###############################################################################
# WaterTAP Copyright (c) 2021, The Regents of the University of California,
# through Lawrence Berkeley National Laboratory, Oak Ridge National
# Laboratory, National Renewable Energy Laboratory, and National Energy
# Technology Laboratory (subject to receipt of any required approvals from
# the U.S. Dept. of Energy). All rights reserved.
#
# Please see the files COPYRIGHT.md and LICENSE.md for full copyright and license
# information, respectively. These files are also available online at the URL
# "https://github.com/watertap-org/watertap/"
#
###############################################################################
import pyomo.environ as pyo
from idaes.core.util.exceptions import ConfigurationError
from ..util import (
register_costing_parameter_block,
make_capital_cost_var,
make_fixed_operating_cost_var,
)
def build_hcl_cost_param_block(blk):
blk.cost = pyo.Param(
mutable=True,
initialize=0.17,
doc="HCl cost", # for 37% sol'n - CatCost v 1.0.4
units=pyo.units.USD_2020 / pyo.units.kg,
)
blk.purity = pyo.Param(
mutable=True,
initialize=0.37,
doc="HCl purity",
units=pyo.units.dimensionless,
)
costing = blk.parent_block()
costing.add_defined_flow("HCl", blk.cost / blk.purity)
def build_naoh_cost_param_block(blk):
blk.cost = pyo.Param(
mutable=True,
initialize=0.59,
doc="NaOH cost", # for 30% sol'n - iDST
units=pyo.units.USD_2020 / pyo.units.kg,
)
blk.purity = pyo.Param(
mutable=True,
initialize=0.30,
doc="NaOH purity",
units=pyo.units.dimensionless,
)
costing = blk.parent_block()
costing.add_defined_flow("NaOH", blk.cost / blk.purity)
def build_meoh_cost_param_block(blk):
# MeOH = Methanol
blk.cost = pyo.Param(
mutable=True,
initialize=3.395,
doc="MeOH cost", # for 100% purity - ICIS
units=pyo.units.USD_2008 / pyo.units.kg,
)
blk.purity = pyo.Param(
mutable=True,
initialize=1,
doc="MeOH purity",
units=pyo.units.dimensionless,
)
costing = blk.parent_block()
costing.add_defined_flow("MeOH", blk.cost / blk.purity)
def build_nacl_cost_param_block(blk):
blk.cost = pyo.Param(
mutable=True,
initialize=0.09,
doc="NaCl cost", # for solid, 100% purity - CatCost
units=pyo.units.USD_2020 / pyo.units.kg,
)
blk.purity = pyo.Param(
mutable=True,
initialize=1,
doc="NaCl purity",
units=pyo.units.dimensionless,
)
costing = blk.parent_block()
costing.add_defined_flow("NaCl", blk.cost / blk.purity)
def build_ion_exhange_cost_param_block(blk):
blk.anion_exchange_resin_cost = pyo.Var(
initialize=205,
units=pyo.units.USD_2020 / pyo.units.ft**3,
doc="Anion exchange resin cost per cubic ft. Assumes strong base polystyrenic gel-type Type II. From EPA-WBS cost model.",
)
blk.cation_exchange_resin_cost = pyo.Var(
initialize=153,
units=pyo.units.USD_2020 / pyo.units.ft**3,
doc="Cation exchange resin cost per cubic ft. Assumes strong acid polystyrenic gel-type. From EPA-WBS cost model.",
)
# Ion exchange pressure vessels costed with 3rd order polynomial:
# pv_cost = A * col_vol^3 + B * col_vol^2 + C * col_vol + intercept
blk.vessel_intercept = pyo.Var(
initialize=10010.86,
units=pyo.units.USD_2020,
doc="Ion exchange pressure vessel cost equation - intercept, Carbon steel w/ plastic internals",
)
blk.vessel_A_coeff = pyo.Var(
initialize=6e-9,
units=pyo.units.USD_2020 / pyo.units.gal**3,
doc="Ion exchange pressure vessel cost equation - A coeff., Carbon steel w/ plastic internals",
)
blk.vessel_B_coeff = pyo.Var(
initialize=-2.284e-4,
units=pyo.units.USD_2020 / pyo.units.gal**2,
doc="Ion exchange pressure vessel cost equation - B coeff., Carbon steel w/ plastic internals",
)
blk.vessel_C_coeff = pyo.Var(
initialize=8.3472,
units=pyo.units.USD_2020 / pyo.units.gal,
doc="Ion exchange pressure vessel cost equation - C coeff., Carbon steel w/ plastic internals",
)
# Ion exchange pressure vessels costed with 3rd order polynomial:
# pv_cost = A * col_vol^3 + B * col_vol^2 + C * col_vol + intercept
blk.backwash_tank_A_coeff = pyo.Var(
initialize=1e-9,
units=pyo.units.USD_2020 / pyo.units.gal**3,
doc="Ion exchange backwash tank cost equation - A coeff., Fiberglass tank",
)
blk.backwash_tank_B_coeff = pyo.Var(
initialize=-5.8587e-05,
units=pyo.units.USD_2020 / pyo.units.gal**2,
doc="Ion exchange backwash tank cost equation - B coeff., Fiberglass tank",
)
