from pyomo.network import Port
from idaes.core import (FlowsheetBlock)
import Custom_prop_2 as props
# import Mod2_hda_ideal_VLE as props
from idaes.unit_models import Mixer
from idaes.unit_models.mixer import MixingType, MomentumMixingType
from idaes.core.util.model_statistics import degrees_of_freedom
m = ConcreteModel()
m.fs = FlowsheetBlock(default={"dynamic": False})
m.fs.properties = props.NaClParameterBlock()
# m.fs.properties = props.HDAParameterBlock()
m.fs.Mixer = Mixer(
default={
"property_package": m.fs.properties,
"inlet_list": ["feed_1", "feed_2"],
"energy_mixing_type": MixingType.extensive,
"momentum_mixing_type": MomentumMixingType.none
})
m.fs.Mixer.feed_1.flow_mass[0].fix(0.5)
m.fs.Mixer.feed_1.mass_frac[0].fix(0.1)
m.fs.Mixer.feed_1.temperature[0].fix(273.15 + 50)
m.fs.Mixer.feed_2.flow_mass[0].fix(0.5)
m.fs.Mixer.feed_2.mass_frac[0].fix(0.035)
m.fs.Mixer.feed_2.temperature[0].fix(273.15 + 25)
# m.fs.Mixer.outlet.temperature[0].fix(273.15 + 40)
# m.fs.Mixer.mixed_state[0].dens_mass
# m.fs.Mixer.mixed_state[0].viscosity
# m.fs.Mixer.mixed_state[0].dens_mass_comp
m.fs.Mixer.mixed_state[0].pressure_osm
def build(self):
super().build()
config = self.config # sorter ref to config for less line splitting
# All feedwater heaters have a condensing section
_set_prop_pack(config.condense, config)
self.condense = FWHCondensing0D(default=config.condense)
# Add a mixer to add the drain stream from another feedwater heater
if config.has_drain_mixer:
mix_cfg = { # general unit model config
"dynamic": config.dynamic,
"has_holdup": config.has_holdup,
"property_package": config.property_package,
"property_package_args": config.property_package_args,
"momentum_mixing_type": MomentumMixingType.none,
"material_balance_type": MaterialBalanceType.componentTotal,
"inlet_list": ["steam", "drain"]
}
self.drain_mix = Mixer(default=mix_cfg)
@self.drain_mix.Constraint(self.drain_mix.flowsheet().config.time)
def mixer_pressure_constraint(b, t):
"""
Constraint to set the drain mixer pressure to the pressure of
the steam extracted from the turbine. The drain inlet should
always be a higher pressure than the steam inlet.
"""
return b.steam_state[t].pressure == b.mixed_state[t].pressure
# Connect the mixer to the condensing section inlet
self.mix_out_arc = Arc(source=self.drain_mix.outlet,
destination=self.condense.inlet_1)
# Add a desuperheat section before the condensing section
if config.has_desuperheat:
_set_prop_pack(config.desuperheat, config)
self.desuperheat = HeatExchanger(default=config.desuperheat)
# set default area less than condensing section area, this will
# almost always be overridden by the user fixing an area later
self.desuperheat.area.value = 10
if config.has_drain_mixer:
self.desuperheat_drain_arc = Arc(
source=self.desuperheat.outlet_1,
destination=self.drain_mix.steam)
else:
self.desuperheat_drain_arc = Arc(
source=self.desuperheat.outlet_1,
destination=self.condense.inlet_1)
self.condense_out2_arc = Arc(source=self.condense.outlet_2,
destination=self.desuperheat.inlet_2)
# Add a drain cooling section after the condensing section
if config.has_drain_cooling:
_set_prop_pack(config.cooling, config)
self.cooling = HeatExchanger(default=config.cooling)
# set default area less than condensing section area, this will
# almost always be overridden by the user fixing an area later
self.cooling.area.value = 10
self.cooling_out2_arc = Arc(source=self.cooling.outlet_2,
destination=self.condense.inlet_2)
self.condense_out1_arc = Arc(source=self.condense.outlet_1,
destination=self.cooling.inlet_1)
TransformationFactory("network.expand_arcs").apply_to(self)
def build_boiler(fs):
# Add property packages to flowsheet library
fs.prop_fluegas = FlueGasParameterBlock()
# Create unit models
# Boiler Economizer
fs.ECON = BoilerHeatExchanger(
default={
"side_1_property_package": fs.prop_water,
"side_2_property_package": fs.prop_fluegas,
"has_pressure_change": True,
"has_holdup": False,
"delta_T_method": DeltaTMethod.counterCurrent,
"tube_arrangement": TubeArrangement.inLine,
"side_1_water_phase": "Liq",
"has_radiation": False
})
# Primary Superheater
fs.PrSH = BoilerHeatExchanger(
default={
"side_1_property_package": fs.prop_water,
"side_2_property_package": fs.prop_fluegas,
"has_pressure_change": True,
"has_holdup": False,
"delta_T_method": DeltaTMethod.counterCurrent,
"tube_arrangement": TubeArrangement.inLine,
"side_1_water_phase": "Liq",
"has_radiation": True
})
# Finishing Superheater
fs.FSH = BoilerHeatExchanger(
default={
"side_1_property_package": fs.prop_water,
"side_2_property_package": fs.prop_fluegas,
"has_pressure_change": True,
"has_holdup": False,
"delta_T_method": DeltaTMethod.counterCurrent,
"tube_arrangement": TubeArrangement.inLine,
"side_1_water_phase": "Liq",
"has_radiation": True
})
# Reheater
fs.RH = BoilerHeatExchanger(
default={
"side_1_property_package": fs.prop_water,
"side_2_property_package": fs.prop_fluegas,
"has_pressure_change": True,
"has_holdup": False,
"delta_T_method": DeltaTMethod.counterCurrent,
"tube_arrangement": TubeArrangement.inLine,
"side_1_water_phase": "Liq",
"has_radiation": True
})
# Platen Superheater
fs.PlSH = Heater(default={"property_package": fs.prop_water})
#Boiler Water Wall
fs.Water_wall = Heater(default={"property_package": fs.prop_water})
#Boiler Splitter (splits FSH flue gas outlet to Reheater and PrSH)
fs.Spl1 = Separator(
default={
"property_package": fs.prop_fluegas,
"split_basis": SplittingType.totalFlow,
"energy_split_basis": EnergySplittingType.equal_temperature
})
# Flue gas mixer (mixing FG from Reheater and Primary SH, inlet to ECON)
fs.mix1 = Mixer(
default={
"property_package": fs.prop_fluegas,
"inlet_list": ['Reheat_out', 'PrSH_out'],
"dynamic": False
})
# Mixer for Attemperator #1 (between PrSH and PlSH)
fs.ATMP1 = Mixer(
default={
"property_package": fs.prop_water,
"inlet_list": ['Steam', 'SprayWater'],
"dynamic": False
})
# Build connections (streams)
# Steam Route (side 1 = tube side = steam/water side)
# Boiler feed water to Economizer (to be imported in full plant model)
# fs.bfw2econ = Arc(source=fs.FWH8.outlet,
# destination=fs.ECON.side_1_inlet)
fs.econ2ww = Arc(source=fs.ECON.side_1_outlet,
destination=fs.Water_wall.inlet)
fs.ww2prsh = Arc(source=fs.Water_wall.outlet,
destination=fs.PrSH.side_1_inlet)
fs.prsh2plsh = Arc(source=fs.PrSH.side_1_outlet, destination=fs.PlSH.inlet)
fs.plsh2fsh = Arc(source=fs.PlSH.outlet, destination=fs.FSH.side_1_inlet)
fs.FSHtoATMP1 = Arc(source=fs.FSH.side_1_outlet,
destination=fs.ATMP1.Steam)
# fs.fsh2hpturbine=Arc(source=fs.ATMP1.outlet,
# destination=fs.HPTinlet)
#(to be imported in full plant model)
# Flue gas route ------------------------------------------------------------
# water wall connected with boiler block (to fix the heat duty)
# platen SH connected with boiler block (to fix the heat duty)
#Finishing superheater connected with a flowsheet level constraint
fs.fg_fsh2_separator = Arc(source=fs.FSH.side_2_outlet,
destination=fs.Spl1.inlet)
fs.fg_fsh2rh = Arc(source=fs.Spl1.outlet_1, destination=fs.RH.side_2_inlet)
fs.fg_fsh2PrSH = Arc(source=fs.Spl1.outlet_2,
destination=fs.PrSH.side_2_inlet)
fs.fg_rhtomix = Arc(source=fs.RH.side_2_outlet,
destination=fs.mix1.Reheat_out)
fs.fg_prsh2mix = Arc(source=fs.PrSH.side_2_outlet,
destination=fs.mix1.PrSH_out)
fs.fg_mix2econ = Arc(source=fs.mix1.outlet,
destination=fs.ECON.side_2_inlet)
def main():
"""
Make the flowsheet object, fix some variables, and solve the problem
"""
# Create a Concrete Model as the top level object
m = ConcreteModel()
# Add a flowsheet object to the model
# time_set has points at 0 and 20 as the start and end of the domain,
# and a point at t=1 to allow for a step-change at this time
m.fs = FlowsheetBlock(default={"dynamic": True, "time_set": [0, 1, 20]})
# Add property packages to flowsheet library
m.fs.thermo_params = thermo_props.SaponificationParameterBlock()
m.fs.reaction_params = reaction_props.SaponificationReactionParameterBlock(
default={"property_package": m.fs.thermo_params})
# Create unit models
m.fs.mix = Mixer(default={
"dynamic": False,
"property_package": m.fs.thermo_params
})
m.fs.Tank1 = CSTR(
default={
"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params,
"has_holdup": True,
"has_equilibrium_reactions": False,
"has_heat_of_reaction": True,
"has_heat_transfer": True,
"has_pressure_change": False
})
m.fs.Tank2 = CSTR(
default={
"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params,
"has_holdup": True,
"has_equilibrium_reactions": False,
"has_heat_of_reaction": True,
"has_heat_transfer": True,
"has_pressure_change": False
})
# Add pressure-flow constraints to Tank 1
m.fs.Tank1.height = Var(m.fs.time,
initialize=1.0,
doc="Depth of fluid in tank [m]")
m.fs.Tank1.area = Var(initialize=1.0,
doc="Cross-sectional area of tank [m^2]")
m.fs.Tank1.flow_coeff = Var(m.fs.time,
initialize=5e-5,
doc="Tank outlet flow coefficient")
def geometry(b, t):
return b.volume[t] == b.area * b.height[t]
m.fs.Tank1.geometry = Constraint(m.fs.time, rule=geometry)
def outlet_flowrate(b, t):
return b.control_volume.properties_out[t].flow_vol == \
b.flow_coeff[t]*b.height[t]**0.5
m.fs.Tank1.outlet_flowrate = Constraint(m.fs.time, rule=outlet_flowrate)
# Add pressure-flow constraints to tank 2
m.fs.Tank2.height = Var(m.fs.time,
initialize=1.0,
doc="Depth of fluid in tank [m]")
m.fs.Tank2.area = Var(initialize=1.0,
doc="Cross-sectional area of tank [m^2]")
m.fs.Tank2.flow_coeff = Var(m.fs.time,
initialize=5e-5,
doc="Tank outlet flow coefficient")
m.fs.Tank2.geometry = Constraint(m.fs.time, rule=geometry)
m.fs.Tank2.outlet_flowrate = Constraint(m.fs.time, rule=outlet_flowrate)
# Make Streams to connect units
m.fs.stream1 = Arc(source=m.fs.mix.outlet, destination=m.fs.Tank1.inlet)
m.fs.stream2 = Arc(source=m.fs.Tank1.outlet, destination=m.fs.Tank2.inlet)
# Discretize time domain
m.discretizer = TransformationFactory('dae.finite_difference')
m.discretizer.apply_to(m, nfe=50, wrt=m.fs.time, scheme="BACKWARD")
TransformationFactory("network.expand_arcs").apply_to(m)
