/** Compares the given pressure p to the saturation pressure at * temperature T and throws and exception if p is lower than * the saturation conditions. * The default value for psat is -1 yielding true if psat * is not redefined in the subclass. * */ bool IncompressibleFluid::checkP(double T, double p, double x) { double ps = 0.0; if (p_sat.type!=IncompressibleData::INCOMPRESSIBLE_NOT_SET) ps = psat(T, x); if (p < 0.0) throw ValueError(format("You cannot use negative pressures: %f < %f. ", p, 0.0)); if (ps> 0.0 && p < ps) throw ValueError(format("Equations are valid for liquid phase only: %f < %f (psat). ", p, ps)); return true; }
/** Compares the given pressure p to the saturation pressure at * temperature T and throws and exception if p is lower than * the saturation conditions. * The default value for psat is -1 yielding true if psat * is not redefined in the subclass. * */ bool IncompressibleSolution::checkP(double T_K, double p, double x) { double ps = psat(T_K,x); if (p<ps) { throw ValueError(format("Equations are valid for solution phase only: %f < %f. ",p,ps)); } else { return true; } }
int _tmain(int argc, _TCHAR* argv[]) { // init. setlocale(LC_ALL, ""); // 使用客户环境的缺省locale. // title. _tprintf(_T("zlatlcv v1.0 (%dbit)\n"), (int)(8*sizeof(int*))); _tprintf(_T("sizeof(wchar_t): %d\n"), (int)(sizeof(wchar_t))); _tprintf(_T("sizeof(TCHAR): %d\n"), (int)(sizeof(TCHAR))); _tprintf(_T("\n")); // printf. fflush(stdout); printf("printf A:\t%s\n", psa); printf("printf W:\t%ls\n", psw); printf("\n"); // UTF-8 to string (UTF-8 转 各种字符串). //CA2AZ psaa(psa, CP_UTF8, 0); CU82A psaa(psa); CU82W psaw(psa); printf("printf A from UTF-8:\t%s\n", psaa); printf("printf W from UTF-8:\t%ls\n", psaw); printf("\n"); // string to UTF-8 (各种字符串 转 UTF-8). CA2U8 psau8(psaa); CW2U8 pswu8(psaw); fflush(stdout); printf("printf UTF-8 from A:\t%s\n", psau8); printf("printf UTF-8 from W:\t%s\n", pswu8); // _tprintf. CA2CT psat(psa); CW2CT pswt(psw); CU82T psu8t(psa); fflush(stdout); _tprintf(_T("_tprintf A:\t%s\n"), psat); _tprintf(_T("_tprintf W:\t%s\n"), pswt); _tprintf(_T("_tprintf U8:\t%s\n"), psu8t); return 0; }
void parcel::setRelaxationTimes ( label celli, scalar& tauMomentum, scalarField& tauEvaporation, scalar& tauHeatTransfer, scalarField& tauBoiling, const spray& sDB, const scalar rho, const vector& Up, const scalar temperature, const scalar pressure, const scalarField& Yfg, const scalarField& m0, const scalar dt ) { const liquidMixture& fuels = sDB.fuels(); scalar mCell = rho*sDB.mesh().V()[cell()]; scalarField mfg(Yfg*mCell); label Ns = sDB.composition().Y().size(); label Nf = fuels.components().size(); // Tf is based on the 1/3 rule scalar Tf = T() + (temperature - T())/3.0; // calculate mixture properties scalar W = 0.0; scalar kMixture = 0.0; scalar cpMixture = 0.0; scalar muf = 0.0; for(label i=0; i<Ns; i++) { scalar Y = sDB.composition().Y()[i][celli]; W += Y/sDB.gasProperties()[i].W(); // Using mass-fractions to average... kMixture += Y*sDB.gasProperties()[i].kappa(Tf); cpMixture += Y*sDB.gasProperties()[i].Cp(Tf); muf += Y*sDB.gasProperties()[i].mu(Tf); } W = 1.0/W; scalarField Xf(Nf, 0.0); scalarField Yf(Nf, 0.0); scalarField psat(Nf, 0.0); scalarField msat(Nf, 0.0); for(label i=0; i<Nf; i++) { label j = sDB.liquidToGasIndex()[i]; scalar Y = sDB.composition().Y()[j][celli]; scalar Wi = sDB.gasProperties()[j].W(); Yf[i] = Y; Xf[i] = Y*W/Wi; psat[i] = fuels.properties()[i].pv(pressure, temperature); msat[i] = min(1.0, psat[i]/pressure)*Wi/W; } scalar nuf = muf/rho; scalar liquidDensity = fuels.rho(pressure, T(), X()); scalar liquidcL = fuels.cp(pressure, T(), X()); scalar heatOfVapour = fuels.hl(pressure, T(), X()); // calculate the partial rho of the