question stringlengths 19 6.88k | answer stringlengths 38 33.3k |
|---|---|
Problem Statement: What is the property GAMPC? | Solution: The property GAMPC refers to the liquid activity coefficient pressure correction and is often mistaken for the Poynting factor, which is the property PHIPC.
The built-in model in Aspen Plus for GAMPC returns 1.0 and there are no other models available. This is supposed to be a pressure correction term to acti... |
Problem Statement: How are the allowable inlet and tail pipe pressure relief losses calculated? | Solution: In most cases, the allowable loss will be set to the percent of differential pressure specified in the design rules. This will typically be 3% and 10% of differential setpoint for inlet and tail piping, respectively. However, if the vessel pressure for dynamic runs or the inlet pressure for steady state runs ... |
Problem Statement: What can the Swing Cut utility be used for? | Solution: The Swing Cut utility, which is used in conjunction with the Petroleum Distillation column, allows you to generate and export assay tables with user-specified swing cuts in PIMS format. Aspen PIMS (Process Industry Modeling System) is a production planning and optimization tool that is widely used in the refi... |
Problem Statement: How smoke point is calculated in Aspen RefSYS? | Solution: Smoke point for a stream is a calculated based on the stream blending rule provided below:
SPidx = Sum [ Vol(i) / SP(i) ]
SP = 1 / SPidx
where:
SP(i) =Smoke Point of Component i
Vol(i) =Liquid Volume Fraction of Component i
SPidx = Smoke Point Index of Stream
SP = Smoke Point of Stream
For more inform... |
Problem Statement: In doing a RBatch simulation with a vent stream, the simulation seems to be taking a very long time. The user is not sure wheather it has 'frozen' or is it simply integrating very slowly. | Solution: Increasing the diagnostics will print a one line integration diagnostic in the Control Panel.
In Aspen Plus 10, increase the On Screen diagnostics level to 5 from its default value of 4 on the RBatch / Block Options / Diagnostics sheet. In Aspen Plus 9, increase the Term-level value from 4 to 5 on the RBATCH.... |
Problem Statement: How is the accuracy and reliability of the pressure relief calculations in Aspen Plus? Do the Aspen Plus calculations meet all of the benchmark calculations for valves and flow through pipe sections? | Solution: The pressure relief system calculations meet all the benchmarks. Initially in version 9.2, there were some cases where the benchmarks were not in agreement. These cases contained a vertical outlet pipe because the pressure loss due to elevation was included in calculating the total pressure loss. This is not ... |
Problem Statement: What is the need of APED component for the use of Aspen HYSYS Petroleum Refining? | Solution: All the reactor model in Aspen HYSYS Petroleum Refining needs Equation oriented solver (EO) to solve. At present EO models can be solved only through Aspen Properties, in Aspen HYSYS. This requires Aspen Properties Enterprise Database APED (default properties database used by Aspen Properties) to be installed... |
Problem Statement: How do I model a supercritical component like N2 at ambient conditions in a mixture that is not supercritical (such as water or methanol)? | Solution: You may take one of two approaches:
Use an equation of state to model the component. If binary interaction parameters are not present in the data base, then a data regression (DRS) run with PTXY data will be needed to get a good representation of the data. To do this regress the binary interaction parameter (... |
Problem Statement: What can the Petroleum Assay utility be used for? | Solution: The Petroleum Assay utility, which is used in conjunction with characterized assays from the Petroleum Assay, allows you to obtain the results of a laboratory style analysis for your simulation streams. The object for the analysis can be a material stream or a stream phase in any stage of a tray section, sepa... |
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: Problem running HYSYS Pipesegment in Aspen HYSYS Dynamics | Solution: The feed and product nozzle objects information does get lost (i.e. empty) and it causes the crash or P/F solver fails, when initializing the segment. This may happen if you have multiple segment added, and you tried to delete them. Or you have feed stream / product stream and it got deleted and you added a n... |
Problem Statement: In the Naphtha Reformer environment / Operation tab / Advanced, there are three factors listed under Activity Profile Constants - what do these three factors do ? When might we have to adjust them? | Solution: The Activity Profile Constants enable you to adjust the activity distribution through a reactor. The only real valid reason for adjusting the activity distribution is to match measured internal reactor temperatures. Great care must be taken in this effort to insure that the exact locations of internal thermoc... |
Problem Statement: Why is the Boiling Point Curves utility not listed?
Boiling Point Curves utility is missing from list of utilities. How do I bring it back? | Solution: Petroleum Assay Utility in RefSYS (Aspen HYSYS Petroleum Refining) is equivalent to Boiling Point Curves utility in HYSYS. When you use RefSYS, Boiling Point Curves utility is removed from the list of utilities. It is not a defect. It is removed by design.
If you rather want to use Boiling Point Curve utility... |
Problem Statement: What are some publications that discuss simulation and troubleshooting? | Solution: Listed below are some publications that are available from the literature.
