##############################################################################
# Institute for the Design of Advanced Energy Systems Process Systems
# Engineering Framework (IDAES PSE Framework) Copyright (c) 2018-2019, by the
# software owners: The Regents of the University of California, through
# Lawrence Berkeley National Laboratory, National Technology & Engineering
# Solutions of Sandia, LLC, Carnegie Mellon University, West Virginia
# University Research Corporation, et al. All rights reserved.
#
# Please see the files COPYRIGHT.txt and LICENSE.txt for full copyright and
# license information, respectively. Both files are also available online
# at the URL "https://github.com/IDAES/idaes-pse".
##############################################################################
"""
Example property package for the combustion of methane in air using
Gibbs energy minimisation.
"""
# Import Python libraries
import logging
# Import Pyomo libraries
from pyomo.environ import Constraint, log, Param, \
PositiveReals, Reals, Set, value, Var
from pyomo.util.calc_var_value import calculate_variable_from_constraint
from pyomo.opt import SolverFactory, TerminationCondition
# Import IDAES cores
from idaes.core import (declare_process_block_class,
PhysicalParameterBlock,
StateBlockData,
StateBlock,
MaterialBalanceType,
EnergyBalanceType,
MomentumBalanceType)
from idaes.core.util.initialization import solve_indexed_blocks
from idaes.core.util.model_statistics import degrees_of_freedom
# Some more inforation about this module
__author__ = "Andrew Lee, Jinliang Ma"
# Set up logger
_log = logging.getLogger(__name__)
[docs]@declare_process_block_class("MethaneCombustionParameterBlock")
class PhysicalParameterData(PhysicalParameterBlock):
"""
Property Parameter Block Class
Contains parameters and indexing sets associated with properties for
superheated steam.
"""
[docs] def build(self):
'''
Callable method for Block construction.
'''
super(PhysicalParameterData, self).build()
self.state_block_class = MethaneCombustionStateBlock
# List of valid phases in property package
self.phase_list = Set(initialize=['Vap'])
# Component list - a list of component identifiers
self.component_list = Set(initialize=['H2', 'N2', 'O2', 'CH4',
'CO', 'CO2', 'H2O', 'NH3'])
# List of components in each phase (optional)
self.phase_comp = {"Vap": self.component_list}
# List of all chemical elements that constitute the chemical species
self.element_list = Set(initialize=['H', 'N', 'O', 'C'])
# Elemental composition of all species
self.element_comp = {'H2': {'H': 2, 'N': 0, 'O': 0, 'C': 0},
'N2': {'H': 0, 'N': 2, 'O': 0, 'C': 0},
'O2': {'H': 0, 'N': 0, 'O': 2, 'C': 0},
'CH4': {'H': 4, 'N': 0, 'O': 0, 'C': 1},
'CO': {'H': 0, 'N': 0, 'O': 1, 'C': 1},
'CO2': {'H': 0, 'N': 0, 'O': 2, 'C': 1},
'H2O': {'H': 2, 'N': 0, 'O': 1, 'C': 0},
'NH3': {'H': 3, 'N': 1, 'O': 0, 'C': 0}}
# Heat capacity parameters - Shomate eqn (from NIST webbook)
# Parameter 9 is the enthalpy at 1500K (Tref) in J/mol
cp_param_dict = {('H2', 1): 18.563083,
('H2', 2): 12.257357,
('H2', 3): -2.859786,
('H2', 4): 0.268238,
('H2', 5): 1.977990,
('H2', 6): -1.147438,
('H2', 7): 156.288133,
('H2', 8): 0.0,
('H2', 9): 36290.28,
('N2', 1): 19.50583,
('N2', 2): 19.88705,
('N2', 3): -8.598535,
('N2', 4): 1.369784,
('N2', 5): 0.527601,
('N2', 6): -4.935202,
('N2', 7): 212.3900,
('N2', 8): 0,
('N2', 9): 38405.02,
('O2', 1): 30.03235,
('O2', 2): 8.772972,
('O2', 3): -3.988133,
('O2', 4): 0.788313,
('O2', 5): -0.741599,
('O2', 6): -11.32468,
('O2', 7): 236.1663,
('O2', 8): 0,
('O2', 9): 40598.9,
('CH4', 1): 85.81217,
