using "types";

#Sections of pipe

Model StraightLineEqual
	
	EQUATIONS
	
	# Ec. Bernoulli for smooth pipe without change in diameter. Area constant throughout the pipe.
	P2_out = P1_in + (g*Rho_Sln*Z1) - (g*Rho_Sln*Z2) - (Rho_Sln*Hf1_2); #J/kg*(kg/m^3) = N/m^2 = Pa
	
	# Pipe characteristics
	ALine = (Pi*D_Line^2)/4; # m
	VLine = (M_point/Rho_Sln)/ALine; #m/s
	
	#Reynolds number for pipe conditions	
	Re = (Rho_Sln*D_Line*VLine)/Mu_Sln; #dimensionless
	
		#Decision for Darcy factor value into Bernoullis equation
		#Laminar flow.
		if Re<2100 
		then
			fD=64/Re; 
			
		else
		#Turbulent flow.		
		#Shacham ecuation
		fD=(-2*log(((Epsilon/D_Line)/3.71)-((5.02/Re)*log(((Epsilon/D_Line)/3.71)+(14.5/Re)))))^(-2);
			
		end
	
	P1_in	= FlowLine_inlet.P_P;
	M_point = FlowLine_inlet.M_point;
	Rho_Sln = FlowLine_inlet.Rho_Sln;
	Mu_Sln	= FlowLine_inlet.Mu_Sln;
	
	
	#Total K factor from the pipe.
	K_Total = (L/D_Line)*fD;
	
	#Calculates total head losses in m2/s2 units	
	Hf1_2 = K_Total*((VLine^2)/2);
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowLine_outlet.P_P;
	M_point1 = FlowLine_outlet.M_point;
	Rho_Sln1 = FlowLine_outlet.Rho_Sln;
	Mu_Sln1	= FlowLine_outlet.Mu_Sln;
	
	
	PARAMETERS
	Pi 	as  Real 	  (Brief="Constant PI");
	g 	as  Real      (Brief="Gravity constant", Unit='m/s^2');
	D_Line as length (Brief="Diameter of Line 1"); #Unit='m'
	L as length (Brief="length of Line 1"); #Unit='m'
	Epsilon as Real (Brief="Roughness abs Line 1", Unit='m');
	Z1 as length (Brief="height of Line 1"); #Unit='m'
	Z2 as length (Brief="height of Line 2"); #Unit='m'
	
	
	SET
	Pi			=3.1416;
	g			=9.8*'m/s^2';
	
	
	VARIABLES
	in FlowLine_inlet as StreamProcess (Brief="Process Stream");
	DeltaP	as	Real (Brief="losses pressure", Unit='Pa');	
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');	
	M_point	as 	flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	#in  P_Exit as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	
	out FlowLine_outlet as StreamProcess (Brief="Process Stream");
	P2_out 	 as  pressure  (Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	M_point1 as  flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln1	 as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'	
	#out P_Exit1 as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	
		ALine		as 	area      (Brief = "Flow area of...1");  #Unit='m^2'
		VLine	as 	velocity  (Brief="velocity inside the line 2"); #Unit='m/s'
		Re	as 	positive  (Brief="Reynolds number for this line section 1"); #Dimensionless
		Hf1_2 as Real (Brief="Total head losses of the line plus fittings", Unit='m^2/s^2');
		K_Total as Real  (Brief="K factor for the straight lines 1");
		fD as positive (Brief="Darcy factor for friction in descending Overflow line", Unit='Pa/Pa',Lower=-0.00001, Upper=5); #Dimensionless 
end


Model StreamProcess

	VARIABLES
	
	P_P as pressure(Brief="discharge pressure of pump", DisplayUnit='Pa');#Unit='atm'
	M_point as flow_mass(Brief="Mass flow solution"); #kg/s
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	
end


#Fittings

Model ElbowModel45

	#*Tips for selecction the elbows characteristics in accordance with algorithm
 * - if your elbow is standard, you must select in the parameters section: 
 * 				Standard = 1
 *				Weld = 0
 *				Long_R = 0
 *
 * - if your elbow is Long-Radius, you must select in the parameters section: 
 *				Standard = 0
 *				Weld = 0
 *   			Long_R = 1 
 *
 * - if your elbow is mitered, you must specify the angle welding in the parameters section: 
 *				Standard = 0
 *				Weld = 45° or 22.5°
 *   			Long_R = 0
*#

	EQUATIONS
	#Conversion of units of inches at meter
	D_m = (ID*0.0254*'m'); 
	
	#Fitting characteristics
	AFit = (Pi*(D_m^2))/4;
	V_Fit = (M_point/Rho_Sln)/AFit; #m/s
	
	#Reynolds number for fittings conditions	
	Re = (Rho_Sln*D_m*V_Fit)/Mu_Sln; #dimensionless
	
	#Selection of K values in agrrement with elbows characteristics
	
	if Standard equal 1
	then
		K1 = 500;
		Kinf = 0.2;
		
	else 
	
		if Long_R equal 1
		then
			K1 = 500;
			Kinf = 0.15;
			
		else 
		
			if Weld equal 45
			then
				K1 = 500;
				Kinf = 0.25;
			
			else 
				K1 = 500;
				Kinf = 0.15;
			end
		end
	end	
	
	P1_in	= FlowElbow45_inlet.P_P;
	M_point = FlowElbow45_inlet.M_point;
	Rho_Sln = FlowElbow45_inlet.Rho_Sln;
	Mu_Sln	= FlowElbow45_inlet.Mu_Sln;
	
	#Equation for determine the K factor of elbow. 
	K_elbow = (K1/Re)+(Kinf*(1 + (1/ID)));	
	
	#Equation for determine losses in elbows
	H_f = K_elbow*((V_Fit^2)/2);
	