# Set inlet and operating conditions, and some initial conditions.
m.fs.mix.inlet_1.flow_vol.fix(0.5)
m.fs.mix.inlet_1.conc_mol_comp[:, "H2O"].fix(55388.0)
m.fs.mix.inlet_1.conc_mol_comp[:, "NaOH"].fix(100.0)
m.fs.mix.inlet_1.conc_mol_comp[:, "EthylAcetate"].fix(0.0)
m.fs.mix.inlet_1.conc_mol_comp[:, "SodiumAcetate"].fix(0.0)
m.fs.mix.inlet_1.conc_mol_comp[:, "Ethanol"].fix(0.0)
m.fs.mix.inlet_1.temperature.fix(303.15)
m.fs.mix.inlet_1.pressure.fix(101325.0)
m.fs.mix.inlet_2.flow_vol.fix(0.5)
m.fs.mix.inlet_2.conc_mol_comp[:, "H2O"].fix(55388.0)
m.fs.mix.inlet_2.conc_mol_comp[:, "NaOH"].fix(0.0)
m.fs.mix.inlet_2.conc_mol_comp[:, "EthylAcetate"].fix(100.0)
m.fs.mix.inlet_2.conc_mol_comp[:, "SodiumAcetate"].fix(0.0)
m.fs.mix.inlet_2.conc_mol_comp[:, "Ethanol"].fix(0.0)
m.fs.mix.inlet_2.temperature.fix(303.15)
m.fs.mix.inlet_2.pressure.fix(101325.0)
m.fs.Tank1.area.fix(1.0)
m.fs.Tank1.flow_coeff.fix(0.5)
m.fs.Tank1.heat_duty.fix(0.0)
m.fs.Tank2.area.fix(1.0)
m.fs.Tank2.flow_coeff.fix(0.5)
m.fs.Tank2.heat_duty.fix(0.0)
# Set initial conditions - accumulation = 0 at time = 0
m.fs.fix_initial_conditions(state="steady-state")
# Initialize Units
m.fs.mix.initialize()
m.fs.Tank1.initialize(
state_args={
"flow_vol": 1.0,
"conc_mol_comp": {
"H2O": 55388.0,
"NaOH": 100.0,
"EthylAcetate": 100.0,
"SodiumAcetate": 0.0,
"Ethanol": 0.0
},
"temperature": 303.15,
"pressure": 101325.0
})
m.fs.Tank2.initialize(
state_args={
"flow_vol": 1.0,
"conc_mol_comp": {
"H2O": 55388.0,
"NaOH": 100.0,
"EthylAcetate": 100.0,
"SodiumAcetate": 0.0,
"Ethanol": 0.0
},
"temperature": 303.15,
"pressure": 101325.0
})
# Create a solver
solver = SolverFactory('ipopt')
results = solver.solve(m.fs)
# Make a step disturbance in feed and solve again
for t in m.fs.time:
if t >= 1.0:
m.fs.mix.inlet_2.conc_mol_comp[t, "EthylAcetate"].fix(90.0)
results = solver.solve(m.fs)
# Print results
print(results)
# For testing purposes
return (m, results)
class FWH0DData(UnitModelBlockData):
CONFIG = UnitModelBlockData.CONFIG()
_define_feedwater_heater_0D_config(CONFIG)
def build(self):
super().build()
config = self.config # sorter ref to config for less line splitting
# All feedwater heaters have a condensing section
_set_prop_pack(config.condense, config)
self.condense = FWHCondensing0D(default=config.condense)
# Add a mixer to add the drain stream from another feedwater heater
if config.has_drain_mixer:
mix_cfg = { # general unit model config
"dynamic": config.dynamic,
"has_holdup": config.has_holdup,
"property_package": config.property_package,
"property_package_args": config.property_package_args,
"momentum_mixing_type": MomentumMixingType.none,
"material_balance_type": MaterialBalanceType.componentTotal,
"inlet_list": ["steam", "drain"]
}
self.drain_mix = Mixer(default=mix_cfg)
@self.drain_mix.Constraint(self.drain_mix.flowsheet().config.time)
def mixer_pressure_constraint(b, t):
"""
Constraint to set the drain mixer pressure to the pressure of
the steam extracted from the turbine. The drain inlet should
always be a higher pressure than the steam inlet.
"""
return b.steam_state[t].pressure == b.mixed_state[t].pressure
# Connect the mixer to the condensing section inlet
self.mix_out_arc = Arc(source=self.drain_mix.outlet,
destination=self.condense.inlet_1)
# Add a desuperheat section before the condensing section
if config.has_desuperheat:
_set_prop_pack(config.desuperheat, config)
self.desuperheat = HeatExchanger(default=config.desuperheat)
# set default area less than condensing section area, this will
# almost always be overridden by the user fixing an area later
self.desuperheat.area.value = 10
if config.has_drain_mixer:
self.desuperheat_drain_arc = Arc(
source=self.desuperheat.outlet_1,
destination=self.drain_mix.steam)
else:
self.desuperheat_drain_arc = Arc(
source=self.desuperheat.outlet_1,
destination=self.condense.inlet_1)
self.condense_out2_arc = Arc(source=self.condense.outlet_2,
destination=self.desuperheat.inlet_2)
# Add a drain cooling section after the condensing section
if config.has_drain_cooling:
_set_prop_pack(config.cooling, config)
self.cooling = HeatExchanger(default=config.cooling)
# set default area less than condensing section area, this will
# almost always be overridden by the user fixing an area later
self.cooling.area.value = 10
self.cooling_out2_arc = Arc(source=self.cooling.outlet_2,
destination=self.condense.inlet_2)
self.condense_out1_arc = Arc(source=self.condense.outlet_1,
destination=self.cooling.inlet_1)
TransformationFactory("network.expand_arcs").apply_to(self)
def initialize(self, *args, **kwargs):
config = self.config # sorter ref to config for less line splitting
sp = StoreSpec.value_isfixed_isactive(only_fixed=True)
istate = to_json(self, return_dict=True, wts=sp)
# the initilization here isn't straight forward since the heat exchanger
# may have 3 stages and they are countercurrent. For simplicity each
# stage in initialized with the same cooling water inlet conditions then
# the whole feedwater heater is solved together. There are more robust
# approaches which can be implimented if the need arises.
# initialize desuperheat if include
if config.has_desuperheat:
if config.has_drain_cooling:
_set_port(self.desuperheat.inlet_2, self.cooling.inlet_2)
else:
_set_port(self.desuperheat.inlet_2, self.condense.inlet_2)
self.desuperheat.initialize(*args, **kwargs)
self.desuperheat.inlet_1.flow_mol.unfix()
if config.has_drain_mixer:
_set_port(self.drain_mix.steam, self.desuperheat.outlet_1)
else:
_set_port(self.condense.inlet_1, self.desuperheat.outlet_1)
# fix the steam and fwh inlet for init
self.desuperheat.inlet_1.fix()
self.desuperheat.inlet_1.flow_mol.unfix() #unfix for extract calc
# initialize mixer if included
if config.has_drain_mixer:
self.drain_mix.steam.fix()
self.drain_mix.drain.fix()
self.drain_mix.outlet.unfix()
self.drain_mix.initialize(*args, **kwargs)
_set_port(self.condense.inlet_1, self.drain_mix.outlet)
if config.has_desuperheat:
self.drain_mix.steam.unfix()
else:
self.drain_mix.steam.flow_mol.unfix()
# Initialize condense section
if config.has_drain_cooling:
_set_port(self.condense.inlet_2, self.cooling.inlet_2)
self.cooling.inlet_2.fix()
else:
self.condense.inlet_2.fix()
self.condense.initialize(*args, **kwargs)
# Initialize drain cooling if included
if config.has_drain_cooling:
_set_port(self.cooling.inlet_1, self.condense.outlet_1)
self.cooling.initialize(*args, **kwargs)
# Solve all together
outlvl = kwargs.get("outlvl", 0)
opt = SolverFactory(kwargs.get("solver", "ipopt"))
opt.options = kwargs.get("oparg", {})
tee = True if outlvl >= 3 else False
assert (degrees_of_freedom(self) == 0)
results = opt.solve(self, tee=tee)
if results.solver.termination_condition == TerminationCondition.optimal:
if outlvl >= 2:
_log.info('{} Initialization Complete.'.format(self.name))
else:
_log.warning('{} Initialization Failed.'.format(self.name))
from_json(self, sd=istate, wts=sp)
class TurbineMultistageData(UnitModelBlockData):
CONFIG = ConfigBlock()
_define_turbine_multistage_config(CONFIG)
def build(self):
super(TurbineMultistageData, self).build()
config = self.config
unit_cfg = { # general unit model config
"dynamic":config.dynamic,
"has_holdup":config.has_holdup,
"has_phase_equilibrium":config.has_phase_equilibrium,
"property_package":config.property_package,
"property_package_args":config.property_package_args,
}
ni = self.config.num_parallel_inlet_stages
inlet_idx = self.inlet_stage_idx = RangeSet(ni)
# Adding unit models
#------------------------
# Splitter to inlet that splits main flow into parallel flows for
# paritial arc admission to the turbine
self.inlet_split = Separator(default=self._split_cfg(unit_cfg, ni))
self.throttle_valve = SteamValve(inlet_idx, default=unit_cfg)
self.inlet_stage = TurbineInletStage(inlet_idx, default=unit_cfg)
# mixer to combine the parallel flows back together
self.inlet_mix = Mixer(default=self._mix_cfg(unit_cfg, ni))
# add turbine sections.
# inlet stage -> hp stages -> ip stages -> lp stages -> outlet stage
self.hp_stages = TurbineStage(RangeSet(config.num_hp),
default=unit_cfg)
self.ip_stages = TurbineStage(RangeSet(config.num_ip),
default=unit_cfg)
self.lp_stages = TurbineStage(RangeSet(config.num_lp),
default=unit_cfg)
self.outlet_stage = TurbineOutletStage(default=unit_cfg)
for i in self.hp_stages:
self.hp_stages[i].ratioP.fix()
self.hp_stages[i].efficiency_isentropic[:].fix()
for i in self.ip_stages:
self.ip_stages[i].ratioP.fix()
self.ip_stages[i].efficiency_isentropic[:].fix()
for i in self.lp_stages:
self.lp_stages[i].ratioP.fix()
self.lp_stages[i].efficiency_isentropic[:].fix()
# Then make splitter config. If number of outlets is specified
# make a specific config, otherwise use default with 2 outlets
s_sfg_default = self._split_cfg(unit_cfg, 2)
hp_splt_cfg = {}
ip_splt_cfg = {}
lp_splt_cfg = {}
# Now to finish up if there are more than two outlets, set that
for i, v in config.hp_split_num_outlets.items():
hp_splt_cfg[i] = self._split_cfg(unit_cfg, v)
for i, v in config.ip_split_num_outlets.items():
ip_splt_cfg[i] = self._split_cfg(unit_cfg, v)
for i, v in config.lp_split_num_outlets.items():
lp_splt_cfg[i] = self._split_cfg(unit_cfg, v)
# put in splitters for turbine steam extractions
if config.hp_split_locations:
self.hp_split = Separator(config.hp_split_locations,
default=s_sfg_default,
initialize=hp_splt_cfg)
if config.ip_split_locations:
self.ip_split = Separator(config.ip_split_locations,
default=s_sfg_default,
initialize=ip_splt_cfg)
if config.lp_split_locations:
self.lp_split = Separator(config.lp_split_locations,
default=s_sfg_default,
initialize=lp_splt_cfg)
# Done with unit models. Adding Arcs (streams).
#------------------------------------------------
# First up add streams in the inlet section
def _split_to_rule(b, i):
return {
"source": getattr(self.inlet_split, "outlet_{}".format(i)),
"destination": self.throttle_valve[i].inlet
}
def _valve_to_rule(b, i):
return {
"source": self.throttle_valve[i].outlet,
"destination": self.inlet_stage[i].inlet
}
def _inlet_to_rule(b, i):
return {
"source": self.inlet_stage[i].outlet,
"destination": getattr(self.inlet_mix, "inlet_{}".format(i))
}
self.split_to_valve_stream = Arc(inlet_idx, rule=_split_to_rule)
self.valve_to_inlet_stage_stream = Arc(inlet_idx, rule=_valve_to_rule)
self.inlet_stage_to_mix = Arc(inlet_idx, rule=_inlet_to_rule)
# There are three sections HP, IP, and LP which all have the same sort
# of internal connctions, so the functions below provide some generic
# capcbilities for adding the internal Arcs (streams).
def _arc_indexes(nstages, index_set, discon, splits):
"""
This takes the index set of all possible streams in a turbine
section and throws out arc indexes for stages that are disconnected
and arc indexes that are not needed because there is no splitter
after a stage.
