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Problem Statement: In Case Study with the option to ‘Save Results to File’, the user does not have the option to browse and select a different location to save a file. By default, Case Study Results are saved as Temp files in the directory c:\tmp\results.csv. | Solution: The user can change the location of where the results are saved via the following steps:
1. First of all the file folder must be created prior to running the case study.
2. Then copy and paste the folder path to Case Study / results / Text file name. The Save Results to File checkbox has to be activated to enable paste.
3. Add the name of case study to the path name.
4. Add the extension (.csv) at the end of the path name.
5. Then Run the case study.
The results should be saved in the nominated folder.
Below is an example of a location path name where a case study named casestudyresult1 has been saved.
:\Users\name\Desktop\New folder\casestudyresult1.csv.
Keywords: Save Results to File, Case Study, Text Filename
References: None |
Problem Statement: Does the Aspen HYSYS column handle apparent or true components when Electrolyte NRTL package is selected? | Solution: When Electrolyte NRTL package is selected, a reaction set can be generated using Electrolyte Wizard. However, this reaction set is NOT applied inside the HYSYS column. HYSYS column uses apparent components to perform the separation calculation. In all the connecting streams of the column, HYSYS will flash the apparent components into true components according to the reaction set created before.
If the user would like to model a reactive distillation column, a separate reaction set should be built in the Properties Environment and call the reaction set in Column | Reactions page, as shown below:
Keywords: Eletrolyte NRTL, Apparent Components, True Components
References: None |
Problem Statement: The inventory projection window can be seen in the Planning Board. By default, it shows the inventory projection of the main product that gets produced. This | Solution: explains some of the other projections that can be seen in this window.
Solution
In the Planning Board, there is a contextual ribbon at the top. In the Schedule tab of this ribbon, look at the Inventory Projection panel. Click on the Settings menu in this ribbon.
This menu provides the options to look at the inventory projection of main product, components (i.e. raw materials consumed) and produced materials (i.e. by-products produced).
The following is a screenshot for the product Gamma 10 which consumes Gamma. The Settings chosen were “Main Product” and “Components”.
In the same panel, you also have another menu called Data.
This menu provides options to Show Max (maximum inventory limit), Show Target (target or safety stock inventory level) and Show Min (minimum inventory limit).
The following is a screenshot for the product Gamma 10. The Data options chosen were “Show Max” and “Show Min”.
Keywords: PB
Inventory
Projection
References: None |
Problem Statement: It might be the preference of some users to have different background colors for the Planning Board Gantt Chart, Inventory Projection Plot, the Tiles and the Screen. This | Solution: explains the options to do the same in V8.
Solution
a. To change the background color of the Gantt chart:
Type SSYC in the command window: If you don't find the GANTT entry in the code column of this set, add it in the code column and give it a suitable description.
Type SCOLOR in the command window: Choose the hexadecimal color that you want to have from this set and identify the corresponding code of the color.
Type SYSCOL in the command window: Enter the relevant code into the GANTT row.
b. To change the color of the Inventory Projection Plot, the Tiles and the Screen:
Type SSYC in the command window: If you don't find the GANTT entry in the code column of this set, add it in the code column and give it a suitable description.
Type SCOLOR in the command window: Choose the hexadecimal color that you want to have from this set and identify the corresponding code of the color.
Type SYSCOL in the command window: Enter the relevant code into the GANTT row.
Keywords: None
References: None |
Problem Statement: In the Plant Scheduler Planning Board, there are a set of predefined time slots that the user can use to zoom to specific periods of the horizon.
These time slots are configurable. This | Solution: explains how to configure these time slots.
Solution
The following steps will accomplish this:
1. Go to the Developer tab | Commands Panel | Command line | Type: PBTSLOTS. This would open the control table for this UI property.
2. This table specifies which day of the horizon each of these options are going to have as the starting point and which day is the ending point. A blank in this table means that the number is zero.
3. To add a new option or to delete an existing option, you should go to the row set of this table which can be opened by right clicking on this table and clicking on “Edit Row Set - PBTSLOTR” option.
4. The code column of this set needs to be unique. It can contain alphanumerical with hyphens(-) and underscores(_). The description column is what you are going to see in the dropdown of the Planning Board.
5. To add a new entry simply add a new row by right clicking on the row before which the new row should be placed and selecting the Insert option. To delete an existing entry, select a cell in that row, right click and select Delete option.
6. Once you add a new row, be sure to specify the number of time slots this new options is going to cover (this number is in terms of the time that the planning board simulator uses).
7. There is a third column in this table called “Send to Web PB?” which is used to send the required time slots to the Web Planning Board - Aspen Scheduling Insight Planning Board. This is a separate product in the Chemical Supply Chain Suite of products of AspenTech which is used for sharing the planning board in a website.
Keywords: Time Slots
Planning Board
Predefined
References: None |
Problem Statement: When using a Petroleum Assay, why are the cut point specs defined in a distillation column and the cut point results shown under Petroleum Assay Analysis different?
For instance, in the column, D86 95% is specified but the value reported in the Petroleum Assay Analysis for the Naphtha stream does not match. | Solution: The spec “Column Cut Point is from HYSYS standard (based on Mid Boiling Point) and the Petroleum Assay Stream Analysis is based on Refsys (based on Final Boiling Point).
Please reviewSolution 126930 for more information.
To match Petroleum Assay Stream Analysis results, add specs as “End Point Based Column Cut Point Spec” or “Column Stream Property Spec”.
With “Column Stream Property Spec” it is necessary to click on “Select Property” button in the Spec window, and define the property to be used.
Keywords: Distillation Column, Column Cut Point, Stream Analysis, Petroleum Assay Analysis, Mid Boiling Point, Final Boiling Point basis, End Point Based Column Cut Point Spec, Column Stream Property Spec
References: None |
Problem Statement: By default, in the standard Plant Scheduler CAP(demo) model, when changing the amount of an activity through the activity editor, if the new quantity of the activity is not adhering to the lot size policies, then the amount gets adjusted automatically.
There might be situations where this is undesirable i.e. when you want the user to override the policy. This | Solution: explains how to disable this lot size policy enforcement.
Solution
The following steps will accomplish this:
1. Go to the Developer tab | Commands Panel | Command line | Type: CNTLS.
2. There is a row in this table: (SPLAN) Activity Editor Control Set/Table. The corresponding cell in this table is the control set for the Activity Editor. By default, this is AECTL1.
3. Right click on this text and click on the Edit option. That would open AECTL1 or the respective table.
4. You would find a column called (AEOPRCTL) AE Operations Control Table. The rows of this table represent the different inventory types available in this case file.
5. Right click on the relevant cell and click on Edit. That would open the activity editor configuration table for that inventory type.
6. In this table, you would find an entry called “*QUANC” in the SOURCE column.
7. If you change this entry to *QUAN, then the lot size enforcement would be disabled.
Keywords: Lot Size Policy
Activity Editor
Amount
Quantity
References: None |
Problem Statement: In the Plant Scheduler application, there is a widget to display the Inventory Exceptions. By default, it shows all the products which has inventory exceptions. If you would like to display Exceptions only on specific products, this | Solution: explains how this can be achieved.
Solution
The following steps will accomplish this:
1. Go to the Developer tab | Commands Panel | Command line | Type: FILL PBRBWK(SELMAT_HEATMAP,1) = MANUAL. Close the table that opens up.
2. Go to the Developer tab | Commands Panel | Command line | Type: FORM _GANI = GANI. This command will create a new set called _GANI and will open it up on the screen.
3. Right click on _GANI's contents and click on Set Attributes. Click on the “Save if Modified” checkbox and click OK.
4. Go to the Developer tab | Commands Panel | Command line | Type: PRO. Select and copy (using Ctrl + C) the entries which you want to display in the Exceptions. Close the PRO set.
5. Paste the copied entries in the _GANI set and save the changes by right clicking on hitting Apply. Close the _GANI set.
6. Go to the Developer tab | Commands Panel | Command line | Type: CNTLS. This command is going to open the table called CNTLS (Planning Board Controls). In this table, find a row called “(UAP) Use all PROs for Problems?”. Replace this row's corresponding table entry with _GANI. Close the CNTLS table.
Keywords: Exceptions
Planning Board
References: None |
Problem Statement: This article is intended for readers who implement Aspen Plant Scheduler.
Starting V8, Plant Scheduler’s Planning Board has new features called Inventory Tiles to view the Inventory of various products simultaneously. These Inventory Tiles can be viewed either in a Panel or a Screen.
There might be requirements when you are implementing a Plant Scheduler project, to reset the Inventory Tiles in a Panel or a Screen. The following | Solution: mentions the commands for performing this reset.
Solution
The reset button for the Inventory Tiles Panel or Screen is at the top right hand corner. It is used to re-build the products listed in the Inventory Tiles.
The same action can be programmatically executed through:
MAIN TILES RESET à For resetting the Inventory Tiles Screen
MAIN TILEP RESET à For resetting the Inventory Tiles Panel
These commands can be executed through Rules or Macros.
Keywords: None
References: None |
Problem Statement: When hovering over an activity in the Planning Board, useful activity details can be found. These are called the Activity Tips.
There might be situations when you need to configure the Activity Tips to show additional details to the end user. This | Solution: explains how to configure this.
The prerequisite for reading this document is a basic understanding of configuration in Aspen SCM.
Solution
In the CNTLS table there is a row called “(ATIPSCTL) Activity Tips Control Set/Table” which points to the control table for the Activity Tips. By default, it is ATIPS. This table is dimensioned by Inventory Types - TYI. Each of the Inventory Types can show a different activity tip.
Each of these tables provides details on what would be shown in the Activity Tips for the activities producing that material belonging to the specified Inventory type. This configuration can contain set or table references or keywords.
If it is a set or table reference, the code column should contain “*TEXT”. The description column should contain the set or the table reference.
The following keywords can also be used in the code column. The data format mentioned here should be specified in the description column:
Control Set Code
Description of Output
Data Format
Default Data Format
*BLANK
Number of blank columns
(#)
-2
*CHAN
Internal demand
F#.#
F5.2
*CHANGE
No output
*CODE
Product Code
C#
Code length
*CONSUM
Internal + external demands
F#.#
F5.2
*DESCR
Product description
C#
Desc. length
*DMND
External demand
F#.#
F5.2
*DURATN
Process time
D, F#.#
D
*ELPROC
Elapsed duration
D, F#
D
*ELSETUP
Elapsed setup time
D, F#
D
*ENDA
Actual end time
A, R, T[C|D]
A
*ENDS
Scheduled end time
A, R, T[C|D]
A
*FAC
Facility Code
C#
Code length
*HIER
Hierarchy level
I#
I8
*IND
MAKE index
I#
I8
*INDEX
Plan Report index
I#
I8
*LEAD
Lead time
D, F#.#
F5.2
*LEVEL
Inventory level
F#.#
F5.2
*NEXT
Next line
*PDESCR
Product Description
C#
Desc. length
*PROD
Product Code
C#
Code length
*PSTART
Manufacturing start time
A, R, T
*QUAN
Batch Quantity
F#.#
F5.2
*QUANC
Batch quantity conform to TDAT
F#.#
F5.2
*SETUP
Setup time
D, F#.#
D
*STARTA
Actual start time
A, R, T[C|D]
A
*STARTS
Scheduled start time
A, R, T[C|D]
A
*THRUPT
Production rate
F#.#
F5.2
*YFACTOR
Yield factor
F#.#
F5.2
*YIELD
Yield factor * lot size
F#.#
F5.2
*TEXT
Label
The set of keywords used are exactly the same as the keywords that can be used in the Labeling control tables and the Activity Editor control tables.
Keywords: Activity Tip
Special Keywords
Planning Board
References: None |
Problem Statement: There may be situations where the users would like to change the color of the activity border for the activities on Planning Board. | Solution: You can now specify the color of the activity border by following the steps below:
1. SSYSC is the Rowset of the SYSCOL table.
2. Add a new entry ABORDER to the Rowset SSYSC of the SYSCOL table.
3. Now specify the color number for the ABORDER entry in the SYSCOL table.
The color numbers can be found in SCOLOR set
Note: The default activity border color is light blue.
Keywords: None
References: None |
Problem Statement: When working on the Planning Board you might prefer to change colors of some of the activities. This | Solution: explains how to perform these color changes in V8.
Solution
There might be requirements when you have to change the color of the activities on the Planning Board. There are two ways to change the colors of the activities in V8:
1. Through the Graphical User Interface:
Through the Format tab of the Planning Board contextual ribbon, you will find the “Show Color Legend” button:
When you click on that button, the Key is displayed as below:
Once you double click on the color that you want to change (for any material, in this example), then you would see a bunch of colors to choose from:
When you click on the required color, corresponding material changes to the new color on the Key window. After making the changes for the other materials, you can close the Key window. You will see the changes on the Planning Board for the corresponding materials.
2. Through the Command Window:
If you type in PCOLOR in the command window, you would see a table which has color assignments:
The code displayed in the table is representative of the hexadecimal codes contained within SCOLOR:
If you would like to change the color of a particular material (in this example), you have to choose a hexadecimal color, identify the corresponding code in SCOLOR and mention it in PCOLOR.
Once you have done these changes, you need to open/re-open the Planning Board to see the changes.
Keywords: None
References: None |
Problem Statement: Does Genetic Algorithms move in consideration of shared resource(M SEARCH BOM) in Plant Scheduler? | Solution: In Plant Scheduler Genetic Algorithms(GA) are not to be used with Shared Resources or Precedence Constraints since these algorithms only work on one asset at a time.
Keywords: GA
Genetic Algorithm
M SEARCH GA
References: None |
Problem Statement: What is purpose of the Intermediate Streams in the Hydrocracker reactor or Catalytic Reformer? | Solution: The purpose of the intermediate streams is to connect the outlet of each reactor (for the Catalytic Reformer) or each bed (for the Hydrocracker). You use these streams in the flowsheet for further analysis or simulation, such as quench systems calculation.
Under Design | Connections tab you will find the Intermediate Streams section. In the External column, just type the name of the stream that you want to see displayed on the main (parent) flowsheet. Then the intermediate stream will be placed on the flowsheet.
Please note that these intermediate streams are not typical product streams as they are intermediate streams for the reactors. The products will have greater mass than the inputs when you connect these streams into the Main flowsheet.