	#Bernoulli Equation 
	P2_out = P1_in - (Rho_Sln*H_f);
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowElbow45_outlet.P_P;
	M_point1 = FlowElbow45_outlet.M_point;
	Rho_Sln1 = FlowElbow45_outlet.Rho_Sln;
	Mu_Sln1	= FlowElbow45_outlet.Mu_Sln;
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Standard as positive (Brief=" Values of 0 and 1, 0 when there is no, 1 when there is");
	Long_R as positive (Brief=" Values of 0 and 1, 0 when there is no, 1 when there is");
	Weld as positive (Brief=" angle when the elbow is welded ");
	

	SET
	Pi =3.1416;
	
	
	VARIABLES
	in FlowElbow45_inlet as StreamProcess (Brief="Process Stream");
	M_point as flow_mass(Brief="Mass flow solution"); #kg/s
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'	
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');
	
	out FlowElbow45_outlet as StreamProcess (Brief="Process Stream");
	M_point1 as  flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Mu_Sln1	 as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	P2_out as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	DeltaP  as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	
	K_elbow as Real (Brief="K Factor elbow"); #Dimensionless
	D_m as length (Brief="Diameter in meter"); #m
	ID as Real (Brief="diameter in Inches"); #Inches
	Re as positive (Brief="Reynolds number"); #Dimensionless
	K1 as positive (Brief="K1 values of 2K Method"); #Dimensionless
	Kinf as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
	V_Fit as velocity (Brief="Velocity in the fitting"); #m/s
	AFit as area (Brief = "Flow area");  #Unit='m^2'
	H_f as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');
	
end


Model ElbowModel90

	#*Tips for selecction the elbows characteristics in accordance with algorithm
 * - if your elbow is standard and Screwed, you must select in the parameters section: 
 * 				Standard = 1
 *				Screwed = 1
 *				Weld = 0
 *				Long_R = 0
 *
 * - if your elbow is standard and welded, you must select in the parameters section: 
 * 				Standard = 1
 *				Screwed = 0
 *				Weld = 0
 *				Long_R = 0
 *
 * - if your elbow is Long-Radius, you must select in the parameters section: 
 *				Standard = 0
 *				Screwed = 0
 *				Weld = 0
 *				Long_R = 1
 *
 * - if your elbow is mitered, you must specify the angle welding in the parameters section: 
 *				Standard = 0
 *				Screwed = 0
 *				Weld = 90°, 45°, 30°, 22.5° or 18°
 *				Long_R = 1
*#

	EQUATIONS	
	#Conversion of units of inches at meter
	D_m = (ID*0.0254*'m'); 
	
	#Fitting characteristics
	AFit = (Pi*(D_m^2))/4;
	V_Fit = (M_point/Rho_Sln)/AFit; #m/s
	
	#Reynolds number for fittings conditions	
	Re = (Rho_Sln*D_m*V_Fit)/Mu_Sln; #dimensionless
	
	#Selection of K values in agrrement with elbows characteristics
	
	if Standard equal 1 
	then
			if Screwed equal 1
			then
				K1 = 800;
				Kinf = 0.4;
			else 
				K1 = 800;
				Kinf = 0.25;
			end
	else 
			
			if Long_R equal 1
			then
				K1 = 800;
				Kinf = 0.2;
			else
		
				if Weld equal 90
				then
					K1 = 1000;
					Kinf = 1.15;
				else
				
					if Weld equal 45
					then
						K1 = 800;
						Kinf = 0.35;
					else
				
						if Weld equal 30
						then
							K1 = 800;
							Kinf = 0.3;
						else
				
							if Weld equal 22.5
							then
								K1 = 800;
								Kinf = 0.27;
							else
				
							K1 = 800;
							Kinf = 0.25;
							end
						end
					end
				end			
			end
	end
	
	P1_in	= FlowElbow_inlet.P_P;
	M_point = FlowElbow_inlet.M_point;
	Rho_Sln = FlowElbow_inlet.Rho_Sln;
	Mu_Sln	= FlowElbow_inlet.Mu_Sln;
	
	
	#Equation for determine the K factor of elbow. 
	K_elbow = (K1/Re)+(Kinf*(1 + (1/ID)));	
	
	#Equation for determine losses in elbows
	H_f = K_elbow*((V_Fit^2)/2);
	
	#Bernoulli Equation 
	P2_out = P1_in - (Rho_Sln*H_f);
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowElbow_outlet.P_P;
	M_point1 = FlowElbow_outlet.M_point;
	Rho_Sln1 = FlowElbow_outlet.Rho_Sln;
	Mu_Sln1	= FlowElbow_outlet.Mu_Sln;
	
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Standard as positive (Brief=" Values of 0 and 1, 0 when there is no, 1 when there is");
	Screwed as positive (Brief=" Values of 0 and 1, 0 when there is no, 1 when there is");
	Long_R as positive (Brief=" Values of 0 and 1, 0 when there is no, 1 when there is");
	Weld as positive (Brief=" angle when the elbow is welded ");

	SET
	Pi =3.1416;
	
	
	VARIABLES
	in FlowElbow_inlet as StreamProcess (Brief="Process Stream");
	M_point as flow_mass(Brief="Mass flow solution"); #kg/s
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'	
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');
	
	out FlowElbow_outlet as StreamProcess (Brief="Process Stream");
	M_point1 as  flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Mu_Sln1	 as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	P2_out as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	DeltaP  as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	
	
	K_elbow as Real (Brief="K Factor elbow"); #Dimensionless
	D_m as length (Brief="Diameter in meter"); #m
	ID as Real (Brief="diameter in Inches"); #Inches
	Re as positive (Brief="Reynolds number"); #Dimensionless
	K1 as positive (Brief="K1 values of 2K Method"); #Dimensionless
	Kinf as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
	V_Fit as velocity (Brief="Velocity in the fitting"); #m/s
	AFit as area (Brief = "Flow area");  #Unit='m^2'	
	H_f as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');

end


Model ElbowModel180

	#*Tips for selecction the elbows characteristics in accordance with algorithm
 * - if your elbow is standard and Screwed, you must select in the parameters section: 
 * 				Standard = 1
 *				Screwed = 1
 *				Long_R = 0
 * - if your elbow is standard and welded, you must select in the parameters section: 
 *				Standard = 1
 *				Screwed = 0
 *   			Long_R = 0
 * - if your elbow is Long-Radius, you must select in the parameters section: 
 *				Standard = 0
 *				Screwed = 0
 *   			Long_R = 1
 *
*#