Args:
nstages (int): Number of stages in section
index_set (Set): Index set for arcs in the section
discon (list): Disconnected stages in the section
splits (list): Spliter locations
"""
sr = set() # set of things to remove from the Arc index set
for i in index_set:
if (i[0] in discon or i[0] == nstages) and i[0] in splits:
# don't connect stage i to next remove stream after split
sr.add((i[0], 2))
elif (i[0] in discon
or i[0] == nstages) and i[0] not in splits:
# no splitter and disconnect so remove both streams
sr.add((i[0], 1))
sr.add((i[0], 2))
elif i[0] not in splits:
# no splitter and not disconnected so just second stream
sr.add((i[0], 2))
else:
# has splitter so need both streams don't remove anything
pass
for i in sr: # remove the unneeded Arc indexes
index_set.remove(i)
def _arc_rule(turbines, splitters):
"""
This creates a rule function for arcs in a turbine section. When
this is used the indexes for nonexistant stream will have already
been removed, so any indexes the rule will get should have a stream
associated.
Args:
turbines (TurbineStage): Indexed block with turbine section stages
splitters (Separator): Indexed block of splitters
"""
def _rule(b, i, j):
if i in splitters and j == 1:
return {
"source": turbines[i].outlet,
"destination": splitters[i].inlet
}
elif j == 2:
return {
"source": splitters[i].outlet_1,
"destination": turbines[i + 1].inlet
}
else:
return {
"source": turbines[i].outlet,
"destination": turbines[i + 1].inlet
}
return _rule
# Create initial arcs index sets with all possible streams
self.hp_stream_idx = Set(initialize=self.hp_stages.index_set() *
[1, 2])
self.ip_stream_idx = Set(initialize=self.ip_stages.index_set() *
[1, 2])
self.lp_stream_idx = Set(initialize=self.lp_stages.index_set() *
[1, 2])
# Throw out unneeded streams
_arc_indexes(config.num_hp, self.hp_stream_idx, config.hp_disconnect,
config.hp_split_locations)
_arc_indexes(config.num_ip, self.ip_stream_idx, config.ip_disconnect,
config.ip_split_locations)
_arc_indexes(config.num_lp, self.lp_stream_idx, config.lp_disconnect,
config.lp_split_locations)
# Create connections internal to each turbine section (hp, ip, and lp)
self.hp_stream = Arc(self.hp_stream_idx,
rule=_arc_rule(self.hp_stages, self.hp_split))
self.ip_stream = Arc(self.ip_stream_idx,
rule=_arc_rule(self.ip_stages, self.ip_split))
self.lp_stream = Arc(self.lp_stream_idx,
rule=_arc_rule(self.lp_stages, self.lp_split))
# Connect hp section to ip section unless its a disconnect location
last_hp = config.num_hp
if 0 not in config.ip_disconnect and last_hp not in config.hp_disconnect:
if last_hp in config.hp_split_locations: # connect splitter to ip
self.hp_to_ip_stream = Arc(
source=self.hp_split[last_hp].outlet_1,
destination=self.ip_stages[1].inlet)
else: # connect last hp to ip
self.hp_to_ip_stream = Arc(
source=self.hp_stages[last_hp].outlet,
destination=self.ip_stages[1].inlet)
# Connect ip section to lp section unless its a disconnect location
last_ip = config.num_ip
if 0 not in config.lp_disconnect and last_ip not in config.ip_disconnect:
if last_ip in config.ip_split_locations: # connect splitter to ip
self.ip_to_lp_stream = Arc(
source=self.ip_split[last_ip].outlet_1,
destination=self.lp_stages[1].inlet)
else: # connect last hp to ip
self.ip_to_lp_stream = Arc(
source=self.ip_stages[last_ip].outlet,
destination=self.lp_stages[1].inlet)
# Connect inlet stage to hp section
# not allowing disconnection of inlet and first regular hp stage
if 0 in config.hp_split_locations:
# connect inlet mix to splitter and splitter to hp section
self.inlet_to_splitter_stream = Arc(
source=self.inlet_mix.outlet,
destination=self.hp_split[0].inlet)
self.splitter_to_hp_stream = Arc(
source=self.hp_split[0].outlet_1,
destination=self.hp_stages[1].inlet)
else: # connect mixer to first hp turbine stage
self.inlet_to_hp_stream = Arc(source=self.inlet_mix.outlet,
destination=self.hp_stages[1].inlet)
@self.Expression(self.flowsheet().config.time)
def power(b, t):
return (sum(b.inlet_stage[i].power_shaft[t]
for i in b.inlet_stage) +
b.outlet_stage.power_shaft[t] +
sum(b.hp_stages[i].power_shaft[t] for i in b.hp_stages) +
sum(b.ip_stages[i].power_shaft[t] for i in b.ip_stages) +
sum(b.lp_stages[i].power_shaft[t] for i in b.lp_stages))
# Connect inlet stage to hp section
# not allowing disconnection of inlet and first regular hp stage
last_lp = config.num_lp
if last_lp in config.lp_split_locations: # connect splitter to outlet
self.lp_to_outlet_stream = Arc(
source=self.lp_split[last_lp].outlet_1,
destination=self.outlet_stage.inlet)
else: # connect last lpstage to outlet
self.lp_to_outlet_stream = Arc(
source=self.lp_stages[last_lp].outlet,
destination=self.outlet_stage.inlet)
TransformationFactory("network.expand_arcs").apply_to(self)
def _split_cfg(self, unit_cfg, no=2):
"""
This creates a configuration dictionary for a splitter.
Args:
unit_cfg: The base unit config dict.
no: Number of outlets, default=2
"""
# Create a dict for splitter config args
s_cfg = copy.copy(unit_cfg) # splitter config based on unit_cfg
s_cfg.update(
split_basis=SplittingType.totalFlow,
ideal_separation=False,
num_outlets=no,
energy_split_basis=EnergySplittingType.equal_molar_enthalpy)
del s_cfg["has_phase_equilibrium"]
return s_cfg
def _mix_cfg(self, unit_cfg, ni=2):
"""
This creates a configuration dictionary for a mixer.
Args:
unit_cfg: The base unit config dict.
ni: Number of inlets, default=2
"""
m_cfg = copy.copy(unit_cfg) # splitter config based on unit_cfg
m_cfg.update(
num_inlets=ni,
momentum_mixing_type=MomentumMixingType.minimize_and_equality)
del m_cfg["has_phase_equilibrium"]
return m_cfg
def throttle_cv_fix(self, value):
"""
Fix the thottle valve coefficients. These are generally the same for
each of the parallel stages so this provides a convenient way to set
them.
Args:
value: The value to fix the turbine inlet flow coefficients at
"""
for i in self.throttle_valve:
self.throttle_valve[i].Cv.fix(value)
def turbine_inlet_cf_fix(self, value):
"""
Fix the inlet turbine stage flow coefficient. These are
generally the same for each of the parallel stages so this provides
a convenient way to set them.
Args:
value: The value to fix the turbine inlet flow coefficients at
"""
for i in self.inlet_stage:
self.inlet_stage[i].flow_coeff.fix(value)
def turbine_outlet_cf_fix(self, value):
"""
Fix the inlet turbine stage flow coefficient. These are
generally the same for each of the parallel stages so this provides
a convenient way to set them.
Args:
value: The value to fix the turbine inlet flow coefficients at
"""
self.outlet_stage.flow_coeff.fix(value)
def initialize(self,
outlvl=0,
solver='ipopt',
optarg={
'tol': 1e-6,
'max_iter': 35
}):
"""
Initialize
"""
stee = True if outlvl >= 3 else False
# sp is what to save to make sure state after init is same as the start
# saves value, fixed, and active state, doesn't load originally free
# values, this makes sure original problem spec is same but initializes
# the values of free vars
sp = StoreSpec.value_isfixed_isactive(only_fixed=True)
istate = to_json(self, return_dict=True, wts=sp)
ni = self.config.num_parallel_inlet_stages
# Initialize Splitter
# Fix n - 1 split fractions
self.inlet_split.split_fraction[0, "outlet_1"].value = 1.0 / ni
for i in self.inlet_stage_idx:
if i == 1: #fix rest of splits at leaving first one free
continue
self.inlet_split.split_fraction[0, "outlet_{}".format(i)].fix(1.0 /
ni)
# fix inlet and free outlet
self.inlet_split.inlet.fix()
for i in self.inlet_stage_idx:
ol = getattr(self.inlet_split, "outlet_{}".format(i))
ol.unfix()
self.inlet_split.initialize(outlvl=outlvl,
solver=solver,
optarg=optarg)
# free split fractions
for i in self.inlet_stage_idx:
self.inlet_split.split_fraction[0, "outlet_{}".format(i)].unfix()
# Initialize valves
for i in self.inlet_stage_idx:
_set_port(self.throttle_valve[i].inlet,
getattr(self.inlet_split, "outlet_{}".format(i)))
self.throttle_valve[i].initialize(outlvl=outlvl,
solver=solver,
optarg=optarg)
# Initialize turbine
for i in self.inlet_stage_idx:
_set_port(self.inlet_stage[i].inlet, self.throttle_valve[i].outlet)
self.inlet_stage[i].initialize(outlvl=outlvl,
solver=solver,
optarg=optarg)
# Initialize Mixer
self.inlet_mix.use_minimum_inlet_pressure_constraint()
for i in self.inlet_stage_idx:
_set_port(getattr(self.inlet_mix, "inlet_{}".format(i)),
self.inlet_stage[i].outlet)
getattr(self.inlet_mix, "inlet_{}".format(i)).fix()
self.inlet_mix.initialize(outlvl=outlvl, solver=solver, optarg=optarg)
for i in self.inlet_stage_idx:
getattr(self.inlet_mix, "inlet_{}".format(i)).unfix()
self.inlet_mix.use_equal_pressure_constraint()
def init_section(stages, splits, disconnects, prev_port):
if 0 in splits:
_set_port(splits[0].inlet, prev_port)
splits[0].initialize(outlvl=outlvl,
solver=solver,
optarg=optarg)
prev_port = splits[0].outlet_1
for i in stages:
if i - 1 not in disconnects:
_set_port(stages[i].inlet, prev_port)
stages[i].initialize(outlvl=outlvl,
solver=solver,
optarg=optarg)
prev_port = stages[i].outlet
if i in splits:
_set_port(splits[i].inlet, prev_port)
splits[i].initialize(outlvl=outlvl,
solver=solver,
optarg=optarg)
prev_port = splits[i].outlet_1
return prev_port
prev_port = self.inlet_mix.outlet
prev_port = init_section(self.hp_stages, self.hp_split,
self.config.hp_disconnect, prev_port)
if len(self.hp_stages) in self.config.hp_disconnect:
prev_port = self.ip_stages[1].inlet
prev_port = init_section(self.ip_stages, self.ip_split,
self.config.ip_disconnect, prev_port)
if len(self.ip_stages) in self.config.ip_disconnect:
prev_port = self.lp_stages[1].inlet
prev_port = init_section(self.lp_stages, self.lp_split,
self.config.lp_disconnect, prev_port)
_set_port(self.outlet_stage.inlet, prev_port)
self.outlet_stage.initialize(outlvl=outlvl,
solver=solver,
optarg=optarg)
from_json(self, sd=istate, wts=sp)
def build(self):
super(TurbineMultistageData, self).build()
config = self.config
unit_cfg = { # general unit model config
"dynamic":config.dynamic,
"has_holdup":config.has_holdup,
"has_phase_equilibrium":config.has_phase_equilibrium,
"property_package":config.property_package,
"property_package_args":config.property_package_args,
}
ni = self.config.num_parallel_inlet_stages
inlet_idx = self.inlet_stage_idx = RangeSet(ni)
# Adding unit models
#------------------------
# Splitter to inlet that splits main flow into parallel flows for
# paritial arc admission to the turbine
self.inlet_split = Separator(default=self._split_cfg(unit_cfg, ni))
self.throttle_valve = SteamValve(inlet_idx, default=unit_cfg)
self.inlet_stage = TurbineInletStage(inlet_idx, default=unit_cfg)
# mixer to combine the parallel flows back together
self.inlet_mix = Mixer(default=self._mix_cfg(unit_cfg, ni))
