public RateBasedSection Ignore(params string[] components)
{
foreach (var compId in components)
{
var comp = System.Components.FirstOrDefault(c => c.ID == compId);
if (comp != null)
{
IgnoredComponents.Add(comp);
}
}
return(this);
}
void ApplyIgnoredComponents()
{
int NT = (int)(NumberOfElements);
for (int c = 0; c < System.Components.Count; c++)
{
if (IgnoredComponents.Contains(System.Components[c]))
{
for (int i = 0; i < NT; i++)
{
_trays[i].x[c].FixValue(0);
_trays[i].y[c].FixValue(0);
_trays[i].yI[c].FixValue(0);
_trays[i].xI[c].FixValue(0);
_trays[i].x[c].IsConstant = true;
_trays[i].y[c].IsConstant = true;
_trays[i].yI[c].IsConstant = true;
_trays[i].xI[c].IsConstant = true;
}
}
}
}
public override void FillEquationSystem(EquationSystem problem)
{
int NC = System.Components.Count;
var VIn = FindMaterialPort("VIn").Streams[0];
var LIn = FindMaterialPort("LIn").Streams[0];
var VOut = FindMaterialPort("VOut").Streams[0];
var LOut = FindMaterialPort("LOut").Streams[0];
var pscale = 1e4;
var hscale = 1e6;
var L0 = LIn.Mixed.TotalMolarflow;
var x0 = LIn.Mixed.ComponentMolarFraction;
var VNT = VIn.Mixed.TotalMolarflow;
var yNT = VIn.Mixed.ComponentMolarFraction;
ApplyIgnoredComponents();
Action <Equation> EQ = (x) => AddEquationToEquationSystem(problem, x);
for (var i = 0; i < NumberOfElements; i++)
{
var tray = _trays[i];
//Calculate average properties on stage, Divide molar weight by 1000 because unit is kg/kmol and not kg/mol as would be SI
var TV = tray.TV;
var p = tray.p;
var rhoVMolar = System.EquationFactory.GetAverageVaporDensityExpression(System, TV, p, tray.y.ToList());
var rhoV = rhoVMolar * System.EquationFactory.GetAverageMolarWeightExpression(System, tray.y);
var etaV = System.EquationFactory.GetAverageVaporViscosityExpression(System, tray.y, TV, p);
var A = Math.PI / 4 * Sym.Pow(tray.d, 2);
//Hydraulics
//Effective exchange area
EQ(tray.aeff.IsEqualTo(tray.h * A * tray.aspez));
//Superficial velocity
EQ(tray.uV.IsEqualTo(tray.V / (rhoVMolar * A)));
//Reynolds number
tray.ReV.BindTo(rhoV * tray.uV * tray.dhyd / etaV);
//Component (M)assbalance
for (var comp = 0; comp < NC; comp++)
{
if (!IgnoredComponents.Contains(System.Components[comp]))
{
if (i == 0)
{
EQ((tray.V * tray.y[comp] - _trays[i + 1].V * _trays[i + 1].y[comp] + tray.N[comp]).IsEqualTo(0));
EQ((tray.L * tray.x[comp] - L0 * x0[comp] - _trays[i].N[comp]).IsEqualTo(0));
}
else if (i == NumberOfElements - 1)
{
EQ((tray.V * tray.y[comp] - VNT * yNT[comp] + _trays[i].N[comp]).IsEqualTo(0));
EQ((tray.L * tray.x[comp] - _trays[i - 1].L * _trays[i - 1].x[comp] - tray.N[comp]).IsEqualTo(0));
}
else
{
EQ((tray.V * tray.y[comp] - _trays[i + 1].V * _trays[i + 1].y[comp] + tray.N[comp]).IsEqualTo(0));
EQ((tray.L * tray.x[comp] - _trays[i - 1].L * _trays[i - 1].x[comp] - tray.N[comp]).IsEqualTo(0));
}
}
}
//(E)quilibrium
for (var comp = 0; comp < NC; comp++)
{
System.EquationFactory.EquilibriumCoefficient(System, tray.K[comp], tray.TI, p, tray.xI.ToList(), tray.yI.ToList(), comp);
if (!IgnoredComponents.Contains(System.Components[comp]))
{
EQ((tray.yI[comp]).IsEqualTo(tray.K[comp] * tray.xI[comp]));
}
}
//(R)ate Equation - Intefacial Mass Transfer
for (var comp = 0; comp < NC; comp++)
{
if (!IgnoredComponents.Contains(System.Components[comp]))
{
if (NoContact)
{
EQ((_trays[i].N[comp]).IsEqualTo(0));
EQ((_trays[i].xI[comp]).IsEqualTo(tray.x[comp]));
}
else
{
if (!_massTransferResistanceOnLiquid)
{
EQ((_trays[i].xI[comp]).IsEqualTo(tray.x[comp]));
}
else
{
var x = tray.x;
var xI = tray.xI;
var n = tray.N;
var ii = comp;
var xiiq = 0.5 * Sym.Par(x[ii] + xI[ii]);
EQ((rhoVMolar * _trays[i].aeff * Sym.Par(tray.xI[ii] - tray.x[ii])).IsEqualTo(Sym.SumX(0, NC, comp, j => (0.5 * Sym.Par(x[j] + xI[j]) * n[ii] - xiiq * n[j]) / tray.BetaL[ii, j])));