Keywords: HCR, CatRef, Intermediate Streams, Product, Hydrocracker
References: None |
Problem Statement: I have assay information in an Excel file. How do I transfer the Excel file to Petroleum Assays? | Solution: The attached case is an example of an Excel file that you can later modify and use it as template. This file contents 5 different crudes in different tabs: Demo 1, Demo 2, Demo 3, Demo 4 and Demo 5. Each crude is different and contents different information. You will have one assay created for each tab with the corresponding fields. This is the format required, the only thing you need to do is fill it within your own information. For that porpoise you can use the Customize tab. Please note that you can change the properties, cuts and pure components . If you want to add a new property that is not added in this example, just type in your Excel file the same property tag that HYSYS uses with the corresponding unit.
To import this Excel file into AAM, go to Petroleum Assays in the Properties environment and select the New Assay button located in the ribbon. Then select the Import from File option.
In the Import Assay Data from Files window, click on the plus green icon and select your Excel file (*.xlsx or *.xls).
Finally click on Import and the information will be transferred from your Excel to AAM.
Keywords: AAM, petroleum assays, import, excel, refsys
References: None |
Problem Statement: How to save a material stream as an assay?
It may happen that for a converged flowsheet, a product stream will be required to be saved and used as an assay. | Solution: Any product material stream connected to a component slate can be saved as an assay
Click the button “Save Stream as Assay” in the Worksheet | Petroleum Assay and then check that it has been added to the Assay Manager list in the properties environment
Check also that the input data and the characterized results are good.
Keywords: material stream, save as assay
References: None |
Problem Statement: What equation is used in the Vetere estimation method for Heat of vaporization? | Solution: The Vetere method used by Aspen Plus to estimate heat of vaporization depends on the Molecular Weight (MW) and Normal Boiling Point (TB). The Vetere method is used to estimate heat of vaporization at TB. The Watson equation is then used to extrapolate heat of vaporization to TC. At TB an average error of 1.6% has been reported.
The Vetere method implimented in Aspen Plus is slightly different from the equation in the The Properties of Gases and Liquids by Reid, Prausnitz and Poling, which depends on Critical Pressure and Temperature (PC and TC) and Boiling Point (TB).
Here''s a copy of the code where the calculation is performed.
FACT = TB - (263.D0*XMW)**0.581D0
IF (FACT .LE. 0D0) FACT = 1D-5
DS = 13.91D0 + 3.27D0*DLOG10(XMW) + 1.55D0*FACT**1.037D0/XMW
DHV = DS*TB*4186.8D0
Keywords:
References: None |
Problem Statement: Does the Naphtha Hydrotreater carry out any cracking reactions? | Solution: The Naphtha Hydrotreater in Aspen HYSYS does not carry out cracking reactions. In order to carry out the cracking reactions, the user can use the component mapper or HYSYS reactors like the Hydrocracker or the Fluidized Catalytic Cracking.
These reactors can be accessed through the Object Palette under Refining section.
Keywords: Naphtha Hydrotreater, Cracking, Reactions.
References: None |
Problem Statement: Why do I see a large gap between the calculated and user input D86 curve in Petroleum Assay? | Solution: In Petroleum Assay, user can input distillation data points based on TBP, ASTM D86, ASTM D1160 and ASTM D2887. A continuous distillation curve is then calculated based on the input data.
However, user may see a large difference between the input and calculated curves, specially when any ASTM curve is selected as input curve type, and no Light Ends are selected. Please see the screenshot as shown below:
The reason for that can be summarized as follows:
1. Internal TBP curve.
Similar to Oil Manager, the input distillation curve in any basis will be converted to internal TBP basis. So providing TBP curve as input will normally generate more accurate calculated curves.
2. Petroleum Assay assume distillation data includes Light Ends information.
Normally, C2 to n-C5 are taken into account as Light Ends. If no Light Ends compositions are provided, the initial point of the calculated curve will start from the boiling point of heaviest component like n-C5.
Therefore, if the first few user input data points are below the boiling point of n-C5, user may see a gap as shown in the screenshot above.
Keywords: Petroleum Assay, Light Ends
References: None |
Problem Statement: Why do I get the message you need at least 3 hypothetical components when creating the macro-cut table from Aspen HYSYS Petroleum Refining? | Solution: The message you need at least 3 hypothetical components will appear in the trace window if fluid package does not have at least 3 hypothetical components in the component list or the component list does not contain the petroleum components. The recommended workflow would be to import the component list from petroleumComp1.cml before creating the macro-cut table following the steps below.
1. Import the petroleumComp1.cml - by clicking the import button on the components tab. It is available under paks folder
2. Add the fluid package.
3. Now select the RefSYS Assay Manager.
4. Specify the assay name and associated fluid package in the Petroleum Assay page
5. Click on the Macro-Cut Table button to open the Assay page
6. Enter the distillation data on the Macro-cut table.
Keywords: Petroleum Assay, Macro-Cut
References: None |
Problem Statement: What is the complete list of CNTLS control parameters? | Solution: CNTLS Parameter
Description
Possible Values
ACODE
Use Encoding A Codes
Yes / C / NONE
AEVER
Activity Editor Version
1 / 2
AFO
Allow FACI Override
Yes / No
ALABELAB
Display Label above activity box
Blank / set or table name
ALABELIN
Display label inside activity box
Blank / set or table name
ATIPSCTL
Activity Tips control set or table
Blank / set or table name
ATIPSDLY
Activity Tips Delay
Blank / Delay time (F)
ATIPSDUR
Activity Tips Duration
Blank / Duration time (F)
COLS
Planning Board Width in Columns
Width (I)
CRMOUSE
Control Right Mouse Button Action
Macro / Rule
DCWI
Display Cost Window
Yes / No
DRWA
Display Recipe with Activity
Yes / No
DSFX
Show Special Effects: D, R, P, S, T
Yes ( to show all)
No ( does not display)
D - Show Demands
R - Show Receipts
P - Show PipeLine
S - Show Setups
T - Show Off Times
GFAC
Number of Facilities to display
Number of fac (I)
GMAX
Inventory Profile Maximum Value
Max value (F)
GMIN
Inventory Profile Minimum Value
Min value (F)
GPRO
Number of Inventories to display
Number of pro (I)
GRIDINT
Grid Interval
Interval (F)
GRIDST
Grid Start time
Time (F)
GUNI
Inventory Profile Scaling
P / % / scaling value (F)
GWFRAME
Gantt Window Frame
Macro / Rule
ICSU
Include Setups in JIT Bounds with Infinite Capacity
Yes / No
IPFRAME
Inventory Profile Frame
Macro / Rule
LGND
Force Display Legend
Yes / No
LWID
Maximum Activity Label Width
Width (I)
MAW
Minimum Activity Width
Width (I)
MFTFXARR
Fixed Material Flow Line Arrows
Single / Double
MFTLINES
Fixed Material Flow Trace Line to Show
Fixed / Float / All
OFAC
Operation Window Scaling Factor
Scaling factor (f)
ORLABEL
Order Activity Labels
Label (C )
PPLAN**
Problem Window Control Set - Storage
Set name
PWIDTOL
Inventory Duration Tolerance
Blank / Number (F) / Table
PWIPTOL
Inventory Percentage Tolerance
Blank / Number (F) / Table
PWIQTOL
Inventory Quantity Tolerance
Blank / Number (F) / Table
PWISORT
Problems window initial sort for Inventory Problems
Any Keyword in Problem window control set
PWTDTOL
Problems window timing link duration tolerance
Blank / Number (F) / Table
QUIET
Quiet Mode
Yes / No / LOUD
REGRID
Reset the inventory Grid window
Yes / No
ROWS
Planning Board height in rows
Height (I)
SPLAN
Activity Editor Control Set/Table
Set name
SRMOUSE
Shift Right mouse button action
Macro / Rule
TLDISP
Timing Link Display
STD / Min / Max
TPLAN
Problem Window Control Set - Timing
Set Name
TRACE
Update PATH table before Trace
Yes / No / SCM command / Macro / Rule
TUOR
Activity Editor Rate Unit
Hourly / Days / Positive Floating number
UAP
Use All PROs for problems
Yes / No
UFDG
Use FAC description in Gantt
Yes / No
UMPB
User Modifiable Planning Board
Yes / No
UMR
User Modifiable Recipes
Yes / No
UNDOLEV
Planning Board Undo and Redo Levels
Number (I) from (0 ~ 50)
UPCD
Use PRO code and Description
Yes / No / DC
UPDL
Use PRO Description in Legend
Yes / No
UPIV
Use PRO Codes in Inventory Profile
Yes / No / ACODE / BCODE / ICODE
XHAIR
Use Cross Hair Pointer
Yes / No
XPOS
Position of Planning Board, X Coordinate
Number (I)
YPOS
Position of Planning Board, Y Coordinate
Number (I)
ZOOM
Zoom Factor
Number (F)
**PPLAN is mistakenly listed as SPLAN in Version V7.2 and V7.3. This typo will be corrected in a future release.
Keywords: Planning Board
Options
Table
Schedule
Schedling
References: None |
Problem Statement: This knowledge base article explains why the supply demand balance report in Aspen Plant Scheduler may not always show the operation description in the report. | Solution: This problem has been observed to occur if routine >ROPR9002 does not exist in the $SIMEND$ macro within the model. Ensure that the >ROPR9002 exists in the $SIMEND$ macro.
Keywords: modeling
configuration
References: None |
Problem Statement: Unable to make DAT file for CAPs cases using the CAS2DAT conversion utility, which generates a 0 byte DAT file. | Solution: CAS2DAT cannot be used for CAPS cases as CAPS cases are protected. If you want to remove unused space from a model use the compress utility (cmprcase.exe).
Keywords: Case format
Converting
Compressing
References: None |
Problem Statement: How does the Lift Gas Control work in the FCC unit? | Solution: The lift gas is mixed with the vapor from the regenerator and goes to the bottom of the riser. The lift gas flow can be specified in the Riser/Reactor page under the Operation tab.
The lift gas can be specified as either volume or mass basis. This is considered to be 100% N2. If this is specified in volume basis this can calculate the mass flow or vice versa assuming that this is 100% N2.
Keywords: FCC, Lift Gas
References: None |
Problem Statement: How does a user run command line tools such as ASPCOMP, DFMS, the AP9TO10 converter, or command line Aspen Plus? | Solution: Users need to open the Aspen Plus Simulation Engine window. This can be accompished in two ways:
From the Windows desktop, click Start and then select Programs. Then select AspenTech, then Aspen Plus 10.x, then Aspen Plus Simulation Engine.
OR
Alternatively, a user can double-click on the Aspen Plus Simulation Engine icon on the desktop.
Both methods open a DOS window with all the environment variables (ASPTOP, etc.) properly set to run these tools.
Keywords: DFMS, AP9TO10, ASPCOMP, ASPLINK, command line
References: None |
Problem Statement: In the Plant Scheduler application, there is a report called Problems Report to display the Inventory Problems in the Format tab of the Planning Board contextual ribbon. By default, the Inventory tab of this window shows the following fields:
This window is customizable. This | Solution: explains how to do this customization using an example.
Solution
The following steps will accomplish this:
1. Go to the Developer tab | Commands Panel | Command line | Type: CNTLS.
2. There is a row in this table: (PPLAN) Problem Window Control Set - Inventory. The corresponding cell in this table is the control set for the Problems Window configuration. By default it is $PROB$. Close CNTLS now.
3. Go to the Developer tab | Commands Panel | Command line | Type: $PROB$. This command will open $PROB$.
4. This set's Code column can take table references which are indexed by PRO (product); it can take special characters which were covered inSolution # 139228 to display fields in the Problems Window. The corresponding Description column will be the column name given to the fields.
5. For example, to add the inventory type to the Problems Window, add a new row at the relevant place in the set. Enter PRODATA(@,TYI) (with the assumption that there is a TYI column in PRODATA table) in the Code column and Inventory Type in Description column. Once applied, the Problems Window will reflect the new field:
Keywords: Problems Window
Inventory
Planning Board
References: None |
Problem Statement: What does a ClChng block do?Can it transfer one component from the mixed substream to a solid substream? | Solution: The ClChng block changes the stream class between blocks and flowsheet sections. You can use ClChng to add or delete solid substreams between flowsheet sections. ClChng does not represent a real unit operation. ClChng is just making the transition. It does not convert from one substream to another. Nor does it change components from one solid substream to another solid substream. To move a component from one substream to another, use an RStoic block.
Note that if the inlet of a ClChng has a substream and the outlet does not have the substream, ClChng just drops the inlet substream information. ClChng does not maintain mass and energy balances if any dropped substream contains material flow or heat/work information.
A ClChng is an important tool if one section of a flowsheet needs solid substreams to use a solid unit operations or cannot have a solid substream to use Equation-Oriented (EO) mode which does not support Nonconventional solids.
Keywords: None
References: None |
Problem Statement: When simulating a column using RadFrac with no reboiler and no pumparound to the bottom stage, you will get an error message saying that the bottom stage of the column needs a vapor stream. The error may still appear even if you have a vapor stream entering the bottom of the column.
The error message will be similar to the following:
*** SEVERE ERROR
A VAPOR FEED/PUMPAROUND TO THE BOTTOM STAGE IS REQUIRED WHEN
QN=0 IS SPECIFIED IN COL-SPECS; REQUIRED FEED/PUMPAROUND
HAS ZERO FLOW. | Solution: If there is no reboiler and no vapor stream to a column bottom, the bottom stage will dry up, which is not allowed in RadFrac. Either a reboiler or a vapor stream must be provided. The vapor stream can be a feed or a pumparound return.
Even if you have specified a vapor feed to the bottom of the column you may still get the error message. Ask yourself two questions:
1. What feed-convention was used for this vapor stream: ON-STAGE or ABOVE-STAGE?
If you have used ABOVE-STAGE, the vapor will actually enter the stage above, which leaves the bottom stage without a vapor flow. Change the feed-convention to ON-STAGE or VAPOR.
2. Is the vapor stream entering the bottom of the column a tear stream? If so, did you provide an initial guess for this tear stream?
If you did not provide initial estimates for the tear stream, then on the first iteration of the flowsheet there would be zero flow in this stream and cause the above error. TheSolution is to provide initial estimates.
Similarly, if there is no condenser, there must be a liquid feed on stage 1 to ensure that the top of the column does not have any dry stages.
