def m():
m = ConcreteModel()
m.fs = FlowsheetBlock(default={"dynamic": False})
m.fs.thermo_params = thermo_props.SaponificationParameterBlock()
m.fs.reaction_params = rxn_props.SaponificationReactionParameterBlock(
default={"property_package": m.fs.thermo_params})
m.fs.tank1 = CSTR(default={"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params})
m.fs.tank2 = CSTR(default={"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params})
m.fs.tank_array = CSTR(
range(3),
default={"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params})
m.fs.stream = Arc(source=m.fs.tank1.outlet,
destination=m.fs.tank2.inlet)
def stream_array_rule(b, i):
return (b.tank_array[i].outlet, b.tank_array[i+1].inlet)
m.fs.stream_array = Arc(range(2), rule=stream_array_rule)
TransformationFactory("network.expand_arcs").apply_to(m)
return m
def HX1D_array_model():
# An example of maximum perversity. Dynamics, 1D control volumes, and
# an indexed unit
unit_set = range(3)
time_set = [0,5]
time_units=pyunits.s
fs_cfg = {
"dynamic": True, "time_set": time_set, "time_units": time_units}
m = ConcreteModel()
m.fs = FlowsheetBlock(default=fs_cfg)
m.fs.properties = thermo_props.SaponificationParameterBlock()
m.fs.unit_array = HX1D(unit_set,default={
"shell_side": {"property_package": m.fs.properties},
"tube_side": {"property_package": m.fs.properties}})
def tube_stream_array_rule(b, i):
return {'source':b.unit_array[i].tube_outlet,
'destination':b.unit_array[i+1].tube_inlet}
m.fs.tube_stream_array = Arc(range(2), rule=tube_stream_array_rule)
def shell_stream_array_rule(b, i):
return {'source':b.unit_array[i+1].shell_outlet,
'destination':b.unit_array[i].shell_inlet}
m.fs.shell_stream_array = Arc(range(1,-1,-1), rule=shell_stream_array_rule)
TransformationFactory("network.expand_arcs").apply_to(m)
return m
def test_create_stream_table_dataframe_from_StateBlock_time():
m = ConcreteModel()
m.fs = FlowsheetBlock(default={"dynamic": False, "time_set": [3]})
m.fs.thermo_params = thermo_props.SaponificationParameterBlock()
m.fs.reaction_params = rxn_props.SaponificationReactionParameterBlock(
default={"property_package": m.fs.thermo_params})
m.fs.tank1 = CSTR(default={"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params})
m.fs.tank2 = CSTR(default={"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params})
m.fs.stream = Arc(source=m.fs.tank1.outlet,
destination=m.fs.tank2.inlet)
TransformationFactory("network.expand_arcs").apply_to(m)
df = create_stream_table_dataframe({
"state": m.fs.tank1.control_volume.properties_out},
time_point=3)
assert df.loc["Pressure"]["state"] == 101325
assert df.loc["Temperature"]["state"] == 298.15
assert df.loc["Volumetric Flowrate"]["state"] == 1.0
assert df.loc["Molar Concentration H2O"]["state"] == 100.0
assert df.loc["Molar Concentration NaOH"]["state"] == 100.0
assert df.loc["Molar Concentration EthylAcetate"]["state"] == 100.0
assert df.loc["Molar Concentration SodiumAcetate"]["state"] == 100.0
assert df.loc["Molar Concentration Ethanol"]["state"] == 100.0
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
m.fs = FlowsheetBlock(default={"dynamic": False})
# 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.Tank1 = CSTR(
default={
"property_package": m.fs.thermo_params,
"reaction_package": m.fs.reaction_params,
"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_equilibrium_reactions": False,
"has_heat_of_reaction": True,
"has_heat_transfer": True,
"has_pressure_change": False
})
# Make Streams to connect units
m.fs.stream = Arc(source=m.fs.Tank1.outlet, destination=m.fs.Tank2.inlet)
TransformationFactory("network.expand_arcs").apply_to(m)
# Set inlet and operating conditions, and some initial conditions.
m.fs.Tank1.inlet.flow_vol[0].fix(1.0)
m.fs.Tank1.inlet.conc_mol_comp[0, "H2O"].fix(55388.0)
m.fs.Tank1.inlet.conc_mol_comp[0, "NaOH"].fix(100.0)
m.fs.Tank1.inlet.conc_mol_comp[0, "EthylAcetate"].fix(100.0)
m.fs.Tank1.inlet.conc_mol_comp[0, "SodiumAcetate"].fix(0.0)
m.fs.Tank1.inlet.conc_mol_comp[0, "Ethanol"].fix(0.0)
m.fs.Tank1.inlet.temperature[0].fix(303.15)
m.fs.Tank1.inlet.pressure[0].fix(101325.0)
m.fs.Tank1.volume.fix(1.0)
m.fs.Tank1.heat_duty.fix(0.0)
m.fs.Tank2.volume.fix(1.0)
m.fs.Tank2.heat_duty.fix(0.0)
# Initialize Units
m.fs.Tank1.initialize()
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
})
# =========================================================================
# Adding Optimization
m.fs.obj = Objective(expr=m.fs.Tank2.outlet.conc_mol_comp[0,
"SodiumAcetate"],
sense=maximize)
# Add additional constraint
m.fs.volume_constraint = Constraint(expr=m.fs.Tank1.volume[0] +
m.fs.Tank2.volume[0] == 3.0)
# Set bounds for variables
m.fs.Tank1.volume[0].setlb(0.5)
m.fs.Tank1.volume[0].setub(5.0)
m.fs.Tank2.volume[0].setlb(0.5)
m.fs.Tank2.volume[0].setub(5.0)
# Unfix heat inputs
m.fs.Tank1.volume.unfix()
m.fs.Tank2.volume.unfix()
# =========================================================================
# Create a solver
solver = SolverFactory('ipopt')
results = solver.solve(m, tee=True)
# Print results
print(results)
print()
print("Results")
print()
print("Tank 1 Volume")
m.fs.Tank1.volume.display()
print()
print("Tank 2 Volume")
m.fs.Tank2.volume.display()
print()
print("Tank 1 Outlet")
m.fs.Tank1.outlet.display()
print()
print("Tank 2 Outlet")
m.fs.Tank2.outlet.display()
# For testing purposes
return (m, results)
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)