public static double Shah_Evap_href(string fluid, double d, double g, double p, double x, double q, double l, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double temperature;
double DensityL, DensityV, EnthalpyL, EnthalpyV, ViscosityL, KL, CpL;
coolprop.update(input_pairs.PQ_INPUTS, p * 1000, 0);
temperature = coolprop.T();
coolprop.update(input_pairs.QT_INPUTS, 0, temperature);
DensityL = coolprop.rhomass();
EnthalpyL = coolprop.hmass() / 1000;
ViscosityL = coolprop.viscosity();
CpL = coolprop.cpmass() / 1000;
KL = coolprop.conductivity();
coolprop.update(input_pairs.QT_INPUTS, 1, temperature);
DensityV = coolprop.rhomass();
EnthalpyV = coolprop.hmass() / 1000;
double Pr_l = CpL * ViscosityL / KL * 1000;
double h_fg = EnthalpyV - EnthalpyL; //"KJ"
double qflux = q / (l * 3.14159 * d);
double Bo = qflux / (g * h_fg);
double Co = Math.Pow(1 / x - 1, 0.8) * Math.Pow(DensityV / DensityL, 0.5);
double Fr_l = Math.Pow(g, 2.0) / (Math.Pow(DensityL, 2.0) * 9.8 * d);
double h_LO = 0.023 * Math.Pow(g * (1 - x) * d / ViscosityL, 0.8) * Math.Pow(Pr_l, 0.4) * (KL / d);
double h_LT = 0.023 * Math.Pow(g * (1 - 0) * d / ViscosityL, 0.8) * Math.Pow(Pr_l, 0.4) * (KL / d);
int N = 0;
double f = 0.0;
if (Fr_l > 0.04)
{
N = 0;
}
else
{
N = 1;
}
if (Bo > 0.0011)
{
f = 14.7;
}
else
{
f = 15.43;
}
double h1 = 230 * Math.Pow(Bo, 0.5) * h_LO;
double h2 = 1.8 * Math.Pow(Co * Math.Pow(0.38 * Math.Pow(Fr_l, -0.3), N), -0.8) * h_LO;
double h3 = f * Math.Pow(Bo, 0.5) * Math.Exp(2.47 * Math.Pow(Co * Math.Pow(0.38 * Math.Pow(Fr_l, -0.3), N), -0.15)) * h_LO;
double h4 = f * Math.Pow(Bo, 0.5) * Math.Exp(2.74 * Math.Pow(Co * Math.Pow(0.38 * Math.Pow(Fr_l, -0.3), N), -0.1)) * h_LO;
double h5 = h_LT;
double href = Math.Max(Math.Max(Math.Max(Math.Max(h1, h2), h3), h4), h5);
return(href);
}
public static double deltap_JR(string fluid, double d, double g, double p, double x, double l, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double DensityL, DensityV, ViscosityL, ViscosityV;
coolprop.update(input_pairs.PQ_INPUTS, p * 1000, 0);
double tsat = coolprop.T();
coolprop.update(input_pairs.QT_INPUTS, 0, tsat);
DensityL = coolprop.rhomass();
ViscosityL = coolprop.viscosity();
coolprop.update(input_pairs.QT_INPUTS, 1, tsat);
DensityV = coolprop.rhomass();
ViscosityV = coolprop.viscosity();
double Re_l = g * d / ViscosityL;
double f_sp = RefrigerantSPDP.ff_Friction(Re_l);
double DP_L = f_sp / d * Math.Pow(g, 2.0) / DensityL / 2000;
double dp = 0;
if (x <= 1.0)//0.93
{
double X_tt = Math.Pow(1 / x - 1, 0.9) * Math.Pow(DensityV / DensityL, 0.5) * Math.Pow(ViscosityL / ViscosityV, 0.1);
double f_tp = 12.82 * Math.Pow(X_tt, -1.47) * Math.Pow(1 - x, 1.8);
double f_fo = 0.046 * Math.Pow(Re_l, -0.2);
double DP_l = 2 * f_fo * Math.Pow(g, 2.0) / (DensityL * d);
double DP_tp = DP_l * f_tp;
dp = Math.Max(DP_L, DP_tp) * l;
dp = dp * 0.001;
}
else
{
double Re_v = g * d / ViscosityV;
double f_sp1 = RefrigerantSPDP.ff_Friction(Re_v);
double DP_1 = f_sp1 / d * Math.Pow(g, 2.0) / DensityV / 2000;
double x_point93 = 0.93;
double X_tt = Math.Pow(1 / x_point93 - 1, 0.9) * Math.Pow(DensityV / DensityL, 0.5) * Math.Pow(ViscosityL / ViscosityV, 0.1);
double f_tp = 12.82 * Math.Pow(X_tt, -1.47) * Math.Pow(1 - x_point93, 1.8);
double f_fo = 0.046 * Math.Pow(Re_l, -0.2);
double DP_l = 2 * f_fo * Math.Pow(g, 2.0) / (DensityL * d);
double DP_tp_point93 = DP_l * f_tp;
double DP_tp = (DP_tp_point93 + (x - 0.8) / (1.0 - 0.93) * (DP_1 - DP_tp_point93)) * l;
dp = DP_tp * 0.001;
}
return(dp);
}
public static double Kandlikar_Evap_href(string fluid, double d, double g, double p, double x, double q, double l, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double temperature;
double a_g = 9.8;
double DensityL, DensityV, EnthalpyL, EnthalpyV, ViscosityL, KL, CpL;
coolprop.update(input_pairs.PQ_INPUTS, p * 1000, 0);
temperature = coolprop.T();
coolprop.update(input_pairs.QT_INPUTS, 0, temperature);
DensityL = coolprop.rhomass();
EnthalpyL = coolprop.hmass() / 1000;
ViscosityL = coolprop.viscosity();
CpL = coolprop.cpmass() / 1000;
KL = coolprop.conductivity();
coolprop.update(input_pairs.QT_INPUTS, 1, temperature);
DensityV = coolprop.rhomass();
EnthalpyV = coolprop.hmass() / 1000;
//KL = CoolProp.PropsSI("L", "T", temperature, "Q", 0, fluid);
double Pr_l = CpL * ViscosityL / KL * 1000;
double Re_l = g * d * (1 - x) / ViscosityL;
double h_fg = (EnthalpyV - EnthalpyL);
double qflux = q / (l * 3.14159 * d);
double Fr_l = 0;
if (fluid == "Water")
{
Fr_l = 1;
}
else if (fluid == "R11")
{
Fr_l = 1.3;
}
else if (fluid == "R12")
{
Fr_l = 1.5;
}
else if (fluid == "R22")
{
Fr_l = 2.2;
}
else if (fluid == "R113")
{
Fr_l = 1.3;
}
else if (fluid == "R114")
{
Fr_l = 1.24;
}
else if (fluid == "R152a")
{
Fr_l = 1.1;
}
else if (fluid == "R13B1")
{
Fr_l = 1.31;
}
else if (fluid == "Nitrogen")
{
Fr_l = 4.7; //液氮
}
else if (fluid == "Neon")
{
Fr_l = 3.5; //液氖
}
else
{
Fr_l = 1;
}
double c1 = 1.136;
double c2 = -0.9;
double c3 = 1058;
double c4 = 0.7;
double c5 = 0.3;
if (Fr_l > 0.04)
{
c5 = 0;
}
double Fr_lo = Math.Pow(g, 2) / (Math.Pow(DensityL, 2) * a_g * d);
double Bo = qflux / (g * h_fg);
double Co = Math.Pow(DensityV / DensityL, 0.5) * Math.Pow(1 / x - 1, 0.8);
double h_L = 0.023 * Math.Pow(Re_l, 0.8) * Math.Pow(Pr_l, 0.4) * KL / d;
double href = (c1 * Math.Pow(Co, c2) * Math.Pow(25 * Fr_lo, c5) + c3 * Math.Pow(Bo, c4) * Fr_l) * h_L;
return(href);
}
public static double Dobson_Cond_href(string fluid, double d, double g, double p, double x, double Ts, double l, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double temperature;
double a_g = 9.80665;
double DensityL, DensityV, EnthalpyL, EnthalpyV, ViscosityL, ViscosityV, KL, CpL;
coolprop.update(input_pairs.PQ_INPUTS, p * 1000, 0);
temperature = coolprop.T();
coolprop.update(input_pairs.QT_INPUTS, 0, temperature);
DensityL = coolprop.rhomass();
EnthalpyL = coolprop.hmass() / 1000;
ViscosityL = coolprop.viscosity();
CpL = coolprop.cpmass() / 1000;
KL = coolprop.conductivity();
coolprop.update(input_pairs.QT_INPUTS, 1, temperature);
DensityV = coolprop.rhomass();
EnthalpyV = coolprop.hmass() / 1000;
ViscosityV = coolprop.viscosity();
double Pr_l = CpL * ViscosityL / KL * 1000;
double Re_l = g * (1.0 - x) * d / ViscosityL;
double X_tt = Math.Pow(DensityV / DensityL, 0.5) * Math.Pow(ViscosityL / ViscosityV, 0.1) * Math.Pow(1 / x - 1.0, 0.9);
double Re_vo = g * d / ViscosityV;
double G_a = a_g * DensityL * (DensityL - DensityV) * Math.Pow(d, 3.0) / Math.Pow(ViscosityL, 2.0);
//double Tsat = 1;
//double Ts = 0;
double Ja_l = CpL * (temperature - Ts) / (EnthalpyV - EnthalpyL);//Ts : surface temperature of tube wall
double Fr_l = Math.Pow(g, 2.0) / (Math.Pow(DensityL, 2.0) * g * d);
double c1 = 0;
double c2 = 0;
if (Fr_l > 0 && Fr_l <= 0.7)
{
c1 = 4.172 + 5.48 * Fr_l - 1.564 * Math.Pow(Fr_l, 2.0);
c2 = 1.773 - 0.169 * Fr_l;
}
else
{
c1 = 7.242;
c2 = 1.655;
}
double alpha = 1.0 / (1.0 + (1.0 - x) / x * Math.Pow(DensityV / DensityL, 2.0 / 3.0));
double thita_l = 3.14159 - Math.Acos(2.0 * alpha - 1);
double a = Math.Pow(1.376 + c1 / Math.Pow(X_tt, c2), 0.5);
double Nu_forced = 0.0195 * Math.Pow(Re_l, 0.8) * Math.Pow(Pr_l, 0.4) * a;
double Nu1 = 0.023 * Math.Pow(Re_l, 0.8) * Math.Pow(Pr_l, 0.4) * (1 + 2.22 / Math.Pow(X_tt, 0.89));
double Nu2 = 0.23 * Math.Pow(Re_vo, 0.12) / (1.0 + 1.11 * Math.Pow(X_tt, 0.58)) * Math.Pow(G_a * Pr_l / Ja_l, 0.25) + (1.0 - thita_l / 3.14159) * Nu_forced;
double h_tp;
double Fr_so = 0;
if (Re_l <= 1250)
{
Fr_so = 0.025 * Math.Pow(Re_l, 1.59) * Math.Pow((1.0 + 1.09 * Math.Pow(X_tt, 0.039)) / X_tt, 1.5) * Math.Pow(G_a, -0.5);
}
else
{
Fr_so = 1.26 * Math.Pow(Re_l, 1.04) * Math.Pow((1.0 + 1.09 * Math.Pow(X_tt, 0.039)) / X_tt, 1.5) * Math.Pow(G_a, -0.5);
}
if (g >= 500)
{
h_tp = KL * Nu1 / d;
}
else
{
if (Fr_so <= 20)
{
h_tp = KL * Nu2 / d;
}
else
{
h_tp = KL * Nu1 / d;
}
}
return(h_tp);
}
public static double Shah_Cond_href(string fluid, double d, double g, double p, double x, double q, double l, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double temperature;
double pc;
double a_g = 9.8;
double DensityL, DensityV, EnthalpyL, EnthalpyV, ViscosityL, ViscosityV, KL, CpL;
coolprop.update(input_pairs.PQ_INPUTS, p * 1000, 0);
temperature = coolprop.T();
coolprop.update(input_pairs.QT_INPUTS, 0, temperature);
DensityL = coolprop.rhomass();
EnthalpyL = coolprop.hmass() / 1000;
ViscosityL = coolprop.viscosity();
CpL = coolprop.cpmass() / 1000;
KL = coolprop.conductivity();
coolprop.update(input_pairs.QT_INPUTS, 1, temperature);
DensityV = coolprop.rhomass();
EnthalpyV = coolprop.hmass() / 1000;
ViscosityV = coolprop.viscosity();
pc = coolprop.p_critical() / 1000;
double pr = p / pc;
double Pr_l = CpL * ViscosityL / KL * 1000.0;
double Re_l = g * (1.0 - x) * d / ViscosityL;
//double h_fg = r.EnthalpyV - r.EnthalpyL; //"KJ"
//double qflux = q / (l * 3.14159 * d);
//double Bo = qflux / (g * h_fg);
//double Co = Math.Pow(1 / x - 1, 0.8) * Math.Pow(r.DensityV / r.DensityL, 0.5);
//double Fr_l = Math.Pow(g, 2.0) / (Math.Pow(r.DensityL, 2.0) * 9.8 * d);
//double h_LO = 0.023 * Math.Pow(g * (1 - x) * d / r.ViscosityL, 0.8) * Math.Pow(Pr_l, 0.4) * (r.KL / d);
//double h_LT = 0.023 * Math.Pow(g * (1 - 0) * d / r.ViscosityL, 0.8) * Math.Pow(Pr_l, 0.4) * (r.KL / d);
//int N = 0;
//double f = 0.0;
//if (Fr_l > 0.04) N = 0; else N = 1;
//if (Bo > 0.0011) f = 14.7; else f = 15.43;
//double h1 = 230 * Math.Pow(Bo, 0.5) * h_LO;
//double h2 = 1.8 * Math.Pow(Co * Math.Pow(0.38 * Math.Pow(Fr_l, -0.3), N), -0.8) * h_LO;
//double h3 = f * Math.Pow(Bo, 0.5) * Math.Exp(2.47 * Math.Pow(Co * Math.Pow(0.38 * Math.Pow(Fr_l, -0.3), N), -0.15)) * h_LO;
//double h4 = f * Math.Pow(Bo, 0.5) * Math.Exp(2.74 * Math.Pow(Co * Math.Pow(0.38 * Math.Pow(Fr_l, -0.3), N), -0.1)) * h_LO;
//double h5 = h_LT;
//double href = Math.Max(Math.Max(Math.Max(Math.Max(h1, h2), h3), h4), h5);
//return href;
double Z = Math.Pow(1.0 / x - 1.0, 0.8) * Math.Pow(pr, 0.4);
double J_g = x * g / Math.Pow(a_g * d * DensityV * (DensityL - DensityV), 0.5);
double h_LS = 0.023 * Math.Pow(Re_l, 0.8) * Math.Pow(Pr_l, 0.4) * KL / d;
double h_I = h_LS * (1 + 3.8 / Math.Pow(Z, 0.95)) * Math.Pow(ViscosityL / (14.0 * ViscosityV), (0.0058 + 0.557 * pr));
double h_Nu = 1.32 * Math.Pow(Re_l, -1.0 / 3.0) * Math.Pow(DensityL * (DensityL - DensityV) * a_g * Math.Pow(KL, 3.0) / Math.Pow(ViscosityL, 2.0), 1.0 / 3.0);
double a = 0.95 / (1.254 + 2.27 * Math.Pow(Z, 1.249));
double b = 0.98 * Math.Pow(Z + 0.263, -0.62);
double h_tp = 0;
if (J_g <= a)
{
h_tp = h_Nu;
}
else
{
if (J_g >= b)
{
h_tp = h_I;
}
else
{
h_tp = h_I + h_Nu;
}
}
return(h_tp);
}
public static double JR_Evap_href(string fluid, double d, double g, double p, double x, double q, double l, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double temperature;
double a_g = 9.8;
double sigma = 1;
int phase1 = 1;
double DensityL, DensityV, EnthalpyL, EnthalpyV, ViscosityL, ViscosityV, KL, CpL;
coolprop.update(input_pairs.PQ_INPUTS, p * 1000, 0);
temperature = coolprop.T();
coolprop.update(input_pairs.QT_INPUTS, 0, temperature);
DensityL = coolprop.rhomass();
EnthalpyL = coolprop.hmass() / 1000;
ViscosityL = coolprop.viscosity();
CpL = coolprop.cpmass() / 1000;
KL = coolprop.conductivity();
coolprop.update(input_pairs.QT_INPUTS, 1, temperature);
DensityV = coolprop.rhomass();
EnthalpyV = coolprop.hmass() / 1000;
ViscosityV = coolprop.viscosity();
double Pr_l = CpL * ViscosityL / KL * 1000;
double Re_l = g * d * (1 - x) / ViscosityL;
double h_fg = (EnthalpyV - EnthalpyL);
double qflux = q / (l * 3.14159 * d);
//单相流体的经验关联式
double Bo = qflux / (g * h_fg);
double X_tt = Math.Pow(DensityV / DensityL, 0.5) * Math.Pow(1 / x - 1, 0.9) * Math.Pow(ViscosityL / ViscosityV, 0.1);
double N = 1;
if (X_tt < 1)
{