Constant Volume problems
Horwitz, B. A., The Case of the Collapsing Can, Chem. Engr. Prog. June 1997, pp 61-65.
Distillation
Kister, H.Z. Troubleshooting Distillation Simulations, Chem. Eng. Prog. 91, 63 June 1995.
Taylor, R., R. Kri... |
Problem Statement: There are multiple options through which you can zoom in or out of the Planning Board. This | Solution: discusses some of these options.
Solution
The following methods can be used to zoom in/out of the Planning Board:
1. By using the Planning Board contextual ribbon | Format tab | Time Range panel. This panel has 3 options:
a. Predefined
b. From-To Date
c. Around Selected
a. Predefined: P... |
Problem Statement: Can solids components be included in the Pressure Relief block calculations? | Solution: The input stream to the vessel can contain solids. However, solids must be included in the MIXED substream, and not in one of the solid substreams. Solids are not included in the phase equilibrium calculations or the pressure drop
calculations for the vent stream.
The amount of solids in the feed stream will ... |
Problem Statement: Why do some rupture disk simulations show toggling between open and close status? | Solution: In a rupture disk simulation, the vessel pressure drops very steeply when the rupture disk bursts. When the pressure falls to the same value as the vent discharge pressure, the integrator runs into trouble and tends to fail.
In order to get around this problem in the calculations, the rupture disk is set to... |
Problem Statement: Using the same TBPCUT points with the same assay as Pro/II, pseudocomponents with somewhat similar properties are generated, but the volume distribution of the pseudos (to represent the entire assay) are grossly different on the light ends | Solution: The Pro/II default temperature for D1160 is 1 atmosphere, instead of the industry standard 10 mm Hg. Aspen assumes the D1160 data is at 10 mm Hg, unless the user modifies it. If the user forgets to modify it, the light end distribution of the psedo components is totally different.
Keywords: petroleum
ada
assa... |
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 wi... |
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 | Mani... |
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 th... |
Problem Statement: Why does the input Dynamic Viscosity not match the Aspen Assay Manager (AAM) Results? | Solution: In general, AAM in V8.8 is a better tool to do assay characterization because it provides more properties and more flexibility. For instance, it works well to match yield (given only three distillation data point up to 20% only), and bulk properties such as flash point, pour point, sulfur content, etc.
For ... |
Problem Statement: Is there an example model for Dock Scheduling? | Solution: Yes! When V8.5 is installed, a new sample model is also installed that demonstrates Dock Scheduling. The sample model is DemoDSS.mdb and is located with the other sample models under
C:\Users\Public\Documents\AspenTech\Aspen Petroleum Scheduler\Demo\Access
Keywords: Dock Scheduling Example
Sampl... |
Problem Statement: A phase may have flipped between the vapor and liquid slots in operation Vessel | Solution: A phase may have flipped between the vapor and liquid slots in operation Vessel ?.
This can happen with supercritical mixtures. If a spike or discontinuity has also occurred in your dynamic simulation, please check the model choices in regions that may be affected. For example, make sure valves use the simple... |
Problem Statement: We are trying to bring Crude Run events via the staging tables in APS. Nevertheless, we don't know which are the values that needs to be populated for this kind of events. | Solution: For a crude run event these are the values that must be populated in ORION_MGR_ tables:
1. ORION_MGR_EVENT_IMPORT
a. START_DATE
b. STOP_DATE
c. QUANTITY
d. MOVEMENT- this number is important because will be used to relate the other tables
e. EVENT_TYPE- for crude run events the number... |
Problem Statement: Upgrade to PCLS0113 & PCDM0112 to provide the full CL functionality compatable with the TDC v1.0 schematics. The parameter IPNSUB was added to PCDM0111 and the file was renamed. Logic for the mode switching was improved in PCLS0113.
The TDC v1.1 schematics have other CL versions. | Solution: To replace the program PCLS0112.CL with PCLS0113.CL on existing LCN controllers you need to ;
Print system entities of the sub point to an EB file. It is important to print the current sub entity because most of the parameters are built NOT BUILD_VISIBLE and configuration data is lost when reconstituted to t... |
Problem Statement: Messages are not appearing on the production control webserver | Solution: Run the AcoBase shutdown and then the AcoBase Startup.
An alternative method would be to stop and then restart each controller individually in the hopes of stopping the controller that has the lock on the message queue.
This condition is caused by a process in the control system having locked the message queu... |
Problem Statement: How can GMULTs be deleted from DMCplus Build | Solution: This is relatively simple to accomplish.
Step One: Capture the CCF and Model.
Step Two: Capture the non-zero gmults and update the model curves with a model curve operation.
At this point you have some choices.
Option 1: Leave the gmults in the controller with a value of 1 and with each gmult set to 1.0. {Thi... |
Problem Statement: How do I manipulate the user group rights for the model accuracy screen? | Solution: The table GROUPS defines which group of users has permissions to add screens. If a user belongs to this group he can add or delete Model Accuracy screens. Once a screen has been added, any user can modify the Event Facilities and Stream Facilities by right clicking and choosing the relevant option.