Keywords: QN = 0
References: None |
Problem Statement: How is the Pour Point calculated in Aspen Plus?
How can Pour Point be used in a flowsheet simulation? | Solution: When liquid petroleum products are cooled a point is reached at which some of the constituents begin to solidify, and if cooling is continued the oil eventually ceases to flow. The temperature at which this occurs (in a standard test) is recorded as the setting or solid point. The pour point is defined as the temperature 5 F above that point.
The user can input a pour point curve by supplying temperature values for the pour point at different mid-percent distilled points. Four such data points are required to define a property curve.
To enter the pour point for an existing assay, go to the Components->Assay/Blend->Property Curve form for that Assay. Then choose the Property Type of POURPT and enter the data on the Petro Properties sheet.
In a simulation, the value of the pour point may be accessed by two different Prop-Set properties:
The prop-set property POURPT and POURCRV calculate the pour point of a stream based on the pour point property curve entered for the assay. The bulk property value is reported by POURPT and the whole property curve is reported by POURCRV.
The prop-set property ''PRPT-API'' calculates the pour point based on API procedure 2B8.1. This procedure is a function of molecular weight, specific gravity and kinematic viscosity.
The following equation is used to estimate the pour point of petroleum fractions:
(2.970566) (0.61235-0.473575 *S ) (0.310311-0.32834*S)
Tpp = 234.85 * S * M * v100
Where,
Tpp = Pour point of petroleum fraction.
v100 = Kinematic viscosity at 100F, in centistokes
S = Specific gravity at 60F/60F
M = Molecular weight of petroleum fraction
Please, refer to the API Technical Data Book - Petroleum Refining for more details
Keywords: pour point
petroleum
assay
ada
References: None |
Problem Statement: Why does the assay show a status Invalid Fluid Package? | Solution: This message is shown when there is no fluid package attached to the assay.
You can select the fluid package to be associated to the assay from the drop down menu of the Fluid Package cell. This should be done especially when there are several fluid packages in the case.
Keywords: Invalid fluid package, Assay
References: None |
Problem Statement: What is the definition of ECP in the petroleum distillation column? | Solution: ECP is the effective cut point and is usually close to the TBP cut point. There is an explanation of it in the petroleum column simulation word document which is located in the example cases that come with a standard AspenOne Engineering install. Users can access this document by following this file path C:\Program Files (x86)\AspenTech\Aspen HYSYS V7.3\Samples\Refining Cases.
ECP is a feature within the petroleum distillation, which is also known as the short-cut column because of its ability to provide quick convergence at imperfect separation. The short-cut works in this way; a plot is made of the normal boiling point of a curve against the Ln(Di/Bi) for all the components. Di is the mass flow of component i leaving the top stage as a distillate. Bi is the mass flow for the component ‘i’ leaving at the bottoms. This plot is typically bilinear in the petroleum distillation column. The negative reciprocals of the slopes are SI top and SI bottom. I. e. if the top line has a slope of -0.1, then the SI top is 10. The temperature at which the two lines intersect is the effective cut point (ECP) for that draw stream.
When the user specifies yields for each cut, the SI top/bottom supplied by the user is used to create that graph. The ECP is then varied to match the specified yields. With the right ECP for a cut, users can calculate the value of Ln(Di/Bi) from the graph and subsequently use the mass balances to get the yield for that cut. Although the TBP cut point is the typical refining specification this specification is not really relevant to the model that the shortcut distillation column uses.
In contrast, the Component Splitter can be used to obtain the various product distillation cuts defined in terms of their TBP. This separates the components arbitrarily and therefore can achieve perfect separation. The short cut distillation model, however, cannot give perfect separation, so true TBPs can't really be defined for the various cuts.
Please note the short cut column is intended to give fast, consistent results for the column to be able to quickly test multiple oils/feeds. If users want results to properly design a column, then the Aspen Hysys rigorous column should be used. The main purpose of the short-cut column is for when the user is focused on simulating other parts of the refinery and needs a column that will converge quickly.
For example if modelling an FCC, the user might want to connect the FCC effluent to a shortcut distillation column. However both models should ideally be calibrated with existing plant data.
Keywords: ECP, TBP, Short-cut column, petroleum distillation column, bi-linear distillation
References: None |
Problem Statement: What does the light gas tuning parameter calibrate in the Hydrocracker? | Solution: The light gas tuning parameters adjust the relative amounts of C1, C2, C3, and C4 formed. Some of the reactions are written in such a way that there are multiple product groups.
The C10P can crack to C9P and C1, C8P and C2, C7P and C3, C6P and C4, or two C5s. By default, these products would be produced in equal amounts. However, the relative amounts of these can be changed. There are many reactions such as these and the light ends tuning factors are used to adjust the relative amounts of these products. Note, though, that this tuning is limited since there are also many reactions with fixed products ratios.
Keywords: Hydrocracker, Light gas parameter tuning
References: None |
Problem Statement: The Std Ideal Liq. Mass Density is found in the stream properties as a standard correlation while the Std. Liquid Density [petrol] is found in the petroleum correlations.
Std. Liquid Density [petrol] doesn’t mention that it is using ideal properties. So, why is the value calculated for the Std Liquid density [petrol] the same as the Std Ideal Liq. Mass Density? | Solution: The Std. Liquid Density [petrol] and the Std. Ideal Liq. Mass Density are the same because they use the same algorithm that includes the pure components ideal liquid density.
First, the average liquid density is calculated with the equation below.
Where:
Avg. Ideal Liq. Density: average ideal liquid density
Xi: molar fraction of component i
MW: molecular weight of component i
ρi: pure component ideal liquid density
The average liquid density is then used to calculate the Std. Ideal Liq. Mass Density.
Where:
Std. Ideal Liq. Mass Density: standard ideal liquid mass density
Mass liq density: mass liquid density
MWbulk: bulk molecular weight
Average liquid density: average liquid density
Keywords: Standard ideal liquid mass density, Standard Liquid density [petrol]
References: None |
Problem Statement: When user tries to open Refining cases (Hydrocraker reactor, Catalytic Reformer reactor, etc) , a message “Intel Visual Fortran run-time error” appears and Aspen HYSYS closes unexpectedly.
This can happen when loading cases from the example library, opening existing files, creating new templates or adding the refinery reactor from the palette.
Root Cause
The issue is caused by the memory allocation of the 32 bit Windows operating system. The 32 bit machines by default will only allocate up to 2 GB for any given application, whereas 64 bit operating system will allow up to 4 GB for a 32 bit application (and much more for a 64 bit application).
This is critical for the reactor models because Aspen HYSYS is using Aspen Properties and Equation Oriented (EO) solver which both require large amounts of memory. The 2 GB memory has to do with the operating system and not the physical memory. The total memory is generally fine, but the refinery reactors (the EO | Solution: in particular) need relatively large chunks of contiguous, so the 2GB is often not enough.Solution
The 32 bit operating systems do have a switch, though, that can be set to allow 3 GB per application.
To enable the 3GB switch on Windows Vista™, Windows 7 or Windows 8:
1. Right-click on the Command Prompt icon in the Accessories program group of the Start menu. Click Run as Administrator.
2. At the command prompt, enter: bcdedit /set IncreaseUserVa 3072
3. Restart the computer.
To disable the 3GB switch:
1. Right-click on Command Prompt in the Accessories program group of the Start menu. Click Run as Administrator.
2. At the command prompt, enter: bcdedit /deletevalue IncreaseUserVa
3. Restart the computer.
For more information, please refer to
https://msdn.microsoft.com/en-us/library/windows/hardware/Dn613959(v=vs.85).aspx
Keywords: Hydrocraker, Reformer, Fortran run-time error, 2 GB, 3GB switch
References: None |
Problem Statement: How do I calculate the shell-side heat transfer coefficient
and the corrected LMTD for a heat excahnger in Aspen Plus? How do these results compare with other heat exchanger design programs such as B-JAC in Aspen Plus? | Solution: Following are some generalizations about an Aspen Plus HEATX block.
The shell-side heat transfer calculations are based on the
Bell-Delaware method, which is considered to be the best open literature method available. For this method, calculate the shell-side heat transfer coefficient, which is based on an ideal heat transfer coefficient for pure cross flow across the tube bank (that is, the B stream).
Multiply this h(ideal) by various correction factors to account for the effects of the by-pass streams. Various leakage and bypass streams affect the heat trasnfer rate by reducing the ideal cross flow stream B and therefore the local heat transfer coefficient, and by changing the temperature profile. The magnitude of the correction factors is a function of the shell-side geometry and flow characteristics. The following reduce the heat transfer coefficient for ideal flow across the tube bank:
TEMA shell type and size
tube size
pitch pattern
baffle spacing and cut
sealing strips
other mechanical clearances
The corrected shell-side heat transfer coefficient is typically 60% of the ideal value.
The values entered or defaulted for the following items should be closely examined:
Baffel Cut
Baffel Spacing (inlet, outlet, central)
Shell-to- Baffel clearance
Tube-to-Baffel clearance
Shell-to-Bundle Clearance (espcially for pull through designs TEMA type T)
Sealing Strips
The data base upon which the Delaware method was developed is limited to the E shell configurations using plain tubes, making Aspen Plus results most accurate for this type of heat exchanger. This presents some difficulty in low pressure applications. TEMA type J or X are more commonly used with large baffle cuts and spacing. This results in significant increase in the amount of by-pass and leakage streams and reduces shellside heat transfer coefficient.
The results calculated by Aspen Plus can be improved by increasing the number of points at which heat transfer coefficients are calculated for each zone. Typically, Aspen Plus divids a heat exchanger into a number of zones. Zone boundaries are usually defined at all points where a phase change occurs. At each point (up to a max. of 5) in each zone; a local heat transfer coefficient and a local LMTD is first calculated and then used to calcualate the local area required. This is repeated for all points in all the zones. The areas are added up to determine the overall required area.
Given the number of zones, the total duty is divided equally, and, starting from one side of the exchanger, the outlet temperature of each zone for that side is computed assuming a common outlet temperature for all streams exiting that zone. If the T-Q curve is not linear, the more zones you have, the less approximate the LMTD and UA calculations will be. In the limit, in other words, as you increase the number of zones, you should see the LMTD and UA to approach some limiting value. Instead of adding more zones manually to find that limit, you can use the checkbox for Add extra zones in regions where the profile is non-linear on the Zone Analysis sheet. Once the outlet temperatures of all zones are calculated for both hot and cold sides, LMTD, and thus UA are computed.
For the purpose of comparing the results of Aspen Plus to other programs, it is generally better to compare results for each zone, rather than the overall results. This is because Aspen Plus reports an overall corrected LMTD factor based on the terminal conditions, multiplied by a correction factor. Most other programs report a mean or weighted LMTD which is computed as follows:
MTD = Qtotal /[sum (Ui * Ai)]
where is are the points within each zone.
The value of U is then calcualted from the overall duty, LMTD, and the required Area. Therefore as long as definitions of LMTD are different the overall heat transfer coefficients will be different as well.
Keywords: None
References: None |
Problem Statement: My REquil reactor block is not converging! What can be done? | Solution: If an REquil block is not converging, several options are available to aid
convergence.
Explicitly specify the Valid phases for the reactor on the REquil / Input / Specifications sheet. (In Aspen Plus 9, Specify NPHASE and PHASE on the REQUIL.MAIN form in ModelManager or the PARAM sentence for input language.)
Increase the maximum number of flash interations in the Convergence Parameters section and the maximum number of chemical equilibrium calculations in the Chemical Equilibrium Convergence Parameters section on the REquil / Input / Convergence sheet. (In Aspen Plus 9, Specify MAXIT and CHEM-MAXIT on the REQUIL.MAIN form in ModelManager or the PARAM sentence for input language.)
Specify an initial Extent Estimate for reactions that have a Temperature Approach specification (i.e are not already fixed by a Molar Extent specification) on the REquil / Input / Reactions sheet. (In Aspen Plus 9, Specify EXTENT-EST)
Precede the REquil reactor by an RGibbs reactor working at a slightly lower temperature and pass the product stream to the REquil reactor.
For the cases when an 8.5-6 run does not converge in Aspen Plus 9, use old algorithm by adding ALGORITHM=OLD to PARAM sentence (not supported in MM)
For more information about REquil, consult the Aspen Plus Unit Operations
Keywords:
References: manual, Chapter 6, Reactors. |
Problem Statement: How can I add a new assay from Petroleum Assay library? | Solution: Below are the steps to add Petroleum Assay from the Assay Library:
1) Add the Fluid package and then go to Petroleum Assay window.
2) Press 'Add' button to add Petroleum assay-1 and double click on it.
3) Pick 'assay source' as 'specified' and select the fluid package from drop down menu.
4) Click on 'import from' to select 'Assay Library'
5) The list of assays will appear.
Keywords:
References: None |
Problem Statement: What kind of Feed types are avaliable for Refining Reactor Transition? | Solution: When you set up the Refining Reactor Transition in stream cutter, you sometime find some properties may be little bit off your desired properties when you use default fingerprint.
Default feed type:
This may be due to the default which is a VGO material. If you feed is LCO, this may cause the trouble for the properties after transition or even impact the convergence of the reactor.
In the case, you can change the fingerprint by importing from Refsys reactor folder in HYSYS installation folder, such as C:\Program Files (x86)\AspenTech\Aspen HYSYS V8.0\RefSYS\refreactor\HCR\feedlibrary.
Keywords: Feed type, stream cutter, Refining reactor transition.
References: None |
Problem Statement: A resource in the Aspen Supply Planner model is running at three times capacity.
Upon reviewing the resource group mapping, it was found that the resource was also listed 3 times there. Twice where the Resource Groupings are blank and then once where the Resource Grouping is listed as Undefined Resource Grouping.
Checking the base excel files and the import tables, including the view, showed that each of the database tables (and in the view) listed the resource only once. Having it appear three times would account for the increased capacity that the model is showing when solving the model. | Solution: Duplicate data was accidentally imported into the model (RES and CAP sets) and unfortunately, the duplicates were not being removed during import, so there was no way of getting rid of the bad data. To alleviate this problem, manually delete the bad/duplicate data and re-import the correct data.
