question stringlengths 19 6.88k | answer stringlengths 38 33.3k |
|---|---|
Problem Statement: Can I add a process utility stream such as high pressure steam in Aspen HYSYS? | Solution: In Aspen HYSYS, users may tag and designate material and energy streams as utilities. With this information Aspen HYSYS can calculate the utility consumption per utility type as well as total hot/cold utility consumption in the flowsheet.
This functionality is provided through the flowsheet summary (Home t... |
Problem Statement: What are the Activated Analysis Dashboard in Aspen Plus? | Solution: Tools built-in to Aspen Plus to aid in process analysis and optimization
- Activated Economic Analysis provides high level cost estimates that can be used to compare process alternatives
- Activated Energy Analysis looks for opportunities to reduce energy consumption using pinch technology
- Activated Exchang... |
Problem Statement: As a scheduler, most of the times the events scheduled vary from the actual scenario and the schedule prepared needs corrections,
In such a case, to edit all the events in a schedule one by one can be a tedious and painful process making the application difficult to use.
So how can we Edit multiple ... | Solution: In APS, a functionality named Edit in Excel is available. This function has replaced the old application named as Multiple Event Editor which was available in previous versions before V9.
This functionality allows the Scheduler to edit and modify multiple events simultaneously in Microsoft Excel and Multi-Eve... |
Problem Statement: In version 2006 of Aspen Calc a new feature called 'Shared On-Demand Calculations' was introduced. Can these 'Shared On-Demand Calculation' be executed via Aspen SQLplus and see the results in window? | Solution: Yes, you can!
Please note that 'Shared On Demand calculations' are stored in InfoPlus.21 record sets called 'IP_CalcDef'. Through this IP_CalcDef record, we can fetch the formula defined in the 'Shared On-Demand Calculation' and execute the formula using Process data automation in SQLplus. Here is the sample ... |
Problem Statement: Is it possible to get the historical data of a Strip Chart in tabular format in Aspen HYSYS Dynamics? | Solution: Users may set up as many strip charts as needed in Aspen HYSYS Dynamics to track the behavior of key process variables when running the model in dynamic mode.
However, there might be instances in which users might prefer to get the historical data of a strip chart in a tabular format rather than in a plot.
... |
Problem Statement: Why the main flow sheet stream hydraulics mass flow is different than sub-flowsheet? | Solution: The difference between the mass flow in the Hydraulics sub-flowsheet and the main HYSYS flowsheet is due to the linking of the two dynamic solvers.
The dynamic solver in Aspen Hydraulics requires a velocity boundary at the inlets and a pressure boundary at the outlets in order to solve the pressure-flow distr... |
Problem Statement: What are the supported ProII Versions to import into Aspen Basic Engineering? | Solution: Please refer to the table below and make sure the ProII file is supported.
ABE Version Supported ProII Version
V8.0 with CPs Versions 5.01, 5.1, 5.11.1, 5.5, 5.55, 5.6, 5.61, 6.0, 6.01, 7.0, 7.1, 8.0, 8.1, 8.2, 8.3,9.0,9.1
V8.4 with CPs Versions 5.01, 5.1, 5.11.1, 5.5, 5.55, 5.6, 5.61, 6.0, 6.01, 7.0, 7.1,... |
Problem Statement: How do I change the currency format based on region? | Solution: The currency format may be changed from Windows Settings | Control Panel | Region.
On the Formats tab, choose the appropriate format from the drop-down list.
On the Location tab, make the appropriate selection from the drop-down list.
Save your file, close the program and then re-open your file. The curre... |
Problem Statement: How do I get my Adjust, Set, or Balance to solve before my Column (or any other) operation? | Solution: An example where you may wish to do this is if you have an adjust operation that is setting one of the conditions (temperature, pressure or flow rate) of your feed stream to the column or operation. You may want the Adjust to solve first, so that your column does not have to solve every time the feed conditio... |
Problem Statement: This knowledge base article provides an example script which illustrates how to return all sub-batch start/end times and duration for a given batch using Aspen SQLplus. | Solution: The sample Aspen SQLplus script below calls the Aspen Production Record Manager Application Programming Interface (API) to return the start and end times and duration of all sub-batches of a batch within a specified time frame.
The query uses the following logic:
1. Query for the number of batches whic... |
Problem Statement: How do I split a stream and get outlets at the same temperature and pressure as inlet? | Solution: Here a scheme is presented to split a material stream into two with identical pressure and temperature.
1) Attach the material stream to a component splitter (X-100) as Inlet and attach two product streams to the splitter (1 and 2)
2) Attach an energy to the splitter (Q-100),
3) Set the intended splits for al... |
Problem Statement: How to account for air preheating in a Fired Heater in EDR? | Solution: Air preheating is a common practice in Fired Heaters to increase the fuel efficiency. Using an oxidant (air) at a higher temperature than, for example, atmospheric conditions, could either decrease the amount of fuel needed to meet a specific outlet temperature of the process stream, or increase the outlet te... |
Problem Statement: This | Solution: frames on how to configure one MV as Prediction only for a CV on DMC3 Builder V10
Solution
Prediction only feature is available from DMC3 Builder Version 10. When this feature is enabled we expect the controller to not use all models for control as some of the MVs will not move for certain constraints. In oth... |
Problem Statement: Is it possible to account for air recirculation effects in EDR? | Solution: Recirculation in an air cooled exchanger is a problem that can decrease the overall efficiency of a unit, especially for forced draught configurations.