	EQUATIONS
	#Conversion of units of inches at meter
	D_m = (ID*0.0254*'m'); 
	
	#Fitting characteristics
	AFit = (Pi*(D_m^2))/4;
	V_Fit = (M_point/Rho_Sln)/AFit; #m/s
	
	#Reynolds number for fittings conditions	
	Re = (Rho_Sln*D_m*V_Fit)/Mu_Sln; #dimensionless
	
	#Selection of K values in agrrement with elbows characteristics
	
	if Standard equal 1
	then
		
		if Screwed equal 1
		then
			K1 = 1000;
			Kinf = 0.6;
		else
			K1 = 1000;
			Kinf = 0.35;
		end
	else
		#if Long_R equal 1
		#then
			K1 = 1000;
			Kinf = 0.3;
		#end
	end
	
	#Equation for determine the K factor of elbow. 
	K_elbow = (K1/Re)+(Kinf*(1 + (1/ID)));	
	
	P1_in	= FlowElbow180_inlet.P_P;
	M_point = FlowElbow180_inlet.M_point;
	Rho_Sln = FlowElbow180_inlet.Rho_Sln;
	Mu_Sln	= FlowElbow180_inlet.Mu_Sln;
	
	#Equation for determine losses in elbows
	H_f = K_elbow*((V_Fit^2)/2);
	
	#Bernoulli Equation 
	P2_out = P1_in - (Rho_Sln*H_f);
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowElbow180_outlet.P_P;
	M_point1 = FlowElbow180_outlet.M_point;
	Rho_Sln1 = FlowElbow180_outlet.Rho_Sln;
	Mu_Sln1	= FlowElbow180_outlet.Mu_Sln;
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Standard as positive (Brief=" Values of 0 and 1, 0 when there is no, 1 when there is");
	Long_R as positive (Brief=" Values of 0 and 1, 0 when there is no, 1 when there is");
	Screwed as positive (Brief=" angle when the elbow is welded ");
	

	SET
	Pi =3.1416;

	
	VARIABLES
	in FlowElbow180_inlet as StreamProcess (Brief="Process Stream");
	M_point as flow_mass(Brief="Mass flow solution"); #kg/s
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'	
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');
	
	out FlowElbow180_outlet as StreamProcess (Brief="Process Stream");
	M_point1 as  flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Mu_Sln1	 as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	P2_out as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	DeltaP  as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	
	K_elbow as Real (Brief="K Factor elbow"); #Dimensionless
	D_m as length (Brief="Diameter in meter"); #m
	ID as Real (Brief="diameter in Inches"); #Inches
	Re as positive (Brief="Reynolds number"); #Dimensionless
	K1 as positive (Brief="K1 values of 2K Method"); #Dimensionless
	Kinf as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
	V_Fit as velocity (Brief="Velocity in the fitting"); #m/s
	AFit as area (Brief = "Flow area");  #Unit='m^2'
	H_f as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');
	
end


Model SuddenChange

	EQUATIONS
	# This equation evaluates output pressure of this fitting taken from a Mechanical Energy
	# Balance taken from point1=fitting input and point 2=fitting output
	P2_out = P1_in +(g*Rho_Sln*(Z1-Z2)) + (Rho_Sln*alpha1*((V1_in^2)/2)) 
				- (Rho_Sln*alpha2*((V2_out^2)/2)) - (Rho_Sln*Hf1_2);
	
	# Point 1 characteristics
	A1Line = (Pi*D1_in^2)/4; # m
	V1_in = (M_point/Rho_Sln)/A1Line; #m/s
	
	# Point 2 characteristics
	A2Line = (Pi*D2_out^2)/4; # m
	V2_out = (M_point/Rho_Sln)/A2Line; #m/s
	
	#Reynolds number for point 1 (input) conditions
	Re1 = (Rho_Sln*D1_in*V1_in)/Mu_Sln; #dimensionless

		#Decision for alpha value into Bernoullis equation
		if Re1<2100
		then
			alpha1=2; #Alpha for laminar flow
			
		else
			alpha1=1.01; #Alpha for turbulent flow
			
		end
	
	#Reynolds number for point 2 (output) conditions
	Re2 = (Rho_Sln*D2_out*V2_out)/Mu_Sln; #dimensionless
	
		#Decision for alpha value into Bernoullis equation
		if Re2<2100
		then
			alpha2=2; #Alpha for laminar flow
			
		else
			alpha2=1.01; #Alpha for turbulent flow
			
		end
	
	#Decision between Contraction or Expansion
	
		if (D1_in>D2_out)
		then	
	
			#factor K for gradual contraction	
			K_Sub = 0.5*((1-((D2_out/D1_in)^2))^2) ;
			#Contraction losses
			Hf1_2 = K_Sub*((V2_out^2)/2);
		
		else
		
			# Calculation of gradual expansion
			#factor K for expansion contraction
			K_Sub = ((1-((D2_out/D1_in)^2))^2);	
			#Expansion losses
			Hf1_2 = K_Sub*((V2_out^2)/2);
		
		end
	
	P1_in	= FlowSudden_inlet.P_P;
	M_point = FlowSudden_inlet.M_point;
	Rho_Sln = FlowSudden_inlet.Rho_Sln;
	Mu_Sln	= FlowSudden_inlet.Mu_Sln;
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP =  (P1_in - P2_out);
	
	P2_out	= FlowSudden_outlet.P_P;
	M_point1 = FlowSudden_outlet.M_point;
	Rho_Sln1 = FlowSudden_outlet.Rho_Sln;
	Mu_Sln1	= FlowSudden_outlet.Mu_Sln;
	

	PARAMETERS	
	Pi 	as  Real 	  (Brief="Constant PI");
	g 	as  Real      (Brief="Gravity constant", Unit='m/s^2');
	D2_out as length (Brief="Diameter of Line 2"); #Unit='m'
	D1_in as length (Brief="Diameter of line 1"); #Unit='m'
	Z1 as length (Brief="height of point 1"); #Unit='m'
	Z2 as length (Brief="height of point 2"); #Unit='m'
	