}
if (!_massTransferResistanceOnVapor)
{
EQ((_trays[i].yI[comp]).IsEqualTo(tray.y[comp]));
}
else
{
//Simplified Stefan-Maxwell Equation for Film model
var y = tray.y;
var yI = tray.yI;
var n = tray.N;
var ii = comp;
var yiiq = 0.5 * Sym.Par(y[ii] + yI[ii]);
EQ((rhoVMolar * _trays[i].aeff * Sym.Par(tray.y[ii] - tray.yI[ii])).IsEqualTo(Sym.SumX(0, NC, comp, j => (0.5 * Sym.Par(y[j] + yI[j]) * n[ii] - yiiq * n[j]) / tray.BetaV[ii, j])));
}
}
}
}
//Heat Transfer coefficient calcluation
if (!BetaVIsConstant)
{
for (int k = 0; k < NC; k++)
{
for (int j = 0; j < NC; j++)
{
if (k != j)
{
var parameterSet = System.BinaryParameters.FirstOrDefault(ps => ps.Name == "DVIJ0");
if (parameterSet == null)
{
throw new ArgumentNullException("No Diffusion coefficients defined");
}
//Estimate Diffusion coefficient at system temperature and pressure using the approach by Fuller, Schettler, Giddings
var DVij0 = parameterSet.Matrices["A"][k, j];
var DVij = Sym.Pow(Sym.Par(TV / 273.15), 1.75) / (p / 1e5) * DVij0;
//Schmidt Number
var Scij = etaV / Sym.Par(rhoV * DVij);
//Sherwood Number
var Shij = SherwoodParameter[0] * Sym.Pow(tray.ReV, SherwoodParameter[1]) * Sym.Pow(Scij, SherwoodParameter[2]);
tray.BetaV[k, j].BindTo(Shij * DVij / tray.dhyd);
}
else
{
tray.BetaV[k, j].BindTo(0);
}
}
}
}
//(R)ate Equation - Interfacial Heat Transfer
if (NoContact)
{
EQ((tray.E).IsEqualTo(0));
EQ((tray.TI).IsEqualTo(0.5 * Sym.Par(tray.TL + tray.TV)));
}
else
{
if (!_heatTransferResistanceOnLiquid)
{
EQ((tray.TI).IsEqualTo(tray.TL));
}
if (!_heatTransferResistanceOnVapor)
{
EQ((tray.TI).IsEqualTo(tray.TV));
}
}
//(S)ummation
EQ(Sym.Sum(0, NC, (j) => Sym.Par(tray.x[j])).IsEqualTo(1));
EQ(Sym.Sum(0, NC, (j) => Sym.Par(tray.y[j])).IsEqualTo(1));
//Ent(H)alpy
tray.HL.BindTo(Sym.Sum(0, NC, (idx) => tray.x[idx] * System.EquationFactory.GetLiquidEnthalpyExpression(System, idx, tray.TL)));
tray.HV.BindTo(Sym.Sum(0, NC, (idx) => tray.y[idx] * System.EquationFactory.GetVaporEnthalpyExpression(System, idx, tray.TV)));
if (i == 0)
{
EQ((Sym.Par(_trays[i].V * _trays[i].HV - _trays[i + 1].V * _trays[i + 1].HV + _trays[i].E) / hscale).IsEqualTo(0));
EQ((Sym.Par(_trays[i].L * _trays[i].HL - L0 * LIn.Mixed.SpecificEnthalpy - _trays[i].E + tray.Q) / hscale).IsEqualTo(0));
}
else if (i == NumberOfElements - 1)
{
EQ((Sym.Par(_trays[i].V * _trays[i].HV - VNT * VIn.Mixed.SpecificEnthalpy + _trays[i].E) / hscale).IsEqualTo(0));
EQ((Sym.Par(_trays[i].L * _trays[i].HL - _trays[i - 1].L * _trays[i - 1].HL - _trays[i].E + tray.Q) / hscale).IsEqualTo(0));
}
else
{
EQ((Sym.Par(_trays[i].V * _trays[i].HV - _trays[i + 1].V * _trays[i + 1].HV + _trays[i].E) / hscale).IsEqualTo(0));
EQ((Sym.Par(_trays[i].L * _trays[i].HL - _trays[i - 1].L * _trays[i - 1].HL - _trays[i].E + tray.Q) / hscale).IsEqualTo(0));
}
//Pressure profile
if (i == NumberOfElements - 1)
{
EQ((tray.p / pscale).IsEqualTo((VIn.Mixed.Pressure - _trays[NumberOfElements - 1].DP) / pscale));
}
else
{
EQ((tray.p / pscale).IsEqualTo(Sym.Par(_trays[i + 1].p - _trays[i].DP) / pscale));
}
}
//Setting outlet stream conditions
for (var comp = 0; comp < NC; comp++)
{
EQ(VOut.Mixed.ComponentMolarflow[comp].IsEqualTo(_trays[0].V * _trays[0].y[comp]));
EQ(LOut.Mixed.ComponentMolarflow[comp].IsEqualTo(_trays[NumberOfElements - 1].L * _trays[NumberOfElements - 1].x[comp]));
}
EQ((VOut.Mixed.SpecificEnthalpy / 1e6).IsEqualTo(_trays[0].HV / 1e6));
EQ(VOut.Mixed.Pressure.IsEqualTo(_trays[0].p));
EQ(LOut.Mixed.Temperature.IsEqualTo(_trays[NumberOfElements - 1].TL));
EQ(LOut.Mixed.Pressure.IsEqualTo(_trays[NumberOfElements - 1].p));
base.FillEquationSystem(problem);
}