('CH4', 2): 11.26467,
('CH4', 3): -2.114146,
('CH4', 4): 0.138190,
('CH4', 5): -26.42221,
('CH4', 6): -153.5327,
('CH4', 7): 224.4143,
('CH4', 8): -74.87310,
('CH4', 9): 78142.7,
('CO', 1): 35.15070,
('CO', 2): 1.300095,
('CO', 3): -0.205921,
('CO', 4): 0.013550,
('CO', 5): -3.282780,
('CO', 6): -127.8375,
('CO', 7): 231.7120,
('CO', 8): -110.5271,
('CO', 9): 38852.26,
('CO2', 1): 58.16639,
('CO2', 2): 2.720074,
('CO2', 3): -0.492289,
('CO2', 4): 0.038844,
('CO2', 5): -6.447293,
('CO2', 6): -425.9186,
('CO2', 7): 263.6125,
('CO2', 8): -393.5224,
('CO2', 9): 61707.0,
('H2O', 1): 41.96426,
('H2O', 2): 8.622053,
('H2O', 3): -1.499780,
('H2O', 4): 0.098119,
('H2O', 5): -11.15764,
('H2O', 6): -272.1797,
('H2O', 7): 219.7809,
('H2O', 8): -241.8264,
('H2O', 9): 48150.13,
('NH3', 1): 52.02427,
('NH3', 2): 18.48801,
('NH3', 3): -3.765128,
('NH3', 4): 0.248541,
('NH3', 5): -12.45799,
('NH3', 6): -85.53895,
('NH3', 7): 223.8022,
('NH3', 8): -45.89806,
('NH3', 9): 63578.64}
self.cp_params = Param(self.component_list,
range(1, 10),
mutable=False,
initialize=cp_param_dict,
doc="Shomate equation heat capacity parameters")
# Heat of Formation
hf_dict = {"CH4": -74600,
"CO": -110530,
"CO2": -393520,
"H2": 0,
"H2O": -241830,
"N2": 0,
"NH3": -45900,
"O2": 0}
self.enth_mol_form = Param(
self.component_list,
mutable=False,
initialize=hf_dict,
doc="Component molar heats of formation [J/mol]")
# Gas Constant
self.gas_const = Param(within=PositiveReals,
mutable=False,
default=8.314,
doc='Gas Constant [J/mol.K]')
# Thermodynamic reference state
self.pressure_ref = Param(within=PositiveReals,
mutable=True,
default=101325.0,
doc='Reference pressure [Pa]')
self.temperature_ref = Param(within=PositiveReals,
mutable=True,
default=1500.0,
doc='Reference temperature [K]')
class _StateBlock(StateBlock):
"""
This Class contains methods which should be applied to Property Blocks as a
whole, rather than individual elements of indexed Property Blocks.
"""
def initialize(blk, state_args=None, hold_state=False, outlvl=0,
state_vars_fixed=False, solver='ipopt',
optarg={'tol': 1e-8}):
'''
Initialisation routine for property package.
Keyword Arguments:
state_args : Dictionary with initial guesses for the state vars
chosen. Note that if this method is triggered
through the control volume, and if initial guesses
were not provied at the unit model level, the
control volume passes the inlet values as initial
guess.The keys for the state_args dictionary are:
flow_mol_comp : value at which to initialize component
flows (default=None)
pressure : value at which to initialize pressure
(default=None)
temperature : value at which to initialize temperature
(default=None)
outlvl : sets output level of initialisation routine
* 0 = no output (default)
* 1 = return solver state for each step in routine
* 2 = include solver output infomation (tee=True)
state_vars_fixed: Flag to denote if state vars have already been
fixed.
- True - states have already been fixed by the
control volume 1D. Control volume 0D
does not fix the state vars, so will
be False if this state block is used
with 0D blocks.
- False - states have not been fixed. The state
block will deal with fixing/unfixing.
optarg : solver options dictionary object (default=None)
solver : str indicating whcih solver to use during
initialization (default = 'ipopt')
hold_state : flag indicating whether the initialization routine
should unfix any state variables fixed during
initialization (default=False).
- True - states varaibles are not unfixed, and
a dict of returned containing flags for
which states were fixed during
initialization.
