#*----------------------------------------------------------------------
* File containg models of columns: distillation, stripping, absorbers
* rectifier, ....
*
* The default nomenclature is:
*		Type_Column_reboilertype_condensertyper
*
* where:
*	Type = refluxed or reboiled or section
*	Column = Stripping, Absorption, Rectifier, Distillation
*	Reboiler type (if exists) = kettle or thermosyphon 
*	Condenser type (if exists) = with subccoling or without subcooling
* 
*-----------------------------------------------------------------------
* Author: Paula B. Staudt
* $Id: column.mso 1 2006-06-20 17:33:53Z rafael $
*---------------------------------------------------------------------*#

using "tray";
using "reboiler";
using "condenser";
using "mixers_splitters/splitter";
using "tank";
using "pressure_changers/pump";

#*----------------------------------------------------------------------
* Model of a  column section with:
*	- NTrays=number of trays trays.
* 
*---------------------------------------------------------------------*# 
Model Section_Column
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;

	EQUATIONS
	"Pressure Drop through the tray"
	trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * 
		trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P -
		trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV));
	
	CONNECTIONS
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
end


#*----------------------------------------------------------------------
* Model of a  distillation column containing:
*	- NTrays like tray;
*	- a kettle reboiler;
*	- dymamic condenser;
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream;
*---------------------------------------------------------------------*# 
Model Distillation_kettle_cond
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenser;
	reb as reboiler;
	sp as splitter;
	pump1 as pump;

	EQUATIONS
	if (reb.OutletV.P > reb.InletL.P) then
		"Pressure Drop through the tray"
		reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P)
				/ (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3
	else
		"Prato selado"
		reb.OutletV.F = 0.0 * "mol/s";
	end

	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	reb.OutletV to trays([NTrays]).InletV;
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;

	#liquid
	cond.OutletL to sp.Inlet;	
	sp.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	trays(NTrays).OutletL to reb.InletL;
end


#* -------------------------------------------------------------------
* Distillation Column model with:
*
*	- NTrays like tray;
*	- a vessel in the bottom of column;
*	- a splitter who separate the bottom product and the stream to reboiler;
*	- steady state reboiler (thermosyphon);
*	- a steady state condenser with subcooling;
*	- a vessel drum (layed cilinder);
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream.
*
* ------------------------------------------------------------------*#
Model Distillation_thermosyphon_subcooling
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenserSteady;
	reb as reboilerSteady;
	tbottom as tank;
	ttop as tank_cylindrical;
	spbottom as splitter;
	sptop as splitter;
	pump1 as pump;

	EQUATIONS
	if (reb.OutletV.P > reb.InletL.P) then
		"Pressure Drop through the tray"
		reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P)
				/ (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3
	else
		"Prato selado"
		reb.OutletV.F = 0.0 * "mol/s";
	end

	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	reb.OutletV to trays(NTrays).InletV;
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;
	
	#liquid
	cond.OutletL to ttop.Inlet;
	ttop.Outlet to sptop.Inlet;	
	sptop.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	trays(NTrays).OutletL to tbottom.Inlet;
	tbottom.Outlet to spbottom.Inlet;
	spbottom.Outlet2 to reb.InletL;
end


#* -------------------------------------------------------------------
* Distillation Column model with:
*
*	- NTrays like tray;
*	- a vessel in the bottom of column;
*	- a splitter who separate the bottom product and the stream to reboiler;
*	- steady state reboiler (thermosyphon);
*	- a dynamic condenser without subcooling;
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream.
*
* ------------------------------------------------------------------*#
Model Distillation_thermosyphon_cond
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenser;
	reb as reboilerSteady;
	tbottom as tank;
	spbottom as splitter;
	sptop as splitter;
	pump1 as pump;

	EQUATIONS
	if (reb.OutletV.P > reb.InletL.P) then
		"Pressure Drop through the tray"
		reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P)
				/ (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3
	else
		"Prato selado"
		reb.OutletV.F = 0.0 * "mol/s";
	end

	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
			
	CONNECTIONS
	#vapor
	reb.OutletV to trays(NTrays).InletV;
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;
	
	#liquid
	cond.OutletL to sptop.Inlet;	
	sptop.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	trays(NTrays).OutletL to tbottom.Inlet;
	tbottom.Outlet to spbottom.Inlet;
	spbottom.Outlet2 to reb.InletL;
end


#* -------------------------------------------------------------------
* Distillation Column model with:
*
*	- NTrays like tray;
*	- a kettle reboiler;
*	- a steady state condenser with subcooling;
*	- a vessel drum (layed cilinder);
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream.
*
* ------------------------------------------------------------------*#
Model Distillation_kettle_subcooling
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenserSteady;
	reb as reboiler;
	ttop as tank_cylindrical;
	sptop as splitter;
	pump1 as pump;

