS to analyze.
4. Select the case we ran at step 1 as a base case, set 4% as Acceptable Percentage Reduction in Objective.
5. The partial execution log shows,
--- Base Case
Feedstock AHV = 41.6612577799
Feedstock ANS = 0.
Display Equation OBJFN = 1192.95799205
================================ Starting AHV Maximization Case ===================================
Major
Iteration
=======
Variable
Convergence
Function
=======
Residual
Convergence
Function
=======
Objective
Convergence
Function
=======
Objective
Function
Value
=======
Non
Linearity
Ratio
=======
Time
=======
Most
Infeasible
Row
=======
Total
Infeasible
Row
=======
0
8.8385e-001
2.1397e-001
1.0002e+000
50.00000
1.07
9:27:00 AM
1
3.1910e-001
4.9834e-004
0.0000e+000
50.00000
0.995
9:27:00 AM
2
5.9976e-004
4.9801e-007
0.0000e+000
50.00000
1
9:27:00 AM
--- Case Maximize AHV - Results
Feedstock AHV = 50.
Feedstock ANS = 0.
Display Variable OBJFN = 1145.23957237
=============================== Starting AHV Minimization Case ===============================
Variable Residual Objective Objective Non Most Total
Major Convergence Convergence Convergence Function Linearity Infeasible Infeasible
Iteration Function Function Function Value Ratio Time Row Value
========= =========== =========== =========== ============= ========= =========== ========== ==========
0 1.1865e+001 1.4868e-003 9.9984e-001 19.82250 0.853 9:27:00 AM
1 1.9810e+000 3.4555e-004 2.7814e-002 20.65199 0.776 9:27:00 AM
2 1.4384e+001 5.5734e-004 8.2812e-003 20.39816 0.42 9:27:00 AM
3 2.6742e+000 5.7829e-004 7.6313e-003 20.63014 -0.0789 9:27:00 AM
4 1.5307e+001 5.3961e-004 7.6012e-003 20.39731 -0.0772 9:27:01 AM
5 2.6722e+000 5.7730e-004 7.6650e-003 20.63031 0.0354 9:27:01 AM
6 1.5307e+001 5.3977e-004 7.6056e-003 20.39735 0.0301 9:27:01 AM
7 1.0376e+000 2.1130e-004 5.8599e-003 20.57547 0.623 9:27:01 AM
8 6.6840e-001 1.1945e-004 1.1373e-003 20.61025 0.487 9:27:01 AM
9 9.5714e-001 6.1257e-005 7.6235e-004 20.63358 0.5 9:27:01 AM
10 4.8932e-001 5.3835e-005 5.3753e-004 20.65005 0.0741 9:27:01 AM
11 4.8134e-001 1.3571e-005 2.8150e-004 20.65868 0.744 9:27:01 AM
12 1.6205e-001 3.6004e-006 1.0743e-004 20.66197 0.742 9:27:01 AM
--- Case Minimize AHV - Results
Feedstock AHV = 20.6619705496
Feedstock ANS = 0.
Display Variable OBJFN = 1145.23957237
=============================== Starting ANS Maximization Case ===============================
Variable Residual Objective Objective Non Most Total
Major Convergence Convergence Convergence Function Linearity Infeasible Infeasible
Iteration Function Function Function Value Ratio Time Row Value
========= =========== =========== =========== ============= ========= =========== ========== ==========
0 1.2378e+000 1.3593e-004 9.9998e-001 5.590149 1.03 9:27:02 AM
1 7.1433e+000 1.3370e-003 1.3487e-001 6.478962 -2.91 9:27:02 AM
2 8.7239e-001 1.1351e-003 1.3032e-002 6.381494 0.296 9:27:02 AM
3 6.7292e+000 1.0040e-003 4.3105e-002 6.063314 0.263 9:27:02 AM
4 8.7105e-001 1.0550e-003 2.2667e-002 6.223419 -0.117 9:27:02 AM
5 6.7764e+000 1.0613e-003 9.8332e-003 6.152390 -0.0659 9:27:02 AM
6 8.7133e-001 1.0715e-003 1.4557e-002 6.256509 0.0211 9:27:02 AM
7 6.7671e+000 1.0491e-003 1.6934e-002 6.133624 0.0134 9:27:02 AM
8 8.7127e-001 1.0680e-003 1.6243e-002 6.249497 -0.00459 9:27:02 AM
9 6.7691e+000 1.0516e-003 1.5436e-002 6.137593 -0.00299 9:27:02 AM
10 8.7128e-001 1.0687e-003 1.5886e-002 6.250979 0.00107 9:27:02 AM
11 1.9820e-001 9.1155e-004 4.1029e-003 6.221229 0.148 9:27:03 AM
12 1.2005e+000 7.9958e-004 3.7536e-002 5.950172 0.662 9:27:03 AM
13 5.6075e-001 3.8641e-005 6.7301e-003 5.903397 0.931 9:27:03 AM
14 9.9356e-001 3.5984e-006 2.6537e-004 5.901565 0.574 9:27:03 AM
--- Case Maximize ANS - Results
Feedstock AHV = 36.8632232532
Feedstock ANS = 5.90156506135
Display Variable OBJFN = 1145.23957237
6. PIMS generates a report 'FeedstockRanging001.xls'.
7. From Menu Run | Advanced Optimization | Range Analysis | View, we can view the results graphically.
Keywords: Ranging Analysis
AO
XLP
XNLP
Flexibility Index
Utility Index
References: None
|
Problem Statement: How do I determine if I need to address warning W073?
** Recursion Tolerances for RFG/CARB/CARB3 Property XXX May be too Large
|
Solution: The EPA equations are very sensitive to certain properties and if there is a significant difference between the calculated quality and the quality combined with its error, the pollutant calculation produces errant results. This message is triggered when RTOL > 0.01 or ATOL/value > 10 * RTOL.
Compare the values of the indicated property in two sections of the report to determine if the variance is more than you are comfortable with. To do this, look in:
a) The fullSolution report, in the Stream Property Section (for example, look at SUL of stream URG)
b) The fullSolution report, in the Specification Blend section (look at blend URG blend qualities for the SUL value)
If there is a variance in these values, you need to determine if that is acceptable or if you want the variance reduced. If you want the variance reduced, then you should adjust the ATOL and RTOL values for that property until you are satisfied with the results.
Keywords: ATOL
RTOL
tolerance
References: None
|
Problem Statement: Using Assay Management, I have created some customized assay data. I need to make this data available to all the other Aspen PIMS users in my company. How can I do that?
|
Solution: The user library is saved in the user profile folder:
(e.g., C:\Users\YOURNAME\AppData\Local\AspenTech\Aspen Feedstock Assay Manager)
The file name is UserAssayLibrary.aal. This file can be sent to other users. They can place this file in their profile folder and will then have access to the customized assay library data that you have created.
Keywords: Assay, library, custom, customized
References: None
|
Problem Statement: When importing assay data in Aspen Assay Manager using templates, is it possible to add more cuts to the templates and is there any maximum number of cuts that can be imported?
|
Solution: Aspen Assay Manager comes with a default example template which can be used to import assay data. This template file is called DemoAssays_GCinput and can be found in the following location:
C:\Users\Public\Documents\AspenTech\Aspen PIMS\Library\Aspen Assay Management
This template file is totally freeform and the users can add as many cuts as desired.
Keywords: DemoAssays_GCinput
Template
References: None
|
Problem Statement: I have many parameter rows in my model, I would like to report them. In which reports I can report these parameter rows?
|
Solution: 1. FullSolution Process Submodel Summary
2. PROWS.xls, available in Model Settings | Reporting | Selection | XLS | PROWS
Keywords: Parameter rows
P rows
PROWS.xls
Process Submodel Summary
Report
References: None
|
Problem Statement: What is the Gas Volume to Weight Factor (GVTW) Factor in Aspen PIMS?
|
Solution: Aspen PIMS uses 60 deg. F and 1 Atmosphere as the standard for the default GVTW factor. As with the VTW factor, the user is responsible for making sure that the GVTW factor is consistent with the other unit measure text labels entered in the general model settings for VOL, GAS and WGT and with the SPG data entered for streams that are listed in table GASES. Therefore, the reports will be labeled correctly and the calculated conversions between weight, volume and gas will be correct.
In the past, BFOE (Barrels of Fuel Oil Equivilant) entries may have been used in table UNITS to convert gas volumes to liquid volumes. These entries must be removed from table UNITS when using table GASES. The density of air used to calculate the SPG for the gases should be entered in the GVTW field on the General tab of the General Model Settings dialog box.
The density of air is a function of temperature, pressure, moisture content and gas composition. There is no single standard currently in use everywhere so it is up to the user to make sure the data used in PIMS for SPG for streams entered in the GASES table are consistent with the GVTW factor entered, so that conversions between weight and volume are handled correctly.
Note: Below is a table of example GVTW factors (for dry air):
Gas Unit of Measure
Weight Unit of Measure
GVTW Factor
KSCF at 60 deg F, 1 atm.
K#
0.07636
KSCF at 60 deg F, 1 atm.
Metric Ton (2204.6 #)
0.03464
PIMS default
KSCF at 60 deg F, 1 atm.
Short Ton (2000 #)
0.03818
KSCF at 32 deg F, 1 atm.
K#
0.08066
M3 at 0 deg C, 1 atm.
Metric Ton
0.001292
Example equation for GVTW in kg / cubic meter:
Kg / M3 = 1000 * (0.001293 / ( 1 + 0.00367 * T)) * ( P / 760)
T = temperature in degrees C, P = pressure in mm Hg
Source: Handbook of Chemistry and Physics (47th Edition), The Chemical Rubber Company (CRC)
Keywords: GVTW
conversion
model setting
References: None
|
Problem Statement: Aspen Platinum Server supports two types of databases, Microsoft Access and SQL server. This knowledge base document describes how to access these databases from the Aspen Platinum server.
|
Solution: 1. Go to Start 'Aspen PIMS Platinum Sever Setup' from Start | All Programs | Aspen Tech | Planning,
2. Click 'Setup' to add 'Data Source,
There are two database options to select from, PIMS (Access) and PIMS (SQL Server)
1) If you select Access Database, you have to copy PIMS access database .MDB file to the following location:
C:\ProgramData\AspenTech\PIMSPlatinum\DataSources
2) If you select SQL Server, you need to provide the server name and database name.
Keywords: access
database
platinum
server
SQL
SQL server
configure
configuration
References: None
|
Problem Statement: In
|
Solution: 134186, we talked about that there are 3 dlls related to new matrix generator model loading
PimsModelData.dll
PimsModelLibraryForms.dll
PimsModelLibraryFormsWrapper.dll
One way to check if the dlls are the issue for XLP is to check if the table is loaded. For example, you can check if the tables are in the XLP grid after loading and before running. If you can see table BUY in the grid, then it is not a dll issue. In some rare casse, it is the dll issue. You may need to manually register those dlls.
How do you do it?
Solution
The command used to register those dlls is 'regasm.exe' which is located under .NET framework, depending on which version of .NET you installed. For example, if you installed .NET 4.0 in Window 7, the path will be,
C:\Windows\Microsoft.NET\Framework\v4.0.30319\
To register, open a Command Prompt and go to PIMS folder where those dlls located, type in,
C:\Windows\Microsoft.NET\Framework\v4.0.30319\regasm PimsModelData.dll
The problem with that is your OS may be in Winnt or some other folder instead of Windows, so it's better to use %systemroot% instead,
c:\%SystemRoot%\Microsoft.NET\Framework\v4.0.30319\regasm PimsModelData.dll
You could also put the folder address on your path under 'Environment Variables'. That way, you do not need to write the path, just simply enter,
c:\Regasm PimsModelData.dll
Keywords: XLP
model load
matrix generator
model loaded
generate
matrix
References: None
|
Problem Statement: This knowledge base article describes how to resolve the following error that may be encountered when launching 'Aspen PIMS Platinum Server Setup' from the Windows Start menu
           Server Error in Application Default web site/ASPENTECH/PIMSPLATINUM
           HTTP Error 401.2 - Unauthorized
           Â
|
Solution: This error message is caused by improper Internet Information Services (IIS Security) setup. To resolve the error follow these steps.