	SET
	Pi			=3.1416;
	g			=9.8*'m/s^2';
	
	VARIABLES
	in FlowSudden_inlet as StreamProcess (Brief="Process Stream");
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');	
	M_point as flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	DeltaP as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');

	out FlowSudden_outlet as StreamProcess (Brief="Process Stream");
	P2_out as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	M_point1 as flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Mu_Sln1	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'	
	
	Re1 as positive(Brief="Reynolds number for this line section 1"); #Dimensionless
	Re2 as positive(Brief="Reynolds number for this line section 1"); #Dimensionless
	Hf1_2 as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');
	K_Sub as Real  (Brief="K factor for the straight lines 1");
	alpha1	as 	positive  (Brief="speed correction factor 1"); #Dimensionless
	alpha2	as 	positive  (Brief="speed correction factor 2"); #Dimensionless
	A1Line		as 	area      (Brief = "Flow area of...1");  #Unit='m^2'
	V1_in	as 	velocity  (Brief="velocity inside the line 1"); #Unit='m/s'
	A2Line		as 	area      (Brief = "Flow area of...1");  #Unit='m^2'
	V2_out	as 	velocity  (Brief="velocity inside the line 1"); #Unit='m/s'
	
end


Model GradualChange

	EQUATIONS
	# This equation evaluates output pressure of this fitting taken from a Mechanical Energy
	# Balance taken from point1=fitting input and point 2=fitting output
	P2_out = P1_in +(g*Rho_Sln*(Z1-Z2)) + (Rho_Sln*alpha1*((V1_in^2)/2)) 
				- (Rho_Sln*alpha2*((V2_out^2)/2)) - (Rho_Sln*Hf1_2);
	
	# Point 1 characteristics
	A1Line = (Pi*D1_in^2)/4; # m
	V1_in = (M_point/Rho_Sln)/A1Line; #m/s
	
	# Point 2 characteristics
	A2Line = (Pi*D2_out^2)/4; # m
	V2_out = (M_point/Rho_Sln)/A2Line; #m/s
	
	#Reynolds number for point 1 (input) conditions
	Re1 = (Rho_Sln*D1_in*V1_in)/Mu_Sln; #dimensionless

		#Decision for alpha value into Bernoullis equation
		if Re1<2100
		then
			alpha1=2; #Alpha for laminar flow
			
		else
			alpha1=1.01; #Alpha for turbulent flow
			
		end
	
	#Reynolds number for point 2 (output) conditions
	Re2 = (Rho_Sln*D2_out*V2_out)/Mu_Sln; #dimensionless
	
		#Decision for alpha value into Bernoullis equation
		if Re2<2100
		then
			alpha2=2; #Alpha for laminar flow
			
		else
			alpha2=1.01; #Alpha for turbulent flow
			
		end
	
	#Decision between Contraction or Expansion
	
		if (D1_in>D2_out)
		then	
	
			#Cat_1 = Cateto opuesto --- FiitingL = Cateto adyacente
	
			Cat_1 = (D1_in/2) - (D2_out/2);
			Hip_T = sqrt((Cat_1^2) + (FiitingL^2)); 
			#Ang = (asin((Cat_1/Hip_T)))/1.57079632679e-2;
	
				if Ang>(45/(2*3.1416))*'rad'   and Ang<(180/(2*3.1416))*'rad'
				then
					C_g = sqrt(sin(Ang/2));
				else
					C_g = 1.6*sin(Ang/2);
				end
	
			#factor K for gradual contraction	
			K_Gradual = C_g*((1-((D2_out/D1_in)^2))^2);
			#Contraction losses
			Hf1_2 = K_Gradual*((V1_in^2)/2);
		
		else
		
			# Calculation of gradual expansion
			Cat_1 = (D1_in/2) - (D2_out/2);
			#Cat_1 = Cateto opuesto --- FiitingL = Cateto adyacente
			Hip_T = sqrt((Cat_1^2) + (FiitingL^2)); 	
		
				if Ang>(45/(2*3.1416))*'rad' and Ang<(180/(2*3.1416))*'rad'
				then
					C_g = 1.0;
				else
					C_g = 2.6*sin(Ang/2);
				end		
		
			#factor K for expansion contraction
			K_Gradual = C_g*((1-((D1_in/D2_out)^2))^2);	
			#Expansion losses
			Hf1_2 = K_Gradual*((V1_in^2)/2);
		
		end
	
	P1_in	= FlowGradChange_inlet.P_P;
	M_point = FlowGradChange_inlet.M_point;
	Rho_Sln = FlowGradChange_inlet.Rho_Sln;
	Mu_Sln	= FlowGradChange_inlet.Mu_Sln;
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowGradChange_outlet.P_P;
	M_point1 = FlowGradChange_outlet.M_point;
	Rho_Sln1 = FlowGradChange_outlet.Rho_Sln;
	Mu_Sln1	= FlowGradChange_outlet.Mu_Sln;
	

	PARAMETERS	
	Pi 	as  Real 	  (Brief="Constant PI");
	g 	as  Real      (Brief="Gravity constant", Unit='m/s^2');
	D2_out as length (Brief="Diameter of Line 2"); #Unit='m'
	D1_in as length (Brief="Diameter of line 1"); #Unit='m'
	Z1 as length (Brief="height of point 1"); #Unit='m'
	Z2 as length (Brief="height of point 2"); #Unit='m'
	FiitingL as length (Brief="Total lenght between input and output areas of fitting"); #Unit='m'
	Ang as angle (Brief="Contraction angle"); #Rad
	
	
	SET
	Pi			=3.1416;
	g			=9.8*'m/s^2';
	
	VARIABLES
	in FlowGradChange_inlet as StreamProcess (Brief="Process Stream");
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');	
	M_point as flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	
	out FlowGradChange_outlet as StreamProcess (Brief="Process Stream");
	P2_out as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	M_point1 as flow_mass(Brief="Mass flow of entrace");  #Unit='kg/s'
	Mu_Sln1	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'	
	
