public static double getMolarWeight(Resources res)
{
double MW = 0;
switch (res)
{
case Resources.CO2:
MW = CoolProp.PropsSI("M", "", 0, "", 0, "CO2");
return(MW);
case Resources.O2:
MW = CoolProp.PropsSI("M", "", 0, "", 0, "Oxygen");
return(MW);
case Resources.N2:
MW = CoolProp.PropsSI("M", "", 0, "", 0, "Nitrogen");
return(MW);
case Resources.CH4:
MW = CoolProp.PropsSI("M", "", 0, "", 0, "Methane");
return(MW);
case Resources.Humidity:
MW = CoolProp.PropsSI("M", "", 0, "", 0, "Water");
return(MW);
default:
throw new Exception("Cannot get molar weight for unknown resource");
}
}
//static void Main(string[] args)
//{
// Console.WriteLine(GetH20BoilingPoint(7500));
// //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");
// //var FluidString = CoolProp.get_global_param_string("FluidsList");
// //List<string> Fluids = FluidString.Split(',').ToList();
// //foreach (string Fluid in Fluids)
// //{
// // try {
// // Console.Write("Boiling temperature of " + Fluid + " at 101325 Pa:" + " " + (Math.Round(CoolProp.PropsSI("T", "P", 10000, "Q", 0, Fluid), 2) - 273.15) + " " + "C" + "\n");
// // }
// // catch { }
// //}
// //// 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");
//}
public static decimal GetWaterBoilingPoint(decimal PressureInPa)
{
decimal BoilingPoint = 0;
if (PressureInPa >= 612 && PressureInPa <= 500000)
{
BoilingPoint = Math.Round(Convert.ToDecimal(CoolProp.PropsSI("T", "P", Convert.ToDouble(PressureInPa), "Q", 0, "Water") - 273.15), 2);
}
return(BoilingPoint);
}
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, "T", 300, "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("REFPROP version:" + " " + CoolProp.get_global_param_string("REFPROP_version") + "\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", "METHANEÐANE");
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");
}
static void Main(string[] args)
{
AbstractState State = AbstractState.factory("HEOS", "Water");
State.update(input_pairs.PT_INPUTS, 1e5, 300);
double hmol = State.hmolar();
Console.Write("Hmol: " + hmol + " J/kg" + "\n");
double T, h, p, D;
//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");
Console.Write(" " + "\n");
Console.Write("************ USING EOS *************" + "\n");
Console.Write(" " + "\n");
Console.Write("FLUID STATE INDEPENDENT INPUTS" + "\n");
//Console.Write("Critical Density Propane: " + CoolProp.Props1SI("Propane", "rhocrit") + " kg/m^3" + "\n");
Console.Write("TWO PHASE INPUTS (Pressure)" + "\n");
Console.Write("Density of saturated liquid Propane at 101325 Pa: " + CoolProp.PropsSI("D", "P", 101325, "Q", 0, "Propane") + " kg/m^3" + "\n");
Console.Write("Density of saturated vapor R290 at 101325 Pa: " + CoolProp.PropsSI("D", "P", 101325, "Q", 1, "R290") + " kg/m^3" + "\n");
Console.Write("TWO PHASE INPUTS (Temperature)" + "\n");
Console.Write("Density of saturated liquid Propane at 300 K: " + CoolProp.PropsSI("D", "T", 300, "Q", 0, "Propane") + " kg/m^3" + "\n");
Console.Write("Density of saturated vapor R290 at 300 K: " + CoolProp.PropsSI("D", "T", 300, "Q", 1, "R290") + " kg/m^3" + "\n");
Console.Write("SINGLE PHASE CYCLE (propane)" + "\n");
p = CoolProp.PropsSI("P", "T", 300, "D", 1, "Propane");
h = CoolProp.PropsSI("H", "T", 300, "D", 1, "Propane");
Console.Write("T,D -> P,H " + 300 + "," + 1 + " --> " + p + "," + h + "\n");
T = CoolProp.PropsSI("T", "P", p, "H", h, "Propane");
D = CoolProp.PropsSI("D", "P", p, "H", h, "Propane");
Console.Write("P,H -> T,D " + p + "," + h + " --> " + T + "," + D + "\n");
//~ Console.Write(" " + "\n");
//~ Console.Write("************ USING TTSE ***************" + "\n");
//~ Console.Write(" " + "\n");
//~ //CoolProp.enable_TTSE_LUT("Propane");
//~ Console.Write("TWO PHASE INPUTS (Pressure)" + "\n");
//~ Console.Write("Density of saturated liquid Propane at 101325 Pa: " + CoolProp.PropsSI("D", "P", 101325, "Q", 0, "Propane") + " kg/m^3" + "\n");
//~ Console.Write("Density of saturated vapor R290 at 101325 Pa: " + CoolProp.PropsSI("D", "P", 101325, "Q", 1, "R290") + " kg/m^3" + "\n");
//~ Console.Write("TWO PHASE INPUTS (Temperature)" + "\n");
//~ Console.Write("Density of saturated liquid Propane at 300 K: " + CoolProp.PropsSI("D", "T", 300, "Q", 0, "Propane") + " kg/m^3" + "\n");
//~ Console.Write("Density of saturated vapor R290 at 300 K: " + CoolProp.PropsSI("D", "T", 300, "Q", 1, "R290") + " kg/m^3" + "\n");
//~ Console.Write("SINGLE PHASE CYCLE (propane)" + "\n");
//~ p = CoolProp.PropsSI("P", "T", 300, "D", 1, "Propane");
//~ h = CoolProp.PropsSI("H", "T", 300, "D", 1, "Propane");
//~ Console.Write("T,D -> P,H " + 300 + ","+ 1+ " --> " + p + "," + h + "\n");
//~ T = CoolProp.PropsSI("T", "P", p, "H", h, "Propane");
//~ D = CoolProp.PropsSI("D", "P", p, "H", h, "Propane");
//~ Console.Write("P,H -> T,D " + p + "," + h + " --> " + T + "," + D + "\n");
//CoolProp.disable_TTSE_LUT("Propane");
try
{
Console.Write(" " + "\n");
Console.Write("************ USING REFPROP ***************" + "\n");
Console.Write(" " + "\n");
Console.Write("TWO PHASE INPUTS (Pressure)" + "\n");
Console.Write("Density of saturated liquid Propane at 101325 Pa: " + CoolProp.PropsSI("D", "P", 101325, "Q", 0, "REFPROP::Propane") + " kg/m^3" + "\n");
Console.Write("TWO PHASE INPUTS (Temperature)" + "\n");
Console.Write("Density of saturated liquid Propane at 300 K: " + CoolProp.PropsSI("D", "T", 300, "Q", 0, "REFPROP::Propane") + " kg/m^3" + "\n");
Console.Write("SINGLE PHASE CYCLE (propane)" + "\n");
p = CoolProp.PropsSI("P", "T", 300, "D", 1, "REFPROP::Propane");
h = CoolProp.PropsSI("H", "T", 300, "D", 1, "REFPROP::Propane");
Console.Write("T,D -> P,H " + 300 + "," + 1 + " --> " + p + "," + h + "\n");
T = CoolProp.PropsSI("T", "P", p, "H", h, "REFPROP::Propane");
D = CoolProp.PropsSI("D", "P", p, "H", h, "REFPROP::Propane");
Console.Write("P,H -> T,D " + p + "," + h + " --> " + T + "," + D + "\n");
}
catch
{
Console.Write(" " + "\n");
Console.Write("************ CANT USE REFPROP ************" + "\n");
Console.Write(" " + "\n");
}
Console.Write(" " + "\n");
Console.Write("************ BRINES AND SECONDARY WORKING FLUIDS *************" + "\n");
Console.Write(" " + "\n");
Console.Write("Density of 50% (mass) ethylene glycol/water at 300 K, 101325 Pa: " + CoolProp.PropsSI("D", "T", 300, "P", 101325, "EG-50%") + " kg/m^3" + "\n");
Console.Write("Viscosity of Therminol D12 at 350 K, 101325 kPa: " + CoolProp.PropsSI("V", "T", 350, "P", 101325, "INCOMP::TD12") + " Pa-s" + "\n");
Console.Write(" " + "\n");
Console.Write("************ HUMID AIR PROPERTIES *************" + "\n");
Console.Write(" " + "\n");
//Console.Write("Humidity ratio of 50% rel. hum. air at 300 K, 101.325 kPa: " + CoolProp.HAProps("W", "T", 300, "P", 101.325, "R", 0.5) + " kg_w/kg_da" + "\n");
//Console.Write("Relative humidity from last calculation: " + CoolProp.HAProps("R", "T", 300, "P", 101.325, "W", CoolProp.HAProps("W", "T", 300, "P", 101.325, "R", 0.5)) + "(fractional)" + "\n");
//Console.Write("Enter to quit");
//Console.ReadLine();
}
double ICoolProp.PropsSI(string Output, string Name1, double Prop1, string Name2, double Prop2, string FluidName)
{
return(CoolProp.PropsSI(Output, Name1, Prop1, Name2, Prop2, FluidName));
}
public void PlotPHChart(string fluidName)
