==== AFT Fathom 7.0 (Version Date 2012.01.06) Release Notes ===== This file contains the changes that have been made to Fathom 7.0 *** Changes for Version Date 2008.02.22 *** None: Initial Release *** Changes for Version Date 2008.04.18 *** >> Changes to computation logic that could impact results << 1. This change does not affect results per se, but it does fix a problem that could prevent convergence. If modeling heat transfer, it was possible that a model would not converge on temperature if there were pipes which were non-flowing connected to a tee or branch which had other pipes which were flowing. This was fixed. 2. Fixed a problem where the losses for a detailed tee/wye that had flow coming in the branch and going out both straight-through pipes (or the opposite flow directions) were being set to zero. 3. Fixed a problem where during an XTS simulation where a transient was set on an Assigned Pressure and there were fixed flows in series a flow imbalance would occur at the branching points by the flows. >> Changes to data management that could impact results << 1. When using the XTS module and a pump with a fixed pressure or head rise model, and if the user is using a design factor or viscosity correction, the first time step calculation is correct but thereafter the design factor and/or viscosity correction to head rise gets multiplied twice for all subsequent time steps. This was fixed. 2. Fixed problem displaying the pipe heat transfer profile. The pipe outlet temperature was displayed correctly, but the others were set to the ambient temperature. 3. Fixed problem displaying BEP in the Pump Summary, it was always 0. 4. Fixed problem in Global Junction Editing where if only the database name was selected, the data was not applied, only the name which caused inconsistent data. >> Changes that do not impact results << 1. Fixed snap to grid problem when pipes or junctions were near an edge. 2. Fixed Workspace drawing anomaly when pressing the escape key while drawing a new pipe. 3. Was not displaying pulp and paper stock properties when using constant properties in System Properties. Fixed this. 4. Fixed printing problem for Graph Results which could cutoff part of a graph in certain cases. 5. Added a Caution message to the Output when user disabled either mass balance or energy balance in Solution Control. 6. Fixed display problem in Graph Results if a graph is made using the "Selected Solutions" tab and then another graph is made for a different tab. The x-axis labels were not being updated. 7. If cavitation occurred when using XTS and the time units in Output Control were other than "seconds" then the warning message would be incorrect as it would list cavitations time in seconds always rather than user time units. This was fixed. 8. In XTS models in some cases warning messages would not display for minimum values such as minimum pressure because the correct minimum was not being determined properly. This was fixed. 9. Allowed empty database files to be the target file in Database Manager. 10. Fixed problem in Visual Report where the junction output parameters were not shown. 11. Fixed problem importing Fathom 5.0 files that did not have efficiency data for a pump. 12. Fixed problem where the model data setting for pipes would not be set as the user default unless the Model Data Control window was first closed and reopened. 13. Fixed problem reselecting the previous selection when the selection was dissolved by clicking on the Workspace so nothing was selected. 14. Fixed a problem in the Fittings & Losses database the use of a comma in the type or subtype name would cause the data to become corrupted. 15. Databases are now automatically connected when added to the list of available databases. 16. Fixed a problem where detailed pipe data for non-cylindrical pipe in Model Data was not being displayed properly. 17. Added more information explaining what happened when a valid license was not found. *** Changes for Version Date 2008.04.30 *** >> Changes to computation logic that could impact results << 1. When data was reloaded from a past GSC model simulation and the GSC variable was a a junction that changed state (open/closed) from the initial point the flowrate results were not set correctly. This was fixed. >> Changes to data management that could impact results << 1. When a user-defined fluid was in an external database any changes to were not being saved. 2. When a goal used a density-based mass flowrate (like scfm) errors would be displayed and the incorrect actual goal was displayed when the model was reopened. The flows in the pipes and junctions were correct. >> Changes that do not impact results << 1. Fixed problem when using Fluid Groups and global pipe editing whereby the fluid group information could get corrupted causing an error when the model is run. 2. Changing units in the Heat Exchanger Summary would result in an subscript error. This was fixed. *** Changes for Version Date 2008.08.08 *** >> Changes to computation logic that could impact results << 1. Fixed a problem with the Viscosity Correction when the efficiency is entered as a percent with the pump curve. The conversion to decimal was done twice and the value was several orders of magnitude too low. Other values (flow, pressures, etc.) were not affected. 