# add turbine sections.
# inlet stage -> hp stages -> ip stages -> lp stages -> outlet stage
self.hp_stages = TurbineStage(RangeSet(config.num_hp),
default=unit_cfg)
self.ip_stages = TurbineStage(RangeSet(config.num_ip),
default=unit_cfg)
self.lp_stages = TurbineStage(RangeSet(config.num_lp),
default=unit_cfg)
self.outlet_stage = TurbineOutletStage(default=unit_cfg)
for i in self.hp_stages:
self.hp_stages[i].ratioP.fix()
self.hp_stages[i].efficiency_isentropic[:].fix()
for i in self.ip_stages:
self.ip_stages[i].ratioP.fix()
self.ip_stages[i].efficiency_isentropic[:].fix()
for i in self.lp_stages:
self.lp_stages[i].ratioP.fix()
self.lp_stages[i].efficiency_isentropic[:].fix()
# Then make splitter config. If number of outlets is specified
# make a specific config, otherwise use default with 2 outlets
s_sfg_default = self._split_cfg(unit_cfg, 2)
hp_splt_cfg = {}
ip_splt_cfg = {}
lp_splt_cfg = {}
# Now to finish up if there are more than two outlets, set that
for i, v in config.hp_split_num_outlets.items():
hp_splt_cfg[i] = self._split_cfg(unit_cfg, v)
for i, v in config.ip_split_num_outlets.items():
ip_splt_cfg[i] = self._split_cfg(unit_cfg, v)
for i, v in config.lp_split_num_outlets.items():
lp_splt_cfg[i] = self._split_cfg(unit_cfg, v)
# put in splitters for turbine steam extractions
if config.hp_split_locations:
self.hp_split = Separator(config.hp_split_locations,
default=s_sfg_default,
initialize=hp_splt_cfg)
if config.ip_split_locations:
self.ip_split = Separator(config.ip_split_locations,
default=s_sfg_default,
initialize=ip_splt_cfg)
if config.lp_split_locations:
self.lp_split = Separator(config.lp_split_locations,
default=s_sfg_default,
initialize=lp_splt_cfg)
# Done with unit models. Adding Arcs (streams).
#------------------------------------------------
# First up add streams in the inlet section
def _split_to_rule(b, i):
return {
"source": getattr(self.inlet_split, "outlet_{}".format(i)),
"destination": self.throttle_valve[i].inlet
}
def _valve_to_rule(b, i):
return {
"source": self.throttle_valve[i].outlet,
"destination": self.inlet_stage[i].inlet
}
def _inlet_to_rule(b, i):
return {
"source": self.inlet_stage[i].outlet,
"destination": getattr(self.inlet_mix, "inlet_{}".format(i))
}
self.split_to_valve_stream = Arc(inlet_idx, rule=_split_to_rule)
self.valve_to_inlet_stage_stream = Arc(inlet_idx, rule=_valve_to_rule)
self.inlet_stage_to_mix = Arc(inlet_idx, rule=_inlet_to_rule)
# There are three sections HP, IP, and LP which all have the same sort
# of internal connctions, so the functions below provide some generic
# capcbilities for adding the internal Arcs (streams).
def _arc_indexes(nstages, index_set, discon, splits):
"""
This takes the index set of all possible streams in a turbine
section and throws out arc indexes for stages that are disconnected
and arc indexes that are not needed because there is no splitter
after a stage.
Args:
nstages (int): Number of stages in section
index_set (Set): Index set for arcs in the section
discon (list): Disconnected stages in the section
splits (list): Spliter locations
"""
sr = set() # set of things to remove from the Arc index set
for i in index_set:
if (i[0] in discon or i[0] == nstages) and i[0] in splits:
# don't connect stage i to next remove stream after split
sr.add((i[0], 2))
elif (i[0] in discon
or i[0] == nstages) and i[0] not in splits:
# no splitter and disconnect so remove both streams
sr.add((i[0], 1))
sr.add((i[0], 2))
elif i[0] not in splits:
# no splitter and not disconnected so just second stream
sr.add((i[0], 2))
else:
# has splitter so need both streams don't remove anything
pass
for i in sr: # remove the unneeded Arc indexes
index_set.remove(i)
def _arc_rule(turbines, splitters):
"""
This creates a rule function for arcs in a turbine section. When
this is used the indexes for nonexistant stream will have already
been removed, so any indexes the rule will get should have a stream
associated.
Args:
turbines (TurbineStage): Indexed block with turbine section stages
splitters (Separator): Indexed block of splitters
"""
def _rule(b, i, j):
if i in splitters and j == 1:
return {
"source": turbines[i].outlet,
"destination": splitters[i].inlet
}
elif j == 2:
return {
"source": splitters[i].outlet_1,
"destination": turbines[i + 1].inlet
}
else:
return {
"source": turbines[i].outlet,
"destination": turbines[i + 1].inlet
}
return _rule
# Create initial arcs index sets with all possible streams
self.hp_stream_idx = Set(initialize=self.hp_stages.index_set() *
[1, 2])
self.ip_stream_idx = Set(initialize=self.ip_stages.index_set() *
[1, 2])
self.lp_stream_idx = Set(initialize=self.lp_stages.index_set() *
[1, 2])
# Throw out unneeded streams
_arc_indexes(config.num_hp, self.hp_stream_idx, config.hp_disconnect,
config.hp_split_locations)
_arc_indexes(config.num_ip, self.ip_stream_idx, config.ip_disconnect,
config.ip_split_locations)
_arc_indexes(config.num_lp, self.lp_stream_idx, config.lp_disconnect,
config.lp_split_locations)
# Create connections internal to each turbine section (hp, ip, and lp)
self.hp_stream = Arc(self.hp_stream_idx,
rule=_arc_rule(self.hp_stages, self.hp_split))
self.ip_stream = Arc(self.ip_stream_idx,
rule=_arc_rule(self.ip_stages, self.ip_split))
self.lp_stream = Arc(self.lp_stream_idx,
rule=_arc_rule(self.lp_stages, self.lp_split))
# Connect hp section to ip section unless its a disconnect location
last_hp = config.num_hp
if 0 not in config.ip_disconnect and last_hp not in config.hp_disconnect:
if last_hp in config.hp_split_locations: # connect splitter to ip
self.hp_to_ip_stream = Arc(
source=self.hp_split[last_hp].outlet_1,
destination=self.ip_stages[1].inlet)
else: # connect last hp to ip
self.hp_to_ip_stream = Arc(
source=self.hp_stages[last_hp].outlet,
destination=self.ip_stages[1].inlet)
# Connect ip section to lp section unless its a disconnect location
last_ip = config.num_ip
if 0 not in config.lp_disconnect and last_ip not in config.ip_disconnect:
if last_ip in config.ip_split_locations: # connect splitter to ip
self.ip_to_lp_stream = Arc(
source=self.ip_split[last_ip].outlet_1,
destination=self.lp_stages[1].inlet)
else: # connect last hp to ip
self.ip_to_lp_stream = Arc(
source=self.ip_stages[last_ip].outlet,
destination=self.lp_stages[1].inlet)
# Connect inlet stage to hp section
# not allowing disconnection of inlet and first regular hp stage
if 0 in config.hp_split_locations:
# connect inlet mix to splitter and splitter to hp section
self.inlet_to_splitter_stream = Arc(
source=self.inlet_mix.outlet,
destination=self.hp_split[0].inlet)
self.splitter_to_hp_stream = Arc(
source=self.hp_split[0].outlet_1,
destination=self.hp_stages[1].inlet)
else: # connect mixer to first hp turbine stage
self.inlet_to_hp_stream = Arc(source=self.inlet_mix.outlet,
destination=self.hp_stages[1].inlet)
@self.Expression(self.flowsheet().config.time)
def power(b, t):
return (sum(b.inlet_stage[i].power_shaft[t]
for i in b.inlet_stage) +
b.outlet_stage.power_shaft[t] +
sum(b.hp_stages[i].power_shaft[t] for i in b.hp_stages) +
sum(b.ip_stages[i].power_shaft[t] for i in b.ip_stages) +
sum(b.lp_stages[i].power_shaft[t] for i in b.lp_stages))
# Connect inlet stage to hp section
# not allowing disconnection of inlet and first regular hp stage
last_lp = config.num_lp
if last_lp in config.lp_split_locations: # connect splitter to outlet
self.lp_to_outlet_stream = Arc(
source=self.lp_split[last_lp].outlet_1,
destination=self.outlet_stage.inlet)
else: # connect last lpstage to outlet
self.lp_to_outlet_stream = Arc(
source=self.lp_stages[last_lp].outlet,
destination=self.outlet_stage.inlet)
TransformationFactory("network.expand_arcs").apply_to(self)
def test_serialize_flowsheet():
# Construct the model from idaes/examples/workshops/Module_2_Flowsheet/Module_2_Flowsheet_Solution.ipynb
m = ConcreteModel()
m.fs = FlowsheetBlock(default={"dynamic": False})
m.fs.thermo_params = thermo_props.HDAParameterBlock()
m.fs.reaction_params = reaction_props.HDAReactionParameterBlock(
default={"property_package": m.fs.thermo_params})
m.fs.M101 = Mixer(
default={
"property_package": m.fs.thermo_params,
"inlet_list": ["toluene_feed", "hydrogen_feed", "vapor_recycle"]
})
m.fs.H101 = Heater(
default={
"property_package": m.fs.thermo_params,
"has_pressure_change": False,
"has_phase_equilibrium": True
})
m.fs.R101 = StoichiometricReactor(
default={
"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params,
"has_heat_of_reaction": True,
"has_heat_transfer": True,
"has_pressure_change": False
})
m.fs.F101 = Flash(
default={
"property_package": m.fs.thermo_params,
"has_heat_transfer": True,
"has_pressure_change": True
})
m.fs.S101 = Splitter(
default={
"property_package": m.fs.thermo_params,
"ideal_separation": False,
"outlet_list": ["purge", "recycle"]
})
m.fs.C101 = PressureChanger(
default={
"property_package": m.fs.thermo_params,
"compressor": True,
"thermodynamic_assumption": ThermodynamicAssumption.isothermal
})
m.fs.F102 = Flash(
default={
"property_package": m.fs.thermo_params,
"has_heat_transfer": True,
"has_pressure_change": True
})
m.fs.s03 = Arc(source=m.fs.M101.outlet, destination=m.fs.H101.inlet)
m.fs.s04 = Arc(source=m.fs.H101.outlet, destination=m.fs.R101.inlet)
m.fs.s05 = Arc(source=m.fs.R101.outlet, destination=m.fs.F101.inlet)
m.fs.s06 = Arc(source=m.fs.F101.vap_outlet, destination=m.fs.S101.inlet)
m.fs.s08 = Arc(source=m.fs.S101.recycle, destination=m.fs.C101.inlet)
m.fs.s09 = Arc(source=m.fs.C101.outlet,
destination=m.fs.M101.vapor_recycle)
m.fs.s10 = Arc(source=m.fs.F101.liq_outlet, destination=m.fs.F102.inlet)
fss = FlowsheetSerializer()
fss.serialize_flowsheet(m.fs)
unit_models = fss.get_unit_models()
unit_model_names_types = []
for unit_model in unit_models:
unit_model_names_types.append(unit_models[unit_model])
unit_models_names_type_truth = [{
'name': 'M101',
'type': 'mixer'
}, {
'name': 'H101',
'type': 'heater'
}, {
'name': 'R101',
'type': 'stoichiometric_reactor'
}, {
'name': 'F101',
'type': 'flash'
}, {
'name': 'S101',
'type': 'separator'
}, {
'name': 'C101',
'type': 'pressure_changer'
}, {
'name': 'F102',
'type': 'flash'
}]
set_result = set(tuple(sorted(d.items())) for d in unit_model_names_types)
set_truth = set(
tuple(sorted(d.items())) for d in unit_models_names_type_truth)
difference = list(set_truth.symmetric_difference(set_result))
