def AIT(x2,end_t):
#comp = 'CH4:1.0, O2:2, N2:7.52'
tempx = 980
gasx.set(T = tempx, P = OneAtm, X = x2)
r = Reactor(gasx)
try:
sim = ReactorNet([r])
sim.advance(time)
except:
pass
t_x=r.temperature()
print t_x-tempx
return t_x-tempx
c = (4.0-3.0*R)/(4.0*(1.0-R))
e = c/phi
d = 3.7*e
comp = 'CH4:0.5, H2:%(b)f, O2:%(e)f, N2:%(d)f'% vars()
print '#'+comp
gas = GRI30()
gas.set(T = T0, P = OneAtm, X = comp)
r = Reactor(gas)
env = Reservoir(Air())
w = Wall(r,env)
w.set(K = 0) # set expansion parameter. dV/dt = KA(P_1 - P_2)
w.set(A = 1.0)
sim = ReactorNet([r])
time = 0.0
#Told = r.temperature()
#print '%10.3e %10.3f %10.3f %14.6e' % (sim.time(), r.temperature(), r.pressure(), r.intEnergy_mass())
for n in range(36):
time = (n+1)*0.0005
sim.advance(time)
print '%10.3e %10.3f %10.3f %14.6e' % (sim.time(), r.temperature(), r.pressure(), r.intEnergy_mass())
#while time <= tFinal:
# time = sim.step(tFinal)
# print '%10.3e %10.3f %10.3f %14.6e' % (sim.time(), r.temperature(),
# r.pressure(), r.intEnergy_mass())#print MC_Gemisch(3,1)
print air_mdot,fuel_mdot
# create and install the mass flow controllers
m1 = MassFlowController(upstream = fuel_in, downstream = combustor, mdot = fuel_mdot)
m2 = MassFlowController(upstream = air_in, downstream = combustor, mdot = air_mdot)
igniter_mdot = Gaussian(t0=1.0, FWHM = 0.04, A = 0.1)
m2 = MassFlowController(upstream = igniter, downstream = combustor, mdot = igniter_mdot)
v = Valve (upstream = combustor, downstream = exhaust, Kv = 0.5)
sim = ReactorNet([combustor])
tfinal = 6.0
tnow = 0.0
time_list=[]
temp_list=[]
temp_list3=[]
while tnow< tfinal:
tnow = sim.step(tfinal)
time_list.append(tnow)
#temp_list.append(combustor.density())
temp_list.append(combustor.temperature())
p.plot(list_to_array(time_list),list_to_array(temp_list))
p.xlabel('Zeit')
p.ylabel('Temperatur')
p.show()
# create two mass flow controllers connecting the upstream reservoirs
# to the mixer, and set their mass flow rates to values corresponding
# to stoichiometric combustion.
mfc1 = MassFlowController(upstream = res_a, downstream = mixer,
mdot = rho_a*2.5/0.21)
mfc2 = MassFlowController(upstream = res_b, downstream = mixer,
mdot = rho_b*1.0)
# connect the mixer to the downstream reservoir with a valve.
outlet = Valve(upstream = mixer, downstream = downstream, Kv = 1.0)
sim = ReactorNet([mixer])
# Since the mixer is a reactor, we need to integrate in time to reach
# steady state. A few residence times should be enough.
t = 0.0
for n in range(30):
tres = mixer.mass()/(mfc1.massFlowRate() + mfc2.massFlowRate())
t += 0.5*tres
sim.advance(t)
print '%14.5g %14.5g %14.5g %14.5g %14.5g' % (t, mixer.temperature(),
mixer.enthalpy_mass(),
mixer.pressure(),
mixer.massFraction('CH4'))
# view the state of the gas in the mixer
print mixer.contents()
# flow rates change or if there is chemistry occurring.
mixer = Reactor(gas_b)
