# -*- coding: utf-8
"""Module of class Condenser.
This file is part of project TESPy (github.com/oemof/tespy). It's copyrighted
by the contributors recorded in the version control history of the file,
available from its original location
tespy/components/heat_exchangers/condenser.py
SPDX-License-Identifier: MIT
"""
import math
import numpy as np
from tespy.components.component import component_registry
from tespy.components.heat_exchangers.base import HeatExchanger
from tespy.tools.data_containers import SimpleDataContainer as dc_simple
from tespy.tools.document_models import generate_latex_eq
from tespy.tools.fluid_properties import dh_mix_dpQ
from tespy.tools.fluid_properties import h_mix_pQ
from tespy.tools.helpers import convert_from_SI
[docs]
@component_registry
class Condenser(HeatExchanger):
r"""
A Condenser cools a fluid until it is in liquid state.
The condensing fluid is cooled by the cold side fluid. The fluid on the hot
side of the condenser must be pure. Subcooling is available.
**Mandatory Equations**
- :py:meth:`tespy.components.component.Component.fluid_func`
- :py:meth:`tespy.components.component.Component.mass_flow_func`
- :py:meth:`tespy.components.heat_exchangers.base.HeatExchanger.energy_balance_func`
- condensate outlet state, function can be disabled by specifying
:code:`set_attr(subcooling=True)`
:py:meth:`tespy.components.heat_exchangers.condenser.Condenser.subcooling_func`
**Optional Equations**
- :py:meth:`tespy.components.heat_exchangers.base.HeatExchanger.energy_balance_hot_func`
- :py:meth:`tespy.components.heat_exchangers.condenser.Condenser.kA_func`
- :py:meth:`tespy.components.heat_exchangers.condenser.Condenser.kA_char_func`
- :py:meth:`tespy.components.heat_exchangers.condenser.Condenser.ttd_u_func`
- :py:meth:`tespy.components.heat_exchangers.base.HeatExchanger.ttd_l_func`
- :py:meth:`tespy.components.heat_exchangers.base.HeatExchanger.ttd_min_func`
- :py:meth:`tespy.components.heat_exchangers.base.HeatExchanger.eff_cold_func`
- :py:meth:`tespy.components.heat_exchangers.base.HeatExchanger.eff_hot_func`
- :py:meth:`tespy.components.heat_exchangers.base.HeatExchanger.eff_max_func`
- hot side :py:meth:`tespy.components.component.Component.pr_func`
- cold side :py:meth:`tespy.components.component.Component.pr_func`
- hot side :py:meth:`tespy.components.component.Component.zeta_func`
- cold side :py:meth:`tespy.components.component.Component.zeta_func`
- hot side :py:meth:`tespy.components.component.Component.dp_func`
- cold side :py:meth:`tespy.components.component.Component.dp_func`
Inlets/Outlets
- in1, in2 (index 1: hot side, index 2: cold side)
- out1, out2 (index 1: hot side, index 2: cold side)
Image
.. image:: /api/_images/Condenser.svg
:alt: flowsheet of the condenser
:align: center
:class: only-light
.. image:: /api/_images/Condenser_darkmode.svg
:alt: flowsheet of the condenser
:align: center
:class: only-dark
Parameters
----------
label : str
The label of the component.
design : list
List containing design parameters (stated as String).
offdesign : list
List containing offdesign parameters (stated as String).
design_path : str
Path to the components design case.
local_offdesign : boolean
Treat this component in offdesign mode in a design calculation.
local_design : boolean
Treat this component in design mode in an offdesign calculation.
char_warnings : boolean
Ignore warnings on default characteristics usage for this component.
printout : boolean
Include this component in the network's results printout.
Q : float, dict
Heat transfer, :math:`Q/\text{W}`.
pr1 : float, dict, :code:`"var"`
Outlet to inlet pressure ratio at hot side, :math:`pr/1`.
pr2 : float, dict, :code:`"var"`
Outlet to inlet pressure ratio at cold side, :math:`pr/1`.
dp1 : float, dict, :code:`"var"`
Inlet to outlet pressure delta at hot side, :math:`dp/\text{Pa}`.
dp2 : float, dict, :code:`"var"`
Inlet to outlet pressure delta at cold side, :math:`dp/\text{Pa}`.
zeta1 : float, dict, :code:`"var"`
Geometry independent friction coefficient at hot side,
:math:`\frac{\zeta}{D^4}/\frac{1}{\text{m}^4}`.
zeta2 : float, dict, :code:`"var"`
Geometry independent friction coefficient at cold side,
:math:`\frac{\zeta}{D^4}/\frac{1}{\text{m}^4}`.
