Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified Authorization required, but no authorization protocol specified /*---------------------------------------------------------------------------*\ ========= | \\ / F ield | OpenFOAM: The Open Source CFD Toolbox \\ / O peration | Website: https://openfoam.org \\ / A nd | Version: 13 \\/ M anipulation | \*---------------------------------------------------------------------------*/ Build : 13-65eda17ad4ca Exec : foamRun -parallel Date : Jul 15 2025 Time : 08:56:52 Host : "franco-work" PID : 11420 I/O : uncollated Case : /home/franco/Downloads/bubbleColumn2kV13 nProcs : 8 Slaves : 7 ( "franco-work.11421" "franco-work.11422" "franco-work.11423" "franco-work.11424" "franco-work.11425" "franco-work.11426" "franco-work.11427" ) Pstream initialised with: floatTransfer : false nProcsSimpleSum : 0 commsType : nonBlocking polling iterations : 0 sigFpe : Enabling floating point exception trapping (FOAM_SIGFPE). SetNaN : Initialising allocated memory to NaN (FOAM_SETNAN). fileModificationChecking : Monitoring run-time modified files using timeStampMaster (fileModificationSkew 10) allowSystemOperations : Allowing user-supplied system call operations // * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * * // Create time Create mesh for time = 0 Selecting solver multiphaseEuler No MRF models present Selecting phaseModel for gas: multicomponentIsothermalPhaseModel Selecting diameterModel for phase gas: velocityGroup Selecting thermodynamics package { type heRhoThermo; mixture multicomponentMixture; transport const; thermo eConst; equationOfState perfectGas; specie specie; energy sensibleInternalEnergy; } Calculating face flux field phi.gas Selecting turbulence model type laminar Selecting laminar stress model Stokes Selecting thermophysical transport type laminar Selecting default laminar thermophysical transport model unityLewisFourier Selecting phaseModel for liquid: multicomponentIsothermalPhaseModel Selecting diameterModel for phase liquid: constant Selecting thermodynamics package { type heRhoThermo; mixture multicomponentMixture; transport const; thermo eConst; equationOfState rPolynomial; specie specie; energy sensibleInternalEnergy; } Calculating face flux field phi.liquid Selecting turbulence model type laminar Selecting laminar stress model Stokes Selecting thermophysical transport type laminar Selecting default laminar thermophysical transport model unityLewisFourier Selecting surfaceTensionCoefficientModel for gas_liquid: constant Selecting dragModel blending method for gas_liquid: linear Selecting dragModel for gas_dispersedIn_liquid: TomiyamaCorrelatedOrlando Selecting dragModel for liquid_dispersedIn_gas: SchillerNaumann Selecting virtualMassModel blending method for gas_liquid: linear Selecting virtualMassModel for gas_dispersedIn_liquid: constantCoefficient Selecting virtualMassModel for liquid_dispersedIn_gas: constantCoefficient Selecting SidedInterfacialModel blending method for gas_liquid: linear Selecting heatTransferModel for gas_dispersedIn_liquid_inThe_gas: RanzMarshall Selecting heatTransferModel for gas_dispersedIn_liquid_inThe_liquid: RanzMarshall Selecting heatTransferModel for liquid_dispersedIn_gas_inThe_gas: RanzMarshall Selecting heatTransferModel for liquid_dispersedIn_gas_inThe_liquid: RanzMarshall Setting up population balance: bubbles Selecting coalescence model for bubbles: Luo Selecting binary breakup model for bubbles: powerLawUniformBinary Courant Number mean: 6.01596e-07 max: 0.00692706 Creating fvModels from "constant/fvModels" Selecting finite volume model type massDiffusionLimitedPhaseChange Name: phaseChange Selecting interfaceCompositionModel for gas_liquid_inThe_gas: saturated Selecting saturationPressureModel ArdenBuck Selecting interfaceCompositionModel for gas_liquid_inThe_liquid: Henry Selecting SidedInterfacialModel blending method for gas_liquid: linear