- False - state variables are unfixed after
initialization by calling the
relase_state method
Returns:
If hold_states is True, returns a dict containing flags for
which states were fixed during initialization.
'''
if state_vars_fixed is False:
# Fix state variables if not already fixed
Fcflag = {}
Pflag = {}
Tflag = {}
for k in blk.keys():
for j in blk[k]._params.component_list:
if blk[k].flow_mol_comp[j].fixed is True:
Fcflag[k, j] = True
else:
Fcflag[k, j] = False
if state_args is None:
blk[k].flow_mol_comp[j].fix(1.0)
else:
blk[k].flow_mol_comp[j].fix(state_args["flow_mol_comp"][j])
if blk[k].pressure.fixed is True:
Pflag[k] = True
else:
Pflag[k] = False
if state_args is None:
blk[k].pressure.fix(101325.0)
else:
blk[k].pressure.fix(state_args["pressure"])
if blk[k].temperature.fixed is True:
Tflag[k] = True
else:
Tflag[k] = False
if state_args is None:
blk[k].temperature.fix(1500.0)
else:
blk[k].temperature.fix(state_args["temperature"])
for j in blk[k]._params.component_list:
blk[k].mole_frac_comp[j] = \
(value(blk[k].flow_mol_comp[j]) /
sum(value(blk[k].flow_mol_comp[i])
for i in blk[k]._params.component_list))
# If input block, return flags, else release state
flags = {"Fcflag": Fcflag, "Pflag": Pflag,
"Tflag": Tflag}
else:
# Check when the state vars are fixed already result in dof 0
for k in blk.keys():
if degrees_of_freedom(blk[k]) != 0:
raise Exception("State vars fixed but degrees of freedom "
"for state block is not zero during "
"initialization.")
# Set solver options
if outlvl > 1:
stee = True
else:
stee = False
opt = SolverFactory(solver)
opt.options = optarg
# ---------------------------------------------------------------------
# Initialise values
for k in blk.keys():
for j in blk[k]._params.component_list:
if hasattr(blk[k], "cp_shomate_eqn"):
calculate_variable_from_constraint(blk[k].cp_mol_comp[j],
blk[k].
cp_shomate_eqn[j])
if hasattr(blk[k], "enthalpy_shomate_eqn"):
calculate_variable_from_constraint(
blk[k].enth_mol_phase_comp["Vap", j],
blk[k].enthalpy_shomate_eqn[j])
if hasattr(blk[k], "entropy_shomate_eqn"):
calculate_variable_from_constraint(
blk[k].entr_mol_phase_comp["Vap", j],
blk[k].entropy_shomate_eqn[j])
if hasattr(blk[k], "partial_gibbs_energy_eqn"):
calculate_variable_from_constraint(
blk[k].gibbs_mol_phase_comp["Vap", j],
blk[k].partial_gibbs_energy_eqn[j])
if hasattr(blk[k], "ideal_gas"):
calculate_variable_from_constraint(
blk[k].dens_mol_phase["Vap"],
blk[k].ideal_gas)
if hasattr(blk[k], "mixture_heat_capacity_eqn"):
calculate_variable_from_constraint(
blk[k].cp_mol,
blk[k].mixture_heat_capacity_eqn)
if hasattr(blk[k], "mixture_enthalpy_eqn"):
calculate_variable_from_constraint(
blk[k].enth_mol,
blk[k].mixture_enthalpy_eqn)
if hasattr(blk[k], "mixture_entropy_eqn"):
calculate_variable_from_constraint(
blk[k].entr_mol,
blk[k].mixture_entropy_eqn)
if hasattr(blk[k], "total_flow_eqn"):
calculate_variable_from_constraint(
blk[k].flow_mol,
blk[k].total_flow_eqn)
if hasattr(blk[k], "mixture_gibbs_eqn"):
calculate_variable_from_constraint(
blk[k].gibbs_mol,
blk[k].mixture_gibbs_eqn)
results = solve_indexed_blocks(opt, blk, tee=stee)
if outlvl > 0:
if results.solver.termination_condition \
== TerminationCondition.optimal:
_log.info('{} Initialisation Step 1 Complete.'
.format(blk.name))
else:
_log.warning('{} Initialisation Step 1 Failed.'