Keywords: ... |
Problem Statement: Calculate NEWPV to indicate availability of new analysis. | Solution: The
following CCF calculation will enable this:
CVtag
R4 DEP
DBVL
CVtag
I4 NEWPV
LOCAL Init = 0
CVtag
R4 TOLANZ LOCAL
(user-defined entry)
CVtag
R4 DEPOLD LOCAL
(user-defined entry) Init = -9999
Input Calc
DEP:CVtag|NEWPV =
@IF( @GT( @ABS(DEP:CVtag|DEPOLD - DEP:CVtag|DEP), DEP:CVtag|TOLANZ), 1, 0)
BAD va... |
Problem Statement: I've installed a stand alone key on the correct machine, but cannot get a valid license key for application. | Solution: Go to Start / Programs / AspenTech / Common Utilities / SLM Configuration Wizard
Use the Configure button to reveal the SLM configuration information for that machine.
If the entry for the license source directory does not read c:\Program Files\Common Files\Hyprotech\Shared, then go to the registry and delete... |
Problem Statement: For some unknown reason, the TDC3000 parameters RESETCMD and STRTSTOP values are set BAD in the controller common buffer. Subsequent runs of the controller process will fail with messages in acodhome:[etc]valid.err like those shown below:
Sun Apr 19 07:57:09 1998
ctlr_name Error writing tag: ORD tag... | Solution: Change the values for RESETCMD and STRTSTOP to 0 and load and start the controller.
.STRTSTOP~~~AWRITE~~~I4~~~0~~~::tag_name.STRTSTOP:ORD:
.RESETCMD~~~AWRITE~~~I4~~~0~~~::tag_name.RESETCMD:ORD:
The controller should run aok now. The work-around to ensure that this problem does not recur is to place output ca... |
Problem Statement: Item Count: 3
Item: 1
Summary: Model loses double-precision model gains when a model assembly (.dpa) file is used to create the model.
Topic: Model v1.10.04, Double-Precision Model Gains
When a model is exported, the steady-state gain is written to the text .mdl file as a double-precision number for ... | Solution:
Keywords:
References: None |
Problem Statement: When I’m defining the number of treating and total beds in a Hydrocracker Configuration Wizard, how does the configuration look like? | Solution: For the Hydrocracker Reactor Model in Aspen HYSYS Petroleum Refining, you select the TOTAL number of beds (Number of beds cell at the right of the Configuration Wizard). Then, you specify how many of those beds are treating beds.
By default the reactor will put the treating beds before the cracking beds.
... |
Problem Statement: What does the Extend Stream Functionality button do? | Solution: The Extend Stream Functionality button (found on the Worksheet | Composition pagetab of the stream view) is designed for use with Aspen RefSYS, and allows you to associate an assay (created with the Aspen RefSYS Petroleum Assay Manager) with a given stream in the flowsheet.
If Aspen RefSYS has not installed... |
Problem Statement: Aspen RefSYS can represent all oils in a single case with a single component slate. This is very different from the Aspen HYSYS method of representing each oil with its own set of hypothetical components. How does this affect the properties associated with each component and each stream? | Solution: This is one of the major distinguishing features of modeling with Aspen RefSYS versus Aspen HYSYS. By using a single component slate in Aspen RefSYS, the simulation time can be greatly reduced. Each component in the Aspen RefSYS component slate has a vector of properties associated with it, and these properti... |
Problem Statement: What is the recommended transition type in a stream cutter when moving from assay basis to the Hydrocracker Product Transition (HCRSRK) basis? | Solution: When going from an assay basis to an HCRSRK basis, the defualt transition type is the Fluid Package Transition, but it might not maintain all the assay properties (e.g. sulfur and nitrogen content).
The preferred transition when going from the assay basis to the HCRSRK basis is the Refining Reactor Transiti... |
Problem Statement: How to work within a simulation with various sets of property values for pure components using calculator blocks. | Solution: Most parameters used in property models can have more than one set of values for a given component or pair of components, this allows users to assign appropriate values for different range of temperatures or pressures for instance. Conversely, in the case of properties of pure compounds that possibility is no... |
Problem Statement: The .ocr file syntax for designing user forms is unclear. What should be on each line? | Solution: The syntax is as shown below. These details augment the description in the Getting Started Customizing Unit Operation Models manual.
Line 1: Blocks\blockname, blockname.form_name, tabname, index, 1
(repeat Line 1 for n = number of input tabs)
Line n+1: Blocks\blockname, blockname... |
Problem Statement: Why the amount of NH3 is present in the Product Yields results for the Hydrocracker Unit when there is no NH3 in the outlet stream? | Solution: Typically, the NH3 is removed with wash water before the HPS unit (high-pressure separator) and this is modeled as a component splitter internally in the Hydrocracker. This is the reason why there is no NH3 in the outlet stream but NH3 yield is shown in Product Results.