Selecting diffusiveMassTransferModel for gas_dispersedIn_liquid_inThe_gas: spherical Selecting diffusiveMassTransferModel for gas_dispersedIn_liquid_inThe_liquid: Frossling Selecting diffusiveMassTransferModel for liquid_dispersedIn_gas_inThe_gas: Frossling Selecting diffusiveMassTransferModel for liquid_dispersedIn_gas_inThe_liquid: spherical Selecting finite volume model type porosityForce Name: filter1 Porosity region filter1: selecting model: DarcyForchheimer creating porous zone: filter Creating fvConstraints from "system/fvConstraints" Selecting finite volume constraint type limitPressure Name: limitp min 10000 PIMPLE: No convergence criteria found PIMPLE: No corrector convergence criteria found Calculations will do 3 corrections PIMPLE: Operating solver in transient mode with 3 outer correctors Using dynamicCode for coded updateO2liquid at line 21 in "/home/franco/Downloads/bubbleColumn2kV13/system/functions/updateO2liquid" Using dynamicCode for coded alphaSpecie at line 63 in "/home/franco/Downloads/bubbleColumn2kV13/system/functions/alphaSpecie" Starting time loop Courant Number mean: 6.01596e-07 max: 0.00692706 deltaT = 0.000239981 Time = 0.000239981s PIMPLE: Iteration 1 massDiffusionLimitedPhaseChange: phaseChange min/mean/max Ts = 303/303/303 min/mean/max mDot = 0/0/0 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147216 0 1 liquid fraction, min, max = 0.852784 0 1 Phase-sum volume fraction, min, max = 1 1 1 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147217 0 1 liquid fraction, min, max = 0.852783 0 1 Phase-sum volume fraction, min, max = 1 1 1 Constructing momentum equations DILUPBiCGStab: Solving for O2.gas, Initial residual = 1, Final residual = 1.16097e-14, No Iterations 1 DILUPBiCGStab: Solving for H2O.gas, Initial residual = 0, Final residual = 0, No Iterations 0 DILUPBiCGStab: Solving for O2.liquid, Initial residual = 0, Final residual = 0, No Iterations 0 DILUPBiCGStab: Solving for N2.liquid, Initial residual = 0, Final residual = 0, No Iterations 0 GAMG: Solving for p_rgh, Initial residual = 0.122152, Final residual = 7.91206e-09, No Iterations 35 GAMG: Solving for p_rgh, Initial residual = 5.63566e-06, Final residual = 8.13023e-09, No Iterations 8 PIMPLE: Iteration 2 massDiffusionLimitedPhaseChange: phaseChange min/mean/max Ts = 298.992/303/303 min/mean/max mDot = -3.63426/-0.000396911/0 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147216 0 1 liquid fraction, min, max = 0.852784 0 1 Phase-sum volume fraction, min, max = 1 1 1 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147217 -1.85872e-21 1 liquid fraction, min, max = 0.852783 0 1 Phase-sum volume fraction, min, max = 1 1 1 Constructing momentum equations DILUPBiCGStab: Solving for O2.gas, Initial residual = 0.0106276, Final residual = 7.48352e-13, No Iterations 1 DILUPBiCGStab: Solving for H2O.gas, Initial residual = 1, Final residual = 6.77365e-15, No Iterations 2 DILUPBiCGStab: Solving for O2.liquid, Initial residual = 1, Final residual = 3.86207e-13, No Iterations 2 DILUPBiCGStab: Solving for N2.liquid, Initial residual = 0, Final residual = 0, No Iterations 0 GAMG: Solving for p_rgh, Initial residual = 0.0194645, Final residual = 8.32797e-09, No Iterations 29 GAMG: Solving for p_rgh, Initial residual = 1.56321e-06, Final residual = 5.90464e-09, No Iterations 5 PIMPLE: Iteration 3 massDiffusionLimitedPhaseChange: phaseChange min/mean/max Ts = 288.402/302.952/303 min/mean/max mDot = -0.840112/-0.000108195/0 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147216 -2.41776e-21 1 liquid fraction, min, max = 0.852784 0 1 Phase-sum volume fraction, min, max = 1 1 1 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147216 -2.142e-17 1 liquid fraction, min, max = 0.852784 0 1 Phase-sum volume fraction, min, max = 1 1 1 populationBalance bubbles: Iteration 1 DILUPBiCGStab: Solving for f0.gas, Initial residual = 1, Final residual = 1.03867e-07, No