1. From Control Panel | Programs and Features, Select 'Turn Windows features on or off' on the left,
Â
Â
2. Find Internet Information Services (IIS) and make sure 'Windows Authentication' under 'World Wide Web Services | Security' is checked.
Â
Keywords: Platinum
HTTP Error
402.2
Unauthorized
server
IIS
Internet
Windows Authentication
Security
References: None
|
Problem Statement: Which license key is needed for Aspen PIMS Platinum and Aspen Assay Manager for V8.4 and earlier releases?
|
Solution: You need a new license key in order to run Aspen PIMS Platinum.
You can check if your license file includes specific license keys using the Aspen 'SLM License Profiler'. Look for the following keys shown in the screenshots. If you do not have the key 'SLM_RN_ALL_PLNSCHDINTF' you will not be able to run Aspen PIMS Platinum. However, you will still be able to run Aspen Assay Manager even without the key 'SLM_TR_ALL_AFAM':
.
.
Please refer toSolution 118066 for 'What is the SLM License Profiler and how do you use it'.
The Aspen Assay Manager key ('SLM_TR_ALL_AFAM') is only used for tracking, it is not required in order to run Assay Manager.
Keywords: License
Profiler
SLM_RN
SLM_RN_ALL
SLM_RN_ALL_ASPENONEWEB
SLM_RN_ALL_PLNSCHDINTF
commercial
license key
ASSAY Manager
Platinum
References: None
|
Problem Statement: How can I fix the error message: Failed to create PIMS Model Settings Treeview ?
|
Solution: For this specific problem the error show in screen shot pops up whenever the user tries to open a PIMS model (any model, even volume sample model). This error goes away after un installing GLOBAL VIEW, a third party software.
Keywords: PIMS model settings tree view
Tree view failed
Failed to create PIMS model tree
References: None
|
Problem Statement: The Property Calculation formula dialog box used to have a check box Inversion. I no longer see this.
|
Solution: The Inversion option is no longer necessary and was removed. PIMS now automatically detects if an index specification is used to replace the quality specification and the sense of the spec row must be changed from a min to a max (or vice versa).
Keywords: inversion
property calculation formula
References: None
|
Problem Statement: How can you define new crudes as combinations (blends) of existing crudes in the Aspen PIMS model?
Another Statement
I have two crude towers. Feed stream for each crude is from same tank.
It means, feed quality for each feed is always same.
How can I make it?
|
Solution: Table CRDBLEND allows to define new crudes as a blend of two or more existing crudes. The resulting crude has to be treated as any regular crude, i.e. it has to be purchased (T. BUY) and lined up to the destination crude units (T. CRDDISTL).
The resulting yields and properties of the crude will be calculated as a linear blend of the member crudes in the basis of the model, i.e. in a VOLUME based model it will be blended in volume, in a WEIGHT based model, it will be blended in weight.
In the example below, a new crude MX1 is created as a blend of 40% ARL and 60% AHV. If the total does not add to 100%, the sum of the component fractions or percentages will be normalized.
The crude MX1 also has to be added to tables BUY and CRDDISTL:
If you enter the MX1 to two logical crude units, they use the same crude mix as the feedstock.
You can review the resulting yields and properties in the Data Validation report by following the procedure fromSolution 126032:
Keywords: CRDBLEND
Blend of crudes
Mixture of Crudes
Crude Blending
Crude Pooling
References: None
|
Problem Statement: In addition to the ABML (Aspen Blending Model Library) blending methods, UBML (User Blend Model Library) provides the ability to incorporate user-defined blending correlations into the model.
How do you set up UBML?
|
Solution: The user defined UBML blending methods are stored in a file created by the user called PUBML.dll. This file has to be pasted into the Aspen PIMS installation folder, which by default is:
C:\Program Files\AspenTech\Aspen PIMS
The Aspen PIMS sample models that use AMBL and UBML provide this PUBML.dll file. For details on these sample models seeSolution 127884
In the sample models folder there is also a folder with instructions and templates on how to create the PUBML.dll file.
In default installations, for Aspen PIMS 2006.5 and higher, they can be located under this folder:
C:\Documents and Settings\All Users\Documents\AspenTech\Aspen PIMS\Library\PUBML CPP Template
Keywords: UBML
ABML
PUBML.dll
References: None
|
Problem Statement: How do I enable Queries for Aspen Report Writer in Aspen PIMS V 7.1 and above?
|
Solution: Aspen PIMS generates output file Results.Mdb, with all necessary output data. This is a Microsoft ACCESS type of Database and it required Database Views to work with Aspen Report Writer.
To create Aspen Report Writer Queries, Aspen PIMS users needs to enable the option, so that Aspen PIMS generates all required queries, at the end of Report file generation. Starting V 7.1 and above, to enable the option,
1. Go to Model Settings
2. Right Click on General
3. Go to Output Tab
4. Click on Options button and then Check the option for Create Report Writer Queries.
Please refer the screen shot for details.
For PIMS Versions prior to V 7.1, please referSolution http://support.aspentech.com/webteamcgi/SolutionDisplay_view.cgi?key=122399
Keywords: Queries
ARW Queries
Create RW Queries
References: None
|
Problem Statement: This article describes the key tuning parameters that can be adjusted to improve convergence for Aspen PIMS-AO models
|
Solution: The ?Pre-solve? Option
Aspen PIMS includes a Pre-solve options for XPRESS. The goal of the pre-solve option is to eliminate redundant rows in the LP matrix which cause increased running time, but do not contribute to the optimalSolution.
The pre-solve option appears in the Model Settings | LP | Options tab. It is the IFPRES check box near the center of the window. For better convergence we recommend this option be checked.
The Feasibility Objective Factor
This option appears in the Model Settings | Non-linear Solver | Advanced 1 tab
The Feasibility Objective Function value is the cost of a unit of infeasibility. If a non-linear equation is an E-Row, the Infeasibility Breaker option allows you to buy a unit of non-zero. For example, if the Feasibility Objective Factor value is 10,000 it will cost $10,000 to have the equation equal to 1 instead of 0. This is a major incentive to make this column have a value of 0 so you don't have to pay the $10,000.
In some cases the model has difficulties converging due to tight tolerance required or due to high non-linearity introduced by external models. Increasing this value can reduce micro infeasibilities caused by external models and helps convergence.
Keywords: PIMS-AO settings, Pre-solve, Feasibility objective factor
References: None
|
Problem Statement: There are two types of usual constraints in process units:
Flow related (e.g. the feed to the unit, one of the products, etc.)
Property or Process Parameter related (e.g. the sulfur of the feed pool, the severity or conversion of a unit)
To model the first type of constraint, table CAPS is used to impose the limits, and CCAPTAG rows are used in the submodels to defined the constraint, i.e. which column's activities will be included in the restriction.
For the second type of constraint, table PROCLIM is used to impose the limits, and two type of rows are used in the submodels, ZLIMPRM, or ZPRPTAG (PRP is a property), as described below.
|
Solution: For a Minimum specification:
For a Maximum specification:
As
The specification equations become:
For a Minimum specification:
For a Maximum specification:
These are the equations that are modeled internally when setting up limits using table PROCLIM.
There are differences in modeling when you try to access recursed properties or when you use static process parameters from the components.
PROCLIM structure using static parameters
Let?s assume that we want to limit the severity of a reformer that has 4 modes (severities) of operation.
In Submodel SREF, we need to write the following structure:
The row name used is ZLIMSEV. The first part of the name, ZLIM, is mandatory, SEV is the actual name for the restriction. The values 88, 92, 96, 102 and 104 are the actual severities at which each mode operates.
In table PROCLIM, we need to write ZSEV as the row name and enter the limits for this specification under columns MIN and MAX. Columns REPORT and PENALTY are optional.
PROCLIM structure using recursed properties
Let?s assume that we want to limit the sulfur (SUL) of the feed pool to the cat cracker. To access recursed properties from pool components, we use the -999 placeholders. They will be replaced by the actual property value for the component.
The row name used in the process submodel will now be ZSULTAG, where SUL is the property name and TAG is the restriction tag, in the example, CFP is used in the row name ZSULCFP.
In table PROCLIM, we need to write the full name ZSULCFP as the row name and enter the limits for this specification under columns MIN and MAX. Columns REPORT and PENALTY are optional.
Results
The results are reported in the ?Process Limit Summary? section in the FullSolution report (or in the Across, Down reports in PPIMS).
Each limit is also reported in the local submodel to which it applies.
Keywords: Table PROCLIM
Process Limit
Process Limits
Process Parameters
References: None
|
Problem Statement: What user rights are needed in order to install Aspen PIMS or use Aspen PIMS?
|
Solution: To install Aspen PIMS, the user needs to have an Administrator privilege. However, a regular user privilege can run Aspen PIMS.
Keywords: Admin, Administrator, Power user, user, users, installation, install, PIMS
References: None
|
Problem Statement: When checking the Results.MDB file for an XPIMS model, in Table: PrEconomicSummary, Field: EconomicSummaryTypeID = 4 (Local Utility Costs), why are the results for the individual plants all 0 but the overall grand total is OK?
|
Solution: Contrary to the headline the PrEconomicSummary table contains both GLOBAL and LOCAL utility cost data. The GLOBAL costs are in the EconomicSummaryTypeID=4, Description=Local Utility Costs while the LOCAL costs are in the EconomicSummaryTypeID=9 &10, Description=Utility Purchases & Utility Sales.
Here is a query referencing the above types that can show that they are included (and equal);
Select
CaseID , PeriodID, '1-3' as ModelId, 'Net Utilities' as Description, Sum(activity) as Activity_
from PrEconomicSummary es inner join PrEconomicSummaryType est on es.EconomicSummaryTypeID =est.EconomicSummaryTypeID
where es.EconomicSummaryTypeID in (9, 10)
group by CaseID , PeriodID
Union Select
CaseID , PeriodID, ModelId, Description, activity
from PrEconomicSummary es inner join PrEconomicSummaryType est on es.EconomicSummaryTypeID =est.EconomicSummaryTypeID
where es.EconomicSummaryTypeID in (4)
and activity<>0
order by 1, 2, 3
And here are the results from the query to demonstrate that they are equal.
CaseID
PeriodID
ModelId
Description
Activity_
1
0
1-3
Net Utilities
-95.9583418655096
1
0
4
Local Utility Costs
-95.9583418655096
1
1
1-3
Net Utilities
-91.4453227577133
1
1
4
Local Utility Costs
-91.4453227577133
1
2
1-3
Net Utilities
-97.4796952367828
1
2
4
Local Utility Costs
-97.4796952367828
Results from Query to show Local vs. Global
Keywords: Local Utility Cost
Utility Purchases & Utility Sales
Query
XPIMS
References: None
|
Problem Statement: How do I plot an envelope on a wet basis?
|
Solution: [NOTE: This only works if the stream is two phase. If there is enough water to give a separate aqueous phase, then this approach does not plot a full 3phase envelope because the vf=1 flashes are not enough to distinguish between water and HC dewpoints.]
You can use the Property Table utility to generate such a plot. Go to the Attachment tab page of the stream and attach a Property Table utility.
Independent Variable 1: Vapor Fraction, Mode: State, State Values: 0 and 1
Independent Variable 2: Pressure, Mode: Incremental, specify upper and lower pressure and number of increments.
Dependent Variable: Temperature
Calculate and look at the plot!
Please note that the range of your P-T plot should be away from the critical condition of the stream. Not like the Envelope utility where special treatment is applied to assure the closure of the phase envelope at the critical point, the dew point and bubble point curves generated in a Property Table utility would not necessarily overlap at the critical point.