2. The laminar friction factor for Bingham Plastic calculations was not being converted to Darcy friction factor correctly. >> Changes to data management that could impact results << 1. There was a data handling problem with the parameter "Residence Time" when creating Graphs and the graph values were always zero. This was fixed. 2. Relief valves that use the Cv vs. dP loss model sometimes did not have any units set for the delta pressure and would generate errors. The units are now always set. 3. If a junction with pipe elevations/depths (like a reservoir) is moved and then the move is undone, the elevation/depth values were erased. This is fixed. 4. Curve fit configurations that use temperature would allow users to change the temperature units without redoing the curve fit. >> Changes that do not impact results << 1. When using the batch run on multiple model files and including Model Data in the output report content, and sending output directly to PDF files, the PDF file Was not created because of a file name issue. This was fixed. 2. When using the GSC module, if the user transfers both the GSC variables and the hydraulic results back into the initial guesses it could cause matrix errors on future errors. This was fixed. 3. When double-clicking a pipe or junction label on the Workspace, the user is offered the option of relocating the label or opening the specifications window. And the user has the option to remember the selection for the future. This final option was shown inadvertently and did not do anything. The option is now hidden. 4. In the Output window junction table the inlet and outlet static and stagnation pressures displayed confused some users in certain cases. Specifically, when junctions had multiple pipes connected the definition of inlet and outlet, as well as the difference between static and stagnation pressure was ambiguous. No calculation logic was changed, but the display logic was changed to make the displayed values less confusing. This was done for Spray Discharge, Assigned Pressure and Relief Valve junctions. 5. The thickness of insulation was not being applied to the pipes if a default insulation setting was added to the pipe thought the Material Database. If the name of the insulation data set was selected again in the pipe specification window and closed, the thickness would be applied. 6. If only one data point was used for a pump curve the resulting curve fit was not done and the graph looked like random noise. This was changed to be a flat line. 7. Flow units for HEX junctions in the curve fit configuration window did not have the default units set properly so it was possible to set the units to a blank value. 8. When user selects "No" when prompted to update the curve fits in the Curve Fit Configuration window after changes are made, control is returned to the configuration window instead of closing the window. *** Changes for Version Date 2008.08.21 *** >> Changes to computation logic that could impact results << 1. Fixed logic for GSC when a check valve closes during the goal seeking. The check valve stayed closed rather than re-opening when conditions allowed. 2. Improved logic for when multiple control valves cannot control and check valves, relief valves, and controlled pumps exist. In the past these other components could open, close or lose control when Fathom was trying to sort through which control valves could not control. Now Fathom waits until all control valves are first determined before looking at the other components. >> Changes to data management that could impact results << 1. When using the GSC module and a three-way valve with a GSC goal for valve position specified, if after the GSC run is finished the user transferred the goal value back to the input using the menu option, the Cv values did not get automatically updated for the valve position. If GSC was then turned off, this would make subsequent runs not agree with the GSC results. This was fixed. >> Changes that do not impact results << 1. If part or all of the Workspace where a hidden annotation is located the annotation would be selected. If the selected objects were deleted the annotation would also be deleted. Now hidden annotations cannot be selected and are not deleted. 2. Fixed a problem introduced in the 2008.08.08 release where the Add New Fluid button caused and error in Fathom. *** Changes for Version Date 2008.12.03 *** >> Changes to computation logic that could impact results << 1. Fixed a problem where a model would be reinitialized after a control valve failure to a flowrate larger than what can be produced by the pump. In certain closed-loop cases then could result in a matrix error. 2. Fixed problem with fixed volumetric flow rate junctions like pumps, assigned flows, and flow control valves when using volumetric flow rate and heat transfer. When the density was updated the volumetric flow rate was not always updated. 3. Fixed problem with single flow path systems which use ASME Steam Tables or Chempak. Pressure initialization was being skipped in this case and once physical properties were needed a zero value of pressure was passed into the ASME or Chempak data access. This caused an error. This was fixed. >> Changes to data management that could impact results << 1. Fixed problem reading in older models with a user specified additional loss valve. Unit conversion error would most likely occur when the decimal delimiter was a comma. 