Processes for upgrading a hydrocarbon. The process can include (I) contacting a hydrocarbon-containing feed with a catalyst that can include a Group 8-10 element or a compound thereof disposed on a support to effect conversion of the hydrocarbon-containing feed to produce a coked catalyst and an effluent. The process can also include (II) contacting the coked catalyst with an oxidant to effect combustion the coke to produce a regenerated catalyst. The process can also include (IIa) contacting the regenerated catalyst with a reducing gas to produce a regenerated and reduced catalyst. The process can also include (III) contacting an additional quantity of the hydrocarbon-containing feed with the regenerated and reduced catalyst. A cycle time from the contacting the hydrocarbon-containing feed with the catalyst in step (I) to the contacting the additional hydrocarbon-containing feed with the regenerated and reduced catalyst in step (III) can be 1 hours.

The disclosure relates to a process for enriching a synthesis gas in hydrogen by contacting said synthesis gas with a water gas shift catalyst, the synthesis gas being a CO-rich synthesis gas including at least 15 vol % CO and at least 1 ppmv sulfur, and the water gas shift catalyst including Zn, Al, optionally Cu, and an alkali metal or alkali metal compound; the water gas shift catalyst is free of chromium (Cr) and iron (Fe), and has a pore volume, as determined by mercury intrusion, of 240 ml/kg or higher.

Described is a catalyst obtained by supporting magnesium and cerium on activated alumina, firing same to immobilize the metals, and then impregnating same with palladium and performing reduction thereon, and is applied, when hydrogen peroxide is prepared by means of an anthraquinone process, to operation solution regeneration or hydrogenation, and thus an efficient regeneration conversion rate or synthesis yield is achieved.

The present disclosure relates to an improved water gas shift catalyst, in particular an improved high temperature shift catalyst and process using the catalyst. The water gas shift catalyst includes Zn, Al, optionally Cu, and an alkali metal or alkali metal compound, wherein the content of alkali metal, preferably K, is in the range 1-6 wt %, such as 1-5 wt % or 2.5-5 wt % based on the weight of oxidized catalyst, and wherein the water gas shift catalyst has a pore volume, as determined by mercury intrusion, of 240 ml/kg or higher, such as 250 ml/kg or higher. A process for enriching a synthesis gas in hydrogen by contacting the synthesis gas in a water gas shift reactor with the water gas shift catalyst.

A catalyst includes a support, where the support includes an external surface, about 60 wt % to about 99 wt % silica, and about 1.0 wt % to about 5.0 wt % alumina. A catalytic layer is disposed within the support adjacent to the external surface, where the catalytic layer further includes Pd, Au, and potassium acetate (KOAc). In the catalyst, (a) the KOAc is from about 60 kg/m.sup.3 to about 150 kg/m.sup.3 of the catalyst; or (b) the catalytic layer has an average thickness from about 50 m to about 150 m; or (c) both (a) and (b). The catalyst also possesses a Brunauer-Emmett-Teller surface area of about 130 m.sup.2/g to about 300 m.sup.2/g and a geometric surface area per packed bed volume from about 550 m.sup.2/m.sup.3 to about 1500 m.sup.2/m.sup.3. The catalyst is highly active for the synthesis of vinyl acetate monomer and exhibits a high selectivity for vinyl acetate monomer.

A honeycomb structure includes a porous partition wall defining a plurality of cells, wherein the plurality of cells include a first cell and a second cell, on the partition wall disposed to surround the at least one first cell, a protrusion is each provided with, the first protrusion and the second protrusion are each disposed to at least partially overlap with each other on extended lines in extending directions of the respective protrusions, and an inter-protrusion length (X) of a distal end of the first protrusion and a distal end of the second protrusion is equal to or more than 10% and equal to or less than 70% with respect to a mutual distance (W) from the one part to the other part on the partition walls facing each other.

A unique process and catalyst is described that operates efficiently for the direct production of a high cetane diesel type fuel or diesel type blending stock from stochiometric mixtures of hydrogen and carbon monoxide. This invention allows for, but is not limited to, the economical and efficient production high quality diesel type fuels from small or distributed fuel production plants that have an annual production capacity of less than 10,000 barrels of product per day, by eliminating traditional wax upgrading processes. This catalytic process is ideal for distributed diesel fuel production plants such as gas to liquids production and other applications that require optimized economics based on supporting distributed feedstock resources.

A metal porous body having a three-dimensional network structure, includes: a framework forming the three-dimensional network structure; and a coating layer having fine pores and coating the framework, the three-dimensional network structure including a rib and a node connecting a plurality of ribs, the framework including an alkali-resistant first metal, the fine pores having an average fine pore diameter of 10 nm or more and 1 m or less, the coating layer including an alkali-resistant second metal and optionally including an alkali-soluble metal, the alkali-soluble metal being contained at a proportion of 0% by mass or more and 30% by mass or less with reference to a total mass of the framework and the coating layer.

A method for producing a catalyst or catalyst precursor is described including: applying a slurry of a particulate catalyst compound in a carrier fluid to an additive layer manufactured support structure to form a slurry-impregnated support, and drying and optionally calcining the slurry-impregnated support to form a catalyst or catalyst precursor. The mean particle size (D50) of the particulate catalyst compound in the slurry is in the range 1-50 m and the support structure has a porosity 0.02 ml/g.

A catalyst, methods of making, and process of dehydrogenating paraffins utilizing the catalyst. The catalyst includes at least 20 mass % Zn, a catalyst support and a catalyst stabilizer. The catalyst is further characterizable by physical properties such as activity parameter measured under specified conditions. The catalyst may also be disposed on a porous support in an attrition-resistant form and used in a fluidized bed reactor.