Another issue to be aware of is that the property table may have some trouble at the points in the curve where the discontinuity occurs, such as in the retrograde region.
Keywords: phase envelope, wet basis, dry basis, retrograde, P-T plot
References: None
|
Problem Statement: Aspen PIMS Advanced Optimization (PIMS-AO) Analysis tools include:
Parametric Analysis
Goal Programming
Ranging Analysis
Feedstock Basket Reduction
Each of these analysis tools will execute a set of automatically generated cases. Starting with Aspen PIMS V7.1, it is possible to generate
|
Solution: and report files for each of the intermediate steps in the analysis.
How do you force the creation of these reports and what are the file names?
Solution
In the Run windows for each of the PIMS-AO Analysis tools, the option Write Each Solve to the Database can be chosen. When this option is active, it will create one report andSolution file for each of the analysis steps.
The names of the files will be the regular name of the report orSolution file followed by six numbers. The first three indicate the Case Number, the other three indicate the Analysis step.
For example, if you are running Case 3 and there are 10 Parametric Analysis steps, the FullSolution report will be called FullSolution003010.html).
The intermediate Cases stored in the Results.mdb will be identified as 003001, ..., 003010.
Keywords: PIMS Advanced Optimization
PIMS-AO Analysis tools
References: None
|
Problem Statement: How does PIMS create PROCLIM limits in the matrix?
|
Solution: We can use Table PROCLIM to apply model constraints in a PIMS model. In the following example, we want to limit AR2 in Cat Crack Feed. In submodel SCCU, we set up a row ZLIMARC, then in T.PROCLIM we set up MIN/MAX to limit AR2.
* TABLE
SCCU
CAT CRACKER UNIT
*
TEXT
BAS
AFC
SUL
LV1
HV1
DCG
AR2
CCF
*
FREE
Free up adjustor
1
1
*
Material Balance:
VBALLV1
Lt vac gas oil
1.0
VBALHV1
Hv vac gas oil
1.0
VBALDCG
Coker gas oil
1.0
VBALAR2
CR2 Atmos Btms
1.0
VBALH2S
H2 sulfide, foeb
-0.0010
-0.0002
-0.0012
*
Balance check
-1.2345
0.0152
0.0021
*
Control Rows:
ECHGCCU
Feed charge
1.0
-1
-1
-1
-1
EAFCCCU
Feed aromaticity
15.4
5.0
-999
-999
-999
-999
ESULCCU
Feed sulfur
0.8
1.0
-999
-999
-999
-999
LAR2CCU
AR2 ratio control
-0.05
-0.05
-0.05
1.00
*
ZLIMARC
AR2 LIMIT IN CAT FEED
0.00
0.00
0.00
100.0
* TABLE
PROCLIM
PROCESS LIMITS
*
TEXT
MIN
MAX
*
ZARC
AR2 LIMIT IN CAT FEED
0
2
For every Z-row, PIMS will generate a column vector with the same Z-row name, and three rows, one E-row, one G-row and one L-row. In this case, the Z-row name is ZLIMARC, so the z-column vector name is ZLIMARC.
The three rows generated by PIMS are as follows in the matrix,
Row Name
SCCUAR2
SCCUDCG
SCCUHV1
SCCULV1
ZLIMARC
RHS
ELIMARC
-1
-1
-1
-1
1
0
GLIMARC
-100
2
0
LLIMARC
-100
0
Notice that the E-row coefficient is independent on the coefficient entered in the submodel. The result in fullSolution report shows,
Process Limit Summary
Process Limit
Activity
Minimum
Maximum
Marg Val
ARC
AR2 LIMIT IN CAT FEE
2.00
0.00
2.00
0.320
Keywords: Process limits
PROCLIM
Constraint
References: None
|
Problem Statement: When only PSCP is installed, the user might encounter the following warning message when attempting to execute Matrix Comparison after running PSCP:
|
Solution: The workaround is to either:
Install PIMS before or after PSCP installation, or
Go to a computer where PIMS is installed, find SharedResDll.dll in the PIMS install directory, place that file in the same directory where MatComp.exe is installed on the computer that has PSCP installed.
Keywords: DPO, Installation, known issue, PSCP, SharedResDLL.dll, MatComp.exe, system error
References: None
|
Problem Statement: When blending with an additive there are original and recursed susceptibility values in the Recursion Log Report. How these values are calculated and how they are used to calculate the amount of additive used?
|
Solution: Simple example of Specification Blend based on minimum MON required:
1. In order to calculate the Original Susceptibility of MON in blend product BLE, PIMS subtracts the arithmetic average MON from the arithmetic average M11 blend stock values:
2. To calculate the Recursed Susceptibility of MON in blend product BLE, PIMS subtracts the weighted average MON from weighted average M11 blend stock values, where weights are volume percentages of blend stocks in the blend product:
3. Blend product has MON = 88.9696 and required MON minimum is 89.0000.
4. PIMS will use the TEL additive to increase the MON to the required value.
The required susceptibility:
The amount of TEL is calculated using corelation from ADDITIVE table:
Small discrepancies between PIMS results and manually calculated results are caused by number rounding.
Keywords: susceptibility
SUS
additive
References: None
|
Problem Statement: A model is using table INDEX or Property Calculation Formulas to calculate property index, for example RVI=RVP^1.25. RVI is specified in Table BLNSPEC. Aspen PIMS should report both RVI and RVP in the full
|
Solution: report for that blending product. However, the RVP value is not equal to the the value back calculated from RVI^(1/1.25). What could cause a discrepancy between the reported RVP value and the corresponding RVI index?
Solution
Take volume sample model as an example. We modified the PGUESS by adding a column RVP for blending product URG row.
* TABLE
PGUESS
*
Initial Property Estimates
TEXT
RVI
RVP
*
URG
15.00000
8.00000
*
In the fullSolution report, we will get the property report RVI and RVP for URG as below,
Product: URG Regular Gasoline
Product Qualities
Minimum
Product
Maximum
Marg Val
$/Unit/BBLS
RVI
Vapor Pressure Index
15.5885
15.5885
0.372
RVP*
Minimum RVP
-1000.0000
6.1260
9.0000
0.806
+For gravimetric qualities, marg value is $/Unit/MTONS
*Quality calculated from blend index
Base of RVI=RVP^1.25, with RVI= 15.5885, RVI should be 9.0 instead of 6.126.
The reason for this discrepancy is that having a PGUESS entry present prompts PIMS to recurse the RVP. Recursion has a higher order of precedence than the Property Calculation Formula or Table INDEX. Therefore PIMS recursed the RVP independent of the relationship defined in Property Calculation Formula or Table INDEX and it is this recursed value that is reported.
When we comment out the column in PGUESS, the report says 9.0 as below.
Product: URG Regular Gasoline
Product Qualities
Minimum
Product
Maximum
Marg Val
$/Unit/BBLS
RVI
Vapor Pressure Index
15.5885
15.5885
0.372
RVP*
9.0000
9.0000
0.806
+For gravimetric qualities, marg value is $/Unit/MTONS
*Quality calculated from blend index
Keywords: Index, report, RVP, RVI,
References: None
|
Problem Statement: How do I know if I have a network version of HYSYS?
|
Solution: If you are looking on the HYSYS software CD, there will be a sticker with an install code and S/N number. The S/N number is the key number. It will say NET on the sticker if you have a network version. Also, the key will be a beige colour and will go on the parallel port while the stand alone keys are a green colour and go on the serial port.
If you don't have the HYSYS CD but rather you are just starting up a HYSYS.EXE file on a PC and it is not finding the key, the error message will tell you whether or not you have a network version. For example if you get the error message Error 2: A Hyprotech network security key was found that has an invalid serial number. No licenses were available on other valid Hyprotech network security keys. Use one of the supplied rainbow technologies key monitoring tools for further information or the error message No more users are allowed on the Network security key or there are no valid operating Hyprotech network security keys... These message will only come up for the network software. Whether HYSYS is networked or standalone is governed by the install code used to install the software. You cannot run a HYSYS network version using a standalone key.
Please refer to the Get Started manual for further information. This is contained on every HYSYS software CD as well as on the HYSYS documentation CD in .pdf format.
Keywords: Network, HYSYS, pre-SLM
References: None
|
Problem Statement: Why are the baffle cut percent height and percent area values the same in my heat exchanger datasheet?
|
Solution: Aspen HYSYS reports the same values for the baffle cut (%height) and baffle cut (%area), but they are not the same. In this case, you have to be aware that:
The correct baffle cut is defined as
Baffle Cut% = Hb / Ds * 100
In the above equation, Hb is the height of baffle window and Ds is the internal diameter of the shell. This is the definition used in the heat exchanger program. For more information please refer toSolution 127651
For example:
You will see the following with double click on the heat exchanger:
And for the Data Sheet you will see:
So, please enter the value based on the correct definition of Baffle Cut.
For more information about heat exchangers please refer to the Unit Operation Guide, Chapter 4 Version7.3)
Keywords: Baffle cut, %area, %height
References: None
|
Problem Statement: I would like to add a Reid Vapour Pressure (RVP) specification to a column stream but cannot find it under Column Cold Properties Spec - where is it?
|
Solution: An RVP specification can be added under Column Vapour Pressure Spec (select Reid Vapour Pressure as ''type'').
Keywords: vapor
References: None
|
Problem Statement: If I have a model that was developed in a language environment other than English, how can I display Aspen PIMS
|
Solution: s with the text in that language even though I am using an English Windows Operating System?
Solution
You need to make sure that you have the proper language and code pages selected from the Regional & Language Options dialog in the Windows control panel.
The following steps are for Windows XP.
1. Under CONTROL PANEL, Regional and Language Options, select the language you desire.
2. From Advanced tab, under 'Language for non-unicode programs', select the same language you chose from the previous step. Click OK to exit the settings and then restart your PC.
For Windows 7, the 'Regional & Language Options' dialog is a little different and the steps are below:
1. In the Regional and Language dialog from the control panel, select the proper language in the Format tab for the format. Click Apply.
2. Click the Administrative tab. Click the 'Change system locale...' button and select the proper language. Then restart your PC.
If the text in the Aspen PIMS reports still does not show the choosen language, do the following:
a) In PIMS, from Tools menu. Select Program Options | Report tab. Click the Screen Font button. In the Script dropdown text box, select that particular language.
b) If you want to print the report, you have to make the same selection after clicking the Printer Font button.
Keywords: display
language
text
regional
region
References: None
|
Problem Statement: Does the Assay Manager support PIMS extended tags?
|
Solution: No, it does not. All tags are 3 characters long.
Keywords: AFAM
References: None
|
Problem Statement: What is the basis (volume or weight) of true boiling point (TBP) curve?
|
Solution: The default basis of TBP curve is volume%. You can change the basis under Design tab of Boiling Point Curve utility.
Keywords: TBP, true boiling point, basis, weight, volume, %
References: None
|
Problem Statement: How do I transfer information from HYSYS to HTRI?
|
Solution: The latest releases of the HTRI Software include interfaces which will read exchangers from Aspen HYSYS cases. The HTRI interface is free to users of HTRI products (as it is built into the HTRI software).
This utility is the only way to transfer data for a heat exchanger from Aspen HYSYS to HTRI if the applications are on different machines.
The current HTRI software product - HTRI Xchanger Suite - (and each of its two heat transfer sub-components Xist, and Xace) will automatically sense the presence of HYSYS by reading the Hyprotech Registry entries. If HYSYS is also installed, Xist (for example) will make an additional Property Generator button appear on its Hot (and Cold) Fluid Properties panel. By clicking that button, the Xist (or Xace)/Hysys user may import information component by component (from scratch), or unit by unit and stream by stream from within an existing .hsc file.
The older HTRI programs (up through the 2000 release of IST 2.0, and all prior legacy programs) can not use this new interface. The first release that can talk interactively to HYSYS is HTRI Xchanger Suite 1, from 2001.
Before the link was added to HTRI software, published articles alluded to a tool historically provided by Hyprotech which would generate information from HYSYS to be imported into HTRI. This can be found in the attached .zip file.