	DeltaP   as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	Cat_1 as Real (Brief="opposite of leg of the triangle", Unit='m'); #m
	Re1 as positive(Brief="Reynolds number for this line section 1"); #Dimensionless
	Re2 as positive(Brief="Reynolds number for this line section 1"); #Dimensionless
	Hf1_2 as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');
	K_Gradual as Real  (Brief="K factor for the straight lines 1");
	alpha1	as 	positive  (Brief="speed correction factor 1"); #Dimensionless
	alpha2	as 	positive  (Brief="speed correction factor 2"); #Dimensionless
	C_g	as 	Real  (Brief="contraction correction factor"); #Dimensionless
	Hip_T as length (Brief="hypothenuse of the triangle contraction");   #Unit='m'	
	A1Line		as 	area      (Brief = "Flow area of...1");  #Unit='m^2'
	V1_in	as 	velocity  (Brief="velocity inside the line 1"); #Unit='m/s'
	A2Line		as 	area      (Brief = "Flow area of...1");  #Unit='m^2'
	V2_out	as 	velocity  (Brief="velocity inside the line 1"); #Unit='m/s'
	
	
end


Model TeeModelThrough


	EQUATIONS
	
	#Bernoulli Equation 
	P2_out = P1_in - (Rho_Sln*H_f);
	
	#Equation for Pressure losses in Tee
	H_f = K_thro*((V_Fit^2)/2);
	
	#Factor K equation.
	K_thro = (K1/Re)+(Kinf*(1 + (1/ID)));	
	
	#Conversion of units of inches at meter
	D_m = (ID*0.0254*'m'); 
	
	#Fitting characteristics
	AFit = (Pi*(D_m^2))/4;
	V_Fit = (M_point/Rho_Sln)/AFit; #m/s
	
	#Reynolds number for fittings conditions	
	Re = (Rho_Sln*D_m*V_Fit)/Mu_Sln; #dimensionless
	
	#Selection of K values in agrrement with elbows characteristics
	
	if Screwed equal 1 
		then
			K1 = 200;
			Kinf = 0.1;
	else 
	
		if Welded equal 1
			then
				K1 = 150;
				Kinf = 0.5;
		else
		
			K1 = 100;
			Kinf = 0;
		end
	end
	
	P1_in	= FlowTee_inlet.P_P;
	M_point = FlowTee_inlet.M_point;
	Rho_Sln = FlowTee_inlet.Rho_Sln;
	Mu_Sln	= FlowTee_inlet.Mu_Sln;
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowTee_outlet.P_P;
	M_point1 = FlowTee_outlet.M_point;
	Rho_Sln1 = FlowTee_outlet.Rho_Sln;
	Mu_Sln1	= FlowTee_outlet.Mu_Sln;
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Screwed as positive(Brief="Characteristic of Tee, Posible values: 1 or 0");
	Welded as positive(Brief="Characteristic of Tee, Posible values: 1 or 0");

	SET
	Pi =3.1416;
	
	
	VARIABLES
	in FlowTee_inlet as StreamProcess (Brief="Process Stream");
	M_point	as 	flow_mass (Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'	
	Rho_Sln  as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	DeltaP   as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	
	
	out FlowTee_outlet as StreamProcess (Brief="Process Stream");
	Mu_Sln1	 as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	P2_out   as  pressure  (Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');	
	M_point1 as  flow_mass (Brief="Mass flow of entrace");  #Unit='kg/s'	
	
	
		K_thro as Real (Brief="K Factor Tee"); #Dimensionless
		D_m as length (Brief="Diameter in meter"); #m
		ID as Real (Brief="diameter in Inches"); #Inches
		Re as positive (Brief="Reynolds number"); #Dimensionless
		K1 as positive (Brief="K1 values of 2K Method"); #Dimensionless
		Kinf as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
		V_Fit as velocity (Brief="Velocity in the fitting"); #m/s
		AFit as area (Brief = "Flow area");  #Unit='m^2'
		H_f as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');
	
	
	
end


Model TeeModelElbow

	#*Tips for selecction the Tee characteristics in accordance with algorithm
 * - if your Tee is Satndard and Screwed, you must select in the parameters section: 
 * 				Standard = 1
 *				Screwed = 1
 *				Welded = 0
 *				Long_R = 0
 *
 * - if your Tee is Satndard and Welded, you must select in the parameters section: 
 * 				Standard = 1
 *				Screwed = 0
 *				Welded = 1
 *				Long_R = 0
 *
 * - if your Tee is Long-radius and Screwed, you must select in the parameters section: 
 *				Standard = 0
 *				Screwed = 0
 *				Welded = 0
 *				Long_R = 1
 *				
 * - if your Tee is stub in type branch, you must select in the parameters section: 
 *				Standard = 0
 *				Screwed = 0
 *				Welded = 0
 *				Long_R = 0
 *#

	EQUATIONS
	
	#Bernoulli Equation 
	P2_out = P1_in - (Rho_Sln*H_f);
	
	#Equation for Pressure losses in Tee
	H_f = K_TaE*((V_Fit^2)/2);
	
	#Factor K equation.
	K_TaE = (K1/Re)+(Kinf*(1 + (1/ID)));	
	
	#Conversion of units of inches at meter
	D_m = (ID*0.0254*'m'); 
	
	#Fitting characteristics
	AFit = (Pi*(D_m^2))/4;
	V_Fit = (M_point/Rho_Sln)/AFit; #m/s
	
	#Reynolds number for fittings conditions	
	Re = (Rho_Sln*D_m*V_Fit)/Mu_Sln; #dimensionless
	
	P1_in	= FlowTeeElbow_inlet.P_P;
	M_point = FlowTeeElbow_inlet.M_point;
	Rho_Sln = FlowTeeElbow_inlet.Rho_Sln;
	Mu_Sln	= FlowTeeElbow_inlet.Mu_Sln;
	