N = 4048 * Math.Pow(X_tt, 1.22) * Math.Pow(Bo, 1.13);
}
double F_p = 2.37 * Math.Pow(0.29 + 1 / X_tt, 0.85);
//表面张力sigma的Refprop调用方法
double b_d = 0.0146 * (35 / 180 * 3.14159) * Math.Pow(2 * sigma / a_g / (DensityL - DensityV), 0.5);
double h_L = 0.023 * Math.Pow(Re_l, 0.8) * Math.Pow(Pr_l, 0.4) * KL / d;
double h_SA = 207 * KL / (b_d) * Math.Pow((qflux / KL) * (b_d / temperature), 0.745) * Math.Pow(DensityV / DensityL, 0.581) * Math.Pow(Pr_l, 0.533);
double h_nbc = N * h_SA;
double h_cec = F_p * h_L;
double href = h_nbc + h_cec;
return(href);
//两相传热关联式
//重点理解混合物换热关联式对纯质换热关联式的修正
//混合工质两组分各自泡核沸腾的计算式不清楚
//double X = 500;
//double Y = 30;
//double X_1 = 500;
//double X_2 = 500;
//double b2 = (1 - X) * log((1.01 - X) / (1.01 - Y)) + X * log(X / Y);
//double b3 = 0;
//if (X < 0.01)
//b3 = Math.Pow(Y/X, 0.1) - 1;
//double b4 = 152 * Math.Pow(p / p_cmvc, 3.9);
//double b5 = 0.92 * Math.Pow(abs(Y - X), 0.001) * Math.Pow(p / p_cmvc, 0.66);
//double C_un = (1 + (b2 + b3) * (1 + b4)) * (1 + b5);
//double N = 1;
//if (X_tt < 1)
//N = 4048 * Math.Pow(X_tt, 1.22) * Math.Pow(Bo, 1.13);
//double F_p = 2.37 * Math.Pow(0.29 + 1 / X_tt, 0.85);
//double C_me = 1 - 0.35 * Math.Pow(abs(Y - X), 1.56);
//double h_lo = 0.023 * Math.Pow(Re_l, 0.8) * Math.Pow(Pr_l, 0.4) * r.KL / d;
//double h_i = 1 / (X_1 / h_1 + X_2 / h_2);
//double h_un = h_i / C_un;
//double h_tp = N / C_un * h_un + C_me * F_p * h_lo;
//return h_tp;
}
static void Main(string[] args)
{
Console.Write("**************** INFORMATION ***************" + "\n");
Console.Write("This example was auto-generated by the language-agnostic dev/scripts/example_generator.py script written by Ian Bell" + "\n");
Console.Write("CoolProp version:" + " " + CoolProp.get_global_param_string("version") + "\n");
Console.Write("CoolProp gitrevision:" + " " + CoolProp.get_global_param_string("gitrevision") + "\n");
Console.Write("CoolProp Fluids:" + " " + CoolProp.get_global_param_string("FluidsList") + "\n");
// See http://www.coolprop.org/coolprop/HighLevelAPI.html#table-of-string-inputs-to-propssi-function for a list of inputs to high-level interface;
Console.Write("*********** HIGH LEVEL INTERFACE *****************" + "\n");
Console.Write("Critical temperature of water:" + " " + CoolProp.Props1SI("Water", "Tcrit") + " " + "K" + "\n");
Console.Write("Boiling temperature of water at 101325 Pa:" + " " + CoolProp.PropsSI("T", "P", 101325, "Q", 0, "Water") + " " + "K" + "\n");
Console.Write("Phase of water at 101325 Pa and 300 K:" + " " + CoolProp.PhaseSI("P", 101325, "Q", 0, "Water") + "\n");
Console.Write("c_p of water at 101325 Pa and 300 K:" + " " + CoolProp.PropsSI("C", "P", 101325, "T", 300, "Water") + " " + "J/kg/K" + "\n");
Console.Write("c_p of water (using derivatives) at 101325 Pa and 300 K:" + " " + CoolProp.PropsSI("d(H)/d(T)|P", "P", 101325, "T", 300, "Water") + " " + "J/kg/K" + "\n");
Console.Write("*********** HUMID AIR PROPERTIES *****************" + "\n");
Console.Write("Humidity ratio of 50% rel. hum. air at 300 K, 101325 Pa:" + " " + CoolProp.HAPropsSI("W", "T", 300, "P", 101325, "R", 0.5) + " " + "kg_w/kg_da" + "\n");
Console.Write("Relative humidity from last calculation:" + " " + CoolProp.HAPropsSI("R", "T", 300, "P", 101325, "W", CoolProp.HAPropsSI("W", "T", 300, "P", 101325, "R", 0.5)) + " " + "(fractional)" + "\n");
Console.Write("*********** INCOMPRESSIBLE FLUID AND BRINES *****************" + "\n");
Console.Write("Density of 50% (mass) ethylene glycol/water at 300 K, 101325 Pa:" + " " + CoolProp.PropsSI("D", "T", 300, "P", 101325, "INCOMP::MEG-50%") + " " + "kg/m^3" + "\n");
Console.Write("Viscosity of Therminol D12 at 350 K, 101325 Pa:" + " " + CoolProp.PropsSI("V", "T", 350, "P", 101325, "INCOMP::TD12") + " " + "Pa-s" + "\n");
// If you don't have REFPROP installed, disable the following lines;
Console.Write("*********** REFPROP *****************" + "\n");
Console.Write("Critical temperature of water:" + " " + CoolProp.Props1SI("REFPROP::Water", "Tcrit") + " " + "K" + "\n");
Console.Write("Boiling temperature of water at 101325 Pa:" + " " + CoolProp.PropsSI("T", "P", 101325, "Q", 0, "REFPROP::Water") + " " + "K" + "\n");
Console.Write("c_p of water at 101325 Pa and 300 K:" + " " + CoolProp.PropsSI("C", "P", 101325, "T", 300, "REFPROP::Water") + " " + "J/kg/K" + "\n");
Console.Write("*********** TABULAR BACKENDS *****************" + "\n");
AbstractState TAB = AbstractState.factory("BICUBIC&HEOS", "R245fa");
TAB.update(input_pairs.PT_INPUTS, 101325, 300);
Console.Write("Mass density of refrigerant R245fa at 300 K, 101325 Pa:" + " " + TAB.rhomass() + " " + "kg/m^3" + "\n");
Console.Write("*********** SATURATION DERIVATIVES (LOW-LEVEL INTERFACE) ***************" + "\n");
AbstractState AS_SAT = AbstractState.factory("HEOS", "R245fa");
AS_SAT.update(input_pairs.PQ_INPUTS, 101325, 0);
Console.Write("First saturation derivative:" + " " + AS_SAT.first_saturation_deriv(parameters.iP, parameters.iT) + " " + "Pa/K" + "\n");
Console.Write("*********** LOW-LEVEL INTERFACE *****************" + "\n");
AbstractState AS = AbstractState.factory("HEOS", "Water&Ethanol");
DoubleVector z = new DoubleVector(new double[] { 0.5, 0.5 });
AS.set_mole_fractions(z);
AS.update(input_pairs.PQ_INPUTS, 101325, 1);
Console.Write("Normal boiling point temperature of water and ethanol:" + " " + AS.T() + " " + "K" + "\n");
// If you don't have REFPROP installed, disable the following block;
Console.Write("*********** LOW-LEVEL INTERFACE (REFPROP) *****************" + "\n");
AbstractState AS2 = AbstractState.factory("REFPROP", "Methane&Ethane");
DoubleVector z2 = new DoubleVector(new double[] { 0.2, 0.8 });
AS2.set_mole_fractions(z2);
AS2.update(input_pairs.QT_INPUTS, 1, 120);
Console.Write("Vapor molar density:" + " " + AS2.keyed_output(parameters.iDmolar) + " " + "mol/m^3" + "\n");
}
public static CalcResult ElementCalc1(string fluid, double l, double Aa_fin, double Aa_tube, double A_r_cs, double Ar, Geometry geo, double tai,
double RHi, double tri, double pri, double hri, double mr, double g, double ma, double ha, double haw,
double eta_surface, double zh, double zdp, int hexType, double thickness, double conductivity, AbstractState coolprop, double[,] SourceTableData)
{
Model.HumidAirProp humidairprop = new Model.HumidAirProp();
RHi = RHi > 1 ? 1 : RHi;
double dh = geo.Di;
double r_metal = thickness / conductivity / Ar;
double gg = 9.8;
double q_initial = 0.01;
double q = q_initial;
bool flag = false;
double err = 0.01;
int iter = 1;
CalcResult res = new CalcResult();
double EnthalpyL, EnthalpyV;
coolprop.update(input_pairs.PQ_INPUTS, pri * 1000, 0);
tri = coolprop.T() - 273.15;
//tri = CoolProp.PropsSI("T", "P", pri * 1000, "Q", 0, fluid) - 273.15;
coolprop.update(input_pairs.QT_INPUTS, 0, tri + 273.15);
EnthalpyL = coolprop.hmass() / 1000;
//EnthalpyL = CoolProp.PropsSI("H", "T", tri + 273.15, "Q", 0, fluid) / 1000;
coolprop.update(input_pairs.QT_INPUTS, 1, tri + 273.15);
EnthalpyV = coolprop.hmass() / 1000;
//EnthalpyV = CoolProp.PropsSI("H", "T", tri + 273.15, "Q", 1, fluid) / 1000;
res.x_i = (hri - EnthalpyL) / (EnthalpyV - EnthalpyL);
RefHTCandDPResult htc_dp = new RefHTCandDPResult();
do
{
flag = false;
htc_dp = RefrigerantHTCandDP.HTCandDP_2p(fluid, dh, g, pri, res.x_i, l, q, zh, zdp, hexType, coolprop);
res.href = htc_dp.Href;
res.DP = htc_dp.DPref;
double k_fin = 237;
double Fthickness = geo.Fthickness;
double Pt = geo.Pt;
double Pr = geo.Pr;
double Do = geo.Do;
double r_eta = Do / 2;
double XD = Math.Pow((Pr * Pr + Pt * Pt / 4), 0.5) / 2;
double XT = Pt / 2;
double rf_r = 1.27 * XT / r_eta * Math.Pow((XD / XT - 0.3), 0.5);
double m = Math.Pow((2 * ha / k_fin / Fthickness), 0.5);
double fai = (rf_r - 1) * (1 + (0.3 + Math.Pow((m * r_eta * (rf_r - r_eta) / 2.5), (1.5 - 1 / 12 * rf_r)) * (0.26 * Math.Pow(rf_r, 0.3) - 0.3)) * Math.Log(rf_r));
double eta_0 = Math.Tanh(m * r_eta * fai) / m / r_eta / fai * Math.Cos(0.1 * m * r_eta * fai);
double eta_a = (eta_0 * Aa_fin + Aa_tube) / (Aa_fin + Aa_tube);
////
//double cp_a0 = CoolProp.HAPropsSI("C", "T", tai + 273.15, "P", 101325, "R", RHi);
//double cp_a = 1005.1458551 + 0.1541627 * tai + 4.3454442 * RHi - 0.0090904 * Math.Pow(tai, 2) - 0.3409659 * Math.Pow(RHi, 2) - 0.0007819 * tai * RHi + 0.0001851 * Math.Pow(tai, 3) + 0.0049274 * Math.Pow(RHi, 3) + 0.0476513 * tai * Math.Pow(RHi, 2) + 0.020268209 * Math.Pow(tai, 2) * RHi;
double cp_a = humidairprop.Cp(tai, RHi, SourceTableData);
double UA = 1 / (1 / ha / (Aa_fin * eta_0 + Aa_tube) + 1 / (res.href * Ar) + r_metal);
double Ntu_dry = UA / (ma * cp_a);
double epsilon_dry = 1 - Math.Exp(-Ntu_dry);
double Q_dry = epsilon_dry * ma * cp_a * (tai - tri) * Math.Pow(-1, hexType);
double tao = tai - Q_dry / (ma * cp_a) * Math.Pow(-1, hexType);
double hro = hri + Q_dry / 1000 / mr * Math.Pow(-1, hexType);
double UA_o = ha * (Aa_fin * eta_0 + Aa_tube);
double UA_i = res.href * Ar;
double NTU_o = UA_o / (cp_a * ma);
double T_so_a = (UA_o * tai + UA_i * tri) / (UA_o + UA_i);
double T_so_b = (UA_o * tao + UA_i * tri) / (UA_o + UA_i);
double Q = Q_dry;
double Q_sensible = 0;
//double omega_in0 = CoolProp.HAPropsSI("W", "T", tai + 273.15, "P", 101325, "R", RHi);
//double omega_in = (-0.0682340 + 0.0292341 * tai + 4.1604535 * RHi - 0.0025985 * Math.Pow(tai, 2) - 0.0769009 * Math.Pow(RHi, 2) + 0.1246489 * tai * RHi + 6.008 * Math.Pow(10, -5) * Math.Pow(tai, 3) - 0.0006775 * Math.Pow(RHi, 3) + 0.0267183 * tai * Math.Pow(RHi, 2) + 0.019904969 * Math.Pow(tai, 2) * RHi) / 1000;
double omega_in = humidairprop.O(tai, RHi, SourceTableData);
//double hai0 = CoolProp.HAPropsSI("H", "T", tai + 273.15, "P", 101325, "R", RHi);
//double hai = -244.2924077 + 1135.8711 * tai + 10101.404 * RHi - 12.968219 * Math.Pow(tai, 2) - 11.356807 * Math.Pow(RHi, 2) + 357.25464 * tai * RHi + 0.3178346 * Math.Pow(tai, 3) - 0.0024329 * Math.Pow(RHi, 3) + 44.100799 * tai * Math.Pow(RHi, 2) + 50.31444812 * Math.Pow(tai, 2) * RHi;
double hai = humidairprop.H(tai, "R", RHi, SourceTableData);
//double ha2 = ((1.006 + 1.805 * omega_in1) * tai + 2501 * omega_in1) * 1000;//采用湿空气 物性的关系来写
//double omega_out = omega_in;
double hout_a = hai - Q / ma * Math.Pow(-1, hexType);
/////
//***delete***//
//res.RHout = CoolProp.HAPropsSI("R", "T", tao + 273.15, "P", 101325, "W", omega_out);
//res.RHout = 0.0215344 - 0.0059467 * tao + 0.2386894 * (omega_out * 1000) + 0.0004378 * Math.Pow(tao, 2) + 0.0004635 * Math.Pow((omega_out * 1000), 2) - 0.0125912 * tao * (omega_out * 1000) - 9.134 * Math.Pow(10, -6) * Math.Pow(tao, 3) + 1.696 * Math.Pow(10, -6) * Math.Pow((omega_out * 1000), 3) - 2.214 * Math.Pow(10, -5) * tao * Math.Pow((omega_out * 1000), 2) + 0.000200865 * Math.Pow(tao, 2) * (omega_out * 1000);
//***delete***//
//double resRHout0 = CoolProp.HAPropsSI("R", "T", tao + 273.15, "P", 101325, "H", hout_a);
//res.RHout = 0.0259124 - 0.0996818 * tao + 0.0934877 * (hout_a / 1000) + 0.0040018 * Math.Pow(tao, 2) - 0.0003662 * Math.Pow((hout_a / 1000), 2) - 0.0034077 * tao * (hout_a / 1000) - 1.76447 * Math.Pow(10, -5) * Math.Pow(tao, 3) - 2.74524 * Math.Pow(10, -6) * Math.Pow((hout_a / 1000), 3) + 2.99291 * Math.Pow(10, -5) * tao * Math.Pow((hout_a / 1000), 2) - 9.56644 * Math.Pow(10, -6) * Math.Pow(tao, 2) * (hout_a / 1000);
double Tdp_out = humidairprop.Ts(hout_a, SourceTableData);
res.RHout = humidairprop.RHI(tao, Tdp_out, SourceTableData);
double f_dry = 0;
if (hexType == 0 && tri < tai)
{
double hao = 0;
//double Tdp0 = CoolProp.HAPropsSI("D", "T", tai + 273.15, "P", 101325, "R", RHi) - 273.15;
//double Tdp = -273.15 + 241.0212518 + 0.5718833 * tai + 84.99553 * RHi + 0.002691 * Math.Pow(tai, 2) - 95.003186 * Math.Pow(RHi, 2) + 0.7135779 * tai * RHi - 2.691 / Math.Pow(10, 5) * Math.Pow(tai, 3) + 42.58183 * Math.Pow(RHi, 3) - 0.3227474 * tai * Math.Pow(RHi, 2) - 0.000884612 * Math.Pow(tai, 2) * RHi;
