A membrane reactor includes a catalyst layer, a separation membrane, and a buffer layer. The catalyst layer contains a catalyst for promoting a conversion reaction from a feed gas containing hydrogen and carbon oxide to a liquid fuel. The separation membrane is permeable to water vapor which is a byproduct of the conversion reaction. The buffer layer is disposed between the separation membrane and the catalyst layer, and permeable to the water vapor toward the separation membrane.

Disclosed herein are reactors comprising: a) a first mixing zone, b) a first reaction zone, c) a first cooling zone, d) a first H.sub.2O separation zone, e) a second mixing zone, f) a second reaction zone, g) a second cooling zone, and h) a second H.sub.2O separation zone, wherein the first mixing zone is in fluid communication with the first reaction zone, wherein the first reaction zone is in fluid communication with the first cooling zone, wherein the first cooling zone is in fluid communication with the first H.sub.2O separation zone, wherein the first H.sub.2O separation zone is in fluid communication with the second mixing zone, wherein the second mixing zone is in fluid communication with the second reaction zone, wherein the second reaction zone is in fluid communication with the second cooling zone, and wherein the second cooling zone is in fluid communication with the second H.sub.2O separation zone.

A catalytic reactor for industrial-scale hydrogenation processes is described. The catalytic reactor contains a catalytic fixed bed that comprises a support structure and a catalyst. During operation of the reaction in the catalytic reactor, the fixed bed is filled with reaction medium to at least 85% by volume. A very high contact area of the catalyst with the reaction medium is at the same time provided. The support structure is formed from material webs having a thickness of 5 to 25 μm, with a crosslinking density of at least 3 mm.sup.−3 present. The support structure consists of metals selected from elements of groups 8, 6 and 11 of the periodic table of the elements and mixtures thereof.

A catalytic reactor for industrial-scale hydrogenation processes is described. The catalytic reactor contains a catalytic fixed bed that comprises a support structure and a catalyst. During operation of the reaction in the catalytic reactor, the fixed bed is filled with reaction medium to at least 85% by volume. A very high contact area of the catalyst with the reaction medium is at the same time provided. The support structure is formed from material webs having a thickness of 5 to 25 μm, with a crosslinking density of at least 3 mm.sup.−3 present. The support structure consists of metals selected from elements of groups 8, 6 and 11 of the periodic table of the elements and mixtures thereof.

A continuous flow catalytic reactor, an assembling method therefor and an application thereof includes a reaction vessel, a filler packaged in the reaction vessel and a charged catalytic component; the charged catalytic component is fixed to the filler under an action of a direct-current electric field. The continuous flow catalytic reactor may be applied to continuous flow reactions such as a monosaccharide epimerization reaction. A monosaccharide epimerization reaction method includes: providing the continuous flow catalytic reactor; electrically connecting the continuous flow catalytic reactor with a direct-current power supply, thereby to forming the direct-current electric field by electrically connecting the continuous flow catalytic reactor with the direct-current power supply; and heating a reactor container to a target temperature, and inputting a monosaccharide solution from a liquid flow inlet of the reaction vessel and then collecting a solution containing a target product from a liquid flow outlet of the reaction vessel.

A continuous flow catalytic reactor, an assembling method therefor and an application thereof includes a reaction vessel, a filler packaged in the reaction vessel and a charged catalytic component; the charged catalytic component is fixed to the filler under an action of a direct-current electric field. The continuous flow catalytic reactor may be applied to continuous flow reactions such as a monosaccharide epimerization reaction. A monosaccharide epimerization reaction method includes: providing the continuous flow catalytic reactor; electrically connecting the continuous flow catalytic reactor with a direct-current power supply, thereby to forming the direct-current electric field by electrically connecting the continuous flow catalytic reactor with the direct-current power supply; and heating a reactor container to a target temperature, and inputting a monosaccharide solution from a liquid flow inlet of the reaction vessel and then collecting a solution containing a target product from a liquid flow outlet of the reaction vessel.

The present invention relates to a removable basket for a catalytic reactor comprising a horizontal base (1) and a plurality of vertical side walls (2) and/or at least one ellipsoidal side wall, and a plurality of vertical chimneys (3, 4) that are open at their lower (5) and upper (6) ends, each chimney comprising a lower part (7) comprising the lower end fastened to the base and extending between the side walls, in which a first chimney comprises an upper part (8) extending above the side walls, and the upper part of the first chimney is suitable for being inserted into a lower part of a chimney of another removable basket. The present invention also relates to a filtration and distribution device comprising said removable basket, a reactor comprising said device, and a hydrotreating and/or hydrocracking process using said reactor.

The present invention relates to a removable basket for a catalytic reactor comprising a horizontal base (1) and a plurality of vertical side walls (2) and/or at least one ellipsoidal side wall, and a plurality of vertical chimneys (3, 4) that are open at their lower (5) and upper (6) ends, each chimney comprising a lower part (7) comprising the lower end fastened to the base and extending between the side walls, in which a first chimney comprises an upper part (8) extending above the side walls, and the upper part of the first chimney is suitable for being inserted into a lower part of a chimney of another removable basket. The present invention also relates to a filtration and distribution device comprising said removable basket, a reactor comprising said device, and a hydrotreating and/or hydrocracking process using said reactor.

Disclosed herein are reactors comprising: a) a first mixing zone, b) a first reaction zone, c) a first cooling zone, d) a first H.sub.2O separation zone, e) a second mixing zone, f) a second reaction zone, g) a second cooling zone, and h) a second H.sub.2O separation zone, wherein the first mixing zone is in fluid communication with the first reaction zone, wherein the first reaction zone is in fluid communication with the first cooling zone, wherein the first cooling zone is in fluid communication with the first H.sub.2O separation zone, wherein the first H.sub.2O separation zone is in fluid communication with the second mixing zone, wherein the second mixing zone is in fluid communication with the second reaction zone, wherein the second reaction zone is in fluid communication with the second cooling zone, and wherein the second cooling zone is in fluid communication with the second H.sub.2O separation zone.

A system used for converting multiple fuel feedstocks may include three reactors. The reactor system combination can be so chosen that one of the reactors completely or partially converts the fuel while the other generates the gaseous product required by utilizing the gaseous product from the second reactor. The metal-oxide composition and the reactor flow-patterns can be manipulated to provide the desired product. A method for optimizing the system efficiency where a pressurized gaseous fuel or a pressurized utility is used for applications downstream can be used to any system processing fuels and metal-oxide.