IMPORTANT: With the integration of support for Aspen HYSYS exchangers in HTRI software, this file should not be necessary moving forward, and as such is not tested for compatibility with current Hyprotech or HTRI software versions and will no longer be supported. By downloading this tool, the user assumes any risk associated with its use.
For air coolers, you can use the utility too, but you have to create a dummy HX in Aspen HYSYS and then edit the DAT file to remove the data for the other side of the exchanger.
It is recommended that you contact either Hyprotech or HTRI, respectively, for the most recent version(s) of their software.
Keywords: HYSYS-HTRI link
References: None
|
Problem Statement: Why am I getting the message Required model files have not been selected for COMThermo when I try to enter the Simulation Environment?
|
Solution: You must have a property package selected for both the vapour and liquid phases before you try to enter the Simulation Environment.
Keywords: COMThermo
References: None
|
Problem Statement: Getting OLGAS, Pipesys and black oil license errors, do I still entitle OLGAS licenses provided from AspenTech?
|
Solution: Contract signed after 1 Nov 2010 - The client needs to work with SPT group. Aspentech will not provide customers licenses anymore.
For OLGAS and Pipesys to work WITHOUT SLM licenses (contracts signed after Nov. 1, 2010) customers need to have V7.3 or V7.2 CP2.
Contract signed before1 Nov 2010 - Our license should include the SLM key. And Aspentech will provide those customers the third party license as it used to be for OLGAS and Pipesys.
Neotec Black oil will only work in V7.3 and later version if the client got the license from Neotec (SPT Group). If some one wants to use it in V7.2, then we need to release a hot fix for them.
Keywords: Neotec black oil, OLGAS, PIPESYS.
References: None
|
Problem Statement: I get an error The Property Wizard could not be launched. Please make sure it is installed and that the amf file is in the correct directory. How to fix it?
Property Method Assistant does not launch. How to fix it?
|
Solution: 1. PropertyMethodAssistant.amf file should be present in C:\Program Files\AspenTech\Aspen HYSYS (version)\Support folder. If you don't have this file, please copy it from another computer and put it there.
2. If you already have the file in the folder, run Restore File Associations (Start || Programs || AspenTech || .... || Aspen HYSYS (version) || Restore File Associations. You need administrative privilege to run it.
Please note that you can run the assistant from C:\Program Files\AspenTech\Aspen HYSYS (version)\Support folder directly by double clicking on it.
Keywords: property method assistant
References: None
|
Problem Statement: How do I find a component by CAS number in Aspen HYSYS?
|
Solution: Users will need to use ?Aspen Properties? component databank, when search by CAS number is desirable.
1. Select ?Aspen Properties? from Component List interface, and click ''Add''.
2. An Aspen Properties Component Databank window will pop up. Click ''Launch Find Component Window.
3. The component search engine window will appear, where you can now use CAS number as the search key word. Below is an example of search 'water using CAS number.
Keywords: CAS number, search component, HYSYS, Aspen Properties
References: None
|
Problem Statement: What is New in Aspen HYSYS V7.3 - Modeling of Spiral Wound Heat Exchangers
|
Solution: Liquefied natural gas (LNG) facilities are important assets for energy companies. In LNG plants, the cold box is often a spiral wound heat exchanger that exchanges heat between multiple streams in a complex pattern.
The HYSYS LNG Exchanger unit operation model now includes an option to simulate spiral wound heat exchangers. The approach is to translate the spiral wound heat exchanger (SWHE) geometry into an ?equivalent? configuration of a plate fin heat exchanger (PFHE).
A new Wound Coil tab has been added to the HYSYS LNG block to enable simulation of spiral wound heat exchangers. You can input the appropriate information such as tube bundle
The equivalent plate-fin configuration is calculated and displayed on the Plate Fin Equivalent page. You can then interact with the LNG model in the standard ways.
Keywords: None
References: None
|
Problem Statement: What is the difference between the information on the first page and on the second page of Hydrate Formation utility?
|
Solution: The information shown on the first page of Hydrate formation refers to the stream conditions, temperature AND pressure. What you see on the second page tells you the hydrate formation pressure at the current stream temperature and the hydrate formation temperature at the current stream pressure. If the operating temperature is below the indicated hydrate temperature at this fix pressure, for example, hydrate will form.
Keywords: Hydrate,
References: None
|
Problem Statement: How can I determine which flowsheet environment is currently active via Automation?
|
Solution: In HYSYS versions prior to 3.1 this is a particularly important question since topology changes (e.g. adding streams / operations) can only be made when HYSYS is in the environment of the flowsheet where the changes are to be made. This limitation no longer applies for HYSYS 3.1+.
In HYSYS you can tell which environment you are in by looking at the Environment at the top right hand corner. How can this be done via Automation?
A backdoor variableSolution is required to determine which is the current flowsheet:
Dim hyBD As HYSYS.BackDoor
Dim CurrFlwSht As object 'Use a generic object type since this can be a col or normal FS
'Get a backdoor object for the case
Set hyBD = [Simulation Case Object]
'Link to the moniker for the current flowsheet
Set CurrFlwSht = hyBD.BackDoorVariable(:FlowSht.301).Variable.Object
NB Backdoor methods are only recommended when there is no other alternative, the internal HYSYS monikers may not remain constant between versions so care should be exercised when upgrading.
This then leads into the follow up question: Once the current flowsheet has been determined how can I get back to the main flowsheet?
The answer to this is a bit more complicated...
The CurrFlwSht object returned above can either be of type Flowsheet or ColumnFlowsheet depending on whether HYSYS is editing a column or normal flowsheet. Depending on what kind of flowsheet is being edited the parent object will have a different object type (ColumnOp or TemplateOp). However both have a method called .EnterParentEnvironment which is equivalent to pressing the Enter Parent Simulation Environment button in HYSYS (Up arrow button on button bar). Hence using
CurrFlwSht.Parent.EnterParentEnvironment
will take HYSYS to the next flowsheet level above.
The following code illustrates a simple procedure that uses a Do While loop with the code above to bring a case back to the main flowsheet. To use the code: open up HYSYS with any case; paste the code into the VBA editor in Excel; make a reference to the HYSYS type library (Tools ...
Keywords: None
References: s menu option in the VBA editor) and run the procedure.
Public Sub ReturnToMainFlowsheet()
'
'Description: Brings the currently open HYSYS case back to the main environment
'
'Declare Variables
|
Problem Statement: Which equation is used for phase change in Heat Exchanger?
|
Solution: Heat Exchanger in Aspen HYSYS uses open literature correlations for calculating film coefficients and pressure drops.
Please see the attached PDF document for more details.
Keywords: Heat Transfer, Coefficient Correlations
References: s:
1. Gnielinski, V., Forced Convection in Ducts. In: Heat Exchanger Design Handbook. New York:Hemisphere
Publishing Corporation, 1983.
2. Steiner, D. and Taborek, J., Flow Boiling Heat Transfer in Vertical Tubes Correlated by an Asymptotic
Model. In: Heat Transfer Engineering, 13(2):43-69, 1992.
3. Shah, M.M., A New Correlation for Heat Transfer During Boiling Flow Through Pipes. In: ASHRAE
Transactions, 82(2):66-86, 1976.
4. Shah, M.M., Chart Correlation for Saturated Boiling Heat Transfer: Equations and Further Study. In:
ASHRAE Transactions, 87(1):185-196, 1981.
5. Nusselt, W., Surface Condensation of Water Vapor. Z. Ver. Dtsch, Ing., 60(27):541-546, 1916.
6. Kutateladze, S.S., Fundamentals of Heat Transfer. New York: Academic Press, 1963.
7. Labuntsov, D.A., Heat Transfer in Film Condensation of Pure Steam on Vertical Surfaces and Horizontal
Tubes. In: Teploenergetika, 4(7):72-80, 1957.
8. Rohsenow, W.M., Webber, J.H., and Ling, A.T., Effect of Vapor Velocity on Laminar and Turbulent Film
Condensation. In: Transactions of the ASME, 78:1637-1643, 1956.
9. Jaster, H. and Kosky, P.G., Condensation Heat Transfer in a Mixed Flow Regime.In: International
Journal of Heat and Mass Transfer, 19:95-99, 1976.
10. Taborek, J., Shell-and-Tube Heat Exchangers: Single Phase Flow. In: Heat Exchanger Design Handbook.
New York: Hemisphere Publishing Corporation, 1983.
11. Bell, K.J., Delaware Method for Shell Side Design. In: Kakac, S., Bergles, A.E., and Mayinger, F.,
editors, Heat Exchangers: Thermal-Hydraulic Fundamentals and Design. New York: Hemisphere
Publishing Corporation, 1981.
12. Gentry, C.C., RODBaffle Heat Exchanger Technology. In: Chemical Engineering Progress 86(7):48-57,
July 1990.
13. Jensen, M.K. and Hsu, J.T., A Parametric Study of Boiling Heat Transfer in a Tube Bundle. In: 1987
ASME-JSME Thermal Engineering Joint Conference, pages 133-140, Honolulu, Hawaii, 1987.
14. Grant, I.D.R. and Chisholm, D., Two-Phase Flow on the Shell Side of a Segmentally Baffled Shell-and-
Tube Heat Exchanger. In: Journal of Heat Transfer, 101(1):38-42, 1979.
|
Problem Statement: MAXSTEP and MAXSTEPD options are available in Model Settings | Recursion | General when user runs the model with Distributive Recursion (DR), which is by default. What are these options used for?
|
Solution: In general, MAXSTEP is used to assist models that have problem in convergence to converge quickly. It imposes bounds on how much the error vectors can change in each pass, and therefore by using this option the user is actually adding more constraints to the model. Using MAXSTEP could lead to a differentSolution path and hence it is possible to get an objective function value that is different than that without using MAXSTEP. It is recommended to use the option “Step bounding on error vectors of non-converged properties only”.
The tradeoff of using MAXSTEP is that it can lead to local optimum. There is another option available called MAXSTEPD which allows the user to delay MAXSTEP until the recursion pass that the user specified. If this option is used, a typical value is 4 or 5. This value can be adjusted based on model performance and response to the setting. The higher this number is, the lesser effect MAXSTEP has on convergence.
Keywords: MAXSTEP
MAXSTEPD
Distributive Recursion (DR)
References: None
|
Problem Statement: When you have a simulation with many streams and unit operations it might not be as easy to find an object especially when the case was built by someone else.
|
Solution: Go to the Tools menu and choose the first option: 'Select Objects'
This will open a new window where you will be able to browse through the different objects on the PFD. Browse through the names or select one of the filters available to display only streams, unit operations, logical operations or other specific objects.
After you hit the OK button, the object will be selected and a white box surrounding it will be blinking for a few seconds allowing the user to identify the location on the PFD. Now the user can zoom in towards the object selected and continue working.
Keywords: Stream
Object
Unit operation
Find
Highlight
Select
References: None
|
Problem Statement: What is the differences between PROFES and HTFS?
|
Solution: Profes calculates the Nusselt number using the Dittus-Boelter equation for turbulent flow and uses a value of 3.66 for laminar flow. In the transition region of flow (Reynolds numbers between 2000 and 5000), this correlation will use a Nusselt number that lies on a linear extrapolation of the Dittus-Boelter equation between Reynolds numbers of 5000 and 0. For vapor flow, the Grashof number is calculated, and heat transfer due to natural convection is considered.
In the HTFS model, there are many correlations for Nusselt number. Depending on the situation, the HTFS model for heat transfer will choose the most appropriate Nusselt number. It takes into account flow inside the pipe (including multi-phase flow), orientation of the pipe, and convection within the pipe (the Grashof number is calculated).
The recommendation would be the HTFS model as it is more in depth and investigates many more Nusselt number correlations for finding the heat transfer coefficient.