# create two mass flow controllers connecting the upstream reservoirs
# to the mixer, and set their mass flow rates to values corresponding
# to stoichiometric combustion.
mfc1 = MassFlowController(upstream=res_a,
downstream=mixer,
mdot=rho_a * 2.5 / 0.21)
mfc2 = MassFlowController(upstream=res_b, downstream=mixer, mdot=rho_b * 1.0)
# connect the mixer to the downstream reservoir with a valve.
outlet = Valve(upstream=mixer, downstream=downstream, Kv=1.0)
sim = ReactorNet([mixer])
# Since the mixer is a reactor, we need to integrate in time to reach
# steady state. A few residence times should be enough.
t = 0.0
for n in range(30):
tres = mixer.mass() / (mfc1.massFlowRate() + mfc2.massFlowRate())
t += 0.5 * tres
sim.advance(t)
print '%14.5g %14.5g %14.5g %14.5g %14.5g' % (
t, mixer.temperature(), mixer.enthalpy_mass(), mixer.pressure(),
mixer.massFraction('CH4'))
# view the state of the gas in the mixer
print mixer.contents()
NotOpenVent = False
for n in range(166000):
time = (n+1)*0.00002
area_valve = 5.E-5
roh = r1.density()
kappa = gas.cp_mole()/gas.cv_mole()
nym_real = min(gas_sink.pressure()/r1.pressure(),((2./(kappa+1.))**(kappa/(kappa-1.))))
#print nym_real,gas_sink.pressure()/r1.pressure(),((2./(kappa+1.))**(kappa/(kappa-1.)))
Ausfluss = ( (kappa/(kappa-1.)) * (nym_real**(2./kappa))* (1.-(nym_real**((kappa-1.)/kappa)))**(1./2.))
Kv = area_valve * 1. * Ausfluss * (2*gas_sink.pressure()*roh)**(1./2.) / roh
print r1.density(),r1.temperature(),r1.pressure()
if (r1.pressure()/1E5)>1.5 or NotOpenVent:
v1.setValveCoeff(Kv)
NotOpenVent = True
sim.advance(time)
time_list.append(time)
temp_list.append(r1.pressure()/1E5)
time_list2.append(time)
temp_list2.append(Kv*10)
time_list3.append(time)
temp_list3.append(r1.temperature()/1000)
#print time,0.000010*(r1.pressure()-gas_sink.pressure())
# note that this connects two reactors with different reaction
# mechanisms and different numbers of species. Downstream and upstream
# species are matched by name.
m2 = MassFlowController(upstream = air_in,
downstream = combustor, mdot = air_mdot)
# The igniter will use a Gaussian 'functor' object to specify the
# time-dependent igniter mass flow rate.
igniter_mdot = Gaussian(t0 = 1.0, FWHM = 0.2, A = 0.1)
m3 = MassFlowController(upstream = igniter,
downstream = combustor, mdot = igniter_mdot)
# put a valve on the exhaust line to regulate the pressure
v = Valve(upstream = combustor, downstream = exhaust, Kv = 1.0)
# the simulation only contains one reactor
sim = ReactorNet([combustor])
# take single steps to 6 s, writing the results to a CSV file
# for later plotting.
tfinal = 6.0
tnow = 0.0
f = open('combustor.csv','w')
while tnow < tfinal:
tnow = sim.step(tfinal)
tres = combustor.mass()/v.massFlowRate()
writeCSV(f, [tnow, combustor.temperature(), tres]
+list(combustor.moleFractions()))
f.close()
sim = ReactorNet([r])
# set the tolerances for the solution and for the sensitivity
# coefficients
sim.setTolerances(rtol = 1.0e-6, atol = 1.0e-15,
rtolsens = 1.0e-5, atolsens = 1.0e-5)
time = 0.0
np = 400
tim = zeros(np,'d')
data = zeros([np,6],'d')
for n in range(np):
time += 5.0e-6
sim.advance(time)
tim[n] = time
data[n,0] = r.temperature()
data[n,1] = r.moleFraction('OH')
data[n,2] = r.moleFraction('H')
data[n,3] = r.moleFraction('CH4')
# sensitivity of OH to reaction 2
data[n,4] = sim.sensitivity('OH',2)
# sensitivity of OH to reaction 3
data[n,5] = sim.sensitivity('OH',3)
print '%10.3e %10.3f %10.3f %14.6e' % (sim.time(), r.temperature(),
r.pressure(), r.intEnergy_mass())
#sim.sensitivity("OH",0))
sim = ReactorNet([r1, r2])
# Now the problem is set up, and we're ready to solve it.
print 'finished setup, begin solution...'
