question stringlengths 19 6.88k | answer stringlengths 38 33.3k |
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Problem Statement: The flare tip outlet pressure that I am seeing on the flare tip Summary tab does not correspond to the atmospheric pressure that I specified in the Calculation Options Editor. Why is this so, and how can I fix this? | Solution: It is possible that a different system back pressure for a particular scenario has been set on the General tab of the Scenario Editor (under Build | Scenarios). This would normally be atmospheric pressure, but it is sometimes used to represent system design conditions at the exit point. If a system back press... |
Problem Statement: How to directly import Aspen HYSYS Depressuring Utility peak flow results into sources | Solution: The composition, temperature, pressure and mass flow results of the depressuring utility peak flow can be imported directly as the data for the sources in the flare system networks built in Aspen Flare System Analyzer.
1. Make sure your Aspen HYSYS depressuring utility solved.
2. Go to Aspen One button in Asp... |
Problem Statement: What is the difference between the flow regime by Beggs & Brill on the pipe window and the one on Results | Flow map? | Solution: The Flow regime presented under Results | Flow map is calculated accordingly to Mandhane flow map.
On the other hand the flow regime calculated by Beggs & Brill is calculated based on the flow regimes that are part of the Beggs & Brill correlations, e.g.
The Beggs & Brill method was primarily develope... |
Problem Statement: Can I add my own fitting to the fittings database? | Solution: Yes, it is possible to modify the fittings database used in Aspen FLARENET to include a user-defined fitting. The fitting can be added to the database interactively, i.e. while Aspen FLARENET is running. While the program is running go to the Database menu and select Pipe Fittings from the list of available o... |
Problem Statement: Can I edit multiple pipe segments simultaneously? | Solution: Yes, it is possible to edit multiple pipes simultaneously by following the steps below:
1. Select Pipes from the Build menu and select multiple pipes by holding down the <Ctrl> key and picking the desired pipes from the list.
2. Click on the Edit button to display the Pipe Editor view.
3. Make the appropriate... |
Problem Statement: What parameters define the flare tip curve: mass flow versus total pressure drop or rated flow versus total pressure drop or flow versus static pressure drop? | Solution: The flare tip curve allows the user to input mass flowrate versus static pressure drop at different molecular weights.
The mass flowrate is used because it does not depend on temperature and pressure unlike volume.
Many flare tip vendors provide the curve data in terms of total pressure drop. Currently, Aspen... |
Problem Statement: Where are the \Samples, \Database and \Help folders located in the Aspen FLARENET 2004 installation? | Solution: In Aspen FLARENET 2004, by default the \Samples, \Database and \Help folders are installed to:-
C:\Documents and Settings\All Users\Application Data\AspenTech\Aspen FLARENET 2004\
This location is based on Microsoft's recommendation for User application data and is used to avoid problems with Administrators p... |
Problem Statement: What does the Rated Flow for Tailpipes option on the Calculations\Options\General tab mean? | Solution: When modelling tailpipes, FlareNet can base the pressure drop calculations on either the design (nominal) mass flows or the rated mass flows from upstream Relief Valve sources (see alsoSolution # 109493 for details of the rated flow calculation in Relief Valves http://support.aspentech.com/webteamcgi/Solution... |
Problem Statement: Can Aspen FLARENET be used for continuous flare/vent systems? | Solution: Aspen FLARENET is a steady state modeling tool that will calculate the pressures and flows throughout the network based on specified boundary conditions (flows at the relief sources and pressures at the flare tips). For convergent (non-looped) systems it can also be used to size pipes so that back pressure, M... |
Problem Statement: How can I make Aspen FLARENET calculate the outlet temperature of a PSV / BDV? It is asking me to input it. | Solution: To have Aspen FLARENET calculate a PSV/BDV outlet temperature, first ensure that you have selected a two phase VLE and enthalpy method (i.e. Peng-Robinson with Lee Kesler enthalpies). This can be done via the Calculations | Options | Methods menu item. You can then get the outlet temperature by clicking on th... |
Problem Statement: What does the option Calculate Ignored Sources with Zero Flow mean? | Solution: The MAWP constraint is ignored by sizing calculation when a source si ignored.
If the user selects the option Calculate Ignored Sources with Zero Flow (located under Calculations | Options), then the sources that have been ignored will be treated as if they have zero flow.
This will result in the back pressur... |
Problem Statement: How can a multi-stage flare tip pressure drop curve be entered in Aspen Flare System Analyzer? | Solution: For detailed information about entering regular curves on flare tips, please reviewSolution 109487.
The best available way to enter this kind of data is to enter it as a single curve. The only challenge while handling these types of curves is if there are two different pressure drop values for the same mass f... |
Problem Statement: When you are using the Exchanger Design and Rating (EDR) functionality embedded inside of Aspen HYSYS and you try to print the datasheet of a heat exchanger, the printed document has several pages.