Keywords: Hydrocracker, Results, Produc... |
Problem Statement: How can I re-characterize an assay using the Petroleum Shift Reactor? | Solution: First you need to have your original assay with Petroleum Assays and not with Oil Manager.
If you have your assay ready, the following step by step shows the way to re-characterize an assay using the Petroleum Shift Reactor.
1) Having a simulation with an assay from Petroleum Assays, create a stream and m... |
Problem Statement: What can the Delta Base utility be used for? | Solution: The Delta Base utility generates the required derivatives for use in delta base linear programming models, which in turn provides a simplified model that can be imported into programs such as PIMS (PIMS is an Aspen product that allows you to determine the best operating conditions at minimum cost using numeri... |
Problem Statement: Sometimes, users have multiple versions of Aspen Plus installed on their PC. Even if the user visits the TOOLS | | Solution: VBA/ActiveX will open the latest installed version of Aspen Plus - this is a registry parameter. To easily see which version of Aspen Plus is being opened by default, after the open simulation code executes, add a message box to display the version number:
msgbox The following Aspen Plus version is running & ... |
Problem Statement: Is it possible to predict Petroleum properties such as Research Octane Number (RON) or Motor Octane Number (MON) for a Chromatography analysis data? | Solution: If you have a Chromatography analysis data and directly enter the composition in a stream, you will not be able to read the petroleum properties. These will be shown as empty.
This type of analysis is not included in Petroleum Assays which is the tool that allow the users to get petroleum properties such as R... |
Problem Statement: In a 3-phase (vapor-liquid-liquid) distillation, if there is only one liquid phase present how does Aspen Plus determine whether it is in the 1st liquid (L1) or 2nd liquid (L2) phase? | Solution: When Aspen Plus is writing the report, it must identify the liquid phase as L1 or L2. This is not a problem when two liquids exist. However, it becomes an issue when only one liquid is present. To decide, Aspen Plus checks the concentration of the key components to identify the 2nd liquid phase as specified o... |
Problem Statement: What internal specifications are used/assumed by Aspen HYSYS when switching a petroleum distillation column from zone by zone to stage by stage calculations? | Solution: When switching from the zone-by-zone to stage-by-stage solver in the petroleum distillation column, the following active specs are provided:
Flow rates for top vapor, bottoms and all side products.
Local reflux ratios for all bottom stages at borders between zones. In the short cut model we assume that there ... |
Problem Statement: In Aspen Plus 10, one sometimes encounters the following problem when running a file containing Fortran code:
*** SEVERE ERROR
ERROR DURING DYNAMIC LINK OF USER ROUTINE(S) OR IN-LINE FORTRAN PLEASE CHECK FILE _2734lfo.LD FOR LINKER MESSAGES.
*** SEVERE ERROR
COULD NOT RESOLVE USER OR IN-LINE FORTRAN... | Solution: When Aspen Plus encounters a Fortran statement that can not be interpreted, Aspen Plus creates a temporary Fortran file that contains a subroutine with the name ZZFORT. The subroutine contains all the fortran block statements and is compiled and linked dynamically (during the run) by the external Fortran comp... |
Problem Statement: What type of distillation method is used for variable CutYieldByVol(%), CutYieldByMol(%) and CutYieldByWt(%)? How should I enter the distillation data? | Solution: The CutYieldByVol(%), CutYieldByMol(%) and CutYieldByWt(%) in both Input Summary form and Results Summary form it's always showed as TBP distillation type.
If you go to Distillation Data tab you can enter different type of curves, such as: TBP, D86, D1160, D2887.
Keywords: CutYieldByVol, Input Summary, Disti... |
Problem Statement: Are there any tips for importing HYSYS D86 curves into RefSYS? | Solution: If you define an assay using a D86 curve in the HYSYS Oil Environment and want to use this assay in RefSYS you must use the API 1994 D86-TBP Conversion Method. This must be done to each individual assay.
To change the conversion method follow the steps below:
Enter the Oil Environment from the Basis Manager.
... |
Problem Statement: How do I use calculated UA for air cooler in dynamic simulation? | Solution: The UA value in the air cooler is taken as the steady state value. In dynamic mode, the UA value can be derived from the steady state value as follows:
UA-Dynamic = F x UA-Steadystate
Where, UA-steadystate value is the value entered on the Parameters page of the Design tab and F is the flow scale factor. This... |
Problem Statement: How is it possible to find true critical point for a mixture? | Solution: The Aspen Plus Prop-set properties PCMX for critical pressure, TCMX for critical temperature, (as well as VCMX for critical volume and ZCMX for critical compressibility factor) give simple mole fraction averages (pseudocritical) for the critical properties of a mixture which should not be considered very accu... |
Problem Statement: How can I see which stream is related to a Petroleum Assay? | Solution: This situation may happen when in a big simulation user wants to locate all streams with Petroleum Assay analysis quickly. The following steps will help to locate such streams.