time = 0.0
f = open('piston.csv','w')
writeCSV(f,['time (s)','T1 (K)','P1 (Bar)','V1 (m3)',
'T2 (K)','P2 (Bar)','V2 (m3)'])
temp = zeros([300, 2], 'd')
pres = zeros([300, 2], 'd')
vol = zeros([300, 2], 'd')
tm = zeros(300,'d')
for n in range(300):
time += 4.e-4
print time, r2.temperature(),n
sim.advance(time)
tm[n] = time
temp[n,:] = [r1.temperature(), r2.temperature()]
pres[n,:] = [1.0e-5*r1.pressure(), 1.0e-5*r2.pressure()]
vol[n,:] = [r1.volume(), r2.volume()]
writeCSV(f, [tm[n], temp[n,0], pres[n,0], vol[n,0],
temp[n,1], pres[n,1], vol[n,1]])
f.close()
import os
print 'Output written to file piston.csv'
print 'Directory: '+os.getcwd()
args = sys.argv
if len(args) > 1 and args[1] == '-plot':
try:
# Now the problem is set up, and we're ready to solve it.
print 'finished setup, begin solution...'
time = 0.0
f = open('piston.csv', 'w')
writeCSV(f, [
'time (s)', 'T1 (K)', 'P1 (Bar)', 'V1 (m3)', 'T2 (K)', 'P2 (Bar)',
'V2 (m3)'
])
temp = zeros([300, 2], 'd')
pres = zeros([300, 2], 'd')
vol = zeros([300, 2], 'd')
tm = zeros(300, 'd')
for n in range(300):
time += 4.e-4
print time, r2.temperature(), n
sim.advance(time)
tm[n] = time
temp[n, :] = [r1.temperature(), r2.temperature()]
pres[n, :] = [1.0e-5 * r1.pressure(), 1.0e-5 * r2.pressure()]
vol[n, :] = [r1.volume(), r2.volume()]
writeCSV(f, [
tm[n], temp[n, 0], pres[n, 0], vol[n, 0], temp[n, 1], pres[n, 1],
vol[n, 1]
])
f.close()
import os
print 'Output written to file piston.csv'
print 'Directory: ' + os.getcwd()
args = sys.argv
# create two mass flow controllers connecting the upstream reservoirs
# to the mixer, and set their mass flow rates to values corresponding
# to stoichiometric combustion.
mfc1 = MassFlowController(upstream = res_a, downstream = mixer,
mdot = rho_a*2.5/0.21)
mfc2 = MassFlowController(upstream = res_b, downstream = mixer,
mdot = rho_b*1.0)
# connect the mixer to the downstream reservoir with a valve.
outlet = Valve(upstream = mixer, downstream = downstream, Kv = 1.0)
sim = ReactorNet([mixer])
# Since the mixer is a reactor, we need to integrate in time to reach
# steady state. A few residence times should be enough.
t = 0.0
for n in range(30):
tres = mixer.mass()/(mfc1.massFlowRate() + mfc2.massFlowRate())
t += 0.5*tres
sim.advance(t)
print '%14.5g %14.5g %14.5g %14.5g %14.5g' % (t, mixer.temperature(),
mixer.enthalpy_mass(),
mixer.pressure(),
mixer.massFraction('CH4'))
# view the state of the gas in the mixer
print mixer.contents()
reactors = ReactorNet([r1, r2])
tim = []
t1 = []
t2 = []
v1 = []
v2 = []
v = []
xco = []
xh2 = []
for n in range(30):
time = (n+1)*0.002
reactors.advance(time)
print fmt % (time, r1.temperature(), r2.temperature(),
r1.volume(), r2.volume(), r1.volume() + r2.volume(),
r2.moleFraction('CO'))
tim.append(time)
t1.append(r1.temperature())
t2.append(r2.temperature())
v1.append(r1.volume())
v2.append(r2.volume())
v.append(r1.volume() + r2.volume())
xco.append(r2.moleFraction('CO'))
xh2.append(r1.moleFraction('H2'))
