Methods for making a supported chromium catalyst are disclosed, and can comprise contacting a silica-coated alumina containing at least 30 wt. % silica with a chromium-containing compound in a liquid, drying, and calcining in an oxidizing atmosphere at a peak temperature of at least 650° C. to form the supported chromium catalyst. The supported chromium catalyst can contain from 0.01 to 20 wt. % chromium, and typically can have a pore volume from 0.5 to 2 mL/g and a BET surface area from 275 to 550 m.sup.2/g. The supported chromium catalyst subsequently can be used to polymerize olefins to produce, for example, ethylene-based homopolymers and copolymers having high molecular weights and broad molecular weight distributions.

A porous carbon-based metal catalyst, a preparation method and application thereof are provided. The preparation method includes: successively performing activation, surface corrosion, nitrogen-doping treatment and graphitization treatment on washed micro-grade porous carbon, then performing sensitization treatment, and subsequently carrying out loading, reduction and other treatments of catalytic metal, so as to finally obtain the porous carbon-based metal catalyst. The porous carbon-based metal catalyst provided by the present application has excellent catalytic performance, is especially suitable for producing hydrogen by efficiently catalytically decomposing ammonia borane, is not prone to inactivation, and is easy to regenerate after inactivation. Meanwhile, the preparation method is environmental-friendly, is suitable for large-scale production and has a wide application prospect in the fields such as hydrogen fuel batteries.

Method for preparing a catalyst comprising a bimetallic active phase made of nickel and copper, and a support comprising a refractory oxide, comprising the following steps: a step of bringing the support into contact with a solution containing a nickel precursor is carried out; a step of bringing the support into contact with a solution containing a copper precursor is carried out; a step of drying the catalyst precursor at a temperature lower than 250° C. is carried out; the catalyst precursor obtained is supplied to a hydrogenation reactor, and a step of reduction by bringing said precursor into contact with a reducing gas at a temperature lower than 200° C. for a period greater than or equal to 5 minutes and less than 2 hours is carried out.

A method for producing a hydrogen rich gas from a heavy hydrocarbon feed comprising the steps of introducing the hydrocarbon feed to a reactor, the reactor comprising a low temperature reforming catalyst, the low temperature reforming catalyst comprising an amount of praseodymium, 12 wt % nickel, and an aluminum oxide component, contacting the low temperature reforming catalyst with the hydrocarbon feed in the reactor, wherein the reactor operates at a temperature between 500° C. and 600° C., wherein the reactor operates at a pressure between 3 bar and 40 bar, and producing the hydrogen rich gas over the low temperature reforming catalyst, wherein the hydrogen rich gas comprises hydrogen.

The invention relates to a catalyst system suitable for hydrogenating aromatic nitro compounds (I) to form the corresponding aromatic amines (II), the catalyst system containing, as essential constituents: a component A selected from the group consisting of silicon carbide, corundum (alpha-Al.sub.2O.sub.3) and slightly porous to non-porous zirconium oxide (ZrO.sub.2); and a component B, containing B1—a carrier substance selected from the group consisting of silicon dioxide, gamma-, delta- or theta-aluminum oxide Al.sub.2O.sub.3, titanium dioxide, zirconium dioxide and graphite, B2—a metal or a plurality of metals selected from the group consisting of copper, nickel, palladium, platinum and cobalt, and optionally B3—an additional metal selected from the group consisting of at least one metal selected from main group I, main group II, main group IV and sub-groups II, V, VI and VIII of the periodic table of the elements, the proportion of component A being in the range of 5 to 60 wt %, in relation to the total weight of the catalyst system, and the aromatic nitro compounds (I) being those of the general formula R—(NO.sub.2).sub.n, (I), and the aromatic amines (II) being those of the general formula R—(NH.sub.2).sub.n, (II), and the moieties R and indices n in formulas (I) and (II) having the following meaning: R is a substituted or unsubstituted aromatic C.sub.6-C.sub.10 moiety and n is an integer from 1 to 5.

The present invention provides a catalyst comprising at least one first metal selected from the group consisting of Groups 3 to 6 of the periodic table, wherein an amount of Bronsted acid sites of the catalyst is 1.8 μmol/g or less.

A monolithic catalyst used for a carbon dioxide hydrogenation reaction and a method for preparing the same. The catalyst comprises a carrier, a coating, and active components. The carrier is a honeycomb ceramic. The coating and the active components are separately applied to honeycomb ceramic hole walls from inside to outside. Moreover, each of the honeycomb ceramic holes is divided into an upper segment and a lower segment, and different active components are separately loaded on the two segments. The method for preparing the monolithic catalyst comprises first applying a coating to a honeycomb ceramic by means of impregnation to obtain a coating-containing carrier, and then applying active components to an upper segment and a lower segment of the coating-containing carrier successively by means of impregnation to obtain the monolithic catalyst.

A method for preparing a catalyst with a bimetallic active phase made of nickel and copper, and a support comprising a refractory oxide, wherein the method involves: a) placing the support in contact with at least one solution containing a nickel precursor; b) placing the support in contact with a solution containing a copper precursor; wherein a) and b) are carried out separately in any order; c) drying the catalyst precursor at the end of a) and b), or b) and a), at a temperature less than 250° C.; and d) supplying the catalyst precursor obtained at the end of c), into a hydrogenation reactor, and carrying out a reduction step by placing the precursor in contact with a reducing gas at a temperature of less than 200° C. and for a period greater than or equal to 5 minutes and less than 2 hours.

A hydrotreating catalyst comprising an active phase containing at least one group VIB metal and at least one group VIII metal, and a porous support containing alumina and at least one spinel MAl.sub.2O.sub.4 where M is chosen from nickel and cobalt, characterized in that: the molar ratio (r1) between said group VIII metal and said group VIB metal of the active phase is between 1.0 and 3.0 mol/mol; the molar ratio (r2) between said metal M of the porous support and said group VIII metal of the active phase is between 0.3 and 0.7 mol/mol; the molar ratio (r3) between the sum of the contents of the metal M and of the group VIII metal relative to the content of group VIB metal is between 2.2 and 3.0 mol/mol.

A catalyst for converting ethane to monoaromatic hydrocarbons including: a zeolite; cesium oxide, wherein cesium of the cesium oxide is present in an amount of 0.01 to 0.5 weight percent, preferably 0.01 to 0.1 weight percent, more preferably 0.03 to 0.07 weight percent, based on a total weight of the catalyst; platinum oxide, wherein platinum of the platinum oxide is present in an amount of 0.01 to 1 weight percent, preferably 0.01 to 0.5 weight percent, more preferably 0.01 to 0.05 weight percent, based on a total weight of the catalyst; and gallium oxide, wherein gallium of the gallium oxide is present in an amount of 0.01 to 1 weight percent, preferably 0.03 to 0.5 weight percent, more preferably 0.05 to 0.2 weight percent, based on a total weight of the catalyst; wherein the monoaromatic hydrocarbons include benzene, toluene, xylene, or a combination including at least one of the foregoing.