Coke formation during CO2 reforming of CH4 over alumina-supported nickel catalysts

Al–Fatish, A.S.A.; Ibrahim, Ahmed A.; Fakeeha, Anis H.; Soliman, M.A.; Siddiqui, Mohammed Rafiq H.; Abasaeed, Ahmed E.

doi:10.1016/j.apcata.2009.05.043

Cited by 121 publications

(52 citation statements)

References 25 publications

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“…Ni supported over alumina catalyst was synthesized by simple wet impregnation method [23]. Nickel nitrate (NiNO 3 .6H 2 O) salt was impregnated over high surface area alumina (SA-6175), and was then dried for 14h at 110 o C. The material was then calcined at 800 o C for 3h.…”

Section: Methods and Materials Synthesis Of Catalystmentioning

confidence: 99%

Effects of catalytic bed position on hydrogen production by methane decomposition

Sikander¹,

Sufian²,

KuShaari³

et al. 2018

J. MECH. ENG. SCI.

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CO x free hydrogen can be produced by thermal decomposition of methane. Such process is carried out in a fixed bed catalytic reactor. Where heterogeneous catalytic reaction occur when methane come in contact with catalyst bed at a temperature range of 650-900ºC. In this work effect of different catalyst bed positions are investigated on the overall methane conversion to hydrogen. Experimental studies are carried out to in a Fixed Bed Reactor at 700 o C, by placing a catalyst bed of same porosity µ=0.2 at 25%, 50%, 75% column height, and at top of reactor. It is found that same catalyst has shown different results when placed at different heights in reactor column. Highest methane conversion of 85% is found when catalyst bed is placed at 25% column height from bottom. It is found that for endothermic reactions like methane decomposition catalyst bed position has its significance due to its effects on process thermal conditions and on bed expansion by carbon deposition.

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Section: Methods and Materials Synthesis Of Catalystmentioning

confidence: 99%

Effects of catalytic bed position on hydrogen production by methane decomposition

Sikander¹,

Sufian²,

KuShaari³

et al. 2018

J. MECH. ENG. SCI.

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“…The data were collected every 30 min on stream for 9 h. Reaction products were analyzed by an online gas chromatograph (Varian Star 3400 CX). The schematic of the experimental setup and procedure is provided in [32,33].…”

Section: Catalytic Testingmentioning

confidence: 99%

Ni catalysts with different promoters supported on zeolite for dry reforming of methane

et al. 2015

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Dry reforming of methane (DRM) is considered a high endothermic reaction with operating temperatures between 700 and 1000°C to achieve high equilibrium conversion of CH 4 and CO 2 to the syngas (H 2 and CO). The conventional catalysts used for DRM are Ni-based catalysts. However, many of these catalysts suffer from the short longevity due to carbon deposition. This study aims to evaluate the effect of La and Ca as promoters for Nibased catalysts supported on two different zeolite supports, ZL (A) (BET surface area = 925 m 2 /g, SiO 2 /Al 2 O 3 mol ratio = 5.1), and ZL (B) (BET surface area = 730 m 2 /g, SiO 2 /Al 2 O 3 mol ratio = 12), for DRM. The physicochemical properties of the prepared catalysts were characterized with XRD, BET, TEM and TGA. These catalysts were tested for DRM in a microtubular reactor at reaction conditions of 700°C. The catalyst activity results show that the catalysts Ni/ZL (B) and Ca-Ni/ZL (B) give the highest methane conversion (60 %) with less time on stream stability compared with promoted Ni on ZL (A). In contrast, La-containing catalysts, La-Ni/ZL (B), show more time on stream stability with minimum carbon content for the spent catalyst indicating the enhancement of the promoters to the Ni/ZL (A) and (B), but with less catalytic activity performance in terms of methane and carbon dioxide conversions due to rapid catalyst deactivation.

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“…In comparison to noble and other transition metals, Ni seems to be the most promising choice because it is cheaper, and comparatively more active and selective. However Ni based catalysts have a tendency to deactivate due to sintering, coking, phase transformation and loss of active component [6], [7]. In the literature, numerous metallic oxides such as Al 2 O 3 , SiO 2 , MgO, TiO 2 , ZrO 2 and CeO 2 have been investigated as supports for DRM [8].…”

Section: Introductionmentioning

confidence: 99%

Syngas Production from Dry Reforming of Methane over Nano Ni Polyol Catalysts

Naeem¹,

Al‐Fatesh²,

Khan³

et al. 2013

IJCEA

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Abstract-Dry reforming of methane (DRM) is an environment friendly process since it utilizes two major greenhouse gases (CH 4 and CO 2 ) to produce valuable syngas. Polyol process was adopted to prepare nano supported (Al 2 O 3 , ZrO 2 and CeO 2 ) Ni based nano catalysts for DRM reaction. All catalysts were prepared in ethylene glycol medium with polyvinylpyrrolidone as a nucleation-protective agent. The main objective of this study was to develop a suitable catalyst, for syngas production, which possessed high activity, stability and minimum coking rate during DRM. The catalytic activities of the prepared catalysts were evaluated in the temperature range 500-800°C. The obtained results revealed that catalytic performance depends on the nature of support. Amongst all tested catalysts, Ni-Zr Pol showed highest activity (87.2%) and stability (%D.F= -0.46). On the other hand Ni-Al Pol catalyst exhibited acceptable activity (84.8%) with minimum coking rate (0.015 g/g cat .h) while Ni-Ce Pol showed smallest activity (83.2%) with large amount of coke deposition (0.025 g/g cat .h).Index Terms-CO 2 /CH 4 reforming, nano-Ni, nano support, polyol method, activity.

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Coke formation during CO2 reforming of CH4 over alumina-supported nickel catalysts

Cited by 121 publications

References 25 publications

Effects of catalytic bed position on hydrogen production by methane decomposition

Effects of catalytic bed position on hydrogen production by methane decomposition

Ni catalysts with different promoters supported on zeolite for dry reforming of methane

Syngas Production from Dry Reforming of Methane over Nano Ni Polyol Catalysts

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