In the main Flowsheet go to the Flowsheet/Modify Tab and in the right hand side you will find the Conditional Formatting part.
Displa... |
Problem Statement: Can I specify viscosity data for my assays using Aspen RefSYS? | Solution: YES. Starting with version 2006, users can input viscosity data for their assays in Aspen RefSYS. Attached with thisSolution is a recorded demo with detailed instructions.
This video will demonstrate the difference the new assay parameter adds to the viscosity calculation of the petroleum assay stream.
1. Sta... |
Problem Statement: Assistance with setting up Perfmon | Solution: Perfmon is a tool for monitoring various statistics about system operation. It can look at the system as a whole, or individual processes that are running. The following procedure configures PerfMon to collect some key memory statistics:
1. Go to Windows Start -> Run
2. Type in perfmon and click Ok.... |
Problem Statement: What is the significance of bundle top height and bundle bottom height entered on the Dynamics | Heat Exchanger page of the Separator property view? | Solution: HYSYS is using the Bundle Top Height and the Bundle Bottom Height values to calculate the liquid Cover percentage and from that it calculates the Liquid Area and the overall Vapor Area . Afterwards these areas are used to estimate the overall Shell heat transfer coefficient UA_shell and the overall Tube heat ... |
Problem Statement: How do I read LOOPST and AWSCOD from EXAOPC to DMCplus through CIMIO for OPC ? | Solution: Refer to attached document.
Keywords: DMCplus, connect, EXAOPC, cim-io, opc, smart data types
References: None |
Problem Statement: How is the LP solved? | Solution: The LP, due to ranking, is solved in a sequence of steps. These steps can be categorized into two main areas: 1. A feasibility calculation, and 2. an optimality calculation. The feasibility calculation solves a sequence of linear programs. The decision variables in these linear programs are the give-up on the... |
Problem Statement: We defined descriptions in all MTGIND and MTGDEP entries. Before we
did so, we had the correct message in the message overview in DMCview.
But now, we only have the first 12 characters of the description, and
then nothing anymore. In the ENG file the whole message is still
available. What did we do w... | Solution: For v1.04.xx, change all MTGIND and MTGDEP entries to be 12 characters. This problem is fixed for v1.10 to be out in early November.
Keywords:
References: None |
Problem Statement: How do I configure an anti-surge controller in Aspen HYSYS? | Solution: To model an anti-surge controller Aspen HYSYS is using a modified PID Controller logic, as the controller need to act very rapidly.
Refer to the attached PDF document for full instructions and to the attached hysys file and spreadsheet for and example.
Instructions
AspenTech product documentation can be copie... |
Problem Statement: What are the guidelines for converging and troubleshooting the Delayed Coker model and Visbreaker model in Aspen HYSYS Petroleum Refining? | Solution: The delayed coker model or The visbreaker model may fail to converge or calibrate for a number of reasons
· Incompatible property slate in feed assay
· Errors in calibration data (mass balance, property balance, etc)
· Large step cha... |
Problem Statement: You are trying to load a controller and although you have checked and double-checked your Cimio_logical_devices.def file and your .cncdev parameter in the Aspen DMCplus controller configuration file, and they are correct, continue to get logical device not found error messages. This is most likely to... | Solution: The most likely cause for this problem is that there are non-default logical devices specified for a few tags in the controller. They could be anywhere in the .ccf.
Clients will no doubt recognize the tag name syntax for many DCSs which looks something like the following:
::FC2001.PV:DBVL:
If we expand it wit... |
Problem Statement: How do I configure the set point ramping in the PID controller? | Solution: The PID controller in Aspen HYSYS Dynamics can be configured to include the set point (SP) ramping functionality. This facility is available in the Advanced page of the PID controller page. See the screenshot below.
The Advanced page contains the following four groups:
Group
Description
Set point Ramping
You ... |
Problem Statement: What is zero speed flow resistance [k] sizing parameter for reciprocating compressor? | Solution: In HYSYS Dynamics, when the speed of the compressor is exactly zero, then the flow through the unit is governed by a typical pressure flow relationship:
Flow = K zero speed* Sqrt (Density * Frictional Pressure drop)
Where K zero speed = zero speed flow resistance
The zero speed flow resistance [k] parameter ... |
Problem Statement: Why are derivative events - blend component (type 38) not published in _EVENTS table even when the option publish derivative event is selected? | Solution: Event Type ID: 38 was purposely, eliminated from Publishing with recent versions in order to reduce the amount of data that is published in the _Events table, and increase the publishing speed. The required information is also published in EV_XXXX tables. Therefore we suggest to use EV_XXXX tables to extract ... |
Problem Statement: How do I test an automation code for Aspen Petroleum Scheduler or Aspen Multi-Blend Optimizer? | Solution: Below are steps that can be used to test an automation code.
