def test_model_checks():
m = ConcreteModel()
m.fs = Flowsheet(default={"dynamic": False})
m.fs.pp = PhysicalParameterTestBlock()
m.fs.sep = Separator(default={
"property_package": m.fs.pp,
"ideal_separation": False})
m.fs.sep.model_check()
assert m.fs.sep.outlet_1_state[0].check is True
assert m.fs.sep.outlet_2_state[0].check is True
assert m.fs.sep.mixed_state[0].check is True
def test_initialize():
m = ConcreteModel()
m.fs = Flowsheet(default={"dynamic": False})
m.fs.pp = PhysicalParameterTestBlock()
m.fs.sb = TestStateBlock(m.fs.time, default={"parameters": m.fs.pp})
m.fs.sep = Separator(
default={
"property_package": m.fs.pp,
"mixed_state_block": m.fs.sb,
"ideal_separation": False,
"split_basis": SplittingType.phaseComponentFlow
})
# Change one outlet pressure to check initialization calculations
m.fs.sep.outlet_1_state[0].pressure = 8e4
f = m.fs.sep.initialize(hold_state=True)
assert m.fs.sep.outlet_1_state[0].init_test is True
assert m.fs.sep.outlet_2_state[0].init_test is True
assert m.fs.sb[0].init_test is True
assert m.fs.sep.outlet_1_state[0].hold_state is False
assert m.fs.sep.outlet_2_state[0].hold_state is False
assert m.fs.sb[0].hold_state is True
assert m.fs.sep.outlet_1.component_flow[0, "p1", "c1"].value == 0.5
assert m.fs.sep.outlet_1.component_flow[0, "p1", "c2"].value == 0.5
assert m.fs.sep.outlet_1.component_flow[0, "p2", "c1"].value == 0.5
assert m.fs.sep.outlet_1.component_flow[0, "p2", "c2"].value == 0.5
assert m.fs.sep.outlet_1.enthalpy[0, "p1"].value == 2
assert m.fs.sep.outlet_1.enthalpy[0, "p2"].value == 2
assert m.fs.sep.outlet_1.pressure[0].value == 1e5
assert m.fs.sep.outlet_2.component_flow[0, "p1", "c1"].value == 0.5
assert m.fs.sep.outlet_2.component_flow[0, "p1", "c2"].value == 0.5
assert m.fs.sep.outlet_2.component_flow[0, "p2", "c1"].value == 0.5
assert m.fs.sep.outlet_2.component_flow[0, "p2", "c2"].value == 0.5
assert m.fs.sep.outlet_2.enthalpy[0, "p1"].value == 2
assert m.fs.sep.outlet_2.enthalpy[0, "p2"].value == 2
assert m.fs.sep.outlet_2.pressure[0].value == 1e5
m.fs.sep.release_state(flags=f)
assert m.fs.sep.outlet_1_state[0].hold_state is False
assert m.fs.sep.outlet_2_state[0].hold_state is False
assert m.fs.sb[0].hold_state is False
def test_initialize_inconsistent_keys():
m = ConcreteModel()
m.fs = Flowsheet(default={"dynamic": False})
m.fs.pp = PhysicalParameterTestBlock()
m.fs.sb = TestStateBlock(m.fs.time, default={"parameters": m.fs.pp})
m.fs.sep = Separator(default={
"property_package": m.fs.pp,
"mixed_state_block": m.fs.sb,
"ideal_separation": False,
"split_basis": SplittingType.phaseFlow})
# Change one outlet pressure to check initialization calculations
m.fs.sep.outlet_1_state[0].pressure = 8e4
with pytest.raises(KeyError):
m.fs.sep.initialize()
def test_build_default():
m = ConcreteModel()
m.fs = Flowsheet(default={"dynamic": False})
m.fs.pp = PhysicalParameterTestBlock()
m.fs.sep = Separator(default={"property_package": m.fs.pp,
"ideal_separation": False})
assert isinstance(m.fs.sep.material_splitting_eqn, Constraint)
assert len(m.fs.sep.material_splitting_eqn) == 8
assert isinstance(m.fs.sep.temperature_equality_eqn, Constraint)
assert len(m.fs.sep.temperature_equality_eqn) == 2
assert isinstance(m.fs.sep.pressure_equality_eqn, Constraint)
assert len(m.fs.sep.pressure_equality_eqn) == 2
assert isinstance(m.fs.sep.outlet_1, Port)
assert isinstance(m.fs.sep.outlet_2, Port)
assert isinstance(m.fs.sep.inlet, Port)
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 build(self):
"""
Begin building model (pre-DAE transformation).
