The present invention refers to a catalytic system comprising a transition metal compound on a solid carrier, wherein the content of the transition metal compound on the surface of the solid carrier is from 0.1 to 30 wt.-%, based on the dry weight of the solid carrier. Furthermore, the present invention refers to a method for manufacturing the catalytic system, the use of the inventive catalytic system in a chemical reaction, the use of a solid carrier loaded with a transition metal compound as a catalyst and to granules mouldings or extrudates comprising the catalytic system.

The present invention refers to a catalytic system comprising a transition metal compound on a solid carrier, wherein the content of the transition metal compound on the surface of the solid carrier is from 0.1 to 30 wt.-%, based on the dry weight of the solid carrier. Furthermore, the present invention refers to a method for manufacturing the catalytic system, the use of the inventive catalytic system in a chemical reaction, the use of a solid carrier loaded with a transition metal compound as a catalyst and to granules mouldings or extrudates comprising the catalytic system.

Oxidative dehydrogenation (ODH) of alkanes to alkenes, e.g., propane to propylene, may use solid phase oxygen in VO.sub.x based mixed oxide catalysts. Beyond catalysis, the metal oxide species provide lattice oxygen. The catalysts can be prepared by depositing vanadium oxide(s) on θ-Al.sub.2O.sub.3 mixed with various alkaline earth metal oxide support, e.g., CaO, MgO, BaO, etc. Surface area, acidity, and reduction properties of the catalyst systems can be modified by the support. The catalysts may allow multistage reduction of VO.sub.x, indicating different VO.sub.x species. Vanadium on θ-Al.sub.2O.sub.3/CaO can suppress COx species, while vanadium on θ-Al.sub.2O.sub.3/BaO can yield at least ca. 49% olefins.

Oxidative dehydrogenation (ODH) of alkanes to alkenes, e.g., propane to propylene, may use solid phase oxygen in VO.sub.x based mixed oxide catalysts. Beyond catalysis, the metal oxide species provide lattice oxygen. The catalysts can be prepared by depositing vanadium oxide(s) on θ-Al.sub.2O.sub.3 mixed with various alkaline earth metal oxide support, e.g., CaO, MgO, BaO, etc. Surface area, acidity, and reduction properties of the catalyst systems can be modified by the support. The catalysts may allow multistage reduction of VO.sub.x, indicating different VO.sub.x species. Vanadium on θ-Al.sub.2O.sub.3/CaO can suppress COx species, while vanadium on θ-Al.sub.2O.sub.3/BaO can yield at least ca. 49% olefins.

The present invention relates to a process of hydrogenating an alkyne selectively to an alkene by hydrogen using a hydrogenation catalyst which is palladium supported on a carrier in the presence of an additive mixture of an organic phosphorus compound (AP) and an organic sulphur compound (AS).

The present disclosure relates to a hydrothermally stable catalyst composition. The hydrothermally stable supported catalyst composition comprises K.sub.2CO.sub.3 impregnated on an amorphous silica-alumina support. The weight ratio of silica to alumina in the support is in the range of 0.1 to 1.5. The amount of K.sub.2CO.sub.3 is in the range of 5 wt % to 60 wt % with respect to the total catalyst composition. The catalyst composition is characterized by a pore volume in the range of 0.1 cc/g to 0.9 cc/g, a surface area in the range of 40 m.sup.2/g to 250 m.sup.2/g and an attrition index in the range of 2% to 8%. The present disclosure also relates to a process for preparing the catalyst composition. The catalyst composition provides improved hydrothermal stability, attrition resistance, high pore volume and surface area for gasifying carbonaceous feed at low temperature, as compared to a conventional catalyst composition.

The present disclosure relates to a hydrothermally stable catalyst composition. The hydrothermally stable supported catalyst composition comprises K.sub.2CO.sub.3 impregnated on an amorphous silica-alumina support. The weight ratio of silica to alumina in the support is in the range of 0.1 to 1.5. The amount of K.sub.2CO.sub.3 is in the range of 5 wt % to 60 wt % with respect to the total catalyst composition. The catalyst composition is characterized by a pore volume in the range of 0.1 cc/g to 0.9 cc/g, a surface area in the range of 40 m.sup.2/g to 250 m.sup.2/g and an attrition index in the range of 2% to 8%. The present disclosure also relates to a process for preparing the catalyst composition. The catalyst composition provides improved hydrothermal stability, attrition resistance, high pore volume and surface area for gasifying carbonaceous feed at low temperature, as compared to a conventional catalyst composition.

This document relates to oxidative dehydrogenation catalyst materials that include molybdenum, vanadium, beryllium, oxygen, and optionally aluminum.

An organic material decomposition catalyst that contains BaCO.sub.3 and a perovskite composite oxide represented by A.sub.xB.sub.yM.sub.zO.sub.w, wherein A contains Ba, B contains Zr, and M denotes Mn. A peak intensity I(BaCO.sub.3(111)) of BaCO.sub.3(111) of the BaCO.sub.3 and a peak intensity I(BaZrO.sub.3(110)) of a perovskite composite oxide A.sub.xB.sub.yM.sub.zO.sub.w(110) of the perovskite composite oxide represented by A.sub.xB.sub.yM.sub.zO.sub.w, each determined by X-ray diffractometry of the organic material decomposition catalyst, have a ratio I(BaCO.sub.3(111))/I(BaZrO.sub.3(110)) in a range of 0.022 to 0.052. In another aspect, in the perovskite composite oxide represented by A.sub.xB.sub.yM.sub.zO.sub.w, 1.01≤x≤1.06, 0.1≤z≤0.125, and y+z=1 are satisfied, w denotes a positive value that satisfies electroneutrality, and the organic material decomposition catalyst has a specific surface area in the range of 12.3 to 16.9 m.sup.2/g.

A synthesis gas production system for producing CO and H.sub.2 by electrolyzing an aqueous solution containing CO.sub.2 includes: an electrolysis device including an anode chamber and a cathode chamber separated by a separator membrane; a cathode-side circulation line connected to the cathode chamber to circulate a cathode solution containing CO.sub.2; a catalyst supply device provided in the cathode-side circulation line to supply a CO production catalyst to the cathode solution; and a gas composition detection device configured to measure a ratio between CO and H.sub.2 in a production gas produced in the cathode chamber. At least one of control of a supply amount of the CO production catalyst by the catalyst supply device and control of a voltage applied between the anode and the cathode by the electrolysis device is performed to make a ratio of H.sub.2 to CO in the production gas be within a predetermined target range.