blk.backwash_tank_C_coeff = pyo.Var(
initialize=2.2911,
units=pyo.units.USD_2020 / pyo.units.gal,
doc="Ion exchange backwash tank cost equation - C coeff., Fiberglass tank",
)
blk.backwash_tank_intercept = pyo.Var(
initialize=4717.255,
units=pyo.units.USD_2020,
doc="Ion exchange backwash tank cost equation - exponent, Fiberglass tank",
)
# Ion exchange regeneration solution tank costed with 2nd order polynomial:
# regen_tank_cost = A * tank_vol^2 + B * tank_vol + intercept
blk.regen_tank_intercept = pyo.Var(
initialize=4408.327,
units=pyo.units.USD_2020,
doc="Ion exchange regen tank cost equation - C coeff. Stainless steel",
)
blk.regen_tank_A_coeff = pyo.Var(
initialize=-3.258e-5,
units=pyo.units.USD_2020 / pyo.units.gal**2,
doc="Ion exchange regen tank cost equation - A coeff. Stainless steel",
)
blk.regen_tank_B_coeff = pyo.Var(
initialize=3.846,
units=pyo.units.USD_2020 / pyo.units.gal,
doc="Ion exchange regen tank cost equation - B coeff. Stainless steel",
)
blk.annual_resin_replacement_factor = pyo.Var(
initialize=0.05,
units=pyo.units.year**-1,
doc="Fraction of ion excange resin replaced per year, 4-5% of bed volume - EPA",
)
blk.hazardous_min_cost = pyo.Var(
initialize=3240,
units=pyo.units.USD_2020 / pyo.units.year,
doc="Min cost per hazardous waste shipment - EPA",
)
blk.hazardous_resin_disposal = pyo.Var(
initialize=347.10,
units=pyo.units.USD_2020 * pyo.units.ton**-1,
doc="Hazardous resin disposal cost - EPA",
)
blk.hazardous_regen_disposal = pyo.Var(
initialize=3.64,
units=pyo.units.USD_2020 * pyo.units.gal**-1,
doc="Hazardous liquid disposal cost - EPA",
)
[docs]@register_costing_parameter_block(
build_rule=build_hcl_cost_param_block,
parameter_block_name="hcl",
)
@register_costing_parameter_block(
build_rule=build_naoh_cost_param_block,
parameter_block_name="naoh",
)
@register_costing_parameter_block(
build_rule=build_meoh_cost_param_block,
parameter_block_name="meoh",
)
@register_costing_parameter_block(
build_rule=build_nacl_cost_param_block,
parameter_block_name="nacl",
)
@register_costing_parameter_block(
build_rule=build_ion_exhange_cost_param_block,
parameter_block_name="ion_exchange",
)
def cost_ion_exchange(blk):
"""
Volume-based capital cost for Ion Exchange
"""
make_capital_cost_var(blk)
make_fixed_operating_cost_var(blk)
# Conversions to use units from cost equations in reference
col_vol_gal = pyo.units.convert(blk.unit_model.col_vol_per, to_units=pyo.units.gal)
bed_vol_ft3 = pyo.units.convert(blk.unit_model.bed_vol, to_units=pyo.units.ft**3)
bed_mass_ton = pyo.units.convert(
blk.unit_model.bed_vol * blk.unit_model.resin_bulk_dens,
to_units=pyo.units.ton,
)
bw_tank_vol = pyo.units.convert(
(
blk.unit_model.bw_flow * blk.unit_model.t_bw
+ blk.unit_model.rinse_flow * blk.unit_model.t_rinse
),
to_units=pyo.units.gal,
)
regen_tank_vol = pyo.units.convert(
(
blk.unit_model.properties_regen[0].flow_vol_phase["Liq"]
* blk.unit_model.t_regen
),
to_units=pyo.units.gal,
)
ix_type = blk.unit_model.ion_exchange_type
TIC = 1.65
blk.capital_cost_vessel = pyo.Var(
initialize=1e5,
domain=pyo.NonNegativeReals,
units=blk.costing_package.base_currency,
doc="Capital cost for one vessel",
)
blk.capital_cost_resin = pyo.Var(
initialize=1e5,
domain=pyo.NonNegativeReals,
units=blk.costing_package.base_currency,
doc="Capital cost for resin for one vessel",
)
blk.capital_cost_regen_tank = pyo.Var(
initialize=1e5,
domain=pyo.NonNegativeReals,
units=blk.costing_package.base_currency,
doc="Capital cost for regeneration solution tank",
)
blk.capital_cost_backwash_tank = pyo.Var(
initialize=1e5,
domain=pyo.NonNegativeReals,
units=blk.costing_package.base_currency,
doc="Capital cost for backwash + rinse solution tank",
)
blk.operating_cost_hazardous = pyo.Var(
initialize=1e5,
domain=pyo.NonNegativeReals,
units=blk.costing_package.base_currency / blk.costing_package.base_period,
doc="Operating cost for hazardous waste disposal",
)
ion_exchange_params = blk.costing_package.ion_exchange
# TODO: add way to have other regen chemicals
if ix_type == "cation":
resin_cost = ion_exchange_params.cation_exchange_resin_cost
elif ix_type == "anion":
resin_cost = ion_exchange_params.anion_exchange_resin_cost
elif ix_type == "mixed":
raise ConfigurationError(
"IonExchangeOD model for IonExchangeType.mixed has not been implemented yet."