The problem is that after the first page, you have a page feed for each item. The issue occurs only wh... | Solution: The workarounds are:
Export the *.edr file, then run in the standalone version 7.3 to print.
To print in EDR V7.3 follow the steps below:
1. Go to the File Menu > Print
2. Check the box against the Calculation details
3. Select Print
Upgrade to V8. This is a defect that has been fixed in V8.0 an... |
Problem Statement: How can I predict laboratory data of oil and gas mixtures accurately using an Equation of State (EoS)? | Solution: Cubic equations of state (EoS) usually do not predict laboratory data of oil/gas mixtures accurately without tuning of the EoS parameters. DBR PVT Pro provides a wizard to guide the user through the tuning process. Model tuning is achieved in Aspen HYSYS by using a multi-variable regression package to fit one... |
Problem Statement: How can I specify a fixed pressure drop across a Flare Tip? | Solution: You can force FlareNet to use a fixed pressure drop across a Flare Tip by specify a Pressure Drop Curve with a single data point of zero flow and the required pressure drop. Ensure also that no reference temperature is specified to prevent FlareNet from performing a pressure drop temperature correction.
See a... |
Problem Statement: In Aspen Flare System Analyzer, users can specify back pressure and relieving pressure. What is the maximum pressure value set in Aspen Flare System Analyzer? | Solution: The allowable back pressure upper limit set in Aspen Flare System Analyzer is 600 bar while the back pressure upper limit is 1000 bar. This is usually reached when the model is not converging.
The relieving pressure upper limit set in Aspen Flare System Analyzer is 600 barg.
Keywords: limit, back pressure, re... |
Problem Statement: Why doesn't the utility design load match the sum of each exchanger load in Aspen Energy Analyzer? | Solution: This utility load discrepancy is due to an inappropriate splitter ratio for this utility.
In Aspen Energy Analyzer (AEA), one utility stream can be split into branches in order to satisfy the Heat Exchanger Network (HEN) design requirement. As the split ratio for the utility cannot be determined automatically... |
Problem Statement: The pipe segment block inside a Hydraulics subflowsheet gives the user the option to Estimate the heat transfer coefficients to calculate the heat losses to the environment. What are the methods used for estimating those values? | Solution: There are a few different methods available:
· For the inner convection heat transfer coefficient, the calculation in Hydraulics is done with the HTFS method. This method is further described in the HTFS Handbook.
· For the outer convection HTC, the method used is described by J.P. Holman in... |
Problem Statement: I have multiple scenarios in my case - how can I tell which scenario is active? | Solution: At the far right-hand side of the row of icons below the main menu is a drop-down list containing the names of all the scenarios in the case. The scenario name which is displayed is the active scenario. To switch active scenarios, select the drop-down arrow on the right-hand side of the list and choose the de... |
Problem Statement: What is the best way to model a pure steam system in Aspen Flare System Analyzer? | Solution: In order to model pure steam correctly, you need to do the following:
1. Make sure your inlet is steam. If you only specify the relieving pressure and inlet temperature at bubble point, Aspen Flare System Analyzer may treat as inlet. You may want to use superheat option and give a small number for superheat v... |
Problem Statement: How to model splitter? | Solution: Reverse the TEE to make it splitter. For example, make one outlet as inlet and inlet as two outlet (inlet and branch) TEE can handle negative flow.
Note: Red dot is normally an inlet and blue dot is an outlet. If you connect outlet at red dot and inlet at blue dot, Flarenet solver will represent it as negativ... |
Problem Statement: How are two-phase sonic velocities calculated in FlareNet? | Solution: FlareNet uses a homogeneous model assuming no-slip between phases for the calculation of two phase sonic velocities (in general the assumption of a homogeneous two-phase mixture is reasonable given the flow velocities usually experienced in flare systems). The sonic velocity is defined as:
c^2 = dP/d(rho) @ c... |
Problem Statement: Can I specify only the molecular weight of a stream without inputting a composition? | Solution: Yes you can, however you still need to specify a component slate. Once you have selected the components, you can then specify the molecular weight of the stream. Flarenet will then look at the molecular weights of the components that straddle the specified molecular weight and propagate the corresponding comp... |
Problem Statement: What does the colour of the status bar in FLARENET mean? | Solution: The FLARENET status bar is activated via the Show Status Bar option under the File\Preferences menu. When activated, the colour of the status bar has the following meanings:
RED - no scenarios calculated
YELLOW - some scenarios calculated
GREEN - all scenarios calculated
Keywords: status bar colour color
Ref... |
Problem Statement: OLE Automation Example, Produce a table of which sources are active/ignored for all scenarios in the model | Solution: Attached is an Excel spreadsheet that uses OLE Automation code to produce a table of which sources are active / ignored for all scenarios in the model. Simply press the button to produce the table for the current Flarenet case.
