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June 8, 2011, 13:12 
Water subcooled boiling

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Attesz
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I have troubles with boiling simulation in CFX. The main problems are that the solver crashes when vapour generates and until crash (3040iterations) the vapour temperatures grows up to 300000 K. I have used the default empirical terms for the boiling phenomena. The water jacket inside pressure is 6 bar, inlet temperature 85 C, wall temperature 180 degrees. Material: IAPWS water and steam, where the saturation temperature is given in tables. Any suggestion about the used models, boundaries are welcome. Thank you in advance, Attila LIBRARY: CEL: EXPRESSIONS: Gravity = 9.81[m s^2] InletTemp = 86 [C] MaxAbsPress = OutPress+1 [atm] OutPress = 5 [bar] SaturationTemperature = Function Saturation(Absolute Pressure) SurfaceTensionCoefficient = 10^3*Function \ SurfaceTensionCoefficient(Water.T) TempBoresValveplate = 200 [C] TempHousingValveplate = 150 [C] WallHeatTemp = 220 [C] END FUNCTION: Function Saturation Argument Units = bar Option = Interpolation Result Units = C INTERPOLATION DATA: Data Pairs = \ 0.006112,0.01,0.012271,10.00,0.023368,20.00,0.0424 17,30.00,0.073749\ ,40.00,0.12334,50.00,0.19919,60.00,0.31161,70.00,0 .47359,80.00,0.70\ 108,90.00,1.0132,100.00,1.4326,110.00,1.9854,120.0 0,2.7012,130.00,3\ .6136,140.00,4.7597,150.00,6.1804,160.00,7.9202,17 0.00,10.003,180.0\ 0,12.552,190.00,15.551,200.00,19.08,210.00,23.201, 220.00,27.979,230\ .00,33.48,240.00,39.776,250.00,46.94,260.00,55.051 ,270.00,64.191,28\ 0.00,74.448,290.00,85.917,300.00,98.697,310.00,112 .9,320.00,128.65,\ 330.00,146.08,340.00,165.37,350.00,186.74,360.00,2 10.53,370.00,221.\ 2,374.15 Extend Max = No Extend Min = No Option = One Dimensional END END FUNCTION: Function SurfaceTensionCoefficient Argument Units = C Option = Interpolation Result Units = N m^1 INTERPOLATION DATA: Data Pairs = \ 0.01,75.6,10,74.24,20,72.78,30,71.23,40,69.61,50,6 7.93,60,66.19,70,\ 64.4,80,62.57,90,60.69,100,58.78,110,56.83,120,54. 85,130,52.83,140,\ 50.79,150,48.7,160,46.59,170,44.44,180,42.26,190,4 0.5,200,37.81,210\ ,35.53,220,33.23,230,30.9,240,28.56,250,26.19,260, 23.82,270,21.44,2\ 80,19.07,290,16.71,300,14.39,310,12.11,320,9.89,33 0,7.75,340,5.71,3\ 50,3.79,360,2.03,370,0.47,374.15,0,380,0 Extend Max = On Extend Min = No Option = One Dimensional END END END MATERIAL: Aluminium EN AC 46000 Material Group = CHT Solids Option = Pure Substance Thermodynamic State = Solid PROPERTIES: Option = General Material EQUATION OF STATE: Density = 2650 [kg m^3] Molar Mass = 26.98 [kg kmol^1] Option = Value END SPECIFIC HEAT CAPACITY: Option = Value Specific Heat Capacity = 910 [J kg^1 K^1] END REFERENCE STATE: Option = Specified Point Reference Specific Enthalpy = 0 [J/kg] Reference Specific Entropy = 0 [J/kg/K] Reference Temperature = 25 [C] END THERMAL CONDUCTIVITY: Option = Value Thermal Conductivity = 120 [W m^1 K^1] END END END MATERIAL: Cast Iron GG25 Material Group = CHT Solids Option = Pure Substance Thermodynamic State = Solid PROPERTIES: Option = General Material EQUATION OF STATE: Density = 7870 [kg m^3] Molar Mass = 55.85 [kg kmol^1] Option = Value END SPECIFIC HEAT CAPACITY: Option = Value Specific Heat Capacity = 460 [J kg^1 K^1] END REFERENCE STATE: Option = Specified Point Reference Specific Enthalpy = 0 [J/kg] Reference Specific Entropy = 0 [J/kg/K] Reference Temperature = 25 [C] END THERMAL CONDUCTIVITY: Option = Value Thermal Conductivity = 48.5 [W m^1 K^1] END END END MATERIAL: IAPWS STEAM Material Group = IAPWS IF97,Interphase Mass Transfer,Water Data Option = Pure Substance Thermodynamic State = Gas PROPERTIES: Option = IAPWS Library REFERENCE STATE: Option = Automatic END TABLE GENERATION: Maximum Absolute Pressure = MaxAbsPress*1.1 Maximum Points = 200 Maximum Temperature = WallHeatTemp*1.5 Minimum Absolute Pressure = 0.5 [atm] Minimum Temperature = InletTemp*0.9 Pressure Extrapolation = On Temperature Extrapolation = Yes END END END MATERIAL: IAPWS WATER Material Group = IAPWS IF97,Interphase