Currently EDR does not model these effects as it is complicated to estimate what fraction of the air (gas) flow rate will be recirculated.
Nevertheless, if ... |
Problem Statement: What are the different types of Reactions that can be modeled in Aspen HYSYS? | Solution: In Aspen HYSYS, five types of Reactions can be modeled namely, Conversion, Equilibrium, Heterogeneous Catalytic, Kinetic and Simple Rate.
For creating a Conversion reaction set, users require the stoichiometry of all the reactions and the conversion of the base component in the reaction.
For creating a Equi... |
Problem Statement: This Knowledge Base article shows how to resolve the following error message: Run-time error '91' : Object variable or With block variable not set.
One or both of the problems will be observed:
1. The AFW Security Client Service is not visible in the list of services.
2. The following error ... | Solution: 1. Open a command prompt window and cd to \Program Files\AspenTech\BPE - if you are running 32-bit version then specify Program Files (x86)
2. At the command prompt type: AfwSecCliSvc /unregserver to unregister the service
3. Reboot the computer and verify that the service is gone.
4. At the next prompt t... |
Problem Statement: How to add static head contribution for vessel downstream pressure calculation? | Solution: By default, Contribution of static head on liquid outlet pressure is not incorporated. However, in models with a liquid holdup, we have the option of representing the effect of the liquid static head on the liquid outlet pressure.
This option can be enabled either from Global options or individual models.
Fo... |
Problem Statement: How to resolve the Error-Failed to Launch Help received in APS when Help File is not found? | Solution: The root cause of this issue is that The Help file is missing from the Installation folder of Aspen Petroleum Scheduler i.e.
C:\Program Files (x86)\AspenTech\Aspen Petroleum Scheduler\HTMLHelp
To resolve this issue, two approaches can be followed:
1) You can copy this Default.htm file & the Content folder f... |
Problem Statement: Can I perform Pipe Flow Assurance studies in Aspen HYSYS Dynamics? | Solution: Aspen HYSYS Pipe Segment Flow Assurance options allow users to check the physical structures of a pipe against the predicted wear caused by the type of fluid it is carrying to estimate the functional viability of the pipeline over time. In Aspen HYSYS Steady State, users can predict the formation of hydrates,... |
Problem Statement: How do I export the simulation workbook pages from Aspen HYSYS to Excel? | Solution: Please follow the workflow below to export the simulation workbook from HYSYS to Excel:
1. Select the Workbook button from the Home tab (top ribbon)
2. From the Workbook tab, click the Excel button from the Export section
3. Select pages to export
4. Finally, click Export to Excel button.
... |
Problem Statement: Does RYield calculate adiabatic reactor temperature rise? | Solution: Yes. RYield calculates adiabatic reactor temperature rise.
For RYield, the duty is the difference between the inlet and outlet enthalpies. You do not need to specify heats of reaction, because Aspen Plus uses the elemental enthalpy reference state for the definition of the component heat of formation. Therefo... |
Problem Statement: Does Aspen Flare System Analyzer (AFSA) use rated flow or mass (design) flow for the pressure drop of inlet piping? | Solution: AFSA will use the design (mass) flow for inlet piping pressure drop calculations by default. However, you may set AFSA to make use of rated flow instead, by going to Calculation Settings | General | Rated Flow for inlet pipes.
Keywords: Inlet Pipes, Pressure Loss, Mass Flow, Rated Flow.
References: None |
Problem Statement: How to model tray types that are not available in the Column Internals database? | Solution: Tray types like Superfrac are proprietary and currently, the Column Internals database does not include the correlations for these tray types to perform the hydraulic calculations.
However, the user can select an existing valve tray type and modify the weir length to mimic the Superfrac tray. Weir Length can ... |
Problem Statement: How can I add component mass fractions to a Workbook Report? | Solution: Open the Workbook and view the Compositions tab. From the Workbook tab in the top ribbon,click the Setup button.
Ensure the Compositions tab is selected and click the Add button.
You may type mass frac to auto-filter the variables. Click the arrow to add selected component mass fractions. Click Done when... |
Problem Statement: How do I change a specification type for the column side operation? | Solution: The specification type used for a column side operation such as pump around can be changed following the steps given below:
1. Open the column and then select the Side Ops tab.
2. Select the side operation from the available list.
3. Click the View button.
4. Double-click on an Active Spec.... |
Problem Statement: Can I run the Fired Heater in steady state? | Solution: Yes, the steady state Fired Heater model supports the specification of combustion efficiency and flue gas temperature and solves based on these parameters and fully defined feed and fuel / air streams.