{
MathOperation PH = new MathOperation();
//===============Test ===================//
//for (double y = 0.005; y < 40; y *= 2)
//{
// double pressureVal= PH.IAPWS_IF97_TowParameterEquivalentFxn("P", "T", 483.15, "H", 400 * 1000, fluidName); //--This multiply is done to convert MPa to Pa and enthlapy is divided to convert J/kg to kJ/Kg
// aListTemperature.Add(temperature);
//}
//================End of test=========//
/*
* Lets do it step by step as the way that has been done in the Matlab
*
*/
//--1. press_rng = logspace(-2,2,300); % [MPa] pressure (p) range
// var stopWatch = System.Diagnostics.Stopwatch.StartNew();
//double[] press_rng = PH.LogSpace(-2, 2, 300,true,10).ToArray();
double[] press_rng = PH.LogSpace(-3, 2, 300, true, 10).ToArray();// initially it was form -2,2,300 //-4,4,300 is not supported by coolprop
//--For line spacing values
//2. temp_rng = 273.15+linspace(1,800,300);
//double[] temp_rng = PH.LinSpace(1, 800, 300, true).ToArray();
//--Here -4,800,300 doesnot work error by cool prop 0 onwards on negative axis(eg.0,-1,-2,-3,...) does not work
double[] temp_rng = PH.LinSpace(1, 800, 300, true).ToArray();// changed from 1,800,300
for (int i = 0; i < temp_rng.Length; i++)
{
temp_rng[i] += 273.15;
}
//--Now for meshgrid we have created truple
//MeshGrid_Class ms1 = new MeshGrid_Class();
//3.[p,T] = meshgrid(press_rng,temp_rng); % [MPa,K] mesh p & T
MeshGridClass.MeshGrid(press_rng, temp_rng);
Tuple <double[, ], double[, ]> tuple_x = MeshGridClass.MeshGrid(press_rng, temp_rng);
double[,] p = tuple_x.Item1;
double[,] T = tuple_x.Item2;
//--8 pcrit = 22.064; % [MPa] critical pressure
double pcrit = CoolProp.Props1SI(fluidName, "Pcrit") / 1000000;//To convert to Pa form MPa //22.064;//CoolProp.Props1SI( "Water", "Pcrit");//PropsSI("Pcrit", "", 0, "", 0, "Water");//PH.IAPWS_IF97_TowParameterEquivalentFxn("Pcrit", "", 0, "",0, fluidName); //CoolProp.Props1SI(fluidName, "Pcrit");// CP.PropsSI("Tcrit","",0,"",0,"Water")
//--Now lets do the calculation for others
//4.h = IAPWS_IF97('h_pT',p,T); % [kJ/kg] enthalpy = f(p,T)
P_Value = p; //Copy
T_Value = T; //Copy
double[,] h = new double[p.GetLength(0), p.GetLength(1)];
for (int i = 0; i < h.GetLength(0); i++)
{
for (int j = 0; j < h.GetLength(1); j++)
{
double enthalpy = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", p[i, j] * 1000000, "T", T[i, j], fluidName) / 1000; //--This multiply is done to convert MPa to Pa and enthlapy is divided to convert J/kg to kJ/Kg
h[i, j] = enthalpy;
}
}
H_Value = h;//Copy
//--5 psat = IAPWS_IF97('psat_T',temp_rng); % [MPa] saturation pressure
// 6. also trimming is done in this section
List <double> psatList = new List <double>();
psatList.Clear();
//--Finding boundary condition i.e maximun temperature range and minimum temperature range for different fluid
//--eg. For Water min to max is 273.06K - 647.096K [in kelvin]
double maxCriticalTemperature = 0;
//--For critical CP.PropsSI("Tcrit","",0,"",0,"Water")
maxCriticalTemperature = PH.IAPWS_IF97_TowParameterEquivalentFxn("Tcrit", "", 0, "Q", 0, fluidName);
for (int i = 0; i < temp_rng.Length; i++)
{
if (((temp_rng[i] <= maxCriticalTemperature)))
{
double psat = PH.IAPWS_IF97_TowParameterEquivalentFxn("P", "T", temp_rng[i], "Q", 0, fluidName) / 1000000;
psatList.Add(psat);
} //Close of if statement
} //Close of for
//-- 6. psat = psat(~isnan(psat));
//--Use dynamic list to trim data which are empty rather than array
//--6 . hLsat = IAPWS_IF97('hL_p',psat); % [kJ/kg] saturated liquid enthalpy
List <double> hLsatList = new List <double>();
hLsatList.Clear();
foreach (var item in psatList)
{
double hLsat = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", item * 1000000, "Q", 0, fluidName) / 1000;//Q=0 for liquid
hLsatList.Add(hLsat);
}
//--7 . hVsat = IAPWS_IF97('hV_p',psat); % [kJ/kg] saturated vapor enthalpy
List <double> hVsatList = new List <double>();
hVsatList.Clear();
foreach (var item in psatList)
{
double hVsat = CoolProp.PropsSI("H", "P", item * 1000000, "Q", 1, fluidName) / 1000; // PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", item, "Q", 1.0, fluidName);//Zero for vapor
hVsatList.Add(hVsat);
}
//--8. already declared
//--9 hLcrit = IAPWS_IF97('hL_p',pcrit);
double hLcrit = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", pcrit * 1000000, "Q", 0, fluidName) / 1000;//Zero for liquid
//--10 . hVcrit = IAPWS_IF97('hV_p',pcrit);
double hVcrit = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", pcrit * 1000000, "Q", 1, fluidName) / 1000; //Zero for liquid
//--11. Tcrit = IAPWS_IF97('Tsat_p',pcrit);
double Tcrit = maxCriticalTemperature; // CoolProp.PropsSI("Tcrit", "", 0, "", 0, "Water");//PH.IAPWS_IF97_TowParameterEquivalentFxn("Tcrit", "", 0, "", 0, fluidName);//CoolProp.Props1SI(fluidName, "Tcrit");
//--12. hcrit = IAPWS_IF97('h_pT',pcrit,Tcrit);
double hcrit = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", pcrit * 1000000, "T", Tcrit, fluidName) / 1000; //Zero for liquid
//--13.hVL = hVsat - hLsat; % [kJ/kg] heat of vaporization
List <double> hVL_List = new List <double>();
hVL_List.Clear();
for (int i = 0; i < hVsatList.Count; i++)
{
double subtracted_value = hVsatList[i] - hLsatList[i];
hVL_List.Add(subtracted_value);
}
//--14. hX = hLsat*ones(1,9) + hVL*(0.1:0.1:0.9); % [kJ/kg] mixture enthalpy
double[,] hX = new double[hLsatList.Count, 9];
double[,] hVL_LeftSideValue = new double[hLsatList.Count, 9]; //stores hVL*(0.1:0.1:0.9);
double[,] hLsat_RightSideValue = new double[hLsatList.Count, 9]; //stores hLsat*ones(1,9)
double stepVal = 0.1;
for (int i = 0; i < 9; i++)
{
for (int j = 0; j < hVL_List.Count; j++)
{
hVL_LeftSideValue[j, i] = hVL_List[j] * stepVal;
}
stepVal += 0.1;
}
for (int i = 0; i < 9; i++)
{
for (int j = 0; j < hLsatList.Count; j++)
{
hLsat_RightSideValue[j, i] = hLsatList[j];
}
}
//For final sum
for (int i = 0; i < 9; i++)
{
for (int j = 0; j < hLsatList.Count; j++)
{
hX[j, i] = hLsat_RightSideValue[j, i] + hVL_LeftSideValue[j, i];// hLsatList[j].Value;
}
}
//--Now lets move to plotting the things
//Conture plot and
/*
* For this function plot
* plot([hLsat;hLcrit],[psat;pcrit],'b', ...
* [hVsat;hVcrit],[psat;pcrit],'r', ...
* hcrit,pcrit,'o', ...
* hX,psat*ones(1,9),'g') % vapor dome
*/
phChart.Series.Clear();
phChart.ChartAreas[0].AxisX.Minimum = 1 / 1000; //--This was 1/1000
phChart.ChartAreas[0].AxisX.Maximum = 4000; //4000;
phChart.ChartAreas[0].AxisX.Interval = 500;
phChart.ChartAreas[0].AxisY.Minimum = 0.01; //--This was 0.001
phChart.ChartAreas[0].AxisY.IsLogarithmic = true;
phChart.ChartAreas[0].AxisY.LogarithmBase = 10;
phChart.ChartAreas[0].AxisY.Interval = 1;
// phChart.ChartAreas[0].AxisY.Maximum = 50;
//--this one is for [hLsat;hLcrit],[psat;pcrit],'b', ...
// ph_chart.ChartAreas[0].AxisX.Minimum =
phChart.Series.Clear();
phChart.Series.Add("Series01");
phChart.Series["Series01"].ChartType = SeriesChartType.Line;
for (int i = 0; i < hLsatList.Count; i++)
{
phChart.Series["Series01"].Points.AddXY(hLsatList[i], psatList[i]);
}
phChart.Series["Series01"].Points.AddXY(hLcrit, pcrit);
phChart.Series["Series01"].Color = Color.Blue;
phChart.Series["Series01"].Font = new Font(FontFamily.GenericSansSerif, 8, FontStyle.Bold);
//phChart.Series["Series01"].Font.