	EQUATIONS
	if (reb.OutletV.P > reb.InletL.P) then
		"Pressure Drop through the tray"
		reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P)
				/ (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3
	else
		"Prato selado"
		reb.OutletV.F = 0.0 * "mol/s";
	end

	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	reb.OutletV to trays(NTrays).InletV;
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;
	
	#liquid
	cond.OutletL to ttop.Inlet;
	ttop.Outlet to sptop.Inlet;	
	sptop.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	trays(NTrays).OutletL to reb.InletL;
end


#*----------------------------------------------------------------------
* Model of a  rectifier containing:
*	- NTrays like tray;
*	- dymamic condenser without subcooling;
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream;
*---------------------------------------------------------------------*# 
Model Rectifier
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenser;
	sp as splitter;
	pump1 as pump;

	EQUATIONS
	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;

	#liquid
	cond.OutletL to sp.Inlet;	
	sp.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
end


#* -------------------------------------------------------------------
* Rectifier Column with:
*
*	- NTrays like tray;
*	- a steady state condenser with subcooling;
*	- a vessel drum (layed cilinder);
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream.
*
* ------------------------------------------------------------------*#
Model Rectifier_subcooling
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenserSteady;
	ttop as tank_cylindrical;
	sptop as splitter;
	pump1 as pump;

	EQUATIONS
	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;
	
	#liquid
	cond.OutletL to ttop.Inlet;
	ttop.Outlet to sptop.Inlet;	
	sptop.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
end


#*----------------------------------------------------------------------
* Model of a  Refluxed Stripping column containing:
*	- NTrays like tray;
*	- dymamic condenser without subcooling;
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream;
*---------------------------------------------------------------------*# 
Model Refluxed_Stripping
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenser;
	sp as splitter;
	pump1 as pump;

	EQUATIONS
	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;

	#liquid
	cond.OutletL to sp.Inlet;	
	sp.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
end


#* -------------------------------------------------------------------
* Refluxed Stripping Column with:
*
*	- NTrays like tray;
*	- a steady state condenser (with subcooling);
*	- a vessel drum (layed cilinder);
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream.
*
* ------------------------------------------------------------------*#
Model Refluxed_Stripping_subcooling
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenserSteady;
	ttop as tank_cylindrical;
	sptop as splitter;
	pump1 as pump;

	EQUATIONS
	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;
	
	#liquid
	cond.OutletL to ttop.Inlet;
	ttop.Outlet to sptop.Inlet;	
	sptop.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
end


#*----------------------------------------------------------------------
* Model of a  Refluxed Absorption column containing:
*	- NTrays like tray;
*	- dymamic condenser without subcooling;
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream;
*---------------------------------------------------------------------*# 
Model Refluxed_Absorption
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenser;
	sp as splitter;
	pump1 as pump;

	EQUATIONS
	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - cond.OutletL.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		cond.OutletL.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;

	#liquid
	cond.OutletL to sp.Inlet;	
	sp.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
end


#* -------------------------------------------------------------------
* Refluxed Absorption Column with:
*
*	- NTrays like tray;
*	- a steady state condenser (with subcooling);
*	- a vessel drum (layed cilinder);
*	- a splitter which separate reflux and distillate;
*	- a pump in reflux stream.
*
* ------------------------------------------------------------------*#
Model Refluxed_Absorption_subcooling
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	cond as condenserSteady;
	ttop as tank_cylindrical;
	sptop as splitter;
	pump1 as pump;

	EQUATIONS
	"Pressure Drop through the tray"
	trays(1).OutletV.F = (1 + tanh(1 * (trays(1).OutletV.P - ttop.Outlet.P)))/2 * 
		trays(1).Ah/trays(1).vV * sqrt(2*(trays(1).OutletV.P -
		ttop.Outlet.P + 1e-8 * "atm") / (trays(1).alfa*trays(1).rhoV));
		
	trays([2:NTrays]).OutletV.F = (1 + tanh(1 * (trays([2:NTrays]).OutletV.P - trays([2:NTrays]).InletL.P)))/2 * 
		trays([2:NTrays]).Ah/trays([2:NTrays]).vV * sqrt(2*(trays([2:NTrays]).OutletV.P -
		trays([2:NTrays]).InletL.P + 1e-8 * "atm") / (trays([2:NTrays]).alfa*trays([2:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	trays(1).OutletV to cond.InletV;
	
	#liquid
	cond.OutletL to ttop.Inlet;
	ttop.Outlet to sptop.Inlet;	
	sptop.Outlet2 to pump1.Inlet;
	pump1.Outlet to trays(1).InletL;
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
end