In steady state mode, the fired heater supports multiple fuel and air streams. To facilitate the transition ... |
Problem Statement: If we open a stream property view, select Worksheet tab, Compositions page, and click on the button View Properties, we find a property Molar Volume as in the screen shot below.
What are the conditions at which the molar volume is calculated? | Solution: The is the same property known as GS/CS - Mol Vol, see screenshot using N2 as an example. Here GS denotes Grayson-Streed property package, while CS denotes Chao-Seader property package. This property is calculated from COSTALD at 25 C and 1 atm if Tc is higher than 300 K, or calculated using liquid density at... |
Problem Statement: How to Create a DFMS File for Aspen Enterprise Database Using Aspen Plus Engine | Solution: A DFMS (.dfm) file can be generated from an Aspen Plus or Aspen Properties simulation and used to create a custom user Aspen Properties Enterprise Database (APED) Databank.
This Solution explains how to create an enterprise database from a simulation model and requires the user to access the Aspen Plus User ... |
Problem Statement: Can I rearrange streams in alphabetical or any other order in HYSYS workbook? | Solution: Yes, you may rearrange streams in a workbook.
Please follow these steps:
Open workbook and then right click anywhere on the workbook.
Choose the option - Order/Hide/Reveal.
Choose the sorting order radio button. If you choose Manual, use the up or down arrow to move a stream up or down in the list.
... |
Problem Statement: Why does the non-recoverable pressure loss equal total pressure loss when using either the Isothermal Gas or Adiabatic Gas pressure drop correlations for inlet piping? | Solution: The Adiabatic Gas and Isothermal Gas pressure drop correlations are closed form analytical equations (see the Help Menu Guide for details).
They only calculate the total pressure drop and not the individual parts of the pressure drop (e.g. pressure drop due to frictional / gravitational / acceleration effects... |
Problem Statement: Can I view individual heat transfer coefficients for the Aspen HYSYS Pipe Segment operation? | Solution: The individual heat transfer coefficients are available via the Overall HTC radio button on the Rating | Heat Transfer page.
Keywords: HTC, pipe segment, individual HTC, heat transfer coefficient, heat transfer
References: None |
Problem Statement: Why RBatch does not maintain mass balance around the block? | Solution: RBatch is a batch reactor used in a continuous flowsheet. Holding tanks are used to interface to steady-state simulations.
The mass calculation equations for RBatch are:
For charge stream:
Batch charge = F_charge * T_cycle
If T_cycle is missing, then
Batch charge = F_charge * T_feed
For product stream:
F... |
Problem Statement: Find Fouling calculation in Air Cooled Exchanger | Solution: Within EDR, there isn’t a specific ‘Find Fouling’ Calculation Mode as there is for S&T. However, Air Cooled Exchanger has 9 different variations for the Simulation mode.
One of these Simulation modes allows the user to calculate the Process fouling resistance and the X-side outlet temperature.
The outlet tem... |
Problem Statement: When is the “Tmom” parameter used in polymer procedures? | Solution: The third moment (TMOM) parameter is only used when the simulation model has included TMOM in the list of polymer attributes when setting up the properties or in the original Aspen Plus model. TMOM is required to calculate the Z-Average molecular weight, MWZ. The Free-Radical bulk, FR Emulsion, Ziegler-Natta... |
Problem Statement: What are the auto-recovery and backup settings options under File | Options |Preferences Simulation in Aspen HYSYS? | Solution: You have the ability to choose whether or not HYSYS will keep a backup of your cases or not. You have below options available under File | Options | Simulation | Auto-recovery Settings
1. Save Auto-recovery case: When this checkbox is active, HYSYS will save an auto recovery case every specified amount of tim... |
Problem Statement: How Kappa (Isothermal Compressibility) is defined in Aspen HYSYS? | Solution: The isothermal compressibility is defined as:
b = -1/V*(dV/dP)(Tconstant)
It represents the change of volume that takes place when pressure changes at constant temperature. Unfortunately, HYSYS doesn't display the property values of Isothermal compressibility coefficient. You can implement this in a spreadshe... |
Problem Statement: After the installation the web application fails to run and returns an error message referring to HTTP Error 500.21 | Solution: Many web applications use managed code from the Microsoft .NET Framework codebase. What this error is saying is that it does not know how to handle ASP.NET pages. This is in much the same way that if you received a Microsoft Word Document but you didn't have MS Office installed - the operating system would no... |
Problem Statement: AspenONE Process Explorer Admin, and Trend search shows error code 500.
AspenONE Process Explorer Admin search error occurs “A connection with the server could not be established (error code: 500)” and the Tomcat Catalina.log file includes error “An attempt was made to authenticate the locked user “... | Solution: below.