2. Fixed problem where the NPSH affinity exponent was being reset to 2 when the pump configuration was opened. 3. If doing heat transfer models and plotting pump and system curves, Fathom was allowing the density to change and it is supposed to stay constant in this graph. This could cause some strange and incorrect plot results for the set. This was fixed. 4. Fixed minor problem with pipes with intermediate elevations. If the user uses a "reverse pipe direction" on a pipe with intermediate elevations, and then immediately runs the model without re-opening the pipe window or saving the model and re-opening from disk, then the maximum and minimum pressure output could be incorrect. 5. Fixed a problem when you have a pump in your model with variable speed control to control on suction or discharge pressure (or head) and the control point is conditional in that the pump only controls when the control point is exceeded. The results are correct when you run the model, but if you save the model and re-open it the speed is displayed as 100% and the pressure and head rise are displayed as if the pump was running at 100%. This was fixed. 6. In the Output window junction table the inlet and outlet static and stagnation pressures displayed confused some users in certain cases. Specifically, when junctions had multiple pipes connected the definition of inlet and outlet, as well as the difference between static and stagnation pressure was ambiguous. No calculation logic was changed, but the display logic was changed to make the displayed values less confusing. This was done for exit Orifices and exit Valves. >> Changes that do not impact results << 1. Fixed problem where the Junction Deltas would not be retained when a scenario was promoted. 2. Fixed problem loading Check Valves from Impulse 4.0 models. 3. Fixed problem with the pop-up inspection window on the Workspace where it would lock up or crash depending on what mouse action was done while it was open. 4. Fixed bug in Valve, Control Valve and Three-Way Valve Specifications windows where the Open Percentage table looked for a maximum open percentage of 100% and treated decimal values like 100.0% as not equal to 100% and gave a warning. This no longer happens. 5. Pipe intermediate elevation data was not saving the elevation units. 6. Global editing of junction size could cause a run-time error and program crash because Fathom was not handling the larger 200% and 150% icon sizes in global editing. This was fixed. 7. Added vapor pressure as a usable parameter for Bingham Plastic and Power Law fluids. *** Changes for Version Date 2009.08.03 *** >> Changes to computation logic that could impact results << 1. A change made in the previous maintenance release caused the pump head at initial iteration to be counted twice. Once the simulation began it would reset to the correct value. This could cause convergence problems in select cases. This was fixed. 2. When a control valve is in a flow path that is closed off it cannot maintain its setpoint because there is no flow. The logic to handle this in some cases could cause premature determination of other control valve states and hence incorrect results. >> Changes to data management that could impact results << 1. When pipe scaling is used and the pipe is connected to a valve and the valve used open pct vs. Cv data, the open percentage and valve open area were calculated incorrectly. 2. After creating a pump vs. system curve which includes multiple pumps in parallel or in series, the pressure results were not being reset back to the original values. What this means is that when a model is run and this type of graph is created, subsequent graphs which use the pressure data will be incorrect. The user could also see incorrect results in the Output window if they returned to the Output window and opened Output Control and redisplayed the output. Finally pressure results in Visual Report could be affected. Once the model was rerun the problem would go away. This was fixed. 3. When using Global Junction Edit to changing from a controlled to a fixed flow pump the control setting was not cleared which left the pump in the controlled state. This was fixed. 4. There was a data corruption problem when older models were opened when the transient data in child scenarios was set to 0 even if the XTS module was not active. This has been fixed. 5. Fixed problem displaying pump operation the Cost Report with multi-scenarios. 6. Changes in the way pressures were reported for junctions in the 12/03/08 release affected the display of the max/min pressure results in the general section. The output was modified to reflect the max/min pressures in the pipes, including pipes with intermediate pipe elevations. >> Changes that do not impact results << 1. When using variable fluid properties and Chempak, some of the Chempak fluid names have commas. When using such a fluid for a specific pipe, the pipe data would become corrupted. This was fixed. 