The invention is related to a carbon supported catalyst comprising a carbon-comprising support with a BET surface area in a range from 400 m.sup.2/g to 2000 m.sup.2/g, a modifier comprising at least one mixed metal oxide, comprising niobium and titanium, and/or a mixture, comprising niobium oxide and titanium oxide, a catalytically active metal compound, wherein the catalytically active metal compound is platinum or an alloy comprising platinum and a second metal or an intermetallic compound comprising platinum and a second metal, the second metal being selected from the group consisting of cobalt, nickel, chromium, copper, palladium, gold, ruthenium, scandium, yttrium, lanthanum, niobium, iron, vanadium and titanium.

The invention is further related to a process for preparing the carbon supported catalyst.

The invention is related to a carbon supported catalyst comprising a carbon-comprising support with a BET surface area in a range from 400 m.sup.2/g to 2000 m.sup.2/g, a modifier comprising at least one mixed metal oxide, comprising niobium and titanium, and/or a mixture, comprising niobium oxide and titanium oxide, a catalytically active metal compound, wherein the catalytically active metal compound is platinum or an alloy comprising platinum and a second metal or an intermetallic compound comprising platinum and a second metal, the second metal being selected from the group consisting of cobalt, nickel, chromium, copper, palladium, gold, ruthenium, scandium, yttrium, lanthanum, niobium, iron, vanadium and titanium.

The invention is further related to a process for preparing the carbon supported catalyst.

The invention relates to a catalyst which comprises: a) a mixed metal oxide of molybdenum, vanadium, niobium and optionally tellurium; and b) ceria particles having a crystallite size greater than 15 nanometers (nm); wherein the amount of the ceria particles, based on the total amount of the catalyst, is of from 1 to 60 wt. %. Further, the invention relates to a process for preparing a catalyst, which comprises mixing a mixed metal oxide of molybdenum, vanadium, niobium and optionally tellurium with ceria particles having a crystallite size greater than 15 nanometers (nm), wherein the amount of the ceria particles, based on the total amount of the catalyst, is of from 1 to 60 wt. %. Still further, the invention relates to an alkane oxidative dehydrogenation and/or alkene oxidation process wherein such catalyst is used.

The invention relates to a catalyst which comprises: a) a mixed metal oxide of molybdenum, vanadium, niobium and optionally tellurium; and b) ceria particles having a crystallite size greater than 15 nanometers (nm); wherein the amount of the ceria particles, based on the total amount of the catalyst, is of from 1 to 60 wt. %. Further, the invention relates to a process for preparing a catalyst, which comprises mixing a mixed metal oxide of molybdenum, vanadium, niobium and optionally tellurium with ceria particles having a crystallite size greater than 15 nanometers (nm), wherein the amount of the ceria particles, based on the total amount of the catalyst, is of from 1 to 60 wt. %. Still further, the invention relates to an alkane oxidative dehydrogenation and/or alkene oxidation process wherein such catalyst is used.

Multi-metallic bulk catalysts and methods for synthesizing the same are provided. The multi-metallic bulk catalysts contain nickel, molybdenum tungsten, niobium, and optionally, titanium and/or copper. The catalysts are useful for hydroprocessing, particularly hydrodesulfurization and hydrodenitrogenation, of hydrocarbon feedstocks.

Multi-metallic bulk catalysts and methods for synthesizing the same are provided. The multi-metallic bulk catalysts contain nickel, molybdenum tungsten, niobium, and optionally, titanium and/or copper. The catalysts are useful for hydroprocessing, particularly hydrodesulfurization and hydrodenitrogenation, of hydrocarbon feedstocks.

Methods and a reactor system for producing acetic acid in a selective oxidation (SO) reactor are provided. An example method includes providing a fresh feed stream to the SO reactor, wherein the fresh feed stream includes a light hydrocarbon feed stream, a carbon dioxide feed stream, and a steam feed stream. Acetic acid is formed in the SO reactor. An acetic acid product stream is separated from a reactor effluent stream in a scrubber. A recycle gas stream is obtained from the scrubber. At least a portion of the recycle gas stream is combined into the fresh feed stream to the SO reactor.

A catalyst for oxidative dehydrogenation (ODH) of ethane with an empirical formula Mo—V—Te—Nb—Pd—O produced using a process comprising impregnation of the Pd component on the surface of the catalyst following a calcination step using a Pd compound free of halogens. The resulting catalyst can be used in both diluted and undiluted ODH processes and shows higher than expected activity without any loss of selectivity.

A catalyst for oxidative dehydrogenation (ODH) of ethane with an empirical formula Mo—V—Te—Nb—Pd—O produced using a process comprising impregnation of the Pd component on the surface of the catalyst following a calcination step using a Pd compound free of halogens. The resulting catalyst can be used in both diluted and undiluted ODH processes and shows higher than expected activity without any loss of selectivity.

A method includes supplying a gas containing acrolein to a fixed bed reactor including a reaction tube to produce acrylic acid by vapor phase catalytic oxidation of acrolein. The reaction tube is packed with catalysts having different activities in such a way that catalyst layers are formed in a tube axis direction. A catalyst X having the highest activity among the catalysts contained in all the catalyst layers is placed in the whole or a part of a section up to 30% of a length of all the catalyst layers from a rearmost portion on a gas outlet side toward a gas inlet side. A catalytically active component x in the catalyst X has Mo, V, and optionally Cu. When Cu is included, its amount is 0.8 mol or less per 12 mol of Mo. A specific surface area of the catalytically active component x is 15-40 m.sup.2/g.