When linking Excel to Flarenet, the Flarenet type library must be correctly refere... |
Problem Statement: What is the difference between a convergent, divergent and looped system? | Solution: A convergent system is a network that has a single exit point, e.g.
A divergent system terminates in multiple exit points:
In the case of looped systems, this applies when there are multiple flow path options:
Keywords: System
Network
Looped
Convergent
Divergent
References: None |
Problem Statement: How do I export data from Aspen Flare System Analyzer to MS Excel? | Solution: The attached excel files will provide a way to extract data from Aspen Flare System Analyzer. You will be able to select different scenarios and export the data to MS Excel. In order to do it, you have to open the Flarenet and the attached MS Excel at same time. If option Save Phase Properties (File->Preferen... |
Problem Statement: How to solve the error Design Calculations Not Available For Looped/Split Systems | Solution: Aspen Flare System Analyzer (AFSA) has three calculation modes available, there are described inSolution ID 119537
In Design or Debottlenecking run modes, AFSA first evaluates the amount of flow that goes through each pipe to then determine the conditions of this, then calculates the Mach number on each pipe ... |
Problem Statement: What is the Number Of Valves option for on the Relief Valve Editor \ Conditions page and how is the value used? | Solution: In Flarenet a single relief valve source can be used to model several relief valves connected to a common tailpipe. This is done by setting the Number Of Valves field on the Relief Valve Editor \ Conditions page to the appropriate value.
The value for the specified Number Of Valves is used as follows:
The spe... |
Problem Statement: How do I change the atmospheric pressure in Aspen Flare System Analyzer? | Solution: If you use Aspen Flare System Analyzer V7.2 or previous versions, you can go to Calculation->options->general tab:
Calculation:
Options Editor:
If you use version V7.3, you will need click Options in RUN group as following:
Options:
Options Editor:
Keywords: Atmospheric pressure, calculation, option... |
Problem Statement: The relief valve in Aspen Flare System Analyzer is sized based on static pressure at the outlet of the relief valve. What is the basis for sizing pipes, flanges and fittings? Total pressure or Static pressure? | Solution: Normally, the design aspect of the tailpipe and header piping is a sizing exercise (i.e. selection of appropriate diameter) such that one or all of the Mach number, velocity, Rho V2 and noise constraints are satisfied.
The pipe walls or fittings feels the static pressure, not dynamic pressure. Therefore sizin... |
Problem Statement: How can I change the number of decimal points for a variable that is shown in the output results of a .pdf? | Solution: Yes, User can change default settings by following below procedure
Go to File || Preferences || Formatting tab || Click on Edit Variables Format tab
In next window under Objects please select Results then select required property to be changed under variable list then click on Format tab then change decimal d... |
Problem Statement: Can I protect my simulation with a password so no one else can modify it? | Solution: This option is not available in Aspen Flare System Analyzer.
However the databases can be protected so they cannot be modified, i.e. no one would be able to change the pipe fitting, schedule and components).
To do so, click on the AspenONE button on the upper left corner of the application window. Choose the ... |
Problem Statement: End users are getting a Aspen HYSYS Upstream licensing error after the installation of the new license file received from Aspentech and created after January 1st 2010. | Solution: From the SLM perspective the newer license files issued as of 1 January 2010 will only support the versions of Aspen HYSYS Upstream V7.1 and above and in the case of Aspen HYSYS Upstream V7.1 it has the following additional requirements:
? Aspen HYSYS V7.1 should be upgraded with the CP2
The hotfix ... |
Problem Statement: The temperature results do not match each other when switching between steady state model and dynamic model in the hydraulic subflowsheet. | Solution: One of reasons is not including dissipation effects in the energy balance during dynamics. By default, this is turned off (on the dynamics tab, solver control box, Dissipation during Heat Transfer). When the mass flow is pretty high, viscous dissipation can have an impact on the temperature profile. If you tu... |
Problem Statement: How can I import a PVTSim text file into HYSYS? | Solution: The user can add PVTSim .txt file into the Fluid Basis using the PVT Environment inside HYSYS. It does not require a separate PVTSim reader, but to access this feature the user will need the HYSYS Upstream license.
1. First enter the Simulation Basis Environment and select Enter PVT Environment.
2. From the P... |
Problem Statement: How does Hydraulic subflowsheet calculates the pressure drop for single phase flow when I set up the pipe with two-phase flow correlation? | Solution: In a single phase flow in steady-state, Hydraulics uses the darcy equation. In a single phase flow in dynamics, one momentum and one energy equation are solved. The interfacial terms are zero and a single friction factor is calculated for the single phase.
