2528df0f75
These changes make it unnecessary to copy header files around during the build process, which tends to confuse IDEs and debuggers. The headers which comprise Cantera's external C++ interface are now in the 'include' directory. All of the samples and demos are now in the 'samples' subdirectory.
183 lines
6.2 KiB
Python
183 lines
6.2 KiB
Python
# This example solves a plug flow reactor problem, where the chemistry
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# is surface chemistry. The specific problem simulated is the partial
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# oxidation of methane over a platinum catalyst in a packed bed
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# reactor.
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from Cantera import *
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from Cantera.Reactor import *
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from Cantera import rxnpath
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import math
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import sys
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#######################################################################
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# unit conversion factors to SI
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cm = 0.01
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minute = 60.0
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#######################################################################
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#
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# Input Parameters
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#
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#######################################################################
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tc = 800.0 # Temperature in Celsius
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length = 0.3 * cm # Catalyst bed length
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area = 1.0 * cm * cm # Catalyst bed area
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cat_area_per_vol = 1000.0 / cm # Catalyst particle surface area
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# per unit volume
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velocity = 40.0 * cm / minute # gas velocity
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porosity = 0.3 # Catalyst bed porosity
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# input file containing the surface reaction mechanism
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cti_file = 'methane_pox_on_pt.cti'
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# The PFR will be simulated by a chain of 'NReactors' stirred
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# reactors.
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NReactors = 201
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#
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# Decreased the time step by a factor of 100 to help convergence
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# 12/28/2009 HKM
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#
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# dt = 1.0
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dt = 0.01
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#####################################################################
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t = tc + 273.15 # convert to Kelvin
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# import the gas model
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gas = importPhase(cti_file,'gas')
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# set the initial conditions
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gas.set(T = t, P = OneAtm, X = 'CH4:1, O2:1.5, AR:0.1')
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rho0 = gas.density()
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nsp = gas.nSpecies()
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g_names = gas.speciesNames()
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# import the surface model
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surf = importInterface(cti_file,'Pt_surf', [gas])
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surf.setTemperature(t)
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s_names = surf.speciesNames()
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nsurf = surf.nSpecies()
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rlen = length/(NReactors-1)
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rvol = area * rlen * porosity
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names = gas.speciesNames()
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f = open('surf_pfr_output.csv','w')
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writeCSV(f, ['Distance (mm)', 'T (C)', 'P (atm)'] + g_names + s_names)
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# catalyst area in one reactor
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cat_area = cat_area_per_vol*rvol
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mass_flow_rate = velocity * rho0 * area
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# The plug flow reactor is represented by a linear chain of
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# zero-dimensional reactors. The gas at the inlet to the first one has
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# the specified inlet composition, and for all others the inlet
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# composition is fixed at the composition of the reactor immediately
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# upstream. Since in a PFR model there is no diffusion, the upstream
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# reactors are not affected by any downstream reactors, and therefore
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# the problem may be solved by simply marching from the first to last
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# reactor, integrating each one to steady state.
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for n in range(NReactors):
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# create a new reactor
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r = Reactor(contents = gas, energy = 'off', volume = rvol)
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# create a reservoir to represent the reactor immediately
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# upstream. Note that the gas object is set already to the
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# state of the upstream reactor
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upstream = Reservoir(gas, name = 'upstream')
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# create a reservoir for the reactor to exhaust into. The
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# composition of this reservoir is irrelevant.
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downstream = Reservoir(gas, name = 'downstream')
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# use a 'Wall' object to implement the reacting surface in the
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# reactor. Since walls have to be installed between two
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# reactors/reserviors, we'll install it between the upstream
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# reservoir and the reactor. The area is set to the desired
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# catalyst area in the reactor, and surface reactions are
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# included only on the side facing the reactor.
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w = Wall(left = upstream, right = r, A = cat_area, kinetics = [None, surf])
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# We need a valve between the reactor and the downstream reservoir.
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# This will determine the pressure in the reactor. Set Kv large
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# enough that the pressure difference is very small.
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v = Valve(upstream = r, downstream = downstream, Kv = 3.0e-6)
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# The mass flow rate into the reactor will be fixed by using a
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# MassFlowController object.
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m = MassFlowController(upstream = upstream,
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downstream = r, mdot = mass_flow_rate)
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sim = ReactorNet([upstream, r, downstream])
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# set relative and absolute tolerances on the simulation
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sim.setTolerances(rtol = 1.0e-4, atol = 1.0e-11)
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time = 0
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while 1 > 0:
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time = time + dt
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sim.advance(time)
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# check whether surface coverages are in steady
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# state. This will be the case if the creation and
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# destruction rates for a surface (but not gas) species
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# are equal.
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alldone = 1
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# Note: netProduction = creation - destruction. By
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# supplying the surface object as an argument, only the
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# values for the surface species are returned by these
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# methods
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sdot = surf.netProductionRates(surf)
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cdot = surf.creationRates(surf)
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ddot = surf.destructionRates(surf)
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for ks in range(nsurf):
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ratio = sdot[ks]/(cdot[ks] + ddot[ks])
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if ratio < 0.0: ratio = -ratio
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if ratio > 1.0e-9 or time < 10*dt:
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alldone = 0
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if alldone: break
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# set the gas object state to that of this reactor, in
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# preparation for the simulation of the next reactor
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# downstream, where this object will set the inlet conditions
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gas = r.contents()
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dist = n*rlen * 1.0e3 # distance in mm
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# write the gas mole fractions and surface coverages
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# vs. distance
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writeCSV(f, [dist, r.temperature() - 273.15,
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r.pressure()/OneAtm] + list(gas.moleFractions())
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+ list(surf.coverages()))
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f.close()
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# make a reaction path diagram tracing carbon. This diagram will show
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# the pathways by the carbon entering the bed in methane is convered
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# into CO and CO2. The diagram will be specifically for the exit of
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# the bed; if the pathways are desired at some interior point, then
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# put this statement inside the above loop.
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#
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# To process this diagram, give the command on the command line
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# after running this script:
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# dot -Tps < carbon_pathways.dot > carbon_pathways.ps
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# This will generate the diagram in Postscript.
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element = 'C'
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rxnpath.write(surf, element, 'carbon_pathways.dot')
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