Solution
Edit the file
…\AspenTech Shared\Tomcat8.0.36\conf\tomcat-users.xml
Scroll to the bottom of the file and change the line with the encrypted password to admin. [see example below]
EXAMPLE;
Original,
<role rolename=AspenSearch/><role rolename=manager-gui/><user username=admin password=21232f297a... |
Problem Statement: Sample calculation for NPSH | Solution: The following equations are used to calculate the available NPSH:
P1 - Pvap (V1)2
NPSHavailable = ------------- + ------
ρ * g 2g
where:
P1 = inlet stream pressure to the pump
Pvap = vapour pressure of the inlet stream
ρ = density of the fluid
V1 = velocity of the inlet stream
g = gravity constant
V1 is the f... |
Problem Statement: How to locate local help files for the Aspen Process Data Addins ? | Solution: The following locale install location contains a number of helpful files which cover the MES products.
C:\Program Files (x86)\Common Files\AspenTech Shared\Help\En
The following files are the Aspen Process Data Addins.
ProcessDataAddin.chm
ProcessDataExcelAddin.chm
Keywords: How to use.
Process Data
Exce... |
Problem Statement: For inlet piping, sources report ‘Piping non-recoverable pressure drop’, as well as ‘Piping pressure drop’. What is the difference between them? | Solution: Sources in Aspen Flare System Analyzer report both ‘Piping non-recoverable pressure drop’ and ‘Piping pressure drop’.
Their definitions are the following:
1) Piping non-recoverable pressure drop accounts for friction losses only.
2) Piping pressure drop includes static head as well as friction losses.
Keyw... |
Problem Statement: Why does the distillation curve reported for an assay sometimes differ from the input curve? | Solution: The input curve might be just the distillation data. E.g., ASTM D86
However, one can enter additional data related to assay. Assay data of certain crude oils, especially light crudes, may contain detailed analysis of defined components, typically including methane through n-hexane. You can enter the fraction... |
Problem Statement: In addition to built-in attributes, what are other properties calculated by Emulsion Polymerization? | Solution: For RBatch and RPlug reactor, the following additional variables are calculated when Emulsion Polymerization kinetics is selected:
Glass transition temperature of the polymer (°C)
Average number of radicals per particle
% Soap coverage of the polymer particles
Volume of the monomer droplet phase (m3)
Concentr... |
Problem Statement: After specifying a subcooled temperature for the condenser, stage 1 (condenser) temperature in TPFQ profile does not get updated. | Solution: The behavior you observed is by design. The convention is that the temperature in the TPFQ table is the equilibrium temperature of the stages. If you want to look at the subcooled temperature of the reflux stream, you could create a pseudo stream for the liquid stream on stage 1 (condenser).
Keywords: None
Re... |
Problem Statement: When trying to access to the Aspen HYSYS Online Help, the Help page does not open in Aspen HYSYS, how do I fix it? | Solution: This issue occurs due to a corrupted Aspen HYSYS installation since the help files could not be saved on the right folder. Hence, in order to solve this, one can condiser below two methods:
1. Repair the installation of Aspen HYSYS.
2. Please check the following directory: C:\ProgramData\AspenTech\Aspen ... |
Problem Statement: What are ‘Logical Connections For’ in Aspen HYSYS and how can users access them? | Solution: The ‘Logical Connections For’ property view enables you to determine simulation dependencies between objects which are not otherwise shown via connecting lines on the PFD. Certain HYSYS operations can write to any other object and if you are looking at the object being written to, they have no way of telling ... |
Problem Statement: What are the available options to manually enter the Petroleum Assay data? | Solution: Each option allows you to enter information differently:
Multi Cut Properties (default option) lets you specify mass, molar, or volumetric cuts of the crude assay sample with user defined initial and final boiling points.
Single Stream Properties, lets you define the distillation percent and temperature of in... |
Problem Statement: How do we understand the back pressure when choking happens downstream PSV in Aspen Flare System Analyzer (AFSA)? | Solution: In Aspen Flare System Analyzer, if you use a required mass flow > critical mass flow of the PSV orifice (rated flow of a PSV which is choked in other words), that would be an physically incorrect boundary condition and your back pressure results would be wrong.
At the point of secondary chokes in the downs... |
Problem Statement: How shall I use Symbol Replication Tool to improve the Symbol Loading experience in Drawing Editor? | Solution: Symbol Replication tool can download the Symbol Library from the server to local client machine. It will speed up the performance of each client machine when a PFD in drawing editor is loaded.
This application can be launched from the start menu (Start > Aspen Basic Engineering > Symbols Replication) on a cl... |
Problem Statement: Are Heat Ports from ACM supported in Aspen HYSYS? | Solution: If an ACM model containing Heat Ports is exported to Aspen HYSYS, these won’t be available (HYSYS does not support these ports).
As an alternative, the heat duty calculated by the ACM model could be exported to a Spreadsheet block, and from there, even to an Energy Stream if additional manipulation is necessa... |
Problem Statement: When defining inlet pipe segments for sources in Aspen Flare System Analyzer (AFSA), does AFSA imply that an expander/reducer exists between each segment? Does it account for the pressure loss caused by the expander/reducer? | Solution: For different inlet pipe segment diameters, AFSA does not consider that a swage exists between two different sizes, so the pressure loss due to the change of pipe sizes is not considered. As a workaround you may enter an equivalent length for each pipe to account for such pressure loss.