ttd_l : float, dict
Lower terminal temperature difference :math:`ttd_\mathrm{l}/\text{K}`.
ttd_u : float, dict
Upper terminal temperature difference (referring to saturation
temprature of condensing fluid) :math:`ttd_\mathrm{u}/\text{K}`.
ttd_min : float, dict
Minumum terminal temperature difference :math:`ttd_\mathrm{min}/\text{K}`.
eff_cold : float, dict
Cold side heat exchanger effectiveness :math:`eff_\text{cold}/\text{1}`.
eff_hot : float, dict
Hot side heat exchanger effectiveness :math:`eff_\text{hot}/\text{1}`.
eff_max : float, dict
Max value of hot and cold side heat exchanger effectiveness values
:math:`eff_\text{max}/\text{1}`.
kA : float, dict
Area independent heat transfer coefficient,
:math:`kA/\frac{\text{W}}{\text{K}}`.
kA_char : tespy.tools.data_containers.SimpleDataContainer
Area independent heat transfer coefficient characteristic.
kA_char1 : tespy.tools.characteristics.CharLine, dict
Characteristic line for hot side heat transfer coefficient.
kA_char2 : tespy.tools.characteristics.CharLine, dict
Characteristic line for cold side heat transfer coefficient.
subcooling : boolean
Enable/disable subcooling, default value: disabled.
Note
----
The condenser has an additional equation for enthalpy at hot side outlet:
The fluid leaves the component in saturated liquid state. If subcooling
is activated, it possible to specify the enthalpy at the outgoing
connection manually.
It has different calculation method for given heat transfer coefficient and
upper terminal temperature dierence: These parameters refer to the
**condensing** temperature, even if the fluid on the hot side enters the
component in superheated state.
Example
-------
Air is used to condensate water in a condenser. 1 kg/s waste steam is
chilled with a terminal temperature difference of 15 K.
>>> from tespy.components import Sink, Source, Condenser
>>> from tespy.connections import Connection
>>> from tespy.networks import Network
>>> from tespy.tools.fluid_properties import T_sat_p
>>> import shutil
>>> nw = Network(T_unit='C', p_unit='bar', h_unit='kJ / kg',
... m_range=[0.01, 1000], iterinfo=False)
>>> amb_in = Source('ambient air inlet')
>>> amb_out = Sink('air outlet')
>>> waste_steam = Source('waste steam')
>>> c = Sink('condensate sink')
>>> cond = Condenser('condenser')
>>> cond.component()
'condenser'
>>> amb_he = Connection(amb_in, 'out1', cond, 'in2')
>>> he_amb = Connection(cond, 'out2', amb_out, 'in1')
>>> ws_he = Connection(waste_steam, 'out1', cond, 'in1')
>>> he_c = Connection(cond, 'out1', c, 'in1')
>>> nw.add_conns(amb_he, he_amb, ws_he, he_c)
The air flow can not be controlled, thus is constant in offdesign
operation. If the waste steam mass flow or the ambient air temperature
change, the outlet temperature of the air will change, too.
>>> cond.set_attr(pr1=0.98, pr2=0.999, ttd_u=15, design=['pr2', 'ttd_u'],
... offdesign=['zeta2', 'kA_char'])
>>> ws_he.set_attr(fluid={'water': 1}, h=2700, m=1)
>>> amb_he.set_attr(fluid={'air': 1}, T=20, offdesign=['v'])
>>> he_amb.set_attr(p=1, T=40, design=['T'])
>>> nw.solve('design')
>>> nw.save('tmp')
>>> round(amb_he.v.val, 2)
103.17
>>> round(ws_he.T.val - he_amb.T.val, 1)
66.9
>>> round(ws_he.calc_T_sat() - 273.15 - he_amb.T.val, 1)
15.0
>>> ws_he.set_attr(m=0.7)
>>> amb_he.set_attr(T=30)
>>> nw.solve('offdesign', design_path='tmp')
>>> round(ws_he.T.val - he_amb.T.val, 1)
62.5
>>> round(ws_he.calc_T_sat() - 273.15 - he_amb.T.val, 1)
11.3
It is possible to activate subcooling. The difference to boiling point
temperature is specified to 5 K.