	#Selection of K values in agrrement with elbows characteristics
	
	if Standard equal 1 
	then
		if Screwed equal 1
			then
			K1 = 500;
			Kinf = 0.7;
		else 
			K1 = 800;
			Kinf = 0.8;
		end
	else 
		
		if Long_R equal 1
			then
			K1 = 800;
			Kinf = 0.4;
		else 
			K1 = 1000;
			Kinf = 1;
		end
	end
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowTeeElbow_outlet.P_P;
	M_point1 = FlowTeeElbow_outlet.M_point;
	Rho_Sln1 = FlowTeeElbow_outlet.Rho_Sln;
	Mu_Sln1	= FlowTeeElbow_outlet.Mu_Sln;
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Screwed as positive(Brief="Characteristic of Tee, Posible values: 1 or 0");
	Welded as positive(Brief="Characteristic of Tee, Posible values: 1 or 0");
	Standard as positive(Brief="Characteristic of Tee, Posible values: 1 or 0");
	Long_R as positive(Brief="Characteristic of Tee, Posible values: 1 or 0");


	SET
	Pi =3.1416;
	
	
	VARIABLES
	in FlowTeeElbow_inlet as StreamProcess (Brief="Process Stream");
	M_point	as 	flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');
	
	DeltaP   as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	
	out FlowTeeElbow_outlet as StreamProcess (Brief="Process Stream");
	P2_out as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');	
	M_point1 as flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln1  as viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	
	K_TaE as Real (Brief="K Factor Tee"); #Dimensionless
	D_m as length (Brief="Diameter in meter"); #m
	ID as Real (Brief="diameter in Inches"); #Inches
	Re as positive (Brief="Reynolds number"); #Dimensionless
	K1 as positive (Brief="K1 values of 2K Method"); #Dimensionless
	Kinf as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
	V_Fit as velocity (Brief="Velocity in the fitting"); #m/s
	AFit as area (Brief = "Flow area");  #Unit='m^2'	
	H_f as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');
	
end


Model ValveModelGate


	EQUATIONS
	
	#Conversion of units of inches at meter
	D_m = (ID*0.0254*'m'); 
	
	#Fitting characteristics
	AFit = (Pi*(D_m^2))/4;
	V_Fit = (M_point/Rho_Sln)/AFit; #m/s
	
	#Reynolds number for fittings conditions	
	Re = (Rho_Sln*D_m*V_Fit)/Mu_Sln; #dimensionless
	
	#Selection of K values in agrrement with elbows characteristics
	
	if Beta equal 1 
		then
			K1 = 300;
			Kinf = 0.1;
	else 
	
		if Beta equal 0.9
			then
				K1 = 500;
				Kinf = 0.15;
		else
		
			K1 = 1000;
			Kinf = 0.25;
		end
	end
	
	#Bernoulli Equation 
	P2_out = P1_in - (Rho_Sln*H_f);
	
	#Factor K equation.
	K_100 = (K1/Re)+(Kinf*(1 + (1/ID)));	
	
	#Correction for the valve aperture
	
	if Aperture equal 100
		then
			K_valG = 1*K_100;
	else
	
		K_valG = (5e-6*(Aperture^(-3.31)))*K_100;
	end
	
	P1_in	= FlowGate_inlet.P_P;
	M_point = FlowGate_inlet.M_point;
	Rho_Sln = FlowGate_inlet.Rho_Sln;
	Mu_Sln	= FlowGate_inlet.Mu_Sln;
	
	#Equation for Pressure losses in Tee
	H_f = K_valG*((V_Fit^2)/2);
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowGate_outlet.P_P;
	M_point1 = FlowGate_outlet.M_point;
	Rho_Sln1 = FlowGate_outlet.Rho_Sln;
	Mu_Sln1	= FlowGate_outlet.Mu_Sln;
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Beta as positive(Brief="Characteristic of valve, Posible values: 1.0, 0.9 or 0.8");
	Aperture as positive(Brief="Characteristic of valve, Posible values: 100, 75, 50 or 25");

	SET
	Pi =3.1416;
	
	
	VARIABLES
	in FlowGate_inlet as StreamProcess (Brief="Process Stream");
	M_point	as 	flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln  as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');
	DeltaP   as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	
	out FlowGate_outlet as StreamProcess (Brief="Process Stream");
	P2_out   as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');	
	M_point1 as flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln1  as viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	

	K_valG as Real (Brief="K Factor valve"); #Dimensionless
	K_100 as Real (Brief="K Factor valve"); #Dimensionless
	D_m as length (Brief="Diameter in meter"); #m
	ID as Real (Brief="diameter in Inches"); #Inches
	Re as positive (Brief="Reynolds number"); #Dimensionless
	K1 as positive (Brief="K1 values of 2K Method"); #Dimensionless
	Kinf as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
	V_Fit as velocity (Brief="Velocity in the fitting"); #m/s
	AFit as area (Brief = "Flow area");  #Unit='m^2'	
	H_f as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');

end


Model ValveModelGlobe

	EQUATIONS
	
	#Conversion of units of inches at meter
	D_m = (ID*0.0254*'m'); 
	
	#Fitting characteristics
	AFit = (Pi*(D_m^2))/4;
	V_Fit = (M_point/Rho_Sln)/AFit; #m/s
	
	#Reynolds number for fittings conditions	
	Re = (Rho_Sln*D_m*V_Fit)/Mu_Sln; #dimensionless
	
	#Selection of K values in agrrement with elbows characteristics
	
	if Standard equal 1 
		then
			K1 = 1500;
			Kinf = 4;
	else 
	
		if Butterfly equal 1
			then
				K1 = 800;
				Kinf = 0.25;
		else
		
			if Y_type equal 1
				then
					K1 = 1000;
					Kinf = 2;
			else
				K1 = 1000;
				Kinf = 2;
			end
		end
	end
	
	#Bernoulli Equation 
	P2_out = P1_in - (Rho_Sln*H_f);
	
	#Factor K equation.
	K_100 = (K1/Re)+(Kinf*(1 + (1/ID)));	
	