.format(blk.name))
# ---------------------------------------------------------------------
if outlvl > 0:
if outlvl > 0:
_log.info('{} Initialisation Complete.'.format(blk.name))
if state_vars_fixed is False:
if hold_state is True:
return flags
else:
blk.release_state(flags)
def release_state(blk, flags, outlvl=0):
'''
Method to relase state variables fixed during initialisation.
Keyword Arguments:
flags : dict containing information of which state variables
were fixed during initialization, and should now be
unfixed. This dict is returned by initialize if
hold_state=True.
outlvl : sets output level of of logging
'''
if flags is None:
return
# Unfix state variables
for k in blk.keys():
for j in blk[k]._params.component_list:
if flags['Fcflag'][k, j] is False:
blk[k].flow_mol_comp[j].unfix()
if flags['Pflag'][k] is False:
blk[k].pressure.unfix()
if flags['Tflag'][k] is False:
blk[k].temperature.unfix()
if outlvl > 0:
if outlvl > 0:
_log.info('{} State Released.'.format(blk.name))
[docs]@declare_process_block_class("MethaneCombustionStateBlock",
block_class=_StateBlock)
class MethaneCombustionStateBlockData(StateBlockData):
"""
An example property package for ideal gas properties with Gibbs energy
"""
[docs] def build(self):
"""
Callable method for Block construction
"""
super(MethaneCombustionStateBlockData, self).build()
# Create state variables
self.flow_mol_comp = Var(self._params.component_list,
initialize=1.0,
doc='Component molar flowrate [mol/s]')
self.pressure = Var(domain=Reals,
initialize=101325.0,
bounds=(1e3, 1e6),
doc='State pressure [Pa]')
self.temperature = Var(domain=Reals,
initialize=1500,
bounds=(1450, 3000),
doc='State temperature [K]')
self.mole_frac_comp = Var(self._params.component_list,
domain=Reals,
initialize=0.0,
doc='State component mole fractions [-]')
# Create standard constraints
# Mole fractions
def mole_frac_constraint(b, j):
return b.flow_mol_comp[j] == (
b.mole_frac_comp[j] *
sum(b.flow_mol_comp[k]
for k in b._params.component_list))
self.mole_frac_constraint = Constraint(self._params.component_list,
rule=mole_frac_constraint)
def _dens_mol_phase(self):
# Molar density
self.dens_mol_phase = Var(self._params.phase_list,
doc="Molar density")
def ideal_gas(b, p):
return (b.dens_mol_phase[p]*b._params.gas_const*b.temperature ==
b.pressure)
try:
# Try to build constraint
self.ideal_gas = Constraint(self._params.phase_list,
rule=ideal_gas)
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.dens_mol_phase)
self.del_component(self.ideal_gas)
raise
def _cp_mol_comp(self):
# Pure component vapour heat capacities
self.cp_mol_comp = Var(self._params.component_list,
domain=Reals,
initialize=1.0,
doc="Pure component vapour heat capacities "
"[J/mol.K]")
def pure_component_cp_mol(b, j):
return b.cp_mol_comp[j] == (
b._params.cp_params[j, 1] +
b._params.cp_params[j, 2]*(b.temperature*1e-3) +
b._params.cp_params[j, 3]*(b.temperature*1e-3)**2 +
b._params.cp_params[j, 4]*(b.temperature*1e-3)**3 +
b._params.cp_params[j, 5]/(b.temperature*1e-3)**2)
try:
# Try to build constraint
self.cp_shomate_eqn = Constraint(self._params.component_list,
rule=pure_component_cp_mol)
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.cp_mol_comp)
self.del_component(self.cp_shomate_eqn)
raise
def _cp_mol(self):
# Mixture heat capacities
self.cp_mol = Var(domain=Reals,
initialize=1.0,
doc="Mixture heat capacity [J/mol.K]")
def cp_mol(b):
return b.cp_mol == sum(b.cp_mol_comp[j]*b.mole_frac_comp[j]
for j in b._params.component_list)
try:
# Try to build constraint
self.mixture_heat_capacity_eqn = Constraint(
rule=cp_mol)