Keywords: PROFES, HTFS, correlation
References: None
|
Problem Statement: How can I create a minimum selector (or maximum selector) for controller?
|
Solution: You can use the Selector Block, where you connect your input PV's, then select a mode of operation, i.e. Minimum, Maximum, Mean, etc.. For more details regarding the selector block please consult Section 12 of the Aspen HYSYS v2004.1 Operations Guide Manual.
Keywords: Controls, selector block
References: None
|
Problem Statement: How do I import the output file from the Text to File option into Excel so that the data goes into individual columns?
|
Solution: It is important to select the proper delimiter. This may be either a comma or a space, depending how the file was setup when printed. This will depend on how your options are configured.
Use the Text File Import wizard in Excel to select this delimiter. This wizard should be automatically started once you select a text file as the type of file that you want to open.
Keywords:
References: None
|
Problem Statement: How do I find the Activity of a
|
Solution: Variable, from the LP Matrix in Aspen PIMS?Solution
Aspen PIMS using DR Technology generates two files related to matrix structures.
1. MpsProb.MPS
2. MpsBcd.Mps
(ReviewSolution 130370 for details about those two Matrix files.
Assume, you would like to see the Activity of a Variable called DCN, from SNHT Submodel.
Note that , for a submodel structure, PIMS generates the variable names using
A A A A A A A A A A A A <SUBMODEL name-4 Char> <Variable name-3 Char>
In this case the LP Matrix name is SNHTDCN.
To review the Activity of thisSolution Variable:
A? Open MpsBcd.Mps file using Matrix analyzer
A? Click on the Display by Column Command button in the Matrix Analyser
A? Search and Locate the Variable SNHTDCN
A? You can see the Activity of thisSolution variable in this Screen
Please refer the screen shot for details. Activity of theSolution variable SNHTDCN = 3.32588
Keywords:
References: None
|
Problem Statement: Is it possible to access the Air Cooler Operation through Automation?
|
Solution: Yes, although this cannot be achieved with any of the standard Automation methods. Since the Air cooler operation is not yet fully wrapped for Automation access - you will note there is no Air Cooler object in the HYSYS type library.
Instead a 'Backdoor method' must be used.
NB. Backdoor methods are only recommended when there is no other alternative, the internal HYSYS monikers or messages may not remain constant between versions so care should be exercised when upgrading.
The attached Excel (2000) file illustrates how to access the main air cooler properties.
Keywords: OLE Automation, Backdoor, Air Cooler
References: None
|
Problem Statement: Why do some petroleum properties show [empty] for some streams?
|
Solution: There can be multiple reasons for it:
1. The library components added to the model does not have petroleum properties added to the purecomponentpetroleumdata.csv file (C:\Program Files (x86)\AspenTech\Aspen HYSYS V7.3\ReactorModels)
Solution
Open the file in Notepad++ and add the missing components in the bottom row. Then save the file.
2. If you have added GC properties, make sure the properties are entered for complete distillation data. Any empty value here will bring empty value in the simulation environment. It is good idea to replace the empty values by zero if you are sure those values is zero.
3. Recycle is not passing the petroleum properties from inlet stream to outlet stream.
Solution
Ignore all the recycles and solve the flow sheet. Put the solver in hold mode. Go to each recycle and initialize the petroleum properties from a stream which has the petroleum properties. Do not worry about the numbers. It will be updated to the correct number later on. Once you have initialized all recycles, un-ignore all the recycles. And then press the solver on mode to run it. The stream should be having the petroleum properties now.
Keywords: petroleum properties, empty
References: None
|
Problem Statement: This knowledge base article describes why E200 and E300 may show as zero for the final blend.
|
Solution: This problem may happen if in Table PGUESS; the input values for Evaporative ABML correlation do not monotonically increase, which causes the Evaporative calculation to fail. Monotonic means that the numbers always increase or stay the same without decreasing. When the values are modified such that they monotonically increase in PGUESS the error is no longer returned.
Keywords: ABML Percent off
E200
E300
Zero in final blend
References: None
|
Problem Statement: How can you model a static property that has a different value in a different period?
|
Solution: Table BLNPROP supports a period specific input. By adding the one character period identifier as the 4th character to the material tag, the value for the property becomes specific for that period.
The example shows how to enter three different SPG values for a Purchased Gasoil stream in three different periods.
Keywords: Period specific property
Period specific properties
Period dependent property
References: None
|
Problem Statement: Is there a maximum stream velocity for Aspen HYSYS Pipeline Hydraulics - PIPESYS calculations?
|
Solution: PIPESYS permits a maximum velocity of 2000 ft/s. Generally, convergence problems in Pipesys are related to high velocity, low pressure or small diameter.
Keywords: Pipesys, velocity
References: None
|
Problem Statement: How to use the user variable to compute the viscosity with different compositions in the stream?
|
Solution: Here is an example code how to change the composition, flash and get the new viscosity based on new compositions.
Sub PostExecute()
Dim hystream As ProcessStream
Dim hyFluid As Fluid
Dim CompMoleFrac As Variant
Dim i As Integer
On Error GoTo ToError
Set hystream = activeobject
' random composition
Set hyFluid = hystream.DuplicateFluid
CompMoleFrac = hyFluid.MolarFractionsValue
' get dummy new composition
For i = 0 To hyFluid.Components.Count -1
CompMoleFrac(i) =1/(hyFluid.Components.Count-1)
Next i
hyFluid.MolarFractionsValue = CompMoleFrac
If hyFluid.TPFlash(hyFluid.TemperatureValue,hyFluid.PressureValue )= fsFlashOK Then
Activevariablewrapper.Variable.SetValue(hyFluid.LightLiquidPhase.ViscosityValue,cP )
End If
Exit Sub
ToError:
MsgBox Error in User Variable
End Sub
Keywords: viscosity, user variable
References: None
|
Problem Statement: Every time I try to increase parallel shell passes (any value above 1) in a Rating Exchanger, it doesn't take it?
|
Solution: Multiple Parallel Shell passes is not supported in Hysys right now.
Keywords: Heat Exchanger
References: None
|
Problem Statement: What is the calculation sequence for an extension?
|
Solution: When a change is made to a variable which affects the extension, HYSYS performs a Forgetting pass and two Calculation passes.
The Forgetting pass is used to identify the streams, unit operations, etc. affected by the change.
The first Calculation pass is used to allow the extension to complete its internal calculations.
The second Calculation pass is made so that external references made by the extension use correct values. If the extension makes no external references, then the second pass can be bypassed using the SolveComplete method of the Container object.
See alsoSolution #109156 and #109157
Keywords: calculation sequence, extension, forget pass, execute pass
References: None
|
Problem Statement: When I change values in HYSYS via Excel VBA it takes a long time to solve and I get the message Microsoft Excel is waiting for another application to complete an OLE Action. Is there a way around this?
|
Solution: Each time VBA is used to make a change in HYSYS, code execution pauses on the line that caused the change until HYSYS has finished solving. Sometimes when HYSYS takes a long time to solve, Excel displays a modal message box like Microsoft Excel is waiting for another application to complete an OLE Action, and this must be OK'd before code execution will continue.
It is possible to automatically answer OK to this message ...
The Excel Application object has a property called .DisplayAlerts. Setting this to False means that Excel automatically chooses the default response. If you set this property to False, Microsoft Excel doesn't automatically set it back to True when your macro stops running. Your macro should always set the property back to True when it is complete
[This property can also be used to suppress any other Excel messages - for example those that pop up when you delete a worksheet or close a spreadsheet.]
For example:
Application.DisplayAlerts = False
'... Make changes that cause HYSYS to solve
Application.DisplayAlerts = True
If multiple changes are being made to HYSYS using VB it is worth switching off the HYSYS solver (using [Case Object].Solver.CanSolve = False), making all the changes, and then switching the solver back on again. This prevents the solver from starting after each individual change is made.
Keywords: Excel, waiting, application, OLE action, Solver, CanSolve
References: None
|
Problem Statement: 같은 압력곡선분포도를 임의의 유체에 사용할 수 있을가요?
Please refer to the English
|
Solution: 131672 and ChineseSolution 132708.Solution
펌프나 압축기의 압력곡선에서의 압력은 유체와 관련되어 있다. 일반적으로 공급상은 펌프의 압력곡선정보를 제공한다. 사용자는 같은 곡선을 임의의 유체에 사용할 수 있다. 다만 출구의 압력은 유체에 따라 틀리게 된다. 왜냐하면 밀도가 틀리기 때문이다.
Keywords: pump curve, compressor curve, head, water, process fluid.
References: None
|
Problem Statement: How to apply the Aspen Dynamic Pipeline Solver to sub-sea pipeline modeling.
|
Solution: Aspen Dynamic Pipeline Solver is incorporated into the Aspen HYSYS Upstream option in Dynamics (Aspen Hydraulics flowsheet).
Kindly refer toSolution 128977 - Example of an Aspen Hydraulics dynamic simulation of a long sub-sea pipeline.
Keywords: Aspen Dynamic Pipeline Solver, HYSYS Upstream, Aspen Hydraulics
References: None
|
Problem Statement: How do you specify vapur fraction on mass basis?
|
Solution: The vapour fraction of material streams in Hysys by default is molar basis. Mass vapour fraction of a stream is a calculated value which can be added from Property Correlation Controls (or Correlation Manager) | Standard | Phase Fraction [Mass Basis]. This value cannot be modified directly by the user.
However, if the mass vapour fraction is required, the user can implement this using an Adjust operation. In such case, the Adjusted Variable is the molar vapour fraction and the Target Variable is the mass vapour fraction of the same stream. It may be necessary to reduce the Tolerance or change the step size/Maximum Iterations in the parameters page of the Adjust function. .
The mass vapour fraction as a Target Value can also be applied in a Case Study to automatically generate flash results for a number of scenarios.
Please find the example file in the attachment.
Keywords: Mass Vapour Fraction
References: None
|
Problem Statement: What is required to use Infochem Multiflash feature in Aspen HYSYS Upstream?
|
Solution: The following items are required for using Infochem Multiflash feature in Aspen HYSYS Upstream.
Aspen HYSYS V7.3 (or later) with Aspen HYSYS Upstream license key obtained from Aspen tech. The following license keys can be used: SLM_RN_PML_HYSUPSTRM and SLM_RN_PML_HYSUPSTRM_R3
Multiflash version 4.0 (or later) with license key obtained from Infochem
When installing Multiflash, the ?HYSYS upstream support? option must be selected such that the appropriate interface software and registry keys are installed/created.
Keywords: Upstream, Infochem Multiflash, HYSYS, HYSYS Upstream
References: None
|
Problem Statement: When I enter the Design Phase, HYSYS freezes on me. What can I do?
|
Solution: When running Win 98, with an expired set of license files from ASPEN (the Icarus.fil and System.ver files), HYSYS will freeze. The only way to leave HYSYS is to use Ctrl-Alt-Delete and end the HYSYS task.
In order to avoid this problem in the first place, do not enter the Design Phase unless your license files are current.
This does not happen with Win NT. In Win NT, a message box will pop up advising you that the files are expired.
Keywords: Freeze, Economix, Design Phase
References: None
|
Problem Statement: What are the different Hydrate Types predicted in Hydrate Formation Utility?
|
Solution: The only requirement for hydrate formation is that some water must be present in either the vapor or condensed hydrocarbon phase with hydrate forming components. Once favorable pressure and temperature conditions are reached (high pressures or low temperatures), the mixture of hydrate-forming molecules and water molecules form a non-stoichiometric solid phase.
These conditions can be well above the freezing point of water, or well before the point where free water or ice would drop out.
The three types of hydrates formed are known as Type I, Type II, and Type H.