// /*
phChart.Series["Series01"].Points[12].Label = "S";
phChart.Series["Series01"].Points[15].Label = "a";
phChart.Series["Series01"].Points[18].Label = "t";
phChart.Series["Series01"].Points[21].Label = "u";
phChart.Series["Series01"].Points[24].Label = "r";
phChart.Series["Series01"].Points[27].Label = "a";
phChart.Series["Series01"].Points[30].Label = "t";
phChart.Series["Series01"].Points[33].Label = "i";
phChart.Series["Series01"].Points[36].Label = "o";
phChart.Series["Series01"].Points[40].Label = "n";
phChart.Series["Series01"].Points[50].Label = "L";
phChart.Series["Series01"].Points[55].Label = "i";
phChart.Series["Series01"].Points[63].Label = "q";
phChart.Series["Series01"].Points[69].Label = "u";
phChart.Series["Series01"].Points[75].Label = "i";
phChart.Series["Series01"].Points[80].Label = "d";
// */
phChart.Series["Series01"].ChartArea = "ChartArea1";
//This one if for [hVsat;hVcrit],[psat;pcrit],'r', ...
phChart.Series.Add("Series2");
phChart.Series["Series2"].ChartType = SeriesChartType.Line;
for (int i = 0; i < hVsatList.Count; i++)
{
phChart.Series["Series2"].Points.AddXY(hVsatList[i], psatList[i]);
}
phChart.Series["Series2"].Points.AddXY(hVcrit, pcrit);
phChart.Series["Series2"].Color = Color.Red;
//Chart1.Series(0).Font = New Font(Me.Font.Name, 5, FontStyle.Regular)
phChart.Series["Series2"].Font = new Font(FontFamily.GenericSansSerif, 8, FontStyle.Bold);
// phChart.Series["Series2"].Points[12].Label = $"Saturation Vapour";
// /*
phChart.Series["Series2"].Points[12].Label = "S";
phChart.Series["Series2"].Points[15].Label = "a";
phChart.Series["Series2"].Points[18].Label = "t";
phChart.Series["Series2"].Points[21].Label = "u";
phChart.Series["Series2"].Points[24].Label = "r";
phChart.Series["Series2"].Points[27].Label = "a";
phChart.Series["Series2"].Points[31].Label = "t";
phChart.Series["Series2"].Points[35].Label = "i";
phChart.Series["Series2"].Points[39].Label = "o";
phChart.Series["Series2"].Points[44].Label = "n";
phChart.Series["Series2"].Points[50].Label = "V";
phChart.Series["Series2"].Points[55].Label = "a";
phChart.Series["Series2"].Points[60].Label = "p";
phChart.Series["Series2"].Points[67].Label = "o";
phChart.Series["Series2"].Points[74].Label = "u";
phChart.Series["Series2"].Points[80].Label = "r";
// */
phChart.Series["Series2"].ChartArea = "ChartArea1";
//--For critical point
//This one if for hcrit,pcrit,'o', ...
phChart.Series.Add("Series3");
phChart.Series["Series3"].ChartType = SeriesChartType.Point;
phChart.Series["Series3"].Points.AddXY(hcrit, pcrit);
phChart.Series["Series3"].Color = Color.Orange;
phChart.Series["Series3"].ChartArea = "ChartArea1";
//--This one is the last one
double[,] psatOneToNine = new double[psatList.Count, 9];
for (int i = 0; i < 9; i++)
{
for (int j = 0; j < psatList.Count; j++)
{
psatOneToNine[j, i] = psatList[j];
}
}
for (int i = 0; i < hX.GetLength(1); i++)//Row
{
phChart.Series.Add("Series4" + i);
phChart.Series["Series4" + i].ChartType = SeriesChartType.Line;
for (int j = 0; j < hX.GetLength(0); j++)//Column
{
phChart.Series["Series4" + i].Points.AddXY(hX[j, i], psatOneToNine[j, i]);
}
phChart.Series["Series4" + i].Color = Color.Green;
phChart.Series["Series4" + i].Points[12].Label = $"{(i + 1) * 10} %";//initially no. 12
phChart.Series["Series4" + i].Font = new Font(FontFamily.GenericSansSerif, 8, FontStyle.Bold);
phChart.Series["Series4" + i].ChartArea = "ChartArea1";
}
//---Contour line plotting chunk of code -----------//
/*
* Steps :
* 1. number of contour
* 2. series decleration
* 3. ds the data setting for Jack xu book[data is already calculated so]
* 4. calling the plot function in Jack xu code
*/
int numberOfContour = 25;
ArrayList alSeries = new ArrayList();
for (int i = 0; i < numberOfContour; i++)
{
string name = "ContourSeries" + i;
alSeries.Add(name);
}
ChartFunctions cf = new ChartFunctions();
DataSeries ds = new DataSeries();
Form1_jack_xu f1 = new Form1_jack_xu();
DrawChart dc = new DrawChart(f1);
cf.SetDataPoints(ds, P_Value, T_Value, H_Value);
//==After calling this we need to call the number of contour plots
/* numberContours values =
* 28 gives 20 lines,
* 30 gives 20 lines,
* 25 gives 17 lines
* 35 gives 25 lines [max limit]
* 20 gives 14 lines
* 27 gives 19 lines
* 13 gives 8 lines
*/
dc.numberContours = 35;
List <DrawChart.DataTypeForPointList> listPoints = new List <DrawChart.DataTypeForPointList>();
listPoints = dc.AddContour_MyCustomFxn(ds);
//-------------For indicator of Temperature---------//
string seriesName1 = "TemperaturePoints";
phChart.Series.Add(seriesName1);
phChart.Series[seriesName1].ChartType = SeriesChartType.Point;
int ind = 0;
int flagSingleTemperatureIndicator = 1;//on first
double zlevelValueForTempIndicator = 0;
int dataPointCounter = 0;
// int enthalpyValueForIndiator = 2000;
//---------------End of indicator of temperature---//
//--Serching z-levels and plotting
int initialZ = listPoints[0].zlevel;
int initalIndex = 0;
int runningz = 0;
for (int i = 0; i < numberOfContour; i++)
{
//==First one is for moving in the list
string seriesName = alSeries[i].ToString();
Series s1 = new Series(seriesName);
//s1.MarkerSize = 15;//--This does not work so
s1.ChartType = SeriesChartType.Line;
phChart.Series.Add(s1);
//phChart.Series.Add(seriesName);
//phChart.Series[seriesName].ChartType = SeriesChartType.Line;
//phChart.Series[seriesName].MarkerSize = 60;
//==For moving in the list
for (int z = initalIndex; z < listPoints.Count; z++)
{
runningz = z;
if (initialZ == listPoints[z].zlevel)
{
//==Same zlevel then draw on one line
phChart.Series[seriesName].Points.AddXY(listPoints[z].x1, listPoints[z].y1);
phChart.Series[seriesName].Points.AddXY(listPoints[z].x2, listPoints[z].y2);
dataPointCounter++;
// /*
//===========Temperature indicator================//
if (flagSingleTemperatureIndicator == 1 && dataPointCounter > (listPoints[z].zlevel) && (listPoints[z].x1 > 200 && listPoints[z].x1 < 2500)) //(flagSingleTemperatureIndicator == 1 && zlevelValueForTempIndicator == listPoints[z].zlevel) //(listPoints[z].x1 == 2000)
{
double temperature = PH.IAPWS_IF97_TowParameterEquivalentFxn("T", "H", listPoints[z].x1 * 1000, "P", listPoints[z].y1 * 1000000, fluidName); //--This multiply is done to convert MPa to Pa and enthlapy is divided to convert J/kg to kJ/Kg
phChart.Series[seriesName1].Points.AddXY(listPoints[z].x1, listPoints[z].y1);
phChart.Series[seriesName1].Points[ind++].Label = $"{Math.Round(temperature - 273.15, 0)}°C";
flagSingleTemperatureIndicator = 0;//off
dataPointCounter = 0;
}
if (listPoints[z].zlevel > zlevelValueForTempIndicator)
{
flagSingleTemperatureIndicator = 1;//on
////zlevelValueForTempIndicator = listPoints[z].zlevel;
}
zlevelValueForTempIndicator = listPoints[z].zlevel;
//===========Temper indiactor end==============//
// */
}
else
{
initialZ = listPoints[z].zlevel;
initalIndex = z;
//flagSingleTemperatureIndicator = 1;//on
break;
}
}
if (runningz == listPoints.Count)
{
break;
}
}
//stopWatch.Stop();
//MessageBox.Show($"Elapsed millisecond = { stopWatch.ElapsedMilliseconds} ms");
//---End of the contour line plot chunk of code---//
ArrayList aListTemperature = new ArrayList();
//string seriesName1 = "TemperaturePoints";
//phChart.Series.Add(seriesName1);
//phChart.Series[seriesName1].ChartType = SeriesChartType.Point;
//int ind = 0;
//for (double y = 0.005; y < 40; y *= 2)
//{
// double temperature = PH.IAPWS_IF97_TowParameterEquivalentFxn("T", "H", 400 * 1000, "P", y * 1000000, fluidName); //--This multiply is done to convert MPa to Pa and enthlapy is divided to convert J/kg to kJ/Kg
// aListTemperature.Add(temperature);
// phChart.Series[seriesName1].Points.AddXY(400, y);