# plot the results if matplotlib is installed.
# see http://matplotlib.sourceforge.net to get it
sim = ReactorNet([r])
# set the tolerances for the solution and for the sensitivity
# coefficients
sim.setTolerances(rtol=1.0e-6, atol=1.0e-15, rtolsens=1.0e-5, atolsens=1.0e-5)
time = 0.0
np = 400
tim = zeros(np, 'd')
data = zeros([np, 6], 'd')
for n in range(np):
time += 5.0e-6
sim.advance(time)
tim[n] = time
data[n, 0] = r.temperature()
data[n, 1] = r.moleFraction('OH')
data[n, 2] = r.moleFraction('H')
data[n, 3] = r.moleFraction('CH4')
# sensitivity of OH to reaction 2
data[n, 4] = sim.sensitivity('OH', 2)
# sensitivity of OH to reaction 3
data[n, 5] = sim.sensitivity('OH', 3)
print '%10.3e %10.3f %10.3f %14.6e %10.3f %10.3f' % (
sim.time(), r.temperature(), r.pressure(), r.intEnergy_mass(),
data[n, 4], data[n, 5])
# plot the results if matplotlib is installed.
# make it flexible, so that the pressure in the reactor is held
# at the environment pressure.
w = Wall(r, env)
w.set(K=1.0e6) # set expansion parameter. dV/dt = KA(P_1 - P_2)
w.set(A=1.0)
sim = ReactorNet([r])
time = 0.0
tim = zeros(100, 'd')
data = zeros([100, 5], 'd')
for n in range(100):
time += 1.e-5
sim.advance(time)
tim[n] = time
data[n, 0] = r.temperature()
data[n, 1] = r.moleFraction('OH')
data[n, 2] = r.moleFraction('H')
data[n, 3] = r.moleFraction('H2')
print '%10.3e %10.3f %10.3f %14.6e' % (sim.time(), r.temperature(),
r.pressure(), r.intEnergy_mass())
# plot the results if matplotlib is installed.
# see http://matplotlib.sourceforge.net to get it
args = sys.argv
if len(args) > 1 and args[1] == '-plot':
try:
from matplotlib.pylab import *
clf
subplot(2, 2, 1)
plot(tim, data[:, 0])
# note that this connects two reactors with different reaction
# mechanisms and different numbers of species. Downstream and upstream
# species are matched by name.
m2 = MassFlowController(upstream = air_in,
downstream = combustor, mdot = air_mdot)
# The igniter will use a Guassiam 'functor' object to specify the
# time-dependent igniter mass flow rate.
igniter_mdot = Gaussian(t0 = 1.0, FWHM = 0.2, A = 0.1)
m3 = MassFlowController(upstream = igniter,
downstream = combustor, mdot = igniter_mdot)
# put a valve on the exhaust line to regulate the pressure
v = Valve(upstream = combustor, downstream = exhaust, Kv = 1.0)
# the simulation only contains one reactor
sim = ReactorNet([combustor])