Keywords: Single phase, two phase flow, HTFS, pressur... |
Problem Statement: In HYSYS Dynamics, the pipe segment can model heat transfer using a cylindrical co-ordinate system when selecting the 'Radial Losses' option. What does this mean? | Solution: In HYSYS dynamics the Radial Losses option inside the pipe segment is shown below:
Heat conduction in solids can be reduced to theSolution of a single differential equation. The equation can be derived by making a thermal energy balance on a differential volume element in the solid. For the case of conduction... |
Problem Statement: In Aspen HYSYS what stream input variable should I use to represent Sm3/h? | Solution: The unit of measurement Sm3/h refers to Standard Cubic Meter per Hour which means the flow rate per hour at standard conditions.
In Aspen HYSYS, the stream variable input for Sm3/h will be the Liq Vol Flow @ Std Cond. Refer to Knowledge Base article 110700.
Standard condition varies from industry to indust... |
Problem Statement: How do you set the Stock Tank Density property in a stream? | Solution: This property is only available when you use the Oil and Gas Feed page to define your stream. The Oil and Gas Feed page it is used to define stream composition as a mixture of oil and gas. You can define the feed makeup as an oil and gas feed using bulk properties or one using information from an imported pet... |
Problem Statement: How to fix dbupdate error: Failed to execute, file sharing lock exceeded. | Solution: This error is caused when the conversion process failed to modify a Table (Example CRDCUTX Table as shown in the screenshot). It is a common error message that is issued when the specific Table contains too many records (CRDCUTX, in this case). This problem can be resolved by increasing MaxLocksPerFile. Plea... |
Problem Statement: What is the definition of the Compressible Transition value located in the Aspen Hydraulics Orifice? | Solution: The Compressible Transition defines the pressure drop as a fraction of the inlet pressure at which compressible flow pressure drop calculations will be used. For fractional pressure drops larger than the specified value, compressible calculations will be used. Enter zero to always use compressible calculation... |
Problem Statement: In Aspen Refinery Multiblend Optimizer, you cannot see the Beginning Inventories data input screen enabled, after creating a new Event Screen, Why? | Solution: Every Event Screen for Aspen Refinery Multiblend Optimizer, requirs at least one Product be defined. If any of the screens does not have a Product defined, then the Beginning Inventory data input Screen is disabled, for that particular Event Screen.
To enable this Option, you need to define at least one o... |
Problem Statement: How do I report results in both volume and weight for Aspen Multi-Blend Optimizer? | Solution: 1) Turn on memory cache and then run the optimizer
2) Click on report wizard
3) Click on new template
4) Click on Get Started
5) Select volume and weight and push it to the right hand side by clicking on the arrow
6) Click next, give a name in the next dialog and then click finish
7) ... |
Problem Statement: You may notice that if you attempt to lump pure non-petrochemical components (hydrogen, for example) to hypothetical components – you will get some unrealistic property predictions as shown in the following image. | Solution: The lumper and de-lumper are unit operations intended to help manage converting component sets to different bases.
The Lumper converts a large number of pure and hypothetical components to a smaller reduced slate of components required by other applications, to improve performance or match known stream char... |
Problem Statement: The value for ‘Regime’ in the Profiles page in the Performance tab of a Pipe Segment inside an Aspen Hydraulics subflowsheet is displayed as: Unknown. | Solution: The prediction of the flow regime is performed using the calculation method specified in the Data page of the Design page of this unit. If the default option (HTFS) is selected, no flow regime prediction occurs. The same applies to the following methods: Lockhart and Martinelli, Hagedorn and Brown, and Dukler... |
Problem Statement: I am unable to specify the maximum return of investment when I add a heat exchanger in Retrofit mode? | Solution: Inside the base case in retrofit mode it is possible to conduct a retrofit design such as ‘Add Area’ to optimize the heat exchanger network (HEN) design. This feature to add area to optimize the HEN diagram is shown below:
Select the ‘Add Area’ to optimize the HEN
The user selects the base design inside ret... |
Problem Statement: From the 'Model Settings' window, do we need to configure 'MBO ODBC Data Source Name (DSN)' when we choose to use MBO Microsoft Access Database File? If not, why does it show a DSN name? | Solution: The 'MBO ODBC Data Source Name (DSN)' field reads the User DSN and System DSN of the ODBC data source in the machine automatically. In the above screen, it shows 'AspenScop11g' which is the first DSN data source which is shown on this field by default.
In the above model configuration, it reads recipe source ... |
Problem Statement: What could cause Aspen Petroleum Scheduler (APS) or Aspen Refinery Multi-Blend Optimizer (MBO) to crash when launched? | Solution: There are multiple causes that can lead the application to crash. Please follow the next steps to find the root cause of the problem.
1. Check the version of the APS/MBO on the machine. The application folder is located by default in the next path: C:\Program Files (x86)\AspenTech
           ... |
Problem Statement: How can discretization of pipe segments cause dynamic run issues? | Solution: The spatial discretization plays an important role on the time step on dynamic Integrator. When arranging different length pipe segments in Hydraulics sub flowsheet, please make sure number of cells selected will result into uniform length/cell. In the screen shot, pipes are of different length while number o... |
Problem Statement: What is net cross pinch duty? | Solution: Net cross pinch duty is the sum of all cross pinch duties in a heat exchanger network (HEN).