Keywords: Resource Groupings
Excess capacity
Importing data
References: None |
Problem Statement: Jump Start: Delayed Coker Model in Aspen HYSYS Petroleum Refining | Solution: This document is intended as a “getting started” guide. It will cover the process of creating a delayed coking model, including setting up a heavy crude feed with a petroleum assay, configuring a delayed coker unit operation, calibrating the coker unit, and putting a recycle network together.
Keywords: Delayed Coker Model, V8.4, Aspen HYSYS Petroleum Refining
References: None |
Problem Statement: The PONA reported in my stream does not sum up to 100% - how do I fix this? | Solution: Follow the steps below to normalize your PONA analysis:
Enter the Basis Environment.
Open the Petroleum Assay that the stream is using.
Navigate to the Analysis tab.
Click the Resolve PONA button.
You can now return to the Simulation Environment to view the results.
Keywords: PONA, Assay, PNA
References: None |
Problem Statement: I am using a wide temperature range to regress VLE data--from below to above the critical point of one component.
Can I regress both the Henry constant and activity coeff. binary parameters together? | Solution: Yes, it is possible to regress Henry and NTRL, UNIQUAC or Wilson binary parameters simultaneously with the data regression system.
However, it is better to regress the Henry's constants first using the low-concentration data (up to 5% solute), and then regress the activity coefficient binary parameters alone, fixing the Henry's constants obtained in the previous step.
Keywords: DRS
References: None |
Problem Statement: After v8.7,the handling of pipeline segments have changed. What is the new PIPELINE_INV table? | Solution: Before v8.7, the pipeline segments where limited to a count of 2 (primary and secondary pipelines).
After v8.7, this has been enhanced that there can be any number of segments for a pipeline route. With this new change there have been certain database changes, one of them being that PLINV has been replaced by PIPELINE_INV.
When there is a DBUpdate between versions, and the users run the pipeline conversion wizard, the exisitng data from the older PIPELINES table and the PLINV table are migrated into new tables. The PLINV entries are now stored in PIPELINE_INV and this is the table used by the new pipeline system. The following is the schema of the table:
Keywords: PLINV, PIPELINE_INV, DBupdate
References: None |
Problem Statement: The Compressor (Compr) block will fail if the flowrate exceeds the Stonewall limit. What is the stonewall? | Solution: Surge and stonewall are the minimum and maximum flow rates between which a compressor
must be operated. The problem is that the compressor is operating above the stonewall.
The following error message is generated by Aspen Plus:
* WARNING WHILE EXECUTING UNIT OPERATIONS BLOCK: R-300-1 (MODEL: COMPR)
(CMCTAB.3)
OPERATING POINT IS ABOVE STONEWALL
CURVE NUMBER = 1
OUTLET TEMP = 348.0 OUTLET PRES = 0.2056E+06 INDICATED HP = 0
POLYTROPIC EFFICIENCY = 0.7297
OUTLET TEMP = 361.4 OUTLET PRES = 0.2478E+06 INDICATED HP = 0
POLYTROPIC EFFICIENCY = 0.7430
01 vars not converged, Max Err/Tol -0.70957E+04
CURVE NUMBER = 1
The stonewall is maximum throughput or the flow rate at which the compressor can operate. It can be specified by the user or interpolated if several performance curves are entered.
If you specify tabular data, the end points are taken as surge and stonewall. If you specify polynomial curves, a surge point is required for each curve, specified after the four coefficients on the Curve Data sheet; stonewall is optionally specified here also. For extended polynomial curves, specify the surge curve on the Surge sheet; no stonewall is allowed in this case. If you specify performance curves via a user subroutine, the subroutine also provides percentage above surge and below stonewall.
Keywords: stone wall
References: None |
Problem Statement: How do I input petroleum properties for the first cut in Macro-Cut Table? | Solution: When characterizing a petroleum assay using the Macro-Cut Table, it is assumed that the distillation data includes light ends information. So the first assay cut will have a summation of hypo components and all the lighter pure components.
It is true for the Distillation Yield Vs Temp, as well as for other Petroleum Properties, which means the property will also require a bulk value for the whole cut not just for the hypo. For example, the Standard Liquid Density of the first cut in the assay is the bulk value for the hypo and light ends together.
Keywords: Macro-Cut Table, Petroleum Properties
References: None |
Problem Statement: What is required to migrate from Aspen Plus 9.x to 10.x?
Will the Aspen Plus 9.2 and 9.3 files will work in Aspen Plus 10? | Solution: Aspen Plus simulations are designed to be upwardly compatible, provided that the Aspen Plus simulation files that are version independent are saved before changing Aspen Plus versions. Due to continual advances in the Aspen Plus architecture, some modifications may be required in order to use older simulations in more recent releases. These modifications are generally required in simulations which contain: in-line Fortran; external Fortran subroutines for customized unit operation or physical property models; or custom user or in-house physical property databanks. In any new release which contain architectural changes that require changes in user Fortran or input specifications, one-time conversion utilities are provided with the new Aspen Plus release to facilitate the process.
To work with Aspen Plus version 9.x generated problems with Aspen Plus 10.x you must make sure that you have .BKP and .INP extension files saved. Binary .IWB and .IWD extension files are NOT upwardly compatible from version 9.x to version 10.x. Binary .APW extension files from earlier Aspen Plus 10 releases are also not upwardly compatible.
The second issue that needs to be addressed is FORTRAN. Both in-line fortran and user fortran subroutines for customized unit operation or physical property models have to be converted from Aspen Plus version 9.x format to Aspen Plus 10.x format using the delivered utility. You will require a compatible fortran compiler - the recommended compiler for PC version is Digital Visual Fortran.
The third issue is customizations. If you have inhouse databanks from Aspen Plus 9.x, you will also need to migrate these files to Aspen Plus 10.x. as they are binary files which are NOT upwardly compatible.
Summary
Save all files with Fortran blocks as input files (*.inp)
Save all other files as backup (.bkp) OR (.inp) files - backup files can be generated from input files, but original flowsheet graphics is not saved
Install Aspen Plus 10.x
Install the FORTRAN compiler
Convert all files containing Fortran (both user subroutines (.f or .for) and in-line Fortran blocks). (see Aspen Plus System Management
Keywords: migrate
update
migration
y2k
upgrade
References: manual, Chapter 1 and |
Problem Statement: Why do I get an Out Of Memory Exception using 32 bit Aspen Supply Chain Manager and a large case file (over 1 GB)? | Solution: For such a larger case, it will hit the 2G limit at some point. It is our recommendation you use 64 bit SCM.
Keywords: None
References: None |
Problem Statement: What is the best way to open Aspen Plus runs with Visual Basic (VB) applications when the License Manager is used? | Solution: When using License Manager with Aspen Plus, a Connect to Engine Dialog box will be displayed prompting the user to specify the simulation engine platform information. This dialog box will be displayed even though the simulation engine and user interface reside locally on a PC. An acknowledge dialog box will also be displayed after the connection has been established.
Instead of using the GetObject Visual Basic (VB) function to create an Aspen Plus object, use CreateObject to create a blank Aspen Plus User Interface (IHapp) object. The Aspen Plus InitFromArchive2 method can then be used to load a simulation into the object. If the index to the platform is specified as part of the call, the two connection dialog boxes will not be displayed. This index is passed as a Long Integer and has a value of zero for the Local PC platform. The following code fragment will open an Aspen Plus simulation on a local PC when another host is running License Manager:
Set go_Simulation = CreateObject(Apwn.Document)
Call go_Simulation.InitFromArchive2(ls_FilePathName, 0)
go_Simulation is a global object variable that is based on the Aspen Plus IHapp Visual Basic type. The name of the License Manager Host should be specified using the Aspen Plus License Manager Selector. Select Programs from the Windows Start button, then Aspen Tech, Common Utilities then License Manager Selector. Platform indexes for other platforms are 1 for unix, 2 for OpenVMS and 3 for WindowsNT server.
Chapter 38 of the Aspen Plus User Guide (Volume 3) provides more details in using the Aspen Plus ActiveX interface with Visual Basic. The ActiveX interface provides a way to automate Aspen Plus User Interface tasks. These applications can be based on standalone Visual Basic (VB) or other software that supports Microsoft''s Visual Basic for Applications (VBA) such as Excel.
This procedure is similar to how client/host runs can be opened. SeeSolution 102611 for a description of how to open these runs.
Keywords: Visual Basic, VBA, ActiveX, Client Server, dialog box, License Manager
References: None |
Problem Statement: How do I solve “Reactor TransitionObject” problems in the message window? | Solution: If you have a Catalytic Reformer that is not solving, look in the message window below the PFD, to check if the error is such as PNA missing data.
Normally this kind of error comes when there is a missing parameter between the Main Flowsheet and the Reactor Sub-Flowsheet or the other way around. Double click in the error message “red print” and the transition basis will appear, look for the missing property that is required for you reactor to solve.
There are two ways of solving missing data: The first is to select a different Feed (In the transition window) to one you can edit and input the missing parameters. The other way is to close the transition window and look in the properties of the feed stream to check if any component is missing data. Do a scan for the missing parameters:
If you have components that are Hypotheticals or complex components, there is a chance that some of these are missing data. Go to the Simulation Environment and input the required data by editing each component property.
Once no input is missing Hysys will be able to solve for the property with the internal mixing rule and you can keep “Selected Feed: -> Stream” in the transition window.
Keywords: Catalytic Reformer, Reactor, PNA, Reactor TransitionObject
References: None |
Problem Statement: How are pseudocomponents generated in Aspen Plus 10? | Solution: An example of pseudocomponent generation:
Start Aspen Plus session. On the file selection window, in the section titled Create a New Simulation Using select Template, and click OK.
A list of predefined templates comes up. Select Petroleum with English Units. Leave the Run Type as Flowsheet (default).
In the data browser, go to Components. Specify Water as a conventional component. This is required as the Use Free Water Calculations box is checked in the Setup\Specifications form.
Go to Components\Assay/Blend.
Click on New to define a new assay. Accept the default assay name (in this case AB-1) or enter a name. From the pull down list select Assay in the Select Type box. Click on OK.
The assay Basic Data form opens up. From the pull down list select True Boiling Point (Liquid Volume basis). Enter an API gravity of 34.8 and the following TBP distillation values.
% Distilled
Temperature (F)
6.5
120
10
200
20
300
30
400
40
470
50
550
60
650
70
750
80
850
90
1100
95
1300
98
1475
99
1670
Check the component list. AB-1 is added, type is Assay. The pseudocomponents will be generated automatically when the simulation is run, according to the internally set default cut points. If the user wants to define the cut points, this can be done through the Petro Characterization option under Components. There is no need to go there if the default cuts are acceptable.
Click on the Next button ( N => ).
The Expert system takes you to the Properties Specification form. Select Grayson as the Basic Method. Click on the Next button. The expert system informs you that a flowsheet must be drawn.
Set up a heater block with a feed of 1000 Bbl/day of component AB-1 at 100 F and 50 psi.
Specify the heater block with an outlet temperature of 150 F and 0 pressure drop. The flowsheet is now complete and the file is ready to run.
Run the file. The simulation status (Bottom right corner) should show Results Available.
Checking the Pseudocomponents generated:
The pseudocomponents generated do not show up individually on the Components\Specifications form. Only the assay AB-1 will show up there.
Go to Components\Assay/Blend\ AB-1\Results and look under the Pseudocomp Breakdown option. The pseudo-components generated are shown there. For greater detail, look under Petro Characterization\Results.
Alternatively, simply check the Stream Results of the heater block. The pseudocomponents show up in the stream summary.
Keywords: petroleum
ada
assay
pseudo
pseodocomp
pseudocomponent
generation
References: None |
Problem Statement: This | Solution: is intended for users who have basic configuration experience in Aspen SCM.
In the Planning Board, there is an option to run routines when the user right clicks on an activity. The followingSolution explains how this can be configured.
Solution
In the table CNTLS there is a row “(GWFRAME) Gantt Window Frame” which presents a rule that runs when the user right clicks on an Activity.
By default, there is no rule running in the Plant Scheduler CAP (demo).
If there is rule or macro that you would like to run when the user right clicks on an Activity, then this cell is the place to mention it.
For example: If you want to show the material trace of that activity when the user right clicks, then you would have to create the following rule:
Code
Description
_RTEST1
IF
S TRACE ROUTING
THEN
RULE_DONE
Then, this rule's name “>_RTEST1” should be mentioned in the CNTLS table.
Alternatively, a macro can also be created.
Keywords: Right Click
Activity
PB
References: None |
Problem Statement: How to import Assay from Assay library to Material Stream directly? | Solution: Open an example case Petroleum Column.HSC from Refining Cases folder from Open Example Case from Hysys
+ Select Material Stream Material Stream: 1 from Object Palette
+ Worksheet/Petroleum Assay/ Please select Create New Assay On Stream from drop down box
+ Click on Petroleum Assay Specification tab
+ In new window MacroCut Data:Stream -1 click on Import From tab then click on Assay Library tab
+ Select Assay to Import from list then click on Import Selected Assay tab
+ Data will be imported to MacroCut Data:Stream -1 window the close
+ Check Material Stream/Worksheet/Composition
Keywords: Refsys, import Assay library etc;
References: None |
Problem Statement: Aspen Plus uses a default erosional coefficient of 100 for the Pipe Unit. Is this a good value for all applications and why should the erosional coefficient be considered in pipe designs? | Solution: When sizing a pipe, the selected inside diameter needs to be large enough so the erosional velocity is greater than the expected pipe velocity. This prevents unwanted erosion inside the pipe.
On the PIPE PARAMETERS sheet of the PIPE unit's setup, a default erosional coefficient of 100 is displayed. This default value may not be appropriate for all applications and should be modified based on the pipe's type of service.
The PIPE unit uses the API 14E publication to calculate the erosional velocity. The equation is:
Ve = C /(RhoMix)**0.5
C = erosional coefficient
RhoMix = Fluid density at flowing conditions.
The API publication 14E has suggested guidelines for the erosional coefficient 'C' for solid-free fluids:
Erosional
Coefficient
C
Application
100
Continuous flow, no corrosion prevention
125
Intermittent flow, no corrosion prevention
150-200
Continuous flow with corrosion prevention
250
Intermittent flow with corrosion prevention
The corrosion prevention implies the use of corrosion resistant alloys and/or corrosion inhibition inside the pipes. This correlation implies that a pipe with less corrosion inside is smoother and can tolerate higher velocities before eroding.