2. Fixed problem with junctions when using Renumber Increment. It could cause Fathom to crash. 3. When using GSC it was possible, probably through morphing, to confuse the GSC Manager about what type of junction was in the variable or goal. This would cause an error when the GSC model was run. A new check was added to tell the user what happened and what to do about it. 4. Added microns as an available unit of length. 5. Fixed a couple small issues related to orthogonal drawing. 6. Improved the Pump vs. System Curve logic for multiple dissimilar pumps in parallel using the Enhanced method to spread the flow differently at lower flow rates. 7. Fixed a problem with importing pump data from Intelliquip-enabled websites. If data for NPSH or efficiency was not present or not read correctly an error would occur and no data could be used in Fathom. Now Fathom can still use the head curve data. 8. Fixed some problems running batch jobs when an error occurs in one of the models or scenarios. The batch run could get hung up. 9. Adding a warning when using XTS and specifying a variable geometry tank which has possible incorrect data. 10. Fixed a typo on the header for creating pump curve vs. system curve. 11. Restricted the Cost Report to only have one instance of a particular output parameter. Since the entire report uses the same unit type, there is no need to have more than one instance of a parameter. 12. Modified the Isentropic Exponent calculation for ASME Steam calculations to use gamma=w^2/p*v instead of Cp/Cv. Cp/Cv is only an approximation, and the equation, which is derived from the the ASME formulation for sonic velocity, provides accurate calculations over the full range of steam table values. Isentropic Exponent is not currently used in Fathom calcs, but the ASME routines were modified to keep them in snyc with other applications. 13. Fixed an issue where carriage returns were not handled properly when adding notes to existing notes using Global Edit. *** Changes for Version Date 2009.08.19 *** >> Changes to computation logic that could impact results << 1. None. >> Changes to data management that could impact results << 1. Fixed problem when a solid was entered to the Solids Database without specific heat or thermal conductivity defined, a wrong set of units error was given when the slurry was being defined in System Properties. >> Changes that do not impact results << 1. Fixed problem accessing CrypKey copy protection as a model was run. 2. Added the SSL User Guide to the Help menu for easy access. *** Changes for Version Date 2009.10.07 *** >> Changes to computation logic that could impact results << 1. A change in the SSL module code was made to correct a slight inconsistency in use of specific gravity. There were two definitions before which caused a slight difference in results in some cases. 2. For control valves modeled as PSVs with a fully open loss value when wide open, if the valve cannot control its setpoint because of insufficient upstream pressure the valve was supposed to fail open but in fact failed closed. This was fixed. 3. The relief valve variable Cv model was changed. Previously the dP and Cv data was converted to dP vs flowrate data and dP was interpolated on this basis. However, the resulting dP value is different than if obtained by interpolating based on dP and Cv because the curve relating dP, Q and Cv is non-linear. Neither is necessarily more correct than the other and all inconsistencies between the two could be resolved by using more data points in the Cv vs dP input. It was decided that since the data is entered in dP and Cv that should be the basis of interpolation and so the solver was changed. Results should not change dramatically but it is likely there will be some differences if the relief valve opens. 4. In pipe sequences which have no flow and junctions with elevation differences at the junction the pressure was not being calculated properly in some cases. This was fixed. 5. Fixed a problem with PSVs not getting the fully open loss from the Cv/Open Percentage table correctly to evaluate if the valve should fail. 6. Fixed a problem using variable fluid properties when the fluid was changed in System Properties but the pipes were not updated. Now, if the fluid is changed the pipes retain the original fluid and values. >> Changes to data management that could impact results << 1. For relief valves that use the variable Cv method the calculation for pressure loss used a definition of water specific gravity slightly off with the rest of AFT Fathom which could cause some slight inconsistency of results. This routine used density at S.G. = 1 of 62.4 while the rest of AFT Fathom used 62.375. This was all made consistent. 2. Pump vs. system curve creation for multiple dissimilar pumps was not working properly. A code change that fixed a problem in the 2009.08.03 release created another problem that affected the system curve generation. The system curve would come out as a flat line. This was fixed. 3. When using Global Edit and changing curve-fit data, the data was changed even if the edit was canceled. 4. Fixed a problem when changing to an Unspecified fluid in the SSL module if there had previously been solids. This solid data is not cleared to avoid errors. 