Args:
None
Returns:
None
"""
# Call UnitModel.build to setup dynamics
super(FlashData, self).build()
# Build Control Volume
self.control_volume = ControlVolume0DBlock(
default={
"dynamic": self.config.dynamic,
"has_holdup": self.config.has_holdup,
"property_package": self.config.property_package,
"property_package_args": self.config.property_package_args
})
self.control_volume.add_state_blocks(has_phase_equilibrium=True)
self.control_volume.add_material_balances(
balance_type=self.config.material_balance_type,
has_phase_equilibrium=True)
self.control_volume.add_energy_balances(
balance_type=self.config.energy_balance_type,
has_heat_transfer=self.config.has_heat_transfer)
self.control_volume.add_momentum_balances(
balance_type=self.config.momentum_balance_type,
has_pressure_change=self.config.has_pressure_change)
# Add Ports
self.add_inlet_port()
split_map = {}
for p in self.config.property_package.phase_list:
split_map[p] = p
self.split = Separator(
default={
"property_package": self.config.property_package,
"property_package_args": self.config.property_package_args,
"outlet_list": ["Vap", "Liq"],
"split_basis": SplittingType.phaseFlow,
"ideal_separation": True,
"ideal_split_map": split_map,
"mixed_state_block": self.control_volume.properties_out
})
self.vap_outlet = Port(extends=self.split.Vap)
self.liq_outlet = Port(extends=self.split.Liq)
# Add references
if (self.config.has_heat_transfer is True
and self.config.energy_balance_type != 'none'):
add_object_reference(self, "heat_duty", self.control_volume.heat)
if (self.config.has_pressure_change is True
and self.config.momentum_balance_type != 'none'):
add_object_reference(self, "deltaP", self.control_volume.deltaP)
def test_initialize_total_flow():
m = ConcreteModel()
m.fs = FlowsheetBlock(default={"dynamic": False})
m.fs.properties = SaponificationParameterBlock()
m.fs.sb = Separator(default={
"property_package": m.fs.properties,
"ideal_separation": False,
"split_basis": SplittingType.totalFlow})
m.fs.sb.inlet.flow_vol.fix(1.0e-03)
m.fs.sb.inlet.conc_mol_comp[0, "H2O"].fix(55388.0)
m.fs.sb.inlet.conc_mol_comp[0, "NaOH"].fix(100.0)
m.fs.sb.inlet.conc_mol_comp[0, "EthylAcetate"].fix(100.0)
m.fs.sb.inlet.conc_mol_comp[0, "SodiumAcetate"].fix(0.0)
m.fs.sb.inlet.conc_mol_comp[0, "Ethanol"].fix(0.0)
m.fs.sb.inlet.temperature.fix(303.15)
m.fs.sb.inlet.pressure.fix(101325.0)
m.fs.sb.split_fraction[0, "outlet_1"].fix(0.2)
assert degrees_of_freedom(m) == 0
m.fs.sb.initialize(outlvl=5, optarg={'tol': 1e-6})
assert (pytest.approx(0.2, abs=1e-3) ==
m.fs.sb.split_fraction[0, "outlet_1"].value)
assert (pytest.approx(0.8, abs=1e-3) ==
m.fs.sb.split_fraction[0, "outlet_2"].value)
assert (pytest.approx(101325.0, abs=1e-2) ==
m.fs.sb.outlet_1.pressure[0].value)
assert (pytest.approx(303.15, abs=1e-2) ==
m.fs.sb.outlet_1.temperature[0].value)
assert (pytest.approx(2e-4, abs=1e-6) ==
m.fs.sb.outlet_1.flow_vol[0].value)
assert (pytest.approx(55388.0, abs=1e-2) ==
m.fs.sb.outlet_1.conc_mol_comp[0, "H2O"].value)
assert (pytest.approx(100.0, abs=1e-2) ==
m.fs.sb.outlet_1.conc_mol_comp[0, "NaOH"].value)
assert (pytest.approx(100.0, abs=1e-2) ==
m.fs.sb.outlet_1.conc_mol_comp[0, "EthylAcetate"].value)
assert (pytest.approx(0.0, abs=1e-2) ==
m.fs.sb.outlet_1.conc_mol_comp[0, "SodiumAcetate"].value)
assert (pytest.approx(0.0, abs=1e-2) ==
m.fs.sb.outlet_1.conc_mol_comp[0, "Ethanol"].value)
assert (pytest.approx(101325.0, abs=1e-2) ==
m.fs.sb.outlet_2.pressure[0].value)
assert (pytest.approx(303.15, abs=1e-2) ==
m.fs.sb.outlet_2.temperature[0].value)
assert (pytest.approx(8e-4, abs=1e-6) ==
m.fs.sb.outlet_2.flow_vol[0].value)
assert (pytest.approx(55388.0, abs=1e-2) ==
m.fs.sb.outlet_2.conc_mol_comp[0, "H2O"].value)
assert (pytest.approx(100.0, abs=1e-2) ==
m.fs.sb.outlet_2.conc_mol_comp[0, "NaOH"].value)
assert (pytest.approx(100.0, abs=1e-2) ==
m.fs.sb.outlet_2.conc_mol_comp[0, "EthylAcetate"].value)
assert (pytest.approx(0.0, abs=1e-2) ==
m.fs.sb.outlet_2.conc_mol_comp[0, "SodiumAcetate"].value)
assert (pytest.approx(0.0, abs=1e-2) ==
m.fs.sb.outlet_2.conc_mol_comp[0, "Ethanol"].value)