Keywords: Pipe Segment... |
Problem Statement: I have set up a Storage Tank Protection object in Safety Analysis, but even though there are results for Normal Venting, no results are shown for Emergency Venting. Why? | Solution: A 'Storage Tank Protection' object may be correctly set up, but the 'Bottom Tan Above Grade' and 'Flame Height from Grade' values might not be right, thus no results will be computed for Emergency Venting.
The 'Flame Height from Grade' value must be greater than the 'Bottom Tan Above Grade' plus the vessel... |
Problem Statement: Why is the specified number of Tie Rods not being used for the Tubesheet Layout results? | Solution: The user-defined number of tie rods is accepted if it is above the TEMA minimum (usually >6) or zero. The user can always edit the number of tie rods on the tube layout, and reposition them. The tie rods have no effect on other calculated results, unless they occupy a potential tube location, in which case th... |
Problem Statement: In HYSYS, how to calculate the heat of mixing of electrolyte | Solution: ? For example, the heat of mixing sulfuric acid with water.
Solution
1. In Properties environment, choose Aspen Properties when adding component list. Add sulfuric acid with water.
2. Choose Aspen Properties when adding fluid packages. The reason we choose Aspen Properties here is because Electrolyte NRTL i... |
Problem Statement: How to give pipe specifications for all the pipe segments in Aspen Hydraulics? | Solution: Users can use pipe segment editor under Piping Network Ribbon in Aspen Hydraulics to give specifications for all the pipelines together.
In the editor, users can specify pipe details quickly in an grid similar to excel. Also, it is possible to apply the properties values to all the pipes together.
Keywords: ... |
Problem Statement: I would like to track the erosion rate for the whole pipe network in a Hydraulics subflowsheet, similar to what I see in pipe segment. How do I accomplish this? | Solution: Unfortunately there is no direct way to show the overall erosion rate as in a pipe segment. There are three options we can use to get this:
1.- Get the report for each pipe. Enter to the Hydraulics subflowsheet, and fro each pipe select the Flow Assurance tab where you can sactivate the Erosion Speed analysi... |
Problem Statement: When running the Icarus Excel reports, a message pops up referring to an Excel Report Header Error and/or the named range does not exist in the template | Solution: These error messages may come up for one of the following reasons:
1. If you use or have modified the Reporter_User.accdb file (found in C:\Program Files (x86)\AspenTech\Economic Evaluation VX.X\Program\Sys\Reporter\Database). Where VX.X represents your current version.
If a new Excel report was added in 'Sto... |
Problem Statement: Can I connect my Aspen HYSYS model to ASW if they are from different versions? | Solution: You can have different versions of ASW and Aspen HYSYS installed on your machine and still connect your process model to ASW.
For example, if you have the ASW V9.0 add-in installed and activated on your machine, and Aspen HYSYS V10 installed as well, you can still have ASW V9.0 connect to your HYSYS V10 model... |
Problem Statement: What is the definition of the Vessel Base Elevation Relative to Ground Level and Nozzle Elevations on the Rating tab of a unit operation? Do they influence pressure drop calculations? | Solution: 1) The 'Base Elevation of Inlet Relative to Ground' field allows users to specify whether the process equipment's bottom head touches the ground or not, it is, if the vessel is located at ground level.
2) The 'Elevation' fields on the Nozzle Parameters section refer to the location of the feed and product noz... |
Problem Statement: How is the Operating Weight of a Kettle exchanger calculated in Shell and Tube Mechanical? | Solution: Shell & Tube Mechanical (EDR) considers the normal liquid level to calculate the Operating Weight. The normal liquid level is taken as 25-50 mm above the OD of the highest tube row in the bundle, since the bundle must be covered by the boiling liquid.
Keywords: Operating weight, kettle, mechanical
References:... |
Problem Statement: Is it possible to have Aspen HYSYS save a copy of the Steady State model when switching to Dynamic mode? | Solution: It is a best practice to always keep a copy of the steady state file used when switching from steady state to dynamic mode. Unfortunately, users may forget sometimes to do so and that can become a problem.
For this reason, it is possible to set up Aspen HYSYS to save a copy of the steady state model once the ... |
Problem Statement: I have built an AFSA model in which I set up tear streams in the flowsheet, but the model comes across convergence issues. What I can I do to overcome them? | Solution: There might be some cases in which Aspen Flare System Analyzer (AFSA) models set up with tear streams will not be able to be solved with the default solver settings.
An example of this kind of situations would be KO Drums set up with dual feeds, as shown in the image below:
To overcome the convergence iss... |
Problem Statement: Why Integrator may fail if default bed discretization method is changed? | Solution: In Aspen Adsorption, the default discretization method for the gas_bed model is UDS1 (Upwind Differencing Scheme). UDS1 works very efficiently for almost all gas bed configuration and should not be changed if there is no specific reason.
While using other methods, user should be aware that other methods can ... |
Problem Statement: How to model double-wall tubes in EDR? | Solution: The following description and attached example illustrate how to model double-wall tubes in EDR.