Mass Transfer,Water Data Option = Pure Substance Thermodynamic State = Liquid PROPERTIES: Option = IAPWS Library REFERENCE STATE: Option = Automatic END TABLE GENERATION: Maximum Absolute Pressure = 2.5 [atm] Maximum Points = 200 Maximum Temperature = 550 [K] Minimum Absolute Pressure = 0.5 [atm] Minimum Temperature = 350 [K] Pressure Extrapolation = On Temperature Extrapolation = Yes END END END MATERIAL: Steel Material Group = CHT Solids Option = Pure Substance Thermodynamic State = Solid PROPERTIES: Option = General Material EQUATION OF STATE: Density = 7854 [kg m^3] Molar Mass = 55.85 [kg kmol^1] Option = Value END SPECIFIC HEAT CAPACITY: Option = Value Specific Heat Capacity = 4.34E+02 [J kg^1 K^1] END REFERENCE STATE: Option = Specified Point Reference Specific Enthalpy = 0 [J/kg] Reference Specific Entropy = 0 [J/kg/K] Reference Temperature = 25 [C] END THERMAL CONDUCTIVITY: Option = Value Thermal Conductivity = 60.5 [W m^1 K^1] END END END MATERIAL: Water Glycol Material Group = User Option = Pure Substance Thermodynamic State = Liquid PROPERTIES: Option = General Material EQUATION OF STATE: Density = 1045 [kg m^3] Molar Mass = 40.9 [kg kmol^1] Option = Value END SPECIFIC HEAT CAPACITY: Option = Value Specific Heat Capacity = 3490 [J kg^1 K^1] Specific Heat Type = Constant Pressure END DYNAMIC VISCOSITY: Dynamic Viscosity = 0.00105 [Pa s] Option = Value END THERMAL CONDUCTIVITY: Option = Value Thermal Conductivity = 0.39 [W m^1 K^1] END END END END FLOW: Flow Analysis 1 SOLUTION UNITS: Angle Units = [rad] Length Units = [m] Mass Units = [kg] Solid Angle Units = [sr] Temperature Units = [K] Time Units = [s] END ANALYSIS TYPE: Option = Steady State EXTERNAL SOLVER COUPLING: Option = None END END DOMAIN: FLUID_WATERJACKET Coord Frame = Coord 0 Domain Type = Fluid Location = TET_FLUID BOUNDARY: FLUID_ADIABATIC Boundary Type = WALL Location = INTER_WJ_SUPERCOOLING_GASKET_UPPER BOUNDARY CONDITIONS: HEAT TRANSFER: Option = Adiabatic END MASS AND MOMENTUM: Option = No Slip Wall END WALL CONTACT MODEL: Option = Specify Area Fraction END WALL ROUGHNESS: Option = Smooth Wall END END FLUID PAIR: Vapour  Water BOUNDARY CONDITIONS: WALL ADHESION: Option = None END WALL BOILING MODEL: Bubble Diameter Influence Factor = 2.0 Fixed Yplus for Liquid Subcooling = 250.0 Mass Source Under Relaxation = 0.1 Maximum Area Fraction of Bubble Influence = 0.5 Option = RPI Model BUBBLE DEPARTURE DIAMETER: Liquid Subcooling Scale = 45.0 [K] Maximum Departure Diameter = 1.4E3 [m] Option = Tolubinski Kostanchuk Reference Departure Diameter = 0.6E3 [m] END BUBBLE DETACHMENT FREQUENCY: Drag Coefficient = 1.0 Option = Terminal Velocity over Departure Diameter END BUBBLE WAITING TIME: Option = Proportional to Detachment Period Waiting Time Fraction = 0.8 END LIQUID QUENCHING HEAT TRANSFER COEFFICIENT: Option = Del Valle Kenning END WALL NUCLEATION SITE DENSITY: Option = Lemmert Chawla Power Law Index = 1.805 Reference Nucleation Site Density = 7.9384e5 [m^2] Reference Wall Superheat = 10.0 [K] END END END END FLUID: Vapour BOUNDARY CONDITIONS: WALL CONTACT AREA: Area Fraction = 0 Option = Area Fraction END END END FLUID: Water BOUNDARY CONDITIONS: WALL CONTACT AREA: Area Fraction = 1 Option = Area Fraction END END END END BOUNDARY: FLUID_WATERJACKET Default Boundary Type = WALL Location = Primitive 2D,Primitive 2D A,Primitive 2D B,Primitive 2D \ C,Primitive 2D D,Primitive 2D E,Primitive 2D F,Primitive 2D \ G,Primitive 2D H,Primitive 2D I,Primitive 2D J,Primitive 2D \ K,Primitive 2D L,Primitive 2D M BOUNDARY CONDITIONS: HEAT TRANSFER: Option = Adiabatic END MASS AND MOMENTUM: Option = Fluid Dependent END WALL CONTACT MODEL: Option = Specify Area Fraction END WALL ROUGHNESS: Option = Smooth Wall END END FLUID PAIR: Vapour  Water BOUNDARY CONDITIONS: WALL ADHESION: Option = None END WALL BOILING MODEL: Bubble Diameter Influence Factor = 2.0 Fixed Yplus for Liquid Subcooling = 250.0 Mass Source Under Relaxation = 0.1 Maximum Area Fraction of Bubble Influence = 0.5 Option = RPI Model BUBBLE DEPARTURE DIAMETER: Liquid Subcooling Scale = 45.0 [K] Maximum Departure Diameter = 1.4E3 [m] Option = Tolubinski Kostanchuk Reference Departure Diameter = 0.6E3 [m] END BUBBLE DETACHMENT FREQUENCY: Drag Coefficient = 1.0 Option = Terminal Velocity over Departure Diameter END BUBBLE WAITING TIME: Option = Proportional to Detachment Period Waiting Time Fraction = 0.8 END LIQUID QUENCHING HEAT TRANSFER COEFFICIENT: Option = Del Valle Kenning END WALL NUCLEATION SITE DENSITY: Option = Lemmert Chawla Power Law Index = 1.805 Reference Nucleation Site Density = 7.9384e5 [m^2] Reference Wall Superheat = 10.0 [K] END END END END FLUID: Vapour BOUNDARY CONDITIONS: MASS AND MOMENTUM: Option = No Slip Wall END WALL CONTACT AREA: Area Fraction = 0 Option = Area Fraction END END END FLUID: Water BOUNDARY CONDITIONS: MASS AND MOMENTUM: Option = No Slip Wall END WALL CONTACT AREA: Area Fraction = 1 Option = Area Fraction END END END END BOUNDARY: INLET Boundary Type = INLET Location = WATER_INLET BOUNDARY CONDITIONS: FLOW DIRECTION: Option = Normal to Boundary Condition END FLOW REGIME: Option = Subsonic END HEAT TRANSFER: Option = Static Temperature Static Temperature = InletTemp END MASS AND MOMENTUM: Mass Flow Rate = 0.24383 [kg s^1] Option = Bulk Mass Flow Rate END TURBULENCE: Eddy Length Scale = 0.03 [m] Fractional Intensity = 0.05 Option = Intensity and Length Scale END END FLUID: Vapour BOUNDARY CONDITIONS: VOLUME FRACTION: Option = Value Volume Fraction = 0 END END END FLUID: Water BOUNDARY CONDITIONS: VOLUME FRACTION: Option = Value Volume Fraction = 1 END END END END BOUNDARY: OUTLET Boundary Type = OUTLET Location = WATER_OUTLET BOUNDARY CONDITIONS: FLOW REGIME: Option = Subsonic END MASS AND MOMENTUM: Option = Average Static Pressure Pressure Profile Blend = 0.05 Relative Pressure = OutPress END PRESSURE AVERAGING: Option = Average Over Whole Outlet END END END BOUNDARY: PIPES Boundary Type = WALL Location = WATER_INLET_PIPE,WATER_OUTLET_PIPE BOUNDARY CONDITIONS: HEAT TRANSFER: Option = Adiabatic END MASS AND MOMENTUM: Option = No Slip Wall END WALL CONTACT MODEL: Option = Use Volume Fraction END WALL ROUGHNESS: Option = Smooth Wall END END FLUID PAIR: Vapour  Water BOUNDARY CONDITIONS: WALL ADHESION: Option = None END END END END BOUNDARY: WallHeated Boundary Type = WALL Location = INTER_WJ_VALVEPLATE BOUNDARY CONDITIONS: HEAT TRANSFER: Fixed Temperature = WallHeatTemp Option = Fixed Temperature END MASS AND MOMENTUM: Option = Fluid Dependent END WALL CONTACT MODEL: Option = Specify Area Fraction END WALL ROUGHNESS: Option = Smooth Wall END END FLUID PAIR: Vapour  Water BOUNDARY CONDITIONS: WALL ADHESION: Option = None END WALL BOILING MODEL: Bubble Diameter Influence Factor = 2.0 Fixed Yplus for Liquid Subcooling = 250.0 Mass Source Under Relaxation = 0.1 Maximum Area Fraction of Bubble Influence = 0.5 Option = RPI Model BUBBLE DEPARTURE DIAMETER: Liquid Subcooling Scale = 45.0 [K] Maximum Departure Diameter = 1.4E3 [m] Option = Tolubinski Kostanchuk Reference Departure Diameter = 0.6E3 [m] END BUBBLE DETACHMENT FREQUENCY: Drag Coefficient = 1.0 Option = Terminal Velocity over Departure Diameter END BUBBLE WAITING TIME: Option = Proportional to Detachment Period Waiting Time Fraction = 0.8 END LIQUID QUENCHING HEAT TRANSFER COEFFICIENT: Option = Del Valle Kenning END WALL NUCLEATION SITE DENSITY: Option = Lemmert Chawla Power Law Index = 1.805 Reference Nucleation Site Density = 7.9384e5 [m^2] Reference Wall Superheat = 10.0 [K] END END END END FLUID: Vapour BOUNDARY CONDITIONS: MASS AND MOMENTUM: Option = No Slip Wall END WALL CONTACT AREA: Area Fraction = 0 Option = Area Fraction END END END FLUID: Water BOUNDARY CONDITIONS: MASS AND MOMENTUM: Option = No Slip Wall END WALL CONTACT AREA: Area Fraction = 1 Option = Area Fraction END END END END DOMAIN MODELS: BUOYANCY MODEL: Buoyancy Reference Density = 0.5974 [kg m^3] Gravity X Component = 0 [m s^2] Gravity Y Component = 0 [m s^2] Gravity Z Component = Gravity Option = Buoyant BUOYANCY REFERENCE LOCATION: Option = Automatic END END DOMAIN MOTION: Option = Stationary END MESH DEFORMATION: Option = None END REFERENCE PRESSURE: Reference Pressure = 1 [atm] END END FLUID DEFINITION: Vapour Material = IAPWS STEAM