fuel vapour // alternative is to use the mass fraction // however, if rhoFuelVap is small (zero) // d(mass)/dt = 0 => no evaporation... hmmm... is that good? NO! // Assume equilibrium at drop-surface => pressure @ surface // = vapour pressure to calculate fuel-vapour density @ surface scalar pressureAtSurface = fuels.pv(pressure, T(), X()); scalar rhoFuelVap = pressureAtSurface*fuels.W(X())/(specie::RR*Tf); scalarField Xs(sDB.fuels().Xs(pressure, temperature, T(), Xf, X())); scalarField Ys(Nf, 0.0); scalar Wliq = 0.0; for(label i=0; i<Nf; i++) { label j = sDB.liquidToGasIndex()[i]; scalar Wi = sDB.gasProperties()[j].W(); Wliq += Xs[i]*Wi; } for(label i=0; i<Nf; i++) { label j = sDB.liquidToGasIndex()[i]; scalar Wi = sDB.gasProperties()[j].W(); Ys[i] = Xs[i]*Wi/Wliq; } scalar Reynolds = Re(Up, nuf); scalar Prandtl = Pr(cpMixture, muf, kMixture); // calculate the characteritic times if(liquidCore_> 0.5) { // no drag for parcels in the liquid core.. tauMomentum = GREAT; } else { tauMomentum = sDB.drag().relaxationTime ( Urel(Up), d(), rho, liquidDensity, nuf, dev() ); } // store the relaxationTime since it is needed in some breakup models. tMom_ = tauMomentum; tauHeatTransfer = sDB.heatTransfer().relaxationTime ( liquidDensity, d(), liquidcL, kMixture, Reynolds, Prandtl ); // evaporation-properties are evaluated at averaged temperature // set the boiling conditions true if pressure @ surface is 99.9% // of the pressure // this is mainly to put a limit on the evaporation time, // since tauEvaporation is very very small close to the boiling point. for(label i=0; i<Nf; i++) { scalar Td = min(T(), 0.999*fuels.properties()[i].Tc()); bool boiling = fuels.properties()[i].pv(pressure, Td) >= 0.999*pressure; scalar Di = fuels.properties()[i].D(pressure, Td); scalar Schmidt = Sc(nuf, Di); scalar partialPressure = Xf[i]*pressure; // saturated vapour if(partialPressure > psat[i]) { tauEvaporation[i] = GREAT; } // not saturated vapour else { if (!boiling) { // for saturation evaporation, only use 99.99% for numerical robustness scalar dm = max(SMALL, 0.9999*msat[i] - mfg[i]); tauEvaporation[i] = sDB.evaporation().relaxationTime ( d(), fuels.properties()[i].rho(pressure, Td), rhoFuelVap, Di, Reynolds, Schmidt, Xs[i], Xf[i], m0[i], dm, dt ); } else { scalar Nusselt = sDB.heatTransfer().Nu(Reynolds, Prandtl); // calculating the boiling temperature of the liquid at ambient pressure scalar tBoilingSurface = Td; label Niter = 0; scalar deltaT = 10.0; scalar dp0 = fuels.properties()[i].pv(pressure, tBoilingSurface) - pressure; while ((Niter < 200) && (mag(deltaT) > 1.0e-3)) { Niter++; scalar pBoil = fuels.properties()[i].pv(pressure, tBoilingSurface); scalar dp = pBoil - pressure; if ( (dp > 0.0) && (dp0 > 0.0) ) { tBoilingSurface -= deltaT; } else { if ( (dp < 0.0) && (dp0 < 0.0) ) { tBoilingSurface += deltaT; } else { deltaT *= 0.5; if ( (dp > 0.0) && (dp0 < 0.0) ) { tBoilingSurface -= deltaT; } else { tBoilingSurface += deltaT; } } } dp0 = dp; } scalar vapourSurfaceEnthalpy = 0.0; scalar vapourFarEnthalpy = 0.0; for(label k = 0; k < sDB.gasProperties().size(); k++) { vapourSurfaceEnthalpy += sDB.composition().Y()[k][celli]*sDB.gasProperties()[k].H(tBoilingSurface); vapourFarEnthalpy += sDB.composition().Y()[k][celli]*sDB.gasProperties()[k].H(temperature); } scalar kLiquid = fuels.properties()[i].K(pressure, 0.5*(tBoilingSurface+T())); tauBoiling[i] = sDB.evaporation().boilingTime ( fuels.properties()[i].rho(pressure, Td), fuels.properties()[i].cp(pressure, Td), heatOfVapour, kMixture, Nusselt, temperature - T(), d(), liquidCore(), sDB.runTime().value() - ct(), Td, tBoilingSurface, vapourSurfaceEnthalpy, vapourFarEnthalpy, cpMixture, temperature, kLiquid ); } } } }