def test_initialize(self, Crystallizer_frame):
# Add costing function, then initialize
m = Crystallizer_frame
m.fs.costing = WaterTAPCosting()
m.fs.unit.costing = UnitModelCostingBlock(default={
"flowsheet_costing_block":
m.fs.costing,
"costing_method_arguments": {
"cost_type": CrystallizerCostType.mass_basis
},
}, )
m.fs.costing.cost_process()
initialization_tester(Crystallizer_frame)
def build(number_of_stages=2):
# ---building model---
m = ConcreteModel()
m.fs = FlowsheetBlock(default={"dynamic": False})
m.fs.properties = props.NaClParameterBlock()
m.fs.costing = WaterTAPCosting()
m.fs.NumberOfStages = Param(initialize=number_of_stages)
m.fs.StageSet = RangeSet(m.fs.NumberOfStages)
m.fs.LSRRO_StageSet = RangeSet(2, m.fs.NumberOfStages)
m.fs.NonFinal_StageSet = RangeSet(m.fs.NumberOfStages-1)
m.fs.feed = Feed(default={'property_package': m.fs.properties})
m.fs.product = Product(default={'property_package': m.fs.properties})
m.fs.disposal = Product(default={'property_package': m.fs.properties})
# Add the mixers
m.fs.Mixers = Mixer(m.fs.NonFinal_StageSet, default={
"property_package": m.fs.properties,
"momentum_mixing_type": MomentumMixingType.equality, # booster pump will match pressure
"inlet_list": ['upstream', 'downstream']})
total_pump_work = 0
# Add the pumps
m.fs.PrimaryPumps = Pump(m.fs.StageSet, default={"property_package": m.fs.properties})
for pump in m.fs.PrimaryPumps.values():
pump.costing = UnitModelCostingBlock(default={
"flowsheet_costing_block":m.fs.costing})
m.fs.costing.cost_flow(pyunits.convert(pump.work_mechanical[0], to_units=pyunits.kW), "electricity")
# Add the equalizer pumps
m.fs.BoosterPumps = Pump(m.fs.LSRRO_StageSet, default={"property_package": m.fs.properties})
for pump in m.fs.BoosterPumps.values():
pump.costing = UnitModelCostingBlock(default={
"flowsheet_costing_block":m.fs.costing})
m.fs.costing.cost_flow(pyunits.convert(pump.work_mechanical[0], to_units=pyunits.kW), "electricity")
# Add the stages ROs
m.fs.ROUnits = ReverseOsmosis0D(m.fs.StageSet, default={
"property_package": m.fs.properties,
"has_pressure_change": True,
"pressure_change_type": PressureChangeType.calculated,
"mass_transfer_coefficient": MassTransferCoefficient.calculated,
"concentration_polarization_type": ConcentrationPolarizationType.calculated})
for ro_unit in m.fs.ROUnits.values():
ro_unit.costing = UnitModelCostingBlock(default={
"flowsheet_costing_block":m.fs.costing})
# Add EnergyRecoveryDevice
m.fs.EnergyRecoveryDevice = Pump(default={"property_package": m.fs.properties})
m.fs.EnergyRecoveryDevice.costing = UnitModelCostingBlock(default={
"flowsheet_costing_block":m.fs.costing,
"costing_method_arguments":{"pump_type":PumpType.energy_recovery_device}})
m.fs.costing.cost_flow(pyunits.convert(m.fs.EnergyRecoveryDevice.work_mechanical[0], to_units=pyunits.kW), "electricity")
# additional variables or expressions
# system water recovery
m.fs.water_recovery = Var(
initialize=0.5,
bounds=(0, 1),
domain=NonNegativeReals,
units=pyunits.dimensionless,
doc='System Water Recovery')
m.fs.eq_water_recovery = Constraint(expr=\
sum(m.fs.feed.flow_mass_phase_comp[0,'Liq',:]) * m.fs.water_recovery == \
sum(m.fs.product.flow_mass_phase_comp[0,'Liq',:]) )
# costing
m.fs.costing.cost_process()
product_flow_vol_total = m.fs.product.properties[0].flow_vol
m.fs.costing.add_LCOW(product_flow_vol_total)
m.fs.costing.add_specific_energy_consumption(product_flow_vol_total)
# objective
m.fs.objective = Objective(expr=m.fs.costing.LCOW)
# connections
# Connect the feed to the first pump
m.fs.feed_to_pump = Arc(source=m.fs.feed.outlet, destination=m.fs.PrimaryPumps[1].inlet)