Keywords: Net cross pinch duty
References: None |
Problem Statement: Does modifying the pour point, wax content or paraffin number using an Assay Manipulator affect the feed characterization properties of a Hydrocracker? | Solution: Using a manipulator to modify these properties does not affect the feed characterization in the Hydrocracker. This behavior is normal since by default these parameters are not considered directly as part of the calibration for the feed properties.
The hydrocracker uses the specific gravity, the 9 distillation... |
Problem Statement: I would like MBO to always give inventory infeasibilities over quality infeasibilities. This way MBO will allow component tanks to go infeasible in order to make on spec blends if necessary. | Solution: In order to accomplish this you can increase the Specs Infeasibility Breaker Factor. For example, the next blend was optimized with a Specs Infeasibility Breaker Factor equal to 1:
Notice that we are not complying with specs DON and T160 and we don't have enough inventory of HCL and ALK.
If we change the valu... |
Problem Statement: What is Improved in Aspen HYSYS Upstream V7.3 - Aspen Hydraulics and HYSYS Pipe segment | Solution: Aspen Hydraulics is a subflowsheet available with Aspen HYSYS Upstream for the rigorous modeling of pipeline and hydraulic networks. In V7.3, both its flexibility and functionality has been improved, which are summarized below and in the attached presentation.
Substantial Improvement inSolution Speed for Stea... |
Problem Statement: What could prevent the actual volume flow calculated by the stream from matching the user-supplied oil flow target? | Solution: The oil flow target supplied by the user in the material stream (Worksheet tab/Oil & Gas Feed page), is assumed by Aspen HYSYS to be at stock tank conditions and relatively free ofSolution gas. Therefore, the input value may not be the same as the actual liquid flow, or actual volume flow - liquid phase, whic... |
Problem Statement: I'm in the process of making additions and deletions to our component tanks in MBO. Nevertheless, when I add a new component in Model/Components, I cannot see it in the Model/Component Rundowns section. | Solution: In order to the component to appear in the Component Rundowns section, the component must be used in a product blend. For example if I add the component CMP1 in the component section:
I will not be able to see it in the Component rundown section:
Until I have specified it to a blend in Model/Products (reme... |
Problem Statement: Tray sizing Warning: Weir loading is too high | Solution: This is a warning to inform users that the calculated weir load by Aspen HYSYS has exceeded the user specified Max Weir Loading or the default value of 120 USGPM/ft If not specified by user.
The weir loading is a measure of the liquid loading on the weirs. Aspen HYSYS calculates the average weir loading for a... |
Problem Statement: What are the definitions of Oil & Gas Feed (Black Oil) properties in Aspen HYSYS Upstream? | Solution: Oil Formation Volume Factor (FVF) - The Oil FVF is equal to the ratio of the volume of oil andSolution gas at the given process conditions to the volume of dead oil at stock tank conditions.
Solution Gas Oil Ratio (GOR) - TheSolution GOR is a measure of the amount of gas dissolved in the oil at current proces... |
Problem Statement: I know the inlet stream pressure and the outlet stream pressure as well as the temperature of each, the composition, the heat loss, and the length and diameter of my pipe. Will HYSYS be able to calculate the flow rate of my stream given those conditions? | Solution: This is achievable with the Hydraulics Sub-Flowsheet in HYSYS.
To calculate the flow through the pipe given stream and pipe conditions/dimensions you must do the following:
1. Add the stream in question, and give it Temperature, pressure and composition specifications:
2. Add the Hydraulics subflowshe... |
Problem Statement: How can I model restriction orifice in a pipe line? | Solution: You can enter the orifice diameter or upstream diameter ratio or downstream diameter ratio.
Note: Orifice can be used to divert the flow from one direction to other direction in the network. For example if flow is moving in direction A and direction B (user have two flare tip). And capacity to handle large fl... |
Problem Statement: Aspen HYSYS Automation including ASW no longer works after installing a new version: “Error dll not found� | Solution: Certain object type interfaces have changed in newer releases of Aspen HYSYS, so tlbs of different versions are slightly incompatible. Windows will always go to the newest version of the type library when finding interfaces, even if the interfaces were registered with an older version of the type library. T... |
Problem Statement: Optimization in MBO takes too long when using Rundown components. | Solution: The performance is a direct result of the large size of the resulting MIP problem. In order to improve performance the user can follow the next steps.
1.- Open the CONFIG table inside the database:
2.- Add the next line:
3.- Save the database and run the optimization.
This will reduce theSo... |
Problem Statement: I have a software crash when using Aspen HYSYS. How do I view the Event View Log to analyse the source of the crash? | Solution: To help Customer Support solve the issue surrounding the crash we might require the Event View Log. The steps below detail how one can retrieve the Event View Log for the associated crash in Aspen HYSYS.