double Tdp = humidairprop.Tdp(tai, RHi, SourceTableData);
/*
* double Ps = omega_in * 101325 / (0.622 + omega_in);
* double Tdp1 = -39.957 - 1.8762 * Math.Log(Ps) + 1.1689 * Math.Pow(Math.Log(Ps), 2);
* double Tdp3 = 8.22 + 12.4 * Math.Log(Ps) + 1.9 * Math.Pow(Math.Log(Ps), 2);
* if (Tdp1 <= 0)
* {
* Tdp1 = -60.45 + 7.0322 * Math.Log(Ps) + 0.37 * Math.Pow(Math.Log(Ps), 2);
* }
*/
if (T_so_b > Tdp)
{
f_dry = 1.0;
Q = Q_dry;
Q_sensible = Q;
//omega_out = omega_in;
}
else
{
double T_ac = 0;
double h_ac = 0;
if (T_so_a < Tdp)
{
f_dry = 0.0;
Q_dry = 0.0;
T_ac = tai;
h_ac = hai;
}
else
{
T_ac = Tdp + UA_i / UA_o * (Tdp - tri);
epsilon_dry = (tai - T_ac) / (tai - tri);
f_dry = -1.0 / Ntu_dry * Math.Log(1.0 - epsilon_dry);
//double h_ac0 = CoolProp.HAPropsSI("H", "T", T_ac + 273.15, "P", 101325, "W", omega_in);
//h_ac = -244.2924077 + 1135.8711 * T_ac + 10101.404 * RHi - 12.968219 * Math.Pow(T_ac, 2) - 11.356807 * Math.Pow(RHi, 2) + 357.25464 * T_ac * RHi + 0.3178346 * Math.Pow(T_ac, 3) - 0.0024329 * Math.Pow(RHi, 3) + 44.100799 * T_ac * Math.Pow(RHi, 2) + 50.31444812 * Math.Pow(T_ac, 2) * RHi;
h_ac = humidairprop.H(T_ac, "Omega", omega_in, SourceTableData);
Q_dry = ma * cp_a * (tai - T_ac);
}
//double h1 = 58.732687 * Math.Pow(tri + 273.15 + 0.01, 2) - 30921.970577 * (tri + 273.15 + 0.01) + 4075493.951473;
double h1 = humidairprop.H(tri + 0.01, "R", 1, SourceTableData);
//double h2 = 58.732687 * Math.Pow(tri + 273.15 - 0.01, 2) - 30921.970577 * (tri + 273.15 - 0.01) + 4075493.951473;
double h2 = humidairprop.H(tri - 0.01, "R", 1, SourceTableData);
double c_s = (h1 - h2) / 0.02;
//double c_s0 = (CoolProp.HAPropsSI("H", "T", tri + 273.15 + 0.01, "P", 101325, "R", 1.0) - CoolProp.HAPropsSI("H", "T", tri + 273.15 - 0.01, "P", 101325, "R", 1.0)) / 0.02;
m = Math.Pow((2 * haw / k_fin / Fthickness), 0.5);
fai = (rf_r - 1) * (1 + (0.3 + Math.Pow((m * r_eta * (rf_r - r_eta) / 2.5), (1.5 - 1 / 12 * rf_r)) * (0.26 * Math.Pow(rf_r, 0.3) - 0.3)) * Math.Log(rf_r));
double eta_wet = Math.Tanh(m * r_eta * fai) / m / r_eta / fai * Math.Cos(0.1 * m * r_eta * fai);
//eta_a = (eta_0 * Aa_fin + Aa_tube) / (Aa_fin + Aa_tube);
UA_o = haw * (eta_wet * Aa_fin + Aa_tube);
NTU_o = UA_o / (ma * cp_a);
double UA_wet = 1 / (c_s / UA_i + cp_a / UA_o);
double Ntu_wet = UA_wet / ma;
double epsilon_wet = 1 - Math.Exp(-(1 - f_dry) * Ntu_wet);
//double h_s_s_o0 = CoolProp.HAPropsSI("H", "T", tri + 273.15, "P", 101325, "R", 1.0);
//double h_s_s_o = 58.732687 * Math.Pow(tri + 273.15, 2) - 30921.970577 * (tri + 273.15 - 0.01) + 4075493.951473;
double h_s_s_o = humidairprop.H(tri, "R", 1, SourceTableData);
double Q_wet = epsilon_wet * ma * (h_ac - h_s_s_o);
Q = Q_wet + Q_dry;
hao = h_ac - Q_wet / ma;
double h_s_s_e = h_ac - (h_ac - hao) / (1 - Math.Exp(-(1 - f_dry) * NTU_o));
//double T_s_e0 = CoolProp.HAPropsSI("T","H",h_s_s_e,"P",101325,"R",1.0)-273.15;
//double T_s_e = -273.15 - 1.96 * Math.Pow(10, -3) * Math.Pow(h_s_s_e / 1000, 2) + 0.5357597 * h_s_s_e / 1000 + 268.871551;
double T_s_e = humidairprop.Ts(h_s_s_e, SourceTableData);
tao = T_s_e + (T_ac - T_s_e) * Math.Exp(-(1 - f_dry) * NTU_o);
Q_sensible = ma * cp_a * (tai - tao);
hro = hri + Q / 1000 / mr;
}
hout_a = hai - Q / ma * Math.Pow(-1, hexType);
//double resRHout00 = CoolProp.HAPropsSI("R", "T", tao + 273.15, "P", 101325, "H", hout_a);
//res.RHout = 0.0259124 - 0.0996818 * tao + 0.0934877 * (hout_a / 1000) + 0.0040018 * Math.Pow(tao, 2) - 0.0003662 * Math.Pow((hout_a / 1000), 2) - 0.0034077 * tao * (hout_a / 1000) - 1.76447 * Math.Pow(10, -5) * Math.Pow(tao, 3) - 2.74524 * Math.Pow(10, -6) * Math.Pow((hout_a / 1000), 3) + 2.99291 * Math.Pow(10, -5) * tao * Math.Pow((hout_a / 1000), 2) - 9.56644 * Math.Pow(10, -6) * Math.Pow(tao, 2) * (hout_a / 1000);
Tdp_out = humidairprop.Ts(hout_a, SourceTableData);
res.RHout = humidairprop.RHI(tao, Tdp_out, SourceTableData);
if (res.RHout > 1)
{
res.RHout = 1;
//double tao0 = CoolProp.HAPropsSI("T", "H", hao, "P", 101325, "R", 1)-273.15;
//tao = -273.15 - 1.96 * Math.Pow(10, -3) * Math.Pow(hao / 1000, 2) + 0.5357597 * hao / 1000 + 268.871551;
tao = humidairprop.Ts(hao, SourceTableData);
Q_sensible = ma * cp_a * (tai - tao);
}
}
res.R_1a = 1 / ((eta_0 * Aa_fin + Aa_tube) * ha);
res.R_1r = 1 / (res.href * Ar);
res.R_1 = res.R_1a + res.R_1r + r_metal;
res.Q = Q / 1000;
res.Tao = tao;
res.hro = hro;
res.Pro = pri - res.DP;
if (res.Pro < 0)
{
res.Pro = -10000000; return(res);
}
coolprop.update(input_pairs.HmassP_INPUTS, res.hro * 1000, res.Pro * 1000);
res.Tro = coolprop.T() - 273.15;
//res.Tro = CoolProp.PropsSI("T", "P", res.Pro * 1000, "H", res.hro * 1000, fluid);
double rho_o = coolprop.rhomass();
//double rho_o = CoolProp.PropsSI("D", "P", res.Pro * 1000, "H", res.hro * 1000, fluid);
res.Vel_r = g / rho_o;
res.x_o = (res.hro - EnthalpyL) / (EnthalpyV - EnthalpyL); //+ 139.17 for reference state, to be changed
if (Math.Abs(q - res.Q) / res.Q > err)
{
q = res.Q;
flag = true;
}
iter++;
} while (flag && iter < 20);
//if (iter >= 20)
//{
// throw new Exception("iter for href > 100.");
//}
return(res);
}
public static CalcResult ElementCalc(string fluid, double l, double Aa_fin, double Aa_tube, double A_r_cs, double Ar, Geometry geo, double tai,
double RHi, double tri, double pri, double hri, double mr, double g, double ma, double ha, double haw,
double eta_surface, double zh, double zdp, int hexType, double thickness, double conductivity, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double dh = geo.Di;
double r_metal = thickness / conductivity / Ar;
double gg = 9.8;
double q_initial = 0.01;
double q = q_initial;
double err = 0.01;
bool flag = false;
int iter = 1;
CalcResult res = new CalcResult();
//res.Tao[0] = new double();
double EnthalpyL, EnthalpyV;
//recalc tri to make sure it is 2ph, ruhao, 20180225
coolprop.update(input_pairs.PQ_INPUTS, pri * 1000, 0);
tri = coolprop.T() - 273.15;
//tri = CoolProp.PropsSI("T", "P", pri * 1000, "Q", 0, fluid) - 273.15;
coolprop.update(input_pairs.QT_INPUTS, 0, tri + 273.15);
EnthalpyL = coolprop.hmass() / 1000;
//EnthalpyL = CoolProp.PropsSI("H", "T", tri + 273.15, "Q", 0, fluid) / 1000;
coolprop.update(input_pairs.QT_INPUTS, 1, tri + 273.15);
EnthalpyV = coolprop.hmass() / 1000;
//EnthalpyV = CoolProp.PropsSI("H", "T", tri + 273.15, "Q", 1, fluid) / 1000;
res.x_i = (hri - EnthalpyL) / (EnthalpyV - EnthalpyL);
RefHTCandDPResult htc_dp = new RefHTCandDPResult();
do
{
flag = false;
htc_dp = RefrigerantHTCandDP.HTCandDP_2p(fluid, dh, g, pri, res.x_i, l, q, zh, zdp, hexType, coolprop);
res.href = htc_dp.Href;
res.DP = htc_dp.DPref;
double cp_a = 1.0; //keep it for now as a constant
cp_a = (hexType == 0 ? 1.027 : 1.02);
double C_a = ma * cp_a;
res.R_1a = 1 / ((eta_surface * Aa_fin + Aa_tube) * ha);
res.R_1r = 1 / (res.href * Ar);
res.R_1 = res.R_1a + res.R_1r + r_metal;
double UA = 1 / res.R_1;
double NTU = UA / (C_a * 1000);
double epsilon = 1 - Math.Exp(-NTU);
res.Q = epsilon * C_a * (tai - tri) * Math.Pow(-1, hexType);//Math.Abs(tai - tri)
res.Tao = tai + Math.Pow(-1, (hexType + 1)) * res.Q / C_a;
res.hro = hri + Math.Pow(-1, hexType) * res.Q / mr;
//0:evap, 1:cond
res.x_o = (res.hro - EnthalpyL) / (EnthalpyV - EnthalpyL); //+ 139.17 for reference state, to be changed
//res.DP = 0;
res.Pro = pri - res.DP;
if (res.Pro < 0)
{
res.Pro = -10000000; return(res);
}
coolprop.update(input_pairs.HmassP_INPUTS, res.hro * 1000, res.Pro * 1000);
res.Tro = coolprop.T();
//res.Tro = CoolProp.PropsSI("T", "P", res.Pro * 1000, "H", res.hro * 1000, fluid);
double rho_o = coolprop.rhomass();
//double rho_o = CoolProp.PropsSI("D", "P", res.Pro * 1000, "H", res.hro * 1000, fluid);
res.Tro = res.Tro - 273.15;
res.Vel_r = g / rho_o;
if (Math.Abs(q - res.Q) / res.Q > err)
{
q = res.Q;
flag = true;
}
iter++;
} while (flag && iter < 100);
if (iter >= 100)
{
throw new Exception("iter for href > 100.");
}
return(res);
}
public static Capiliary_res CapiliaryCalc(int index, string fluid, double d_cap, double lenth_cap, double tri, double pri, double hri, double mr, double Pwater, int hexType, AbstractState coolprop, double[,] SourceTableData)
{
//毛细管守恒方程模型
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
Capiliary_res res_cap = new Capiliary_res();
double Ar_cs = Math.PI * Math.Pow(d_cap, 2) / 4;
double g = mr / Ar_cs;
coolprop.update(input_pairs.PQ_INPUTS, pri * 1000, 0);
double tsat = coolprop.T();
//double tsat = CoolProp.PropsSI("T", "P", pri * 1000, "Q", 0, fluid);
coolprop.update(input_pairs.QT_INPUTS, 0, tsat);
double h_l = coolprop.hmass() / 1000;
//double h_l = CoolProp.PropsSI("H", "T", tsat, "Q", 0, fluid) / 1000;
coolprop.update(input_pairs.QT_INPUTS, 1, tsat);
double h_v = coolprop.hmass() / 1000;
//double h_v = CoolProp.PropsSI("H", "T", tsat, "Q", 1, fluid) / 1000;
double x_i = (hri - h_l) / (h_v - h_l);
coolprop.update(input_pairs.PQ_INPUTS, (fluid == "Water" ? Pwater : pri) * 1000, 1);
double rho_gi = coolprop.rhomass();
//double rho_gi = CoolProp.PropsSI("D", "Q", 1, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
coolprop.update(input_pairs.PQ_INPUTS, (fluid == "Water" ? Pwater : pri) * 1000, 0);
double rho_li = coolprop.rhomass();
//double rho_li = CoolProp.PropsSI("D", "Q", 0, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double mgi = x_i * mr;
double mli = (1 - x_i) * mr;
double esp_i = 1 / (1 + (1 / x_i - 1) * rho_gi / rho_li);
double Vgi = (x_i * mr) / (rho_gi * esp_i * Ar_cs);
double Vli = (1 - x_i) * mr / (rho_li * (1 - esp_i) * Ar_cs);
//初始化出口参数
double x_o = x_i;
double mgo = mgi;
double mlo = mli;
double rho_go = rho_gi;
double rho_lo = rho_li;
double esp_o = esp_i;
double Vgo_set = Vgi;
double Vlo = Vli;
double rho_avg = rho_gi * x_i + rho_li * (1 - x_i);
coolprop.update(input_pairs.QT_INPUTS, 0, tsat);
double ViscosityL = coolprop.viscosity();
//double ViscosityL = CoolProp.PropsSI("V", "T", tsat, "Q", 0, fluid);
coolprop.update(input_pairs.QT_INPUTS, 1, tsat);
double ViscosityV = coolprop.viscosity();
//double ViscosityV = CoolProp.PropsSI("V", "T", tsat, "Q", 1, fluid);
double ViscosityTP = x_i * ViscosityV + (1 - x_i) * ViscosityL;
double ReTP = g * d_cap / ViscosityTP;
double f_tpi = 0.11 * Math.Pow(0.0014 + 68 / ReTP, 0.25);//0.0014表面粗糙度
double f_tp = f_tpi;
double Vgo_cal = 0;
int i = 0;
double Pro = 0;
double hro = 0;
double tro = 0;
coolprop.update(input_pairs.HmassP_INPUTS, hri * 1000, pri * 1000);
double tro1 = coolprop.T() - 273.15;
//double tro1 = CoolProp.PropsSI("T", "H", hri * 1000, "P", pri * 1000, fluid) - 273.15;
double tro2 = 0;
if (hri <= h_v && hri >= h_l)
{
do
{
if (i != 0)
{
Vgo_set = Vgo_cal;
}
//守恒方程
double a = f_tp / 4 * Math.Pow(mr, 2) / (2 * rho_avg * Math.Pow(Ar_cs, 2)) * Math.PI * d_cap + mr / lenth_cap * (x_o * Vgo_set + (1 - x_o) * Vlo) - mr / lenth_cap * (x_i * Vgi + (1 - x_i) * Vli);
Pro = pri - lenth_cap / Ar_cs * (f_tp / 4 * Math.Pow(mr, 2) / (2 * rho_avg * Math.Pow(Ar_cs, 2)) * Math.PI * d_cap + mr / lenth_cap * (x_o * Vgo_set + (1 - x_o) * Vlo) - mr / lenth_cap * (x_i * Vgi + (1 - x_i) * Vli));
hro = 1 / mr * (mr * hri + 1 / 2 * mgi * Math.Pow(Vgi, 2) + 1 / 2 * mli * Math.Pow(Vli, 2) - 1 / 2 * mgo * Math.Pow(Vgo_set, 2) - 1 / 2 * mlo * Math.Pow(Vlo, 2));
//新一轮赋值
coolprop.update(input_pairs.PQ_INPUTS, Pro * 1000, 0);
double tsato = coolprop.T();
//double tsato = CoolProp.PropsSI("T", "P", Pro * 1000, "Q", 0, fluid);
coolprop.update(input_pairs.QT_INPUTS, 0, tsato);
double h_lo = coolprop.hmass();
//double h_lo = CoolProp.PropsSI("H", "T", tsato, "Q", 0, fluid) / 1000;
coolprop.update(input_pairs.QT_INPUTS, 1, tsato);
double h_vo = coolprop.hmass();
//double h_vo = CoolProp.PropsSI("H", "T", tsato, "Q", 1, fluid) / 1000;
coolprop.update(input_pairs.PQ_INPUTS, (fluid == "Water" ? Pwater : Pro) * 1000, 1);