# Connect the primary RO permeate to the product
m.fs.primary_RO_to_product = Arc(source=m.fs.ROUnits[1].permeate, destination=m.fs.product.inlet)
# Connect the Pump n to the Mixer n
m.fs.pump_to_mixer = Arc(m.fs.NonFinal_StageSet,
rule=lambda fs,n : {'source':fs.PrimaryPumps[n].outlet,
'destination':fs.Mixers[n].upstream})
# Connect the Mixer n to the Stage n
m.fs.mixer_to_stage = Arc(m.fs.NonFinal_StageSet,
rule=lambda fs,n : {'source':fs.Mixers[n].outlet,
'destination':fs.ROUnits[n].inlet})
# Connect the Stage n to the Pump n+1
m.fs.stage_to_pump = Arc(m.fs.NonFinal_StageSet,
rule=lambda fs,n : {'source':fs.ROUnits[n].retentate,
'destination':fs.PrimaryPumps[n+1].inlet})
# Connect the Stage n to the Eq Pump n
m.fs.stage_to_eq_pump = Arc(m.fs.LSRRO_StageSet,
rule=lambda fs,n : {'source':fs.ROUnits[n].permeate,
'destination':fs.BoosterPumps[n].inlet})
# Connect the Eq Pump n to the Mixer n-1
m.fs.eq_pump_to_mixer = Arc(m.fs.LSRRO_StageSet,
rule=lambda fs,n : {'source':fs.BoosterPumps[n].outlet,
'destination':fs.Mixers[n-1].downstream})
# Connect the Pump N to the Stage N
last_stage = m.fs.StageSet.last()
m.fs.pump_to_stage = Arc(source=m.fs.PrimaryPumps[last_stage].outlet,
destination=m.fs.ROUnits[last_stage].inlet)
# Connect Final Stage to EnergyRecoveryDevice Pump
m.fs.stage_to_erd = Arc(source=m.fs.ROUnits[last_stage].retentate,
destination=m.fs.EnergyRecoveryDevice.inlet)
# Connect the EnergyRecoveryDevice to the disposal
m.fs.erd_to_disposal = Arc(source=m.fs.EnergyRecoveryDevice.outlet,
destination=m.fs.disposal.inlet)
# additional bounding
for b in m.component_data_objects(Block, descend_into=True):
# NaCl solubility limit
if hasattr(b, 'mass_frac_phase_comp'):
b.mass_frac_phase_comp['Liq', 'NaCl'].setub(0.26)
TransformationFactory("network.expand_arcs").apply_to(m)
return m
def build():
# flowsheet set up
m = ConcreteModel()
m.fs = FlowsheetBlock(default={'dynamic': False})
m.fs.properties = props.NaClParameterBlock()
m.fs.costing = WaterTAPCosting()
# unit models
m.fs.feed = Feed(default={'property_package': m.fs.properties})
m.fs.S1 = Separator(default={
"property_package": m.fs.properties,
"outlet_list": ['P1', 'PXR']
})
m.fs.P1 = Pump(default={'property_package': m.fs.properties})
m.fs.PXR = PressureExchanger(default={'property_package': m.fs.properties})
m.fs.P2 = Pump(default={'property_package': m.fs.properties})
m.fs.M1 = Mixer(
default={
"property_package": m.fs.properties,
"momentum_mixing_type":
MomentumMixingType.equality, # booster pump will match pressure
"inlet_list": ['P1', 'P2']
})
m.fs.RO = ReverseOsmosis0D(
default={
"property_package":
m.fs.properties,
"has_pressure_change":
True,
"pressure_change_type":
PressureChangeType.calculated,
"mass_transfer_coefficient":
MassTransferCoefficient.calculated,
"concentration_polarization_type":
ConcentrationPolarizationType.calculated,
})
m.fs.product = Product(default={'property_package': m.fs.properties})
m.fs.disposal = Product(default={'property_package': m.fs.properties})
# costing
m.fs.costing.cost_flow(
pyunits.convert(m.fs.P1.work_mechanical[0], to_units=pyunits.kW),
"electricity")
m.fs.costing.cost_flow(
pyunits.convert(m.fs.P2.work_mechanical[0], to_units=pyunits.kW),
"electricity")
m.fs.P1.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.costing})
m.fs.P2.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.costing})
m.fs.RO.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.costing})
m.fs.PXR.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.costing})
