Methane steam reforming in large pore catalyst

Oliveira, Eduardo L.G.; Grande, Carlos A.; Rodrigues, Alı́rio E.

doi:10.1016/j.ces.2009.10.018

Cited by 74 publications

(35 citation statements)

References 42 publications

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“…The value of dispersion reported here (1.29%) for commercial Ni/Al 2 O 3 catalyst is similar to one reported by Oliveira et al [43] (1.42%) and by Seo et al [44] (1.5%). Prepared NieCu/Al 2 O 3 catalyst showed a metal dispersion slightly higher than commercial Ni catalyst.…”

Section: 2supporting

confidence: 79%

Characterization and activity test of commercial Ni/Al2O3, Cu/ZnO/Al2O3 and prepared Ni–Cu/Al2O3 catalysts for hydrogen production from methane and methanol fuels

Khzouz

Wood

Pollet

et al. 2013

International Journal of Hydrogen Energy

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Khzouz, M. et al. (2013). Characterization and activity test of commercial Ni/Al203, Cu/ZnO/Al203 and prepared NieCu/Al203 catalysts for the hydrogen production from methane and methanol fuels. A comprehensive comparison between these two fuels is established in terms of reaction conditions, fuel conversion, H2 selectivity, CO2 and CO selectivity. The prepared catalyst showed low selectivity for CO in both fuels and it was more selective to H2, with H2 selectivities of 99% in methane and 89% in methanol reforming reactions. A significant objective is to develop catalysts which can operate at lower temperatures and resist deactivation. Methanol steam reforming is carried out at a much lower temperature than methane steam reforming in prepared and commercial catalyst (275-325 o C). However, methane steam reforming can be carried out at a relatively low temperature on NieCu catalyst (600-650 o C) and at higher temperature in commercial methane reforming catalyst (700-800 o C). Commercial Ni/Al2O3 catalyst resulted in high coke formation (28.3% loss in mass) compared to prepared NieCu/Al2O3 (8.9%) and commercial Cu/ZnO/Al2O3 catalysts (3.5%).

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Section: 2supporting

confidence: 79%

Characterization and activity test of commercial Ni/Al2O3, Cu/ZnO/Al2O3 and prepared Ni–Cu/Al2O3 catalysts for hydrogen production from methane and methanol fuels

Khzouz

Wood

Pollet

et al. 2013

International Journal of Hydrogen Energy

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“…Due to emerging industrial trends, methane cracking and reforming to syngas or H 2 has attracted research and development (R&D) interests from academia and industry in recent years [1][2][3]. Steam methane reforming is the most common process for the production of hydrogen and synthesis gas, but catalyst deactivation may occur during methane steam reforming with Ni catalysts since it promotes carbon deposition over the catalyst [4].…”

Section: Introductionmentioning

confidence: 99%

Catalytic Performance of Coal Char for the Methane Reforming Process

Sun

et al. 2014

Chem Eng & Technol

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A new concept of combined coal gasification and methane reforming in a single reactor was proposed as an alternative path for syngas production using coal and coalbed methane. Here, the results of this process are summarized. The experimental work was carried out in a fixed-bed reactor. Methane cracking, CO 2 /steam reforming of methane over coal char, and the effects of chars made from different types of parent coal on methane conversion were examined. The catalytic effect of coal char on methane cracking and reforming increased with decreasing coalification degree. A synergistic effect was observed in that, while the coal char catalyzed the methane reforming reactions, gasification of the coal char took place simultaneously, which counter-balanced the deposition of carbon especially for the methane-steam-char system.

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“…The simulation parameters used are given in Table 1. The reactions were modeled using the kinetic model of Langmuir-Hinshelwood proposed by Xu and Froment [19] with appropriate kinetic and equilibrium constants from [20]. Simulations are completed for three different values for inlet temperature ( Table 1).…”

Section: Pr-dns Setupmentioning

confidence: 99%

Multiscale Modeling of a Packed Bed Chemical Looping Reforming (PBCLR) Reactor

et al. 2017

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Packed bed reactors are broadly used in industry and are under consideration for novel reactor concepts such as packed bed chemical looping reforming (PBCLR). Mass and heat transfer limitations in and around the particles in packed bed reactors strongly affect the behavior of these units. This study employs a multiscale modeling methodology to simulate a PBCLR reactor. Specifically, small-scale particle-resolved direct numerical simulation is utilized to improve large-scale mass transfer models for use in an industrial scale 1D model. Existing intra-particle mass transfer models perform well for simple first order reactions, but several model enhancements were required to model the more complex steam methane reforming reaction system. Three specific aspects required enhanced modeling: the generation of additional gas volume by the reforming reactions, the lack of clear reaction orders in the equilibrium reactions, and the diffusion of multiple reactant species into the particle. Large-scale simulations of the PBCLR reactor with the enhanced 1D model showed that the highly reactive Ni-based catalyst/oxygen carrier employed allows for the use of large particle sizes and high gas flowrates, offering potential for process intensification.

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Methane steam reforming in large pore catalyst

Cited by 74 publications

References 42 publications

Characterization and activity test of commercial Ni/Al2O3, Cu/ZnO/Al2O3 and prepared Ni–Cu/Al2O3 catalysts for hydrogen production from methane and methanol fuels

Characterization and activity test of commercial Ni/Al2O3, Cu/ZnO/Al2O3 and prepared Ni–Cu/Al2O3 catalysts for hydrogen production from methane and methanol fuels

Catalytic Performance of Coal Char for the Methane Reforming Process

Multiscale Modeling of a Packed Bed Chemical Looping Reforming (PBCLR) Reactor

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