// phChart.Series[seriesName1].Points[ind++].Label = $"{Math.Round(temperature - 273.15, 2)} DegC";
//}
//=================================This part is for regregration cycle=====================//
///*
//--We need to convert temp to kelvine
double T1 = 106 + 273.15; //Deg C+273.15 = kelving temperature ==>TEMPERATURE // changed from 10
double P1 = 0.05; //MPa ==>Y-Axis[Pressure] //changed form 0.05mpa
double T2 = 200 + 273.15;
double P2 = 2; //MPa //changed form 1 MPa
double T3 = 200 + 273.15;
double P3 = P2;
double T4 = T1;
double P4 = P1;
//--Lets calculate enthalpy
//double enthalpy1 = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", P1 * 1000000, "T", T1, fluidName) / 1000;
//double enthalpy2 = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", P2 * 1000000, "T", T2, fluidName) / 1000;
//double enthalpy3 = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", P3 * 1000000, "T", T3, fluidName) / 1000;
//double enthalpy4 = PH.IAPWS_IF97_TowParameterEquivalentFxn("H", "P", P4 * 1000000, "T", T4, fluidName) / 1000;
double enthalpy1 = 2650;
double enthalpy2 = 2900;
double enthalpy3 = 900;
double enthalpy4 = 900;
// MessageBox.Show($"Different enthalpy values en1[same input as en4]= {enthalpy1} , en2 = {enthalpy2},en3 = {enthalpy3} , en4 ={enthalpy4}");
string sName1 = "RefregrationCyclePoints";
phChart.Series.Add(sName1);
phChart.Series[sName1].ChartType = SeriesChartType.Point;
phChart.Series[sName1].MarkerStyle = MarkerStyle.Circle;
phChart.Series[sName1].MarkerSize = 8;
phChart.Series[sName1].Points.AddXY(enthalpy1, P1);
phChart.Series[sName1].Points.AddXY(enthalpy2, P2);
phChart.Series[sName1].Points.AddXY(enthalpy3, P3);
phChart.Series[sName1].Points.AddXY(enthalpy4, P4);
string lineCycle1 = "LineRefCycle1";
phChart.Series.Add(lineCycle1);
phChart.Series[lineCycle1].ChartType = SeriesChartType.Line;
phChart.Series[lineCycle1].BorderWidth = 5;
phChart.Series[lineCycle1].MarkerStyle = MarkerStyle.Circle;
phChart.Series[lineCycle1].MarkerSize = 5;
phChart.Series[lineCycle1].Color = Color.Green;
phChart.Series[lineCycle1].Points.AddXY(enthalpy1, P1);
phChart.Series[lineCycle1].Points.AddXY((enthalpy1 + enthalpy2) / 2, 0.3);//1.2 is pressure it is manually given as scale is in log
phChart.Series[lineCycle1].Points.AddXY(enthalpy2, P2);
phChart.Series[lineCycle1].Points[1].Label = "Compression";
string lineCycle2 = "LineRefCycle2";
phChart.Series.Add(lineCycle2);
phChart.Series[lineCycle2].ChartType = SeriesChartType.Line;
phChart.Series[lineCycle2].MarkerStyle = MarkerStyle.Circle;
phChart.Series[lineCycle2].BorderWidth = 5;
phChart.Series[lineCycle2].MarkerSize = 5;
phChart.Series[lineCycle2].Color = Color.Green;
phChart.Series[lineCycle2].Points.AddXY(enthalpy2, P2);
phChart.Series[lineCycle2].Points.AddXY((enthalpy2 + enthalpy3) / 2, (P2 + P3) / 2);
phChart.Series[lineCycle2].Points.AddXY(enthalpy3, P3);
phChart.Series[lineCycle2].Points[1].Label = "Condensor";
string lineCycle3 = "LineRefCycle3";
phChart.Series.Add(lineCycle3);
phChart.Series[lineCycle3].ChartType = SeriesChartType.Line;
phChart.Series[lineCycle3].MarkerStyle = MarkerStyle.Circle;
phChart.Series[lineCycle3].BorderWidth = 5;
phChart.Series[lineCycle3].MarkerSize = 5;
phChart.Series[lineCycle3].Color = Color.Green;
phChart.Series[lineCycle3].Points.AddXY(enthalpy3, P3);
phChart.Series[lineCycle3].Points.AddXY((enthalpy3 + enthalpy4) / 2, 0.3);//0.3 is a pressure ie 0.3mpa
phChart.Series[lineCycle3].Points.AddXY(enthalpy4, P4);
phChart.Series[lineCycle3].Points[1].Label = "Expansion Valve";
string lineCycle4 = "LineRefCycle4";
phChart.Series.Add(lineCycle4);
phChart.Series[lineCycle4].ChartType = SeriesChartType.Line;
phChart.Series[lineCycle4].MarkerStyle = MarkerStyle.Circle;
phChart.Series[lineCycle4].BorderWidth = 5;
phChart.Series[lineCycle4].MarkerSize = 5;
phChart.Series[lineCycle4].Color = Color.Green;
phChart.Series[lineCycle4].Points.AddXY(enthalpy4, P4);
phChart.Series[lineCycle4].Points.AddXY((enthalpy4 + enthalpy1) / 2, (P4 + P1) / 2);
phChart.Series[lineCycle4].Points.AddXY(enthalpy1, P1);
phChart.Series[lineCycle4].Points[1].Label = "Evaporator";
// */
//=================================End regregration cycle=====================//
}
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
}
//------------------------End of logspace---------------------------------------------------//
/// <summary>
/// Equivalent of matlab function IAPWS_IF97()
/// returns parameters based on the outputName
/// </summary>
/// <param name="outputName">output we want</param>
/// <param name="prop1">proerty1(like T(tempr), P(Pressure),h(enthalpy),etc)</param>
/// <param name="prop1Value">Value of prop1</param>
/// <param name="prop2">proerty2(like T(tempr), P(Pressure),h(enthalpy),etc)</param>
/// <param name="prop2Value">Value of prop2</param>
/// <param name="fluidName">Fluid Name(eg. Water,n-Propane,etc)</param>
/// <returns>values based on pased parameter generally, temperature, pressure and enthalpy</returns>
public double IAPWS_IF97_TowParameterEquivalentFxn(string outputParamName, string prop1, double prop1Value, string prop2, double prop2Value, string fluidName)
{
return(CoolProp.PropsSI(outputParamName, prop1, prop1Value, prop2, prop2Value, fluidName));
}
//Start
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, int AirFlowDirection, List <NodeInfo> Nodes, int N_Node, CapiliaryInput cap_inlet, CapiliaryInput cap_outlet, AbstractState coolprop, double[,] SourceTableData)
{
double tri = te; //Refrigerant.SATP(fluid, composition, pri, 1).Temperature - 273.15;
double pri = pe;
double te_calc_org = 0;
int N_tube = Ntube[0];
CirArr[] cirArr = new CirArr[Nrow * N_tube];
CirArrforAir cirArrforAir = new CirArrforAir();
cirArrforAir = CirArrangement.ReadCirArr(CirArrange, CircuitInfo, Nrow, Ntube, AirFlowDirection);
cirArr = cirArrforAir.CirArr;
CheckAir airConverge = new CheckAir();
CheckDP dPconverge = new CheckDP();
CheckPri priconverge = new CheckPri();
int iterforAir = 0;
int iterforDP = 0;
int iterforPri = 0;
CalcResult r = new CalcResult();
CalcResult res_slab = new CalcResult();
int N_cir = CircuitInfo.TubeofCir.Length;
int N_tube_total = CircuitInfo.TubeofCir.Sum();
CalcResult[] res_cir = new CalcResult[N_cir];
double[, ,] taout_calc = new double[Nelement, N_tube, Nrow];
double[, ,] RHout_calc = new double[Nelement, N_tube, Nrow];
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 index_Node = 0;
int index_couple = 0;
int index_last_Node = 0;
bool index_end = false;
int[] index_status = new int[N_Node];
int[] index_FullStatus = new int[N_Node];
int[] index_DP = new int[N_Node];//
double mri_cal = 0;
double pri_cal = 0;
double hri_cal = 0;
double tri_cal = 0;
int index_cir = 0;
double te_calc;
do //Pri iteration
{
if (hexType == 0) // need to be under pri iteration
{
tri = CoolProp.PropsSI("T", "P", pri * 1000, "Q", 0, fluid) - 273.15;
}
else
{
te = CoolProp.PropsSI("T", "P", pri * 1000, "Q", 0, fluid) - 273.15;
}
int iiii = 0;
do//Air iteration
{
//Node[] Nodes=new Node[N_node];
//Nodes[0]=First Node;
for (int i = 0; i < N_Node; i++)
{
index_FullStatus[i] = Math.Max(Nodes[i].N_in, Nodes[i].N_out);
index_status[i] = 0;
}
index_Node = SearchNode.FindNextNode(-1, 0, Nodes, N_Node); //Find the first node
index_status[index_Node] = 0; //initial status
//index_FullStatus[index_Node]=Nodes[index_Node].N_out;
//index_DP[index_Node] = 0;
index_end = false;
for (int i = 0; i < 1000; i++) //for DP converge
{
if (Nodes[index_Node].inlet[0] == -1) //First Node(diverse)
{
Nodes[index_Node].mri[0] = mr;
Nodes[index_Node].pri[0] = pri;
Nodes[index_Node].hri[0] = hri;
Nodes[index_Node].tri[0] = tri;
//index_cir=Node[index].out[i];//?