rho_go = coolprop.rhomass();
//rho_go = CoolProp.PropsSI("D", "Q", 1, "P", (fluid == "Water" ? Pwater : Pro) * 1000, fluid);
coolprop.update(input_pairs.PQ_INPUTS, (fluid == "Water" ? Pwater : Pro) * 1000, 0);
rho_lo = coolprop.rhomass();
//rho_lo = CoolProp.PropsSI("D", "Q", 0, "P", (fluid == "Water" ? Pwater : Pro) * 1000, fluid);
x_o = (hro - h_lo) / (h_vo - h_lo);
esp_o = 1 / (1 + (1 / x_o - 1) * rho_go / rho_lo);
Vgo_cal = (x_o * mr) / (rho_go * esp_o * Ar_cs);
Vlo = (1 - x_o) * mr / (rho_lo * (1 - esp_o) * Ar_cs);
mgo = x_o * mr;
mlo = (1 - x_o) * mr;
rho_avg = (rho_gi * x_i + rho_li * (1 - x_i) + rho_go * x_o + rho_lo * (1 - x_o)) / 2;
coolprop.update(input_pairs.QT_INPUTS, 0, tsato);
double ViscosityLo = coolprop.viscosity();
//double ViscosityLo = CoolProp.PropsSI("V", "T", tsato, "Q", 0, fluid);
coolprop.update(input_pairs.QT_INPUTS, 1, tsato);
double ViscosityVo = coolprop.viscosity();
//double ViscosityVo = CoolProp.PropsSI("V", "T", tsato, "Q", 1, fluid);
double ViscosityTPo = x_o * ViscosityVo + (1 - x_o) * ViscosityLo;
double ReTPo = g * d_cap / ViscosityTPo;
double f_tpo = 0.11 * Math.Pow(0.0014 + 68 / ReTPo, 0.25);
f_tp = (f_tpi + f_tpo) / 2;
i++;
} while (Math.Abs((Vgo_cal - Vgo_set) / Vgo_cal) > 0.02);
}
else
{
do
{
if (i != 0)
{
tro1 = tro2;
}
if (i != 0)
{
Vgo_set = Vgo_cal;
}
//守恒方程
double a = f_tp / 4 * Math.Pow(mr, 2) / (2 * rho_avg * Math.Pow(Ar_cs, 2)) * Math.PI * d_cap + mr / lenth_cap * (x_o * Vgo_set + (1 - x_o) * Vlo) - mr / lenth_cap * (x_i * Vgi + (1 - x_i) * Vli);
Pro = pri - lenth_cap / Ar_cs * (f_tp / 4 * Math.Pow(mr, 2) / (2 * rho_avg * Math.Pow(Ar_cs, 2)) * Math.PI * d_cap + mr / lenth_cap * (x_o * Vgo_set + (1 - x_o) * Vlo) - mr / lenth_cap * (x_i * Vgi + (1 - x_i) * Vli));
hro = 1 / mr * (mr * hri + 1 / 2 * mgi * Math.Pow(Vgi, 2) + 1 / 2 * mli * Math.Pow(Vli, 2) - 1 / 2 * mgo * Math.Pow(Vgo_set, 2) - 1 / 2 * mlo * Math.Pow(Vlo, 2));
//新一轮赋值
coolprop.update(input_pairs.PQ_INPUTS, Pro * 1000, 0);
double tsato = coolprop.T();
//double tsato = CoolProp.PropsSI("T", "P", Pro * 1000, "Q", 0, fluid);
coolprop.update(input_pairs.QT_INPUTS, 0, tsato);
double h_lo = coolprop.hmass();
//double h_lo = CoolProp.PropsSI("H", "T", tsato, "Q", 0, fluid) / 1000;
coolprop.update(input_pairs.QT_INPUTS, 1, tsato);
double h_vo = coolprop.hmass();
//double h_vo = CoolProp.PropsSI("H", "T", tsato, "Q", 1, fluid) / 1000;
coolprop.update(input_pairs.PQ_INPUTS, (fluid == "Water" ? Pwater : Pro) * 1000, 1);
rho_go = coolprop.rhomass();
//rho_go = CoolProp.PropsSI("D", "Q", 1, "P", (fluid == "Water" ? Pwater : Pro) * 1000, fluid);
coolprop.update(input_pairs.PQ_INPUTS, (fluid == "Water" ? Pwater : Pro) * 1000, 0);
rho_lo = coolprop.rhomass();
//rho_lo = CoolProp.PropsSI("D", "Q", 0, "P", (fluid == "Water" ? Pwater : Pro) * 1000, fluid);
x_o = (hro - h_lo) / (h_vo - h_lo);
esp_o = 1 / (1 + (1 / x_o - 1) * rho_go / rho_lo);
Vgo_cal = (x_o * mr) / (rho_go * esp_o * Ar_cs);
Vlo = (1 - x_o) * mr / (rho_lo * (1 - esp_o) * Ar_cs);
mgo = x_o * mr;
mlo = (1 - x_o) * mr;
rho_avg = (rho_gi * x_i + rho_li * (1 - x_i) + rho_go * x_o + rho_lo * (1 - x_o)) / 2;
coolprop.update(input_pairs.QT_INPUTS, 0, tsato);
double ViscosityLo = coolprop.viscosity();
//double ViscosityLo = CoolProp.PropsSI("V", "T", tsato, "Q", 0, fluid);
coolprop.update(input_pairs.QT_INPUTS, 1, tsato);
double ViscosityVo = coolprop.viscosity();
//double ViscosityVo = CoolProp.PropsSI("V", "T", tsato, "Q", 1, fluid);
double ViscosityTPo = x_o * ViscosityVo + (1 - x_o) * ViscosityLo;
double ReTPo = g * d_cap / ViscosityTPo;
double f_tpo = 0.11 * Math.Pow(0.0014 + 68 / ReTPo, 0.25);
f_tp = (f_tpi + f_tpo) / 2;
coolprop.update(input_pairs.HmassP_INPUTS, hro * 1000, Pro * 1000);
tro2 = coolprop.T() - 273.15;
//tro2 = CoolProp.PropsSI("T", "H", hro * 1000, "P", Pro * 1000, fluid) - 273.15;
i++;
} while (Math.Abs(tro2 - tro1) > 0.02);
}
double DP_cap = pri - Pro;
coolprop.update(input_pairs.HmassP_INPUTS, hro * 1000, Pro * 1000);
tro = coolprop.T() - 273.15;
//tro = CoolProp.PropsSI("T", "H", hro * 1000, "P", Pro * 1000, fluid) - 273.15;
res_cap.pro = Pro;
res_cap.hro = hro;
res_cap.tro = tro;
res_cap.DP_cap = DP_cap;
res_cap.x_o = x_o;
return(res_cap);
}
public static CalcResult ElementCal(string fluid, double l,
double Aa_fin, double Aa_tube, double A_r_cs, double Ar, Geometry geo, double tai, double RHi,
double tri, double pri, double hri, double mr, double g, double ma, double ha, double haw,
double eta_surface, double zh, double zdp, int hexType, double thickness, double conductivity, double Pwater, AbstractState coolprop, double[,] SourceTableData)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double tsat;
coolprop.update(input_pairs.PQ_INPUTS, pri * 1000, 0);
tsat = coolprop.T();
//tsat = CoolProp.PropsSI("T", "P", pri * 1000, "Q", 0, fluid);
double Vol_tubes = A_r_cs * l; //Tube volume, for charge calculation
coolprop.update(input_pairs.QT_INPUTS, 0, tsat);
double h_l = coolprop.hmass() / 1000;
//double h_l = CoolProp.PropsSI("H", "T", tsat, "Q", 0, fluid) / 1000 ;
coolprop.update(input_pairs.QT_INPUTS, 1, tsat);
double h_v = coolprop.hmass() / 1000;
//double h_v1 = CoolProp.PropsSI("H", "T", tsat, "Q", 1, fluid) / 1000 ;
double Tri_mod;
double alpha;
var res_element = new CalcResult();
// **********Superheated state**********
if (hri > h_v && fluid != "Water")
{
if (hri < 1.02 * h_v) //ignore modification for now, ruhao,20180226
{
Tri_mod = tri + 0.5 * 0; //"for Tri modification in the transition region"
}
else
{
Tri_mod = tri;
}
res_element = SPElement.ElementCalc3(fluid, l, Aa_fin, Aa_tube, A_r_cs, Ar, geo, tai, RHi, Tri_mod, pri, hri, mr, g, ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, coolprop, SourceTableData);
if (res_element.Pro < 0)
{
return(res_element);
}
res_element.x_i = (hri - h_l) / (h_v - h_l);
res_element.x_o = (res_element.hro - h_l) / (h_v - h_l);
alpha = 1; //set void fraction to 1 to identify a superheated state
//{Equations are for charge calculation}
coolprop.update(input_pairs.HmassP_INPUTS, hri * 1000, pri * 1000);
double rho = coolprop.rhomass();
res_element.M = Vol_tubes * rho; //"Mass calculated"
}
// **********Twophase state**********"
if (hri <= h_v && hri >= h_l && fluid != "Water")
{
res_element = TPElement.ElementCalc1(fluid, l, Aa_fin, Aa_tube, A_r_cs, Ar, geo, tai, RHi, tri, pri, hri, mr, g, ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, coolprop, SourceTableData);
if (res_element.Pro < 0)
{
return(res_element);
}
//x=x_o "outlet quality of the element"
double x_avg = (res_element.x_i + res_element.x_o) / 2; //Average quality of the element
if (x_avg < 0) //"If negative, set quality to inlet value"
{
x_avg = res_element.x_i;
}
double T_avg = (tri + res_element.Tro) / 2; //Average temperature of the element
//Call VOIDFRACTION_charge(ref$,x_avg, T_avg, G_r, Dh: alpha) "Average void fraction of the element"
alpha = 1;
//{Equations are for charge calculation}
double P_avg = (pri + res_element.Pro) / 2; //Average pressure of the element
coolprop.update(input_pairs.PQ_INPUTS, P_avg * 1000, 0);
double rho_l = coolprop.rhomass();
//double rho_l = CoolProp.PropsSI("D", "P", P_avg * 1000, "Q", 0, fluid);
coolprop.update(input_pairs.PQ_INPUTS, P_avg * 1000, 1);
double rho_v = coolprop.rhomass();
//double rho_v = CoolProp.PropsSI("D", "P", P_avg * 1000, "Q", 1, fluid);
//{Call VOIDFRACTION_pressure(ref$, x_avg, P_avg : alpha_p) "Baroczy void fraction model" }
double alpha_homog = 1 / (1 + (1 - x_avg) / x_avg * (rho_v / rho_l)); // Homogeneous model, Intermittent flow void fraction
res_element.M = Vol_tubes * (alpha_homog * rho_v + (1 - alpha_homog) * rho_l); //Mass calculated
}
//**********Subcooled state**********
if (hri < h_l || fluid == "Water")
{
if (hri > 0.98 * h_l) //ignore modification for now, ruhao,20180226
{
Tri_mod = tri - 0.5 * 0; //"for Tri modification in the transition region"
}
else
{
Tri_mod = tri;
}
if (fluid == "Water")
{
Tri_mod = tri - 0.0001;
}
res_element = SPElement.ElementCalc3(fluid, l, Aa_fin, Aa_tube, A_r_cs, Ar, geo, tai, RHi, Tri_mod, pri, hri, mr, g, ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, coolprop, SourceTableData);
if (res_element.Pro < 0)
{
return(res_element);
}
//Call SUBCOOLED(ref$, Dh, L, A_a, A_r, Tai, Tri_mod, Pri, hri, m_r, G_r, m_a, h_air, eta_surface: Tro, Pro, hro, Tao, Q, h_ref, R_1, R_1a, R_1r, DELTAP, Vel_r )
res_element.x_i = (hri - h_l) / (h_v - h_l);
res_element.x_o = (res_element.hro - h_l) / (h_v - h_l);
//x=x_o "outlet quality of the element"
//{x=-1 "set quality to -100 to identify a subcooled state"}
alpha = -1; //set void fraction to -100 to identify a subcooled state
//{Equations are for charge calculation}
coolprop.update(input_pairs.HmassP_INPUTS, hri * 1000, pri * 1000);
double rho = coolprop.rhomass();
res_element.M = Vol_tubes * rho; //Mass calculated
}
return(res_element);
}
public static CalcResult SlabCalc(int[,] CirArrange, CircuitNumber CircuitInfo, int Nrow, int[] Ntube, int Nelement, string fluid, //double Npass, int[] N_tubes_pass,
double l, Geometry geo, double[, ,] ta, double[, ,] RH,
double te, double pe, double hri, double mr, double[,] ma, double[,] ha, double[,] haw,
double eta_surface, double zh, double zdp, int hexType, double thickness, double conductivity, double Pwater, string Airdirection, CapiliaryInput cap_inlet, CapiliaryInput cap_outlet, AbstractState coolprop, double[,] SourceTableData)
{
//------->
// R2 R1
// [11 1] <====
// [12 2] <====
// <==== Air
// [13 3] <====
// [14 4] <====
// [15 5] <====
// [16 6] <====
// [17 7] <====
// [18 8] <====
// [19 9] <====
// [20 10] <====
// Ncir=1, 11in, 20->10 1out
// [19 - 17 - 15 - 13 11 9 7 5 3 1] <====Air
// [20 - 18 - 16 - 14 12 10 8 6 4 2] <====Air
// Ncir=1, 20in, 20->19 1out
// CirArrange = new int[,] { { 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 10, 9, 8, 7, 6, 5, 4, 3, 2, 1 } };
// Nrow=2
// Ncir=2
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double[] Q1 = new double[50];
double tri = te; //Refrigerant.SATP(fluid, composition, pri, 1).Temperature - 273.15;
double pri = pe;
int Nciri = CircuitInfo.number[0];
int Nciro = CircuitInfo.number[1];
int Ncir = (Nciri == Nciro ? Nciri : Nciri + Nciro);
int N_tube = Ntube[0];
int N_tube_total = 0;
int iRow = 0;
int iTube_o = 0;
int iTube_n = 0;
int index_o = 0;
int index_n = 0;
double te_calc_org = 0;
CirArr[] cirArr = new CirArr[Nrow * N_tube];
CirArrforAir cirArrforAir = new CirArrforAir();
cirArrforAir = CirArrangement.ReadCirArr(CirArrange, CircuitInfo, Nrow, Ntube, 0);
cirArr = cirArrforAir.CirArr;
CalcResult res_slab = new CalcResult();
double[] pri_cir = new double[Ncir]; //[element, tube, row]
double[] hri_cir = new double[Ncir];
double[] tri_cir = new double[Ncir];
double[] mr_ciri = new double[Nciri];
List <double[]> mr_ciri_base = new List <double[]>();
double[] mr_ciro = new double[Nciro];
int[] Ngroupin = new int[Nciro];
int index = 0;
int restartDP_index = 0;
int N_tube2 = 0;
int[] index_cir = new int[Ncir];
int index_mr_ciri_base = 0;
CalcResult[] r = new CalcResult[Ncir];
CalcResult[] r1 = new CalcResult[Ncir];
CalcResult[] r2 = new CalcResult[Ncir]; //for NinMout only
CalcResult[] res_cir2 = new CalcResult[Nciro + 1];
CalcResult[] res_type = new CalcResult[Nciri + 1];
double[,] Q_detail = new double[N_tube, Nrow];//detail output
double[,] DP_detail = new double[N_tube, Nrow];
double[,] Tri_detail = new double[N_tube, Nrow];
double[,] Pri_detail = new double[N_tube, Nrow];
double[,] hri_detail = new double[N_tube, Nrow];
double[,] Tro_detail = new double[N_tube, Nrow];
double[,] Pro_detail = new double[N_tube, Nrow];
double[,] hro_detail = new double[N_tube, Nrow];
double[,] href_detail = new double[N_tube, Nrow];