Option = Material Library MORPHOLOGY: Mean Diameter = 0.6 [mm] Option = Dispersed Fluid END END FLUID DEFINITION: Water Material = IAPWS WATER Option = Material Library MORPHOLOGY: Option = Continuous Fluid END END FLUID MODELS: COMBUSTION MODEL: Option = None END FLUID: Vapour FLUID BUOYANCY MODEL: Option = Density Difference END HEAT TRANSFER MODEL: Option = Thermal Energy END TURBULENCE MODEL: Option = Dispersed Phase Zero Equation END END FLUID: Water FLUID BUOYANCY MODEL: Option = Density Difference END HEAT TRANSFER MODEL: Include Viscous Dissipation Term = On Option = Thermal Energy END TURBULENCE MODEL: Option = SST BUOYANCY TURBULENCE: Option = Production Turbulent Schmidt Number = 0.9 END END TURBULENT WALL FUNCTIONS: Option = Automatic END END HEAT TRANSFER MODEL: Homogeneous Model = False Option = Fluid Dependent END THERMAL RADIATION MODEL: Option = None END TURBULENCE MODEL: Homogeneous Model = False Option = Fluid Dependent END END FLUID PAIR: Vapour  Water Surface Tension Coefficient = SurfaceTensionCoefficient INTERPHASE HEAT TRANSFER: Option = Two Resistance FLUID1 INTERPHASE HEAT TRANSFER: Option = Zero Resistance END FLUID2 INTERPHASE HEAT TRANSFER: Option = Ranz Marshall END END INTERPHASE TRANSFER MODEL: Option = Particle Model END MASS TRANSFER: Option = Phase Change PHASE CHANGE MODEL: Option = Thermal Phase Change Saturation Temperature = SaturationTemperature WALL BOILING MODEL: Bubble Diameter Influence Factor = 2.0 Fixed Yplus for Liquid Subcooling = 250.0 Mass Source Under Relaxation = 0.1 Maximum Area Fraction of Bubble Influence = 0.5 Option = RPI Model BUBBLE DEPARTURE DIAMETER: Liquid Subcooling Scale = 45.0 [K] Maximum Departure Diameter = 1.4E3 [m] Option = Tolubinski Kostanchuk Reference Departure Diameter = 0.6E3 [m] END BUBBLE DETACHMENT FREQUENCY: Drag Coefficient = 1.0 Option = Terminal Velocity over Departure Diameter END BUBBLE WAITING TIME: Option = Proportional to Detachment Period Waiting Time Fraction = 0.8 END LIQUID QUENCHING HEAT TRANSFER COEFFICIENT: Option = Del Valle Kenning END WALL NUCLEATION SITE DENSITY: Option = Lemmert Chawla Power Law Index = 1.805 Reference Nucleation Site Density = 7.9384e5 [m^2] Reference Wall Superheat = 10.0 [K] END END END END MOMENTUM TRANSFER: DRAG FORCE: Option = Ishii Zuber END LIFT FORCE: Option = Tomiyama END TURBULENT DISPERSION FORCE: Option = Favre Averaged Drag Force Turbulent Dispersion Coefficient = 1.0 END VIRTUAL MASS FORCE: Option = Virtual Mass Coefficient Virtual Mass Coefficient = 0.5 END WALL LUBRICATION FORCE: Lubrication Coefficient C1 = 0.05 Lubrication Coefficient C2 = 0.01 Option = Antal END END SURFACE TENSION MODEL: Option = Continuum Surface Force Primary Fluid = Water Volume Fraction Smoothing Type = VolumeWeighted END TURBULENCE TRANSFER: ENHANCED TURBULENCE PRODUCTION MODEL: Option = Sato Enhanced Eddy Viscosity END END END INITIALISATION: Option = Automatic FLUID: Vapour INITIAL CONDITIONS: Velocity Type = Cartesian CARTESIAN VELOCITY COMPONENTS: Option = Automatic with Value U = 0 [m s^1] V = 0 [m s^1] W = 0 [m s^1] END TEMPERATURE: Option = Automatic with Value Temperature = InletTemp END VOLUME FRACTION: Option = Automatic with Value Volume Fraction = 0 END END END FLUID: Water INITIAL CONDITIONS: Velocity Type = Cartesian CARTESIAN VELOCITY COMPONENTS: Option = Automatic with Value U = 0 [m s^1] V = 0 [m s^1] W = 0 [m s^1] END TEMPERATURE: Option = Automatic with Value Temperature = InletTemp END TURBULENCE INITIAL CONDITIONS: Option = Low Intensity and Eddy Viscosity Ratio END VOLUME FRACTION: Option = Automatic with Value Volume Fraction = 1 END END END INITIAL CONDITIONS: STATIC PRESSURE: Option = Automatic with Value Relative Pressure = OutPress END END END MULTIPHASE MODELS: Homogeneous Model = False FREE SURFACE MODEL: Option = Standard END END END OUTPUT CONTROL: BACKUP RESULTS: Backup Results 1 File Compression Level = Default Option = Standard Output Equation Residuals = None OUTPUT FREQUENCY: Elapsed Time Interval = 2 [h] Option = Elapsed Time Interval END END
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June 8, 2011, 13:13 