}
if (Nodes[index_Node].type == 'D' || Nodes[index_Node].type == 'S') //Diverse Node Distribution
{
if (index_DP[index_Node] == 0) //first time calculation
{
Nodes[index_Node].mro[index_status[index_Node]] = Nodes[index_Node].mri[0] / Nodes[index_Node].N_out;
}
else
{
Nodes[index_Node].mro[index_status[index_Node]] = Nodes[index_Node].mri[0] * Nodes[index_Node].mr_ratio[index_status[index_Node]];
}
Nodes[index_Node].pro[index_status[index_Node]] = Nodes[index_Node].pri[0];
Nodes[index_Node].tro[index_status[index_Node]] = Nodes[index_Node].tri[0];
Nodes[index_Node].hro[index_status[index_Node]] = Nodes[index_Node].hri[0];
if (Nodes[index_Node].outType[index_status[index_Node]] == 0)//0:out is Node,1:out is Circuit
{
index_last_Node = index_Node;
index_Node = SearchNode.FindNextNode(index_Node, index_status[index_Node], Nodes, N_Node);//find node
Nodes[index_Node].pri[0] = Nodes[index_last_Node].pro[index_status[index_last_Node]];
Nodes[index_Node].tri[0] = Nodes[index_last_Node].tro[index_status[index_last_Node]];
Nodes[index_Node].hri[0] = Nodes[index_last_Node].hro[index_status[index_last_Node]];
Nodes[index_Node].mri[0] = Nodes[index_last_Node].mro[index_status[index_last_Node]];
index_status[index_Node] = 0;
//i_end=Nodes[index_Node].N_out;
continue;
}
else//out is Circuit
{
mri_cal = Nodes[index_Node].mro[index_status[index_Node]];
pri_cal = Nodes[index_Node].pro[index_status[index_Node]];
tri_cal = Nodes[index_Node].tro[index_status[index_Node]];
hri_cal = Nodes[index_Node].hro[index_status[index_Node]];
index_cir = Nodes[index_Node].outlet[index_status[index_Node]];
}
}
else if (Nodes[index_Node].type == 'C')//Converge Node
{
mri_cal = Nodes[index_Node].mro[0];
pri_cal = Nodes[index_Node].pro[0];
hri_cal = Nodes[index_Node].hro[0];
tri_cal = Nodes[index_Node].tro[0];
index_cir = Nodes[index_Node].outlet[0];
}
//index_status[index_Node]=i;//status
r = Circuit.CircuitCalc(index_cir, cirArr, CircuitInfo, Nrow, Ntube, Nelement, fluid, l, geo, ta, RH,
tri_cal, pri_cal, hri_cal, mri_cal, ma, ha, haw, eta_surface, zh, zdp, hexType, thickness, conductivity, Pwater, cap_inlet, cap_outlet, coolprop, SourceTableData);
res_cir[index_cir] = r;
if (r.Pro < 0)
{
res_slab.Pro = -10000000; return(res_slab);
}
for (int aa = 0; aa < Nrow; aa++)// detail result print
{
for (int bb = 0; bb < N_tube; bb++)
{
Q_detail[bb, aa] = r.Q_detail[bb, aa] == 0 ? Q_detail[bb, aa] : r.Q_detail[bb, aa];
DP_detail[bb, aa] = r.DP_detail[bb, aa] == 0 ? DP_detail[bb, aa] : r.DP_detail[bb, aa];
Pri_detail[bb, aa] = r.Pri_detail[bb, aa] == 0 ? Pri_detail[bb, aa] : r.Pri_detail[bb, aa];
Tri_detail[bb, aa] = r.Tri_detail[bb, aa] == 0 ? Tri_detail[bb, aa] : r.Tri_detail[bb, aa];
hri_detail[bb, aa] = r.hri_detail[bb, aa] == 0 ? hri_detail[bb, aa] : r.hri_detail[bb, aa];
Pro_detail[bb, aa] = r.Pro_detail[bb, aa] == 0 ? Pro_detail[bb, aa] : r.Pro_detail[bb, aa];
Tro_detail[bb, aa] = r.Tro_detail[bb, aa] == 0 ? Tro_detail[bb, aa] : r.Tro_detail[bb, aa];
hro_detail[bb, aa] = r.hro_detail[bb, aa] == 0 ? hro_detail[bb, aa] : r.hro_detail[bb, aa];
href_detail[bb, aa] = r.href_detail[bb, aa] == 0 ? href_detail[bb, aa] : r.href_detail[bb, aa];
mr_detail[bb, aa] = r.mr_detail[bb, aa] == 0 ? mr_detail[bb, aa] : r.mr_detail[bb, aa];
charge_detail[bb, aa] = r.charge_detail[bb, aa] == 0 ? charge_detail[bb, aa] : r.charge_detail[bb, aa];
for (int cc = 0; cc < Nelement; cc++)
{
taout_calc[cc, bb, aa] = r.Tao_Detail[cc, bb, aa] == 0 ? taout_calc[cc, bb, aa] : r.Tao_Detail[cc, bb, aa];
RHout_calc[cc, bb, aa] = r.RHo_Detail[cc, bb, aa] == 0 ? RHout_calc[cc, bb, aa] : r.RHo_Detail[cc, bb, aa];
}
}
}
index_Node = SearchNode.FindNextNode(index_Node, index_status[index_Node], Nodes, N_Node); //Find Next Node
if (Nodes[index_Node].type == 'D') //Diverse Node cal
{
index_status[index_Node] = 0;
//i_end=Nodes[index_Node].N_out;
Nodes[index_Node].pri[0] = r.Pro;
Nodes[index_Node].tri[0] = r.Tro;
Nodes[index_Node].hri[0] = r.hro;
Nodes[index_Node].mri[0] = r.mr;
continue;
}
else if (Nodes[index_Node].type == 'C')//Converge Node cal
{
for (int ii = 0; ii < N_Node; ii++)
{
if (Nodes[ii].couple == Nodes[index_Node].couple && ii != index_Node)
{
index_couple = ii;
break;
}
}//Find the Couple Node
Nodes[index_Node].pri[index_status[index_couple]] = r.Pro;
Nodes[index_Node].tri[index_status[index_couple]] = r.Tro;
Nodes[index_Node].hri[index_status[index_couple]] = r.hro;
Nodes[index_Node].mri[index_status[index_couple]] = r.mr;
for (int k = 0; k < 100; k++)
{
if (index_status[index_couple] < index_FullStatus[index_couple] - 1)//continue
{
index_Node = index_couple;
index_status[index_Node]++;
//i_end=Nodes[index_couple].N_out;
break;
}
else if (index_status[index_couple] == index_FullStatus[index_couple] - 1)//dp converge calculation
{
//DPconverge=DPConverge(Nodes[index_Node].mri,Nodes[index_Node].pri);
dPconverge = CheckDPforCircuits.CheckDPConverge2(hexType, iterforPri, Nodes[index_Node].mri, Nodes[index_Node].pri, Nodes[index_couple].pri[0], index_FullStatus[index_couple]);
iterforDP++;
if (dPconverge.flag == false)//need to be modified
{
Nodes[index_couple].mro = dPconverge.mr;
Nodes[index_couple].mr_ratio = dPconverge.mr_ratio;
index_DP[index_couple]++;
index_Node = index_couple;
index_status[index_Node] = 0;
//i_end=Nodes[index_Node].N_out;
break;
}
else if (dPconverge.flag == true)
{
index_DP[index_couple] = 1;
Nodes[index_couple].mr_ratio = dPconverge.mr_ratio;
double mr_sum = 0;
double tro_ave = 0;
double hro_ave = 0;
for (int ii = 0; ii < index_FullStatus[index_couple]; ii++)
{
mr_sum += Nodes[index_Node].mri[ii];
}
for (int ii = 0; ii < index_FullStatus[index_couple]; ii++)
{
tro_ave += Nodes[index_Node].mri[ii] * Nodes[index_Node].tri[ii];
hro_ave += Nodes[index_Node].mri[ii] * Nodes[index_Node].hri[ii];
}
Nodes[index_Node].mro[0] = mr_sum;
Nodes[index_Node].tro[0] = tro_ave / mr_sum;
Nodes[index_Node].hro[0] = hro_ave / mr_sum;
Nodes[index_Node].pro[0] = Nodes[index_Node].pri[0];
if (Nodes[index_Node].outType[0] == 0)//0:out is Node
{
index_last_Node = index_Node;
index_Node = SearchNode.FindNextNode(index_Node, 0, Nodes, N_Node);
if (Nodes[index_Node].type == 'C')
{
for (int ii = 0; ii < N_Node; ii++)
{
if (Nodes[ii].couple == Nodes[index_Node].couple && ii != index_Node)
{
index_couple = ii;
break;
}
}//Find the Couple Node
Nodes[index_Node].pri[index_status[index_couple]] = Nodes[index_last_Node].pro[0];
Nodes[index_Node].tri[index_status[index_couple]] = Nodes[index_last_Node].tro[0];
Nodes[index_Node].hri[index_status[index_couple]] = Nodes[index_last_Node].hro[0];
Nodes[index_Node].mri[index_status[index_couple]] = Nodes[index_last_Node].mro[0];
continue;
}
else if (Nodes[index_Node].type == 'D')
{
index_status[index_Node] = 0;
Nodes[index_Node].mri[0] = Nodes[index_last_Node].mro[0];
Nodes[index_Node].tri[0] = Nodes[index_last_Node].tro[0];
Nodes[index_Node].hri[0] = Nodes[index_last_Node].hro[0];
Nodes[index_Node].pri[0] = Nodes[index_last_Node].pro[0];
break;
}
}
else if (Nodes[index_Node].outType[0] == -1)
{
index_end = true;
break;
}
else//out is Circuit
{
break;
}
continue;
}
} //end if
} //end for
if (index_end == true)
{
break;
}
}
else if (Nodes[index_Node].type == 'E')//for 1 out case
{
Nodes[index_Node].pri[0] = r.Pro;