assert len(difference) == 0
# TODO Figure out how to test ports. Maybe find out if we can find the parent component for the port?
# ports = fss.get_ports()
# assert ports == {"<pyomo.network.port.SimplePort object at 0x7fe8d0d79278>": "<idaes.core.process_block._ScalarMixer object at 0x7fe8d0d60360>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d792e8>": "<idaes.core.process_block._ScalarMixer object at 0x7fe8d0d60360>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d79358>": "<idaes.core.process_block._ScalarMixer object at 0x7fe8d0d60360>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d793c8>": "<idaes.core.process_block._ScalarMixer object at 0x7fe8d0d60360>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d797b8>": "<idaes.core.process_block._ScalarHeater object at 0x7fe8d0db74c8>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d79828>": "<idaes.core.process_block._ScalarHeater object at 0x7fe8d0db74c8>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d79a58>": "<idaes.core.process_block._ScalarStoichiometricReactor object at 0x7fe8d0de2ab0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d79ac8>": "<idaes.core.process_block._ScalarStoichiometricReactor object at 0x7fe8d0de2ab0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d79eb8>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8d0e0fdc8>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41128>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8d0e0fdc8>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41198>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8d0e0fdc8>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0d79f98>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8d0e0fdc8>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41048>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8d0e0fdc8>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e410b8>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8d0e0fdc8>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41278>": "<idaes.core.process_block._ScalarSeparator object at 0x7fe8d0e45708>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41588>": "<idaes.core.process_block._ScalarSeparator object at 0x7fe8d0e45708>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e415f8>": "<idaes.core.process_block._ScalarSeparator object at 0x7fe8d0e45708>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41828>": "<idaes.core.process_block._ScalarPressureChanger object at 0x7fe8d0e686c0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41898>": "<idaes.core.process_block._ScalarPressureChanger object at 0x7fe8d0e686c0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41c88>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8e1405cf0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41eb8>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8e1405cf0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41f28>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8e1405cf0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41e48>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8e1405cf0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41dd8>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8e1405cf0>",
# "<pyomo.network.port.SimplePort object at 0x7fe8d0e41d68>": "<idaes.core.process_block._ScalarFlash object at 0x7fe8e1405cf0>"
# }
named_edges_results = {}
edges = fss.get_edges()
for edge in edges:
named_edges_results[edge.getname()] = [
x.getname() for x in edges[edge]
]
named_edges_truth = {
'M101': ['H101'],
'H101': ['R101'],
'R101': ['F101'],
'F101': ['S101', 'F102'],
'S101': ['C101'],
'C101': ['M101']
}
assert named_edges_results == named_edges_truth
def main():
# Create a Concrete Model as the top level object
m = ConcreteModel()
# Add a flowsheet object to the model
m.fs = FlowsheetBlock(default={"dynamic": False})
# Add property packages to flowsheet library
m.fs.thermo_params = thermo_props.HDAParameterBlock()
m.fs.reaction_params = reaction_props.HDAReactionParameterBlock(
default={"property_package": m.fs.thermo_params})
# Create unit models
m.fs.M101 = Mixer(
default={
"property_package": m.fs.thermo_params,
"inlet_list": ["toluene_feed", "hydrogen_feed", "vapor_recycle"]
})
m.fs.H101 = Heater(
default={
"property_package": m.fs.thermo_params,
"has_pressure_change": False,
"has_phase_equilibrium": True
})
m.fs.R101 = StoichiometricReactor(
default={
"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params,
"has_heat_of_reaction": True,
"has_heat_transfer": True,
"has_pressure_change": False
})
m.fs.F101 = Flash(
default={
"property_package": m.fs.thermo_params,
"has_heat_transfer": True,
"has_pressure_change": True
})
m.fs.S101 = Splitter(
default={
"property_package": m.fs.thermo_params,
"ideal_separation": False,
"outlet_list": ["purge", "recycle"]
})
# This is needed to avoid pressure degeneracy in recylce loop
m.fs.C101 = PressureChanger(
default={
"property_package": m.fs.thermo_params,
"compressor": True,
"thermodynamic_assumption": ThermodynamicAssumption.isothermal
})
m.fs.F102 = Flash(
default={
"property_package": m.fs.thermo_params,
"has_heat_transfer": True,
"has_pressure_change": True
})
m.fs.H101.control_volume.scaling_factor_energy = 1e-3
m.fs.R101.control_volume.scaling_factor_energy = 1e-3
m.fs.F101.control_volume.scaling_factor_energy = 1e-3
m.fs.C101.control_volume.scaling_factor_energy = 1e-3
m.fs.F102.control_volume.scaling_factor_energy = 1e-3
# Connect units
m.fs.s03 = Arc(source=m.fs.M101.outlet, destination=m.fs.H101.inlet)
m.fs.s04 = Arc(source=m.fs.H101.outlet, destination=m.fs.R101.inlet)
m.fs.s05 = Arc(source=m.fs.R101.outlet, destination=m.fs.F101.inlet)
m.fs.s06 = Arc(source=m.fs.F101.vap_outlet, destination=m.fs.S101.inlet)
m.fs.s08 = Arc(source=m.fs.S101.recycle, destination=m.fs.C101.inlet)
m.fs.s09 = Arc(source=m.fs.C101.outlet,
destination=m.fs.M101.vapor_recycle)
m.fs.s10 = Arc(source=m.fs.F101.liq_outlet, destination=m.fs.F102.inlet)
TransformationFactory("network.expand_arcs").apply_to(m)
# Set operating conditions
m.fs.M101.toluene_feed.flow_mol_phase_comp[0, "Vap", "benzene"].fix(1e-5)
m.fs.M101.toluene_feed.flow_mol_phase_comp[0, "Vap", "toluene"].fix(1e-5)
m.fs.M101.toluene_feed.flow_mol_phase_comp[0, "Vap", "hydrogen"].fix(1e-5)
m.fs.M101.toluene_feed.flow_mol_phase_comp[0, "Vap", "methane"].fix(1e-5)
m.fs.M101.toluene_feed.flow_mol_phase_comp[0, "Liq", "benzene"].fix(1e-5)
m.fs.M101.toluene_feed.flow_mol_phase_comp[0, "Liq", "toluene"].fix(0.30)
m.fs.M101.toluene_feed.flow_mol_phase_comp[0, "Liq", "hydrogen"].fix(1e-5)
m.fs.M101.toluene_feed.flow_mol_phase_comp[0, "Liq", "methane"].fix(1e-5)
m.fs.M101.toluene_feed.temperature.fix(303.2)
m.fs.M101.toluene_feed.pressure.fix(350000)
m.fs.M101.hydrogen_feed.flow_mol_phase_comp[0, "Vap", "benzene"].fix(1e-5)
m.fs.M101.hydrogen_feed.flow_mol_phase_comp[0, "Vap", "toluene"].fix(1e-5)
m.fs.M101.hydrogen_feed.flow_mol_phase_comp[0, "Vap", "hydrogen"].fix(0.30)
m.fs.M101.hydrogen_feed.flow_mol_phase_comp[0, "Vap", "methane"].fix(0.02)
m.fs.M101.hydrogen_feed.flow_mol_phase_comp[0, "Liq", "benzene"].fix(1e-5)
m.fs.M101.hydrogen_feed.flow_mol_phase_comp[0, "Liq", "toluene"].fix(1e-5)
m.fs.M101.hydrogen_feed.flow_mol_phase_comp[0, "Liq", "hydrogen"].fix(1e-5)
m.fs.M101.hydrogen_feed.flow_mol_phase_comp[0, "Liq", "methane"].fix(1e-5)
m.fs.M101.hydrogen_feed.temperature.fix(303.2)
m.fs.M101.hydrogen_feed.pressure.fix(350000)
m.fs.H101.outlet.temperature.fix(600)
m.fs.R101.conversion = Var(initialize=0.75, bounds=(0, 1))
m.fs.R101.conv_constraint = Constraint(
expr=m.fs.R101.conversion *
m.fs.R101.inlet.flow_mol_phase_comp[0, "Vap", "toluene"] == (
m.fs.R101.inlet.flow_mol_phase_comp[0, "Vap", "toluene"] -
m.fs.R101.outlet.flow_mol_phase_comp[0, "Vap", "toluene"]))
m.fs.R101.conversion.fix(0.75)
m.fs.R101.heat_duty.fix(0)
m.fs.F101.vap_outlet.temperature.fix(325.0)
m.fs.F101.deltaP.fix(0)
m.fs.S101.split_fraction[0, "purge"].fix(0.2)
m.fs.C101.outlet.pressure.fix(350000)
m.fs.F102.vap_outlet.temperature.fix(375)
m.fs.F102.deltaP.fix(-200000)
# Define expressions
# Product purity
m.fs.purity = Expression(
expr=m.fs.F102.vap_outlet.flow_mol_phase_comp[0, "Vap", "benzene"] /
(m.fs.F102.vap_outlet.flow_mol_phase_comp[0, "Vap", "benzene"] +
m.fs.F102.vap_outlet.flow_mol_phase_comp[0, "Vap", "toluene"]))
# Operating cost ($/yr)
m.fs.cooling_cost = Expression(expr=0.212e-7 * -m.fs.F101.heat_duty[0] +
0.212e-7 * -m.fs.R101.heat_duty[0])
m.fs.heating_cost = Expression(expr=2.2e-7 * m.fs.H101.heat_duty[0] +
1.9e-7 * m.fs.F102.heat_duty[0])
m.fs.operating_cost = Expression(
expr=(3600 * 24 * 365 * (m.fs.heating_cost + m.fs.cooling_cost)))
print(degrees_of_freedom(m))
# Initialize Units
# Define method for initialising each block
def function(unit):
unit.initialize(outlvl=1)
# Create instance of sequential decomposition tool
seq = SequentialDecomposition()
seq.options.select_tear_method = "heuristic"
seq.options.tear_method = "Wegstein"
seq.options.iterLim = 5
# Determine tear stream and calculation order
G = seq.create_graph(m)
heu_result = seq.tear_set_arcs(G, method="heuristic")
order = seq.calculation_order(G)
# Display tear stream and calculation order
for o in heu_result:
print(o.name)
for o in order:
for oo in o:
print(oo.name)
# Set guesses for tear stream
tear_guesses = {
"flow_mol_phase_comp": {
(0, "Vap", "benzene"): 1e-5,
(0, "Vap", "toluene"): 1e-5,
(0, "Vap", "hydrogen"): 0.30,
(0, "Vap", "methane"): 0.02,
(0, "Liq", "benzene"): 1e-5,
(0, "Liq", "toluene"): 0.30,
(0, "Liq", "hydrogen"): 1e-5,
(0, "Liq", "methane"): 1e-5
},
"temperature": {
0: 303
},
"pressure": {
0: 350000
}
}
seq.set_guesses_for(m.fs.H101.inlet, tear_guesses)
# Run sequential initialization
seq.run(m, function)
# # Create a solver
solver = SolverFactory('ipopt')
solver.options = {'tol': 1e-6}
solver.options = {'tol': 1e-6, 'max_iter': 5000}
results = solver.solve(m, tee=True)
# Print results
print("M101 Outlet")
m.fs.M101.outlet.display()
print("H101 Outlet")
m.fs.H101.outlet.display()
print("R101 Outlet")
m.fs.R101.outlet.display()
print("F101")
m.fs.F101.liq_outlet.display()
m.fs.F101.vap_outlet.display()
print("F102")
m.fs.F102.liq_outlet.display()
