def build_feed_block(m):
m.fs.feed = Feed(
default={"property_package": m.fs.stoich_softening_thermo_params})
comp_list = ["Na", "Ca", "Mg", "SO4", "Cl"]
feed_flow_mass = 1 # kg/s
feed_mass_frac_comp = {
"Na": 11122e-6,
"Ca": 382e-6,
"Mg": 1394e-6,
"SO4": 2136e-6,
"Cl": 20316.88e-6,
}
feed_mass_frac_comp["H2O"] = 1 - sum(x
for x in feed_mass_frac_comp.values())
mw_comp = {
"H2O": 18.015e-3,
"Na": 22.990e-3,
"Ca": 40.078e-3,
"Mg": 24.305e-3,
"SO4": 96.06e-3,
"Cl": 35.453e-3,
}
feed_flow_mol_comp = {}
for j in feed_mass_frac_comp:
feed_flow_mol_comp[
j] = feed_flow_mass * feed_mass_frac_comp[j] / mw_comp[j]
feed_mole_frac_comp = {}
for j in feed_flow_mol_comp:
feed_mole_frac_comp[j] = feed_flow_mol_comp[j] / sum(
feed_flow_mol_comp[jj] for jj in feed_flow_mol_comp)
m.fs.feed.properties[0].mole_frac_comp["Ca(HCO3)2"].fix(
feed_mole_frac_comp["Ca"])
m.fs.feed.properties[0].mole_frac_comp["Ca(OH)2"].fix(0)
m.fs.feed.properties[0].mole_frac_comp["CaCO3"].fix(0)
m.fs.feed.properties[0].mole_frac_comp["H2O"].fix(
feed_mole_frac_comp["H2O"])
m.fs.feed.properties[0].mole_frac_comp["Mg(HCO3)2"].fix(
feed_mole_frac_comp["Mg"])
m.fs.feed.properties[0].mole_frac_comp["Mg(OH)2"].fix(0)
m.fs.feed.properties[0].mole_frac_comp["NaCl"].fix(
feed_mole_frac_comp["Na"])
m.fs.feed.properties[0].mole_frac_comp["SO4_2-"].fix(
feed_mole_frac_comp["SO4"])
m.fs.feed.properties[0].mole_frac_comp["Cl_-"].fix(
feed_mole_frac_comp["Cl"] - feed_mole_frac_comp["Na"])
m.fs.feed.properties[0].flow_mol.fix(55.56)
m.fs.feed.properties[0].pressure.fix(101325)
m.fs.feed.properties[0].temperature.fix(298)
def build_feed(m, base='TDS'):
"""
Build a feed block for a specified property base. The state vars are fixed to the standard condition.
Property bases include: 'TDS', 'ion', 'salt'
"""
# feed block
prop = property_models.get_prop(m, base=base)
# build
m.fs.feed = Feed(default={'property_package': prop})
# specify
property_models.specify_feed(m.fs.feed.properties[0], base=base)
m.fs.feed.properties[0].mass_frac_phase_comp # touch so the block can be initialized
def build_feed_block(m):
m.fs.feed = Feed(default={'property_package': m.fs.stoich_softening_thermo_params})
comp_list = ['Na', 'Ca', 'Mg', 'SO4', 'Cl']
feed_flow_mass = 1 # kg/s
feed_mass_frac_comp = {'Na': 11122e-6,
'Ca': 382e-6,
'Mg': 1394e-6,
'SO4': 2136e-6,
'Cl': 20316.88e-6}
feed_mass_frac_comp['H2O'] = 1 - sum(x for x in feed_mass_frac_comp.values())
mw_comp = {'H2O': 18.015e-3,
'Na': 22.990e-3,
'Ca': 40.078e-3,
'Mg': 24.305e-3,
'SO4': 96.06e-3,
'Cl': 35.453e-3}
feed_flow_mol_comp = {}
for j in feed_mass_frac_comp:
feed_flow_mol_comp[j] = feed_flow_mass * feed_mass_frac_comp[j] / mw_comp[j]
feed_mole_frac_comp = {}
for j in feed_flow_mol_comp:
feed_mole_frac_comp[j] = feed_flow_mol_comp[j] / sum(feed_flow_mol_comp[jj] for jj in feed_flow_mol_comp)
m.fs.feed.properties[0].mole_frac_comp['Ca(HCO3)2'].fix(feed_mole_frac_comp['Ca'])
m.fs.feed.properties[0].mole_frac_comp['Ca(OH)2'].fix(0)
m.fs.feed.properties[0].mole_frac_comp['CaCO3'].fix(0)
m.fs.feed.properties[0].mole_frac_comp['H2O'].fix(feed_mole_frac_comp['H2O'])
m.fs.feed.properties[0].mole_frac_comp['Mg(HCO3)2'].fix(feed_mole_frac_comp['Mg'])
m.fs.feed.properties[0].mole_frac_comp['Mg(OH)2'].fix(0)
m.fs.feed.properties[0].mole_frac_comp['NaCl'].fix(feed_mole_frac_comp['Na'])
m.fs.feed.properties[0].mole_frac_comp['SO4_2-'].fix(feed_mole_frac_comp['SO4'])
m.fs.feed.properties[0].mole_frac_comp['Cl_-'].fix(feed_mole_frac_comp['Cl'] - feed_mole_frac_comp['Na'])
m.fs.feed.properties[0].flow_mol.fix(55.56)
m.fs.feed.properties[0].pressure.fix(101325)
m.fs.feed.properties[0].temperature.fix(298)
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()
financials.add_costing_param_block(m.fs)
# 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
})
m.fs.product = Product(default={'property_package': m.fs.properties})
m.fs.disposal = Product(default={'property_package': m.fs.properties})
# additional variables or expressions
feed_flow_vol_total = m.fs.feed.properties[0].flow_vol
product_flow_vol_total = m.fs.product.properties[0].flow_vol
m.fs.recovery = Expression(expr=product_flow_vol_total /
feed_flow_vol_total)
m.fs.annual_water_production = Expression(expr=pyunits.convert(
product_flow_vol_total, to_units=pyunits.m**3 / pyunits.year) *
m.fs.costing_param.load_factor)
pump_power_total = m.fs.P1.work_mechanical[0] + m.fs.P2.work_mechanical[0]
m.fs.specific_energy_consumption = Expression(
expr=pyunits.convert(pump_power_total, to_units=pyunits.kW) /
pyunits.convert(product_flow_vol_total,
to_units=pyunits.m**3 / pyunits.hr))
# costing
m.fs.P1.get_costing(module=financials, pump_type="High pressure")
m.fs.P2.get_costing(module=financials, pump_type="High pressure")
m.fs.RO.get_costing(module=financials)
m.fs.PXR.get_costing(module=financials)
financials.get_system_costing(m.fs)
# 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
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'))
iscale.calculate_scaling_factors(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