m.fs.costing.cost_process()
m.fs.costing.add_LCOW(m.fs.product.properties[0].flow_vol)
m.fs.costing.add_specific_energy_consumption(
m.fs.product.properties[0].flow_vol)
# connections
m.fs.s01 = Arc(source=m.fs.feed.outlet, destination=m.fs.S1.inlet)
m.fs.s02 = Arc(source=m.fs.S1.P1, destination=m.fs.P1.inlet)
m.fs.s03 = Arc(source=m.fs.P1.outlet, destination=m.fs.M1.P1)
m.fs.s04 = Arc(source=m.fs.M1.outlet, destination=m.fs.RO.inlet)
m.fs.s05 = Arc(source=m.fs.RO.permeate, destination=m.fs.product.inlet)
m.fs.s06 = Arc(source=m.fs.RO.retentate,
destination=m.fs.PXR.high_pressure_inlet)
m.fs.s07 = Arc(source=m.fs.PXR.high_pressure_outlet,
destination=m.fs.disposal.inlet)
m.fs.s08 = Arc(source=m.fs.S1.PXR, destination=m.fs.PXR.low_pressure_inlet)
m.fs.s09 = Arc(source=m.fs.PXR.low_pressure_outlet,
destination=m.fs.P2.inlet)
m.fs.s10 = Arc(source=m.fs.P2.outlet, destination=m.fs.M1.P2)
TransformationFactory("network.expand_arcs").apply_to(m)
# scaling
# set default property values
m.fs.properties.set_default_scaling('flow_mass_phase_comp',
1,
index=('Liq', 'H2O'))
m.fs.properties.set_default_scaling('flow_mass_phase_comp',
1e2,
index=('Liq', 'NaCl'))
# set unit model values
iscale.set_scaling_factor(m.fs.P1.control_volume.work, 1e-3)
iscale.set_scaling_factor(m.fs.P2.control_volume.work, 1e-3)
iscale.set_scaling_factor(m.fs.PXR.low_pressure_side.work, 1e-3)
iscale.set_scaling_factor(m.fs.PXR.high_pressure_side.work, 1e-3)
# touch properties used in specifying and initializing the model
m.fs.feed.properties[0].flow_vol_phase['Liq']
m.fs.feed.properties[0].mass_frac_phase_comp['Liq', 'NaCl']
m.fs.S1.mixed_state[0].mass_frac_phase_comp
m.fs.S1.PXR_state[0].flow_vol_phase['Liq']
# unused scaling factors needed by IDAES base costing module
# calculate and propagate scaling factors
iscale.calculate_scaling_factors(m)
return m
log_close_to_bounds,
log_infeasible_bounds,
log_infeasible_constraints,
)
from pyomo.common.log import LoggingIntercept
import logging
if __name__ == "__main__":
# create model, flowsheet
m = ConcreteModel()
m.fs = FlowsheetBlock(default={"dynamic": False})
# attach property package
m.fs.properties = props.NaClParameterBlock()
m.fs.costing = WaterTAPCosting()
# build the unit model
m.fs.crystallizer = Crystallization(default={"property_package": m.fs.properties})
# now specify the model
print("DOF before specifying:", degrees_of_freedom(m.fs))
# Specify the Feed
m.fs.crystallizer.inlet.flow_mass_phase_comp[0, "Liq", "NaCl"].fix(10.5119)
m.fs.crystallizer.inlet.flow_mass_phase_comp[0, "Liq", "H2O"].fix(38.9326)
# m.fs.crystallizer.properties_in[0].flow_vol_phase['Liq'].fix(150/3600)
# m.fs.crystallizer.properties_in[0].mass_frac_phase_comp['Liq', 'NaCl'].fix(0.2126)
m.fs.crystallizer.inlet.flow_mass_phase_comp[0, "Sol", "NaCl"].fix(1e-6)
m.fs.crystallizer.inlet.flow_mass_phase_comp[0, "Vap", "H2O"].fix(1e-6)
m.fs.crystallizer.inlet.pressure[0].fix(101325)
m.fs.crystallizer.inlet.temperature[0].fix(273.15 + 20)
def add_costing(m):
prtrt = m.fs.pretreatment
desal = m.fs.desalination
psttrt = m.fs.posttreatment
# Add costing package for zero-order units
m.fs.zo_costing = ZeroOrderCosting()
m.fs.ro_costing = WaterTAPCosting()
# Add costing to zero order units
# Pre-treatment units
# This really looks like it should be a feed block in its own right
# prtrt.intake.costing = UnitModelCostingBlock(default={
# "flowsheet_costing_block": m.fs.zo_costing})
prtrt.ferric_chloride_addition.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