To better understand the power of this PIPE unit feature, please review the companion model, PipeErosion.bkp and also the below chart:
In the above chart, the red line represents the erosional velocity to be avoided in the pipe design. At the large end of the studied range, the 8 inch pipe is well below the erosional velocity for all of the above mentioned flow conditions in Table 1. But, at the smallest end of the range, the 4 inch pipe, with corrosion resistant pipe material, the 4 inch pipe would also be acceptable. Any pipe material and pipe service with a coefficient of erosion grater than 135 would keep the actual velocity below the erosional velocity.
The API publication 14E correlations were obtained from offshore oil production piping systems. The publication further qualifies its correlations:
Industry experience to date indicates that for solids-free fluids values of C=100 for continuous service and C=125 for intermittent service are conservative. If solids production [slurries] is anticipated, fluid velocities should be significantly reduced. Different values pf 'C' may be used where specific application studies have shown them to be appropriate. Where solids and/or corrosive contaminants are present or where 'C' values higher than 100 for continuous service are used, periodic surveys to assess pipe wall thickness should be considered.
Keywords: PIPE, C-EROSION, EROSIONAL VELOCITY,
References: None |
Problem Statement: Why is the Makeup2 flow rate zero for HPS Loop1 / 2? When is it appropriate to use a positive number? | Solution: The makeup rate is calculated to match the user specifications for Gas to Oil ratio and reactor temperatures. We allow the user to input a second makeup flow if they desire to have a second makeup flow with a different composition (e.g. high purity H2). If the user specifies a non-zero flow for Makeup2, note that the calculated value for Makeup1 will drop.
Keywords: HCR, makeup gas, makeup, HPS, high pressure separator
References: None |
Problem Statement: What's New in Aspen HYSYS V7.2 - Crude Oil Characterization | Solution: In HYSYS Petroleum Refining V7.2, HYSYS based crude characterization expands from Oil Manager methods to a new input form called MacroCut that forms a bridge to powerful third party crude characterization software packages, i.e, SpiralSoft Crude Manager and Haverly H/CAMS.
In the Simulation Basis Manager, a new RefSYS Assay Manager tab has been introduced next to the Oil Manager tab:
The new tab moves the user into the RefSYS Assay Library Manager. From there, the user can execute workflows to build assays from the RefSYS MacroCut input view or reach out to powerful crude characterization packages like SpiralSoft Crude Manager or Haverly H/CAMS. In this way, the user can convert his raw lab data into HYSYS stream models using well known Oil Manager or more powerful methods consistent with the crude oil chararcterization systems used in refinery planning and scheduling applications like Aspen PIMS and Aspen Petroleum Scheduler.
HYSYS Oil Manager is the well proven way to enter data for a small number of crude oils with a small number of properties per crude oil. RefSYS MacroCut provides a more convenient format for entering data for more crude oils with more properties and moves the user and his data into the more efficient RefSYS hypo structure. Ultimately, the client can move his characterization out of HYSYS/RefSYS entirely and into industry standards like SpiralSoft Crude Manager and Haverly H/CAMS using direct links to RefSYS or an intermediate Excel based file.
Keywords: Crude Oil Characterization , What's New, New V7.2, Assay
References: None |
Problem Statement: Can Tabpoly data be entered in the DFMS input file for User or Inhouse databanks? | Solution: No, this is not a feature of DFMS.
TABPOLY-DATA is not a valid DFMS keyword.
Keywords: inhspcd
user databank
References: None |
Problem Statement: Why do I get consistency errors for Molecular Weight (MW) in Aspen HYSYS V7.3 CP3 (and higher) with a file already converged in Aspen HYSYS V7.3 CP2? | Solution: The MW related consistency error is due to a MW fix in HYSYS V7.3 CP3. This fix re-estimates the MW's for hypo components when their density changes. So when re-run a file in HYSYS V7.3 CP3 with a converged case in V7.3 CP2, the MW is updated and consequently it can result in a consistency error.
The current workaround to eliminate the error is to re-characterize the Petroleum Assay:
1. Re-input the distillation curve and bulk properties.
2. Re-calculate the assay.
3. Enter the Simulation Environment.
Keywords: HYSYS V7.3 CP3, MW
References: None |
Problem Statement: Where Can I check blending property method calculation description for various petroleum properties in Refsys Assay Manager? | Solution: Appendix A in Unit Operation Guide in Hysys Petroleum Refining contains brief description of the blending rules of the physical and petroleum properties in petroleum assays
Unit Operation Guide can be located in below path if user install Hysys application in C drive
C:\Program Files\AspenTech\Aspen HYSYS V7.3
PDF File Name: AspenHysysRefiningV7_3-Ops
Keywords: Bledning Rules, Blending Methods, Default Method, Petroleum Properties Calculation etc;
References: None |
Problem Statement: What can I try to converge a HBED? | Solution: When your HBED failed to get convergent, you can do the following:
1. Go to Simulation Engine tab and Change Solve Failure Recovery Option to Restore Variables in Solver settings page
2. Ignore and unignore HEBED two times to see whether you can get it convergent.
3. If not, go to Solver settings page and active
4. In most of case, you can get it convergent without tuning Creep iterations and Step size. If you get the problem, you could increase this interations number and reduce step size.
5. If you try all options on solver sittings, you still could not get it convergent. It means that either yourSolution is very far away from the default initial values for the reactor or your inlet has the problem. You may try to change the default values for HBED reactor. You can find the default var file at the HYSYS installation folder such as: C:\Program Files (x86)\AspenTech\Aspen HYSYS V8.0\RefSYS\refreactor\HCR\plt\htrbed.var.
Make sure you save the back up file before you make any changes. You also can save as other name into different folder and then make your modifications. Then you can load your var file at Simulation Engine page as the following:
After you make your case convergent, you may want to switch back to default setup.
Keywords: HBED, Restore variable, varfile
References: None |
Problem Statement: How can I add a new Petroleum Assay from HYSYS oil Libraries? | Solution: Before you start is recommended, if you want to use REFsys, to select one of the available component list.
In the Simulation Basis Manager go to REFsys Assay Manager.
Import a new Assay and Associate the Fluid Package. Select Macro-Cut Table
Inside the Macro-Cut Table, you will be able to open the list of HYSYS oil assay that are available.
And inside the Macro cut table you will be able to see all the bulk properties.
Once selected you can start a new HYSYS simulation, just need to check that the oil assay is attached to you material stream.
The stream composition will be defined and you are ready to start.
Keywords: Oil assay, Library, REFsys.
References: None |
Problem Statement: What is the procedure to migrate custom icons from Version 9 to Release 10 of Aspen Plus? | Solution: For Release 10.0-1, mmgr9.def and a patched version of icondef must be sent to customer. Both version 9 and Release 10 must be installed to perform migration.
Setup to run Aspen Plus Release 9 in a working directory.
Copy your customized Release 9 icon definition file (mmg.def) into the working directory.
Copy the Version 10 icon definition file (mmgr9.def) from your Aspen Plus 10.0 User Interface installation (Apui100\xeq) into the working directory.
Run the Release 9 Icon Migration Utility (icnmrg0) to convert the custom icons.
Within the utility, define the source and target files using the Open command from the file pull-down menu. Specify mmg.def as the source file and mmgr9.def as the target. The converted icons will be written to mmgr9.def.
Perform the following three steps for each custom icon:
Select the new model name in model/symbol column
Right-mouse click and select Resolve
Select Copy source to overwrite target
Save the file.
Copy the updated Version 10 icon definition file (mmgr9.def) back to the Apui100\xeq directory.
Open the Version 10 simulation engine window and navigate to the Apui100\xeq directory.
Update the Version 10 record definition file (recdef.apr) with the new icons by executing the command icondef recdef.apr mmgr9.def.
Keywords: Migrating Custom Icons Flowsheet GUI
References: None |
Problem Statement: What is the Definition of the Equilibrium Constant (Keq) reported by REquil? | Solution: The chemical equilibrium constant (Keq) used in the REquil block in Aspen Plus is defined as:
Keq = Pi (Activities of Product Components) / Pi (Activities of Reactant Components)
where Pi denotes the multiplication operator.
The Activity of Component i (denoted as ai) is defined as:
ai = Fugacity of Component i in a mixture/Fugacity of pure component i at a standard state.
For chemical equilibrium calculations, 1 atm is used as the fugacity for standard state. Thus
ai = fugacity of component i.
Therefore,
Keq = Pi(Fugacities of Product Components) / Pi (Fugacities of Reactant Components).
Note that here the unit of the fugacity must be atm.
Since the activity is unitless, Keq does not have a unit.
To demonstrate the above calculation, an example file has been attached.
In the example, a property set is used to report PHIMX, which is the fugacity coefficient of a component in a mixture. Then, a Calculator block is used to calculate and report the equilibrium constant from both the vapor and liquid fugacities.
The fugacity of a component can be obtained by
Fugacity = x *P *PHIMX
where x is the mole fraction and P is the total system pressure.
The Keq calculated and reported in the Calculator block match the Keq reported in the REquil block.
Keywords: REquil
Keq
Equilibrium constant
reactors
fortran
References: None |
Problem Statement: What is the difference between Hysys Oil Manager and Refsys Assay Manager? | Solution: User can create a petroleum assay using the options in the Refsys Assay Manager window or in the Oil Manager tab. The differences between the petroleum assays created in Refsys Assay Manager and Oil Manager are listed in the following table
Keywords: Oil Manager, Refsys Assay Manager etc;
References: None |
Problem Statement: What is the difference between various petroleum components list available under import components in Simulation Basis Manager? | Solution: Aspen RefSYS can represent all oils in a single case with a single component slate. When user imports component list from components list directory then user can see below options
Petroleum Component List
Description
petroleumComp1.cml
Various Component list from Hysys Databank & Hypo Components Normal boiling point range is defined up to 900 C
petroleumComp1_extended.cml
Various Component list from Hysys Databank & Hypo Components Normal boiling point range is defined up to 1200 C
petroleumComp1_AspenProp.cml
Various Component list from Aspen Properies Databank & Hypo Components Normal boiling point range is defined up to 900 C
petroleumComp1_extended_AspenProp.cml
Various Component list from Aspen Properies Databank & Hypo Components Normal boiling point range is defined up to 1200 C
Keywords: Refsys component list, petroleum component list etc;
References: None |
Problem Statement: The default Unit of Measure in the Planning Board is Pound (LB). This unit of measure (UOM) is used when creating new activities on the Planning Board through the GUI. When Aspen Plant Scheduler is implemented in countries where default UOM is different from Pound (LB), the Planning Board’s UOM should be changed. This | Solution: explains how to change this.
Solution
Go to the Developer tab | Commands Panel | Command line | Type: APPDATA.
This command is going to open the table called APPDATA. In this table, find the row titled: “(PBM_MODEL_UOM) Model UOM (entry in UOM)”. The entry in this row, is the current UOM of the Planning Board.
Go to the command line and type: UOM. This would open a set called UOM which lists out all the unit of measures.
Any of the entries in the “Code” column of this set can be entered in the above mentioned row of the APPDATA.
Keywords: PB
UOM
Unit
References: None |
Problem Statement: Is it possible to number RadFrac stages from bottom to top? | Solution: Aspen Plus internal calculations are always performed using a top-down stage numbering convention. However the RadFrac text report can be customized to present the results in a bottom-top numbering convention. The bottom-top stage numbering convention may be enabled on the RadFrac's Report | Profile Options sheet in the Format for hardcopy report area. It is not possible to change the order in the graphical user interface.
Keywords: MM RADFRAC REPORT
References: None |
Problem Statement: Aspen Plus can report the pH of a stream as a Prop-Set property. What assumptions are made in the calculation of pH in Aspen Plus, and what will cause the pH to be out of the range 0 <= pH <= 14 ? | Solution: The pH of any aqueousSolution or stream in Aspen Plus can be calculated using the property-set (Prop-Set) property PH. This property is based on the water dissociation equilibrium:
2
H2O
<===>
H3O+
+
OH-
or
H2O
<===>
H+
+
OH-
Note: Aspen Plus can treat acidic species as either H+ or H3O+. However, use of H3O+ is strongly recommended, because the presence of H3O+ in theSolution chemistry is better able to represent the phase and chemical equilibrium of almost all electrolyte systems.
By definition, the pH value is the negative base 10 logarithm of the (relative) ion activity of the hydronium ion inSolution. The pH reported in Aspen Plus is calculated on a molality basis, i.e. the definition of pH as used in the built-in Prop-Set is
pH [Aspen] = - log [a(H3O+)]
a(H3O+) : activity of H3O+ inSolution on a molality scale
The activity of H3O+ on a molality scale is equal to
a(H3O+) = xm(H3O+) * gamma(H3O+)
xm(H3O+) : molality of H3O+
gamma(H3O+) : activity coefficient on a molality basis
Molalities can be reported using the Prop-Set property MTRUE, activity coefficients on a molality basis can be reported using GMTRUE. Example: In the example file (pH.bkp), the Fortran block PHCALC is used to re-calculate the pH for stream OUT. The result which is printed to the Control Panel shows a perfect agreement between this value and the one reported in the stream report.
A more common definition of pH is:
pH [Other] = - log [M(H3O+)]
M(H3O+) : molar concentration of H3O+
The two definitions are not exactly equivalent. An explantion is available on page D-144 of the CRC Handbook of Chemistry and Physics (70th edition, 1989-90). This states that:
pH [Aspen] = pH [Other] + 0.014 * (pH [Other] - 9.2) for pH > 9.2
= pH [Other] + 0.009 * (4.0 - pH [Other]) for pH < 4.0
For all practical purposes, however, the properties pH [Aspen] and pH [Other] are equivalent.
The usual range for pH values is 0 <= pH <= 14. However, values outside this range are possible.
Two cases can be distinguished:
pH < 0
This corresponds to a high acid concentration. Using the pH definition, we can see that pH = 0 corresponds to an H3O+ activity of 1. Accordingly, any pH < 0 corresponds to an H3O+ activity > 1. H3O+ activities larger than unity imply very high acid molalities. This is demonstrated in the example file. A sensitivity analysis is used increase the amount of acid in the feed. The pH, the molality and the activity coefficient as well as the product of the two are reported as a function of the amount of acid added to the system. At high acid concentrations, the pH becomes negative. Conclusion: For concentrated aqueousSolutions of acids it is possible to have negative pH values, if the H30+ activity is larger than unity.
pH > 14
This corresponds to a high base concentration. At the same time, it implies a very small H3O+ activity since nearly all H3O+ is consumed by the excess OH-. For example pH = 14 is equal to 1E-14 for the H3O+ activity. A pH of 15 corresponds to an H3O+ activity = 1E-15. A small uncertainty such as a rounding error in the H3O+ activity can cause the pH to be significantly different, and it is obvious that such small numbers cannot be used for a reliable pH prediction. For this reason, Aspen Plus has a built-in mechanism to obtain the pH from the pOH value at high OH- activities.