5. Pipes with no slurry data are not show in the Slurry output tab for the SSL module. >> Changes that do not impact results << 1. Added a clarifying note to the Pipe Specifications window Fluid Properties tab which displays when variable fluid properties is used. The note explains the possible need for a Volume Balance junction and provides a link to the Help system. 2. Fixed a problem creating pump vs system curves for multiple parallel pumps with identical pumps are used. An error when creating the graph occurred which is now fixed. 3. Added Vs to the SSL output parameters and clarified Vsm. 4. Fixed problem when using Basic Slurry in the SSL module some of the output names were inconsistent between steady-state and transient. 5. Added an Initial Velocity Guess Ration to the Solution Control for the SSL module. This will set the initial guess of the pipe flow to the product of this and the settling velocity to make sure it is in the correct flow regime. 6. Added a bed concentration to the System Properties for the SSL module. *** Changes for Version Date 2009.11.02 *** >> Changes to computation logic that could impact results << 1. None. >> Changes to data management that could impact results << 1. On pipe and junction specifications windows the user can push the F5 function key to jump to the next pipe or junction. If the user happens to have entered a value into a grid on these windows and then pushed the F5 key in some cases the new value was not kept. This was fixed. 2. A change introduced into the 2009.10.07 had an unexpected effect. After running a model and then either exiting the model and reloading it or changing scenarios and reloading the scenario, the pump head displayed in the Pump Summary can change and be incorrect. For water with standard density close to 62.3 lbm/ft3 or 1000 kg/m3 the effect is small. For fluids with different density the change can more significant. 3. Fixed a problem with Valve and Spray junctions when using XTS where the transient value would be erased when the tab in the specifications window was changed. >> Changes that do not impact results << 1. When using the SSL module and creating a slurry system curve in Graph Results, if the water curve is being cross-plotted it can disrupt the default range of the x-axis. This was fixed so the default range is always the same. 2. Fixed a problem when annotations are selected on the Workspace and then deleted using the Annotation Manager Fathom would crash. *** Changes for Version Date 2010.02.02 *** >> Changes to computation logic that could impact results << 1. This change affects Fathom models that use heat transfer with heat input at pumps. There are three options. The second option is to use percent of inefficiency. This calculation was not correct. The calculation should have been based on total pump power but was in fact using ideal pump power. This was fixed. 2. Fixed a problem with pumps when the internal check valve closed. The flow was set to a very small number and the pressure in the downstream pipe was set to the dead head pressure. This should have been zero flow and the pressure based on the hydrostatic pressure. 3. Fixed a problem with the SSL model when the pipe length was shorter than the elevation change. 4. Fixed a problem reading a Bend type Fitting & Loss with a r/D = 1.5 when the decimal separator is a comma. This caused the actual loss for this type to be too large. 5. There was a bug found in a very specific configuration. When a model has a loop with only one outlet that loop can only be pressurized through its outlet path. While Fathom has logic to handle this configuration a hole was found that depended on some arbitrary issues such as the order in how the pipes and junctions were built in the model. The end result was a correct result for everything except the pressures in this piping. All piping could be off by a set amount. This was fixed. >> Changes to data management that could impact results << 1. Fixed problem importing models from Impulse where the pump was shut off. >> Changes that do not impact results << 1. Made a change to pump vs. system curve graphing. For pumps with flat head curves it was possible to cause an error while graphing. Added a more descriptive error message and some logic to first try to work around the flat part of the curve. *** Changes for Version Date 2010.02.11 *** >> Changes to computation logic that could impact results << 1. None. >> Changes to data management that could impact results << 1. None. >> Changes that do not impact results << 1. Certain windows that created small graphs such as the Edit Fluid Database window had a print feature that did not work reliably. This was fixed. 2. When creating curve fits the raw data is cross-plotted vs. the curve fit. For some curve fit functions the raw data was not plotting properly. The curve fits were correct. This was only a display issue. *** Changes for Version Date 2010.03.01 *** >> Changes to computation logic that could impact results << 1. Fixed a problem introduced in the 2010.02.02 release that potentially could corrupt pipes in a scenario if Variable Fluid properties were used in conjunction with a non-Newtonian viscosity model. >> Changes to data management that could impact results << 1. Fixed problem importing pipe size changes from Excel where the pipe ID being used was not changed until the pipe specifications window was opened and OK was clicked. >> Changes that do not impact results << 1. Added warning about pump efficiency being greater than 100% due to user's pump power data issues. 