From Excel, press ALT-F11 to open VBA editor.
Click ‘ThisWorkook’ as shown below. This would open an empty panel on the right where VBA automation code can be written. You can also copy/paste code from the APS HELP.
From Debug Menu, select ‘Compil... |
Problem Statement: Sum of MV moves <> steady-state | Solution: Solution
The message Sum of MV moves <> steady-stateSolution is the result of either the maximum move being set too small, or the move suppression is set too large. It may also require a visit to how the equal concerns are configured. In general this is a tuning issue. It may be advantageous to run the contro... |
Problem Statement: Serious Bug in Copying a Model with DMCplus Model 1.10.04
This is a serious issue. This is based on a previous Advisory and is renamed as an Alert due to concern that the recipients did not take it seriously enough and that the writer did not express the serious nature of the problem concisely. It is... | Solution: The correct procedure for modifying a copied model in DMCplus Model 1.10.04 follows:
copy the model
change the name in the properties dialog
press OK to exit the properties dialog
select the model
edit the properties to remove or re-order variables without problem.
The above procedure will not corrupt the mod... |
Problem Statement: Some of the CIM-IO servers support the acquisition of engineering units and
descriptions into the CLE file. Some of the servers have functioning smart data
types for AWSCOD and LOOPST. Some have been field-tested. Which ones? | Solution: Desc
Smart Field
Eunits
Listsz
Data
Tested
Biles AIM
Centum Exapapi
Centum Exapapi
no
no
yes
no
no
yes
yes ? v1.0
no -1 v 2.4
no -1 v 2.5 Cim-IO kernel 4.7.1
CM50S
CM50S
CM50S
--- -
yes
yes
yes
-
yes
yes
yes
-
yes 299 v 2.0 (Irevers=1)
yes 600 v 3.0
yes -1 v 3.2 CIM-IO kernel 4.7.1,
UCX 4.1 eco 6
Foxboro Br... |
Problem Statement: When is it proper to use MV or CV tracking in DMCplus? | Solution: The intent of thisSolution is to document AspenTech best practice recommendations for the use of MV and/or CV tracking in DMCplus controllers.
MV Tracking - How It Works
Every MV in a DMCplus controller has a tracking flag called TRKMAN. The value of TRKMAN determines how an MV will be treated by the controll... |
Problem Statement: There are three mechanisms that can enable a write from a DMCplus system to the DCS directly or via an intermediate database product. The obvious mechanism is that the DMCplus controller has been turned on by the plant operators and begins writing to the MVs.
The other two mechanisms are less well un... | Solution:
Keywords:
References: None |
Problem Statement: If you issue a delete command from the command line, manage allows you to delete a running controller without stopping the process.
There is no problem if you use the menu. However, if you use a command line like:
$ manage delete ctlr_name
while the controller is running, the process will continue bu... | Solution: The successful command line method to delete the controller is to first stop the controller via:
$ manage stop ctlr_name
then, delete the controller via:
$ manage delete cltr_name
Keywords:
References: None |
Problem Statement: Selecting File from the DMCplus View screen menu, then selecting Print from the pull down menu does not do anything -- the screen is not printed. | Solution: Copy the Config.key file from the GCS32\Displays directory into the directory where the DMCplus View screens are stored. This will enable the print option on the File pull-down menu and will also make tool bar buttons available that provide abilities to zoom in and out on a screen, to page forward and backwar... |
Problem Statement: This document explains how equal concerns errors (ECEs) in the DYNAMIC CALCULATION work. | Solution: Equal concern errors in the dynamic calculation are unlike ECEs in the steady-state or LP calculation. In the steady-state calculation, the ECEs are weights on constraint violation. They provide a way to make trade-offs in constraints of the same rank set.
In the dynamic calculation ECEs are used as weights o... |
Problem Statement: DMC v5.0 to (DMC v5.3 or DMCplus) Migration Issues | Solution: Each controller will be in a separate controller-named directory.
Only one custom input transform (CTRANI) and only one custom output transform (CTRANO) is implmented. This is unique to each controller and must reside in the controller directory. Use of CCF calculations is encouraged.
Equal concern and tran... |
Problem Statement: Note: Negative values of GMULT are not allowed in DMCplus 1.10.01 and before.
This issue is resolved in Patch001.
Some situations can require the use of variable gains. With DMCplus, you can manually adjust the gain using a multiplier applied to a response curve for a dependent/independent variable ... | Solution: Add GMULTE to the Configuration section as a user-defined, integer constant with a value of 1 to enable the use of Gain Multipliers.
Add GMULT as a user-defined real entry to the CCF in Build as a READ, or LOCAL if a CCF calc. It can be placed in the General Section or the specific Independent variable sectio... |
Problem Statement: After running the DBupdate utility, do I need to manually change any of the table fields? | Solution: After running the DBUpdate tool, the user can click the Help button at the bottom right corner. There is a detailed procedure in the HELP explaining the procedure.