#2 
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Attesz
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MONITOR OBJECTS:
MONITOR BALANCES: Option = Full END MONITOR FORCES: Option = Full END MONITOR PARTICLES: Option = Full END MONITOR POINT: BoilCheck1 Cartesian Coordinates = 0.0337414 [m], 0.01 [m], 0.004 [m] Domain Name = FLUID_WATERJACKET Option = Cartesian Coordinates Output Variables List = Vapour.Volume Fraction END MONITOR POINT: BoilCheck2 Cartesian Coordinates = 0.0917695 [m], 0.01 [m], 0.004 [m] Domain Name = FLUID_WATERJACKET Option = Cartesian Coordinates Output Variables List = Vapour.Volume Fraction END MONITOR POINT: BoilCheck3 Cartesian Coordinates = 0.143128 [m], 0.01 [m], 0.004 [m] Domain Name = FLUID_WATERJACKET Option = Cartesian Coordinates Output Variables List = Vapour.Volume Fraction END MONITOR POINT: BoilCheck4 Cartesian Coordinates = 0.180127 [m], 0.01 [m], 0.004 [m] Domain Name = FLUID_WATERJACKET Option = Cartesian Coordinates Output Variables List = Vapour.Volume Fraction END MONITOR POINT: InletTemp Cartesian Coordinates = 0.306848 [m], 0.0938528 [m], 0.0615971 [m] Domain Name = FLUID_WATERJACKET Option = Cartesian Coordinates Output Variables List = Water.Temperature END MONITOR POINT: OutletTemp Cartesian Coordinates = 0.203647 [m], 0.0409154 [m], 0.16532 [m] Domain Name = FLUID_WATERJACKET Option = Cartesian Coordinates Output Variables List = Water.Temperature END MONITOR RESIDUALS: Option = Full END MONITOR TOTALS: Option = Full END END RESULTS: File Compression Level = Default Option = Standard Output Equation Residuals = All END END SOLVER CONTROL: Turbulence Numerics = First Order ADVECTION SCHEME: Option = Upwind END CONVERGENCE CONTROL: Length Scale Option = Conservative Maximum Number of Iterations = 3000 Minimum Number of Iterations = 500 Timescale Control = Auto Timescale Timescale Factor = 1.0 END CONVERGENCE CRITERIA: Conservation Target = 0.01 Residual Target = 0.000001 Residual Type = RMS END DYNAMIC MODEL CONTROL: Global Dynamic Model Control = On END END EXPERT PARAMETERS: tbulk for htc = 354.5 wall clock time = t END END COMMAND FILE: Version = 13.0 Results Version = 13.0 END SIMULATION CONTROL: EXECUTION CONTROL: EXECUTABLE SELECTION: Double Precision = Off END INTERPOLATOR STEP CONTROL: Runtime Priority = Standard MEMORY CONTROL: Memory Allocation Factor = 2 END END PARALLEL HOST LIBRARY: HOST DEFINITION: bu2s0037 Host Architecture String = linuxamd64 Installation Root = /data/progs/ansys_inc_130/v%v/CFX END END PARTITIONER STEP CONTROL: Multidomain Option = Independent Partitioning Runtime Priority = Standard EXECUTABLE SELECTION: Use Large Problem Partitioner = Off END MEMORY CONTROL: Memory Allocation Factor = 1.0 END PARTITIONING TYPE: MeTiS Type = kway Option = MeTiS Partition Size Rule = Automatic END END RUN DEFINITION: Initial Partition File = \ Run Mode = Full Solver Input File = \ INITIAL VALUES SPECIFICATION: INITIAL VALUES CONTROL: Continue History From = Initial Values 1 Use Mesh From = Initial Values END INITIAL VALUES: Initial Values 1 File Name = \ Option = Results File END END END SOLVER STEP CONTROL: Runtime Priority = Standard MEMORY CONTROL: Memory Allocation Factor = 2 END PARALLEL ENVIRONMENT: Number of Processes = 8 Start Method = HP MPI Local Parallel END END END END
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June 8, 2011, 20:55 