	#Correction for the valve aperture
	
	if Aperture equal 100
		then
			K_valGl = 1*K_100;
	else
	
		K_valGl = (1061*(Aperture^(-1.51)))*K_100;
	end
	
	P1_in	= FlowGlobe_inlet.P_P;
	M_point = FlowGlobe_inlet.M_point;
	Rho_Sln = FlowGlobe_inlet.Rho_Sln;
	Mu_Sln	= FlowGlobe_inlet.Mu_Sln;	
	
	#Equation for Pressure losses in Tee
	H_f = K_valGl*((V_Fit^2)/2);
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowGlobe_outlet.P_P;
	M_point1 = FlowGlobe_outlet.M_point;
	Rho_Sln1 = FlowGlobe_outlet.Rho_Sln;
	Mu_Sln1	= FlowGlobe_outlet.Mu_Sln;
	
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Butterfly as positive(Brief="Characteristic of valve, Posible values: 1 or 0");
	Standard as positive(Brief="Characteristic of valve, Posible values: 1 or 0");
	Y_type as positive(Brief="Characteristic of valve, Posible values: 1 or 0");
	Aperture as positive(Brief="Characteristic of valve, Posible values: 100, 75, 50 or 25");

	SET
	Pi =3.1416;
	
	
	VARIABLES
	in FlowGlobe_inlet as StreamProcess (Brief="Process Stream");
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');
	M_point	as 	flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln  as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	DeltaP as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');	
	
	out FlowGlobe_outlet as StreamProcess (Brief="Process Stream");
	P2_out   as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	M_point1 as	flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln1	 as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	
	
	K_valGl as Real (Brief="K Factor valve"); #Dimensionless
	K_100 as Real (Brief="K Factor valve"); #Dimensionless
	D_m as length (Brief="Diameter in meter"); #m
	ID as Real (Brief="diameter in Inches"); #Inches
	Re as positive (Brief="Reynolds number"); #Dimensionless
	K1 as positive (Brief="K1 values of 2K Method"); #Dimensionless
	Kinf as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
	V_Fit as velocity (Brief="Velocity in the fitting"); #m/s
	AFit as area (Brief = "Flow area");  #Unit='m^2'
	H_f as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');
end


Model ValveModelCheck


	EQUATIONS
	
	#Conversion of units of inches at meter
	D_m = (ID*0.0254*'m'); 
	
	#Fitting characteristics
	AFit = (Pi*(D_m^2))/4;
	V_Fit = (M_point/Rho_Sln)/AFit; #m/s
	
	#Reynolds number for fittings conditions	
	Re = (Rho_Sln*D_m*V_Fit)/Mu_Sln; #dimensionless
	
	#Selection of K values in agrrement with elbows characteristics
	
	if Lift equal 1 
		then
			K1 = 2000;
			Kinf = 10;
	else 
	
		if Swing equal 1
			then
				K1 = 1500;
				Kinf = 1.5;
		else
		
			K1 = 1000;
			Kinf = 0.5;
		end
	end
	
	P1_in	= FlowCheck_inlet.P_P;
	M_point = FlowCheck_inlet.M_point;
	Rho_Sln = FlowCheck_inlet.Rho_Sln;
	Mu_Sln	= FlowCheck_inlet.Mu_Sln;	
	
	#Bernoulli Equation 
	P2_out = P1_in - (Rho_Sln*H_f);
	
	#Factor K equation.
	K_valC = (K1/Re)+(Kinf*(1 + (1/ID)));	
	
	#Equation for Pressure losses in Tee
	H_f = K_valC*((V_Fit^2)/2);
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowCheck_outlet.P_P;
	M_point1 = FlowCheck_outlet.M_point;
	Rho_Sln1 = FlowCheck_outlet.Rho_Sln;
	Mu_Sln1	= FlowCheck_outlet.Mu_Sln;
	
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Swing as positive(Brief="Characteristic of valve, Posible values: 1.0, 0.9 or 0.8");
	Lift as positive(Brief="Characteristic of valve, Posible values: 100, 75, 50 or 25");
	

	SET
	Pi =3.1416;
	
	
	VARIABLES
	in FlowCheck_inlet as StreamProcess (Brief="Process Stream");   
	P1_in	as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');	
	M_point	as 	flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	DeltaP as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	
	out FlowCheck_outlet as StreamProcess (Brief="Process Stream");
	P2_out as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	M_point1 as flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln1	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	
	K_valC as Real (Brief="K Factor valve"); #Dimensionless
	D_m as length (Brief="Diameter in meter"); #m
	Re as positive (Brief="Reynolds number"); #Dimensionless
	K1 as positive (Brief="K1 values of 2K Method"); #Dimensionless
	Kinf as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
	V_Fit as velocity (Brief="Velocity in the fitting"); #m/s
	AFit as area (Brief = "Flow area");  #Unit='m^2'
	H_f as Real (Brief="Total head losses of the contraction", Unit='m^2/s^2');
	ID as Real (Brief="diameter in Inches"); #Inches
	
end


#Driving Machines

Model ModelPump

	EQUATIONS

	P_Suc = FlowPump_inlet.P_P;
	M_point = FlowPump_inlet.M_point;
	Rho_Sln = FlowPump_inlet.Rho_Sln;
	Mu_Sln = FlowPump_inlet.Mu_Sln;
	
	#Ec. Bernoulli for determine discharge pressure of pump.
	P_dis = P_Suc + ((Rho_Sln/M_point)*(Pump_Eff*Pump_Pow));
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P_Suc - P_dis);
	
	P_dis 	= FlowPump_outlet.P_P;
	M_point1 = FlowPump_outlet.M_point;
	Rho_Sln1 = FlowPump_outlet.Rho_Sln;
	Mu_Sln1	= FlowPump_outlet.Mu_Sln;
	
	PARAMETERS
	Pump_Eff as fraction(Brief="Pump eficience as fraction 0 to 1");
	Pump_Pow as power(Brief="Pump power in kW");
	