The hydrate formers are limited to molecules that are small enough to fit into the cavities formed by the host water lattice structure. A single hydrate former is required for the Types I and II. These hydrate formers typically include:
low molecular weight paraffinic hydrocarbons up to n-butane (methane, ethane, propane, n-butane, i-butane)
some olefins (ethylene, propylene)
some of the smaller non-hydrocarbon components such as carbon dioxide, nitrogen, oxygen, argon, and hydrogen sulfide
In contrast to the Types I and II, the Type H hydrate requires two kinds of molecules in its formation:
a small Structure H former
methane
nitrogen
xenon
a large Structure H former
isopentane
neohexane
2,3-dimethylbutane
2,2,3-trimethylbutane
2,2-dimethylpentane
3,3-dimethylpentane
2,3-dimethyl-1-butene
3,3-dimethyl-1-butene
cyclooctane
cycloheptane
methylcyclopentane
ethylcyclopentane
methylcyclohexane
cis-1,2-dimethylcyclohexane
1,1-dimethylcyclohexane
ethylcyclohexane
cis-cyclooctene
cycloheptene
Therefore, to obtain the Type H prediction, the given stream must consist of at least one small Structure H former and at least one large Structure H former.
Keywords: Type I, Type II, Type H, Hydrate, Utility.
References: None
|
Problem Statement: Does the PR sour package allow computation of the H2s, NH3 solubility in the hydrocarbon phases?
|
Solution: The answer is yes. Actually H2S and NH3 solubility in hydrocarbon phases is taken care of by the PR equation of state. The word Sour comes from the Wilson's Sour API model that characterizes the ionization of H2S and NH3 in the aqueous phase. The PR Sour or SRK Sour models are specialized in representing sour water systems. They use Wilson's model to account for the ionization of H2S, and NH3 in the aqueous phase and therefore provide a better prediction of the solubility of these components in the water phase. They may be applied to sour water strippers, hydrotreater loops, crude columns, or any process containing hydrocarbons, acid gases and H2O. If no water phase exists the Sour model will be reduced to the ordinary PR or SRK model. More details of the model are available in the original API publication 955 titled A new correlation of NH3, CO2, and H2S volatility data from aqueous sour water systems
Keywords: HYSYS, Sour PR, H2S, NH3, Solubility
References: None
|
Problem Statement: What does the Relative Internal Flow tolerance for the recycle operation mean?
|
Solution: For the recycle the Actual Tolerance is calculated as follows:
Actual Tolerance = Relative Tolerance (specified by user) * Internal Tolerance (fixed)
This gives the permissible tolerance, in HYSYS internal units (C, kPa, flow per second ....) for each variable.
The table in Section 12.7.3 (Page 12-154) of the HYSYS Operations Guide mentions that the internal flow tolerance of the recycle is relative.
For all the other parameters the internal tolerance is absolute. So, taking the example of temperature, multiplying the default relative tolerance of 10 by the set absolute internal tolerance of 0.01degC gives an actual tolerance of 0.1degC. This means that the temperature of the Recycle's outlet stream must be within 0.1degC (0.18degF) of the temperature of the Recycle's inlet stream in order for the operation to be solved.
For flow rate the internal tolerance quoted in the table is relative. The absolute tolerance is calculated by multiplying the flow rate in internal units (kgmole/s) by the factor 0.001. For example with a flow rate of 100 kgmole/s and the standard multiplier of 10 the actual tolerance is calculated as follows.
Actual Tolerance = Relative Tolerance * Absolute Tolerance
= Relative Tolerance 0.001 Flow rate in kgmole/s
= 10 0.001 100 = 1 kgmole/s
Hence the flow will be solved if it is within 99 - 101 kgmole/s.
Keywords: Recycle, Tolerance, Flow, Relative
References: None
|
Problem Statement: How can I make HYSYS automatically generate a material balance?
|
Solution: In HYSYS 3.0.1, a Property Balance utility was added. One of the uses of this tool is to automatically generate a mass balance. Follow these steps to set it up:
Go to Tools | Utilities and select Property Balance Utility.
Press the Add Utility button.
Press Scope Objects.
In the Object Filter box (located in the bottom left hand corner), select FlowSheet Wide.
A FlowSheet Wide box will appear. In this box, select FlowSheet Wide
Press the >>>>>> button to add this to the scope.
Press the Accept List button located in the bottom right hand corner.
Now it is time to select the variables to be displayed.
Press the Insert Variable button on the right hand side of the Property Balance Utility view.
Select variables as required. (i.e.: Mass Flow to view the mass flow of all inlet and outlet streams or Comp Mass Flow to view the mass flow of an individual component)
Select Balance Results to view the material balance table.
To export the table for use in another application, select Print from the File menu and choose Text to File. This will save the table to a *.txt file in comma delimited format.
Keywords: material balance; property balance
References: None
|
Problem Statement: How does the HYSYS heat exchanger work when linked with the Exchanger Design and Rating (EDR) software?
|
Solution: The HYSYS heat exchanger can be linked with the EDR for rigorous heat transfer calculations. When the EDR is linked with the HYSYS heat exchanger then this always runs in simulation mode in HYSYS. In this mode the outlet temperatures and pressure drops both in tube and shell sides are calculated.
Before linking the HYSYS exchanger with the EDR make sure that the inlet conditions in the HYSYS heat exchanger is solved (either calculated by equipment connected with the inlet stream or data specified manually).
In the latest HYSYS version (V8.0 and higher), it is possible to preform the design and rating calculations within the HYSYS heat exchanger or via the utility named Shell&Tube Exchanger Design/Rating. After completing the design, the geometry can be transferred to the linked exchanger. The exchanger will then run in simulation mode.
Keywords: Exchanger Design and Rating (EDR), Simulation Mode
References: None
|
Problem Statement: Why does the cold property utility give different result than HYSYS Reid VP @ 37.8 C?
|
Solution: The reason why cold property utility gives different result than HYSYS Reid VP @ 37.8 C is that ASTM D323-73/79 (Cold Property RVP) is wet basis where as HYSYS stream apply RVP on dry basis. If you set water composition 0.0, both cold property utility and HYSYS RVP should give the similar results. The two methods can still give slightly different results because they use different flash algorithms.
The above has been documented in the user guide AspenHYSYSV7_1-Usr.pdf page 444.
Keywords: RVP, Cold Properties Utilities, ASTM D323-73/79
References: None
|
Problem Statement: How can I input an assay distillation curve derived from the IP480 method?
|
Solution: Aspen HYSYS currently has no direct IP480 to TBP inter-conversion method available.
According to the open literature on web - http://www.astm.org/Standards/D7500.htm:
ASTM D7500-08 method has been developed through the harmonization of two test methods, Test Method D6352 and IP 480. As both of these methods cover the same scope and include very similar operating conditions, it was agreed that a single standard method would benefit the global simulated distillation community.
Developments in the past had recommended to enter ASTM D6352 (which does not have a direct inter-conversion method as well) as TBP by mass in HYSYS . Users hence should be able to enter IP480 data using TBP by mass in HYSYS.
Keywords: IP480, ASTM D635, TBP, Assay
References: None
|
Problem Statement: How can you dipslay the Hydrate formation Information in a table format on the HYSYS PFD?
|
Solution: In-order to display the Hydrate formation utility information on a HYSYS PFD table you can use a spreadsheet as an intermediary operation. The steps are as follows:
1. Add a spreadsheet to your PFD.
2. Open the spreadsheet and click on Add Import.
3. In the window that pops up, hit the radio button for 'Utility', and choose the Utility you desire (you must have one installed).
4. In the Variable column, choose the variable you wish to see. (e.g for Hydrates, either the Hydrate Formation T or P), and choose OK.
5. In the main spreadsheet properties window ('Connections' tab) , you will see that the variable is now in Cell A1 on the spreadsheet. If it is not, please change the cell by typing A1 in the box.
6. Switch to the spreadsheet tab, and click in Cell A2. Enter +A1, hit enter.
7. Close the spreadsheet window, and right click on the spreadsheet, and choose Show Table.
8. Go to your PFD, and right click on the table that was just made, and select view properties.
9. Click on Add variable, and in the window that pops up, scroll and find the variable A2:Click on this and hit OK.
10. Close the table properties window. A table on the PFD now shows the utility information you desire (e.g. for hydrates, hydrate temperature). This will update automatically as you update your simulation.
Keywords: Hydrate Utility, PFD table, Spreadsheet
References: None
|
Problem Statement: How can I tell if a user property is a cloned correlation?
|
Solution: A user property will appear under User tree under available correlations. User property may be a clone of another correlation. To tell it is clone of which property:
A? Go to Tools|Correlation manager.
A? Expand User tree under available correlations.
A? Highlight the correlation of interest.
A? Look under Correlation Name. This will tell the name of correlation from which this property has been cloned.
Keywords:
References: None
|
Problem Statement: How do I configure Aspen HYSYS Stream Reporter to display results for the lower heating value (LHV)?
|
Solution: When trying to report stream results from Aspen HYSYS into Excel using Aspen HYSYS Stream Reporter (HSR) it is important to ensure that the variables desired are properly defined in the HSR set-up page before they are written to the output page in Excel in order for results to be displayed correctly.
If attempting to display results for the LHV variable and you get an error message indicating that the results can?t be displayed, and you have already implementedSolutions 110050 and 131670 but the error message still persists, make sure you have the correct Phase selected.
In the Properties to report section of HSR setup page, Phase column drop down menu, select Correlation and in the Property column type in Gas\LHV Vol. Basis, then select Write Table. This will ensure that the values for the Gas LHV correlation (Vol. Basis) are displayed among your results. This workflow is applicable for other stream correlations and properties.
Keywords: HYSYS Stream Reporter, HSR,
References: None
|
Problem Statement: How do I convert a file from the new version of Aspen HYSYS into an older version?
|
Solution: Open the HYSYS file, then save it as .xml file. Open the recently created .xml file into the older version of Aspen HYSYS. Save it as an .hsc file.
The simulation will have to be run again and all the operations will need to converge again.
Please note that if the file from the recent version contains an operation that's not available on the older version, you will need to delete them from the file in order to convert it.
Keywords: HYSYS case, simulation, conversion, version, old, new, .xml, .hsc, backwards compatibility
References: None
|
Problem Statement: How do I display specific volume of a stream?
|
Solution: HYSYS only shows molar volume in the standard property list. To obtain the specific volume you can do the calculation in a HYSYS spreadsheet either using formula
Specific volume = Molar volume/MW OR
Specific volume=1/Mass density.
After that you can display it on PFD.
Keywords: None
References: None
|
Problem Statement: What is Improved in Aspen HYSYS V7.3 - HYSYS Spreadsheet Tables
|
Solution: Tables in the HYSYS Spreadsheet unit operation model are now customizable. The addition and deletion of columns and rows in an existing spreadsheet is now supported.
This new capability mimics the functionality in Excel spreadsheets, providing improved usability within the HYSYS Spreadsheet unit operation model.
Keywords: None
References: None
|
Problem Statement: When user imported the Depressuring utility from very older version into later HYSYS versions, depressuring utility fails to provide results
|
Solution: It is due to selected flash method in the Basis Manager. If user switch to the HYSYS flash (go to the Basis Manager, view the Fluid Package and on the StabTest page choose Low for the Method in Stability Test Parameters), then the case runs OK. The HYSIM flash is not recommended for dynamics because it is slow and not as reliable as the HYSYS flash.
But if user still see the error shown below then follow the following steps,
1. When the feeder block pops up, select the temperature radio button.
2. Press the Export Conditions to Stream button.
3. Close the feeder block window.
4. Run the depressuring utility again - it should run fine now.
Keywords: Dynamic Depressuring, Flash Failure
References: None
|
Problem Statement: Can I read a previously saved MASSBAL .dat file to be solved using the HYSYS MASSBAL subflowsheet?
|
Solution: Users have the option to read in previously created cases.
When this choice is selected, a DAT file must be provided, accomplished by the Open Model button that will prompt the user for a DAT file. Note that the Sub-Flowsheet Environment button is grayed out when this option is selected. This is because the user is not allowed to modify the cases within the HYSYS interface. Likewise, the specifications and degrees of freedom on the Parameters will be of no use either. Results from MASSBAL are populated on the Results page.
