Nickel based catalyst structures are described herein that include a plurality of metal oxides formed as crystalline phases within the catalyst structures. Each metal oxide of a catalyst structure includes nickel and/or aluminum, where one or more metal oxides includes a nickel aluminum oxide, and the one or more nickel aluminum oxides is greater than 50% by weight of the catalyst structure. The catalyst structures further have surface areas of at least 13 m.sup.2/g. The catalyst structures are resistant to high concentrations of sulfur and are effective in reforming operations for converting methane and other light hydrocarbons to hydrogen and one or more other components. For example, the catalyst structures are effective in coal and biomass gasification systems for the forming and cleanup of synthetic gas.

High temperature metal monoliths for use in reverse flow reactors and methods of preparing said monoliths are provided.

Processes for transforming an inert metal component into an active metal catalyst are provided. Apparatus and methods using active metal catalyst prepared according the process described herein are also provided.

The present disclosure provides a catalyst for a water gas shift reaction at middle temperature, the catalyst comprising a catalytically active component containing 40 to 80 mol % of copper (Cu), 15 to 50 mol % of zinc (Zn), and 1 to 13 mol % of aluminum (Al), relative to all metals of the catalyst, wherein an aluminum-rich layer is present in a surface layer of a particle of the catalyst. Furthermore, the present disclosure provides a preparation method of the catalyst, and a hydrogen preparation method using the same.

This invention is directed to novel mixed transition metal iron (II/III) catalysts for the extraction of oxygen from CO.sub.2 and the selective reaction with organic compounds.

This invention is directed to novel mixed transition metal iron (II/III) catalysts for the extraction of oxygen from CO.sub.2 and the selective reaction with organic compounds.

To provide a catalyst, which is formed from a perovskite oxide, for thermochemical fuel production, and a method of producing fuel using thermochemical fuel production that is capable of allowing a fuel to be produced in a thermochemical manner. Provided is a catalyst for thermochemical fuel production, which is used for producing the fuel from thermal energy by using a two-step thermochemical cycle of a first temperature and a second temperature that is equal to or lower than the first temperature, wherein the catalyst is formed from a perovskite oxide having a compositional formula of AXO.sub.3?? (provided that, 0???1). Here, A represents one or more of a rare-earth element (excluding Ce), an alkaline earth metal element, and an alkali metal element, X represents one or more of a transition metal element and a metalloid element, and O represents oxygen.

The invention relates to CeO.sub.2 and La.sub.2O.sub.3 for catalyzing Fe.sub.2O.sub.3Al.sub.2O.sub.3 based chemical-looping reforming of CH.sub.4 with CO.sub.2 (CL-DRM). The reaction performance of all the composite oxygen carriers was evaluated in a fixed-bed reactor at atmospheric pressure condition. The influencing factors, including temperature and time-on-stream (TOS) were investigated. The characteristics of the oxygen carriers were checked with Brunauer-Emmett-Teller (BET) analysis and X-ray diffraction (XRD). The reducibility of the composite materials was elucidated with temperature-programmed reduction by CH.sub.4 (CH.sub.4-TPR). Preliminary experimental observations suggest that the simultaneous presence of CeO.sub.2 and La.sub.2O.sub.3 can not only enhance the reactivity of Fe.sub.2O.sub.3Al.sub.2O.sub.3 toward CH.sub.4 oxidation and its oxygen releasing rate for fast reaction kinetics, but also improve the reactivity of its reduced form toward CO.sub.2 splitting.

The invention relates to CeO.sub.2 and La.sub.2O.sub.3 for catalyzing Fe.sub.2O.sub.3Al.sub.2O.sub.3 based chemical-looping reforming of CH.sub.4 with CO.sub.2 (CL-DRM). The reaction performance of all the composite oxygen carriers was evaluated in a fixed-bed reactor at atmospheric pressure condition. The influencing factors, including temperature and time-on-stream (TOS) were investigated. The characteristics of the oxygen carriers were checked with Brunauer-Emmett-Teller (BET) analysis and X-ray diffraction (XRD). The reducibility of the composite materials was elucidated with temperature-programmed reduction by CH.sub.4 (CH.sub.4-TPR). Preliminary experimental observations suggest that the simultaneous presence of CeO.sub.2 and La.sub.2O.sub.3 can not only enhance the reactivity of Fe.sub.2O.sub.3Al.sub.2O.sub.3 toward CH.sub.4 oxidation and its oxygen releasing rate for fast reaction kinetics, but also improve the reactivity of its reduced form toward CO.sub.2 splitting.

A hydrogen purifier (100) includes: a shift conversion catalyst (5a) which reduces, through a shift reaction, carbon monoxide contained in a hydrogen-containing gas; and a methanation catalyst (6a) which reduces, through a methanation reaction, carbon monoxide contained in the hydrogen-containing gas that has passed through the shift conversion catalyst (5a). The shift conversion catalyst (5a) and the methanation catalyst (6a) are heat exchangeable with each other via a first partition wall (8), and a flow direction of the hydrogen-containing gas that passes through the shift conversion catalyst (5a) is opposite to a flow direction of the hydrogen-containing gas that passes through the methanation catalyst (6a).