double[,] mr_detail = new double[N_tube, Nrow];
double[,] charge_detail = new double[N_tube, Nrow];
int flag_ciro = 0;
int Ncir_forDP = 0;
double[] mr_forDP = new double[Nciri];
int k;
double te_calc = 0;
CheckAir airConverge = new CheckAir();
CheckDP dPconverge = new CheckDP();
CheckPri priconverge = new CheckPri();
for (int i = 0; i < Nrow; i++)
{
N_tube_total += Ntube[i];
}
for (int i = 0; i < Nciro; i++)
{
mr_ciro[i] = mr / Nciro;
}
bool index_outbig;
if (CircuitInfo.UnequalCir == null || CircuitInfo.UnequalCir[0] > 0)
{
index_outbig = false;
}
else
{
index_outbig = true;
}
if (CircuitInfo.UnequalCir != null)
{
for (int j = 0; j < Nciro; j++)
{
for (int i = 0; i < Ncir; i++)
{
if (CircuitInfo.UnequalCir[i] == Nciri + 1 + j)
{
Ngroupin[j]++;
}
}
//for (int i = 0; i < Nciri; i++) mr_ciri[i] = mr_ciro[j] / Ngroupin[j];
}
}
int iterforAir = 0;
int iterforDP = 0;
int iterforPri = 0;
double pri_1 = 0;
double pri_2 = 0;
double pri_3 = 0;
double pri_4 = 0;
double tri1 = 0;
double te1 = 0;
double iterforDP_ciri = 0;
double iterforDP_ciro = 0;
//Starting properties
iterforDP_ciro = 0;
double[] mr_forDP_o_4 = new double[Nciri];
double[] mr_forDP_o_3 = new double[Nciri];
double[] mr_forDP_o_2 = new double[Nciri];
double[] mr_forDP_o_1 = new double[Nciri];
do
{
#region //AirConverge
do
{
//iterforDP = 0;
r = new CalcResult[Ncir];
r1 = new CalcResult[Ncir];
res_cir2 = new CalcResult[Nciro + 1];
flag_ciro = (index_outbig ? 1 : 0);
//tri = tri;
//制冷制热模块计算切换
if (hexType == 0)
{
coolprop.update(input_pairs.PQ_INPUTS, pri * 1000, 0);
tri = coolprop.T() - 273.15;
tri = CoolProp.PropsSI("T", "P", pri * 1000, "Q", 0, fluid) - 273.15;
int a = 1;
}
else
{
coolprop.update(input_pairs.PQ_INPUTS, pri * 1000, 0);
te = coolprop.T() - 273.15;
te = CoolProp.PropsSI("T", "P", pri * 1000, "Q", 0, fluid) - 273.15;
int a = 1;
}
for (int j = 0; j < (flag_ciro == 1 ? (index_outbig ? Nciri + 1 : 1) : Nciro + 1); j++)
{
if (j >= Nciro)
{
j = j - Nciro; //for Nciro
flag_ciro = (index_outbig ? 0 : 1);
}
if (j == 1 && index_outbig && index == 0)
{
j = j - 1;
flag_ciro = 0;
}
index = 0;
iterforDP_ciri = 0;
double[] mr_forDP_4 = new double[Nciri];
double[] mr_forDP_3 = new double[Nciri];
double[] mr_forDP_2 = new double[Nciri];
double[] mr_forDP_1 = new double[Nciri];
double [] mr0_forDP = new double[5];
#region //DPConverge
do
{
res_type = new CalcResult[Nciri + 1];
k = 0;
if (!index_outbig)
{
for (int i = 0; i < (flag_ciro == 1 ? Nciro : (Nciri == Nciro ? Ncir : Ncir - Nciro)); i++)
{
if (flag_ciro == 1)
{
pri_cir[i + Ncir - Nciro] = res_cir2[i].Pro;
hri_cir[i + Ncir - Nciro] = res_cir2[i].hro;
tri_cir[i + Ncir - Nciro] = res_cir2[i].Tro;
}
else
{
pri_cir[i] = pri;
hri_cir[i] = hri;
tri_cir[i] = tri;
}
}
}
else
{
for (int i = 0; i < (flag_ciro == 1 ? Nciro : Ncir); i++)
{
if (flag_ciro == 1)
{
pri_cir[i] = pri;
hri_cir[i] = hri;
tri_cir[i] = tri;
}
else
{
if (CircuitInfo.UnequalCir[i] == Nciri + 1 + j)
{
pri_cir[i] = r2[j].Pro;
hri_cir[i] = r2[j].hro;
tri_cir[i] = r2[j].Tro;
}
}
}
}
for (int i = 0; i < Ncir; i++)
{
if (flag_ciro == 1)
{
//汇管计算
if (CircuitInfo.UnequalCir[i] <= 0)
{
//for (int i = 0; i < Ncir; i++)
//r[i] = Circuit.CircuitCalc(i, cirArr, CircuitInfo, Nrow, Ntube, Nelement, fluid, dh, l, geo.element, ta, RH,
// tri_cir[i], pri_cir[i], hri_cir[i], mr_ciro[k], ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, Airdirection, d_cap, lenth_cap);
r[i] = Circuit.CircuitCalc(i, cirArr, CircuitInfo, Nrow, Ntube, Nelement, fluid, l, geo, ta, RH,
tri_cir[i], pri_cir[i], hri_cir[i], mr_ciro[k], ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, cap_inlet, cap_outlet, coolprop, SourceTableData);
if (r[i].Pro < 0)
{
res_slab.Pro = -10000000; return(res_slab);
}
r1[k] = r[i].ShallowCopy();
r2[k] = r[i].ShallowCopy();
if (!index_outbig)
{
r1[k].DP += res_cir2[k].DP;
}
index_cir[k] = i;
k++;
Ncir_forDP = Nciro;
mr_forDP = (double[])mr_ciro.Clone(); // mr_forDP = mr_ciro
if (k == Nciro)
{
break;
}
}
}
else if (Nciri == Nciro || CircuitInfo.UnequalCir[i] == Nciri + 1 + j)
{
//均匀流路计算和不均匀流路开始部分（独立管）计算
if (index == 0)
{
if (Nciri == Nciro && iterforPri == 0)
{
mr_ciro.CopyTo(mr_ciri, 0);
}
else if (Nciri != Nciro)
{
if (restartDP_index == 1 || !priconverge.flag)
{
var mm = mr_ciri_base[j].Sum();
//foreach (var item in mr_ciri_base[j])
//mm += item;
mr_ciri[k] = mr_ciri_base[j][k] * mr_ciro[j] / mm;//(mr / Nciro);
}
else
{
mr_ciri[k] = mr_ciro[j] / Ngroupin[j];
}
}
}
//else mr_ciri_base.CopyTo(mr_ciri[k], 0);
//for (int i = 0; i < Ncir; i++)
//首次流路计算
if (CircuitInfo.CirType != null && CircuitInfo.CirType.flag == true)
{
bool circuit_cap = false;
//if (d_cap[index] == 0 && lenth_cap[index] == 0) circuit_cap = true;
if ((CircuitInfo.CirType.flag == true) && (CircuitInfo.CirType.type[i, 0] == 0) && (res_type[CircuitInfo.CirType.type[i, 1]] != null && circuit_cap))
{
//r[i] = res_type[CircuitInfo.CirType.type[i, 1]];
r[i] = new CalcResult();
r[i].DP = res_type[CircuitInfo.CirType.type[i, 1]].DP;
r[i].DP_cap = res_type[CircuitInfo.CirType.type[i, 1]].DP_cap;
r[i].href = res_type[CircuitInfo.CirType.type[i, 1]].href;
r[i].hro = res_type[CircuitInfo.CirType.type[i, 1]].hro;
r[i].M = res_type[CircuitInfo.CirType.type[i, 1]].M;
r[i].Pro = res_type[CircuitInfo.CirType.type[i, 1]].Pro;
r[i].Q = res_type[CircuitInfo.CirType.type[i, 1]].Q;
r[i].R_1 = res_type[CircuitInfo.CirType.type[i, 1]].R_1;
r[i].R_1a = res_type[CircuitInfo.CirType.type[i, 1]].R_1a;
r[i].R_1r = res_type[CircuitInfo.CirType.type[i, 1]].R_1r;
r[i].Ra_ratio = res_type[CircuitInfo.CirType.type[i, 1]].Ra_ratio;
r[i].RHout = res_type[CircuitInfo.CirType.type[i, 1]].RHout;
r[i].Tao = res_type[CircuitInfo.CirType.type[i, 1]].Tao;
r[i].Tri = res_type[CircuitInfo.CirType.type[i, 1]].Tri;
r[i].Tro = res_type[CircuitInfo.CirType.type[i, 1]].Tro;
r[i].x_i = res_type[CircuitInfo.CirType.type[i, 1]].x_i;
r[i].x_o = res_type[CircuitInfo.CirType.type[i, 1]].x_o;
r[i].Vel_r = res_type[CircuitInfo.CirType.type[i, 1]].Vel_r;
r[i].mr = res_type[CircuitInfo.CirType.type[i, 1]].mr;
r[i].Q_detail = new double[N_tube, Nrow];//
r[i].DP_detail = new double[N_tube, Nrow];
r[i].Tri_detail = new double[N_tube, Nrow];
r[i].Pri_detail = new double[N_tube, Nrow];
r[i].hri_detail = new double[N_tube, Nrow];
r[i].Tro_detail = new double[N_tube, Nrow];
r[i].Pro_detail = new double[N_tube, Nrow];
r[i].hro_detail = new double[N_tube, Nrow];
r[i].href_detail = new double[N_tube, Nrow];
r[i].mr_detail = new double[N_tube, Nrow];
r[i].Tao_Detail = new double[Nelement, N_tube, Nrow];
r[i].RHo_Detail = new double[Nelement, N_tube, Nrow];
r[i].charge_detail = new double[N_tube, Nrow];
for (int m = 0; m < CircuitInfo.TubeofCir[i]; m++)
{
index_o = 0;
index_n = 0;
if (i == 0)
{
index_n = 0;
}
else
{
for (int n = 1; n <= i; n++)
{
index_n += CircuitInfo.TubeofCir[n - 1];
}
}
if (res_type[CircuitInfo.CirType.type[i, 1]].index == 0)
{
index_o = 0;
}
else
{
for (int n = 1; n <= res_type[CircuitInfo.CirType.type[i, 1]].index; n++)
{
index_o += CircuitInfo.TubeofCir[n - 1];
}
}
iRow = cirArr[m + index_o].iRow;
iTube_o = cirArr[m + index_o].iTube;
iTube_n = cirArr[m + index_n].iTube;
r[i].Q_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].Q_detail[iTube_o, iRow];//
r[i].DP_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].DP_detail[iTube_o, iRow];
r[i].Tri_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].Tri_detail[iTube_o, iRow];
r[i].Pri_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].Pri_detail[iTube_o, iRow];
r[i].hri_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].hri_detail[iTube_o, iRow];
r[i].Tro_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].Tro_detail[iTube_o, iRow];
r[i].Pro_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].Pro_detail[iTube_o, iRow];
r[i].hro_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].hro_detail[iTube_o, iRow];
r[i].href_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].href_detail[iTube_o, iRow];
r[i].mr_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].mr_detail[iTube_o, iRow];
r[i].charge_detail[iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].charge_detail[iTube_o, iRow];
for (int p = 0; p < Nelement; p++)
{
//ta[p, iTube_n, iRow + 1] = res_type[CircuitInfo.CirType.type[i, 1]].Tao_Detail[p, iTube_o, iRow];
//RH[p, iTube_n, iRow + 1] = res_type[CircuitInfo.CirType.type[i, 1]].RHo_Detail[p, iTube_o, iRow];
r[i].Tao_Detail[p, iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].Tao_Detail[p, iTube_o, iRow];
r[i].RHo_Detail[p, iTube_n, iRow] = res_type[CircuitInfo.CirType.type[i, 1]].RHo_Detail[p, iTube_o, iRow];
}
}
//r[i].Tao_Detail = ta;
//r[i].RHo_Detail = RH;
}
else
{
//r[i] = Circuit.CircuitCalc(i, cirArr, CircuitInfo, Nrow, Ntube, Nelement, fluid, dh, l, geo.element, ta, RH,
//tri_cir[i], pri_cir[i], hri_cir[i], mr_ciri[k], ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, Airdirection, d_cap, lenth_cap);
r[i] = Circuit.CircuitCalc(i, cirArr, CircuitInfo, Nrow, Ntube, Nelement, fluid, l, geo, ta, RH,
tri_cir[i], pri_cir[i], hri_cir[i], mr_ciri[k], ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, cap_inlet, cap_outlet, coolprop, SourceTableData);
if (r[i].Pro < 0)
{
res_slab.Pro = -10000000; return(res_slab);
}
if (CircuitInfo.CirType.type[i, 0] == 0)
{
res_type[CircuitInfo.CirType.type[i, 1]] = r[i];
res_type[CircuitInfo.CirType.type[i, 1]].index = i;
}
}
}
else
{
//r[i] = Circuit.CircuitCalc(i, cirArr, CircuitInfo, Nrow, Ntube, Nelement, fluid, dh, l, geo.element, ta, RH,
//tri_cir[i], pri_cir[i], hri_cir[i], mr_ciri[k], ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, Airdirection, d_cap, lenth_cap);
r[i] = Circuit.CircuitCalc(i, cirArr, CircuitInfo, Nrow, Ntube, Nelement, fluid, l, geo, ta, RH,
tri_cir[i], pri_cir[i], hri_cir[i], mr_ciri[k], ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, cap_inlet, cap_outlet, coolprop, SourceTableData);
if (r[i].Pro < 0)
{
res_slab.Pro = -10000000; return(res_slab);
}
}
r1[k] = r[i].ShallowCopy();
index_cir[k] = i;//不均匀流路的输出才会用到
k++;
if (k == (Nciri == Nciro ? Ncir : Ngroupin[j]))
{
Ncir_forDP = (Nciri == Nciro ? Ncir : Ngroupin[j]);
mr_forDP = (double[])mr_ciri.Clone();
break;
}
}
}
if (index_outbig && flag_ciro == 1)
{
break;
}
index++;
//dPconverge = CheckDPforCircuits.CheckDPConverge(mr, mr_ciri, r, Ncir);
dPconverge = CheckDPforCircuits.CheckDPConverge(hexType, res_cir2, iterforPri, flag_ciro, mr_forDP, r1, Ncir_forDP);
if (flag_ciro == 0)
{
iterforDP_ciri++;
if (iterforDP_ciri >= 5)
{
mr_forDP_4 = mr_forDP_3;
mr_forDP_3 = mr_forDP_2;
mr_forDP_2 = mr_forDP_1;
mr_forDP_1 = mr_forDP;
try
{
if (mr_forDP_1[0] < mr_forDP_2[0] && (Math.Abs(mr_forDP_1[0] - mr_forDP_3[0]) / mr_forDP_1[0] < 0.0001) ||
Math.Abs(mr_forDP_1[0] - mr_forDP_4[0]) / mr_forDP_1[0] < 0.0001)
{
dPconverge.flag = true;
}
}
catch (Exception ex)
{
continue;
}
}
restartDP_index = 0;
if (!dPconverge.flag)
{
dPconverge.mr.CopyTo(mr_ciri, 0); //mr_ciri = dPconverge.mr;
}
}
else //(flag_ciro == 1)
{
iterforDP_ciro++;
if (iterforDP_ciro >= 5)
{
mr_forDP_o_4 = mr_forDP_o_3;
mr_forDP_o_3 = mr_forDP_o_2;
mr_forDP_o_2 = mr_forDP_o_1;
mr_forDP_o_1 = mr_forDP;
try
{
if (mr_forDP_o_1[0] < mr_forDP_o_2[0] && (Math.Abs(mr_forDP_o_1[0] - mr_forDP_o_3[0]) / mr_forDP_o_1[0] < 0.0001) ||
Math.Abs(mr_forDP_o_1[0] - mr_forDP_o_4[0]) / mr_forDP_o_1[0] < 0.0001)
{
dPconverge.flag = true;
}
}
catch (Exception ex)
{
continue;
}
}
if (dPconverge.flag)
{
restartDP_index = 0;
}
else
{
restartDP_index = 1;
dPconverge.mr.CopyTo(mr_ciro, 0); //mr_ciro = dPconverge.mr;
break;
}
}
iterforDP++;
N_tube2 = 0;
#region //Result print out
if (dPconverge.flag)
{
if (Nciri == Nciro)
{
//te_calc = Refrigerant.SATP(fluid, composition, r[j].Pro, 1).Temperature;
coolprop.update(input_pairs.PQ_INPUTS, r[j].Pro * 1000, 0);