#* -------------------------------------------------------------------
* Reboiled Stripping Column model with:
*
*	- NTrays like tray;
*	- a kettle reboiler;
*
* ------------------------------------------------------------------*#
Model Reboiled_Stripping_kettle
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	reb as reboiler;

	EQUATIONS
	if (reb.OutletV.P > reb.InletL.P) then
		"Pressure Drop through the tray"
		reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P)
				/ (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3
	else
		"Prato selado"
		reb.OutletV.F = 0.0 * "mol/s";
	end

	"Pressure Drop through the tray"
	trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * 
		trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P -
		trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	reb.OutletV to trays(NTrays).InletV;
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	
	#liquid
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	trays(NTrays).OutletL to reb.InletL;
end


#* -------------------------------------------------------------------
* Reboiled Stripping Column model with:
*
*	- NTrays like tray;
*	- a vessel in the bottom of column;
*	- a splitter which separate the bottom product and the stream to reboiler;
*	- steady state reboiler (thermosyphon);
*
* ------------------------------------------------------------------*#
Model Reboiled_Stripping_thermosyphon
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	reb as reboilerSteady;
	spbottom as splitter;
	tbottom as tank;

	EQUATIONS
	if (reb.OutletV.P > reb.InletL.P) then
		"Pressure Drop through the tray"
		reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P)
				/ (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3
	else
		"Prato selado"
		reb.OutletV.F = 0.0 * "mol/s";
	end

	"Pressure Drop through the tray"
	trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * 
		trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P -
		trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	reb.OutletV to trays(NTrays).InletV;
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	
	#liquid
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	trays(NTrays).OutletL to tbottom.Inlet;
	tbottom.Outlet to spbottom.Inlet;
	spbottom.Outlet2 to reb.InletL;
end


#* -------------------------------------------------------------------
* Reboiled Absorption Column model with:
*
*	- NTrays like tray;
*	- a kettle reboiler;
*
* ------------------------------------------------------------------*#
Model Reboiled_Absorption_kettle
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	reb as reboiler;

	EQUATIONS
	if (reb.OutletV.P > reb.InletL.P) then
		"Pressure Drop through the tray"
		reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P)
				/ (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3
	else
		"Prato selado"
		reb.OutletV.F = 0.0 * "mol/s";
	end

	"Pressure Drop through the tray"
	trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * 
		trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P -
		trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	reb.OutletV to trays(NTrays).InletV;
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	
	#liquid
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	trays(NTrays).OutletL to reb.InletL;
end


#* -------------------------------------------------------------------
* Reboiled Absorption Column model with:
*
*	- NTrays like tray;
*	- a vessel in the bottom of column;
*	- a splitter which separate the bottom product and the stream to reboiler;
*	- steady state reboiler (thermosyphon);
*
* ------------------------------------------------------------------*#
Model Reboiled_Absorption_thermosyphon
	PARAMETERS
ext PP as CalcObject;
ext NComp as Integer;
	NTrays as Integer(Brief="Number of trays", Default=2);
	
	VARIABLES
	trays(NTrays) as tray;
	reb as reboilerSteady;
	spbottom as splitter;
	tbottom as tank;

	EQUATIONS
	if (reb.OutletV.P > reb.InletL.P) then
		"Pressure Drop through the tray"
		reb.OutletV.F = 34803 * "mm^2"/reb.vV * sqrt((reb.OutletV.P - trays(NTrays).OutletL.P)
				/ (1.3*reb.rhoV) ); # para o modelo com 25 pratos, o beta do refervedor é 0.8. Para a coluna com 80, o beta é:1.3
	else
		"Prato selado"
		reb.OutletV.F = 0.0 * "mol/s";
	end

	"Pressure Drop through the tray"
	trays([1:NTrays]).OutletV.F = (1 + tanh(1 * (trays([1:NTrays]).OutletV.P - trays([1:NTrays]).InletL.P)))/2 * 
		trays([1:NTrays]).Ah/trays([1:NTrays]).vV * sqrt(2*(trays([1:NTrays]).OutletV.P -
		trays([1:NTrays]).InletL.P + 1e-8 * "atm") / (trays([1:NTrays]).alfa*trays([1:NTrays]).rhoV));
	
	CONNECTIONS
	#vapor
	reb.OutletV to trays(NTrays).InletV;
	trays([2:NTrays]).OutletV to trays([1:NTrays-1]).InletV;
	
	#liquid
	trays([1:NTrays-1]).OutletL to trays([2:NTrays]).InletL;
	trays(NTrays).OutletL to tbottom.Inlet;
	tbottom.Outlet to spbottom.Inlet;
	spbottom.Outlet2 to reb.InletL;
end