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.cp_mol)
self.del_component(self.mixture_heat_capacity_eqn)
raise
def _energy_internal_mol_phase_comp(self):
# Pure component vapour internal energies
self.energy_internal_mol_phase_comp = Var(
self._params.phase_list,
self._params.component_list,
domain=Reals,
initialize=1.0,
doc="Pure component internal energies [J/mol]")
def pure_comp_int_energy(b, j):
return b.energy_internal_mol_phase_comp["Vap", j] == (1e3*(
b._params.cp_params[j, 1]*(b.temperature*1e-3) +
b._params.cp_params[j, 2]*(b.temperature*1e-3)**2/2 +
b._params.cp_params[j, 3]*(b.temperature*1e-3)**3/3 +
b._params.cp_params[j, 4]*(b.temperature*1e-3)**4/4 -
b._params.cp_params[j, 5]/(b.temperature*1e-3) +
b._params.cp_params[j, 6] -
b._params.cp_params[j, 8]) -
b._params.cp_params[j, 9] +
b._params.enth_mol_form[j] -
b._params.gas_const*(b.temperature -
b._params.temperature_ref))
try:
# Try to build constraint
self.internal_energy_shomate_eqn = Constraint(
self._params.component_list,
rule=pure_comp_int_energy)
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.energy_internal_phase_mol_comp)
self.del_component(self.internal_energy_shomate_eqn)
raise
def _energy_internal_mol(self):
# Mixture molar internal energy
self.energy_internal_mol = Var(
domain=Reals,
initialize=0.0,
doc='Mixture specific internal energy [J/mol]')
try:
# Try to build constraint
self.mixture_energy_internal_eqn = Constraint(expr=(
self.energy_internal_mol == sum(
self.mole_frac_comp[j] *
self.energy_internal_mol_phase_comp["Vap", j]
for j in self._params.component_list)))
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.energy_internal_mol)
self.del_component(self.mixture_energy_internal_eqn)
raise
def _enth_mol_phase_comp(self):
# Pure component vapour enthalpies
self.enth_mol_phase_comp = Var(
self._params.phase_list,
self._params.component_list,
domain=Reals,
initialize=1.0,
doc="Pure component enthalpies [J/mol]")
def pure_comp_enthalpy(b, j):
return b.enth_mol_phase_comp["Vap", j] == (1e3*(
b._params.cp_params[j, 1]*(b.temperature*1e-3) +
b._params.cp_params[j, 2]*(b.temperature*1e-3)**2/2 +
b._params.cp_params[j, 3]*(b.temperature*1e-3)**3/3 +
b._params.cp_params[j, 4]*(b.temperature*1e-3)**4/4 -
b._params.cp_params[j, 5]/(b.temperature*1e-3) +
b._params.cp_params[j, 6] -
b._params.cp_params[j, 8]) -
b._params.cp_params[j, 9] +
b._params.enth_mol_form[j])
try:
# Try to build constraint
self.enthalpy_shomate_eqn = Constraint(self._params.component_list,
rule=pure_comp_enthalpy)
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.enth_mol_phase_comp)
self.del_component(self.enthalpy_shomate_eqn)
raise
def _enth_mol(self):
# Mixture molar enthalpy
self.enth_mol = Var(domain=Reals,
initialize=0.0,
doc='Mixture specific enthalpy [J/mol]')
try:
# Try to build constraint
self.mixture_enthalpy_eqn = Constraint(expr=(
self.enth_mol == sum(
self.mole_frac_comp[j] *
self.enth_mol_phase_comp["Vap", j]
for j in self._params.component_list)))
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.enth_mol)
self.del_component(self.mixture_enthalpy_eqn)
raise
def _entr_mol_phase_comp(self):
# Partial component entropies
self.entr_mol_phase_comp = Var(
self._params.phase_list,
self._params.component_list,
domain=Reals,
initialize=1.0,
doc="Partial component entropies [J/mol.K]")
def partial_comp_entropy(b, j):
return b.entr_mol_phase_comp["Vap", j] == (
b._params.cp_params[j, 1]*log((b.temperature*1e-3)) +
b._params.cp_params[j, 2]*(b.temperature*1e-3) +
b._params.cp_params[j, 3]*(b.temperature*1e-3)**2/2 +
b._params.cp_params[j, 4]*(b.temperature*1e-3)**3/3 -