te_calc = coolprop.T();
te_calc = CoolProp.PropsSI("T", "P", r[j].Pro * 1000, "Q", 0, fluid);
int a = 1;
}
else
{
if (mr_ciri_base.Count == Nciro && flag_ciro == 0)
{
mr_ciri_base.RemoveAt(index_mr_ciri_base);
mr_ciri_base.Insert(index_mr_ciri_base, mr_forDP);
index_mr_ciri_base++;
index_mr_ciri_base %= mr_ciri_base.Count;
}
if (mr_ciri_base.Count < Nciro)
{
mr_ciri_base.Add(mr_forDP); //keep original mr ratio for fast iter
}
j = (flag_ciro == 1 ? j + Nciro : j);
res_cir2[j] = new CalcResult();
for (int i = 0; i < (flag_ciro == 1 ? Nciro : Ngroupin[j]); i++)
{
res_cir2[j].Q += r1[i].Q;
res_cir2[j].M += r1[i].M;
res_cir2[j].hro += (flag_ciro == 1 ? mr_ciro[i] : mr_ciri[i]) * r1[i].hro;
if (fluid == "Water")
{
res_cir2[j].Tro += (flag_ciro == 1 ? mr_ciro[i] : mr_ciri[i]) * r1[i].Tro;
}
res_cir2[j].Vel_r = r1[i].Vel_r;
res_cir2[j].href += r1[i].href * CircuitInfo.TubeofCir[index_cir[i]];
res_cir2[j].R_1 += r1[i].R_1 * CircuitInfo.TubeofCir[index_cir[i]];
res_cir2[j].R_1a += r1[i].R_1a * CircuitInfo.TubeofCir[index_cir[i]];
res_cir2[j].R_1r += r1[i].R_1r * CircuitInfo.TubeofCir[index_cir[i]];
N_tube2 += CircuitInfo.TubeofCir[index_cir[i]];
}
res_cir2[j].DP = r1[(flag_ciro == 1 ? Nciro : Ngroupin[j]) - 1].DP;
res_cir2[j].Tao_Detail = ta;
res_cir2[j].Pro = r1[(flag_ciro == 1 ? Nciro : Ngroupin[j]) - 1].Pro;
res_cir2[j].hro = res_cir2[j].hro / (flag_ciro == 1 ? mr : mr_ciro[j]);
res_cir2[j].href = res_cir2[j].href / N_tube2;
res_cir2[j].R_1 = res_cir2[j].R_1 / N_tube2;
res_cir2[j].R_1a = res_cir2[j].R_1a / N_tube2;
res_cir2[j].R_1r = res_cir2[j].R_1r / N_tube2;
res_cir2[j].Tri = tri;
//te_calc = Refrigerant.SATP(fluid, composition, res_cir2[j].Pro, 1).Temperature;
coolprop.update(input_pairs.PQ_INPUTS, res_cir2[j].Pro * 1000, 0);
te_calc = coolprop.T();
te_calc = CoolProp.PropsSI("T", "P", res_cir2[j].Pro * 1000, "Q", 0, fluid);
if (fluid == "Water")
{
res_cir2[j].Tro = res_cir2[j].Tro / (flag_ciro == 1 ? mr : mr_ciro[j]) - 273.15;
}
else
{
res_cir2[j].Tro = CoolProp.PropsSI("T", "P", res_cir2[j].Pro * 1000, "H", res_cir2[j].hro * 1000, fluid) - 273.15;
}
}
}
#endregion
#endregion
} while (!dPconverge.flag && iterforDP < 200);
if (Nciri == Nciro)
{
break;
}
if (index_outbig && (j == Nciro - 1) && (res_cir2[0] != null))
{
for (int i = 0; i < Nciro; i++)
{
r2[i].DP += res_cir2[i].DP;
}
flag_ciro = 1;
Ncir_forDP = Nciro;
mr_forDP = (double[])mr_ciro.Clone(); // mr_forDP = mr_ciro
dPconverge = CheckDPforCircuits.CheckDPConverge(hexType, res_cir2, iterforPri, flag_ciro, mr_forDP, r2, Ncir_forDP);
iterforDP_ciro++;
if (iterforDP_ciro >= 5)
{
mr_forDP_o_4 = mr_forDP_o_3;
mr_forDP_o_3 = mr_forDP_o_2;
mr_forDP_o_2 = mr_forDP_o_1;
mr_forDP_o_1 = mr_forDP;
try
{
if (mr_forDP_o_1[0] < mr_forDP_o_2[0] && (Math.Abs(mr_forDP_o_1[0] - mr_forDP_o_3[0]) / mr_forDP_o_1[0] < 0.0001) ||
Math.Abs(mr_forDP_o_1[0] - mr_forDP_o_4[0]) / mr_forDP_o_1[0] < 0.0001)
{
dPconverge.flag = true;
}
}
catch (Exception ex)
{
continue;
}
}
if (!dPconverge.flag)
{
restartDP_index = 1;
dPconverge.mr.CopyTo(mr_ciro, 0); //mr_ciro = dPconverge.mr;
}
break;
}
}
if (Airdirection == "顺流")
{
airConverge.flag = true;
for (int ii = 0; ii < Ncir; ii++)
{
for (int i = 0; i < Nrow; i++)
{
for (int j = 0; j < N_tube; j++)
{
for (int kk = 0; kk < Nelement; kk++)
{
if (r[ii].Tao_Detail[kk, j, i] != 0)
{
ta[kk, j, i + 1] = r[ii].Tao_Detail[kk, j, i];
}
if (r[ii].RHo_Detail[kk, j, i] != 0)
{
RH[kk, j, i + 1] = r[ii].RHo_Detail[kk, j, i];
}
}
}
}
}
}
else//Counter
{
airConverge = CheckAirConvergeforCircuits.CheckAirConverge(cirArrforAir.TotalDirection, Nrow, N_tube, Nelement, ta, RH, r); //taout_calc, RHout_calc
ta = airConverge.ta;
RH = airConverge.RH;
iterforAir++;
}
//Add Q converge criterion to avoid results oscillation, ruhao 20180426
if (Airdirection != "顺流") //No airConverge iter for Parallel
{
for (int i = 0; i < Ncir; i++)
{
Q1[iterforAir - 1] += r[i].Q;
}
try
{
if (Q1[iterforAir - 1] < Q1[iterforAir - 2] && (Math.Abs(Q1[iterforAir - 1] - Q1[iterforAir - 3]) / Q1[iterforAir - 1] < 0.0001) ||
Math.Abs(Q1[iterforAir - 1] - Q1[iterforAir - 4]) / Q1[iterforAir - 1] < 0.0001)
{
airConverge.flag = true;
}
}
catch (Exception ex)
{
continue;
}
}
} while (!airConverge.flag && iterforAir < 50);
#endregion
//using (StreamWriter wr = File.AppendText(@"D:\Work\Simulation\Test\MinNout.txt"))
//{
//for (int i = 0; i < Ncir; i++)
//{
//wr.WriteLine("Q, {0}, DP, {1}, href, {2}, Ra_ratio, {3}, Tao, {4}, Tro, {5}, mr, {6}", r[i].Q, r[i].DP, r[i].href, r[i].Ra_ratio, r[i].Tao, r[i].Tro, r[i].mr);
//}
//}
if (restartDP_index == 1)
{
priconverge.flag = false;
}
else if (hexType == 0 && (fluid != "Water"))
{
priconverge = CheckPin.CheckPriConverge(te, te_calc - 273.15, te_calc_org - 273.15, pri, pe, r[Ncir - 1].Pro); //res_slab.Pro
iterforPri++;
if (iterforPri >= 20)
{
pri_4 = pri_3;
pri_3 = pri_2;
pri_2 = pri_1;
pri_1 = pri;
try
{
if (pri_1 < pri_2 && (Math.Abs(pri_1 - pri_3) / pri_1 < 1e-5) ||
Math.Abs(pri_1 - pri_4) / pri_1 < 1e-5)
{
priconverge.flag = true;
}
}
catch (Exception ex)
{
continue;
}
}
pri = priconverge.pri;
te_calc_org = te_calc;
if (priconverge.flag && iterforPri == 1 && iterforDP == 1)
{
priconverge.flag = false; //to avoid not even iterate but converge by chance
}
}
else
{
priconverge.flag = true;
}
} while (!priconverge.flag && iterforPri < 100);
// if (iterforDP >= 200)
//{
// return res_slab;
// throw new Exception("iter for DPConverge > 100.");
//}
//if (iterforPri >= 50)
//{
// return res_slab;
// throw new Exception("iter for Pri > 50.");
//}
#region //Result print out
for (int i = 0; i < Ncir; i++)
{
res_slab.Q += r[i].Q;
res_slab.M += r[i].M;
if (Nciri == Nciro)
{
res_slab.hro += mr_ciri[i] * r[i].hro;
}
res_slab.href += r[i].href * CircuitInfo.TubeofCir[i];
res_slab.R_1 += r[i].R_1 * CircuitInfo.TubeofCir[i];
res_slab.R_1a += r[i].R_1a * CircuitInfo.TubeofCir[i];
res_slab.R_1r += r[i].R_1r * CircuitInfo.TubeofCir[i];
for (int j = 0; j < N_tube; j++)//detail output
{
for (k = 0; k < Nrow; k++)
{
if (r[i].Q_detail[j, k] != 0)
{
Q_detail[j, k] = r[i].Q_detail[j, k];
}
if (r[i].DP_detail[j, k] != 0)
{
DP_detail[j, k] = r[i].DP_detail[j, k];
}
if (r[i].Tri_detail[j, k] != 0)
{
Tri_detail[j, k] = r[i].Tri_detail[j, k];
}
if (r[i].Pri_detail[j, k] != 0)
{
Pri_detail[j, k] = r[i].Pri_detail[j, k];
}
if (r[i].hri_detail[j, k] != 0)
{
hri_detail[j, k] = r[i].hri_detail[j, k];
}
if (r[i].Tro_detail[j, k] != 0)
{
Tro_detail[j, k] = r[i].Tro_detail[j, k];
}
if (r[i].Pro_detail[j, k] != 0)
{
Pro_detail[j, k] = r[i].Pro_detail[j, k]; //
}
if (r[i].hro_detail[j, k] != 0)
{
hro_detail[j, k] = r[i].hro_detail[j, k];
}
if (r[i].href_detail[j, k] != 0)
{
href_detail[j, k] = r[i].href_detail[j, k];
}
if (r[i].mr_detail[j, k] != 0)
{
mr_detail[j, k] = r[i].mr_detail[j, k];
}
if (r[i].charge_detail[j, k] != 0)
{
charge_detail[j, k] = r[i].charge_detail[j, k];
}
}
}
}
if (Nciri == Nciro)
{
res_slab.hro = res_slab.hro / mr;
res_slab.Pro = r[Ncir - 1].Pro;
res_slab.DP_cap = r[Ncir - 1].DP_cap;
res_slab.Vel_r = r[Ncir - 1].Vel_r;
}
else if (!index_outbig)
{
res_slab.hro = res_cir2[Nciro].hro;
res_slab.Pro = res_cir2[Nciro].Pro;
res_slab.DP_cap = res_cir2[Nciro].DP_cap;
res_slab.Vel_r = res_cir2[Nciro].Vel_r;
}
else
{
res_slab.hro = res_cir2[Nciro - 1].hro;
res_slab.Pro = res_cir2[Nciro - 1].Pro;
res_slab.DP_cap = res_cir2[Nciro - 1].DP_cap;
res_slab.Vel_r = res_cir2[Nciro - 1].Vel_r;
}
res_slab.Pri = pri;
res_slab.Tri = tri;
res_slab.hri = hri;
res_slab.mr = mr;
res_slab.DP = pri - res_slab.Pro;
res_slab.Tao_Detail = ta;
res_slab.RHo_Detail = RH;
res_slab.href = res_slab.href / N_tube_total;
for (int i = 0; i < ha.GetLength(0); i++)
{
for (int j = 0; j < ha.GetLength(1); j++)
{
res_slab.ha += ha[i, j];
}
}
res_slab.ha = res_slab.ha / ha.Length;
res_slab.R_1 = res_slab.R_1 / N_tube_total;
res_slab.R_1a = res_slab.R_1a / N_tube_total;
res_slab.R_1r = res_slab.R_1r / N_tube_total;
coolprop.update(input_pairs.PQ_INPUTS, res_slab.Pro * 1000, 0);
te_calc = coolprop.T() - 273.15;
te_calc = CoolProp.PropsSI("T", "P", res_slab.Pro * 1000, "Q", 0, fluid) - 273.15;
coolprop.update(input_pairs.QT_INPUTS, 0, te_calc + 273.15);
double densityLo = coolprop.rhomass();
//double densityLo = CoolProp.PropsSI("D", "T", te_calc + 273.15, "Q", 0, fluid);
coolprop.update(input_pairs.QT_INPUTS, 1, te_calc + 273.15);
double densityVo = coolprop.rhomass();
//double densityVo = CoolProp.PropsSI("D", "T", te_calc + 273.15, "Q", 1, fluid);
coolprop.update(input_pairs.DmassT_INPUTS, densityLo, te_calc + 273.15);
double hlo = coolprop.hmass() / 1000;
//double hlo = CoolProp.PropsSI("H", "T", te_calc + 273.15, "D", densityLo, fluid) / 1000 ;
coolprop.update(input_pairs.DmassT_INPUTS, densityVo, te_calc + 273.15);
double hvo = coolprop.hmass() / 1000;
//double hvo = CoolProp.PropsSI("H", "T", te_calc + 273.15, "D", densityVo, fluid) / 1000 ;
res_slab.x_o = (res_slab.hro - hlo) / (hvo - hlo);
coolprop.update(input_pairs.PQ_INPUTS, pri * 1000, 0);
double hli = coolprop.hmass() / 1000;
//double hli = CoolProp.PropsSI("H", "P", pri * 1000, "Q", 0, fluid) / 1000 ;
coolprop.update(input_pairs.PQ_INPUTS, pri * 1000, 1);
double hvi = coolprop.hmass() / 1000;
//double hvi = CoolProp.PropsSI("H", "P", pri * 1000, "Q", 1, fluid) / 1000 ;
res_slab.x_i = (res_slab.hri - hli) / (hvi - hli);
coolprop.update(input_pairs.HmassP_INPUTS, res_slab.hro * 1000, res_slab.Pro * 1000);
res_slab.Tro = coolprop.T() - 273.15;
//res_slab.Tro = CoolProp.PropsSI("T", "P", res_slab.Pro * 1000, "H", res_slab.hro * 1000, fluid) - 273.15;
double h = res_slab.hro;
for (int j = 0; j < N_tube; j++)
{
for (int i = 0; i < Nelement; i++)
{
res_slab.Tao += res_slab.Tao_Detail[i, j, Nrow];
res_slab.RHout += res_slab.RHo_Detail[i, j, Nrow];
}
}
res_slab.Tao = res_slab.Tao / (N_tube * Nelement);
res_slab.RHout = res_slab.RHout / (N_tube * Nelement);
res_slab.Ra_ratio = res_slab.R_1a / res_slab.R_1;
for (int i = 0; i < ma.GetLength(0); i++)
{
for (int j = 0; j < ma.GetLength(1); j++)
{
res_slab.ma += ma[i, j];
}
}
res_slab.Va = res_slab.ma / 1.2 * 3600;
res_slab.Q_detail = Q_detail;//detail output
res_slab.DP_detail = DP_detail;
res_slab.Tri_detail = Tri_detail;
res_slab.Pri_detail = Pri_detail;
res_slab.hri_detail = hri_detail;
res_slab.Tro_detail = Tro_detail;
res_slab.Pro_detail = Pro_detail;
res_slab.hro_detail = hro_detail;
res_slab.href_detail = href_detail;
res_slab.mr_detail = mr_detail;
res_slab.Aa = geo.TotalArea.A_a;
res_slab.Ar = geo.TotalArea.A_r;
res_slab.AHx = geo.TotalArea.A_hx;
res_slab.N_row = Nrow;
res_slab.tube_row = N_tube;
res_slab.charge_detail = charge_detail;
return(res_slab);
#endregion
}
public static CalcResult ElementCalc3(string fluid, double l, double Aa_fin, double Aa_tube, double A_r_cs, double Ar, Geometry geo, double tai,
double RHi, double tri, double pri, double hri, double mr, double g, double ma, double ha, double haw,
double eta_surface, double zh, double zdp, int hexType, double thickness, double conductivity, double Pwater, AbstractState coolprop, double[,] SourceTableData)
{
Model.HumidAirProp humidairprop = new Model.HumidAirProp();
RHi = RHi > 1 ? 1 : RHi;
double dh = geo.Di;
double Q = 0;
double Tout_a = 0;
double Q_sensible = 0;
double r_metal = thickness / conductivity / Ar;
CalcResult res = new CalcResult();
coolprop.update(input_pairs.HmassP_INPUTS, hri * 1000, (fluid == "Water" ? Pwater : pri) * 1000);
double mu_r = coolprop.viscosity();
//double mu_r = CoolProp.PropsSI("V", "H", hri * 1000, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double k_r = coolprop.conductivity();
//double k_r = CoolProp.PropsSI("L", "H", hri * 1000, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double rho_r = coolprop.rhomass();