1. Open the Event Viewer by searching through Windows Search Function.
2. Select Application once ... |
Problem Statement: When a stream line is broken and when it's not? | Solution: A solid stream's line means the enthalpy change (duty) of the stream is completely used by exchangers.If there is a gap in it, then that portion is shown by broken line.
Keywords: Broken, stream, solid
References: None |
Problem Statement: What is the Logic behind tanks included in beginning inventories dialog box? | Solution: The logic is that the component must be a part of a blend product on the screen, for it to show up in the beginning inventories dialog box.
Following is an example using the sample model:
The concerned component is Butane and the component tank is TBUT. Component BUT is part of U87, as defined here:
This will... |
Problem Statement: How to locate the time range for a data set that has been imported into APC Builder? | Solution: A user can see (and edit) the time range of the dataset when vector files are initially imported from an external file source into APC Builder.
For the data sets that are already imported into APC Builder, the user will need to look up the properties of the data set in order to view the time range. However, t... |
Problem Statement: The user wants to set the same value for a variable in a large number of objects in a flowsheet, and be able to change this value without opening each object and introducing a new specification. For example, we may want to set the same value of temperature or pressure in multiple inlet streams to a p... | Solution: There are several ways to connect variables in the flowsheet. Assume that we want to specify the same value of a variable (e.g. temperature) to N objects (e.g. N streams). Consider the following options:
1- Using a Set function between two blocks. This involves introducing and specifying N-1 blocks, where the... |
Problem Statement: Aspen Refinery Multi-Blend Optimizer (MBO) now allows the user to change the prices of components, products and tank increases and decreases in the inventory using new feature called Time varying prices | Solution: Since V7.1 three database tables have been added to support this feature and data entered directly:
- ATORIONMaterialPriceDef : Identifies Material Pricing available to the model
- ATORIONMaterialPriceDetails: Price and time when a material pricing is applicable
- ATORIONMaterialPriceSet: Adds a description t... |
Problem Statement: How to troubleshoot, Aspen Process Controller?s Online Servers are not running, after an upgrade? | Solution: After upgrading Aspen Process Controller?s Online Servers are not running.
The following message appears:
?APC Builder
Could not connect to online server `server name?.
Verify that you have permission to access the online system.
Verify that the network is up.
Verify that the Aspen Production Control RTE Serv... |
Problem Statement: How do I configure cache reads for APC software? Aspen Process Controller exception | Solution: How do I configure cache reads for APC software? Aspen Process Controller exception
In the Aspen Process Controller's Online menu \ Configure This Server
Configuring for IO Source Type: OPC
Uses cached reads
Check box, which if selected, enables retrieving tag values from a tag value cache maintained by the O... |
Problem Statement: Regarding the MV definition in the token contract, is it only refer to manipulated variable and doesn't include the Disturbance Variable and Feed Forward Variable?
In other words, the SLM will only charge token by counting the number of manipulated variables but will not count the number of Disturban... | Solution: Correct.
From V 7.1 DMCplus started to support token license. And, its software license agreement says token consumption is based on the number of MV(Manipulated Variable). Feedforward/Disturbance variables are not counted for Token consumption. Only MVs is counted for Token consumption.
Keywords: MV
CV
Token... |
Problem Statement: How can I add and display additives in my BCI XML document? | Solution: These are the steps to display a new additive in the XML document:
1. In MBO:
a. Go to Model->Properties: Click on the New button.
b. Created a property and added additive parameters as follows:
c. In Model-> Products: Map this additive dopant to a particular product (U87-CTDR)
d. Also add... |
Problem Statement: Is there a way to retrieve the value of a parameter with a selector (MODE) from a unit operating event using automation? | Solution: Operating parameters of events are subitems of the Orion.EventItem and Orion.EventsColl methods. The Tag property will identify the parameter and the Quantity property will bring the value of that parameter.
For example, We have defined the next TEST Unit:
And We have added a new unit operation event with ... |
Problem Statement: Depressurization of Liquid filled vessels with Depressuring utility. | Solution: In a liquid filled vessel, the liquid level will be above the nozzle. When the valve opens, it is liquid that will flow out initially until there is sufficient vapour in the top of the vessel. The reason for this is that Aspen HYSYS vessels only allow nozzles to be specified on the side wall of the vessel not... |
Problem Statement: A value for the pressure drop multiplier is specified in EDR Fired Heater in the Program Options ¦ Pressure Drop menu:
However, when the simulation is run with this parameter, and then for the default value (one), the pressure drop ratio between the two runs does not equal the specified value for the... | Solution: The Pressure Drop Multiplier adjusts the stream frictional pressure drop. In order to analyze the effect of this parameter on the outlet stream pressures, the contributions of tube-tube loss and loss after bank in the firebox should be turned off. You can do so by specifying these factors as zero for the resp... |
Problem Statement: How to generate a datasheet (API type or more) in Aspen Fired Heater. | Solution: In Aspen Exchanger Design and Rating (EDR), we have the export to Excel function that can help users generate datasheet. People use this feature most frequently for Aspen Fired Heater because currently the overall summary does not have an API format datasheet.