Keywords: MASSBAL .dat file import
References: None
|
Problem Statement: What is Improved in Aspen HYSYS ? Pipeline Hydraulics Modeling
|
Solution: The V7.3 release contained many new improvements for the modeling of pipeline hydraulics, including substantial improvements inSolution speed for steady-state flow networks, support of flexible boundary conditions, and new flexibility to model shut-in branches of a flow network. More information can be found on these improvements inSolution 131579
Cumulative Patch #1 (CP1) of V7.3 includes additional improvements that extend the capabilities for pipeline modeling.
Flow Assurance Calculations in Aspen HYSYS Pipe Segment Model and the Aspen Hydraulics Pipe and Complex Pipe Models
The pipe segment model in HYSYS and the pipe and complex pipe models in Aspen Hydraulics can now check for a variety of potential flow assurance issues.
These new features can be found on the new Flow Assurance tab within the pipe models.
A separate page is devoted to checking each of the following potential flow impediments:
CO2 Corrosion ? The presence of CO2 in a hydrocarbon pipeline can cause an undesirable deterioration of the pipe wall, and may ultimately lead to a catastrophic failure of the pipe. It is therefore necessary to predict the pipe wall corrosion rate caused by the presence of CO2 in a hydrocarbon pipeline.
The corrosion rate for a set of conditions can only be estimated by correlations. V7.3 CP1 includes three CO2 corrosion correlations:
NORSOK Standard M-506 correlation developed with the support of the Norwegian Oil Industry Association (OLF) and the Federation of Norwegian Manufacturing Industries (TBL). More details on the correlation can be found in attached NORSOK_M-506.pdf document.
de Waard Model 1995 correlation
de Waard Model 1991 correlation
The prediction of the CO2 corrosion rate is supported in both the pipe models in Aspen Hydraulics and the HYSYS pipe segment model.
Erosion ? In multiphase flow through pipelines, the continuous impact of particles (liquids or solids) on the pipe wall surface can cause potential erosion problems. It is therefore imperative that erosion effects are considered when sizing and designing pipelines.
The maximum fluid velocity in a pipeline to prevent erosion is given by:
Vmax = C * (ρm) -0.5
Where ρm is the mixture density and C is an empirical constant based on the correlation chosen. Correlations supported in V7.3 CP1 include:
API-RP-14E Report ? suggests a value of C=100 for solid free corrosive and continuous flow, and C=125 for noncontinuous flow
Salama & Venkatesh (1983) ? suggests a value of C=300
The prediction of the erosion rate is supported in both the pipe models in Aspen Hydraulics and the HYSYS pipe segment model.
Hydrates ? The formation of hydrates in a pipeline can have a severe impact on the flow characteristics through the line, reducing the capacity of the pipeline or significantly increasing the pressure drop.
V7.3 CP1 introduces the ability to predict hydrate formation throughout the pipeline, using the same capabilities that have been available within the HYSYS Hydrate Prediction Utility for streams. The prediction of the hydrate formation is supported in both the pipe models in Aspen Hydraulics and the HYSYS pipe segment model.
Slug Analysis ? Pipelines transporting multiphase fluids (vapor and one or more liquid phases) can experience slugging behavior, especially when the pipeline?s elevation varies significantly over its length. Under certain conditions, slugs of liquid can form in predicts slug properties for horizontal and inclined two-phase flows in each pipe segment.
In V7.3 CP1, the slug analysis functionality available in previous versions in the HYSYS pipe segment model is now found under the Flow Assurance tab. The form has been redesigned to provide both the slug analysis tool options and results on a single form.
Wax Deposition ? Wax deposits can form on pipeline wall surfaces, restricting the flowrate and increasing the pressure drop through the pipeline.
In V7.3 CP1, the wax deposition functionality available in previous versions in the HYSYS pipe segment model is now found under the Flow Assurance tab. The form has been redesigned to provide both the wax deposition input options and results on a single form.
Each Flow Assurance calculation page lets you produce results in table form or, if applicable, in a plot profile. Standard HYSYS viewing and printing controls apply.
Keywords: None
References: None
|
Problem Statement: If I have a model that was developed in a language environment other than English, how can I display Aspen PIMS
|
Solution: s with the text in that language even though I am using an English Windows Operating System?
Solution
You need to make sure that you have the proper language and code pages selected from the Regional & Language Options dialog in the Windows control panel.
The following steps are for Windows XP.
1. Under CONTROL PANEL, Regional and Language Options, select the language you desire.
2. From Advanced tab, under 'Language for non-unicode programs', select the same language you chose from the previous step. Click OK to exit the settings and then restart your PC.
For Windows 7, the 'Regional & Language Options' dialog is a little different and the steps are below:
1. In the Regional and Language dialog from the control panel, select the proper language in the Format tab for the format. Click Apply.
2. Click the Administrative tab. Click the 'Change system locale...' button and select the proper language. Then restart your PC.
If the text in the Aspen PIMS reports still does not show the choosen language, do the following:
a) In PIMS, from Tools menu. Select Program Options | Report tab. Click the Screen Font button. In the Script dropdown text box, select that particular language.
b) If you want to print the report, you have to make the same selection after clicking the Printer Font button.
Keywords: display
language
text
regional
region
References: None
|
Problem Statement: I have verified that SLM Configuration Wizard settings on my machine are correct, but Aspen PIMS won't start and says it cannot find my license file.
|
Solution: Typical SLM configuration problems are reviewed inSolution 127067.
If you are sure the configuration is correct, there are a couple other items that should be checked. The SLM Configuration Wizard settings can be overriden by certain environment variables or an LSHOST file. Check for these by using the steps below:
1) Check for environment variables that may override the SLM settings
a) Go to Control Panel | System | Advanced
b) Click on Environment Variables
c) In the bottom section, check for an environment variable named LSHOST or LSFORCEHOST. If you have one of these variables, it forces the SLM to look for licenses only in the location specified in the variable value.
d) If such an environment variable exists, it may have been put there by a non-Aspentech product. If it appears the environment variable is pointing to a valid location as required by a non-Aspentech product, then add the license location for PIMS to the environment variable value. If the environment variable is not required for a non-Aspentech product, then it can be renamed or removed.
2) Check for a file called LSHOST (file has no extension) in the PIMS installation directory. The default installation directory is C:\Programs Files\Aspentech\Aspen PIMS. If such a file exists then the contents of the file will determine where SLM checks for the PIMS license. When this file is removed, the SLM settings in SLM Configuration Wizard will again be obeyed.
Keywords: license
LSHOST
References: None
|
Problem Statement: When a utility defined as in both BUY and SELL table, what cost/price is used in 'Utilities Used/Produced' section in submodel report?
|
Solution: Starting with version V7.2, a new logic was implemented in Aspen PIMS TXT and HTML reporting. The logic is
1. if the utility is considered a feed or consumed, then the cost or purchase price is used.
2. if the utility is NOT a feed or produced, then the selling price is used.
The exception is when the utility is being consumed in a submodel but does not exist in the UTILBUY table then the price in the UTILSEL table is used in the report. Vice versa for the other scenario where the utility is being produced but the utility does not exist in the UTILSEL table, then the cost in the UTILBUY is used in the report.
Keywords: report, utilities, utility, cost, price, consumption, used, produce, UTILBUY, UTILSELL
References: None
|
Problem Statement: What is a ratio controller?
|
Solution: The Ratio Controller is a special type of Feed Forward controller that maintains the ratio between two process variables. The Ratio Controller takes two inputs with the desired ratio as the SP and calculates an OP. Prior to HYSYS 3.0, this was done using a Spreadsheet Operation. A ratio controller operation was added in HYSYS 3.0.
A classic example of a use for a Ratio Controller is to maintain a desired fuel to air ratio for a furnace
Keywords: ratio; controller
References: None
|
Problem Statement: I'm using the new HTFS-Engines option, within HYSYS. What type of calculation mode is the new TASC interface using? Is it Checking, Simulation or Design?
|
Solution: The new HTFS-Engines option, within HYSYS, was implemented using Simulation. Using the given stream inlet conditions, the Simulation calculation mode is used to determine the heat load, pressure change and stream outlet conditions that will occur with the exchanger you specify.
If you need the Design or Checking calculation modes you can do that with the TASC User Interface via the <Export> facility.
Keywords: HTFS Engines, HYSYS-TASC link, mode, simulation, checking
Creation Date: 18-Mar-2003 08:25AM
References: None
|
Problem Statement: When opening Aspen Properties Database Manager, the error message Snap-in Failed to initialize or
Snap-in Creation failed occurs (See attached error message for detail).
|
Solution: 1. Go to Control Panel | Add/Remove Programs
2. Un-install the Microsoft SQL Server 2005 including the other SQL Components, and then reboot the system.
3. Install the attached SQLEXPRS32.exe from thisSolution.
4. Select the default option, select Mixed Mode Authentication and enter Aspen100 or any password. Select default options for the rest of the installation.
5. Run HYSYS to confirm the error message no longer occurs.
6. Run the Aspen Properties Database Configuration Tester to check if the databases have successfully connected.
(Start | Programs | AspenTech | Process Modeling | Aspen Properties | Aspen Properties Database Configuration)
Keywords: Snap-in, Microsoft SQL Server 2005, HYSYS v7.2, and APED
References: None
|
Problem Statement: I am interested to know how Aspen HYSYS does the extrapolation for the compressor performance curve beyond (or to the right of) the surge limit point in dynamic simulation. Please clarify.
|
Solution: If the “Use Surge Curve� check box in Rating->Flow Limits is checked, the compressor will try to use the surge flow at the given speed as the flow to the compressor, and try to keep the compressor not go under that flow rate. This sometime leads the dynamic solver to non-convergence.
If that check box is not check, the compressor will just use the fitted curve, using above fitting method, to calculate the head based on the flow, without consider the surge point.
Keywords: Compressor Curve, Surge
References: None
|
Problem Statement: How to model a water- acetic acid-hydrocarbon system.
|
Solution: On this issue, acetic-acid water should be handled using a model that includes vapor phase association. In Aspen Plus, UNIQ-HOC or NRTL-HOC should be used, in which Hayden-O’Connell EOS model with Henry’s law is used in the vapor phase. In Aspen HYSYS, you can use NRTL or UNIQUE as fluid package and use virial model in vapour model. Even at very low concentration, the effect is probably not negligible. But if user needs to use an EOS for both vapor and liquid in his process, then there is no way to account for the association of acetic-acid and he has to ignore its affect. User has to estimate the binary parameters by himself.
Keywords: Property package, Acetic acid, polar components, activity model
References: None
|
Problem Statement: What does the error message Error 2: A Hyprotech network security key was found that has an invalid serial number. No licenses were available on other valid Hyprotech network security... mean?
|
Solution: All error messages are explained in detail in the trouble shooting section of the HYSYS Get Started manual, which can be found in PDF format on your HYSYS product CD.
When a network version of HYSYS starts up, it sends out a broadcast message, looking for a network key of a certain key code sitting somewhere on the parallel port somewhere on a networked computer. This error message is telling you that HYSYS found the key but that all the licenses for that key are in use. It also tells you that it found at least one other key but this key does not have the correct key code. Then it tells you that you can run one of the key monitoring tools to find more information. WINMON is a good tool. If you run it on any computer on the network, it will look for all NetSentinel keys and report which ones have been found. It can also report back the IP addresses of users who are taking up the licenses for a specific key. WINMON.EXE can be downloaded off the NetSentinel website at http://www.rainbow.com/tech/download.html under NetSentinel-C. A Word document that contains instructions on how to run it will be part of the download.
If you are concerned that HYSYS is always looking for the wrong key, you can set up a HYSYS.INI file stating the IP address of the computer that the key is sitting on. This will direct HYSYS to only that computer. The HYSYS.INI file is a text file with the following two lines of text. Note the brackets and lack of spaces. Place the IP address of your keyserver computer where it says 192.139...
[RainbowKey]
[BroadcastAddress]=192.139...