Specifications:
Tube OD
For the Tube OD, use the outer tube OD of the double-wall tube.
Contents between walls
To simulate the contents between the double-wall, select a fouling layer thickness equal to the diffe... |
Problem Statement: This article explains how to resolve an incomplete trip time and distance error. Occasionally a User will receive the message “Cannot add shipment to transport because of incomplete trip time information” from the Aspen Fleet Optimizer that a shipment cannot be added to a transport:
This error is s... | Solution: A journey for a truck making a delivery generally consists of at least 2 locations:
The Terminal where the truck starts his day (typically the same terminal where he will load his first load) and often the same he returns to for another load to be loaded after a delivery.
The Station he is making the delivery... |
Problem Statement: I have exported my Aspen HYSYS SM model to EO, but the EO tab is locked up. Why? | Solution: When the EO (Equation Oriented) sub-flowsheet is opened by right-clicking on the EO icon, the EO tab in the sub-flowsheet will be locked up, as shown in the images below:
To enable the EO tab in the sub-flowsheet, the user must double-click on the EO icon and click on the ‘Sub-Flowsheet Environment’ button... |
Problem Statement: I had a customized crude library (System Crude Library) created on an older HYSYS version. Now, I migrated to a newer version of HYSYS. What are the steps to restore my old library on the newer HYSYS version? | Solution: The location where you can find the UserAssayLibrary.aal file (where the customized library is automatically stored) is:
C:\Users\USERNAME\AppData\Local\AspenTech\Aspen Assay Management\Vx.
Then, you can move to the folder of the newer version and replace the... |
Problem Statement: Which gas bed discretization method is recommended for highly nonlinear adsorption cases? | Solution: For highly non-linear adsorption phenomena and where breakthrough curves are very steep, the recommended discretization methods are: Biased Upwind Differencing Scheme (BUDS) and Flux Limiter. These two discretization methods handle near equilibrium behavior which happens in highly nonlinear adsorption cases.
... |
Problem Statement: Suppose the following conversion reactions have been added to a reaction set:
R1) A + B ==> C + D
R2) F ==> B + G
If the reactor feed contains only A and F, reaction R1 will not take place unless some B has been produced via reaction R2. It appears that HYSYS calculates R2 first followed by R1, ther... | Solution: If you manually rank each reaction, you can dictate the order that HYSYS uses to calculate overall conversion. By default, HYSYS will automatically assign a rank to each reaction in a set by examining the dependencies that exist between reactants and products. To override the default behavior, view the desire... |
Problem Statement: What is the maximum number of connections to an Aspen Cim-IO server? | Solution: The Aspen Cim-IO Core limits each program to 128 connections to a Aspen CimIO server. Note; Prior to Aspen Cim-IO v10.1 the limit was 64 connections.
If the maximum number is reached the following message appears in the CIMIO_MSG.LOG file.
CIMIO_MSG_CONN_FULL
Multiple connections are typical with Aspen Cim-... |
Problem Statement: What is the compatibility of Aspen Capital Cost Estimator with Primavera P6? | Solution: The Icarus Project Scheduler (IPS) requires the installation of Primavera P6 Professional Project Management software. The following table list the current compatibility:
Aspen Economic Evaluation Primavera P6
V8.6, V8.8, V8.8.2 Primavera P6 Professional 8.2
V9, V9.1, V10, V10.1 Primavera P6 Professional R1... |
Problem Statement: _TANKS table value does not match with the TNKINV value of the tank inventory, is this a defect? | Solution: This is by design,
If the inventory volume is greater than 0 and less than 3.21e38f then the starting volume of the tank is the value specified in the TNKINV table and the weight is calculated.
Else if the weight of the tank in the inventory table is greater than 0 and less than 3.21e38f then the starting w... |
Problem Statement: Why do I see XAML naming error when I register extensions with a specific name (i.e. satu$rate.dll)? | Solution: Aspen HYSYS shows XAML naming erros (and even sometimes crashes) because V10.0 can only handle alpha-numeric characters when constructing an XAML name (based on DLL name) as the Aspen HYSYS Palette was rebuild.
For example: extension with name satu$rate.dll or saturate.0.dll will show this problem. By chang... |
Problem Statement: Does Aspen calculate shear-dependent viscosity for melted polymers? | Solution: The viscosity of melted polymer is usually very high, and it is a function of shear rate (shear thinning/shear thickening). Therefore, melted polymer is a non-Newtonian fluid. The shear effect on melted polymer viscosity needs to be considered when doing equipment design and rating, like heat exchangers.
How... |
Problem Statement: When trying to write values with over eight digits into Aspen InfoPlus.21 the last digit is usually incorrect in the value written.