Please follow the instructions below.
1. Go... |
Problem Statement: Why is my 3-phase separator not solving when using Acid Gas property package? | Solution: The Acid gas package is by default considering only two phases: Vapor and Liquid. To consider Vapor-Liquid-Liquid equilibrium you need to change the Phase Handling in the Properties environment for the package. After doing this, the 3 phase separator should be solved showing the 3 phases.
Keywords: 3 phase se... |
Problem Statement: A new option has been added in Multi-Period Blend Optimization dialog box | Solution: The Fix In-Progress Blends option has been added in v8.4 which allows users to specify the delay time when working with in-progress blends.
This option allows the user to fix the recipe of any blend that starts prior to the start of the campaign, as shown:
The Fix In-Progress Blends Delay, Min option, allow... |
Problem Statement: Beginning derived properties are not correctly calculated when importing the baseline (bad input data) Eg. DON is not being properly calculated from RON and MON values. Nevertheless, as these properties are derived properties, APS/MBO simulator should correct these values using the correlations defin... | Solution: APS/MBO assumes that TNKINV values are correct. So, the values published at model start date in _TANKS are TNKINV values. In order to tell APS/MBO to publish simulated values you need to add the PUBLISH_AT_10_SEC keyword in the CONFIG table with a value a of Y. This way, the correct derived properties will be... |
Problem Statement: What is the most suitable HYSYS property package to use with the following components: Water, Air, Ammonia, Carbon dioxide and Urea? Most fluid packages indicate that the Urea is in solid phase, whereas the Urea should be vapor in the stream. | Solution: The recommended property package is NRTL. Please find below a step-by-step procedure to select it.
1. Select Aspen Properties database
2. Add your components
3. Select Aspen Properties fluid packages
4. Select Electrolyte NRTL and click Electrolyte Wizard
5. Deselect Salt formation and tick Water dissociation... |
Problem Statement: When modelling an absorber using the Acid Gas package, the property page of the product streams takes a while to open (15-20 seconds). Why does this page take longer to open than any other page? | Solution: When opening the property view of the product streams for the first time, the program will take some time to calculate Cp/Cv and related parameters. This is because of the the rigorous calculation methods used by the acid gas package. This may not happen in every cases, for example the properties are already... |
Problem Statement: How does Aspen HYSYS calculate Bulk Velocity in the Erosion page of Flow Assurance tool? | Solution: The Bulk Velocity as reported in the Erosion page of Flow Assurance is the superficial velocity calculated at actual flowing condition.
Bulk velocity = Volumetric flow rate of the combined phases at actual condition / cross-sectional area of the pipe
Keywords: Flow Assurance, Erosion, Bulk Velocity
Reference... |
Problem Statement: How do I delete and reset my available unit sets to the system default in Aspen HYSYS? | Solution: The available unit sets are viewable in the Unit Sets feature found on the Home ribbon, which opens the Units of Measure menu of the Options window.
In the Load Preference Set button, the user can delete the current .prf file for the version they are using. Once this .prf file is deleted, the unit set will r... |
Problem Statement: How do I save APC controller changes? | Solution: The Aspen Production Control Web Server Manager only shows the Start / Stop button as an active option for the APC controllers.
To save the APC controllers changes you need to go to the APC Builder \ Online Applications (Online menu \ Applications) \ Get Snapshot button.
What’s a Snapshot: “A retrieved appli... |
Problem Statement: Is there a lookup table for AW_INDFLG values? | Solution: It may happen that one controller turns due to variable validation failure. In Aspen Watch, it is useful to see the AW_INDFLG to evaluate which failure this variable has.
A lookuptable for all the errors can be found in the message.dat file (under ProgramData\AspenTech\APC\Online\cfg).
For instance, the cond... |
Problem Statement: How to switch Models and Tuning Sets in APC applications? | Solution: Note: In Aspen Process Controller Builder, the feature for switching models / tuning sets is available only for FIR model-based applications.
Engineer permission is required. Go to Aspen Process Controller Builder, Online menu, Manage Model Switching. The related dialog box is displayed.