//double rho_r = CoolProp.PropsSI("D", "H", hri * 1000, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double cp_r = coolprop.cpmass();
//double cp_r = CoolProp.PropsSI("C", "H", hri * 1000, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double Pr_r = cp_r * mu_r / k_r;
res.Vel_r = g / rho_r;
double Re_r = rho_r * res.Vel_r * dh / mu_r;
double fh = RefrigerantSPHTC.ff_CHURCHILL(Re_r);
double Nusselt = RefrigerantSPHTC.NU_GNIELINSKI(Re_r, Pr_r, fh);
res.href = Nusselt * k_r / dh * zh;
double cp_da = 1.0;
cp_da = (hexType == 0 ? 1.027 : 1.02) * 1000;
double Tin_a = tai;
double Tin_r = tri;
//double cp_da0 = CoolProp.HAPropsSI("C", "T", Tin_a + 273.15, "P", 101325, "R", RHi);
//cp_da = 1005.1458551 + 0.1541627 * Tin_a + 4.3454442 * RHi - 0.0090904 * Math.Pow(Tin_a, 2) - 0.3409659 * Math.Pow(RHi, 2) - 0.0007819 * Tin_a * RHi + 0.0001851 * Math.Pow(Tin_a, 3) + 0.0049274 * Math.Pow(RHi, 3) + 0.0476513 * Tin_a * Math.Pow(RHi, 2) + 0.020268209 * Math.Pow(Tin_a, 2) * RHi;
cp_da = humidairprop.Cp(Tin_a, RHi, SourceTableData);
double h_r = res.href;
double k_fin = 237;
double Fthickness = geo.Fthickness;
double Pt = geo.Pt;
double Pr = geo.Pr;
double Do = geo.Do;
//double h_fin = (Pt - Do) / 2;
//double dc = Do + 2 * Fthickness;
//double df = Math.Pow(4 / Math.PI * Pt * Pr, 0.5);
//double eta_a = 1 / (1 + ha * Math.Pow(df - dc, 2) * Math.Pow(df, 0.5) / 6 / Fthickness / k_fin / Math.Pow(dc, 0.5));
//double m = Math.Sqrt(2 * ha / (k_fin * Fthickness));
//double eta_a= Math.Tanh(m * h_fin) / (m * h_fin);// may cause error
//double eta_dry = eta_surface;
double r_eta = Do / 2;
double XD = Math.Pow((Pr * Pr + Pt * Pt / 4), 0.5) / 2;
double XT = Pt / 2;
double rf_r = 1.27 * XT / r_eta * Math.Pow((XD / XT - 0.3), 0.5);
double m = Math.Pow((2 * ha / k_fin / Fthickness), 0.5);
double fai = (rf_r - 1) * (1 + (0.3 + Math.Pow((m * r_eta * (rf_r - r_eta) / 2.5), (1.5 - 1 / 12 * rf_r)) * (0.26 * Math.Pow(rf_r, 0.3) - 0.3)) * Math.Log(rf_r));
double eta_0 = Math.Tanh(m * r_eta * fai) / m / r_eta / fai * Math.Cos(0.1 * m * r_eta * fai);
double eta_a = (eta_0 * Aa_fin + Aa_tube) / (Aa_fin + Aa_tube);
double UA_i = h_r * Ar;
double UA_o = eta_a * (Aa_fin + Aa_tube) * ha;
double Ntu_i = UA_i / (mr * cp_r);
double Ntu_o = UA_o / (ma * cp_da);
double UA = 1 / (1 / (UA_i) + 1 / (UA_o) + r_metal);
double Cmin = Math.Min(cp_r * mr, cp_da * ma);
double Cmax = Math.Max(cp_r * mr, cp_da * ma);
double C_star = Cmin / Cmax;
double Ntu_dry = UA / Cmin;
double epsilon_dry = (1 - Math.Exp(-Ntu_dry * (1 - C_star))) / (1 - C_star * Math.Exp(-Ntu_dry * (1 - C_star)));
double Q_dry = epsilon_dry * Cmin * (Tin_a - Tin_r) * Math.Pow(-1, hexType);//need to be modified//所以蒸发器算不出Q
double Tout_a_dry = Tin_a - Q_dry / (ma * cp_da) * Math.Pow(-1, hexType);
double Tout_r = Tin_r + Q_dry / (mr * cp_r) * Math.Pow(-1, hexType);
double Tout_s = (UA_o * Tout_a_dry + UA_i * Tin_r) / (UA_o + UA_i);
double Tin_s = (UA_o * Tin_a + UA_i * Tout_r) / (UA_o + UA_i);
double Tout_r_dry = Tout_r;
double f_dry = 1.0;
//double omega_in0 = CoolProp.HAPropsSI("W", "T", Tin_a + 273.15, "P", 101325, "R", RHi);
//double omega_in = (-0.0682340 + 0.0292341 * Tin_a + 4.1604535 * RHi - 0.0025985 * Math.Pow(Tin_a, 2) - 0.0769009 * Math.Pow(RHi, 2) + 0.1246489 * Tin_a * RHi + 6.008 * Math.Pow(10, -5) * Math.Pow(Tin_a, 3) - 0.0006775 * Math.Pow(RHi, 3) + 0.0267183 * Tin_a * Math.Pow(RHi, 2) + 0.019904969 * Math.Pow(Tin_a, 2) * RHi) / 1000;
double omega_in = humidairprop.O(Tin_a, RHi, SourceTableData);
//double omega_out = omega_in;
double hin_a = 0;
if (hexType == 0 && tri < tai)
{
bool isFullyWet = true;
//double hin_a0 = CoolProp.HAPropsSI("H", "T", Tin_a + 273.15, "P", 101325, "R", RHi);
//hin_a = -244.2924077 + 1135.8711 * Tin_a + 10101.404 * RHi - 12.968219 * Math.Pow(Tin_a, 2) - 11.356807 * Math.Pow(RHi, 2) + 357.25464 * Tin_a * RHi + 0.3178346 * Math.Pow(Tin_a, 3) - 0.0024329 * Math.Pow(RHi, 3) + 44.100799 * Tin_a * Math.Pow(RHi, 2) + 50.31444812 * Math.Pow(Tin_a, 2) * RHi;
hin_a = humidairprop.H(Tin_a, "R", RHi, SourceTableData);
double hout_a = hin_a - Q_dry / ma * Math.Pow(-1, hexType);
//double Tdp0 = CoolProp.HAPropsSI("D", "T", Tin_a + 273.15, "P", 101325, "R", RHi) - 273.15;
//double Tdp = -273.15 + 241.0212518 + 0.5718833 * tai + 84.99553 * RHi + 0.002691 * Math.Pow(tai, 2) - 95.003186 * Math.Pow(RHi, 2) + 0.7135779 * tai * RHi - 2.691 / Math.Pow(10, 5) * Math.Pow(tai, 3) + 42.58183 * Math.Pow(RHi, 3) - 0.3227474 * tai * Math.Pow(RHi, 2) - 0.000884612 * Math.Pow(tai, 2) * RHi;
double Tdp = humidairprop.Tdp(Tin_a, RHi, SourceTableData);
//***delete***//
//res.RHout = CoolProp.HAPropsSI("R", "T", Tout_a_dry + 273.15, "P", 101325, "W", omega_out);
//res.RHout = 0.0215344 - 0.0059467 * Tout_a_dry + 0.2386894 * (omega_out * 1000) + 0.0004378 * Math.Pow(Tout_a_dry, 2) + 0.0004635 * Math.Pow((omega_out * 1000), 2) - 0.0125912 * Tout_a_dry * (omega_out * 1000) - 9.134 * Math.Pow(10, -6) * Math.Pow(Tout_a_dry, 3) + 1.696 * Math.Pow(10, -6) * Math.Pow((omega_out * 1000), 3) - 2.214 * Math.Pow(10, -5) * Tout_a_dry * Math.Pow((omega_out * 1000), 2) + 0.000200865 * Math.Pow(Tout_a_dry, 2) * (omega_out * 1000);
//***delete***//
//res.RHout = CoolProp.HAPropsSI("R", "T", Tout_a_dry + 273.15, "P", 101325, "H", hout_a);
//double resRHout0 = CoolProp.HAPropsSI("R", "T", Tout_a_dry + 273.15, "P", 101325, "H", hout_a);
//res.RHout = 0.0259124 - 0.0996818 * Tout_a_dry + 0.0934877 * (hout_a / 1000) + 0.0040018 * Math.Pow(Tout_a_dry, 2) - 0.0003662 * Math.Pow((hout_a / 1000), 2) - 0.0034077 * Tout_a_dry * (hout_a / 1000) - 1.76447 * Math.Pow(10, -5) * Math.Pow(Tout_a_dry, 3) - 2.74524 * Math.Pow(10, -6) * Math.Pow((hout_a / 1000), 3) + 2.99291 * Math.Pow(10, -5) * Tout_a_dry * Math.Pow((hout_a / 1000), 2) - 9.56644 * Math.Pow(10, -6) * Math.Pow(Tout_a_dry, 2) * (hout_a / 1000);
//double Tdp_out0 = CoolProp.HAPropsSI("T", "H", hout_a, "P", 101325, "R", 1.0) - 273.15;//@@@@@@@@@@@@@@@@@@@@@@@@@@
double Tdp_out = humidairprop.Ts(hout_a / 1000, SourceTableData);
res.RHout = humidairprop.RHI(Tout_a_dry, Tdp_out, SourceTableData);
Tout_a = Tout_a_dry;
Q = Q_dry;
if (Tin_s < Tdp)
{
isFullyWet = true;
}
else
{
isFullyWet = false;
}
if (Tout_s < Tdp | isFullyWet == true)
{
double x1 = Tin_r + 0.001;
double x2 = Tin_a - 0.001;
double eps = 1e-8;
int iter = 1;
double change = 999;
double y1 = 0, y2 = 0, x3 = 0;
double m_star = 0, epsilon_wet = 0, h_s_w_i = 0, h_s_w_o = 0, h_s_s_e = 0, T_s_e = 0, h_a_x = 0, T_a_x = 0;
double Q_wet = 0, Ntu_owet = 0, mdot_min = 0;
double Ntu_wet = 0;
while ((iter <= 3 | change > eps) && iter < 100)
{
if (iter == 1)
{
Tout_r = x1;
}
if (iter > 1)
{
Tout_r = x2;
}
double Tout_r_start = Tout_r;
//double h_s_w_i0 = CoolProp.HAPropsSI("H", "T", Tin_r + 273.15, "P", 101325, "R", 1.0);
//h_s_w_i = 58.732687 * Math.Pow(Tin_r + 273.15, 2) - 30921.970577 * (Tin_r + 273.15) + 4075493.951473;
h_s_w_i = humidairprop.H(Tin_r, "R", 1, SourceTableData);
///////
//double h10 = 58.732687 * Math.Pow((Tin_r + Tout_r) / 2 + 273.15 + 0.01, 2) - 30921.970577 * ((Tin_r + Tout_r) / 2 + 273.15 + 0.01) + 4075493.951473;
double h1 = humidairprop.H((Tin_r + Tout_r) / 2 + 0.01, "R", 1, SourceTableData);
//double h20 = 58.732687 * Math.Pow((Tin_r + Tout_r) / 2 + 273.15, 2) - 30921.970577 * ((Tin_r + Tout_r) / 2 + 273.15 ) + 4075493.951473;
double h2 = humidairprop.H((Tin_r + Tout_r) / 2, "R", 1, SourceTableData);
double c_s = (h1 - h2) / 0.01;
//double c_s = (CoolProp.HAPropsSI("H", "T", (Tin_r + Tout_r) / 2 + 273.15 + 0.01, "P", 101325, "R", 1) - CoolProp.HAPropsSI("H", "T", (Tin_r + Tout_r) / 2 + 273.15, "P", 101325, "R", 1)) / 0.01;
//double c_s = 2500;
//m = Math.Sqrt(2 * ha*c_s/cp_da / (k_fin * Fthickness));
//eta_a= Math.Tanh(m * h_fin) / (m * h_fin);// may cause error
//double m_star=ma/(mr*(cp_r/c_s));
//eta_a = eta_a * c_s / cp_da;
m = Math.Pow((2 * haw / k_fin / Fthickness), 0.5);
fai = (rf_r - 1) * (1 + (0.3 + Math.Pow((m * r_eta * (rf_r - r_eta) / 2.5), (1.5 - 1 / 12 * rf_r)) * (0.26 * Math.Pow(rf_r, 0.3) - 0.3)) * Math.Log(rf_r));
eta_0 = Math.Tanh(m * r_eta * fai) / m / r_eta / fai * Math.Cos(0.1 * m * r_eta * fai);
double eta_wet = (eta_0 * Aa_fin + Aa_tube) / (Aa_fin + Aa_tube);
Ntu_owet = (eta_0 * Aa_fin + Aa_tube) * haw / (ma * cp_da);//zzc
m_star = Math.Min(cp_r * mr / c_s, ma) / Math.Max(cp_r * mr / c_s, ma);
mdot_min = Math.Min(cp_r * mr / c_s, ma);
Ntu_wet = Ntu_owet / (1 + m_star * (Ntu_owet / Ntu_i));//zzc
if (cp_r * mr > c_s * ma)
{
Ntu_wet = Ntu_owet / (1 + m_star * (Ntu_owet / Ntu_i));//zzc
}
else
{
Ntu_wet = Ntu_i / (1 + m_star * (Ntu_i / Ntu_owet));
}
epsilon_wet = ((1 - Math.Exp(-Ntu_wet * (1 - m_star))) / (1 - m_star * Math.Exp(-Ntu_wet * (1 - m_star))));
Q_wet = epsilon_wet * mdot_min * (hin_a - h_s_w_i);
hout_a = hin_a - Q_wet / ma;
Tout_r = Tin_r + ma / (mr * cp_r) * (hin_a - hout_a);
//double h_s_w_o0 = CoolProp.HAPropsSI("H", "T", Tout_r + 273.15, "P", 101325, "R", 1.0);
//h_s_w_o = 58.732687 * Math.Pow(Tout_r + 273.15, 2) - 30921.970577 * (Tout_r + 273.15) + 4075493.951473;
h_s_w_o = humidairprop.H(Tout_r, "R", 1, SourceTableData);
//double UA_star = 1 / (cp_da / (eta_a * Aa_fin + Aa_tube) / haw + CoolProp.HAPropsSI("C", "T", (Tin_a + Tout_r) / 2.0 + 273.15, "P", 101325, "R", 1) / h_r / Ar);//zzc
double UA_star = 1 / (cp_da / (eta_a * Aa_fin + Aa_tube) / haw + c_s / h_r / Ar); //zzc
Tin_s = Tout_r + UA_star / h_r / Ar * (hin_a - h_s_w_o);
h_s_s_e = hin_a + (hout_a - hin_a) / (1 - Math.Exp(-Ntu_owet)); //zzc
//double T_s_e0 = CoolProp.HAPropsSI("T", "H", h_s_s_e, "P", 101325, "R", 1.0) - 273.15;
//T_s_e = -273.15 - 1.96 * Math.Pow(10, -3) * Math.Pow(h_s_s_e / 1000, 2) + 0.5357597 * h_s_s_e / 1000 + 268.871551;
T_s_e = humidairprop.Ts(h_s_s_e, SourceTableData);
Tout_a = T_s_e + (Tin_a - T_s_e) * Math.Exp(-Ntu_owet);//zzc
Q_sensible = ma * cp_da * (Tin_a - Tout_a);
double errorToutr = Tout_r - Tout_r_start;
if (iter == 1)
{
y1 = errorToutr;
}
if (iter > 1)
{
y2 = errorToutr;
x3 = x2 - y2 / (y2 - y1) * (x2 - x1);
change = Math.Abs(y2 / (y2 - y1) * (x2 - x1));
y1 = y2;
x1 = x2;
x2 = x3;
}
iter++;
}
//if (iter > 500)
// Q = Q_dry;
double Tout_r_wet = Tout_r;
f_dry = 0.0;
if ((Tin_s > Tdp) && isFullyWet == false)
{
double iter1 = 1;
double error = 1;
double Tout_r_guess = 0;
x1 = 0.0001;
x2 = 0.9999;
eps = 1e-8;
while ((iter1 <= 3 | change > eps) && iter < 100)
{
if (iter1 == 1)
{
f_dry = x1;
}
if (iter1 > 1)
{
f_dry = x2;
}
double K = Ntu_dry * (1.0 - C_star);
double expk = Math.Exp(-K * f_dry);
if (cp_da * ma < cp_r * mr)
{
Tout_r_guess = (Tdp + C_star * (Tin_a - Tdp) - expk * (1 - K / Ntu_o) * Tin_a) / (1 - expk * (1 - K / Ntu_o));//zzc
}
else
{
Tout_r_guess = (expk * (Tin_a + (C_star - 1) * Tdp) - C_star * (1 + K / Ntu_o) * Tin_a) / (expk * C_star - C_star * (1 + K / Ntu_o));//zzc
}
epsilon_dry = ((1 - Math.Exp(-f_dry * Ntu_dry * (1 - C_star))) / (1 - C_star * Math.Exp(-f_dry * Ntu_dry * (1 - C_star))));
epsilon_wet = ((1 - Math.Exp(-(1 - f_dry) * Ntu_wet * (1 - m_star))) / (1 - m_star * Math.Exp(-(1 - f_dry) * Ntu_wet * (1 - m_star))));
double T_w_x = (Tin_r + (mdot_min) / (cp_r * mr) * epsilon_wet * (hin_a - h_s_w_i - epsilon_dry * Cmin / ma * Tin_a)) / (1 - (Cmin * mdot_min) / (cp_r * mr * ma) * epsilon_wet * epsilon_dry);
T_a_x = Tin_a - epsilon_dry * Cmin * (Tin_a - T_w_x) / (ma * cp_da);
h_a_x = hin_a - cp_da * (Tin_a - T_a_x);
Tout_r = (Cmin) / (cp_r * mr) * epsilon_dry * Tin_a + (1 - (Cmin) / (cp_r * mr) * epsilon_dry) * T_w_x;
error = Tout_r - Tout_r_guess;
if (iter1 > 500)
{
Q = Q_dry;
}
if (iter1 == 1)
{
y1 = error;
}
if (iter1 > 1)
{
y2 = error;
x3 = x2 - y2 / (y2 - y1) * (x2 - x1);
change = Math.Abs(y2 / (y2 - y1) * (x2 - x1));
y1 = y2;
x1 = x2;
x2 = x3;
}
iter1++;
}
//if (iter1 > 500)
// Q = Q_dry;
Q = mr * cp_r * (Tout_r - Tin_r);
hout_a = hin_a - Q / ma;