Nodes[index_Node].tri[0] = r.Tro;
Nodes[index_Node].hri[0] = r.hro;
Nodes[index_Node].mro[0] = r.mr;
Nodes[index_Node].pro[0] = r.Pro;
Nodes[index_Node].tro[0] = r.Tro;
Nodes[index_Node].hro[0] = r.hro;
Nodes[index_Node].mro[0] = r.mr;
break;
}
}//end out for
airConverge = CheckAirConvergeforCircuits.CheckAirConverge2(cirArrforAir.TotalDirection, Nrow, N_tube, Nelement, ta, RH, taout_calc, RHout_calc); //taout_calc, RHout_calc
ta = airConverge.ta;
RH = airConverge.RH;
iterforAir++;
} while (airConverge.flag == false && iterforAir < 50);
if (hexType == 0)
{
te_calc = CoolProp.PropsSI("T", "P", Nodes[index_Node].pro[0] * 1000, "Q", 0, fluid);
priconverge = CheckPin.CheckPriConverge(te, te_calc - 273.15, te_calc_org - 273.15, pri, pe, Nodes[index_Node].pro[0]); //res_slab.Pro
iterforPri++;
pri = priconverge.pri;
te_calc_org = te_calc;
if (priconverge.flag && iterforPri == 1)
{
priconverge.flag = false; //to avoid not even iterate but converge by chance
}
}
} while (priconverge.flag == false && iterforPri < 20);
//result print
if (iterforDP >= 200)
{
return(res_slab);
throw new Exception("iter for DPConverge > 200.");
}
if (iterforPri >= 50)
{
return(res_slab);
throw new Exception("iter for Pri > 50.");
}
#region result print
for (int i = 0; i < N_cir; i++)
{
res_slab.R_1 += res_cir[i].R_1 * CircuitInfo.TubeofCir[i];
res_slab.R_1a += res_cir[i].R_1a * CircuitInfo.TubeofCir[i];
res_slab.R_1r += res_cir[i].R_1r * CircuitInfo.TubeofCir[i];
}
for (int j = 0; j < N_tube; j++)//detail output
{
for (int k = 0; k < Nrow; k++)
{
res_slab.Q += Q_detail[j, k];
res_slab.M += charge_detail[j, k];
res_slab.href += href_detail[j, k];
}
}
res_slab.hro = Nodes[index_Node].hro[0];
res_slab.Pro = Nodes[index_Node].pro[0];
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;
te_calc = CoolProp.PropsSI("T", "P", res_slab.Pro * 1000, "Q", 0, fluid) - 273.15;
double densityLo = CoolProp.PropsSI("D", "T", te_calc + 273.15, "Q", 0, fluid);
double densityVo = CoolProp.PropsSI("D", "T", te_calc + 273.15, "Q", 1, fluid);
double hlo = CoolProp.PropsSI("H", "T", te_calc + 273.15, "D", densityLo, fluid) / 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);
double hli = CoolProp.PropsSI("H", "P", pri * 1000, "Q", 0, fluid) / 1000;
double hvi = CoolProp.PropsSI("H", "P", pri * 1000, "Q", 1, fluid) / 1000;
res_slab.x_i = (res_slab.hri - hli) / (hvi - hli);
res_slab.Tro = CoolProp.PropsSI("T", "P", res_slab.Pro * 1000, "H", res_slab.hro * 1000, fluid) - 273.15;
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;
#endregion
return(res_slab);
} //end function
static void Main(string[] args)
{
String s;
String option;
String s1;
Console.WriteLine("please enter the total pressure in atmosphere or bar");
s = Console.ReadLine();
double v = Convert.ToDouble(s);
Console.WriteLine("is the pressure in atmosphere or bar? if it is in atmosphere write atm and if it is in bar please enter bar");
s = Console.ReadLine();
if (s == "bar")
{
v = v * 0.986923267;
}
Console.WriteLine("please give tG in celcius");
s1 = Console.ReadLine();
double tg = Convert.ToDouble(s1);
Console.WriteLine("enter which parameter you would like to enter?");
Console.WriteLine("1. R.H");
Console.WriteLine("2. Absolute Humidity");
Console.WriteLine("3. wet temperature");
Console.WriteLine("4. humidity percentege");
Console.WriteLine("1 or 2 or 3 or 4?");
option = Console.ReadLine();
int option1 = Convert.ToInt32(option);
if (option1 == 1)
{
Console.WriteLine("enter R.H?");
double rh = Convert.ToDouble(Console.ReadLine());
double pa = (CoolProp.PropsSI("P", "T", tg + 273.15, "Q", 0, "Water") * 0.00986923267) / 1000;
double paprime = (rh / 100) * pa;
double yprime = ((paprime) / (v - paprime)) * 0.62;
double H = ((1005 + (1884 * yprime)) * tg) + (yprime * 2502300);
double vp = v * 101325;
double vh = 8315 * ((tg + 273) / vp) * (0.034 + (0.05 * yprime));
double tw = tg - 0.01;
l1 : double yprimew = (CoolProp.PropsSI("P", "T", tw + 273.15, "Q", 0, "Water") * 0.00986923267) / 1000;
double twprime = tg - ((2260 * (yprimew - yprime)) / 950);
if (twprime != tw)
{
tw = twprime;
goto l1;
}
double sum1 = ((yprimew) / (v - yprimew));
double percentage = (yprime / sum1) * 100;
Console.WriteLine("value of Absolute Humidity is " + yprime.ToString());
Console.WriteLine("value of wet temperature is " + tw.ToString());
Console.WriteLine("value of percent humidity is " + percentage.ToString());
Console.WriteLine("value of Humid Volume is " + vh.ToString());
Console.WriteLine("value of Enthalpy is " + H.ToString());
Console.WriteLine("value of partial pressure is " + paprime.ToString());
}
if (option1 == 2)
{
Console.WriteLine("enter Absolute Humidity?");
double yprime = Convert.ToDouble(Console.ReadLine());
double H = ((1005 + (1884 * yprime)) * tg) + (yprime * 2502300);
double vp = v * 101325;
double vh = 8315 * ((tg + 273) / vp) * (0.034 + (0.05 * yprime));
double paprime = (yprime * v) / (0.62 + yprime);
double t1 = ((CoolProp.PropsSI("P", "T", tg + 273.15, "Q", 0, "Water")) * 0.00986923267) / 1000;
double rh = (paprime / t1) * 100;
double tw = tg - 0.01;
l2 : double yprimew = (CoolProp.PropsSI("P", "T", tw + 273.15, "Q", 0, "Water") * 0.00986923267) / 1000;
double twprime = tg - ((2260 * (yprimew - yprime)) / 950);
if (twprime != tw)
{
tw = twprime;
goto l2;
}
double sum1 = ((yprimew) / (v - yprimew));
double percentage = (yprime / sum1) * 100;
//double percentage = (yprime / yprimew) * 100;
Console.WriteLine("value of R.H is " + rh.ToString());
Console.WriteLine("value of wet temperature is " + tw.ToString());
Console.WriteLine("value of percent humidity is " + percentage.ToString());
Console.WriteLine("value of Humid Volume is " + vh.ToString());
Console.WriteLine("value of Enthalpy is " + H.ToString());
Console.WriteLine("value of partial pressure is " + paprime.ToString());
}
if (option1 == 3)
{
Console.WriteLine("enter wet temperature?");
double tw = Convert.ToDouble(Console.ReadLine());
double yprimew = (CoolProp.PropsSI("P", "T", tw + 273.15, "Q", 0, "Water") * 0.00986923267) / 1000;
double yprime = (((tw - tg) * 950) / 2260) + yprimew;
double H = ((1005 + (1884 * yprime)) * tg) + (yprime * 2502300);
double vp = v * 101325;
double vh = 8315 * ((tg + 273) / vp) * (0.034 + (0.05 * yprime));
double paprime = (yprime * v) / (0.62 + yprime);
double t1 = (CoolProp.PropsSI("P", "T", tg + 273.15, "Q", 0, "Water") * 0.00986923267) / 1000;
double rh = (paprime / t1) * 100;
double sum1 = ((yprimew) / (v - yprimew));
double percentage = (yprime / sum1) * 100;
//double percentage = (yprime / yprimew) * 100;
Console.WriteLine("value of Absolute Humidity is " + yprime.ToString());
Console.WriteLine("value of R.H is " + rh.ToString());
Console.WriteLine("value of percent humidity is " + percentage.ToString());
Console.WriteLine("value of Humid Volume is " + vh.ToString());
Console.WriteLine("value of Enthalpy is " + H.ToString());
Console.WriteLine("value of partial pressure is " + paprime.ToString());
}
if (option1 == 4)
{
Console.WriteLine("enter humidity percentage?");
double percentage = Convert.ToDouble(Console.ReadLine());
double yprimew = (CoolProp.PropsSI("P", "T", tg + 273.15, "Q", 0, "Water") * 0.00986923267) / 1000;