b._params.cp_params[j, 5]/(2*(b.temperature*1e-3)**2) +
b._params.cp_params[j, 7] -
b._params.gas_const*log(b.mole_frac_comp[j] *
b.pressure/b._params.pressure_ref))
try:
# Try to build constraint
self.entropy_shomate_eqn = Constraint(self._params.component_list,
rule=partial_comp_entropy)
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.entr_mol_phase_comp)
self.del_component(self.entropy_shomate_eqn)
raise
def _entr_mol(self):
# Mixture molar entropy
self.entr_mol = Var(domain=Reals,
initialize=0.0,
doc='Mixture specific entropy [J/mol.K]')
try:
# Try to build constraint
self.mixture_entropy_eqn = Constraint(expr=(
self.entr_mol == sum(
self.mole_frac_comp[j] *
self.entr_mol_phase_comp["Vap", j]
for j in self._params.component_list)))
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.entr_mol)
self.del_component(self.mixture_entropy_eqn)
raise
def _flow_mol(self):
# Total molar material flow
self.flow_mol = Var(domain=Reals,
initialize=1.0,
doc="Total mixture molar flowrate [mol/s]")
try:
# Try to build constraint
self.total_flow_eqn = Constraint(expr=(
self.flow_mol == sum(
self.flow_mol_comp[j]
for j in self._params.component_list)))
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.flow_mol)
self.del_component(self.total_flow_eqn)
raise
def _gibbs_mol_phase_comp(self):
# Partial component Gibbs free energy
self.gibbs_mol_phase_comp = Var(
self._params.phase_list,
self._params.component_list,
domain=Reals,
initialize=0.0,
doc="Partial component Gibbs free energy [J/mol]")
# Assume constant cp_mol for simplicity and vapour phase only
def comp_gibbs_energy_equation(b, j):
return b.gibbs_mol_phase_comp["Vap", j] == (
b.enth_mol_phase_comp["Vap", j] -
b.temperature*b.entr_mol_phase_comp["Vap", j])
try:
# Try to build constraint
self.partial_gibbs_energy_eqn = Constraint(
self._params.component_list,
rule=comp_gibbs_energy_equation)
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.gibbs_mol_comp)
self.del_component(self.partial_gibbs_energy_eqn)
raise
def _gibbs_mol(self):
# Mixture Gibbs energy
self.gibbs_mol = Var(domain=Reals,
initialize=0.0,
doc='Mixture Gibbs energy [J/mol]')
try:
# Try to build constraint
self.mixture_gibbs_eqn = Constraint(expr=(
self.gibbs_mol == (self.enth_mol -
self.temperature*self.entr_mol)))
except AttributeError:
# If constraint fails, clean up so that DAE can try again later
self.del_component(self.gibbs_mol)
self.del_component(self.mixture_gibbs_eqn)
raise
[docs] def get_material_flow_terms(b, p, j):
return b.flow_mol_comp[j]
[docs] def get_enthalpy_flow_terms(b, p):
return b.flow_mol*b.enth_mol
[docs] def get_material_density_terms(b, p, j):
return b.dens_mol_phase[p]*b.mole_frac_comp[j]
[docs] def get_energy_density_terms(b, p):
return b.dens_mol_phase[p]*b.energy_internal_mol
def default_material_balance_type(self):
return MaterialBalanceType.elementTotal
def default_energy_balance_type(self):
return EnergyBalanceType.enthalpyTotal
[docs] def define_state_vars(b):
return {"flow_mol_comp": b.flow_mol_comp,
"temperature": b.temperature,
"pressure": b.pressure}
[docs] def model_check(blk):
"""
Model checks for property block
"""
# Check temperature bounds
if value(blk.temperature) < blk.temperature.lb:
_log.error('{} Temperature set below lower bound.'
.format(blk.name))
if value(blk.temperature) > blk.temperature.ub:
_log.error('{} Temperature set above upper bound.'
.format(blk.name))
# Check pressure bounds
if value(blk.pressure) < blk.pressure.lb:
_log.error('{} Pressure set below lower bound.'.format(blk.name))
if value(blk.pressure) > blk.pressure.ub:
_log.error('{} Pressure set above upper bound.'.format(blk.name))