Values outside the range of 0 to 14 are possible, however; pH predictions which are outside the usual range of values imply extemely high acid or base concentrations. The thermodynamic model used could predict unreliable results in this composition range. The user should verify that the thermodynamic model applies to this concentration range.
If you are interested in learning more about pH, we recommend the following reference:
Bates, R. G., Determination of PH: theory and practice, New York: John Wiley & Sons, Inc., 1964.
Keywords: pH
Electrolytes
References: None |
Problem Statement: What is the meaning of Multiplier Shift on the Shift Props page of the Assay tab of the Assay Manipulator? | Solution: Multiplier shift: When checked, property curve will be shifted up and down by a common multiplication factor. If not, there will be a common addition factor applied to the property curve to match the given bulk value. The multiplication option is recommended.
Keywords: Multiplier Shift
References: None |
Problem Statement: The XPRESS optlog file name is restricted to 8 characters. You have several users that could potentially solve the same case but may not save it. Typically, you will suffix the optlog with initials and datetime stamp. However XPRESS log files does not accept a name greater than 8 characters which makes it very hard to make it unique for every solve. Is there a way to increase the log name greater than 8 characters? | Solution: The log file name is hard coded and cannot be changed. A suggested naming structure would be xxmmddyy.log
Keywords: optlog
XPRESS
References: None |
Problem Statement: Which petroleum properties can be configured with bulk property data without the curves? | Solution: Please note that thisSolution is applicable for Aspen HYSYS Petroleum Refining V7.3 but not for the older version.
The following is the list of petroleum properties which can be added in the macro-cut table without having data at different cut points.
Sulfur content
Nitrogen content
Basic nitrogen content
Conradson carbon content
Asphaltene content
Nickel content
Iron content
Sodium content
Copper content
Wax content
The assumption here is that these properties behave monotonically and concentrated in the heavier fraction. The same assumption can not be applied for other properties such as paraffins, naphtenes and aromatics. These properties are not expected to follow any particular statistical function and this is the reason why the users need to specify curves for these properties. These properties will not be populated to the stream with only bulk properties. The users need data for at least two cut points as shown in screenshot below.
Keywords: Macro-Cut Table, Petroleum Properties
References: None |
Problem Statement: Can Aspen Plus be used to model polytropic expansion?
Why do I get the following error message about improper outlet pressure specification when I run my Compr block?
*** SEVERE ERROR
IMPROPER OUTLET PRESSURE SPECIFIED FOR THE GIVEN UNIT INPUT PRESSURE = (0.6895E+06) OUTPUT PRESSURE = (0.1379E+06)
SKIPPING REST OF THE BLOCK CALCULATIONS DUE TO INPUT ERRORS. | Solution: Aspen Plus can not model a polytropic expansion process. The only option for modelling expansion turbines is Isentropic.
In the attached example file, both of the Compr blocks are set to expand the inlet gas stream from 100 psia to 20 psia outlet pressure.
The Compr block POLYTROP is specified to expand through a polytropic path and will produce the above mentioned error message
about improper pressure spcification in the Compr block POLYTROP.
The Compr block ISENTROP is specified to expand through an isentropic path and will give an outlet conditions of 20 psi and 56.8 F. An isentropic efficiency could be added if desired.
Keywords: expander
References: None |
Problem Statement: What is Kinematic Viscosity @ X C in petroleum properties? | Solution: Kinematic viscosity is calculated for the liquid phase & the default value is 37.78 C (100 F).
The value for temperature can be specified in the correlation manager (Tools/Correlation Manager)
First, pressure is determined using TV flash (Vapor fraction = 0) and then the kinematic viscosity is determined at this condition.
Please Note sometimes HYSYS TV flash returns two liquid phases and one happens to be a very heavy liquid. The resulting viscosity for this case is generally higher than than that of a single liquid phase. If you are not expecting two liquid phases, you should modify the maximum number of phase settings in the basis environment.
Keywords: Kinematic Viscosity, Refsys Viscosity, Petroleum Viscosity, etc;
References: None |
Problem Statement: How do I update initial values for calibration factors after running a calibration in Aspen HYSYS Hydrocracker? | Solution: The initial values for the calibration factors are updated after running a calibration if the user re-checks the box for Update Initial Value.
Keywords: Hydrocracker, calibration, Initial value
References: None |
Problem Statement: What do the different flow regimes mean in the results of the pipe model? | Solution: Please see attached word file for descriptions and diagrams.
Pipe and Pipeline predict patterns, often called flow regimes, for two-phase horizontal and upward flow. For horizontal flow, the method of Taitel and Dukler, 1976 is used. For upward flow, the method of Taitel, Bornea, and Dukler, 1980 is used.
The flow regimes Pipe and Pipeline use are described below.
Flow Regime
Description
All Liquid
Not two-phase flow; only liquid present.
All Vapor
Not two-phase flow; only gas present.
Bubble
In upward flow, pipe nearly filled with liquid, with small bubbles of vapor throughout the pipe.
Dispersed Bubbly
Pipe nearly filled with liquid with very few small bubbles, widely dispersed in vertical flow, or small bubbles mainly near the top of the pipe for horizontal flow.
Missing
Not calculated because block was not run.
Mist
The gas phase occupies most of the pipe, and the bulk of the liquid is entrained as small droplets carried in the gas, or is carried along the walls.
Slug
The liquid phase is continuous, but a large amount of gas exists in large bubbles. For upward flow, these bubbles nearly fill the pipe cross-section.
Stratified
In horizontal flow, the liquid and gas form two separate, smoothly-flowing layers.
Transition
In upward flow, a churning, chaotic flow in which either or both phases may be discontinuous.
Undefined
Flow regime not calculated for downward flow or error condition.
Wave
In horizontal flow, the liquid and gas form two separate layers with a rippled or wavy interface.
Keywords: None
References: s
Taitel, Yehuda and A. E. Dukler; A Model for Predicting Flow Regime Transitions in Horizontal and Near Horizontal Gas-Liquid Flow; AIChE J., vol. 22, no. 1, January 1976; pp. 47-55.
Taitel, Yehuda; Dvora Bornea; and A. E. Dukler; Modelling Flow Pattern Transitions for Steady Upward Gas-Liquid Flow in Vertical Tubes; AIChE J., vol. 26, no. 3, May 1980; pp. 345-354. |
Problem Statement: Jump Start: Visbreaker Model in Aspen HYSYS Petroleum Refining | Solution: This document is intended as a “getting started” guide. It will cover the process of creating a Visbreaker model, including how to set up a heavy crude feed with a petroleum assay, configure a Visbreaker unit operation, calibrate the Visbreaker unit, and set up a simple component splitter.
Keywords: Visbreaker Model, V8.4, Aspen HYSYS Petroleum Refining
References: None |
Problem Statement: It is possible to vary the Feed Rate in a RadFrac Design Spec and Vary. The Feed Rate variables is hardwired to be mole-flow. Is it possible to enter the flow in units of mass-flow. | Solution: Unfortuntely, this can not be done in the current system since the block does not have the information about the basis of the stream flow. Mole-flow units must be used.
Keywords: radfrac
FEED-FLOW
References: None |
Problem Statement: How does one import an Aspen HYSYS assay into Aspen HYSYS Petroleum Refining (RefSYS)? | Solution: Below are the steps required to import an Aspen HYSYS Assay to Aspen HYSYS Petroleum Refining.
Note: User should have Hysys Petroleum Refining License
Enter the Simulation Basis.
Click on Extend Simulation Basis Manager button. It is at the bottom of the Simulation Basis Manager window. The RefSYS: Petroleum Assay Manager window should appear.
Click on the Add/Import button. THe Petroleum Assay window appears.
Change the name of the assay if desired.
Select the Fluid Package under Associated Fluid Package field.
Click on the HYSYS Oil button.
Select the HYSYS assay from the Select Assay drop down list.
Click OK.
Return to the Simulation environment and open the PFD.
Double click on the desired oil stream.
Go to Worksheet | Composition page.
Click on Extend Stream Functionality button.
Select the Petroleum assay from the dropdown list.
Close the above window.
Keywords: Petroleum Assay, RefSYS Assay, HYSYS to RefSYS
References: None |
Problem Statement: What type of numerical algorithm is used for RGibbs - Gautam-Seider, NASA, or RAND? Can it handle multiple pure solids? | Solution: The algorithm to minimize the Gibbs free energy function used in RGibbs is Gautam-Seider. It can handle multiple solids.
Some optimization approaches typically have employed Newton type methods so that theSolutions found are highly dependent on starting point, and localSolutions can at best be guaranteed. The tangent plane distance criterion first proposed by Gibbs in 1873 is important in the search for equilibriumSolutions corresponding to a global minimum of the Gibbs free energy. Given an equilibriumSolution that satisfies the condition of equipotentials, it is possible to determine if the Gibbs free energy associated with thisSolution can be reduced to provide an improvedSolution. Gautam and Seider (1979) use the tangent plane criterion in conjunction with the minimization of the Gibbs free energy and then combine a phase-splitting algorithm to improve the reliability. No approach can provide any theoretical guarantee that the global minimum of the Gibbs free energy will be obtained in all cases.
Keywords: rgibbs
References: s
Gautam and W.D. Seider. Computation of phase and chemical equilibrium, Part II: Phasesplitting. AIChE J., 25(6):999, 1979. |
Problem Statement: What's New in Aspen HYSYS V7.2 - Refinery Reactor Calibration | Solution: HYSYS Petroleum Refining (RefSYS) introduces rigorous refinery reactor models into HYSYS based flowsheets. The reactor models are available from the RefSYS palette (F6) shown below:
The following reactor models are available:
Cat Cracker for FCC units
Hydrocracker for multi-bed hydroprocessing units
Reformer for naphtha reforming units
ISOM for C5 isomerization
HBED for single bed hydroprocessor units
These reactor models are calibrated in two different ways: manually from simulation views or from special calibration environments.
Manual Calibration: ISOM and HBED
These two models represent standalone reactor beds in either isomerization or hydroprocessing units. They can be used to represent single bed units or connected together to form multi-bed units. They are manually calibrated to match plant data. Specifically, the tuning factors (kinetic coefficients) are exposed on simulation views. The user would change these in trial and error to match a condition. These models are best used on simple units that are not hard to calibrate.
Calibration Environments: Cat Cracker, Hydrocracker and Reformer
These models come with wizards that help the user configure the model to match a complex unit and to provide a calibration environment. The calibration environments provide easy to use views for inputting plant measurements that will be matched automatically by the model in a calibration run. Cat Cracker is used for all FCC types including units with two risers or two regenerators. Reformer is used for semi-regen or continuous catalyst recirculation naphtha reforming units with three to six reactor beds. Hydrocracker is used for multi-bed hydroprocessor units with quench gas streams.
Keywords: Refinery Reactor Calibration, What's New, New V.2, Calibration
References: None |
Problem Statement: What is the SI Top and SI Bottom number in Petroleum Distillation Column? | Solution: SI Top & SI Bottom are called fractionation indices. SI Top & SI Bottom signifies how good the separation between the products (Distillate and Bottoms) is. Refer to the attached documentation from AspenHYSYSRefiningV7_2-Ops.pdf, page 6-4 of AspenHYSYSRefiningV7_2-Ops.pdf shows ln(Di/Bi) vs NBP.
SI Top = -1/S1 and SI Bottom = -1/S2.
The slope of the curve signifies the extent of imperfect fractionation. As S tends to zero, there is virtually no separation (S1 Top = -1/0 = ~ infinity), and inversely as S tends to negative infinity (S1 Top = -1/-infinity = zero), the separation is almost perfect. The position of the curve horizontally is decided by the overall distillate and bottoms flow distribution. Since S1 Top = zero represents perfect separation, that you do not get it in reality. So value of 5 is normally used for practical purpose as a starting point. Then you can calibrate the column with the plant data and get more realistic value.
HYSYS assume that the slopes of the curves drawn above are only a characteristic of the structure of the column, and are independent of the feed or the pressure or other operating conditions. This assumption enables HYSYS to calculate the product composition of the distillate and bottoms streams, for a wide range of feed conditions. Furthermore, HYSYS assume that all Petroleum Columns are in indirect sequence of simple columns.
Keywords: SI Top , SI Bottom
References: None |
Problem Statement: What is Data Regression (DRS) testing when it says TEST LIQUID LIQUID EQUILIBRIUM RESULTS AGAINST THREE PHASE FLASH ALGORITHM? | Solution: All data regression systems based on minimization of Gibbs free energies perform only local minimum analyses. Thus, they only find local minima instead of the global minimum. This leads to potential cases where the local minimum conditions may be satisfied for more than one set of parameters. Therefore, as with other numerical techniques (e.g., Newton), the use of different initial guesses may lead to different local minima. In such cases it is advisable to try different initial guesses and explore the full range of parameter values. The acid test is the evaluation of the parameter descriptions using flash calculations.
Testing the LLE equilibrium results against a 3-PHASE FLASH ALGORITHM is related to the discussion above. Liquid-liquid equilibrium systems are more prone to show multiple local minima. Therefore, the 3-PHASE test is an attempt to resolve the question of whether or not the converged parameters satisfy the condition for a global minimum of Gibbs free energy. Assuming consistent thermodynamic data, this test (comparing flash calculations vs. experimental data) is successful if the DRS actually converged in the vicinity of a true stable minimum. The predicted compositions are generally not satisfied in the case of a metastable or unstable local minimum.
Recall that DRS does not minimize the Gibbs free energy and just matches the fugacities. This is a necessary but not sufficient condition for stable LLE. Therefore, the flash calculations are made to ensure that a Gibbs free energy global minimum has been reached.