)
blk.capital_cost_vessel_constraint = pyo.Constraint(
expr=blk.capital_cost_vessel
== pyo.units.convert(
ion_exchange_params.vessel_intercept
+ ion_exchange_params.vessel_A_coeff * col_vol_gal**3
+ ion_exchange_params.vessel_B_coeff * col_vol_gal**2
+ ion_exchange_params.vessel_C_coeff * col_vol_gal,
to_units=blk.costing_package.base_currency,
)
)
blk.capital_cost_resin_constraint = pyo.Constraint(
expr=blk.capital_cost_resin
== pyo.units.convert(
resin_cost * bed_vol_ft3, to_units=blk.costing_package.base_currency
)
)
blk.capital_cost_backwash_tank_constraint = pyo.Constraint(
expr=blk.capital_cost_backwash_tank
== pyo.units.convert(
ion_exchange_params.backwash_tank_intercept
+ ion_exchange_params.backwash_tank_A_coeff * bw_tank_vol**3
+ ion_exchange_params.backwash_tank_B_coeff * bw_tank_vol**2
+ ion_exchange_params.backwash_tank_C_coeff * bw_tank_vol,
to_units=blk.costing_package.base_currency,
)
)
blk.capital_cost_regen_tank_constraint = pyo.Constraint(
expr=blk.capital_cost_regen_tank
== pyo.units.convert(
ion_exchange_params.regen_tank_intercept
+ ion_exchange_params.regen_tank_A_coeff * regen_tank_vol**2
+ ion_exchange_params.regen_tank_B_coeff * regen_tank_vol,
to_units=blk.costing_package.base_currency,
)
)
blk.capital_cost_constraint = pyo.Constraint(
expr=blk.capital_cost
== pyo.units.convert(
(
(blk.capital_cost_vessel + blk.capital_cost_resin)
* (blk.unit_model.number_columns + blk.unit_model.number_columns_redund)
+ blk.capital_cost_backwash_tank
+ blk.capital_cost_regen_tank
)
* TIC,
to_units=blk.costing_package.base_currency,
)
)
if blk.unit_model.config.hazardous_waste:
blk.operating_cost_hazardous_constraint = pyo.Constraint(
expr=blk.operating_cost_hazardous
== pyo.units.convert(
(
bw_tank_vol * ion_exchange_params.hazardous_regen_disposal
+ bed_mass_ton * ion_exchange_params.hazardous_resin_disposal
)
* ion_exchange_params.annual_resin_replacement_factor
+ ion_exchange_params.hazardous_min_cost,
to_units=blk.costing_package.base_currency
/ blk.costing_package.base_period,
)
)
else:
blk.operating_cost_hazardous.fix(0)
blk.fixed_operating_cost_constraint = pyo.Constraint(
expr=blk.fixed_operating_cost
== pyo.units.convert(
(
(
bed_vol_ft3
* ion_exchange_params.annual_resin_replacement_factor
* resin_cost
)
),
to_units=blk.costing_package.base_currency
/ blk.costing_package.base_period,
)
+ blk.operating_cost_hazardous
)
regen_soln_flow = (
(
blk.unit_model.regen_dose
* blk.unit_model.bed_vol
* (blk.unit_model.number_columns + blk.unit_model.number_columns_redund)
)
/ (blk.unit_model.t_cycle)
) / blk.unit_model.regen_recycle
electricity_flow = (
blk.unit_model.main_pump_power
+ blk.unit_model.regen_pump_power
+ blk.unit_model.bw_pump_power
+ blk.unit_model.rinse_pump_power
)
blk.costing_package.cost_flow(electricity_flow, "electricity")
blk.costing_package.cost_flow(regen_soln_flow, blk.unit_model.regen_chem)