# take single steps to 6 s, writing the results to a CSV file
# for later plotting.
tfinal = 6.0
tnow = 0.0
f = open('combustor.csv','w')
while tnow < tfinal:
tnow = sim.step(tfinal)
tres = combustor.mass()/v.massFlowRate()
writeCSV(f, [tnow, combustor.temperature(), tres]
+list(combustor.moleFractions()))
f.close()
def list_to_array(data):
'''
Wandelt die Liste in Numpyarray um und schneidet erste Datensatz ab
'''
return N.array(data)
from string import *
time = 10.0
gas = GRI30()
comp = 'CH4:1.0, O2:2, N2:7.52'
for n in range(45):
t = 800.0 + 2.0*n
gas.setState_TPX(t, OneAtm, comp)
r = Reactor(gas)
sim = ReactorNet([r])
sim.setTolerances(rtol=1E-12, atol=1E-22, rtolsens=-1, atolsens=-1)
while sim.time()<time:
sim.step(1)
dt = r.temperature() - t
print t-273.15, dt,sim.time()
if dt > 600.0:
print '!!'
break
if dt > 600.0:
print '!!'
break
gas_c.set(T=300.0, P=OneAtm, X='H:1')
igniter = Reactor(gas_c)
mfc3 = MassFlowController(upstream=igniter, downstream=mixer, mdot=0.05)
# connect the mixer to the downstream reservoir with a valve.
outlet = Valve(upstream=mixer, downstream=downstream, Kv=1.0)
sim = ReactorNet([mixer])
# Since the mixer is a reactor, we need to integrate in time to reach
# steady state. A few residence times should be enough.
t = 0.0
for n in range(30):
tres = mixer.mass() / (mfc1.massFlowRate() + mfc2.massFlowRate())
t += 0.5 * tres
sim.advance(t)
# if ignited, turn the igniter off.
# We also need to restart the integration in this case.
if mixer.temperature() > 1200.0:
mfc3.set(mdot=0.0)
sim.setInitialTime(t)
print '%14.5g %14.5g %14.5g %14.5g %14.5g' % (
t, mixer.temperature(), mixer.enthalpy_mass(), mixer.pressure(),
mixer.massFraction('CH4'))
# view the state of the gas in the mixer
print mixer.contents()
reactors = ReactorNet([r1, r2])
tim = []
t1 = []
t2 = []
v1 = []
v2 = []
v = []
xco = []
xh2 = []
for n in range(30):
time = (n+1)*0.002
reactors.advance(time)
print fmt % (time, r1.temperature(), r2.temperature(),
r1.volume(), r2.volume(), r1.volume() + r2.volume(),
r2.moleFraction('CO'))
tim.append(time)
t1.append(r1.temperature())
t2.append(r2.temperature())
v1.append(r1.volume())
v2.append(r2.volume())
v.append(r1.volume() + r2.volume())
xco.append(r2.moleFraction('CO'))
xh2.append(r1.moleFraction('H2'))
# plot the results if matplotlib is installed.
# see http://matplotlib.sourceforge.net to get it
def PSRCalc(self, volume, tfinal):
initial_gas = self.InitialGas()
gas = self._gas1
NoGas = 0 ## Ignition isn't provided if NoGas = 0
mass_flow = 0
upstreams = numpy.empty(self._code, dtype=object)
ms = numpy.empty(self._code, dtype=object)
reactor = Reactor(initial_gas, volume=volume, energy='on')
ControllerCount = 0
for code in range(0, self._argslength, 2):
upstreams[ControllerCount] = Reservoir(self._args[code])
ms[ControllerCount] = MassFlowController()
ms[ControllerCount].install(upstreams[ControllerCount], reactor)
ms[ControllerCount].set(self._args[code + 1])
mass_flow += self._args[code + 1]
ControllerCount += 1
exhaust = Reservoir(gas)
v = Valve()
v.install(reactor, exhaust)
v.setValveCoeff(Kv=0.5) #Change made from 1.0 to 0.5
sim = ReactorNet([reactor])
tnow = 0.0
tracker = datetime.now()
LoopCounter = 0
while (tnow < tfinal):
LoopCounter += 1
tnow = sim.step(tfinal)
tres = reactor.mass() / mass_flow
currenttime = datetime.now()
d = reactor.massFractions()
IndexCounter = 0
for item in d:
if item > 1:
badguy = 1
baditem = item
break
else:
badguy = 0
IndexCounter += 1
if badguy:
break
b = (currenttime.time().minute - tracker.time().minute)
if (b > 2):
break
if (IndexCounter >= gas.nSpecies()):