The precision problem is not actually a problem within IP.21 but with the conversion to a real value: IP.21 will save the value after a conversion to real was made at ... | Solution: To keep precision for values with more than 8 digits it is necessary to use a record which value field has been set to use a Double Precision Real value; IP_AnalogDef is not designed to work with this, but it is possible to create a custom definition record that accepts these values. Having this it is possibl... |
Problem Statement: In the Aspen Plus manual Getting Started Modeling Processes with Solids, the following stoichiometry is used for coal drying:
COAL(wet) -> 0.0555084 H2O
Where is this particular number of 0.0555084 coming from? | Solution: Aspen Plus treats all non-conventional components as if they have a molecular weight of 1.0. The reaction indicates that 1 mole (or 1 lb.) of coal reacts to form 0.0555084 mole (or 1 lb.) of water. Therefore, 0.0555084 is coming from 1/ 18.01528 (the molecular weight of H2O). It's used to keep the mass balanc... |
Problem Statement: How to modify the exchanger weight that is used for Lift Lugs calculations? | Solution: Shell & Tube Mechanical designs each lift lug to lift the entire vessel. So, 2 lift lugs are designed for 2X the vessel weight, 1 lift lug for 1X the vessel weight, etc.
Even when the program calculates the vessel weight, this can be overwritten to account for any additional weight:
1. Go to Input | Program ... |
Problem Statement: How to vary the solid phase heat capacity in different nodes of the bed layer? | Solution: By default, Aspen Adsorption is going to use a constant solid phase heat capacity for the entire bed. However, since V9, we added a new feature to allow the customer to vary the solid phase heat capacity in different nodes of the bed layer from a user submodel. This allows the heat capacity to vary axially, a... |
Problem Statement: This | Solution: frames on the Use Double and Single precision on IP21 and the effect related to DCS and DMC3 controller.
Solution
IP.21 will save the value after a conversion to Real made at computer chip level. This is following the IEEE 754 standard, so the value is saved as a single-precision floating-point value, this is... |
Problem Statement: I have an Aspen Properties Fluid Package using the Peng-Robinson EOS as the property package, but critical properties cannot be calculated for my material stream(s). Why? | Solution: The ‘Critical Properties’ analysis tool in Aspen HYSYS can only be used when users set up a HYSYS Fluid Package with either the Peng-Robinson or SRK cubic EOS, as shown on the images below:
So, if the Fluid Package is an Aspen Properties one, even using either Peng-Robinson or SRK, the analysis will fail, ... |
Problem Statement: For the Continous Catalyst Reforming (CCR) reactor model, does the model assume any value for carbon on the regenerated catalyst (COR)? Would it be possible to study the effect of COR on the product spec? | Solution: The CCR reactor model basically assumes that the coke on catalyst is zero for the regenerated catalyst. How much would the COR vary? For the most part, it would be close enough to zero to not matter, but if users want, they can shift to specifying the coke-on-catalyst (COC) for reactor 1 and add whatever valu... |
Problem Statement: Which heat capacity ratio should be used for API relief calculations? | Solution: We advise the use of the Ideal Gas Cp/Cv method if doing the analysis in the Aspen HYSYS V10 Safety Analysis Environment. In fact, the Ideal Gas Cp/Cv was added to the stream properties view just for this purpose (i.e. facilitation of relief valve rating calculations using the Ideal Gas Cp/Cv), as shown in th... |
Problem Statement: In Aspen Plus Dynamics, how can I know what are the names of both the PV and OP variables of a controller? | Solution: To know the PV and OP variables of a controller in Aspen Plus Dynamics, just right-click on the inlet and outlet signal streams of the controller and go to the Forms | AllVariables sheet. The inlet signal stream will show what is the PV and the outlet signal stream the OP, as shown on the images below:
Keywor... |
Problem Statement: I recursed compositions for C4M in upstream submodel and created depooling structure as below.
Why do I get error ' *** Error. Distribution of XXX to YYY in ZZZ is not Permitted'? | Solution: The error is related to the structure of error distribution and PDIST table.
There is a pool, C4M in the PIMS model.
The compositions for C4M are recursed with the recursion row, RC4UC4M and RC4IC4M.
And they will be used by E-row, EC4UC4M and EC4IC4M in depooling structure.
But this is not permitted because ... |
Problem Statement: For a compressible fluid the velocity at the outlet of pipes is always greater than the velocity at the inlet. Why? | Solution: In compressible pipe flow this behavior is expected due to the following:
1) Velocity rises along the length of the pipe as density decreases when the fluid is moving from higher to lower pressure.
2) Temperature decreases because internal energy gets converted into kinetic energy (as velocity increases).
K... |
Problem Statement: What is Aspen Hydraulics and how does one use it? What features of Aspen Hydraulics are currently available in Aspen HYSYS Upstream? | Solution: Aspen Hydraulics enhances the pipeline simulation of pipes and pipeline objects like junctions, mixers, swages, and valves within Aspen HYSYS. Pipeline and hydraulic network simulations can be solved in Steady State mode or Dynamic mode on a single network, with the ability to switch between the two modes and... |
Problem Statement: How to resolve the error message “unable to validate server response. HTTP code:510” in A1PE? | Solution: When trending some tags in A1PE, user might get the following error message.
To resolve this error, please follow the below steps.