As prerequisite the... |
Problem Statement: How to adjust number of MIP iterations (MAX_MIP_ITER in CONFIG) in MBO? | Solution: In CONFIG setting of Aspen Refinery Multi-Blend Optimizer, MAX_MIP_ITER defines the maximum number of iterations under MIP constraints. The default setting for MAX_MIP_ITER is 100. In most cases, MBO will finish MIP iterations way before 100 so that there is little need to fine tune this parameter.After these... |
Problem Statement: Where can I find all of the Aspen Process Controller messages? | Solution: In V7.2 and earlier, the ACP online messages are stored in a system event log. You can use the standard Event Viewer utility (available from the Administrative Tools menu) to inspect it. In the Event Viewer you will see a custom event log called AspenRTE. Right click on it and select Save Log As. This will al... |
Problem Statement: How do I configure the Language support for Aspen Process Controller Builder? | Solution: Added in V7.3.0.2 and V8.0.0.2, language support is now available in Aspen Process Controller Builder.
There are ten (10) supported languages: English, Chinese, French, German, Italian, Japanese, Korean, Spanish, Portuguese and Russian.
When Aspen Process Controller Builder starts, it detects the Regional... |
Problem Statement: Why does my utility consumption from Retrofit Design go below the Energy Target? | Solution: It is true that the Energy Target is the minimum energy required using Pinch Technology. The utility consumption from user design or retrofit can either equal or higher than the target values. However, user may see the utility calculated from retrofit design goes below the Target, e.g. the screenshot as shown... |
Problem Statement: Can the Post sheet in the Units file be used to add additional constraints in MBO? | Solution: No. The post sheet cannot be used to impose additional constraints in Aspen Refinery Multi-Blend Optimizer. MBO only uses Units worksheet for UserCalcs or automation. If the user doesn't have any UserCalcs/automation in the model, even a blank Units file would work for MBO optimization.
Keywords: Post Sheet
U... |
Problem Statement: A new section called Adjust Stop/Start dependent events, has been added to the Model Settings tab associated with the Setting dialog box | Solution: The associated options allow you to truncate seconds from time dependent event Start/Stop times and to select what to automatically adjust, rate or volume, in order to accommodate the time changes.
Adjust Stop/Start dependent events:
These options allow you to specify if seconds will be removed from the Start... |
Problem Statement: Why can't I find vertical gridlines in trend thumbnails in v7.3.03? | Solution: After enhancing the vertical gridline features (see the Gantt Options - tab Graphic Features), we eliminated vertical gridlines in thumbnails. Thumbnails do not have tickmarks, but some gridline types cannot be implemented without tickmarks. Besides, it makes drawing faster. All the gridline features are set ... |
Problem Statement: Why are the Volume% Yields calculated in a Reformer different from the Volume Fractions reported by the stream properties in HYSYS? | Solution: The calculation of Volume% Yields and Volume Fractions depends on the density used for each component. These differences are caused by two reasons:
1. The density values the Reformer uses for Hydrogen, Methane, Ethane and Ethylene (represented as H2, P1, P2 and OL2 respectively by the Reformer) are not the sa... |
Problem Statement: How HTC is calculated? | Solution: The default velocity and flow area of a stream is given under Physical Properties tab. These two variables along with several physical properties are used to calculate HTC. You need to change the velocity and flow area to have relatively accurate HTC.
The equations used to calculate HTC is provided in page 13... |
Problem Statement: How do I report vapor pressure in Aspen HYSYS? | Solution: There is no direct way to report vapor pressure, however you can add a Property Table for each stream and calculate it.
Go to each stream> Attachments Tab> Utilities> Add> Property Table
Then in the Property Table,
Select the Temperature and the Vapour Fraction as the Independent Variables, and setup the Mode... |
Problem Statement: A new SLM v8.0 hotfix targeted to address high network bandwidth consumption for APC Controllers is available through | Solution: 138502. How does this affect the manner in which the APC software license checkout the licenses?
Solution
With the latest hotfix the APC software itself does not have a timeout on the license check. The message you see every 4 hours is more of a status message than an indication that another checkout attempt ... |
Problem Statement: How can I add constraints on the total volume of blends in MBO? | Solution: In MBO, trend limits can be used to add constraints. Trend limits on the tanks are hard constraints and are taken into consideration while optimization of blends. For example, if the user needs to put a constraint on the Sum of all premium blend volumes, a simple workaround is to blend all the premium blends ... |
Problem Statement: How do you calculate the Overall Efficiency and Firebox Efficiency shown under the Fired Heater Summary page? | Solution: Overall Efficiency = (Total heat absorbed by all process streams in heater)/(heat released from fuel combustion + sensible heat from fuel and oxidant)*100
Firebox Efficiency = (Heat absorbed by process stream in firebox)/(heat released from fuel combustion + sensible heat from fuel and oxidant) *100
Heat ... |
Problem Statement: In the the Configuration form for the column operation in Aspen HYSYS, the user needs to specify the number of trays. How many trays should be entered for a packed column? | Solution: In Aspen HYSYS, by default, the user supplies the number of theoretical trays and the pressure profile in the column. In this way it does not really matter whether the column has trays or packing as the internals. This is because, HYSYS uses the concept of equilibrium 'stages'. Stages in HYSYS do not necessar... |
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