	VARIABLES
	#Variables externas
	in FlowPump_inlet as StreamProcess (Brief="Process Stream");
	out FlowPump_outlet as StreamProcess (Brief="Process Stream");
	
	#Variables de transicion
	P_Suc as pressure(Brief="discharge pressure of pump", DisplayUnit='Pa');#Unit='atm'
	M_point as flow_mass(Brief="Mass flow solution"); #kg/s
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	DeltaP   as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');	
	
	P_dis as pressure(Brief="discharge pressure of pump", DisplayUnit='Pa');#Unit='atm'
	M_point1 as flow_mass(Brief="Mass flow solution"); #kg/s
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln1	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'	

end


Model PowerPump

	EQUATIONS
	
	P_Suc = FlowPowerPump_inlet.P_P;
	M_point = FlowPowerPump_inlet.M_point;
	Rho_Sln = FlowPowerPump_inlet.Rho_Sln;
	Mu_Sln = FlowPowerPump_inlet.Mu_Sln;
	
	#Ec. Bernoulli for determine power pump.
	Pump_Pow = ((M_point/(Rho_Sln*Pump_Eff))*(P_dis-P_Suc)); 
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P_Suc - P_dis);
	
	P_dis 	= FlowPowerPump_outlet.P_P;
	M_point1 = FlowPowerPump_outlet.M_point;
	Rho_Sln1 = FlowPowerPump_outlet.Rho_Sln;
	Mu_Sln1	= FlowPowerPump_outlet.Mu_Sln;
	
	
	PARAMETERS
	Pump_Eff as fraction(Brief="Pump eficience as fraction 0 to 1");
	
	
	VARIABLES
	#Variables externas
	in FlowPowerPump_inlet as StreamProcess (Brief="Process Stream");
	out FlowPowerPump_outlet as StreamProcess (Brief="Process Stream");
	
	DeltaP   as  Real  (Brief="pressure at the outlet of the pipe 1", Unit='Pa');
	Pump_Pow as power(Brief="Pump power in kW");
	
	P_Suc as pressure(Brief="discharge pressure of pump", DisplayUnit='Pa');#Unit='atm'
	M_point as flow_mass(Brief="Mass flow solution"); #kg/s
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	
	P_dis as pressure(Brief="discharge pressure of pump", DisplayUnit='Pa');#Unit='atm'
	M_point1 as flow_mass(Brief="Mass flow solution"); #kg/s
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln1	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP

end


Model Tank1LModel

	EQUATIONS
	P2_out = P1_in + (Rho_Sln*g*(Z1-Z2)) - (Rho_Sln*Alpha*((Vexit^2)/2)) - (Rho_Sln*Hf1_2);
	
	V = Area_T*H_Tank;
	Area_T = (Pi*(Dtank^2))/4;
	ALine = (Pi*(DLine^2))/4;	
	Vexit = (M_point/Rho_Sln)/ALine; #m/s
	
	#Reynolds number for pipe conditions	
	Re = (Rho_Sln*DLine*Vexit)/Mu_Sln; #dimensionless
	
	#Decision for alpha value into Bernoullis equation
		if Re<2100
		then
			Alpha=2; #Alpha for laminar flow
			
		else
			Alpha=1.01; #Alpha for turbulent flow
			
		end
	
	
	if incoming equal 1
	then 
		Ktank = 0.8;
		
	else
		if straight equal 1
		then
			Ktank = 0.5;
		
		else
			Ktank = 0.2;
			
		end
	end	
	
	Hf1_2 = Ktank*((Vexit^2)/2);
	
	M_point1 = M_point;
	Rho_Sln1 = Rho_Sln;
	Mu_Sln1 = Mu_Sln;
	
	DeltaP = (P1_in - P2_out);
	
	P2_out	= FlowTank_outlet.P_P;
	M_point1 = FlowTank_outlet.M_point;
	Rho_Sln1 = FlowTank_outlet.Rho_Sln;
	Mu_Sln1	= FlowTank_outlet.Mu_Sln;
	
	
	PARAMETERS
	Pi 	as  Real (Brief="Constant PI");
	Dtank as length (Brief="Tank Diameter"); #Unit='m'
	DLine as length (Brief="Tank Diameter"); #Unit='m' 
	g 	as  Real (Brief="Gravity constant", Unit='m/s^2');
	H_Tank as length (Brief="Tank Diameter"); #Unit='m'
	
	
	VARIABLES
	Area_T as area(Brief="Cross section area");
	ALine as area(Brief="Cross section area");
	V as volume (Brief="The model volume");
	Z1 as length (Brief="height of Line 1"); #Unit='m'
	Z2 as length (Brief="height of Line 2"); #Unit='m'
	M_point as flow_mass(Brief="mass flow of entrace");  #Unit='m^3/s'
	Vexit as velocity  (Brief="velocity inside the line 2"); #Unit='m/s'
	Ktank as positive (Brief="Kinfinite values of 2K Method"); #Dimensionless
	incoming as positive(Brief="Characteristic of exit tank");
	straight as positive(Brief="Characteristic of exit tank");
	P1_in  as  pressure  (Brief="pressure at the outlet of the pipe 1", DisplayUnit='Pa');
	Rho_Sln as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	Mu_Sln	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Hf1_2 as Real (Brief="Total head losses of the line plus fittings", Unit='m^2/s^2');
	Alpha	as 	positive  (Brief="speed correction factor 1"); #Dimensionless	
	Re as positive(Brief="Reynolds number for this line section 1"); #Dimensionless
	
	DeltaP	as	Real (Brief="losses pressure", Unit='Pa');	
	
	out FlowTank_outlet as StreamProcess (Brief="Process Stream");
	P2_out as pressure(Brief="pressure at the outlet of the pipe 2", DisplayUnit='Pa');
	M_point1 as flow_mass(Brief="Mass flow of entrace", Lower= 0.0005, Upper= 18000);  #Unit='kg/s'
	Mu_Sln1	as  viscosity (Brief="Viscosity of the Sln"); #Unit='cP'
	Rho_Sln1 as  dens_mass (Brief="Density of the Sln");  #Unit='kg/m^3'
	
	
end