Launch AspenONE Credentials as shown below
2. Disable Domain Security and hit Apply as shown below
Keywords: HTTP code: 510
A1PE
References: None |
Problem Statement: How to force liquid entrainment in vapor line in case of pressure relief scenario? | Solution: By default, vapor port connected to any vessel (like flash tank, reactors) only allows vapor flow through it. But in some cases, specially pressure relief scenarios, swollen liquid may also need to be pass through vapor line.
To enable this option, please right click on vessel to access Forms > Configure > Ve... |
Problem Statement: What is the difference between heat exchanger and LNG exchanger in Aspen HYSYS? | Solution: Below is the difference between heat exchanger and LNG exchanger on HYSYS:
Heat Exchanger:
- Used to model heat transfer between two process streams (hot & cold).
- Select preferred Heat Exchanger Model depending on required simulation detail.
- For rating calculations to calculate heat transfer coefficient a... |
Problem Statement: How to initialize RCSTR with padding gas? | Solution: RCSTR can be initialize with a padding gas for specified reactor pressure. To enable that Please select the Configure form > Hold up > select “Pad Component”
Then Check and specify initial Pressure. Once complete, please run the “Initialization” mode.
Key Words
Initial, Padding gas, Pressure
Keywords: None
... |
Problem Statement: What is the difference between pump efficiency and driver efficiency? | Solution: When specifying a pump, you will see two efficiencies. One is the pump efficiency, and the other one is the driver efficiency.
Pump efficiency is the ratio of the fluid horsepower to the brake horsepower. It includes the effects of slurry characteristics, frictional losses in seals, capacity losses due to se... |
Problem Statement: Why excel files are being unattached and PIMS model file (pimx file) is deleted, and how can I solve it? | Solution: The excel files are not attached in the model when opening the pimx file because PIMS cannot read the pimx file. This pimx file is an encrypted, xml file.
Please install Microsoft's KB updates: KB954430 and KB973688 or get the MSXML 4.0 DLL from another machine to copy to the problematic machine.
Keywords... |
Problem Statement: Can EDR Air Cooler model condensation on the outside of the tubes? | Solution: As stated on the Help Guide, the program does not calculate outside condensed liquid when Gas (property specified or from Databank) is selected for Outside tube application. The program can calculate outside condensed water only when Humid Air option is selected, and even then, it will not report an outside l... |
Problem Statement: Why are the MIP threshold values for a product not being honored? | Solution: This Tech Tip explains why sometimes it looks like the MIP threshold values for a product are not being honored and how to attend this issue.
To do the following demonstration we used the Demo model located in C:\Users\Public\Documents\AspenTech\Aspen Petroleum Scheduler\Demo\Access, we will use all the comp... |
Problem Statement: How do I calculate/report the Combustion Temperature of a fuel stream? | Solution: The Combustion Temperature is not reported in Aspen HYSYS as a default variable/property. However, you can obtain the combustion temperature from the flue gas of a fired heater model. The flue gas temperature is calculated by combusting the fuel streams with the air stream and transferring a percent (determin... |
Problem Statement: I would like to track the erosion rate for the whole pipe network in a Hydraulics subflowsheet, similar to what I see in pipe segment. How do I accomplish this? | Solution: Unfortunately there is no direct way to show the overall erosion rate as in a pipe segment. There are three options we can use to get this:
1.- Get the report for each pipe. Enter to the Hydraulics subflowsheet, and fro each pipe select the Flow Assurance tab where you can sactivate the Erosion Speed analysi... |
Problem Statement: When running the Icarus Excel reports, a message pops up referring to an Excel Report Header Error and/or the named range does not exist in the template | Solution: These error messages may come up for one of the following reasons:
1. If you use or have modified the Reporter_User.accdb file (found in C:\Program Files (x86)\AspenTech\Economic Evaluation VX.X\Program\Sys\Reporter\Database). Where VX.X represents your current version.
If a new Excel report was added in 'Sto... |
Problem Statement: How can whole crude property update process in the EIU be simplified? | Solution: In order to import Assays information you can use EIU, the import process is described in kb article How do I add new crudes to APS model?, this can consulted in the following link: https://esupport.aspentech.com/S_Article?id=000014626; this process requires additional clean up with Whole Crude Data worksheet... |
Problem Statement: How can I model a rate-based packed tower in Aspen Plus? | Solution: When modeling distillation towers, equilibrium stage efficiencies are sometimes employed to account for the fact that the amount of mass transfer between liquid and vapor phases may not be sufficient to result in thermodynamic equilibrium being reached. While utilizing equilibrium stage efficiencies can be u... |
Problem Statement: How do I prevent the “Results Warning 1527: The HTFS Condensation Mass Transfer method failed, or was applied to an inappropriate system. The program used the default method (Silver-Bell) for the gas-phase resistance in condensation”? | Solution: From Input Program Options | Method/Correlations | Condensation | Condensation heat transfer model, there are two options:
HTFS – Silver-Bell: is the standard method for mixture condensation or condensation from a non-condensing gas in Shell&Tube, is an adaptation by HTFS of the Silver (Bell and Ghaly) method... |
Subsets and Splits
No community queries yet
The top public SQL queries from the community will appear here once available.