>>> cond.set_attr(subcooling=True)
>>> he_c.set_attr(Td_bp=-5)
>>> nw.solve('offdesign', design_path='tmp')
>>> round(ws_he.T.val - he_amb.T.val, 1)
62.5
>>> round(ws_he.calc_T_sat() - 273.15 - he_amb.T.val, 1)
13.4
>>> shutil.rmtree('./tmp', ignore_errors=True)
"""
[docs]
@staticmethod
def component():
return 'condenser'
[docs]
def get_parameters(self):
params = super().get_parameters()
params.update({
'subcooling': dc_simple(
val=False, num_eq=1, latex=self.subcooling_func_doc,
deriv=self.subcooling_deriv, func=self.subcooling_func)
})
return params
[docs]
def preprocess(self, num_nw_vars):
# if subcooling is True, outlet state method must not be calculated
self.subcooling.is_set = not self.subcooling.val
super().preprocess(num_nw_vars)
[docs]
def subcooling_func(self):
r"""
Equation for hot side outlet state.
Returns
-------
residual : float
Residual value of equation.
.. math::
0=h_{out,1} -h\left(p_{out,1}, x=0 \right)
Note
----
This equation is applied in case subcooling is False!
"""
o = self.outl[0]
return o.h.val_SI - h_mix_pQ(o.p.val_SI, 0, o.fluid_data)
[docs]
def subcooling_func_doc(self, label):
r"""
Equation for hot side outlet state.
Parameters
----------
label : str
Label for equation.
Returns
-------
latex : str
LaTeX code of equations applied.
"""
latex = r'0=h_\mathrm{out,1} -h\left(p_\mathrm{out,1}, x=0 \right)'
return generate_latex_eq(self, latex, label)
[docs]
def subcooling_deriv(self, increment_filter, k):
"""
Calculate partial derivates of subcooling function.
Parameters
----------
increment_filter : ndarray
Matrix for filtering non-changing variables.
k : int
Position of derivatives in Jacobian matrix (k-th equation).
"""
o = self.outl[0]
if self.is_variable(o.p):
self.jacobian[k, o.p.J_col] = -dh_mix_dpQ(o.p.val_SI, 0, o.fluid_data)
if self.is_variable(o.h):
self.jacobian[k, o.h.J_col] = 1
[docs]
def calculate_td_log(self):
i1 = self.inl[0]
i2 = self.inl[1]
o1 = self.outl[0]
o2 = self.outl[1]
T_i1 = i1.calc_T_sat()
T_i2 = i2.calc_T()
T_o1 = o1.calc_T()
T_o2 = o2.calc_T()
if T_i1 <= T_o2 and not i1.T.is_set:
T_i1 = T_o2 + 0.5
if T_i1 <= T_o2 and not o2.T.is_set:
T_o2 = T_i1 - 0.5
if T_o1 <= T_i2 and not o1.T.is_set:
T_o1 = T_i2 + 1
if T_o1 <= T_i2 and not i2.T.is_set:
T_i2 = T_o1 - 1
ttd_u = T_i1 - T_o2
ttd_l = T_o1 - T_i2
if ttd_u == ttd_l:
td_log = ttd_l
else:
td_log = (ttd_l - ttd_u) / math.log((ttd_l) / (ttd_u))
return td_log
[docs]
def kA_func_doc(self, label):
r"""
Calculate heat transfer from heat transfer coefficient.
Parameters
----------
label : str
Label for equation.
Returns
-------
latex : str
LaTeX code of equations applied.
"""
latex = (
r'0 = \dot{m}_\mathrm{in,1} \cdot \left( h_\mathrm{out,1} - '
r'h_\mathrm{in,1}\right)+ kA \cdot \frac{T_\mathrm{out,1} - '
r'T_\mathrm{in,2} -T_\mathrm{sat}\left( p_\mathrm{in,1}\right)'
r'+ T_\mathrm{out,2}}'
r'{\ln{\frac{T_\mathrm{out,1} - T_\mathrm{in,2}}'
r'{T_\mathrm{sat}\left( p_\mathrm{in,1}\right) -'
r'T_\mathrm{out,2}}}}'
)
return generate_latex_eq(self, latex, label)
[docs]
def kA_char_func(self):
r"""
Calculate heat transfer from heat transfer coefficient characteristic.
Returns
-------
residual : float
Residual value of equation.
.. math::
0 = \dot{m}_{in,1} \cdot \left( h_{out,1} - h_{in,1}\right) +
kA_{design} \cdot f_{kA} \cdot \frac{T_{out,1} -
T_{in,2} - T_{sat} \left(p_{in,1}\right) + T_{out,2}}
{\ln{\frac{T_{out,1} - T_{in,2}}
{T_{sat} \left(p_{in,1}\right) - T_{out,2}}}}
f_{kA} = \frac{2}{\frac{1}{f_1 \left( expr_1\right)} +
\frac{1}{f_2 \left( expr_2\right)}}
Note
----
For standard functions f\ :subscript:`1` \ and f\ :subscript:`2` \ see
module :py:mod:`tespy.data`.
"""
return super().kA_char_func()
[docs]
def kA_char_func_doc(self, label):
r"""
Calculate heat transfer from heat transfer coefficient characteristic.
