Effect of potassium content in the activity of K-promoted Ni/Al2O3 catalysts for the dry reforming of methane

Juan-Juan, J.; Román-Martı́nez, M.C.; Illán-Gómez, M.J.

doi:10.1016/j.apcata.2005.11.006

Cited by 220 publications

(102 citation statements)

References 45 publications

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“…Although the highest coke amount was found on the Ni/ZrS sample, no loss of activity was observed for this sample, since carbon was deposited in the form of nanofibers ( Figure 6). This type of coke does not embed metal particles [36], keeping the metal surface accessible for reactants, which, together with the high surface area of the silica support to accommodate large amounts of coke, has been described to have a minor effect on catalyst deactivation [37,38]. However, high coke formation is not desirable, because it would probably result in reactor plugging.…”

Section: Characterization Of Ce-or Zr-modified Ni/sio 2 Catalystsmentioning

confidence: 99%

Effect of Ce and Zr Addition to Ni/SiO2 Catalysts for Hydrogen Production through Ethanol Steam Reforming

et al. 2015

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A series of Ni/Ce x Zr 1−x O 2 /SiO 2 catalysts with different Zr/Ce mass ratios were prepared by incipient wetness impregnation. Ni/SiO 2 , Ni/CeO 2 and Ni/ZrO 2 were also prepared as reference materials to compare. Catalysts' performances were tested in ethanol steam reforming for hydrogen production and characterized by XRD, H 2 -temperature programmed reduction (TPR), NH 3 -temperature programmed desorption (TPD), TEM, ICP-AES and N 2 -sorption measurements. The Ni/SiO 2 catalyst led to a higher hydrogen selectivity than Ni/CeO 2 and Ni/ZrO 2 , but it could not maintain complete ethanol conversion due to deactivation. The incorporation of Ce or Zr prior to Ni on the silica support resulted in catalysts with better performance for steam reforming, keeping complete ethanol conversion over time. When both Zr and Ce were incorporated into the catalyst, Ce x Zr 1−x O 2 solid solution was formed, as confirmed by XRD analyses. TPR results revealed stronger Ni-support interaction in the Ce x Zr 1−x O 2 -modified catalysts than in Ni/SiO 2 one, which can be attributed to an increase of the dispersion of Ni species. All of the Ni/Ce x Zr 1−x O 2 /SiO 2 catalysts exhibited good catalytic activity and stability after 8 h of time on stream at 600• C . The best catalytic performance in terms of hydrogen selectivity was achieved when the Zr/Ce mass ratio was three.

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Section: Characterization Of Ce-or Zr-modified Ni/sio 2 Catalystsmentioning

confidence: 99%

Effect of Ce and Zr Addition to Ni/SiO2 Catalysts for Hydrogen Production through Ethanol Steam Reforming

et al. 2015

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“…19,[29][30][31][32] Reduction peaks at higher temperatures in the 620-770 K and 773-1073 K range, are attributed to the reduction of well dispersed NiO, interacting strongly with the support, and in the range 1000-1273 K to the reduction of the NiAl 2 O 4 spinel. 29,31,32 In the case of the bimetallic catalysts prepared from nickel chloride salts (PdNiCl and NiClPd) a well defined TPR peak corresponding to bulk NiO in the temperature range 623-773 K can be seen. In the case of the bimetallic catalysts prepared from nitrate salt (PdNiN and NiNPd) a bigger presence of NiO interacting strongly with the support is seen.…”

Section: Catalysts Characterizationmentioning

confidence: 99%

MORE ACTIVE AND SULFUR RESISTANT BIMETALLIC Pd-NI CATALYSTS

Betti¹,

Carrara²,

Badano³

et al. 2017

Quim. Nova

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The influence of the kind of metal precursor and the sequence of impregnation on the properties of Pd-Ni catalysts was evaluated during the test reaction of selective hydrogenation of styrene to ethylbenzene by means of physicochemical characterization. The focus was put on the final hydrogenating activity and the resistance to deactivation by sulfided compounds (thiophene). The used techniques of characterization were ICP, XPS, XDR, TPR, CO chemisorption and TEM. XPS results indicated the presence of different Pd species: Pd δ-, Pd 0 and Pd δ+ . In the case of the Ni containing catalysts, Ni 0 and NiO species were also detected. These palladium and nickel species would be responsables of the variation of activity and sulfurresistance of the catalysts. NiClPd catalysts had a higher resistance to deactivation by sulfur poisoning. This was associated to a higher concentration of Pd η+ Cl x O y species that would prevent the adsorption of thiophene by both steric and electronic effects. It could also be due to the lower concentration of Pd 0 and Ni 0 on these catalysts, as compared to those shown by the PdNiCl catalysts. Both the Pd 0 and Ni 0 species are more prone to poisoning because of their higher electronic availability.

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“…Another important reaction is the decomposition of CO fuel into CO 2 and C [Eq. (10) 21) revealed that 70% of CH 4 and 77% of CO 2 of the mixed gas of CH 4 /CO 2 = 1/1 were changed to a H 2 CO fuel at 700°C. This reaction was accompanied by the carbon deposition of 280 mgC/1 g of catalyst after 6 h of reforming.…”

Section: Solid Oxide Fuel Cells Using Biogasmentioning

confidence: 99%

Reforming of biogas using electrochemical cell

Hirata

Matsunaga

Sameshima

2011

J. Ceram. Soc. Japan

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This review reports the recent research results of solid oxide fuel cells using biogas (typical composition, 60% CH 4 40% CO 2 ), reforming of CH 4 with CO 2 (CH 4 + CO 2 ¼ 2CO + 2H 2 ) and shift reaction of CO with H 2 O (CO + H 2 O ¼ H 2 + CO 2 ). Solid oxide fuel cells using dense yttria-stabilized zirconia and gadolinium-doped ceria electrolytes were operated with biogas containing CH 4 of 763 vol % at 630875°C. A maximum power density of 20160 mW/cm 2 was measured and this value was 1/101/3 of that for the cells with a H 2 fuel. The reforming of CH 4 with CO 2 proceeds over a Ni-based catalyst at 700900°C to produce a H 2 CO fuel. The carbon deposition due to the pyrolysis of CH 4 as a parallel reaction is suppressed by addition of second phase such as K 2 O or Ru to Ni catalyst. Electrochemical reforming of CH 4 with CO 2 using a porous Gd-doped ceria (GDC) cell is an attractive process to produce a H 2 CO fuel at 400800°C. The supplied CO 2 is changed to CO and O 2¹ ions by the reaction with electrons at the cathode (CO 2 + 2e . Furthermore, shift reaction of reformed gas with H 2 O vapor proceeded to produce a H 2 fuel using a porous GDC electrochemical cell with Co 2 O 3 catalyst at 400500°C.

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Effect of potassium content in the activity of K-promoted Ni/Al2O3 catalysts for the dry reforming of methane

Cited by 220 publications

References 45 publications

Effect of Ce and Zr Addition to Ni/SiO2 Catalysts for Hydrogen Production through Ethanol Steam Reforming

Effect of Ce and Zr Addition to Ni/SiO2 Catalysts for Hydrogen Production through Ethanol Steam Reforming

MORE ACTIVE AND SULFUR RESISTANT BIMETALLIC Pd-NI CATALYSTS

Reforming of biogas using electrochemical cell

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