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Energies 2019, 12, 469 Energies 2019, 12, x FOR PEER REVIEW Energies 2019, 12, x FOR PEER REVIEW 11 of 15 11 of 15 11 of 15 Figure 8. Measured and modelled conversion of CO for a feed gas with 1.41 or 0.5 vol% CO, 55% H , Figure 8. Measured and modelled conversion of CO for a feed gas with 1.41 or 0.5 vol% CO, 55% H2, 2 ◦ −3 −3 Figure 8. Measured and mode−l3led conversion of CO for a fee−d3 gas with 1.41 or 0.5 vol% CO, 55% H2, C) = 300 kg·s·m for 1.41% CO and 227 kg·s·m for 0.5% CO, p = 1 bar). rest N2 (τ(190 °C) = 300 kg·s·m−3 for 1.41% CO and 227 kg·s·m−3 for 0.5% CO, p = 1 bar). rest N (τ(190 rest N2 (τ2(190 °C) = 300 kg·s·m for 1.41% CO and 227 kg·s·m for 0.5% CO, p = 1 bar). 3.5. Simulation of CO Methanation in an Adiabatic Fixed Bed Reactor Suitable for a Household PEMFC 3.5. Simulation of CO Methanation in an Adiabatic Fixed Bed Reactor Suitable for a Household PEMFC 3.5. Simulation of CO Methanation in an Adiabatic Fixed Bed Reactor Suitable for a Household PEMFC The kinetic equations for CO and CO2 methanation were now used to model the selective The kinetic equations for CO and CO2 methanation were now used to model the selective methanation of CO in a CO /H rich gas stream also containing steam, where both methanation The kinetic equations for2CO2and CO2 methanation were now used to model the selective methanation of CO in a CO2/H2 rich gas stream also containing steam, where both methanation reactions take place simultaneously. The simulation was performed using Matlab and then compared methanation of CO in a CO2/H2 rich gas stream also containing steam, where both methanation reactions take place simultaneously. The simulation was performed using Matlab and then compared with the respective experimental values. reactions take place simultaneously. The simulation was performed using Matlab and then compared with the respective experimental values. The mass balance of a fixed bed reactor and steady state conditions is as follows: with the respective experimental values. The mass balance of a fixed bed reactor and steady state conditions is as follows: The mass balance of a fixed bed reactor and steady state conditions is as follows: dCi−us dCi =∑ri,eff ρb −u =r ρ (14) s dCi di,zeff b −us dz =ri,eff ρb (14) dz u is the superficial gas velocity, and p the bulk density (500 kg−3·m (14) −3 us issthe superficial gas velocity, and pb thbe bulk density (500 kg·m ) of the catalyst (bed porosity is us is the superficial gas velocity, and pb the bulk density (500 kg·m−3) of the catalyst (bed porosity is is 49%). The effective rate r (= η r ) considers the influence of pore diffusion for CO methanation; 49%). The effective rate ri,eff (= iη,efrf i) consiiders the influence of pore diffusion for CO methanation; for 49%). The effective rate ri,eff (= η ri) considers the influence of pore diffusion for CO methanation; for for CO methanation, η is almost one even for temperatures up to 250 C. CO2 meth2anation, η is almost one even for temperatures up to 250 °C. CO2 methanation, η is almost one even for temperatures up to 250 °C. InFigure9,themeasureddegreesofconversionofCOandCO intheisothermallab-scalereactor In Figure 9, the measured degrees of conversion of CO and C2O2 in the isothermal lab-scale In Figure 9, the measured degrees of conversion of CO and CO2 in the isothermal lab-scale are compared with the simulation for a gas containing CO, CO , H O, and H , both with and without reactor are compared with the simulation for a gas containing CO2 , C2O2, H2O, a2nd H2, both with and reactor are compared with the simulation for a gas containing CO, CO2, H2O, and H2, both with and considering the influence of pore diffusion, which lead to similar results as the influence of pore without considering the influence of pore diffusion, which lead to similar results as the influence of without considering the influence of pore diffusion, which lead to similar results as the influence of diffusionissmall.Theagreementisquitewell,andthesimultaneousmethanationofCOandCO are pore diffusion is small. The agreement is quite well, and the simultaneous methanation of CO an2d pore diffusion is small. The agreement is quite well, and the simultaneous methanation of CO and satisfactory described by the kinetic equations. CO2 are satisfactory described by the kinetic equations. CO2 are satisfactory described by the kinetic equations. Figure 9. Measured and modeled CO and CO2 conversion of a feed gas with 1.13 vol% CO, 8% CO2, ) of the catalyst (bed porosity ◦ Figure 9. Measured and modeled CO and CO conversion of a feed gas with 1.13 vol% CO, 8% CO , Figure 9. Measured and modeled CO and CO2 co2n−3version of a feed gas with 1.13 vol% CO, 8% CO2, 2 10%H2Oand55%H2 inN2 (𝜏(200°C)=230kg·s·m ,p=1bar). 10%H Oand55%H inN (τ(200◦C)=230kg−·3s·m−3,p=1bar). 10%H2O2and55%H2in2N2(𝜏2(200°C)=230kg·s·m ,p=1bar). In case of a household application, the exothermic methanation could be conducted in a simple In case of a household application, the exothermic methanation could be conducted in a simple In case of a household application, the exothermic methanation could be conducted in a simple adiabatic fixed bed reactor without the need of a cooling system. For the simulation of the reactor, adiabatic fixed bed reactor without the need of a cooling system. For the simulation of the reactor, adiabatic fixed bed reactor without the need of a cooling system. For the simulation of the reactor, not only the mass balance, but also the temperature change in axial direction has to be considered by not only the mass balance, but also the temperature change in axial direction has to be considered by a respective heat balance (i = CO, CO2; n = all components of the gas): a respective heat balance (i = CO, CO2; n = all components of the gas):PDF Image | Selective Methanation of CO over a Ru-y-AI2O3 Catalyst in CO2 H2
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