2. Added an error message when the .out file cannot be opened because the model is run from a folder where the user does not have write permissions. *** Changes for Version Date 2010.06.29 *** >> Changes to computation logic that could impact results << 1. NSL (Non-settling Slurry Module) released. 2. In systems with exit valves in lines with closed junctions or pipes the stagnant pressure from the exit valve was not being applied properly to the stagnant pipes and junctions. So the pressure results and only pressure results were incorrect only for the stagnant pipes and junctions. And only when there was an open exit valve at the end of the stagnant line. This was fixed. 3. Put in a check for defined reference pressures when a valve or pump changes state and the model is rerun. This check is the same as the check when the model run is started. 4. Changed the logic to allow pressures to cross a failed-open control valve when it is in a pipe flow path that is closed by another junction. 5. Changed the logic to fail FCVs when the flow path that is closed by another junction. 6. When using the XTS module a closed finite reservoir junction has an option for a maximum gas pressure which simulates a relief valve path. This all worked fine. This maximum gas pressure (relief pressure) can be changed with time by the user. The transient on relief pressure was not working. The maximum gas pressure was just staying constant over time. This was fixed. It should be noted that the applications for this are limited. Typically relief pressures will be constant with time. >> Changes to data management that could impact results << 1. When using the XTS module and graphing results for EGL/HGL/Profile plots, if the cross-plot feature was used and more than one pipe sequence was plotted, and a max/min plot was created, some of the curves could be misidentified. The max and min labels were reversed in some cases. 2. Fixed a problem importing Relief Valves from Impulse with Cv cs dP loss data. >> Changes that do not impact results << 1. Fixed a Workspace and Visual Report minor printing problem. If the user directly changed the pipe line pixel thickness on the Pipe Specifications window, it displayed properly on the Workspace and Visual Report but did not print properly. This was fixed. 2. When creating a graph in the Graph Results using the Selected Solutions tab, if the filter was set to All Available Parameters the list did not display properly and the graph would not graph properly. This was fixed. *** Changes for Version Date 2010.07.23 *** >> Changes to computation logic that could impact results << 1. None. >> Changes to data management that could impact results << 1. None. >> Changes that do not impact results << 1. When using Chempak or ASME Steam/Water data and using variable fluid properties, global editing of pipe data and copying data from pipe to pipe did not copy the pressure - only the temperature and other fluid properties. This was fixed. 2. Changed the limit on parallel and series pumps to allow up to 40. *** Changes for Version Date 2011.02.02 *** >> Changes to computation logic that could impact results << 1. A change made in the 2010.06.29 release to fix another problem created a new problem for Relief valves modeled as inline exit valves. The discharge flow and pressure was not being calculated properly. This was fixed. 2. Fixed problem updating the fluid when the database fluid was changed and then the scenario was updated when variable fluid propertied were used. The updated fluid properties associated with the pipes were not being updated correctly. 3. Fixed a problem where the "raw data" was not copied when a copy-paste was performed. This normally does not impact results except when the data is used as an X-Y interpolated fit for pump curves and resistance curves. 4. Fixed a problem calculating pressures in a zero-flow loop (isolated loop) that has the reference flow directions in pipes in opposite directions while also having a hydrostatic pressure difference (elevation change) across a junction in that loop. 5. Fixed a problem calculating the fluid exit temperature when internal insulation is being applied. This calculation was not taking into account the insulation thickness when it used the wetted area. 6. The FCV K factor and Cv calculation did not apply the elevation change across the valve correctly. This was fixed. 7. The pressure drop across a FCV had the hydrostatic pressure across the valve calculated incorrectly. This also affected the inlet conditions of the downstream pipe as well as the valve failure calculations. This was fixed. 8. The valve failure check for a PSV incorrectly included the hydrostatic pressure across the valve twice. This was fixed. >> Changes to data management that could impact results << 1. Fixed a problem where the general heat transfer options were not available in a pipe when SteamCalc with Heat Transfer was selected as the first fluid. 