double yprimes = (yprimew / (v - yprimew));
double yprime = (percentage / 100) * yprimes;
double H = ((1005 + (1884 * yprime)) * tg) + (yprime * 2502300);
double vp = v * 101325;
double vh = 8315 * ((tg + 273) / vp) * (0.034 + (0.05 * yprime));
double paprime = (yprime * v) / (0.62 + yprime);
double t1 = (CoolProp.PropsSI("P", "T", tg + 273.15, "Q", 0, "Water") * 0.00986923267) / 1000;
double rh = (paprime / t1) * 100;
double tw = tg - 0.01;
l3 : double yprimew1 = (CoolProp.PropsSI("P", "T", tw + 273.15, "Q", 0, "Water") * 0.00986923267) / 1000;
double twprime = tg - ((2260 * (yprimew1 - yprime)) / 950);
if (twprime != tw)
{
tw = twprime;
goto l3;
}
Console.WriteLine("value of Absolute Humidity is " + yprime.ToString());
Console.WriteLine("value of wet temperature is " + tw.ToString());
Console.WriteLine("value of R.H is " + rh.ToString());
Console.WriteLine("value of Humid Volume is " + vh.ToString());
Console.WriteLine("value of Enthalpy is " + H.ToString());
Console.WriteLine("value of partial pressure is " + paprime.ToString());
}
Console.WriteLine("please enter any key to exit");
Console.ReadKey();
}
public static decimal GetAcetoneBoilingPoint(decimal PressureInPa)
{
decimal BoilingPoint = Math.Round(Convert.ToDecimal(CoolProp.PropsSI("T", "P", Convert.ToDouble(PressureInPa), "Q", 0, "Acetone") - 273.15), 2);
return(BoilingPoint);
}
public static void ComputeAdditionalProperty(ref SystemInputStream _in, ref double AirX, ref double WaterX)
{
#region Variable declarations
const double Epsilon = 0.75;
//All properties are final state
double DensityWaterInitial;
double DensityAirInitial;
double MassFlowWaterFinal;
double MassFlowAirFinal;
double TWaterFinal;
double TAirFinal;
double TWaterMeanFinal;
double TAirMeanFinal;
double ViscosityAir;
double ViscosityWater;
double CpAir;
double CpWater;
double PrandtlAir;
double PrandtlWater;
double G_Air;
double G_Water;
double Reynolds_Air;
double Reynolds_Water;
double J_Water;
double F_Water;
double J_Air;
double F_Air;
double H_Water;
double H_Air;
double c7;
double c8;
double c9;
double VelocityAir;
double FinEfficiency;
double OverallEfficiency;
double Rw;
double UaInverse;
double C_Water;
double C_Air;
double C_Min;
double C_Star;
double NTU;
double epsilon;
double ConductionAreaWater;
double ConductionAreaAir;
double lambdaAir;
double lambdaWater;
double M1;
double M2;
double EpsilonRatio;
double deltaEpsilon;
double ActualEpsilon;
double HeatTransferRate;
double prevvalWater;
double prevvalAir;
#endregion
#region User Input acquisition
double L1 = _in.NumericalReadings.First(x => x.Parameter == "L1").Value;
double L2 = _in.NumericalReadings.First(x => x.Parameter == "L2").Value;
double L3 = _in.NumericalReadings.First(x => x.Parameter == "L3").Value;
double Xt = _in.NumericalReadings.First(x => x.Parameter == "Xt").Value;
double Xl = _in.NumericalReadings.First(x => x.Parameter == "Xl").Value;
double Do = _in.NumericalReadings.First(x => x.Parameter == "Do").Value;
double Di = _in.NumericalReadings.First(x => x.Parameter == "Di").Value;
double DelH = _in.NumericalReadings.First(x => x.Parameter == "DelH").Value;
double FinThickness = _in.NumericalReadings.First(x => x.Parameter == "FinThickness").Value;
double QWaterInitial = _in.NumericalReadings.First(x => x.Parameter == "QWaterInitial").Value;
double TWaterInitial = _in.NumericalReadings.First(x => x.Parameter == "TWaterInitial").Value;
double PWaterInitial = _in.NumericalReadings.First(x => x.Parameter == "PWaterInitial").Value;
double QAirInitial = _in.NumericalReadings.First(x => x.Parameter == "QAirInitial").Value;
double TAirInitial = _in.NumericalReadings.First(x => x.Parameter == "TAirInitial").Value;
double PAirInitial = _in.NumericalReadings.First(x => x.Parameter == "PAirInitial").Value;
//double Nr = _in.NumericalReadings.First(x => x.Parameter == "Nr").Value;
double FinPitch = _in.NumericalReadings.First(x => x.Parameter == "FinPitch").Value;
double Nr = L3 / Xt;
DensityWaterInitial = PWaterInitial / (287.04 * (TWaterInitial));
DensityAirInitial = PAirInitial / (287.04 * (TAirInitial));
MassFlowWaterFinal = QWaterInitial * DensityWaterInitial;
MassFlowAirFinal = QAirInitial * DensityAirInitial;
#endregion
#region Iteration
do
{
#region TMean calculation
TWaterFinal = TWaterInitial - Epsilon * (TWaterInitial - TAirInitial);
TAirFinal = TAirInitial + Epsilon * (MassFlowWaterFinal / MassFlowAirFinal) * (TWaterInitial - TAirInitial);
TWaterMeanFinal = (TWaterFinal + TWaterInitial) / 2;
TAirMeanFinal = (TAirFinal + TAirInitial) / 2;
#endregion
prevvalAir = TAirFinal;
prevvalWater = TWaterFinal;
#region CoolProp
//Calculate additional properties
ViscosityAir = CoolProp.PropsSI("V", "T", TAirMeanFinal, "P", 101325, "Air");
ViscosityWater = CoolProp.PropsSI("V", "T", TWaterMeanFinal, "P", 101325, "Water");
CpAir = CoolProp.PropsSI("CPMASS", "T", TWaterMeanFinal, "P", 101325, "Water");
CpWater = CoolProp.PropsSI("CPMASS", "T", TWaterMeanFinal, "P", 101325, "Water");
PrandtlAir = CoolProp.PropsSI("CPMASS", "T", TWaterMeanFinal, "P", 101325, "Water");
PrandtlWater = CoolProp.PropsSI("CPMASS", "T", TWaterMeanFinal, "P", 101325, "Water");
#endregion
#region Calculate G and Re
G_Air = MassFlowAirFinal /
((_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.TotalMinFfArea
: _in.TubeOutsideStaggered.TotalMinFfArea);
G_Water = MassFlowWaterFinal /
((_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.TotalMinFfArea
: _in.TubeOutsideStaggered.TotalMinFfArea);
Reynolds_Air = G_Air * ((_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.HydDiameter
: _in.TubeOutsideStaggered.HydDiameter) / ViscosityAir;
Reynolds_Water = G_Water * ((_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.HydDiameter
: _in.TubeOutsideStaggered.HydDiameter) / ViscosityWater;
#endregion
#region Calculation of J
if (Nr <= 1)
{
if (_in.SysType == SystemType.Inline)
{
double c1 = 1.9 - 0.23 * Math.Log(Reynolds_Water);
double c2 = -0.236 + 0.126 * Math.Log(Reynolds_Water);
J_Water = 0.108 * Math.Pow(Reynolds_Water, -0.29) * Math.Pow(Xt / Xl, c1) * Math.Pow(FinPitch / Do, 1.084) *
Math.Pow(FinPitch / _in.TubeOutsideInlineData.HydDiameter, -0.786) *
Math.Pow(FinPitch / Xt, c2);
c1 = 1.9 - 0.23 * Math.Log(Reynolds_Air);
c2 = -0.236 + 0.126 * Math.Log(Reynolds_Air);
J_Air = 0.108 * Math.Pow(Reynolds_Air, -0.29) * Math.Pow(Xt / Xl, c1) * Math.Pow(FinPitch / Do, 1.084) *
Math.Pow(FinPitch / _in.TubeOutsideInlineData.HydDiameter, -0.786) *
Math.Pow(FinPitch / Xt, c2);
}
else
{
double c1 = 1.9 - 0.23 * Math.Log(Reynolds_Water);
double c2 = -0.236 + 0.126 * Math.Log(Reynolds_Water);
J_Water = 0.108 * Math.Pow(Reynolds_Water, -0.29) * Math.Pow(Xt / Xl, c1) * Math.Pow(FinPitch / Do, 1.084) *
Math.Pow(FinPitch / _in.TubeOutsideStaggered.HydDiameter, -0.786) *
Math.Pow(FinPitch / Xt, c2);
c1 = 1.9 - 0.23 * Math.Log(Reynolds_Air);
c2 = -0.236 + 0.126 * Math.Log(Reynolds_Air);
J_Air = 0.108 * Math.Pow(Reynolds_Air, -0.29) * Math.Pow(Xt / Xl, c1) * Math.Pow(FinPitch / Do, 1.084) *
Math.Pow(FinPitch / _in.TubeOutsideStaggered.HydDiameter, -0.786) *
Math.Pow(FinPitch / Xt, c2);
}
}
else
{
if (_in.SysType == SystemType.Inline)
{
//Water
double c3 = -0.361 - 0.042 * Nr / Math.Log(Reynolds_Water) +
0.158 * Math.Log(Nr * Math.Pow(FinPitch / Do, 0.41));