m.fs.F102.vap_outlet.display()
print("Purge")
m.fs.S101.purge.display()
print("Purity:", value(m.fs.purity))
# Optimize process
m.fs.objective = Objective(sense=minimize, expr=m.fs.operating_cost)
# Decision variables
m.fs.H101.outlet.temperature.unfix()
m.fs.R101.heat_duty.unfix()
m.fs.F101.vap_outlet.temperature.unfix()
m.fs.F102.vap_outlet.temperature.unfix()
m.fs.F102.deltaP.unfix()
# Variable bounds
m.fs.H101.outlet.temperature[0].setlb(500)
m.fs.H101.outlet.temperature[0].setub(600)
m.fs.R101.outlet.temperature[0].setlb(600)
m.fs.R101.outlet.temperature[0].setub(800)
m.fs.F101.vap_outlet.temperature[0].setlb(298.0)
m.fs.F101.vap_outlet.temperature[0].setub(450.0)
m.fs.F102.vap_outlet.temperature[0].setlb(298.0)
m.fs.F102.vap_outlet.temperature[0].setub(450.0)
m.fs.F102.vap_outlet.pressure[0].setlb(105000)
m.fs.F102.vap_outlet.pressure[0].setub(110000)
# Additional Constraints
m.fs.overhead_loss = Constraint(
expr=m.fs.F101.vap_outlet.flow_mol_phase_comp[0, "Vap",
"benzene"] <= 0.20 *
m.fs.R101.outlet.flow_mol_phase_comp[0, "Vap", "benzene"])
m.fs.product_flow = Constraint(
expr=m.fs.F102.vap_outlet.flow_mol_phase_comp[0, "Vap",
"benzene"] >= 0.15)
m.fs.product_purity = Constraint(expr=m.fs.purity >= 0.80)
# Create a solver
solver = SolverFactory('ipopt')
solver.options = {'tol': 1e-6}
solver.options = {'tol': 1e-6, 'max_iter': 5000}
results = solver.solve(m, tee=True)
# Print optimization results
print()
print("Optimal Solution")
m.fs.operating_cost.display()
m.fs.H101.heat_duty.display()
m.fs.R101.heat_duty.display()
m.fs.F101.heat_duty.display()
m.fs.F102.heat_duty.display()
# Print results
print("M101 Outlet")
m.fs.M101.outlet.display()
print("H101 Outlet")
m.fs.H101.outlet.display()
print("R101 Outlet")
m.fs.R101.outlet.display()
print("F101")
m.fs.F101.liq_outlet.display()
m.fs.F101.vap_outlet.display()
print("F102")
m.fs.F102.liq_outlet.display()
m.fs.F102.vap_outlet.display()
print("Purge")
m.fs.S101.purge.display()
print("Recycle")
m.fs.S101.recycle.display()
print("Purity:", value(m.fs.purity))
# For testing purposes
return (m, results)
def create_model():
m = pe.ConcreteModel()
m.fs = fs = FlowsheetBlock(default={"dynamic": False})
fs.vapor_props = vapor_props = PhysicalParameterBlock(
default={"valid_phase": 'Vap'})
fs.properties = props = PhysicalParameterBlock(
default={"valid_phase": ('Vap', 'Liq')})
fs.reaction_params = MethanolReactionParameterBlock(
default={'property_package': vapor_props})
fs.feed = feed = Feed(default={"property_package": vapor_props})
fs.compressor1 = IdealGasIsentropicCompressor(
default={
"property_package": vapor_props,
"has_phase_equilibrium": False
})
fs.cooler1 = Heater(default={
"property_package": vapor_props,
"has_phase_equilibrium": False
})
fs.compressor2 = IdealGasIsentropicCompressor(
default={
"property_package": vapor_props,
"has_phase_equilibrium": False
})
fs.equal_electric = pe.Constraint(
expr=fs.compressor1.work[0.0] == fs.compressor2.work[0.0])
fs.mixer = Mixer(
default={
'property_package': vapor_props,
'inlet_list': ['feed', 'recycle'],
'momentum_mixing_type': MomentumMixingType.equality
})
# Reactor
fs.reactor = StoichiometricReactor(
default={
'property_package': vapor_props,
'reaction_package': fs.reaction_params,
'has_heat_of_reaction': True,
'has_pressure_change': False
})
fs.reactor.conversion_eq = pe.Var()
fs.reactor.t_inv = pe.Var()
fs.reactor.p_sq_inv = pe.Var()
fs.reactor.conversion = pe.Var()
fs.reactor.consumption_rate = pe.Var()
fs.reactor.t_inv_con = pe.Constraint(expr=fs.reactor.t_inv *
fs.reactor.outlet.temperature[0] == 1)
fs.reactor.p_sq_inv_con = pe.Constraint(
expr=fs.reactor.p_sq_inv * fs.reactor.inlet.pressure[0]**2 == 1)
fs.reactor.conversion_eq_con = pe.Constraint(expr=(
fs.reactor.conversion_eq == 0.415 *
(1 - 26.25 * pe.exp(-18 * fs.reactor.t_inv) * fs.reactor.p_sq_inv)))
fs.reactor.conversion_con = pe.Constraint(
expr=(fs.reactor.conversion == fs.reactor.conversion_eq *
(1 - pe.exp(-5)) * (fs.reactor.inlet.mole_frac[0, "H2"] +
fs.reactor.inlet.mole_frac[0, "CO"] +
fs.reactor.inlet.mole_frac[0, "CH3OH"])))
fs.reactor.consumption_rate_con = pe.Constraint(
expr=(fs.reactor.consumption_rate == fs.reactor.conversion *
fs.reactor.inlet.mole_frac[0, "H2"] *
fs.reactor.inlet.flow_mol[0]))
fs.reactor.h2_consumption_con = pe.Constraint(expr=(
fs.reactor.outlet.flow_mol[0] *
fs.reactor.outlet.mole_frac[0, "H2"] == fs.reactor.inlet.flow_mol[0] *
fs.reactor.inlet.mole_frac[0, "H2"] - fs.reactor.consumption_rate))
fs.expander = Expander(default={
'property_package': vapor_props,
'has_phase_equilibrium': False
})
fs.cooler2 = Heater(default={
"property_package": vapor_props,
"has_phase_equilibrium": False
})
fs.flash = Flash(default={"property_package": props})
fs.purge_splitter = Separator(
default={
'property_package': vapor_props,
'outlet_list': ['purge', 'recycle'],
'ideal_separation': False
})
fs.compressor3 = IdealGasIsentropicCompressor(
default={
"property_package": vapor_props,
"has_phase_equilibrium": False
})
###########################
# Set scaling factors
###########################
fs.compressor1.control_volume.scaling_factor_energy.value = 1
fs.compressor2.control_volume.scaling_factor_energy.value = 1
fs.cooler1.control_volume.scaling_factor_energy.value = 1
fs.flash.control_volume.scaling_factor_energy.value = 1
fs.reactor.control_volume.scaling_factor_energy.value = 1
fs.cooler2.control_volume.scaling_factor_energy.value = 1
fs.compressor3.control_volume.scaling_factor_energy.value = 1
fs.mixer.scaling_factor_energy.value = 1
fs.cooler1.control_volume.scaling_factor_pressure.value = 1
fs.flash.control_volume.scaling_factor_pressure.value = 1
fs.reactor.control_volume.scaling_factor_pressure.value = 1
fs.cooler2.control_volume.scaling_factor_pressure.value = 1
###########################
# Objective
###########################
m.objective = pe.Objective(expr=(-fs.flash.liq_outlet.flow_mol[0.0]))
###########################
# Connect Units
###########################
fs.stream1 = network.Arc(source=feed.outlet,
destination=fs.compressor1.inlet)
fs.stream2 = network.Arc(source=fs.compressor1.outlet,
destination=fs.cooler1.inlet)
fs.stream3 = network.Arc(source=fs.cooler1.outlet,
destination=fs.compressor2.inlet)
fs.stream4 = network.Arc(source=fs.compressor2.outlet,
destination=fs.mixer.feed)
fs.stream5 = network.Arc(source=fs.mixer.outlet,
destination=fs.reactor.inlet)
fs.stream6 = network.Arc(source=fs.reactor.outlet,
destination=fs.expander.inlet)
fs.stream7 = network.Arc(source=fs.expander.outlet,
destination=fs.cooler2.inlet)
fs.stream8 = network.Arc(source=fs.cooler2.outlet,
destination=fs.flash.inlet)
fs.stream9 = network.Arc(source=fs.flash.vap_outlet,
destination=fs.purge_splitter.inlet)
fs.stream10 = network.Arc(source=fs.purge_splitter.recycle,
destination=fs.compressor3.inlet)
fs.stream11 = network.Arc(source=fs.compressor3.outlet,
destination=fs.mixer.recycle)
pe.TransformationFactory("network.expand_arcs").apply_to(m)
###########################
# Set problem specs
###########################
feed.flow_mol.fix(3.40898)
feed.pressure.fix(1)
feed.temperature.fix(3)
feed.mole_frac[0.0, "CH4"].fix(0.05)
feed.mole_frac[0.0, "CO"].fix(0.3)
feed.mole_frac[0.0, "H2"].fix(0.6)
feed.mole_frac[0.0, "CH3OH"].fix(0.05)
fs.cooler1.heat_duty[0.0].setub(0) # it is a cooler
fs.cooler1.outlet.temperature[0.0].setlb(3)
fs.flash.heat_duty.fix(0)
fs.flash.deltaP.fix(0)
fs.cooler2.heat_duty[0.0].setub(0) # it is a cooler
fs.cooler2.outlet.temperature[0.0].setlb(3)
fs.compressor2.outlet.pressure[0.0].setub(10)
fs.flash.liq_outlet.mole_frac[0.0, 'CH3OH'].expr.setlb(0.9)
fs.purge_splitter.split_fraction[0.0, 'purge'].fix(0.05)
###########################
# Prepare for initialization
###########################
fs.compressor1.outlet.pressure.fix(5)
fs.compressor2.outlet.pressure.fix(10)
fs.cooler1.outlet.temperature.fix(3)
fs.expander.outlet.pressure[0.0].fix(5)
fs.cooler2.outlet.temperature[0.0].fix(3)
fs.flash.liq_outlet.mole_frac[0.0, 'CH3OH'].expr.setlb(None)
# Setup decomposition process
seq = network.SequentialDecomposition()
seq.options.select_tear_method = "heuristic"
seq.options.tear_method = "Wegstein"
seq.options.iterLim = 5
# Determine tear stream and calculation order
G = seq.create_graph(m)
heu_result = seq.tear_set_arcs(G, method="heuristic")
order = seq.calculation_order(G)
# Display tear stream and calculation order
print("Tear")
for o in heu_result:
print(o.name)
print("Order")
for o in order:
for oo in o:
print(oo.name)
# Set guesses for tear stream
tear_guesses = {
"flow_mol": {
0: 10
},
"mole_frac": {
(0, 'CH3OH'): 0.06,
(0, 'CH4'): 0.21,
(0, 'CO'): 0.24,
(0, 'H2'): 0.50
},
"temperature": {
0: 4.4
},
"pressure": {
0: 15
}
}
seq.set_guesses_for(m.fs.reactor.inlet, tear_guesses)
# Define method for initialising each block
def function(unit):
unit.initialize(outlvl=1)
# Run sequential initialisation
seq.run(m, function)
###########################
# Unfix vars that were fixed for initialization
###########################
m.fs.compressor1.outlet.pressure.unfix()
m.fs.compressor2.outlet.pressure.unfix()
m.fs.cooler1.outlet.temperature.unfix()
m.fs.expander.outlet.pressure.unfix()
m.fs.cooler2.outlet.temperature.unfix()
m.fs.flash.liq_outlet.mole_frac[0.0, 'CH3OH'].expr.setlb(0.9)
return m
from pyomo.environ import ConcreteModel, SolverFactory, Constraint, value
from idaes.core import FlowsheetBlock
import Mod2_hda_ideal_VLE as thermo_props
from idaes.unit_models import Mixer
from idaes.core.util.model_statistics import degrees_of_freedom
m = ConcreteModel()
m.fs = FlowsheetBlock(default={"dynamic": False})
m.fs.properties = thermo_props.HDAParameterBlock()
m.fs.Mixer = Mixer(default={
"property_package": m.fs.properties,
"inlet_list": ["feed_1", "feed_2"]
})
#
for comp in m.fs.properties.component_list:
for phase in m.fs.properties.phase_list:
m.fs.Mixer.feed_1.flow_mol_phase_comp[0, phase, comp].fix(1e-5)
m.fs.Mixer.feed_2.flow_mol_phase_comp[0, phase, comp].fix(1e-5)
print("Degrees of Freedom =", degrees_of_freedom(m))
# m.fs.Mixer.report()
def create_model():
"""Create the flowsheet and add unit models. Fixing model inputs is done
in a separate function to try to keep this fairly clean and easy to follow.