If HYSYS is still finding the wrong network key even though you have written a HYSYS.INI, then you should be using Department names. Refer to the Get Started manual for more information.
Keywords: install, error 2 invalid serial number, network installation
References: None
|
Problem Statement: When comparing examples using the Hydrate Formation Utility, what is the difference between the Inhibitor Calculation being Included and Not Included?
|
Solution: KBSolution 128238 provided two examples of how a Hydrate Formation Utility might be used.
In this case, there are two examples:
1. Hydrocarbon.hsc: If you double click on the Utility > Design Tab > Hydrate Formation at Stream Condition > Inhibitor Calculation is marked Included.
2. CO2 rich.hsc: If you double click on the Utility > Design Tab > Hydrate Formation at Stream Condition > Inhibitor Calculation is marked Not Included.
The difference between the two is determined by the composition of each stream.
Example: Hydrocarbon.hsc:
In this case, the composition of stream 3 is the following:
In this case, it is a stream that results in the presence of a free aqueous phase after an equilibrium flash (in other words, Aqueous only, Vapor-Aqueous, Liquid-Aqueous, and Vapor-Liquid-Aqueous, where Liquid refers to a hydrocarbon liquid), so the 3-Phase model is used for hydrate predictions of the Structures I and II.
The 3-Phase model is based on the work of Ng and Robinson 3. The Parrish-Prausnitz algorithm is modified to allow for the prediction of hydrates in aqueous-containing systems. All fluid properties including phase behavior, volumetric behavior, and fugacities are calculated with the selected equation of state (Peng-Robinson or Soave Redlich Kwong). The Kihara parameters for each hydrate-forming component are recalculated based on the work by Ng and Robinson.
This is why the Inhibitor Calculation is marked as Included.
Example CO2 Rich Gas.hsc:
In this case, the composition of stream 3: is the following:
In this case, the calculation mode is set to Assume Free Water. This model is being used because as we can see above, there is no presence of water in the stream. When using this model either the 3-Phase model or the SH model is used for hydrate prediction, but the Inhibitor Calculation is marked as Not Included because the conditions of the stream don't let Aspen HYSYS use either 3 Phase or SH models.
For 3 Phase model, as said above, the stream should result in the presence of a free aqueous phase after an equilibrium flash, which this is not the case.
The SH model is used when two conditions are fulfilled:
The Structure H-forming condition as indicated by available experimental data (namely vapor-Liquid-Aqueous) is obtained from an equilibrium flash calculation.
The given stream contains at least one small Structure H former and at least one large Structure H former.
Neither of these apply, and that is why the Inhibitor Calculation is marked as Not Included.
For more information about the Hydrate Formation Utility, please take a look to the followingSolutions: 109785, 133931, 109332.
Keywords: Hydrate formation utility, inhibitor calculation, included, not included
References: None
|
Problem Statement: Why does my Column Automation code have problems in HYSYS 3?
|
Solution: Columns can no longer be Run while the Solver is switched off.
For example, code like
'Link to HYSYS Objects
Set hyApp = GetObject(, HYSYS.Application)
Set hyCase = hyApp.ActiveDocument
Set hyCol = hyCase.Flowsheet.Operations.Item(T-100)
Set hyColFS = hyCol.ColumnFlowsheet
'Turn Off Solver, Reset Col, Press Run then restart Solver hyCase.Solver.CanSolve = False
hyColFS.Reset
hyColFS.Run
hyCase.Solver.CanSolve = True
Will no longer work. The columns must be Run after the Solver has been switched on. E.g.
'Turn Off Solver, Reset Col, Press Run then restart Solver hyCase.Solver.CanSolve = False
hyColFS.Reset
hyCase.Solver.CanSolve = True
hyColFS.Run
Keywords: OLE Automation, Column, Reset, Run, Solver.CanSolve
References: None
|
Problem Statement: How to interpret the hydrate curve calculated in Envelope utility for a stream with no water?
|
Solution: For the hydrates to form, the stream must contain at least few molecules of water, if the stream in question has no water then one can understand that no hydrates will form. For a stream that has no water, if one calculates the hydrate curve using the Envelope Utility, then it should treated carefully, in other words if one wonder what is meaning of Hydrate curve calculated by Envelope utility then it should be treated as a conservative result for the given stream. Since the curve is calculated assuming a free water phase in the stream (Assume Free water method).
When using the Assume Free Water method, the stream in question is internally saturated with water to the extent there is a free water phase in the system and for this scenario the hydrate curve will be estimated.
Attached file can be opened with HYSYS V7.1 and higher versions and you can see the calculated Hydrate curve is similar for both streams without water and with free water phase.
Keywords: Envelope, Hydrate, Free Water
References: None
|
Problem Statement: In MASSBAL, you could define streams as Chemical, VLE, Fluid, Food, or Pulp. What stream definition is supported in the MASSBAL subflowsheet in HYSYS?
|
Solution: MASSBAL has many different possible stream definitions (e.g. Chemical, VLE, Fluid, Food, Pulp). However, the only one used in HYSYS will be the VLE stream type. Thus, in order for MASSBAL to use HYSYS to perform its thermodynamic calculations, callback functions have been set up. We have callback functions to deal with flashes, property calculations of individual components and streams.
Keywords: MASSBAL, stream definition, VLE
References: None
|
Problem Statement: Why do old Dynamic Depressuring utility cases return different results when loaded in Aspen HYSYS V7.3 CP1 (or newer)?
|
Solution: Some changes have been implemented in Aspen HYSYS V7.3 with CP1 and within the Aspen HYSYS dynamic depressuring utility. When the inlet stream is pure vapor (V/F =1), the liquid level will not be allowed to be specified and will be defaulted to zero.
In earlier versions, Aspen HYSYS allowed the specification of the liquid level even if the inlet stream had a vapor fraction of 1. Now, for consistency purposes, this cannot happen since the attached feed stream defines the entire vessel initial conditions previous to blowdown. As a result, the liquid level is now assigned as 0. This may generate different results with respect to older Aspen HYSYS versions.
In the case of a feed stream at supercritical conditions, the inlet stream's vapor fraction displayed may be 1. The liquid level would then be defaulted to zero.
However, when dealing with feed streams at supercritical conditions, if the user wants a vessel full of liquid instead, manipulating the Dense Phase Tuning factor is an option.
Keywords: Dynamic depressuring utility, pure vapor, liquid level
References: None
|
Problem Statement: How do I tell HYSYS to use the steam tables property package (NBS or ASME) when I have other components besides water in my case?
|
Solution: The heat exchanger operation allows the shell and tube sides to be solved using 2 different property packages. To tell the shell side to use NBS (or ASME), you must create two Fluid Packages and a sub-flowsheet and in the Basis Environment associate the subflowsheet to use the steam table property package.
Steps to create such a case from scratch:
In the Basis Environment, create a Fluid package for your Main Case. We'll assume Peng Robinson and the HYSYS default name Basis-1. Add your components.
Create a Fluid Package using NBS or ASME and add water as the component. We'll call this Basis-2.
Go to the Simulation Environment and add a Flowsheet to your case. Choose the Start with Blank Flowsheet option. Close the window.
Go back to the Basis Environment and on the Simulation Basis Manager Window, Fluid Packages tab, use the drop down menu and associate Flow-1(your subflowsheet) to use Basis-2.
Go back to the simulation environment and add a heat exchanger to your case.
On the Design Connections page, use the dropdown menu under Shell side Flowsheet and choose Flow-1. Close the window.
Go into the subflowsheet (double click on it) and press the Enter SubFlowsheet button.
Create your steam streams in the subflowsheet. One for the Shell feed stream, one for the shell product stream. You only have to specify the composition of one stream. Set the conditions (T and P) if you know them.
Go back to the Main environment (press the arrow icon at the top of the window to exit to Main).
On the design connections page, use the drop down menu's to choose the shell in and shell out streams.
Keywords: subflowsheet, heat exchanger, steam tables, ASME, NBS, components, two fluid packages
References: None
|
Problem Statement: How does Aspen HYSYS depressuring perform with respect to the experiment and the BLOWDOWN simulator?
|
Solution: The Aspen HYSYS Depressuring Utility predictions are validated against experimental data reported in the literature for three experiments originally intended to test the capabilities of the BLOWDOWN? simulator [1]. The experiments were carried out in an order that reflects an increasing degree of difficulty: the first and simplest one simulates a gas phase, pure component case; the second one a three component case with extremely small amount of liquid condensing during the experiment; the third one is the most challenging, since it is in supercritical conditions at initial time and large amounts of liquid undergo condensation.
After recent improvements (the Dense Phase Tuning factor) only available in version V7.2 and on or in version V7.3 (the Venkatarathnam-Oellrich method), it becomes clear that the depressuring utility in Aspen HYSYS successfully predicts the experimental results.
The detailed discussion is in the attached folder ?Depressuring Validation? with test cases that reproduce the experimental setups. This document also emphasizes the need of small recycle efficiencies in the simulation of blowdown vessels and gives suggestions on how to assess the simulation results when very small liquid accumulations result.
Keywords: HYSYS Dynamics, depressuring utility, recycle efficiency, dense phase tuning factor, phase identification
References: s
[1] Haque, M.A., Richardson, S.M., Saville, G., Chamberlain, G., and Shirvill, L., Blowdown of Pressure Vessels, II. Experimental Validation of Computer Model and Case Studies, Trans I. Chem. E., Vol. 70, Part B, February 1992, pp. 10-17
|
Problem Statement: What are the definitions of the pressure types for the Aspen HYSYS Dynamics PSV valve?
|
Solution: Set pressure is when valve starts to open. The inlet static pressure rises above the set pressure of the safety valve, the disc will begin to lift its seat. let say the set pressure is 10 bars. If the inlet pressure is higher than 10 bars then the valve starts to open.
Full open pressure is when the valve is fully opened. The allowable overpressure depends on the standards being followed and the particular application. For compressible fluid, this is normally between 3% and 10%, and for liquids between 10% and 25%. It could be Full Open Pressure = (100+x)*Set pressure.
Closing pressure is when the valve starts to close. Once normal operating conditions have been restored, the valve is required to close again. The closing pressure is slightly lower than set pressure. For example, 9.8 bars if set pressure is 10 bars.
Reseating pressure is when the valve is fully closed. It is usually specified as a percentage of the set pressure as well. For compressible fluids, the blowdown is usually less than 10%, and for liquids, it can be up to 20%.
Figure 1. Relationship between pressure and lift for a typical safety valve (from spiraxsarco.com)
Keywords: Set pressure, Full open pressure, Reseating pressure, closing pressure
References: None
|
Problem Statement: What is the Standard option for Peng Robinson?
|
Solution: The PR model traditionally incorporated in HYSIM and in HYSYS has been enhanced by Hyprotech. In other words, it is different from the Peng-Robinson equation in the original publication.
Beginning with HYSYS 2.3, it is possible to use the original form of the Peng-Robinson equation of state.
This feature can be accessed in the Basis Environment, on the Prop Pkg tab of the Fluid Package manager view. When the Standard radio button is checked, the original form of Peng-Robinson equation of state will be used. The default selection for the PR package would be HYSYS PR, the enhanced model.
Keywords: original Peng Robinson, PR, literature
References: None
|
Problem Statement: Before HYSYS 3.0, there used to be an edit box at the top of each property view. Where has it gone?
|
Solution: The entry box at the top of the view is gone and has been replaced with edit-in-place functionality.
However, the ability to edit only a portion of a user specified value has not be removed from HYSYS 3.0.1. A cell can be put in edit mode, by pressing the F2 button. For users unfamiliar with the F2 key, there is also a small Cell Edit button in the left hand side of any user specified fields. Once familiar with the F2 key, users have the option to turn this off in the Preference file.
Please see attached image files.
Keywords: 3.0; edit; cell; typo
References: None
|
Subsets and Splits
No community queries yet
The top public SQL queries from the community will appear here once available.