2. Fixed a problem using Copy-Paste where the pipes and junctions were not correctly connected. This could lead to problems when copying from one file and pasting into another. The connections would be corrected before the model was run. 3. Fixed a problem where flow imbalance warnings were generated when a model/scenario was reopened When the relaxation and the relative flow tolerance were automatically lowered. This was cause by checking the solution against the user-specified values and not the lowered values which were used during the run. 4. Fixed a problem with the CST Cost Database editor where the scale table data was being corrupted when another cost database file was opened while showing the scale table. 5. Fixed problem when a scenario that had controlled suction or discharge pumps was reloaded when these pumps were not actively controlling. The pumps were set to their control pressure and the results were incorrect. The pump controlling state is now archived in the model results and not recalculated. 6. Fixed a problem when using the SSL module that the viscosity override would not be kept in a child scenario when the scenario was reopened. 7. When using the XTS module and graphing the transient pressure drop, the pressure units were not being converted properly. This was fixed. >> Changes that do not impact results << 1. If a valve was copied from another valve using the SameAs feature and it was the same handbook valve type, the K factor would be erased. This caused the junction to become undefined and the handbook valve type would have to be reselected. 2. When performing junction curve fits one must click the "Generate Curve Fit Now" button. If one clicked the image on the button and not the button itself, the curve fit was not performed. But it should have been. This was fixed. 3. When working with pre-existing pump junctions with multiple impeller configurations, if the engineering units used in the original impeller specification have since been removed from being active units (in the Unit Preferences window) then future editing of the pump configuration will result in a loss of the engineering units and loss of original data. This was fixed. 4. Fixed some display issues when working with pump junctions with multiple impeller configurations and using impeller trim functions. 5. When performing curve fits on pump data users can set a maximum x-axis value for flow. However, on subsequent curve fits for this pump the value is ignored. This was fixed. 6. In the XTS module if the available engineering units were changed then previously entered finite tank cross-sectional area could be lost. This was fixed. 7. Clarified error message if the user somehow had a solution tolerance of zero. 8. The Renumber Wizard allowed you to change the pipe or junction numbers but it did not erase old output. So it could display output for pipes or junction numbers that no longer exists. This would be resolved the next time the scenario was loaded or the model was opened. At the moment of renumbering it could cause confusion. 9. Fixed problem when jumping from one pipe spec window to another when using general convection heat transfer, an extra layer of insulation would be added and the pipe would be undefined. Jumping again would remove this extra layer. 10. Fixed a problem if the Model Data information was included in the output .dat file when a batch run was done. All the scenarios were using the same file name so only the last scenario run was being saved. 11. Linked the .dat and .out file names for the scenarios. 12. Fixed a problem where a comma was missing when the output preferences were saved to a file. 13. Fixed a problem when the ESC key is pressed during a multi-pipe draw. This could lead to zero-length pipes on the Workspace. 14. Fixed a problem when global editing the common junction size. The size selected would not be displayed correctly in the verification table to be applied. *** Changes for Version Date 2011.03.22 *** >> Changes to computation logic that could impact results << 1. SSL Module: Changed the way the hydrostatic head was accounted for in sloped pipes. Also made the horizontal, sloped and vertical pipe equations seamless. The hydrostatic head is no longer included in the Im and Jm terms. This will affect any pipe that is not horizontal. >> Changes to data management that could impact results << 1. None. >> Changes that do not impact results << 1. When running Bingham Plastic non-Newtonian models the Output window could show extraneous input data for Brecht & Heller Pulp and Paper stock. The data had no affect on the model. 2. Changed help file format to .chm for Windows 7 compatibility. *** Changes for Version Date 2011.07.06 *** >> Changes to computation logic that could impact results << 1. SSL Module: Added logic to model the demi-McDonald curve for Vsm. This option is now the default (set on the Slurry tab in the System Properties windows with the value limited by the equation. This may result in lower Vsm values than previously calculated. 2. Fixed a problem with dP vs. Reynolds number resistance curves where the Reynolds number was not being calculated correctly which resulted in incorrect dP results. 