badSpecie = 'No Bad Species present'
baditem = 'None'
else:
badSpecie = gas.speciesName(IndexCounter)
tres = reactor.mass() / v.massFlowRate()
T = reactor.temperature()
P = reactor.pressure()
reactor = Reactor(initial_gas)
x = reactor.contents().moleFractions()
initial_gas.setState_TPX(T, P, x)
return initial_gas, mass_flow, tres
if ratio < 0.0: ratio = -ratio
if ratio > 1.0e-9 or time < 10*dt:
alldone = 0
if alldone: break
# set the gas object state to that of this reactor, in
# preparation for the simulation of the next reactor
# downstream, where this object will set the inlet conditions
gas = r.contents()
dist = n*rlen * 1.0e3 # distance in mm
# write the gas mole fractions and surface coverages
# vs. distance
writeCSV(f, [dist, r.temperature() - 273.15,
r.pressure()/OneAtm] + list(gas.moleFractions())
+ list(surf.coverages()))
f.close()
# make a reaction path diagram tracing carbon. This diagram will show
# the pathways by the carbon entering the bed in methane is convered
# into CO and CO2. The diagram will be specifically for the exit of
# the bed; if the pathways are desired at some interior point, then
# put this statement inside the above loop.
#
# To process this diagram, give the command on the command line
# after running this script:
# dot -Tps < carbon_pathways.dot > carbon_pathways.ps
# This will generate the diagram in Postscript.
def PFR(self, volume, NReactors):
initial_gas = self.InitialGas()
gas = self._gas1
T = gas.temperature()
P = gas.pressure()
x = gas.moleFractions()
initial_gas.setState_TPX(T, P, x)
upstreams = numpy.empty(self._code - 1, dtype=object)
ms = numpy.empty(self._code - 1, dtype=object)
mass_flow = self._args[1]
TOL = 1.0E-10
Niter = 20
nsp = gas.nSpecies()
wdot = [''] * nsp
wold = [''] * nsp
volume_n = volume / NReactors
tres = 0.0
for i in range(0, NReactors):
reactor = Reactor(initial_gas, volume=volume_n, energy='on')
upstream = Reservoir(initial_gas)
downstream = Reservoir(initial_gas)
m = MassFlowController()
m.install(upstream, reactor)
m.set(mass_flow)
if (i == 0):
ControllerCount = 0
for code in range(2, self._argslength, 2):
upstreams[ControllerCount] = Reservoir(self._args[code])
ms[ControllerCount] = MassFlowController()
ms[ControllerCount].install(upstreams[ControllerCount],
reactor)
ms[ControllerCount].set(self._args[code + 1])
mass_flow += self._args[code + 1]
ControllerCount += 1
v = Valve()
v.install(reactor, downstream)
v.setValveCoeff(Kv=0.1)
sim = ReactorNet([reactor])
dt = reactor.mass() / mass_flow
tnow = 0.0
wold = initial_gas.netProductionRates()
while (tnow < Niter * dt):
tnow += dt
sim.advance(tnow)
max_change = 0.0
wdot = initial_gas.netProductionRates()
for k in range(0, nsp):
max_change = max(math.fabs(wdot[k] - wold[k]), max_change)
wold[k] = wdot[k]
if (max_change < TOL):
break
tres += reactor.mass() / mass_flow
T = reactor.temperature()
P = reactor.pressure()
reactor = Reactor(initial_gas)
x = reactor.contents().moleFractions()
initial_gas.setState_TPX(T, P, x)
f = self.FuelMassAnalyzer(initial_gas, mass_flow)
return initial_gas, mass_flow, tres, f
if ratio < 0.0: ratio = -ratio
if ratio > 1.0e-9 or time < 10 * dt:
alldone = 0
if alldone: break
# set the gas object state to that of this reactor, in
# preparation for the simulation of the next reactor
# downstream, where this object will set the inlet conditions
gas = r.contents()
dist = n * rlen * 1.0e3 # distance in mm
# write the gas mole fractions and surface coverages
# vs. distance
writeCSV(f, [dist, r.temperature() - 273.15,
r.pressure() / OneAtm] + list(gas.moleFractions()) +
list(surf.coverages()))
f.close()
