/** 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
);
}
}
}
}