Keywords: None
References: None |
Problem Statement: I want to increase the octane number of some of my gasoline blending stocks in order to run quick 'what-if' scenarios. I don't want to run a full simulation of my refinery for each scenario. How can I do that? | Solution: TheSolution here is to use the Assay Manipulator unit operation in Aspen RefSYS. The Assay Manipulator is used to shift or change petroleum properties for a stream in your simulation.
Add an Assay Manipulator through the RefSYS Object Palette (F6) or through the Flowsheet | Add Operation | Refinery Ops | Manipulator item in the main menu.
To use the Manipulator to specifically change the Research Octane Number (RON) for the straight-run Naphtha stream in the attached case, follow the steps below (the completed example is attached):
1. Go to the Options page of the Assay tab.
2. Select the RON (Clear) property using the drop-down list. Select the Shift Prop option (instead of the Change Props option).
3. Move to the Shift Props page. Shift the product RON number to 90 (from the current value of 40-50) as shown. The Prod ? Feed is automatically calculated.
You can shift or change as many petroleum properties as you wish using only the Assay Manipulator.
Keywords: Manipulator, octane shift, petroleum property
References: None |
Problem Statement: How to make a linear change of properties using Assay Manipulator? | Solution: In the assay manipulator you can specify the targets either entering the value for the target or a value for the difference between the product and feed. For example, if the sulphur content in the feed is 2% and if you want this to be changed to 2.5%, you can either enter this value in the target field for the product or a delta, 0.5 in the target field for Prod - Feed.
If there is a requirement to modify the property using a multiplicative factor or other linear calculations this can be implemented in a HYSYS spreadsheet and the value can be exported to any of the target fields in the manipulator. The attached example illustrates this functionality.
Keywords: Property Shift, Crude, Assay Manipulator
References: None |
Problem Statement: What is the upgrade / migration path for SMCA to DMCplus? | Solution: Will DMCplus v1.2 include tools to convert SMCA models to DMCplus?
Yes. I expect that we will make an attempt at reading the DEF file for the SMCA controller and fill in as much of the CCF file as makes sense. It will not be a completeSolution, because there are quite a few things that do not have a unique translation.
Will DMCplus v1.2 read SMCA models directly?
Yes. (probably) I think this is a necessary part of the conversion process. My uncertainty comes from not being exactly sure of what an SMCA model file contains. We can certainly convert an FIR-type model and likely could handle low-order transfer function models as well.
I think that the nit-picky answer is that DMCplus will not
read SMCA models, but that the conversion tool will convert
SMCA models (both transfer function and FIR model files)
to DMCplus model files.
Will DMCplus v1.2 include SMCA functionality? I recently asked about this as DMCplus v1.2 being a superset of DMCplus and SMCA, but what exactly does that mean?
Yes. Superset means that an SMCA controller could be upgraded to DMCplus with no loss of functionality. The DMCplus v 1.2 controller will have the ability to handle quadratic balancing of constraint violations at steady-state...the QP. We have decided that including the QP in DMCplus means that all of the essential functionality of SMCA is included within DMCplus. There are obviously characteristics of SMCA that are not exactly duplicated within DMCplus, but the same thing could be said of DMC characteristics as well...not all of them are exactly duplicated in DMCplus.
Considerations for Upgrade to SMCA 1.5
> The SMCA documentation we currently have does not give any guidance on
> the procedures for an IDCOM V3.12 to SMCA V1.5 upgrade. We would
> appreciate advice on how this would be done. We would envisage a
> stage-wise migration where SMCA was initially set up to run
> in parallel
> with IDCOM whilst individual controllers were migrated one at a time.
The attached word document (RN13.doc) contains the release notes for SMCA 1.3. It covers the upgrade procedure from a 1.2 version of SMCA. While your IDCOM-M 3.x system is somewhat different than that of an SMCA 1.2, it is still very similar in basic concepts and organization of the applications. Follow the basic outline in the RN13.doc file. Note that steps 1, 2 and 3 really do not apply to you in the How to upgrade an existing SMCA 1.2 OpenVMS system section of the document. This upgrade procedure should give you enough information to get the job done. As far a the stage-wise migration, there is no problem in installing SMCA 1.5 along-side IDCOM-M 3.x. There are no conflicting logicals or symbols between the two software packages.
I have also included the SMCA 1.5 release notes (RN15.doc) for your reference.
> Since there is no mention of the IMG function for the online SMCA, has
> this now been replaced by SMC Display ?
Yes. GCS and the SMC-Display GCS displays is required to look at the SMCA controller data.
> In regard to the offline components for SMCA, we note that the Y2K
> status on the Web is that they are 'Not to be Tested'. Since these
> are important tools for the support of SMCA applications,
> what is your
> advice concerning the use of these post 1999 ?
They should work fine past the millennium as long as you accept the fact that dates may show up in an unexpected manor, and in some cases, yield the wrong date altogether (timestamps on data in SMC-Model for example). You should be able to work around them without any major problem.
Keywords: DMCplus
SMCA
References: None |
Problem Statement: What types of Data can be used to regress a parameter, such as the Ideal Gas Heat Capacity, CPIG? | Solution: The following table summarize the types of data used to regress various parameters.
This list is not exclusive, and contains the most commonly regressed parameters.
Parameter name
Model
Property method
Data types you can use *
BWRKV,BWRKT
BWR-Lee-Starling
BWR-LS
VLE, LLE or VLLE Data,
KVL, KLL
CPIG, CPIGDP
Ideal gas
heat capacity
All
CPV, HV, CPVMX, HVMX,
CPL, HL, CPLMX, HLMX
CPLDIP
DIPPR Liquid
heat capacity
+++
CPL, HL, CPLMX, HLMX
DHVLWT, DHVLDP
HLMX
Watson/DIPPR
Heat of vaporization
**
DHVL, CPL, HL, CPLMX,
NRTL
NRTL Activity
Coefficient
NRTL+
VLE, LLE, VLLE Data,
HLXS, GLXS, GAMMA, KVL, KLL
OMGRKS, OMGPR,
OMRKSS, OMGRKA,
OMGRKU
Equations of state
RKS-BM
PENG-ROB
RKS-SOAVE
RK-ASPEN
SR-POLAR
TP (vapor pressure)
GMUFB
UNIFAC
UNIFAC
UNIF-LL
VLE, LLE VLLE data
HLXS, GLXS, GAMMA, KVL, KLL
WILSON
Wilson Activity
Coefficient
WILSON+
VLE Data, HLXS, GLXS,
GAMMA, KVL
UNIQ
UNIQUAC Activity
Coefficient
UNIQUAC+
VLE, LLE VLLE data
HLXS, GLXS, GAMMA, KVL, KLL
VANL
Van Laar Activity
Coefficient
VANLAAR+
VLE, LLE VLLE Data,
HLXS, GLXS, GAMMA, KVL, KLL
HENRY
Henry's Law
***
VLE data, HNRYMX
HOCETA
Hayden O'Connell
****
VLE data, VVMX, HVMX,
CPVMX, VV, HV, CPV
LKPKIJ
Lee-Kelser-Plocker
LK-PLOCK
VLE, LLE VLLE Data,
KVL, KLL
MULAND,MULDIP
Andrade/DIPPR
liquid Viscosity
Ideal
MUL, MULMX
OMGCTD,VSTCTD
COSTALD liquid
molar volume
*****
VL, VLMX, RHOL, RHOLMX
PLXANT
Antoine vapor
pressure
*
PL
PRKIJ
Peng-Robinson
Equation of state
PENG-ROB
PR-BM
VLE, LLE, VLLE Data,
KVL, KLL
RKAKA0, RKAKA1,
RKAKB0, RKAKB1
Redlich-Kwong ASPEN
Equation of state
RK-ASPEN
VLE, LLE, VLLE Data,
TXX, TXXY, KVL, KLL
RKSKIJ
Redlich-Kwong-Soave
Equation of state
RK-SOAVE
RKS-BM
VLE, LLE VLLE Data
KVL, KLL
RKTKIJ
Rackett mixture
liquid molar volume
++
VLMX, RHOLMX
RKTZRA, DNLDIP
Rackett/DIPPR
liquid molar volume
++
VL, RHOL
RKUKA0, RKUKA1,
RKUKB0, RKUKB1,
RKUKA2, RKUKB2,
RKULA0, RKULA1,
RKULA2
SR-Polar
Equation of state
SR-POLAR
VLE, LLE VLLE Data,
KVL, KLL
WATSOL
Water Solubility
IDEAL
WATSOL
Note: VLE refers to TPXY, TXY or PXY data-types,
LLE refers to TXX, PXX or TPXX data types and
VLLE refers to TPXXY, TXXY or PXXY data types.
* These data types can be specified on the Properties Data form.
** Any activity coefficient option set can be used, but we recommend that you
use the Ideal option set when regressing these parameters.
*** Any activity coefficient option set with Henry's Law.
**** Any activity coefficient option set with Hayden O'Connell EOS model for the
vapor phase.
***** You must modify the option set to use the COSTALD model. No built-in
option sets use this model.
+ Use this option set or its variants
++ Any option set that uses the Rackett model.
+++ Any activity option set that uses the route DHL09.
Keywords: None
References: None |
Problem Statement: How do I configure the Aspen Petroleum Scheduler Integration Configuration tool in order to send information from Aspen PIMS to Aspen APS? How do I visualize that in APS? | Solution: In the next example the Volume sample model from PIMS and the demo model from APS are used.
In APS follow the next steps:
1.-Delete the Information from the next Access tables:
ORION_MGR_PIMS_KPI_DATA
ORION_MGR_PIMS_KPI_TAG
ORION_MGR_PIMS_KPI_IMPORT
2.- Go to Integration/Pims to APS/ Map Planning targets and there must be no values on the dialog box:
Also, there must be no information in the Planning target screen.
For APS integration configuration services tool follow the next steps:
1. Open the program as administrator:
2. It will ask for the name of the machine and some ports. If the ports selected are not open you will need to open them using the Windows Firewall:
a. To open them, go to the Windows Firewall with advanced security:
b. And configure a new Inbound rule with the ports desired.
3. Ports 9999, 9998 and 9995 are the default ports.
4. Â Select the model where you want to send the data. If it is a .dsn file, it will need the user and password to access the server:
5. Test the service connection and click finish:
On PIMS software you need to follow the next steps:
1. Open PIMS and open the Volume Sample model and solve the matrix for the Base case:
2. Go to Integration/Configuration
3. Enter the name of the machine and the port corresponding to APS End Point discovery (9995 is the default) that was set up in the APS integration configuration services step.
4. Click the test button and the next dialog box should prompt:
5. Go to Integration/Production Targets
6. Select the targets that you want to pass to APS. In the next example I have passed the activities of JET, DSL and HSF, in order to achieve that you must select the case (1-Base Case) and then check the box of the product; this will send the information to the spider graph. Then you need to click the red arrow to pass them to the targets dialog.
Make sure that the Start date and End date match the horizon that you are analyzing in APS (this case 6/1/2011 – 6/15/2011).
7. Click the send button:
8. The next dialog box should appear:
Check in the data base that the next tables got new entries:
ORION_MGR_PIMS_KPI_TAG
ORION_MGR_PIMS_KPI_DATA
To visualize the data sent:
1. Load the demo model in APS.
2. Go to Integration/PIMS to APS/Map Planning Targets
3. The next dialog box should appear:
4. Map the required parameters and click OK:
5. Go to Planning targets pane and add a new screen, edit the KPI trends of the screen and add the desired trends:
6. The trends and information should appear on the screen:
7. Simulate all to see the scheduled plots:
Keywords: Integration services, KPI, import, targets, Planning Targets
References: None |
Problem Statement: Is there an automation call to detect the user's current/active event screen name? | Solution: There is an automation call named GetScreenName(), which returns the current Gantt screen name.
The automation call GetScreenName() as per the following VBA syntax.
Sub DisplayEventScreen()
Dim pssl As Object
Set pssl = CreateObject(Orion.CollectionInterface)
Dim result As String
Dim abcd As Long
abcd = pssl.GetScreenName(result)
Set pssl = Nothing
End Sub
Keywords: Automation, VBA, GetScreenName(), Gantt screen
References: None |
Problem Statement: The liquid product from the vessel contains vapour when the level of the vessel goes low. | Solution: The nozzles in the vessels are side ways. When the liquid level becomes less than the diameter of the bottom pipe nozzles then vapour will come out with the liquid product.
It is necessary to provide the correct diameter of the nozzles to accurately represent the vessel operation. You can access the nozzle setup page via Rating and Nozzles in the vessel setup page (see the screenshot below).
Keywords: Vessel, Nozzle
References: None |
Problem Statement: What tables are affected when using Aspen PIMS to Scheduler Interface? | Solution: 1. When we import events from OrionPimsInt.exe, the records are added to stage tables. We can use Import->Events in APS to import the events.
2. When we delete events from OrionPimsInt.exe, the records are only deleted from the stage tables. The events which were added to core tables will not be affected.
Keywords: Aspen PIMS to Scheduler
Integration Tables
References: None |
Problem Statement: After installing Aspen Petroleu Scheduler / Aspen Refinery Multi-Blend Optimizer, the Aspen Excel Integration Utility (EIU) is not shown in the Excel Addins. When the user tries to install it by double clicking the .vsto file from the excel utility folder (C:\Program Files (x86)\Common Files\AspenTech Shared\ExcelUtilities), the error message below shows:
Unable to install this application because an application with the same identity is already installed. To install this application, either modify the manifest version for this application or uninstall the preexisting application. | Solution: Open folder
C:\Users\[your window logon id]\AppData\Local\Apps\2.0
Underneath, there are some folders named with combination of numeric and characters.
Click each folder to go into its subfolder until you can see files. If the user sees any file name started with ‘asp’ then remove its parent folder. For example, if YKLJAEMY.Y1C folder's subfolder contains file started with asp, then delete folder YKLJAEMY.Y1C. Do the same for all the other folders under ‘C:\Users\[your window logon id]\AppData\Local\Apps\2.0\’, including ‘data’ folder.
Now, try to double click the .vsto to install EIU.