# make a reaction path diagram tracing carbon. This diagram will show
# the pathways by the carbon entering the bed in methane is convered
# into CO and CO2. The diagram will be specifically for the exit of
# the bed; if the pathways are desired at some interior point, then
# put this statement inside the above loop.
#
# To process this diagram, give the command on the command line
# after running this script:
# dot -Tps < carbon_pathways.dot > carbon_pathways.ps
# This will generate the diagram in Postscript.
mdot = 0.05)
# connect the mixer to the downstream reservoir with a valve.
outlet = Valve(upstream = mixer, downstream = downstream, Kv = 1.0)
sim = ReactorNet([mixer])
# Since the mixer is a reactor, we need to integrate in time to reach
# steady state. A few residence times should be enough.
t = 0.0
for n in range(30):
tres = mixer.mass()/(mfc1.massFlowRate() + mfc2.massFlowRate())
t += 0.5*tres
sim.advance(t)
# if ignited, turn the igniter off.
# We also need to restart the integration in this case.
if mixer.temperature() > 1200.0:
mfc3.set(mdot = 0.0)
sim.setInitialTime(t)
print '%14.5g %14.5g %14.5g %14.5g %14.5g' % (t, mixer.temperature(),
mixer.enthalpy_mass(),
mixer.pressure(),
mixer.massFraction('CH4'))
# view the state of the gas in the mixer
print mixer.contents()
mfc3 = MassFlowController(upstream = igniter, downstream = mixer,
mdot = 0.05)
# connect the mixer to the downstream reservoir with a valve.
outlet = Valve(upstream = mixer, downstream = downstream, Kv = 1.0)
sim = ReactorNet([mixer])
# Since the mixer is a reactor, we need to integrate in time to reach
# steady state. A few residence times should be enough.
t = 0.0
for n in range(30):
tres = mixer.mass()/(mfc1.massFlowRate() + mfc2.massFlowRate())
t += 0.5*tres
sim.advance(t)
# if ignited, turn the igniter off.
# We also need to restart the integration in this case.
if mixer.temperature() > 1200.0:
mfc3.set(mdot = 0.0)
sim.setInitialTime(t)
print '%14.5g %14.5g %14.5g %14.5g %14.5g' % (t, mixer.temperature(),
mixer.enthalpy_mass(),
mixer.pressure(),
mixer.massFraction('CH4'))
# view the state of the gas in the mixer
print mixer.contents()
time_list = []
temp_list = []
temp_list3 = []
# Abbruchkriterium haelfte des Sauerstoffs ist Verbraucht.
O2_Start = r2.moleFraction("O2")
csvfile = "adiabatic.csv"
f = open(csvfile, "w")
writeCSV(f, ["Temp", "Pressure"])
for n in range(15):
time = (n) * 30.0 + 0.015
sim.advance(time)
time_list.append(time)
# time_list2.append(1000./r2.temperature())
temp_list.append(r2.pressure())
temp_list3.append((r2.temperature() - 273.15))
writeCSV(f, [(r2.temperature() - 273.15), r2.pressure() / 1e5])
# temp_list3.append(r2.enthalpy_mass())
# if r2.temperature()>2500:
# break
# if O2_Start/40.>r2.moleFraction('O2'):
# print time_list[-20],temp_list[-20],temp_list3[-20]
# print time_list[-12],temp_list[-12],temp_list3[-12]
# print time_list[-1],temp_list[-1],temp_list3[-1]
# break
# print time,0.000010*(r1.pressure()-gas_sink.pressure())
# print peakdetect(list_to_array(time_list),list_to_array(temp_list3),lookahead = 50,delta = 5)