Iterations 1 DILUPBiCGStab: Solving for f1.gas, Initial residual = 1, Final residual = 1.02729e-07, No Iterations 1 DILUPBiCGStab: Solving for f2.gas, Initial residual = 1, Final residual = 9.67382e-08, No Iterations 1 DILUPBiCGStab: Solving for f3.gas, Initial residual = 1, Final residual = 9.64042e-08, No Iterations 1 DILUPBiCGStab: Solving for f4.gas, Initial residual = 1, Final residual = 9.24984e-08, No Iterations 1 DILUPBiCGStab: Solving for f5.gas, Initial residual = 1, Final residual = 8.65749e-08, No Iterations 1 DILUPBiCGStab: Solving for f6.gas, Initial residual = 1, Final residual = 8.6644e-08, No Iterations 1 DILUPBiCGStab: Solving for f7.gas, Initial residual = 1, Final residual = 8.30426e-08, No Iterations 1 bubbles sizeGroup phase fraction first, last = 0.00202632 0.00195257 Scaling sizeGroups for velocityGroup gas gas sizeGroups-sum volume fraction, min, max = 1 1 1 gas Sauter mean diameter, min, max = 0.00397376 0.0038808 0.00411469 Constructing momentum equations DILUPBiCGStab: Solving for O2.gas, Initial residual = 0.00355364, Final residual = 3.69437e-14, No Iterations 2 DILUPBiCGStab: Solving for H2O.gas, Initial residual = 0.0030202, Final residual = 9.21234e-16, No Iterations 1 DILUPBiCGStab: Solving for O2.liquid, Initial residual = 0.037639, Final residual = 2.59602e-13, No Iterations 2 DILUPBiCGStab: Solving for N2.liquid, Initial residual = 0, Final residual = 0, No Iterations 0 GAMG: Solving for p_rgh, Initial residual = 0.011965, Final residual = 7.79725e-09, No Iterations 22 GAMG: Solving for p_rgh, Initial residual = 1.60755e-07, Final residual = 4.22874e-09, No Iterations 2 ExecutionTime = 36.0118 s ClockTime = 37 s Courant Number mean: 0.0308413 max: 2.10693 deltaT = 8.54204e-05 Time = 0.000325401s PIMPLE: Iteration 1 massDiffusionLimitedPhaseChange: phaseChange min/mean/max Ts = 287.006/302.903/303 min/mean/max mDot = -0.737385/-8.69935e-05/0 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147217 -2.3223e-22 1 liquid fraction, min, max = 0.852783 0 1 Phase-sum volume fraction, min, max = 1 1 1 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147217 -1.59173e-22 1 liquid fraction, min, max = 0.852783 0 1 Phase-sum volume fraction, min, max = 1 1 1 Constructing momentum equations DILUPBiCGStab: Solving for O2.gas, Initial residual = 0.000232988, Final residual = 1.42623e-14, No Iterations 1 DILUPBiCGStab: Solving for H2O.gas, Initial residual = 0.000141745, Final residual = 2.79718e-15, No Iterations 1 DILUPBiCGStab: Solving for O2.liquid, Initial residual = 0.0543119, Final residual = 8.55811e-14, No Iterations 2 DILUPBiCGStab: Solving for N2.liquid, Initial residual = 0, Final residual = 0, No Iterations 0 GAMG: Solving for p_rgh, Initial residual = 0.0206263, Final residual = 5.84343e-09, No Iterations 9 GAMG: Solving for p_rgh, Initial residual = 7.58675e-07, Final residual = 8.16415e-09, No Iterations 3 PIMPLE: Iteration 2 massDiffusionLimitedPhaseChange: phaseChange min/mean/max Ts = 287.613/302.88/303 min/mean/max mDot = -1.13394/-0.000132882/0 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147217 -2.341e-20 1 liquid fraction, min, max = 0.852783 0 1 Phase-sum volume fraction, min, max = 1 1 1 MULES: Solving for alpha.gas MULES: Solving for alpha.liquid MULES: Correcting alpha.gas MULES: Correcting alpha.liquid gas fraction, min, max = 0.147217 -1.09916e-21 1 liquid fraction, min, max = 0.852783 0 1 Phase-sum volume fraction, min, max = 1 1 1 Constructing momentum equations DILUPBiCGStab: Solving for O2.gas, Initial residual = 0.000123402, Final residual = 2.24357e-14, No Iterations 1 DILUPBiCGStab: Solving for H2O.gas, Initial residual = 0.000394485, Final residual = 5.24147e-15, No Iterations 1 DILUPBiCGStab: Solving for O2.liquid, Initial residual = 0.0196331, Final residual = 3.5455e-14, No Iterations 2 DILUPBiCGStab: Solving for N2.liquid, Initial residual = 0, Final residual = 0, No Iterations 0