A composite catalyst includes a carrier and noble metal particles supported by the carrier, wherein the carrier is a nitrogen-doped porous carbon composite material having a plurality of passages. The nitrogen-doped porous carbon composite material can include a nitrogen-doped porous carbon material and a plurality of metal oxide particles. The plurality of metal oxide particles can be uniformly distributed in the nitrogen-doped porous carbon material. The plurality of metal oxide particles can be partially exposed through the plurality of passages. The noble metal particles can be tightly combined with the exposed metal oxide particles to achieve recombination. And the noble metal particles can be at least one of Pd metal particles, Pt metal particles, Ru metal particles, Rh metal particles, Ir metal particles, Au metal particles, or a combination thereof.

Catalysts are described. The catalysts comprise a dried extrudate of a mixture of -alumina and at least one mixed metal oxide or mixed metal hydroxide, the -alumina having a BET surface area of 150 m.sup.2/g to 275 m.sup.2/g. Processes of making the hydroprocessing catalysts, and hydroprocessing processes using the catalysts are also described.

A catalyst in a calcined state has a specific surface area of 20-50 m.sup.2/g of catalyst, and a specific surface area of nickel metal after reduction of the catalyst of 8 to 11 m.sup.2/g, wherein the average particle size of nickel metal is 3-8 nm, the dispersion of the particles is 10-16%, and the content of nickel is 5-15 wt. % based on the weight of calcined catalyst. A support has a specific surface area of 40-120 m.sup.2/g with a pore volume of the support of 0.2-0.4 cm.sup.3/g, wherein the support is selected from a mixture of zirconium oxide and cerium oxide or magnesium oxide, cerium oxide and the ballast being zirconium oxide. The catalyst further contains a promoter selected from the group consisting of palladium and ruthenium, in an amount of from 0.01 to 0.5 wt. %. The catalyst is prepared by co-precipitation with ammonium hydroxide from a solution containing nickel, cerium and zirconium precursors and distilled water or from a solution containing nickel, cerium, zirconium, and magnesium precursors and distilled water, and having a pH of 8.0-9.0. The process is carried out under agitation at a temperature of 40-45 C. for 1-2 hours, followed by filtration, drying at a temperature of 100-110 C. for 6-8 hours, and calcining at a temperature of 400-650 C. for 4-6 hours. The invention provides a high average conversion of natural/associated gas of at least 90% in an autothermal reforming reaction of natural or associated gas, and a high synthesis gas output of at least 7000 m.sup.3/m.sup.3.sub.cat.Math.h.

A nickel diatomaceous earth catalyst having a weight loss rate measured by hydrogen-TG at 400 to 600 C. of 0.05 to 2.0%.

The invention relates to an improved catalyst based on a tableted molded catalyst body, containing a metal-containing mixture, containing copper, zinc, and aluminum, with calcium aluminate as a binder material with a weight fraction of calcium aluminate in the range of 1.0% to 30.0%, for synthesizing methanol from synthesis gas. The invention further relates to the production of the catalyst and to the use of the catalyst in the synthesis of methanol from synthesis gas.

The invention relates to a catalyst for the methanation of carbon monoxide and/or carbon dioxide, said catalyst comprising aluminium oxide, an Ni-active substance and Mn and being characterised in that the molar Ni/Mn ratio in the catalyst is 3.0 to 10.0, preferably 4.0 to 9.0 and especially preferably 5.5 to 6.5. The catalyst is characterised by an increased activity with high selectivity and stability. The invention also relates to a method for producing a catalyst according to the invention, comprising the steps: a) co-precipitation from a solution containing Al, Ni and Mn in dissolved form in order to obtain a precipitate; b) isolation of the precipitate from step a); c) drying the isolated precipitate from step b); and d) calcination of the dried precipitate from step c).

A method for activating a catalyst is described comprising the steps of: (i) installing a reduced and passivated catalyst containing crystallites of a catalytic metal comprising nickel, cobalt or iron in elemental form encapsulated by a layer comprising an oxide of the catalytic metal in a reactor, such as a steam methane reforming reactor, in which it is to be used, and (ii) heating the reduced and passivated catalyst in the reactor under a vacuum or an inert gas to a temperature in the range (T.sub.T?X) to (T.sub.T+Y), where T.sub.T is the Tammann temperature of the catalytic metal in elemental form in degrees Centigrade, X is 400 and Y is 200, to form a catalytically active surface on the catalyst without requiring the application of a reducing gas.

Processes for converting a hydrocarbon reactant into an alcohol compound and/or a carbonyl compound are disclosed in which the hydrocarbon reactant and either a supported chromium (VI) catalyst or a supported chromium (II) catalyst are contacted, optionally with UV-visible light irradiation, followed by exposure to an oxidizing atmosphere and then hydrolysis to form a reaction product containing the alcohol compound and/or the carbonyl compound. The presence of oxygen significant increases the amount of alcohol/carbonyl product formed, as well as the formation of oxygenated dimers and trimers of certain hydrocarbon reactants.

The present disclosure discloses: a bifunctional Cu/CeZr-based catalyst suitable for reacting a ketone and alcohol which are contained in a fermented product of biomass and have a low molecular weight, and converting same into an aliphatic ketone having an increased carbon number; a method for producing the catalyst; and a method for producing a fuel-range aliphatic ketone, such as gasoline and air fuel, by using the catalyst.

A process to synthesize a catalyst performing Water-Gas shift reaction at a temperature more than 300 C. using a precursor having general formula [(Cu, Zn).sub.1-x (Al, M).sub.x (OH).sub.2].sup.x+ (A.sup.n.sub.x/n).kH.sub.2O with M=Al, La, Ga or In, A=CO.sub.3, 0.33<x<0.5, 1<n<3.