h_s_s_e = h_a_x + (hout_a - h_a_x) / (1 - Math.Exp(-(1 - f_dry) * Ntu_owet));//zzc
//double T_s_e0 = CoolProp.HAPropsSI("T", "H", h_s_s_e, "P", 101325, "R", 1.0) - 273.15;////////////////
//T_s_e = -273.15 - 1.96 * Math.Pow(10, -3) * Math.Pow(h_s_s_e / 1000, 2) + 0.5357597 * h_s_s_e / 1000 + 268.871551;
T_s_e = humidairprop.Ts(h_s_s_e, SourceTableData);
Tout_a = T_s_e + (T_a_x - T_s_e) * Math.Exp(-(1 - f_dry) * Ntu_owet);//zzc
Q_sensible = ma * cp_da * (Tin_a - Tout_a);
}
else
{
Q = Q_wet;
}
//res.RHout = CoolProp.HAPropsSI("R", "T", Tout_a + 273.15, "P", 101325, "H", hout_a);
//double resRHout1 = CoolProp.HAPropsSI("R", "T", Tout_a + 273.15, "P", 101325, "H", hout_a);
//res.RHout = 0.0259124 - 0.0996818 * Tout_a + 0.0934877 * (hout_a / 1000) + 0.0040018 * Math.Pow(Tout_a, 2) - 0.0003662 * Math.Pow((hout_a / 1000), 2) - 0.0034077 * Tout_a * (hout_a / 1000) - 1.76447 * Math.Pow(10, -5) * Math.Pow(Tout_a, 3) - 2.74524 * Math.Pow(10, -6) * Math.Pow((hout_a / 1000), 3) + 2.99291 * Math.Pow(10, -5) * Tout_a * Math.Pow((hout_a / 1000), 2) - 9.56644 * Math.Pow(10, -6) * Math.Pow(Tout_a, 2) * (hout_a / 1000);
Tdp_out = humidairprop.Ts(hout_a, SourceTableData);
res.RHout = humidairprop.RHI(Tout_a, Tdp_out, SourceTableData);
if (res.RHout > 1)
{
//res.RHout = 1;
//double Tout_a0 = CoolProp.HAPropsSI("T", "H", hout_a, "P", 101325, "R", 1)-273.15;
//Tout_a = -273.15 - 1.96 * Math.Pow(10, -3) * Math.Pow(hout_a / 1000, 2) + 0.5357597 * hout_a / 1000 + 268.871551;
//Tdp_out0 = CoolProp.HAPropsSI("T", "H", hout_a, "P", 101325, "R", 1.0) - 273.15;//@@@
Tout_a = humidairprop.Ts(hout_a, SourceTableData);
Q_sensible = ma * cp_da * (Tin_a - Tout_a);
}
}
}
else
{
Tout_a = Tout_a_dry;
Q = Q_dry;
Q_sensible = Q_dry;
double hout_a = hin_a - Q / ma * Math.Pow(-1, hexType);
//***delete***//
//res.RHout = CoolProp.HAPropsSI("R", "T", Tout_a + 273.15, "P", 101325, "W", omega_out);
//res.RHout = 0.0215344 - 0.0059467 * Tout_a + 0.2386894 * (omega_out * 1000) + 0.0004378 * Math.Pow(Tout_a, 2) + 0.0004635 * Math.Pow((omega_out * 1000), 2) - 0.0125912 * Tout_a * (omega_out * 1000) - 9.134 * Math.Pow(10, -6) * Math.Pow(Tout_a, 3) + 1.696 * Math.Pow(10, -6) * Math.Pow((omega_out * 1000), 3) - 2.214 * Math.Pow(10, -5) * Tout_a * Math.Pow((omega_out * 1000), 2) + 0.000200865 * Math.Pow(Tout_a, 2) * (omega_out * 1000);
//***delete***//
//res.RHout = CoolProp.HAPropsSI("R", "T", Tout_a + 273.15, "P", 101325, "H", hout_a);
//double resRHout0 = CoolProp.HAPropsSI("R", "T", Tout_a + 273.15, "P", 101325, "H", hout_a);
//res.RHout = 0.0259124 - 0.0996818 * Tout_a + 0.0934877 * (hout_a / 1000) + 0.0040018 * Math.Pow(Tout_a, 2) - 0.0003662 * Math.Pow((hout_a / 1000), 2) - 0.0034077 * Tout_a * (hout_a / 1000) - 1.76447 * Math.Pow(10, -5) * Math.Pow(Tout_a, 3) - 2.74524 * Math.Pow(10, -6) * Math.Pow((hout_a / 1000), 3) + 2.99291 * Math.Pow(10, -5) * Tout_a * Math.Pow((hout_a / 1000), 2) - 9.56644 * Math.Pow(10, -6) * Math.Pow(Tout_a, 2) * (hout_a / 1000);
//double Tdp_out0 = CoolProp.HAPropsSI("T", "H", hout_a, "P", 101325, "R", 1.0) - 273.15;//@@@
double Tdp_out = humidairprop.Ts(hout_a, SourceTableData);
res.RHout = humidairprop.RHI(Tout_a, Tdp_out, SourceTableData);
}
res.Tao = Tout_a;
res.Tro = Tout_r;
res.Q = Q / 1000;
//res.hro = (hri + Math.Pow(-1, hexType) * res.Q / mr);
double f_sp = RefrigerantSPDP.ff_Friction(Re_r);
res.DP = zdp * f_sp * l / dh * Math.Pow(g, 2.0) / rho_r / 2000;
res.Pro = fluid == "Water" ? pri : pri - res.DP;
if (res.Pro < 0)
{
res.Pro = -10000000; return(res);
}
res.hro = hri + Math.Pow(-1, hexType) * res.Q / mr;
res.R_1a = 1 / ((eta_0 * Aa_fin + Aa_tube) * ha);
res.R_1r = 1 / (res.href * Ar);
res.R_1 = res.R_1a + res.R_1r + r_metal;
if (fluid != "Water")
{
coolprop.update(input_pairs.HmassP_INPUTS, res.hro * 1000, res.Pro * 1000);
res.Tro = coolprop.T() - 273.15;
//res.Tro = CoolProp.PropsSI("T", "P", res.Pro * 1000, "H", res.hro * 1000, fluid) - 273.15;
}
return(res);
}
public static CalcResult ElementCalc(string fluid, double l, double Aa_fin, double Aa_tube, double A_r_cs, double Ar, Geometry geo, double tai,
double RHi, double tri, double pri, double hri, double mr, double g, double ma, double ha, double haw,
double eta_surface, double zh, double zdp, int hexType, double thickness, double conductivity, double Pwater, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double dh = geo.Di;
double r_metal = thickness / conductivity / Ar;
double gg = 9.8;
CalcResult res = new CalcResult();
coolprop.update(input_pairs.HmassP_INPUTS, hri * 1000, (fluid == "Water" ? Pwater : pri) * 1000);
double mu_r = coolprop.viscosity();
//double mu_r = CoolProp.PropsSI("V", "H", hri * 1000, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double k_r = coolprop.conductivity();
//double k_r = CoolProp.PropsSI("L", "H", hri * 1000, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double rho_r = coolprop.rhomass();
//double rho_r = CoolProp.PropsSI("D", "H", hri * 1000, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double cp_r = coolprop.cpmass();
//double cp_r = CoolProp.PropsSI("C", "H", hri * 1000, "P", (fluid == "Water" ? Pwater : pri) * 1000, fluid);
double Pr_r = cp_r * mu_r / k_r;
//for debugging, to check if the 1ph property is in 2ph region but not in 1ph, ruhao20180209
/*
* var rr = new Refrigerant.SATTTotalResult();
* rr = Refrigerant.SATTTotal(fluid, composition, Refrigerant.SATP(fluid, composition, pri, 1).Temperature).SATTTotalResult; //satruration temperature
* if ( rho_r > rr.DensityV && rho_r < rr.DensityL)
* {
* throw new Exception("property is not in 1ph region");
* }
*/
res.Vel_r = g / rho_r;
double Re_r = rho_r * res.Vel_r * dh / mu_r;
double fh = RefrigerantSPHTC.ff_CHURCHILL(Re_r);
double Nusselt = RefrigerantSPHTC.NU_GNIELINSKI(Re_r, Pr_r, fh);
res.href = Nusselt * k_r / dh * zh;
double cp_a = 1.0;
cp_a = (hexType == 0 ? 1.027 : 1.02);
double C_r = mr * cp_r / 1000;
double C_a = ma * cp_a;
res.R_1a = 1 / ((eta_surface * Aa_fin + Aa_tube) * ha);
res.R_1r = 1 / (res.href * Ar);
res.R_1 = res.R_1a + res.R_1r + r_metal;
double UA = 1 / res.R_1;
double C_min = Math.Min(C_a, C_r);
double C_max = Math.Max(C_a, C_r);
double C_ratio = C_min / C_max;
double NTU = UA / (C_min * 1000);
//流体不混合的一次交叉流
//double epsilon_jc = 1 - Math.Exp(Math.Pow(C_ratio,-1.0)*Math.Pow(NTU,0.22)
//*(Math.Exp(-C_ratio*Math.Pow(NTU,0.78))-1));
//顺流计算公式
//double epsilon_downflow = (1 - Math.Exp(-NTU * (1 + C_ratio))) / (1 + C_ratio);
//逆流计算公式
double epsilon_counterflow = (1 - Math.Exp(-NTU * (1 - C_ratio))) / (1 - C_ratio * Math.Exp(-NTU * (1 - C_ratio)));
double epsilon = epsilon_counterflow;
res.Q = epsilon * C_min * (tai - tri) * Math.Pow(-1, hexType);
if (C_r < C_a)
{ // hexType=0 :evap, 1:cond
res.Tro = tri + epsilon * (tai - tri); //Math.Abs(tai - tri);
res.Tao = tai - C_r * ((res.Tro - tri) / C_a); //Math.Abs(res.Tro - tri)
}
else
{
res.Tao = tai - epsilon * (tai - tri); //Math.Abs(tai - tri)
res.Tro = tri + C_a * ((tai - res.Tao) / C_r); //(Math.Abs(tai - res.Tao) / C_r)
}
double f_sp = RefrigerantSPDP.ff_Friction(Re_r);
res.DP = zdp * f_sp * l / dh * Math.Pow(g, 2.0) / rho_r / 2000;
res.Pro = fluid == "Water" ? pri : pri - res.DP;
if (res.Pro < 0)
{
res.Pro = -10000000; return(res);
}
res.hro = hri + Math.Pow(-1, hexType) * res.Q / mr;
//re-calc tro for refrigerant to avoid Tro < Tsat
if (fluid != "Water")
{
coolprop.update(input_pairs.HmassP_INPUTS, res.hro * 1000, res.Pro * 1000);
res.Tro = coolprop.T() - 273.15;
//res.Tro = CoolProp.PropsSI("T", "P", res.Pro * 1000, "H", res.hro * 1000, fluid) - 273.15;
}
res.RHout = 1.1 * RHi;
string arr1 = Convert.ToString(res.Q);
Console.WriteLine("Q={0}", arr1);
return(res);
}
public static double deltap_MS(string fluid, double d, double g, double p, double x, double l, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
//double Co=0.01;
//double f_oil = 0;
//if (x == 1) f_oil = 1.0; else f_oil = 1.15;
//double m_to_ft = 1000 / (12 * 25.4);
//double dp = 0.0;
double DensityL, DensityV, ViscosityL, ViscosityV;
coolprop.update(input_pairs.PQ_INPUTS, p * 1000, 0);
double tsat = coolprop.T();
coolprop.update(input_pairs.QT_INPUTS, 0, tsat);
DensityL = coolprop.rhomass();
ViscosityL = coolprop.viscosity();
coolprop.update(input_pairs.QT_INPUTS, 1, tsat);
DensityV = coolprop.rhomass();
ViscosityV = coolprop.viscosity();
double Re_l = g * (1 - x) * d / ViscosityL;
double Re_v = g * x * d / ViscosityV;
double f_l = 0;
double f_v = 0;
if (Re_l <= 1187)
{
f_l = 64 / Re_l;
}
else
{
f_l = 0.3164 / Math.Pow(Re_l, 0.25);
}
if (Re_v <= 1187)
{
f_v = 64 / Re_v;
}
else
{
f_v = 0.3164 / Math.Pow(Re_v, 0.25);
}
double DP_l = 4 * f_l * l * Math.Pow(g * (1 - x), 2.0) / (2 * DensityL * d);
//摩擦压降
double a = 2 * f_l * Math.Pow(g * (1 - x), 2.0) / (DensityL * d);
double b = 2 * f_v * Math.Pow(g * x, 2.0) / (DensityV * d);
double c = a + 2 * (b - a) * x;
double dp_dz = c * Math.Pow(1 - x, 1.0 / 3) + b * Math.Pow(x, 3);
double f_gd = 1 + dp_dz * ((DensityL / DensityV) / (Math.Pow(ViscosityL / ViscosityV, 0.25)) - 1);
double DP_frict = f_gd * DP_l;
//加速（动力）压降
double DP_mom = 0;
//两相总压降
double dp = (DP_frict + DP_mom) * 0.001;
return(dp);
//double DP_tp = 0;
//if (x <= 0.8)
//{
//double f_tp = 0.007397899 / (Math.Pow(x, 0.8) * Math.Pow(d * m_to_ft, 0.5)); //"Sacks & Geary"
//DP_tp = f_tp * f_oil * Math.Pow(x * g, 2.0) / (2 * r.DensityV * d);
//dp = Math.Max(DP_l, DP_tp) * l;
//dp = dp * 0.001;
//}
//else
//{
//double x_point8 = 0.8;
//double f_tp_x_point8 = 0.007397899 / (Math.Pow(x_point8, 0.8) * Math.Pow(d * m_to_ft, 0.5)); //0.00566
//double DP_tp_point8 = f_tp_x_point8 * f_oil * Math.Pow(x_point8 * g, 2.0) / (2 * r.DensityV * d);
//double x_1 = 1.0;
//double f_tp_x_1 = f_v * (1 + 14.73 * Math.Pow(Co, 0.591958)) / Math.Pow(m_to_ft, 0.5);
//double DP_tp_1 = f_tp_x_1 * f_oil * Math.Pow(x_1 * g, 2.0) / (2 * r.DensityV * d);
//DP_tp = (DP_tp_point8 + (x - 0.8) / (1.0 - 0.8) * (DP_tp_1 - DP_tp_point8)) * l;
//dp = DP_tp * 0.001;
//}
//return dp;
}
//For smooth tube for now;
public static double deltap_smooth(string fluid, double d, double g, double p, double x, double l, AbstractState coolprop)
{
//AbstractState coolprop = AbstractState.factory("HEOS", fluid);
double Co = 0.01;
double f_oil = 0;
if (x == 1)
{
f_oil = 1.0;
}
else
{
f_oil = 1.15;
}
double m_to_ft = 1000 / (12 * 25.4);
double dp = 0.0;
int phase1 = 1;
int phase2 = 2;
double DensityL, DensityV, ViscosityL, ViscosityV;
coolprop.update(input_pairs.PQ_INPUTS, p * 1000, 0);
double tsat = coolprop.T();
coolprop.update(input_pairs.QT_INPUTS, 0, tsat);
DensityL = coolprop.rhomass();
ViscosityL = coolprop.viscosity();
coolprop.update(input_pairs.QT_INPUTS, 1, tsat);
DensityV = coolprop.rhomass();
ViscosityV = coolprop.viscosity();
double Re_l = g * d / ViscosityL;// r.ViscosityL;
double Re_v = g * d / ViscosityV;
double f_l = RefrigerantSPDP.ff_Friction(Re_l);
double f_v = RefrigerantSPDP.ff_Friction(Re_v);
double DP_l = f_l * Math.Pow(g, 2.0) / (2 * DensityL * d);
double DP_tp = 0;
if (x <= 0.8)
{
double f_tp = 0.007397899 / (Math.Pow(x, 0.8) * Math.Pow(d * m_to_ft, 0.5)); //"Sacks & Geary"
DP_tp = f_tp * f_oil * Math.Pow(x * g, 2.0) / (2 * DensityV * d);
dp = Math.Max(DP_l, DP_tp) * l;
dp = dp * 0.001;
}
else
{
double x_point8 = 0.8;
double f_tp_x_point8 = 0.007397899 / (Math.Pow(x_point8, 0.8) * Math.Pow(d * m_to_ft, 0.5)); //0.00566
double DP_tp_point8 = f_tp_x_point8 * f_oil * Math.Pow(x_point8 * g, 2.0) / (2 * DensityV * d);
double x_1 = 1.0;
double f_tp_x_1 = f_v * (1 + 14.73 * Math.Pow(Co, 0.591958)) / Math.Pow(m_to_ft, 0.5);
double DP_tp_1 = f_tp_x_1 * f_oil * Math.Pow(x_1 * g, 2.0) / (2 * DensityV * d);
DP_tp = (DP_tp_point8 + (x - 0.8) / (1.0 - 0.8) * (DP_tp_1 - DP_tp_point8)) * l;
dp = DP_tp * 0.001;
}
return(dp);
}