Args:
None
Returns:
(ConcreteModel) Steam cycle model
"""
############################################################################
# Flowsheet and Properties #
############################################################################
m = pyo.ConcreteModel(name="Steam Cycle Model")
m.fs = FlowsheetBlock(default={"dynamic":
False}) # Add steady state flowsheet
# A physical property parameter block for IAPWS-95 with pressure and enthalpy
# (PH) state variables. Usually pressure and enthalpy state variables are
# more robust especially when the phases are unknown.
m.fs.prop_water = iapws95.Iapws95ParameterBlock(
default={"phase_presentation": iapws95.PhaseType.LG})
# A physical property parameter block with temperature, pressure and vapor
# fraction (TPx) state variables. There are a few instances where the vapor
# fraction is known and the temperature and pressure state variables are
# preferable.
m.fs.prop_water_tpx = iapws95.Iapws95ParameterBlock(
default={
"phase_presentation": iapws95.PhaseType.LG,
"state_vars": iapws95.StateVars.TPX,
})
############################################################################
# Turbine with fill-in reheat constraints #
############################################################################
# The TurbineMultistage class allows creation of the full turbine model by
# providing several configuration options, including: throttle valves;
# high-, intermediate-, and low-pressure sections; steam extractions; and
# pressure driven flow. See the IDAES documentation for details.
m.fs.turb = TurbineMultistage(
default={
"property_package": m.fs.prop_water,
"num_parallel_inlet_stages": 4, # number of admission arcs
"num_hp": 7, # number of high-pressure stages
"num_ip": 10, # number of intermediate-pressure stages
"num_lp": 11, # number of low-pressure stages
"hp_split_locations": [4, 7], # hp steam extraction locations
"ip_split_locations": [5, 10], # ip steam extraction locations
"lp_split_locations": [4, 8, 10, 11
], # lp steam extraction locations
"hp_disconnect": [7], # disconnect hp from ip to insert reheater
"ip_split_num_outlets": {
10: 3
}, # number of split streams (default is 2)
})
# This model is only the steam cycle, and the reheater is part of the boiler.
# To fill in the reheater gap, a few constraints for the flow, pressure drop,
# and outlet temperature are added. A detailed boiler model can be coupled later.
#
# hp_split[7] is the splitter directly after the last HP stage. The splitter
# outlet "outlet_1" is always taken to be the main steam flow through the turbine.
# When the turbine model was instantiated the stream from the HP section to the IP
# section was omitted, so the reheater could be inserted.
# The flow constraint sets flow from outlet_1 of the splitter equal to
# flow into the IP turbine.
@m.fs.turb.Constraint(m.fs.time)
def constraint_reheat_flow(b, t):
return b.ip_stages[1].inlet.flow_mol[t] == b.hp_split[
7].outlet_1.flow_mol[t]
# Create a variable for pressure change in the reheater (assuming
# reheat_delta_p should be negative).
m.fs.turb.reheat_delta_p = pyo.Var(m.fs.time, initialize=0)
# Add a constraint to calculate the IP section inlet pressure based on the
# pressure drop in the reheater and the outlet pressure of the HP section.
@m.fs.turb.Constraint(m.fs.time)
def constraint_reheat_press(b, t):
return (b.ip_stages[1].inlet.pressure[t] ==
b.hp_split[7].outlet_1.pressure[t] + b.reheat_delta_p[t])
# Create a variable for reheat temperature and fix it to the desired reheater
# outlet temperature
m.fs.turb.reheat_out_T = pyo.Var(m.fs.time, initialize=866)
# Create a constraint for the IP section inlet temperature.
@m.fs.turb.Constraint(m.fs.time)
def constraint_reheat_temp(b, t):
return (b.ip_stages[1].control_volume.properties_in[t].temperature ==
b.reheat_out_T[t])
############################################################################
# Add Condenser/hotwell/condensate pump #
############################################################################
# Add a mixer for all the streams coming into the condenser. In this case the
# main steam, and the boiler feed pump turbine outlet go to the condenser
m.fs.condenser_mix = Mixer(
default={
"momentum_mixing_type": MomentumMixingType.none,
"inlet_list": ["main", "bfpt"],
"property_package": m.fs.prop_water,
})
# The pressure in the mixer comes from the connection to the condenser. All
# the streams coming in and going out of the mixer are equal, but we created
# the mixer with no calculation for the unit pressure. Here a constraint that
# specifies that the mixer pressure is equal to the main steam pressure is
# added. There is also a constraint that specifies the that BFP turbine outlet
# pressure is the same as the condenser pressure. Combined with the stream
# connections between units, these constraints effectively specify that the
# mixer inlet and outlet streams all have the same pressure.
@m.fs.condenser_mix.Constraint(m.fs.time)
def mixer_pressure_constraint(b, t):
return b.main_state[t].pressure == b.mixed_state[t].pressure
# The condenser model uses the physical property model with TPx state
# variables, while the rest of the model uses PH state variables. To
# translate between the two property calculations, an extra port is added to
# the mixer which contains temperature, pressure, and vapor fraction
# quantities. The first step is to add references to the temperature and
# vapor fraction expressions in the IAPWS-95 property block. The references
# are used to handle time indexing in the ports by using the property blocks
# time index to create references that appear to be time indexed variables.
# These references mirror the references created by the framework automatically
# for the existing ports.
m.fs.condenser_mix._outlet_temperature_ref = pyo.Reference(
m.fs.condenser_mix.mixed_state[:].temperature)
m.fs.condenser_mix._outlet_vapor_fraction_ref = pyo.Reference(
m.fs.condenser_mix.mixed_state[:].vapor_frac)
# Add the new port with the state information that needs to go to the
# condenser
m.fs.condenser_mix.outlet_tpx = Port(
initialize={
"flow_mol": m.fs.condenser_mix._outlet_flow_mol_ref,
"temperature": m.fs.condenser_mix._outlet_temperature_ref,
"pressure": m.fs.condenser_mix._outlet_pressure_ref,
"vapor_frac": m.fs.condenser_mix._outlet_vapor_fraction_ref,
})
# Add the heat exchanger model for the condenser.
m.fs.condenser = HeatExchanger(
default={
"delta_temperature_callback": delta_temperature_underwood_callback,
"shell": {
"property_package": m.fs.prop_water_tpx
},
"tube": {
"property_package": m.fs.prop_water
},
})
m.fs.condenser.delta_temperature_out.fix(5)
# Everything condenses so the saturation pressure determines the condenser
# pressure. Deactivate the constraint that is used in the TPx version vapor
# fraction constraint and fix vapor fraction to 0.
m.fs.condenser.shell.properties_out[:].eq_complementarity.deactivate()
m.fs.condenser.shell.properties_out[:].vapor_frac.fix(0)
# There is some subcooling in the condenser, so we assume the condenser
# pressure is actually going to be slightly higher than the saturation
# pressure.
m.fs.condenser.pressure_over_sat = pyo.Var(
m.fs.time,
initialize=500,
doc="Pressure added to Psat in the condeser. This is to account for"
"some subcooling. (Pa)",
)
# Add a constraint for condenser pressure
@m.fs.condenser.Constraint(m.fs.time)
def eq_pressure(b, t):
return (b.shell.properties_out[t].pressure ==
b.shell.properties_out[t].pressure_sat +
b.pressure_over_sat[t])
# Extra port on condenser to hook back up to pressure-enthalpy properties
m.fs.condenser._outlet_1_enth_mol_ref = pyo.Reference(
m.fs.condenser.shell.properties_out[:].enth_mol)
m.fs.condenser.outlet_1_ph = Port(
initialize={
"flow_mol": m.fs.condenser._outlet_1_flow_mol_ref,
"pressure": m.fs.condenser._outlet_1_pressure_ref,
"enth_mol": m.fs.condenser._outlet_1_enth_mol_ref,
})
# Add the condenser hotwell. In steady state a mixer will work. This is
# where makeup water is added if needed.
m.fs.hotwell = Mixer(
default={
"momentum_mixing_type": MomentumMixingType.none,
"inlet_list": ["condensate", "makeup"],
"property_package": m.fs.prop_water,
})
# The hotwell is assumed to be at the same pressure as the condenser.
@m.fs.hotwell.Constraint(m.fs.time)
def mixer_pressure_constraint(b, t):
return b.condensate_state[t].pressure == b.mixed_state[t].pressure
# Condensate pump
m.fs.cond_pump = PressureChanger(
default={
"property_package": m.fs.prop_water,
"thermodynamic_assumption": ThermodynamicAssumption.pump,
})