prtrt.chlorination.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
prtrt.static_mixer.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
prtrt.storage_tank_1.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
prtrt.media_filtration.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
prtrt.backwash_handling.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
prtrt.anti_scalant_addition.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
prtrt.cartridge_filtration.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
# RO Train
# RO equipment is costed using more detailed costing package
desal.P1.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.ro_costing}
)
desal.RO.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.ro_costing}
)
if m.erd_type == "pressure_exchanger":
# desal.S1.costing = UnitModelCostingBlock(default={
# "flowsheet_costing_block": m.fs.ro_costing})
desal.M1.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.ro_costing}
)
desal.PXR.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.ro_costing}
)
desal.P2.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.ro_costing}
)
elif m.erd_type == "pump_as_turbine":
pass
# desal.ERD.costing = UnitModelCostingBlock(default={
# "flowsheet_costing_block": m.fs.ro_costing})
else:
raise ConfigurationError(
f"erd_type was {m.erd_type}, costing only implemented "
"for pressure_exchanger or pump_as_turbine"
)
# For non-zero order unit operations, we need to register costed flows
# separately.
# However, to keep costs consistent, we will register these with the ZO
# Costing package
m.fs.zo_costing.cost_flow(desal.P1.work_mechanical[0], "electricity")
if m.erd_type == "pressure_exchanger":
m.fs.zo_costing.cost_flow(desal.P2.work_mechanical[0], "electricity")
elif m.erd_type == "pump_as_turbine":
pass
# m.fs.zo_costing.cost_flow(
# desal.ERD.work_mechanical[0], "electricity")
else:
raise ConfigurationError(
f"erd_type was {m.erd_type}, costing only implemented "
"for pressure_exchanger or pump_as_turbine"
)
# Post-treatment units
psttrt.storage_tank_2.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
psttrt.uv_aop.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
psttrt.co2_addition.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
psttrt.lime_addition.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
psttrt.storage_tank_3.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
# Product and disposal
m.fs.municipal.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
m.fs.landfill.costing = UnitModelCostingBlock(
default={"flowsheet_costing_block": m.fs.zo_costing}
)
# Aggregate unit level costs and calculate overall process costs
m.fs.zo_costing.cost_process()
m.fs.ro_costing.cost_process()
# Combine results from costing packages and calculate overall metrics
@m.Expression()
def total_capital_cost(b):
return (
pyunits.convert(
m.fs.zo_costing.total_capital_cost, to_units=pyunits.USD_2018
)
+ m.fs.ro_costing.total_investment_cost
)
@m.Expression()
def total_operating_cost(b):
return (
pyunits.convert(
m.fs.zo_costing.total_fixed_operating_cost,
to_units=pyunits.USD_2018 / pyunits.year,
)
+ pyunits.convert(
m.fs.zo_costing.total_variable_operating_cost,
to_units=pyunits.USD_2018 / pyunits.year,
)
+ m.fs.ro_costing.total_operating_cost
)
@m.Expression()
def LCOW(b):
return (
b.total_capital_cost * b.fs.zo_costing.capital_recovery_factor
+ b.total_operating_cost
) / (
pyunits.convert(
b.fs.municipal.properties[0].flow_vol,
to_units=pyunits.m**3 / pyunits.year,
)
* b.fs.zo_costing.utilization_factor
)
assert_units_consistent(m)