3. Made a change to how the average internal heat transfer coefficient is calculated. It was based on properties calculated at the average inlet and outlet pipe temperatures, now the properties are based on the log mean average temperatures. This only changed the value that is displayed in the output and not the heat transfer calculations or other results. The average properties shown in the output are still based on the log mean average temperature. 4. Fixed problem with crossflow heat exchangers when mixed flow side (primary or secondary was the Cmin (i.e. mdot * cp) value. The effectiveness and heat rate were not calculated correctly resulting in incorrect outlet temperatures. 5. The relief valve Variable Cv model was not working properly in some cases and would just use a lossless valve. This was fixed. 6. The XTS module had an issue with transients on Spray Discharge and Assigned Pressure junctions which were dual event. The second event sometimes did not begin at the right time step. This was fixed. >> Changes to data management that could impact results << 1. When a scenario other than the current scenario and then the Scenario Manager is closed without loading the current scenario the number of pipe and junction objects from the parent was being reset to what ever the parent of the saved scenario was. This caused the data flow from the parent of the current scenario to be corrupted and some objects that were deleted in the current scenario but that exist in its parent were being shown. This was fixed. 2. When a scenario was promoted it would acquire the XTS/GSC Use of the new parent. This would cause problems graphing if the new parent was used a different state. This was fixed so that the original Analysis Type was retained. 3. When a orifice has pipes that used the ID scaling feature the K factor is calculated based on the reduced pipe diameters. However, when a disconnected scenario was created and then saved to a separate file without first loading it, the K factor was based on the true pipe diameters. This is only an issue when the file is then brought into AFT Impulse because the K factor would not be correctly recalculated by Impulse as it is done in Fathom when the scenario is loaded. 4. When a Impulse model was opened in Fathom the Open Percentage data for a valve was lost. The data is now retained. 5. When junction elevation was used as a GSC variable the connected pipe elevation values displayed in the output were not updated to the new elevation. This only was a display issue with the pipe elevation, the calculations were correct. 6. Updated the fathom7.dat file with minor corrections to PVC, Ductile Iron and Copper Pipe. See notes in the file for specific details. >> Changes that do not impact results << 1. XTS module: Fixed problem when the XTS module was activated from the Options menu, the transient graph parameters were not being shown. Either opening the Output Control and clicking OK or reopening the model would solve this problem. 2. Fixed problem with the display in Model Data for the Jet Pump junction where the headers were mismatched and the data grid was truncated. 3. Change the Model Data to show the insulation layer when heat transfer is used and the pipe heat transfer model is something other than Convective Heat Transfer. *** Changes for Version Date 2012.01.06 *** >> Changes to computation logic that could impact results << 1. The temperature profile along a path which has pipes with intermediate elevations showed temperatures of absolute zero for the intermediate points when plotted. This is because the heat transfer calculations are done as an average along the pipe. The plotting has been fixed to show a linear interpolation between the inlet and outlet temperature values which will match a pipe which does not have intermediate elevation points. If a more detailed temperature profile is needed, the pipe should be broken into several different pipes joined by branch junctions as desired. >> Changes to data management that could impact results << 1. Fixed problem with importing some junctions types specific to Impulse that had special conditions set to ignore. These would come in as closed, but now the special conditions are set to none. 2. Fixed problem when global editing pumps that are from a database. The current configuration was being reset to the first one. It is now the configuration that is selected in the global edit list. 3. A change was made to the Relief Valve specification window. In a somewhat obscure instance, if a user has entered a curve fit for a Resistance Curve loss model, and they change the loss model from Resistance curve to a Variable Cv, and back, the curve fit type would be changed to Interpolation. This has been fixed. >> Changes that do not impact results << 1. If ESC was pressed when a pipe was drawn between two junctions while in multi-pipe drawing mode, the pipe would be deleted. This was fixed so only the multi-pipe mode was exited. 2. Added a caution when the current scenario is not displayed with the Multi-Scenario output. 3. For systems with a single pump, efficiency was not being plotted on the Pump vs. System curve when the option to do so was selected. This has been fixed. 4. Moved metric ton units (m-ton) from the English to SI system of units.