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.

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.

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.

A method of converting one or more alkanes to one or more alkenes that includes a) providing a first stream containing one or more alkanes and oxygen to an oxidative dehydrogenation reactor; b) converting at least a portion of the one or more alkanes to one or more alkenes in the oxidative dehydrogenation reactor to provide a second stream exiting the oxidative dehydrogenation reactor containing one or more alkanes, one or more alkenes, oxygen, carbon monoxide and optionally acetylene; and c) providing the second stream to a second reactor containing a catalyst that includes a group 11 metal to convert a least a portion of the carbon monoxide to carbon dioxide and reacting the acetylene.

A method of converting one or more alkanes to one or more alkenes that includes a) providing a first stream containing one or more alkanes and oxygen to an oxidative dehydrogenation reactor; b) converting at least a portion of the one or more alkanes to one or more alkenes in the oxidative dehydrogenation reactor to provide a second stream exiting the oxidative dehydrogenation reactor containing one or more alkanes, one or more alkenes, oxygen, carbon monoxide and optionally acetylene; and c) providing the second stream to a second reactor containing a catalyst that includes a group 11 metal to convert a least a portion of the carbon monoxide to carbon dioxide and reacting the acetylene.

Provided is a method of preparing a pure M1 phase MoVTeNb-oxide catalyst with a high specific surface area, including S1) mixing and dissolving a molybdenum-containing compound, a vanadium-containing compound, a tellurium-containing compound, a niobium-containing compound and a protective agent to obtain a precursor-protective agent mixed solution, in which the protective agent is a surfactant or a small molecule organic acid and a salt thereof; S2) subjecting the precursor-protective agent mixed solution to a hydrothermal reaction to separate out a solid; S3) calcining the solid in an air atmosphere, followed by calcining the same in an inert gas, and then performing a hydrogen peroxide purification treatment to obtain a pure M1 phase MoVTeNb-oxide catalyst. This catalyst exhibits an excellent conversion rate, selectivity, space time yield and stability in the oxidative dehydrogenation reaction of ethane for preparing ethylene.