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plug-flow reactors (PFR) and related the results with data from MFI-type zeolite membranes. Simulations proved the potential of the membrane reactor, combining a modified MFI membrane and cerium-doped ferrite catalysts, to reach CO conversion above 99.5% at 550 ◦C and ~50 atm at a ratio of H2O/CO ~5.0 [155]. Similarly, Lin et al. [156] evaluated the performance of ZSM-5/silicalite bilayer membranes packed with Fe-Cr-Cu catalysts combining experimental and theoretical studies and defined the optimal conditions under which CO conversion of over 95% together with H2 recovery of over 90% could be achieved. For low-temperature WGS reactions, Zhang et al. [153] illustrated the benefit of PBMRs coupling a H2-permselective MFI membrane modified by CCD of methyldiethoxysilane and CuO/ZnO/Al2O3 catalyst over the conventional packed bed reactor. CO conversion exceeding the equilibrium was obtained at 300 ◦C attributed to the enhanced permeation of H2 at the applied temperature on the one hand and the catalyst activity on the other hand. Very recently, the authors proposed the idea of using steam as sweep gas instead of inert gas in order to avoid subsequent separation to obtain pure hydrogen [157]. Figure 6 illustrates schematically this membrane reactor configuration with modified hollow fibre MFI zeolite membranes where the steam is applied in a counter-diffusion towards the reactions side in order to remove H2. The authors stated that sweeping with pure steam contributes to enhanced conversion combined with direct acquisition of the pure H2. Moreover, despite the fact that the membrane was characterized by high H2 permeate flow, sweeping by N2-steam mixed gas resulted in lower conversion if compared to the experiments where pure steam was applied as sweep. The observed phenomenon was attributed to the dilution of the steam by N2 leading to reduced H2O counter-diffusion effect due to the lower driving force though the membrane. Operating under low sweep steam flow rate as well as low feed pressure and H2O/CO ratio contributed to highly pure H2 permeate streams. 4.1.4. Hydrogen Permeation in Syngas Production The benefit of using zeolitic PBMRs over the traditional fixed-bed reactor has also been reported by Liu et al. [215,216] for selective product permeation in CO2 reforming of methane for syngas production. The authors employed a combination of catalytic composite zeolite membranes either La2NiO4/NaA or La2NiO4/NaY prepared on γ-Al2O3/α-Al2O3 support packed with NiO-La2O3/γ-Al2O3 as catalyst. The idea behind this mixed configuration was the significantly low separation efficiency of the as-prepared inert zeolite membranes for the H2/CH4 mixture (binary mixture separation factor of 4.2 at room temperature decreasing to below 2 at temperature over 600 ◦C) and the arising diffusion of methane through the membranes during reforming. Therefore, the authors introduced the use of the catalytic active zeolite membranes packed with catalyst and managed so further 28PDF Image | Zeolite Catalysis
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