double c4 = -1.224 -
0.076 * Math.Pow(Xl / _in.TubeOutsideInlineData.HydDiameter, 1.42) /
Math.Log(Reynolds_Water);
double c5 = -0.083 + 0.058 * Nr / Math.Log(Reynolds_Water);
double c6 = -5.735 + 1.21 * Math.Log(Reynolds_Water / Nr);
J_Water = 0.086 * Math.Pow(Reynolds_Water, c3) * Math.Pow(Nr, c4) * Math.Pow(FinPitch / Do, c5) *
Math.Pow(FinPitch / _in.TubeOutsideInlineData.HydDiameter, c6) *
Math.Pow(FinPitch / Xt, -0.93);
//Air
c3 = -0.361 - 0.042 * Nr / Math.Log(Reynolds_Air) + 0.158 * Math.Log(Nr * Math.Pow(FinPitch / Do, 0.41));
c4 = -1.224 -
0.076 * Math.Pow(Xl / _in.TubeOutsideInlineData.HydDiameter, 1.42) / Math.Log(Reynolds_Air);
c5 = -0.083 + 0.058 * Nr / Math.Log(Reynolds_Air);
c6 = -5.735 + 1.21 * Math.Log(Reynolds_Air / Nr);
J_Air = 0.086 * Math.Pow(Reynolds_Air, c3) * Math.Pow(Nr, c4) * Math.Pow(FinPitch / Do, c5) *
Math.Pow(FinPitch / _in.TubeOutsideInlineData.HydDiameter, c6) *
Math.Pow(FinPitch / Xt, -0.93);
}
else
{
//Water
double c3 = -0.361 - 0.042 * Nr / Math.Log(Reynolds_Water) +
0.158 * Math.Log(Nr * Math.Pow(FinPitch / Do, 0.41));
double c4 = -1.224 -
0.076 * Math.Pow(Xl / _in.TubeOutsideStaggered.HydDiameter, 1.42) /
Math.Log(Reynolds_Water);
double c5 = -0.083 + 0.058 * Nr / Math.Log(Reynolds_Water);
double c6 = -5.735 + 1.21 * Math.Log(Reynolds_Water / Nr);
J_Water = 0.086 * Math.Pow(Reynolds_Water, c3) * Math.Pow(Nr, c4) * Math.Pow(FinPitch / Do, c5) *
Math.Pow(FinPitch / _in.TubeOutsideStaggered.HydDiameter, c6) *
Math.Pow(FinPitch / Xt, -0.93);
//Air
c3 = -0.361 - 0.042 * Nr / Math.Log(Reynolds_Air) + 0.158 * Math.Log(Nr * Math.Pow(FinPitch / Do, 0.41));
c4 = -1.224 -
0.076 * Math.Pow(Xl / _in.TubeOutsideStaggered.HydDiameter, 1.42) / Math.Log(Reynolds_Air);
c5 = -0.083 + 0.058 * Nr / Math.Log(Reynolds_Air);
c6 = -5.735 + 1.21 * Math.Log(Reynolds_Air / Nr);
J_Air = 0.086 * Math.Pow(Reynolds_Air, c3) * Math.Pow(Nr, c4) * Math.Pow(FinPitch / Do, c5) *
Math.Pow(FinPitch / _in.TubeOutsideStaggered.HydDiameter, c6) * Math.Pow(FinPitch / Xt, -0.93);
}
}
#endregion
#region H Calculation
H_Water = J_Water * G_Water * CpWater / Math.Pow(PrandtlWater, (double)2 / 3);
H_Air = J_Air * G_Air * CpAir / Math.Pow(PrandtlAir, (double)2 / 3);
#endregion
#region F Calculation
c7 = -0.764 + 0.739 * Xt / Xl + 0.177 * FinPitch / Do - 0.00758 / Nr;
c8 = -15.689 + 64.021 / Math.Log(Reynolds_Water);
c9 = 1.696 - 15.695 / Math.Log(Reynolds_Water);
F_Water = 0.0267 * Math.Pow(Reynolds_Water, c7) * Math.Pow(Xt / Xl, c8) * Math.Pow(FinPitch / Do, c9);
c7 = -0.764 + 0.739 * Xt / Xl + 0.177 * FinPitch / Do - 0.00758 / Nr;
c8 = -15.689 + 64.021 / Math.Log(Reynolds_Air);
c9 = 1.696 - 15.695 / Math.Log(Reynolds_Air);
F_Air = 0.0267 * Math.Pow(Reynolds_Air, c7) * Math.Pow(Xt / Xl, c8) * Math.Pow(FinPitch / Do, c9);
#endregion
#region Fin Efficiency
VelocityAir = QAirInitial / (L1 * L3 - Nr * L1 * Do);
if (VelocityAir <= 15 && VelocityAir >= 6)
{
MessageBox.Show("Velocity should be between 6m/s and 15m/s", "Input out of limits");
return;
}
FinEfficiency = 7.41 * Math.Pow(VelocityAir, -0.12) *
Math.Pow(Xt / (2 * FinThickness), -2.32) * Math.Pow(Xl / (2 * FinThickness), -0.198);
OverallEfficiency = 1 - ((1 - FinEfficiency) * (L2 * L3 - _in.Nt * Math.PI * Do * Do) /
((_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.TotalHeatArea
: _in.TubeOutsideStaggered.TotalHeatArea));
Rw = (Do - Di) / (_in.MaterialCoeff * (_in.Nt + 1) * 2 * L1 * L2);
#endregion
#region UA Calculation
if (_in.SysType == SystemType.Inline)
{
UaInverse = Rw + (1 / (OverallEfficiency * H_Water * _in.TubeOutsideInlineData.TotalHeatArea)) +
(1 / (OverallEfficiency * H_Air * _in.TubeOutsideInlineData.TotalHeatArea));
}
else
{
UaInverse = Rw + (1 / (OverallEfficiency * H_Water * _in.TubeOutsideStaggered.TotalHeatArea)) +
(1 / (OverallEfficiency * H_Air * _in.TubeOutsideStaggered.TotalHeatArea));
}
C_Water = MassFlowWaterFinal * CpWater;
C_Air = MassFlowAirFinal * CpAir;
C_Min = Math.Min(C_Air, C_Water);
C_Star = (C_Water / C_Air);
if (C_Star > 1)
{
C_Star = 1 / C_Star;
}
NTU = 1 / (UaInverse * C_Min);
#endregion
epsilon = FactorialCompute(25, NTU, C_Star);
ConductionAreaWater = _in.Nt * Math.PI * Di * L1;
ConductionAreaAir = _in.Nt * Math.PI * Do * L1;
lambdaAir = _in.MaterialCoeff * ConductionAreaAir / (L1 * C_Air);
lambdaWater = _in.MaterialCoeff * ConductionAreaWater / (L1 * C_Water);
M1 = H_Air / H_Water;
M2 = lambdaWater / lambdaAir;
XPlatHelper.OpenImageTables();
while (true)
{
UserInputDialog userInput = new UserInputDialog("Enter Delta(Epsilon)/Epsilon");
userInput.ShowDialog();
if (!string.IsNullOrWhiteSpace(userInput.Answer))
{
double x;
if (double.TryParse(userInput.Answer, out x))
{
EpsilonRatio = x;
break;
}
}
}
deltaEpsilon = EpsilonRatio * Epsilon;
ActualEpsilon = Epsilon - deltaEpsilon;
HeatTransferRate = ActualEpsilon * (TAirInitial - TWaterInitial) * C_Min;
TWaterFinal = prevvalWater - HeatTransferRate / C_Water;
TAirFinal = prevvalAir - HeatTransferRate / C_Air;
} while (!((Math.Abs((prevvalWater - TWaterFinal) / prevvalWater) < 0.05) &&
(Math.Abs((prevvalAir - TAirFinal) / prevvalAir) < 0.05)));
#endregion
{
double TMeanAir = (TAirInitial + TAirFinal) / 2;
double TMeanWater = (TWaterInitial + TWaterFinal) / 2;
double RoFinalAir = (PAirInitial / 287.04) / TAirFinal;
double RoFinalWater = (PWaterInitial / 287.04) / TWaterFinal;
double RoMeanAir = 2 * RoFinalAir * DensityAirInitial / (RoFinalAir + DensityAirInitial);
double RoMeanWater = 2 * RoFinalWater * DensityWaterInitial / (RoFinalWater + DensityWaterInitial);
double RhFinal = (_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.TotalMinFfArea
: _in.TubeOutsideStaggered.TotalMinFfArea;
RhFinal /= 2;
double GAirFinal = MassFlowAirFinal / ((_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.TotalMinFfArea
: _in.TubeOutsideStaggered.TotalMinFfArea);
double GWaterFinal = MassFlowWaterFinal / ((_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.TotalMinFfArea
: _in.TubeOutsideStaggered.TotalMinFfArea);
XPlatHelper.OpenFinalTable();
double Kc, Ke;
while (true)
{
UserInputDialog userInput = new UserInputDialog("Enter Kc");
userInput.ShowDialog();
if (!string.IsNullOrWhiteSpace(userInput.Answer))
{
double x;
if (double.TryParse(userInput.Answer, out x))
{
Kc = x;
break;
}
}
}
while (true)
{
UserInputDialog userInput = new UserInputDialog("Enter Ke");
userInput.ShowDialog();
if (!string.IsNullOrWhiteSpace(userInput.Answer))
{
double x;
if (double.TryParse(userInput.Answer, out x))
{
Ke = x;
break;
}
}
}
double Sigma = (_in.SysType == SystemType.Inline)
? _in.TubeOutsideInlineData.RatioFfFrontalArea
: _in.TubeOutsideStaggered.RatioFfFrontalArea;
double delPAir =
Math.Pow(GAirFinal, 2) / (2 * DensityAirInitial) * (
(1 - Sigma * Sigma + Kc) + 2 * (DensityAirInitial / RoFinalAir - 1) +
(F_Air * L1 / RhFinal * DensityAirInitial / RoMeanAir)
- (1 - Sigma * Sigma - Ke * DensityAirInitial / RoFinalAir));
double delPWater =
Math.Pow(GWaterFinal, 2) / (2 * DensityWaterInitial) * (
(1 - Sigma * Sigma + Kc) + 2 * (DensityWaterInitial / RoFinalWater - 1) +
(F_Water * L1 / RhFinal * DensityWaterInitial / RoMeanWater)
- (1 - Sigma * Sigma - Ke * DensityWaterInitial / RoFinalWater));
AirX = delPAir;
WaterX = delPWater;
}
}