Keywords: unable
vsto
manifest
References: None |
Problem Statement: Adding date/time stamp to print file name | Solution: The DMCplus Online help states:
ACOD_PRT_FMT Determines the format of the date appended to the name of .prt files. PRT files are output once per cycle when the PRTSWC entry is greater than 0. PRTSWC is decremented at the end of each cycle. Valid values are:
%d: day of the month (01-31)
%m: month (01-12)
%y: 2-digit year without century (00-99)
ACOD_DATTIM_FMT Determines the format of the date and time string displayed when messages are listed from Manage (running Manage and selecting Display the Messages). ACOD_DATTIM_FMT also affects the format of the date and time displayed when the controllers are listed (running Manage and selecting List Controllers.) Valid values are:
%a: abbreviated weekday name
%A: full weekday name
%b: abbreviated month name
%B: full month name
%d: day of the month (01-31)
%H: hour (24-hour clock) (01-24)
%I: hour (12-hour clock) (01-12)
%M: minutes (00-59)
%p: local equivalent of AM/PM
%S: seconds (00-59)
%Y: 4-digit year with century
Windows NT systems
1 Right-click the My Computer icon on the desktop.
2 Select Properties.
3 Select the Environment tab.
4 Click on any of the System Variables. The Variable name and its Value appear in the text boxes below. Replace these with the appropriate environment Variable name and format string Value that you wish to define. For example:
Variable Name: ACOD_DATTIM_FMT
Variable Value: %A %B %Y %I:%M:%S %p
5 Click Set. Verify that the new environment variable has been added in the System Variables window.
6 Click OK to close System Properties window.
7 Reboot the computer to use the new settings.
Note: Modifying the value for an existing system environment variable only requires a restart of ACO Base.
Windows 2000 systems
1 Right-click the My Computer icon on the desktop.
2 Select Properties and then select the Advanced tab.
3 Click Environment Variables?. The Environment Variables dialog displays.
4 Under System Variables, click New. The New System Variable dialog displays.
5 Enter the Variable Name and then enter the format string in Variable Value. For example:
Variable Name: ACOD_DATTIM_FMT
Variable Value: %A %B %Y %I:%M:%S %p
6 Click OK and then verify that the new environment variable has been added in the System Variables window.
7 Click OK to close the Environment Variables? dialog.
8 Click OK to close System Properties window.
9 Reboot the computer to use the new settings.
Note: Modifying the value for an existing system environment variable only requires a restart of ACO Base.
1996-2003 Aspen Technology, Inc.
NOTE:
A consideration regarding this online help information includes:
The Microsoft website states that a reboot is needed after changing an existing system environment variable on XP.
Our experience is that this is also true for Windows 2000 SP4.
Changes do not seem to take affect by stopping/starting ACOD base when changing system variables.
Not confirmed for user environment variables.
The following strings can be used to add the date/time to the print file name:
_%Y-%m-%d_%H%M or %y%m%d%H%M
Which inserts the following before the .prt:
_2007_05_18_1301
Note: - and _ appear to work. : did not work. Not sure about /.
Keywords: DMCplus, print, file, acod_prt_fmt, format, date, time
References: None |
Problem Statement: Installation of the CM50S Cim-IO server fails during the VMSINSTAL phase.
%CIMIO_CM50S0-E-NOCM50, Cannot determine CM50S version.
%VMSINSTAL-E-INSFAIL, The installation of CIMIO_CM50S0 V32.3 has failed. | Solution: The CIMIO CM50S Server software installation and startup scripts determine the version of CM50S by using the Logical CM50$VER. If they cannot find this logical or if the logical does not have the correct format the installation or startup will fail. The logical can be displayed by using the show logical command:
$ SHO LOG CM50*
If the CM50$VER is not present or does not have the form
CM50$:[R041]
either the CM50 installation is faulty or the CM50 software is not running.
The CM50$VER logical is automatically unassigned whenever the CM50 software is stopped or when the CM50 software fails to start properly. This means that you cannot install our CIMIO CM50S Server software unless the CM50 software is running.
NOTE: In Japan the CM50$VER logical has the form CM50$:[JR041] which causes the installation and startup to fail. To get around this problem, define a group logical during the installation that matches the release level ;
$ define/group CM50$VER CM50$:[R041]
and modify the CIMIO_CM50S_START and CIMIO_CM50S_STOP com files so that they have the group logical defined in them as well.
Keywords:
References: None |
Problem Statement: 'No Composite licenses available on server.' message is logged in a CLP err file, and the CLP cannot start. Even if the mal-entries and mal-settings of the member Aspen DMCPlus controller were the cause of the problem. | Solution: ImplementingSolution 120532 which enables to log the member Aspen DMCPlus controllers problems.
Keywords: composite licenses
Applicable version 6.0.1 only
References: None |
Problem Statement: After transitioning to Aspen HYSYS Dynamics, a pipe segment will report the following warning:
Operation <<Pipe name>> has an uninitialized stream which is needed for a volume balance.
Please copy over another stream or provide initial conditions and flash it.
In most cases, the Integrator will stop giving further numerical errors. At times, the calculation can continue if the solver is able to recover, however the warning message will be persistent throughout the run. | Solution: The problem is caused by corruption of the holdup k-values calculated during the transition. The only way to eliminate the erroneous k-values is to rebuild the corresponding pipe segment.
Obvious symptoms of this problem include strange k-values as seen in the Performance | Segments pagetab when first switching to Dynamics mode, followed by the above warnings in the trace window.
Please refer to Knowledge BaseSolution 115648 for pipe k values calculations.
Keywords: Pipe, k value, dynamics, uninitialized stream, volume balance
References: None |
Problem Statement: How to obtain the symmetrical (GAMMA) and asymmetrical activity coefficient (GAMUS) in user subroutine? | Solution: GAMUS is for unsymmetrical molecular species (i.e. those in the Henry's list) and GAMMA is for all other components (include charged species like electrolytes)
There are different ways to get the symmetrical and asymmetrical activity coefficients:
1. Retrieve the binary interaction parameter for the activity coefficient model used through the PLEX. Before version 2006, the plex offset was in the IPOFF3_IPOFF3 array where the offset for GAMMA was LGAMMA = IPOFF3_IPOFF3(24), offset for GAMUS was IPOFF3(29). In version 2006 and higher the offset is in the DMS_ALIPOFF3 array where the offset for GAMMA is LGAMMA =DMS_ALIPOFF3(24) and the offset for GAMUS is IPOFF3(29). SeeSolution 121621 for more details.
2. In a regular Aspen Plus run, access GAMMA or GAMUS by setting up a prop-set. If GAMUS is accessed, make sure Henry's law and components are specified.
3. In a user subroutine, access GAMMA or GAMUS through a labelled common by setting up a prop-set in the properties plus run. If GAMUS is accessed, the component must be declared as Henry's component and the Henry's binary must exist. Otherwise, GAMUS is not available.
4. In a user subroutine, call the phase monitor and then use the labelled commons to get GAMMA. Then call the phase monitor again with a hypothetically very low concentration to obtain GAMMA, which effectively is GAMMA at the infinite dilution. Then GAMUS = GAMMA/GAMMA (infinity)
Keywords: Gamma, activity coefficient, user subroutine
References: None |
Problem Statement: How do you use an activity coefficient property method to model a system that consists of non-water polar compounds and light gases modeled as Henry components when no binary data exists for the Henry components? | Solution: TPXY or Henry Constant data can be used to regress the Henry parameters using the Data Regression System. Without any data there are a few options:
1. See if there are Henry parameters for the Henry components and some other common polar compound such as benzene or cyclohexane by adding some of these components to the Component list and seeing if any additional pairs appear on the Henry parameter sheet. Copy these parameter values for the polar components in the system. The additional components can then be deleted.
2. Use the Henry parameters for water.
3. Don't use Henry components. If an activity model is used, but Henry-comps is not used because the data is unavailable, the property method should be modified to take out the Poynting correction, otherwise the light gases may all be in the liquid phase. Do this by checking Modify property models on the Properties | Specifications | Global sheet and then un-checking Poynting correction.
This causes the liquid pure component fugacity to be calculated using Extended Antoine, Ideal Gas models with no Poynting correction.
For greater accuracy, TPxy data MUST be found and Henry parameters regressed.
Keywords: henry-comp
PHIL00
gamma
gamma model
References: None |
Problem Statement: We have seen in some cases that the simulator shows different values when using OXE and when not using it. How can I identify the cause of the problem? | Solution: In order to identify the root cause follow the next steps:
1. Change the DBGINFOLEVEL to 1000 in the config table.
2. This setting will slow down the simulation a lot because it will write all the calculations in debug file; formula and calculated value. So, we recommend to reduce your number of model days; 3 days for example.
3. Open APS and simulate all with OXE turned on.
4. Go to the working folder and in the model folder you will find the ORIONDBG file.
5. Use Find to find all EMPTY words. If you have find any, write the cell and spreadsheet where the formula is calculating EMPTY values.
6. Check the cells in the units workbook (This debug file has all the information from all the periods so you will find a lot of EMPTY words, but is highly probable that is the problem is in the same cell).
7. Correct the cells by checking the APS help file of the excel function that is causing problems. Some functions require all arguments or additional considerations to work with OXE.
8. Changed the debug level back to 1 and publish without OXE. After publishing, send all the information from _ZSTRMS to a new table; you can use the SQL SELECT INTO Statement. Send the information to a new NOOXE table for example.
9. Turn on OXE, publish and send _ZSTRMS information to another table; OXE for example.
10. Run the next script to compare the tables; where [DATABASE] is the name of your database:
SELECT CASE WHEN t1.[CASE] is not null THEN t1.[CASE] ELSE T2.[CASE] END AS [CASE]
,CASE WHEN t1.[DATE_] is not null THEN t1.[DATE_] ELSE T2.[DATE_] END AS [DATE_]
,CASE WHEN t1.[ID] is not null THEN t1.[ID] ELSE T2.[ID] END AS [ID]
,CASE WHEN t1.[PROP] is not null THEN t1.[PROP] ELSE T2.[PROP] END AS [PROP],t1.[VALUE_] AS VALUE__L
,t2.[VALUE_] AS VALUE__R
,(CASE WHEN abs(t1.[VALUE_]) < 1.0 THEN abs(t1.[VALUE_] - t2.[VALUE_]) ELSE abs((t1.[VALUE_] - t2.[VALUE_])/t1.[VALUE_]) END) AS DIFF
FROM [DATABASE].dbo.NOOXE AS t1 FULL OUTER JOIN [DATABASE].dbo.OXE AS t2 ON
t1.[CASE] = t2.[CASE]
AND t1.[DATE_] = t2.[DATE_]
AND t1.[ID] = t2.[ID]
AND t1.[PROP] = t2.[PROP]
WHERE ((CASE WHEN abs(t1.[VALUE_]) < 1.0 THEN abs(t1.[VALUE_] - t2.[VALUE_]) ELSE abs((t1.[VALUE_] - t2.[VALUE_])/t1.[VALUE_]) END) > 1.0e-5)
OR t1.[CASE] is null
OR t2.[CASE] is null
ORDER BY [CASE], [DATE_], [ID], [PROP]
11. If there are no differences, the next result will be shown:
12. If differences are shown, you will have to go to the units workbook, pay attention to the CELLS that are calculating that PROPERTY and go back to step 7.
We recommend you to pay attention to IF statements, VLOOKUP and ISMATCH, because we have found that most of the time they are the root cause of the problem.
Keywords: OXE, debug, DBGINFOLEVEL, ORIONDBG, differences
References: None |
Problem Statement: How can I add an assay using Petroleum Assay if I have Laboratory Assay results or Cut data. | Solution: To add an Assay using Petroleum Assays, you need to do the following.
1) Create a new simulation. You do not need to add components or a property package, you can go straight to the Petroleum Assay folder.
2) Click in the Add arrow>Manually Enter
3) You can use the Multi Cut Properties to add the assay as default. Enter the temperatures of the cuts and click Ok.
4) You will now see the Input Summary table. There, under the Whole Crude column, you can add the bulk properties and the CutYields.
5) You can add more properties by clicking on the +sign in the first empty column and selecting the property you need.
6) Once you have entered all the Assay data, all you need to do is click on Characterize Assay.
7) You should see the Results Summary table displayed.
8) Once the assay is complete, you can go into the Simulation environment, add a stream and attach to that stream the Petroleum Assay. This is done in the Petroleum Assay tab in the stream window, select Attach Existing and then select the assay.
With that we finish with the assay installation, you will only need to define the P/T/Flow conditions as in any other stream.
Keywords: Petroleum Assay, REFSYS, Cut data, Crude
References: None |
Problem Statement: A mnemonic of UNKNOWN is used whenever the CIM-IO error code is not present in any CIM-IO error file on the DMCplus computer. For the CIM-IO server, this can be because the error file
(CIMIOETC:CIMIO_CM50S_ERRORS.DEF) is from a previous version or because the error code is a Honeywell (or other DCS) return code.
If the error code is of the form 25xxx, then it probably means the error code file is out of date (and that DMCplus is being run on a different system than the CM50S CIM-IO Server.) Just copy the cimio_cm50s_errors.def from the server machine to the client machine to resolve this problem. | Solution: CM50
Honeywell return codes are either between 0 and 255 (value statuses) or they are a large number of the format 215xxxxxx (return statuses). These can be looked up in the appendices of the CM50S User's Guide or online using the @CM50$LIB:CM50 utility.
$ @cm50$lib:cm50
Use the VS option for up to 3-digit error codes like 240 and use RS option for the 9-digit error codes like 215000266.
AxM
The v1.2 CIM-IO for Honeywell OpenDDA returns 9-digit status codes. Error interpretation into text is provided starting with v1.3. These codes can be found in the cimio_t_api status return and in cimio_msg.log.
On the AxM, execute the following command:
/opt/DDA/bin/dda_xstatus
Keywords:
References: None |
Problem Statement: DMCplus and CIM-IO Kernel Compatability | Solution: Here is a table of CIM-IO Kernel versions and DMCplus versions. The consequences of each combination are given.
CIM-IO DMCplus DMCplus DMCplus
Kernel 1.04.xx 1.10.00 1.10.01
4.6b [1] [1] [1]
4.7a [1] [2][3] [1]
4.7.1 [1] [1][2] [4]
Explanation Codes
Will work OK if DCS is TDC3000 or ACS. May not properly report read and write statuses for some other devices (eg Yokagawa exaPAPI.)
Minor print file bug related to External Target information.
Writes which fail with CIMIO_STATUS_BAD are treated as if the write succeeded.
Will work OK with all devices.
Keywords: DMCplus, CIM-IO, compatability
References: None |
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