Parameters
----------
label : str
Label for equation.
Returns
-------
latex : str
LaTeX code of equations applied.
"""
latex = (
r'\begin{split}' + '\n'
r'0 = & \dot{m}_\mathrm{in,1} \cdot \left( h_\mathrm{out,1} - '
r'h_\mathrm{in,1}\right)\\' + '\n'
r'&+kA_\mathrm{design} \cdot '
r'f_\mathrm{kA} \cdot \frac{T_\mathrm{out,1} - T_\mathrm{in,2}'
r' - T_\mathrm{sat}\left( p_\mathrm{in,1}\right) +'
r'T_\mathrm{out,2}}{\ln{\frac{T_\mathrm{out,1}-'
r'T_\mathrm{in,2}}{T_\mathrm{sat}\left( p_\mathrm{in,1}\right)'
r'- T_\mathrm{out,2}}}}\\' + '\n'
r'f_\mathrm{kA}=&\frac{2}{\frac{1}{f\left(X_1\right)}+'
r'\frac{1}{f\left(X_2\right)}}\\' + '\n'
r'\end{split}'
)
return generate_latex_eq(self, latex, label)
[docs]
def ttd_u_func(self):
r"""
Equation for upper terminal temperature difference.
Returns
-------
residual : float
Residual value of equation.
.. math::
0 = ttd_{u} - T_{sat} \left(p_{in,1}\right) + T_{out,2}
Note
----
The upper terminal temperature difference ttd_u refers to boiling
temperature at hot side inlet.
"""
i = self.inl[0]
o = self.outl[1]
T_i1 = i.calc_T_sat()
T_o2 = o.calc_T()
return self.ttd_u.val - T_i1 + T_o2
[docs]
def ttd_u_func_doc(self, label):
r"""
Equation for upper terminal temperature difference.
Parameters
----------
label : str
Label for equation.
Returns
-------
latex : str
LaTeX code of equations applied.
"""
latex = (
r'0=ttd_\mathrm{u}-T_\mathrm{sat}\left(p_\mathrm{in,1}\right)'
r' + T_\mathrm{out,2}')
return generate_latex_eq(self, latex, label)
[docs]
def calc_parameters(self):
r"""Postprocessing parameter calculation."""
self.Q.val = self.inl[0].m.val_SI * (
self.outl[0].h.val_SI - self.inl[0].h.val_SI
)
self.ttd_u.val = self.inl[0].calc_T_sat() - self.outl[1].T.val_SI
self.ttd_l.val = self.outl[0].T.val_SI - self.inl[1].T.val_SI
self.ttd_min.val = min(self.ttd_u.val, self.ttd_min.val)
# pr and zeta
for i in range(2):
self.get_attr(f'pr{i + 1}').val = (
self.outl[i].p.val_SI / self.inl[i].p.val_SI
)
self.get_attr(f'zeta{i + 1}').val = self.calc_zeta(
self.inl[i], self.outl[i]
)
self.get_attr(f'dp{i + 1}').val_SI = (
self.inl[i].p.val_SI - self.outl[i].p.val_SI)
self.get_attr(f'dp{i + 1}').val = convert_from_SI(
'p', self.get_attr(f'dp{i + 1}').val_SI, self.inl[i].p.unit
)
# kA and logarithmic temperature difference
if self.ttd_u.val < 0 or self.ttd_l.val < 0:
self.td_log.val = np.nan
elif self.ttd_l.val == self.ttd_u.val:
self.td_log.val = self.ttd_l.val
else:
self.td_log.val = (
(self.ttd_l.val - self.ttd_u.val)
/ math.log(self.ttd_l.val / self.ttd_u.val)
)
self.kA.val = -self.Q.val / self.td_log.val
# heat exchanger efficiencies
try:
self.eff_hot.val = (
(self.outl[0].h.val_SI - self.inl[0].h.val_SI)
/ self.calc_dh_max_hot()
)
except ValueError:
self.eff_hot.val = np.nan
msg = (
"Cannot calculate heat exchanger hot side effectiveness "
"because cold side inlet temperature is out of bounds for hot "
"side fluid."
)
logger.warning(msg)
try:
self.eff_cold.val = (
(self.outl[1].h.val_SI - self.inl[1].h.val_SI)
/ self.calc_dh_max_cold()
)
except ValueError:
self.eff_cold.val = np.nan
msg = (
"Cannot calculate heat exchanger cold side effectiveness "
"because hot side inlet temperature is out of bounds for cold "
"side fluid."
)
logger.warning(msg)
self.eff_max.val = max(self.eff_hot.val, self.eff_cold.val)