#3 
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Glenn Horrocks
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Does it work when you use constant properties water? IAWPS properties are always harder to converge.


June 9, 2011, 05:45 

#4 
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Attesz
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Thanks, I haven't tested it yet, I will give it a try.
The interesting thing is when the vapour phase appears its temperature increases up to 300000K and then it crashez. If I switch to transient simulation and adaptive time step, the solver goes to very small step size (1e9 s) while the PVol residuals grows continously until crash. So the problem is with the phase change and vapour generation or maybe with the heat transfer modelling between the phases...
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June 9, 2011, 06:52 

#5 
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Glenn Horrocks
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Precisely. So to check whether the problem is in the material properties or you rmodel, run a simple constant properties model and see if it works.


June 9, 2011, 07:27 

#6 
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Attesz
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Ok, I start a new simulation with constant properties.
Otherwise I get: ++  An error has occurred in cfx5solve:     The ANSYS CFX solver exited with return code 127. No results   file has been created.  ++ What is the 127 code means in this case? Thank you!
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June 9, 2011, 08:11 

#7 
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Glenn Horrocks
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No, the error codes are not documented unfortunately. But you probably missed something necessary to define the simulation in the material properties.


January 5, 2013, 04:32 

#8 
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Abishek
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you have to force the vapor phase temperature to saturation temperature to be able to use the RPI wall boiling model. hence, the solver will not run the energy equation for vapor phase..


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