############################################################################
# Add low pressure feedwater heaters #
############################################################################
# All the feedwater heater sections will be set to use the Underwood
# approximation for LMTD, so create the fwh_config dict to make the config
# slightly cleaner
fwh_config = {
"delta_temperature_callback": delta_temperature_underwood_callback
}
# The feedwater heater model allows feedwater heaters with a desuperheat,
# condensing, and subcooling section to be added an a reasonably simple way.
# See the IDAES documentation for more information of configuring feedwater
# heaters
m.fs.fwh1 = FWH0D(
default={
"has_desuperheat": False,
"has_drain_cooling": False,
"has_drain_mixer": True,
"property_package": m.fs.prop_water,
"condense": fwh_config,
})
# pump for fwh1 condensate, to pump it ahead and mix with feedwater
m.fs.fwh1_pump = PressureChanger(
default={
"property_package": m.fs.prop_water,
"thermodynamic_assumption": ThermodynamicAssumption.pump,
})
# Mix the FWH1 drain back into the feedwater
m.fs.fwh1_return = Mixer(
default={
"momentum_mixing_type": MomentumMixingType.none,
"inlet_list": ["feedwater", "fwh1_drain"],
"property_package": m.fs.prop_water,
})
# Set the mixer pressure to the feedwater pressure
@m.fs.fwh1_return.Constraint(m.fs.time)
def mixer_pressure_constraint(b, t):
return b.feedwater_state[t].pressure == b.mixed_state[t].pressure
# Add the rest of the low pressure feedwater heaters
m.fs.fwh2 = FWH0D(
default={
"has_desuperheat": True,
"has_drain_cooling": True,
"has_drain_mixer": True,
"property_package": m.fs.prop_water,
"desuperheat": fwh_config,
"cooling": fwh_config,
"condense": fwh_config,
})
m.fs.fwh3 = FWH0D(
default={
"has_desuperheat": True,
"has_drain_cooling": True,
"has_drain_mixer": True,
"property_package": m.fs.prop_water,
"desuperheat": fwh_config,
"cooling": fwh_config,
"condense": fwh_config,
})
m.fs.fwh4 = FWH0D(
default={
"has_desuperheat": True,
"has_drain_cooling": True,
"has_drain_mixer": False,
"property_package": m.fs.prop_water,
"desuperheat": fwh_config,
"cooling": fwh_config,
"condense": fwh_config,
})
############################################################################
# Add deaerator and boiler feed pump (BFP) #
############################################################################
# The deaerator is basically an open tank with multiple inlets. For steady-
# state, a mixer model is sufficient.
m.fs.fwh5_da = Mixer(
default={
"momentum_mixing_type": MomentumMixingType.none,
"inlet_list": ["steam", "drain", "feedwater"],
"property_package": m.fs.prop_water,
})
@m.fs.fwh5_da.Constraint(m.fs.time)
def mixer_pressure_constraint(b, t):
# Not sure about deaerator pressure, so assume same as feedwater inlet
return b.feedwater_state[t].pressure == b.mixed_state[t].pressure
# Add the boiler feed pump and boiler feed pump turbine
m.fs.bfp = PressureChanger(
default={
"property_package": m.fs.prop_water,
"thermodynamic_assumption": ThermodynamicAssumption.pump,
})
m.fs.bfpt = PressureChanger(
default={
"property_package": m.fs.prop_water,
"compressor": False,
"thermodynamic_assumption": ThermodynamicAssumption.isentropic,
})
# The boiler feed pump outlet pressure is the same as the condenser
@m.fs.Constraint(m.fs.time)
def constraint_out_pressure(b, t):
return (b.bfpt.control_volume.properties_out[t].pressure ==
b.condenser.shell.properties_out[t].pressure)
# Instead of specifying a fixed efficiency, specify that the steam is just
# starting to condense at the outlet of the boiler feed pump turbine. This
# ensures approximately the right behavior in the turbine. With a fixed
# efficiency, depending on the conditions you can get odd things like steam
# fully condensing in the turbine.
@m.fs.Constraint(m.fs.time)
def constraint_out_enthalpy(b, t):
return (
b.bfpt.control_volume.properties_out[t].enth_mol ==
b.bfpt.control_volume.properties_out[t].enth_mol_sat_phase["Vap"] -
200)
# The boiler feed pump power is the same as the power generated by the
# boiler feed pump turbine. This constraint determines the steam flow to the
# BFP turbine. The turbine work is negative for power out, while pump work
# is positive for power in.
@m.fs.Constraint(m.fs.time)
def constraint_bfp_power(b, t):
return 0 == b.bfp.control_volume.work[t] + b.bfpt.control_volume.work[t]
############################################################################
# Add high pressure feedwater heaters #
############################################################################
m.fs.fwh6 = FWH0D(
default={
"has_desuperheat": True,
"has_drain_cooling": True,
"has_drain_mixer": True,
"property_package": m.fs.prop_water,
"desuperheat": fwh_config,
"cooling": fwh_config,
"condense": fwh_config,
})
m.fs.fwh7 = FWH0D(
default={
"has_desuperheat": True,
"has_drain_cooling": True,
"has_drain_mixer": True,
"property_package": m.fs.prop_water,
"desuperheat": fwh_config,
"cooling": fwh_config,
"condense": fwh_config,
})
m.fs.fwh8 = FWH0D(
default={
"has_desuperheat": True,
"has_drain_cooling": True,
"has_drain_mixer": False,
"property_package": m.fs.prop_water,
"desuperheat": fwh_config,
"cooling": fwh_config,
"condense": fwh_config,
})
############################################################################
# Additional Constraints/Expressions #
############################################################################
# Add a few constraints to allow a for complete plant results despite the
# lack of a detailed boiler model.
# Boiler pressure drop
m.fs.boiler_pressure_drop_fraction = pyo.Var(
m.fs.time,
initialize=0.01,
doc="Fraction of pressure lost from boiler feed pump and turbine inlet",
)
@m.fs.Constraint(m.fs.time)
def boiler_pressure_drop(b, t):
return (m.fs.bfp.control_volume.properties_out[t].pressure *
(1 - b.boiler_pressure_drop_fraction[t]) ==
m.fs.turb.inlet_split.mixed_state[t].pressure)
# Again, since the boiler is missing, set the flow of steam into the turbine
# equal to the flow of feedwater out of the last feedwater heater.
@m.fs.Constraint(m.fs.time)
def close_flow(b, t):
return (m.fs.bfp.control_volume.properties_out[t].flow_mol ==
m.fs.turb.inlet_split.mixed_state[t].flow_mol)
# Calculate the amount of heat that is added in the boiler, including the
# reheater.
@m.fs.Expression(m.fs.time)
def boiler_heat(b, t):
return (b.turb.inlet_split.mixed_state[t].enth_mol *
b.turb.inlet_split.mixed_state[t].flow_mol -
b.fwh8.desuperheat.tube.properties_out[t].enth_mol *
b.fwh8.desuperheat.tube.properties_out[t].flow_mol +
b.turb.ip_stages[1].control_volume.properties_in[t].enth_mol *
b.turb.ip_stages[1].control_volume.properties_in[t].flow_mol -
b.turb.hp_split[7].outlet_1.enth_mol[t] *
b.turb.hp_split[7].outlet_1.flow_mol[t])
# Calculate the efficiency of the steam cycle. This doesn't account for
# heat loss in the boiler, so actual plant efficiency would be lower.
@m.fs.Expression(m.fs.time)
def steam_cycle_eff(b, t):
return -100 * b.turb.power[t] / b.boiler_heat[t]
############################################################################
## Create the stream Arcs ##
############################################################################
############################################################################
# Connect turbine and condenser units #
############################################################################
m.fs.EXHST_MAIN = Arc(source=m.fs.turb.outlet_stage.outlet,
destination=m.fs.condenser_mix.main)
m.fs.condenser_mix_to_condenser = Arc(source=m.fs.condenser_mix.outlet_tpx,
destination=m.fs.condenser.inlet_1)
m.fs.COND_01 = Arc(source=m.fs.condenser.outlet_1_ph,
destination=m.fs.hotwell.condensate)
m.fs.COND_02 = Arc(source=m.fs.hotwell.outlet,
destination=m.fs.cond_pump.inlet)
############################################################################
# Low pressure FWHs #
############################################################################
m.fs.EXTR_LP11 = Arc(source=m.fs.turb.lp_split[11].outlet_2,
destination=m.fs.fwh1.drain_mix.steam)
m.fs.COND_03 = Arc(source=m.fs.cond_pump.outlet,
destination=m.fs.fwh1.condense.inlet_2)
m.fs.FWH1_DRN1 = Arc(source=m.fs.fwh1.condense.outlet_1,
destination=m.fs.fwh1_pump.inlet)
m.fs.FWH1_DRN2 = Arc(source=m.fs.fwh1_pump.outlet,
destination=m.fs.fwh1_return.fwh1_drain)
m.fs.FW01A = Arc(source=m.fs.fwh1.condense.outlet_2,
destination=m.fs.fwh1_return.feedwater)
# fwh2
m.fs.FW01B = Arc(source=m.fs.fwh1_return.outlet,
destination=m.fs.fwh2.cooling.inlet_2)
m.fs.FWH2_DRN = Arc(source=m.fs.fwh2.cooling.outlet_1,
destination=m.fs.fwh1.drain_mix.drain)
m.fs.EXTR_LP10 = Arc(
source=m.fs.turb.lp_split[10].outlet_2,
destination=m.fs.fwh2.desuperheat.inlet_1,
)
# fwh3
m.fs.FW02 = Arc(source=m.fs.fwh2.desuperheat.outlet_2,
destination=m.fs.fwh3.cooling.inlet_2)
m.fs.FWH3_DRN = Arc(source=m.fs.fwh3.cooling.outlet_1,
destination=m.fs.fwh2.drain_mix.drain)
m.fs.EXTR_LP8 = Arc(source=m.fs.turb.lp_split[8].outlet_2,
destination=m.fs.fwh3.desuperheat.inlet_1)
# fwh4
m.fs.FW03 = Arc(source=m.fs.fwh3.desuperheat.outlet_2,
destination=m.fs.fwh4.cooling.inlet_2)
m.fs.FWH4_DRN = Arc(source=m.fs.fwh4.cooling.outlet_1,
destination=m.fs.fwh3.drain_mix.drain)
m.fs.EXTR_LP4 = Arc(source=m.fs.turb.lp_split[4].outlet_2,
destination=m.fs.fwh4.desuperheat.inlet_1)
############################################################################
# FWH5 (Deaerator) and boiler feed pump (BFP) #
############################################################################
m.fs.FW04 = Arc(source=m.fs.fwh4.desuperheat.outlet_2,
destination=m.fs.fwh5_da.feedwater)
m.fs.EXTR_IP10 = Arc(source=m.fs.turb.ip_split[10].outlet_2,
destination=m.fs.fwh5_da.steam)
m.fs.FW05A = Arc(source=m.fs.fwh5_da.outlet, destination=m.fs.bfp.inlet)
m.fs.EXTR_BFPT_A = Arc(source=m.fs.turb.ip_split[10].outlet_3,
destination=m.fs.bfpt.inlet)
m.fs.EXHST_BFPT = Arc(source=m.fs.bfpt.outlet,
destination=m.fs.condenser_mix.bfpt)
############################################################################
# High-pressure feedwater heaters #
############################################################################
# fwh6
m.fs.FW05B = Arc(source=m.fs.bfp.outlet,
destination=m.fs.fwh6.cooling.inlet_2)
m.fs.FWH6_DRN = Arc(source=m.fs.fwh6.cooling.outlet_1,
destination=m.fs.fwh5_da.drain)
m.fs.EXTR_IP5 = Arc(source=m.fs.turb.ip_split[5].outlet_2,
destination=m.fs.fwh6.desuperheat.inlet_1)
# fwh7
m.fs.FW06 = Arc(source=m.fs.fwh6.desuperheat.outlet_2,
destination=m.fs.fwh7.cooling.inlet_2)
m.fs.FWH7_DRN = Arc(source=m.fs.fwh7.cooling.outlet_1,
destination=m.fs.fwh6.drain_mix.drain)
m.fs.EXTR_HP7 = Arc(source=m.fs.turb.hp_split[7].outlet_2,
destination=m.fs.fwh7.desuperheat.inlet_1)
# fwh8
m.fs.FW07 = Arc(source=m.fs.fwh7.desuperheat.outlet_2,
destination=m.fs.fwh8.cooling.inlet_2)
m.fs.FWH8_DRN = Arc(source=m.fs.fwh8.cooling.outlet_1,
destination=m.fs.fwh7.drain_mix.drain)
m.fs.EXTR_HP4 = Arc(source=m.fs.turb.hp_split[4].outlet_2,
destination=m.fs.fwh8.desuperheat.inlet_1)
############################################################################
# Turn the Arcs into constraints and return the model #
############################################################################
pyo.TransformationFactory("network.expand_arcs").apply_to(m.fs)
return m
