//EQUATIONS
//Units: SI, Temperatures in Celsius, pressures in bar
//Project file: D:\_classement\_Thopt\THERMOPTIM_Pro_282\proj\steam_light.prj
//Date and Time: 2024-08-24 16:04:48

//Flow rate unit: -

//GAS COMPOSITIONS

//PROCESSES

//Process: condenser
//Equation: 1
m_dot_condenser = m_dot_turbine // Upstream process - turbine
// Comment = isobaricExchange
//Equation: 2
p_1 = p_4 // Upstream point - 4 - Downstream point - 1
// Comment = mDeltaH not set
//Equation: 3
Q_dot_condenser = m_dot_condenser*(h_1 - h_4) // Upstream point - 4 - Downstream point - 1 - DeltaH/flow

//Process: superheater
//Equation: 4
m_dot_superheater = m_dot_evaporator // Upstream process - evaporator
// Comment = isobaricExchange
//Equation: 5
p_3 = p_3b // Upstream point - 3b - Downstream point - 3
// Comment = mDeltaH not set
//Equation: 6
h_3 =  h_PT("water",p_3,T_3)// Enthalpy
//Equation: 7
Q_dot_superheater = m_dot_superheater*(h_3 - h_3b) // Upstream point - 3b - Downstream point - 3 - DeltaH/flow

//Process: evaporator
//Equation: 8
m_dot_evaporator = m_dot_economizer // Upstream process - economizer
// Comment = isobaricExchange
//Equation: 9
p_3b = p_3a // Upstream point - 3a - Downstream point - 3b
// Comment = mDeltaH not set
//Equation: 10
Q_dot_evaporator = m_dot_evaporator*(h_3b - h_3a) // Upstream point - 3a - Downstream point - 3b - DeltaH/flow

//Process: economizer
//Equation: 11
m_dot_economizer = m_dot_pump // Upstream process - pump
// Comment = isobaricExchange
//Equation: 12
p_3a = p_2 // Upstream point - 2 - Downstream point - 3a
// Comment = mDeltaH not set
//Equation: 13
Q_dot_economizer = m_dot_economizer*(h_3a - h_2) // Upstream point - 2 - Downstream point - 3a - DeltaH/flow

//Process: pump
//Equation: 14
s_1 = s_Ph("water",p_1,h_1) // Upstream point - 1 - Downstream point - 2
// Comment = Isentropic reference
//Equation: 15
hs_2 = h_Ps("water",p_2,s_1) // Downstream point - 2
//Equation: 16
etaT_pump = 1.0// Isentropic efficiency
//Equation: 17
v_2 = v_Ph("water",p_2,h_2) // Downstream point volume - 
//Equation: 18
h_2 = h_1 + v_2*(p_2 - p_1)/100. // Liquid compression
//Equation: 19
T_2 = T_Ph("water",p_2,h_2) // Downstream point - 2
// Comment = Given outlet pressure
//Equation: 20
p_2 = 128.0// Outlet pressure
//Equation: 21
W_dot_pump = m_dot_pump*(h_2 - h_1) // DeltaH 

//Process: turbine
//Equation: 22
m_dot_turbine = m_dot_superheater // Upstream process - superheater
//Equation: 23
s_3 = s_Ph("water",p_3,h_3) // Upstream point - 3 - Downstream point - 4
// Comment = Isentropic reference
//Equation: 24
hs_4 = h_Ps("water",p_4,s_3) // Downstream point - 4
//Equation: 25
etaT_turbine = 0.9// Isentropic efficiency
//Equation: 26
h_4 = h_3 - etaT_turbine*(h_3 - hs_4) // Upstream point - 3 - Downstream point - 4
//Equation: 27
xl_4 = 0.// Saturated liquid quality
//Equation: 28
Tl_4 = T_4- 0.01// Saturated liquid temperature
//Equation: 29
xv_4 = 1.// Saturated vapor quality
//Equation: 30
Tv_4 = T_4+ 0.01// Saturated vapor temperature
//Equation: 31
hl_4 = hsat_Px("water",p_4,xl_4)// Saturated liquid enthalpy
//Equation: 32
hv_4 = hsat_Px("water",p_4,xv_4)// Saturated vapor enthalpy
//Equation: 33
x_4 = (h_4 - hl_4)/(hv_4 - hl_4)// Quality
//Equation: 34
T_4 = Tsat_P("water",p_4) // Downstream point - 4
//Equation: 35
s_4 = s_Ph("water",p_4,h_4) // Entropy
// Comment = Given outlet pressure
//Equation: 36
p_4 = 0.0356// Outlet pressure
//Equation: 37
W_dot_turbine = m_dot_turbine*(h_4 - h_3) // DeltaH 

//NODES

//HEAT EXCHANGERS

//Number of equations: 37

//POINTS WITH SATURATION TEMPERATURE SET


//Point 1

//Outlet point of process condenser
//Equation: 38
x_1 = 0.0// Quality
//Equation: 39
dTsat_1 = 0.0// Deviation from Tsat
//Equation: 40
T_1 = Tsat_P("water",p_1)+dTsat_1// set Tsat (Celsius)
//Equation: 41
h_1 = hsat_Px("water",p_1,x_1)// Enthalpy


//Point 3a

//Outlet point of process economizer
//Equation: 42
x_3a = 0.0// Quality
//Equation: 43
dTsat_3a = 0.0// Deviation from Tsat
//Equation: 44
T_3a = Tsat_P("water",p_3a)+dTsat_3a// set Tsat (Celsius)
//Equation: 45
h_3a = hsat_Px("water",p_3a,x_3a)// Enthalpy


//Point 3b

//Outlet point of process evaporator
//Equation: 46
x_3b = 1.0// Quality
//Equation: 47
dTsat_3b = 0.0// Deviation from Tsat
//Equation: 48
T_3b = Tsat_P("water",p_3b)+dTsat_3b// set Tsat (Celsius)
//Equation: 49
h_3b = hsat_Px("water",p_3b,x_3b)// Enthalpy


//OTHER POINTS WITH PRESSURE SET


//SET FLOW RATES

//Equation: 50
m_dot_pump = 1.0// Given flow 

//OVERALL BALANCE

//Equation: 51
useful_Energy = W_dot_pump + W_dot_turbine
//Equation: 52
purchased_Energy = Q_dot_superheater + Q_dot_evaporator + Q_dot_economizer
//Equation: 53
eta_global = abs(useful_Energy/purchased_Energy)
//Equation: 54
T_3 = 447