The last step (step 5) indicated the DBupdate utility also generates a script (highlighted on the HELP screen shot). Please find the generat... |
Problem Statement: s and | Solution: s:
Issues with the use of hiway gateway points:
1. Ensure that the box is in Full Control.
2. HG (highway) points. There are -TWO- timeout parameters on each MV. Make sure that you use the correct time-out parameter. There is T1 and T2. Check to see that you are using the correct one by pulling up... |
Problem Statement: What are Pipe Flow Models used for in HYSYS PIPE segment dynamic page? | Solution: In Aspen HYSYS Pipe segment dynamics the user has the choice to use two Pipe Flow Models.They are explained as below:
1) Simple pipe friction model method:
a) Turbulent: The calculation is fast and simple. This method calculates the friction factor once and uses that value irrespective of the Reynolds number... |
Problem Statement: The AxM services file was modified for the installation of DMCplus. On system reboot, the 3 cdsdaemons required for the AxM wouldn't start. | Solution: >On my recent trip to Europe I encountered 2 more of the renegade AxM boxes
>that didn't want to start the 3 cdsdaemons required for the AxM. After
>talking with TAC in Europe Rafi and I discovered that there is some sort of
>problem with the services files in the /etc directory. The TAC folks asked
>us to mo... |
Problem Statement: Comm Buf error between DMCplus and Composite
CLPTGT 15024 Composite - Comm buffer connect error | Solution: The Comm Buffer error is caused when there is an error connecting to the shared memory that Composite uses to communicate. When a controller communicates with the composite it maps and locks this buffer. When it has completed its communications, it disconnects and frees the lock. The error can occur at the be... |
Problem Statement: What considerations should be taken into account when selecting the correct feedback controller? | Solution: The following is a flowchart that outlines a method for selecting a feedback controller:
In general, if an offset can be tolerated, a proportional controller should be used. If there is significant noise, or if there is significant dead time and/or a small capacity in the process, the PI controller shou... |
Problem Statement: Using Wollongong TCP/IP software. | Solution: Wollong Pathways
(aka Attachmate Pathways)
Must be 2.5 or later. This command shows the version:
$RUN TWG$TCP:[PATHWAY_ADMIN]PATHWAY$LIST_SOFTWARE
LISTSZ must be 600 or less (with 4.6B.) LISTSZ should be -1 with kernel 4.7.1.
Pathways consumes one file quota per socket. Each of the CIM-IO processes uses two ... |
Problem Statement: How to add a level controller to downstream of Reboiler weir | Solution: Unfortunately the reboiler operation does not have the Chamber 2 liquid percent as one of the variables. Thus the user is not able to control the liquid level downstream of weir. However, there are two ways in which you can work around this to use the level in chamber 2 as a control variable.
The first method... |
Problem Statement: How do I change default sampling interval in HYSYS Dynamics? | Solution: The default sample interval is 20 seconds and number of data points in the logger is 300. For any individual stripchart this can be changed via Right-mouse click and selecting the Graph Control page.Click the Set-up Logger button to open the page as shown below.
The default setting can also be changed in the ... |
Problem Statement: DMCplus Collect?IACO BASE???????i?????e???B | Solution: Collect?ITest API?????l?E????????CIM-IO?N???C?A???g?\?t?g?????B???????A?A?AACO_BASE???K?v?????U?????B
?b????????????.exe???>?I?u?I?e?`?t?@?C??(input file)???????ECIM-IO???Y?u???e?A???e?}?V???E?R?s?[???e???????A?@Collect?I?i?????A.bin?t?@?C?????i?e?????????
Keywords: DMCplus
Collect
ACO BASE
CIM-IO
JP-
Refer... |
Problem Statement: Our PIMS model has recently been updated with a new crude. How do I add this crude to the APS model? | Solution: Given that there is no specific workbook logic regarding specific crude types - which is usually not the case - we will demonstrate below one possible and fairly simple way to add a new crude to the APS model:
1) Open your model
2) Find table CRUDES under ASSAYS branch of TABLES
3) Insert data f... |
Problem Statement: Pooling crude tanks is easy if you just want pool volume/composition by crude. However, what if I want the properties of that mix of crudes? | Solution: For crude pool types, the properties by component crude are reported. The available volume and ullage are based on the fraction of the crude in the pool. However, for viewing the properties of the pool, you can add a new trend line of the pool for each property, after reloading the simulator. (Found in the T... |
Problem Statement: Frequently, a controller will need to be changed, and that change could involve removing a variable that has been determined to not be useful in the control strategy. How is that variable removed from the model? | Solution: To remove any variable pair from a model,
Import the model from which you wish to remove the variable
Create a new assembled model
Set the two models where both are visible on the desktop.
Highlight some of the variables you wish to have in the new model, careful to not include the variables you want to delet... |
Problem Statement: Selecting each object from the variable navigator to add to the Dynamic Initialization Manager one at a time is tedious. Is there a way to select multiple objects all at once? | Solution: To add several objects in one go, follow the steps below.
1. Select in the flowsheet the several objects you want to initialize.
2. With the mouse right-button click in one of them (while all selected), and choose Dynamic Initialization
3. From the menu that appears, select the desired option (Add... |
Problem Statement: How are pipe fittings modeled in Aspen HYSYS Dynamics? | Solution: In steady state, appending fittings to a pipe affects pressure drop calculations in the the pipe and a fitting loss factor (K-factor) is determined for the fitting (refer toSolution 109436) and subsequently an equivalent length will be assigned to the fitting. Take note that the K-factor for swages are determ... |
Problem Statement: I have installed the latest ER2 to my DMCplus Controllers and they are not showing up on the WebServer. | Solution: Unload ALL controllers, even the controllers that are not running, or were loaded originally for testing, such as the COL5X3. Reload and restart the controllers as needed.
Then go to Program Files \ Common Files \ AspenTech Shared and run the dmcpview_shutdown.bat to ensure the dmcp_viewsrv process is stopped... |
Problem Statement: Apollo Viewer is not working, reports No controllers are running to attach to cannot save run file. | Solution: The work around of this issue is using the Production Control Web Server to SAVE the RUN File.
If you go to the Configuration Page of the PCWS, Select the Apollo Column sets, Select General from the Category drop down list, and Controller Detail(engineer) from the Apollo Column set to edit. There are two Sa... |
Problem Statement: GCS will not run, BGCSNET not running | Solution: Add the following lines to the autostartlist.txt which can be found in the ACONLINE/SYS/ETC directory.
PROCNAME=BGCSNET
SEQNUM=79
APPPATH=$ACODHOME\bin\bgcsnet.exe
ARGLIST=gcsdmcp E:\AspenTech\AC Online\bin\dmcpview.exe
APPTYPE=0
This will start the required process on a reboot of the machine or when an Acoba... |
Problem Statement: DMCplus Controller reporting QP Internal errors | Solution: This is to be considered a first pass at an attempt to trouble shoot any QP errors:
We recommended use of the SVD Tool which can be found in the DMCplus Desktop / Utilities directory for checking the model file. It is also recommended to reset the paramater EPSMVPMX to 2, you will have to stop, unload, reload... |
Problem Statement: DMCplus Model fails to plot and/or create the Model Uncertainty plots for datasets whose sampling interval exceeds once per minute. In addition, regional settings other then English (US) may cause the plotting utility to fail (i.e. data and timestamp format other then English (US).
The attached plot ... | Solution: Copy the attached zip file and extract both plotting executables into the DMCplus Desktop folder.
Keywords: DMC
DMCplus
DMCplus Model
Model Uncertainty
References: None |
Problem Statement: Is DMCplus 4.1 supported on Windows XP? | Solution: DMCplus 4.1 is currently supported on Windows NT, Windows 98 and Windows 2000 Only. Version 5.0 of the DMCplus Desktop tools, which will be part of the AMS 5.0 deliverable expected by the end of 2002, will be supported in the Windows XP environment as well. Keep in mind this will be the Desktop applications o... |
Problem Statement: I compiled my User Blend Model Library file (UBML.dll) and it works well with APS on my computer. However when I sent the file to my colleague, it does not work with APS on his computer. | Solution: The problem is most likely caused by compiling UBML file in Debug mode. In order to be able to use UBML file on any machine it needs to be compiled in Release mode:
Recompile the UBML.dll in the Release mode and provide that to your colleague.
Keywords: UBML
compile
References: None |
Problem Statement: How do I see the velocity and temperature profiles in the pipe segment in Aspen HYSYS dynamics? | Solution: There are two possible ways to view property profile in pipe segment when running the HYSYS in dynamic mode.
1. In Dynamic mode the profile is based on holdup in the pipe segment. A pipe can be configured with multiple segments. This will provide holdup information for each segment. More number of pipe segmen... |
Problem Statement: We have found that some firewall software applications may prevent the ACO desktop software from obtaining a license although the license server is installed and configured on the very same computer. Typically an error dialog opens showing the user that the particular desktop application is trying to... | Solution: Typical installation procedure is to specify the node name of the license server on the AspenTech License Manager Selection dialog. Thus in order to resolve the ip address for the selected server name, the licensing software must access the network to obtain the ip address from the host table. It is this netw... |
Problem Statement: Firewall Configuration recommendations and considersation | Solution: The basic objective of any firewall is to limit the connectivity between the outside and the inside so that you can exercise as much control as possible on the traffic traversing the firewall. Obviously, you can make a totally secure firewall by disconnecting the outside from the inside. But, while totally se... |
Subsets and Splits
No community queries yet
The top public SQL queries from the community will appear here once available.