A process for producing hydrogen sulfide from hydrogen and elemental sulfur, comprising: bringing the sulfur into contact with a solid catalyst comprising at least one metal, chosen from metals from groups VIB and VIII of the Periodic Table of the Elements, in metal sulfide form, at a temperature ranging from 120 C. to 160 C.; circulating the mixture of sulfur and catalyst resulting from step (a) in a reaction zone, in which said mixture is brought into contact with hydrogen, the reaction zone having a temperature at the inlet point of the catalyst of greater than or equal to 150 C. and a temperature at the outlet point of the catalyst of less than or equal to 300 C., and a pressure of less than or equal to 3 bar; separating the catalyst and the gaseous effluents containing hydrogen sulfide; and recycling the catalyst to the step of bringing.

A catalyst for a selective conversion of hydrocarbons. The catalyst includes a first component selected from the group consisting of Group VIII noble metals and mixtures thereof, a second component selected from the group consisting of alkali metals or alkaline-earth metals and mixtures thereof, and a third component selected from the group consisting of tin, germanium, lead, indium, gallium, thallium and mixtures thereof. The catalyst is a support formed as a spherical catalyst particle with an average pore diameter between 200 to 350 Angstroms, a porosity of at least 75% and an apparent bulk density between 0.60 and 0.3 g/cc. Also, a process of using such a catalyst for a selective hydrocarbon conversion reaction and a process for regenerating such a catalyst by removing coke from same.

In a method for producing an aliphatic carboxylic acid ester by reacting an aliphatic carboxylic acid having from 1 to 5 carbon atoms and an olefin having from 2 to 4 carbon atoms in a gas phase by use of a solid acid catalyst, a solid acid catalyst in which a heteropolyacid or a salt thereof is supported on a silica carrier obtainable by kneading fumed silica obtained by a combustion method, silica gel obtained by a gel method, and colloidal silica obtained by a sol-gel method or a water glass method, molding the resulting kneaded product, and calcining the resulting molded body, is used.

The present invention relates to a method for manufacturing a catalyst for synthesizing a fatty acid methyl or ethyl ester and a method for manufacturing a fatty acid methyl or ethyl ester using the catalyst. It provides a method for manufacturing a solid catalyst by mixing the oxides of manganese as active catalytic material and the soda lime glass as carrier wherein the content of the oxides of manganese is in the range of 0.1 w % to 70 w %, molding the mixture to spherical or cylindrical shape and sintering the molded catalyst. It also provides a method for manufacturing fatty acid methyl or ethyl ester with high purity by reacting fatty acid or a mixture of oil and fatty acid with methanol or ethanol by placing the solid catalyst in the reactor.

Oxidative dehydrogenation catalysts for converting lower paraffins to alkenes such as ethane to ethylene when prepared as an agglomeration, for example extruded with supports chosen from slurries of TiO.sub.2, ZrO.sub.2 Al.sub.2O.sub.3, AlO(OH) and mixtures thereof have a lower temperature at which 25% conversion is obtained.

A photocatalyst filter is provided. The photocatalyst filter includes: a base in which an internal space is formed. The internal space is permeable to fluid, and a plurality of photocatalyst beads are provided in the internal space, wherein a surface of the internal space is reflective.

Presented is a selective hydrogenation catalyst and a method of making the catalyst. The catalyst comprises a carrier containing bi-metallic nanoparticles. The nanoparticles comprise a silver component and a palladium component. The catalyst is made by incorporating an aqueous dispersion of the bi-metallic nanoparticles onto a catalyst carrier followed by drying and calcining the carrier having incorporated therein the dispersion. The catalyst is used in the selective hydrogenation of highly unsaturated hydrocarbons contained olefin product streams.

A zeolite fluid catalytic cracking catalyst is provided that passivates nickel and vanadium during catalytic cracking. The zeolite fluid catalytic cracking catalyst includes Y-faujasite crystallized in-situ from a metakaolin-containing calcined microsphere. The zeolite fluid catalytic cracking catalyst further includes an alumina-containing matrix obtained by calcination of a dispersible crystalline boehmite and a kaolin contained in the metakaolin-containing calcined microsphere, where the dispersible crystalline boehmite has a crystallite size of less than 500 . Also provided are a method of reducing contaminant coke and hydrogen yields and a method of catalytic cracking of heavy hydrocarbon feed stocks.

A catalyst comprises an active phase constituted by palladium, and a porous support comprising at least one refractory oxide selected from the group constituted by silica, alumina and silica-alumina, in which: the palladium content in the catalyst is in the range 0.0025% to 1% by weight with respect to the total weight of catalyst; at least 80% by weight of the palladium is distributed in a crust at the periphery of the porous support, the thickness of said crust being in the range 25 to 450 m; the specific surface area of the porous support is in the range 70 to 160 m.sup.2/g; the metallic dispersion D of the palladium is less than 20%.

A method for treating reverse osmosis concentrated water, comprises adding precipitant and oxidant to reverse osmosis concentrated water for treatment, filtering to obtain clear liquid, and adding catalyst for water treatment to clear liquid for catalytic oxidation to obtain a first-stage treated water. Optionally, the liquid may be subjected after catalytic oxidation to an adsorption treatment; performing reverse osmosis treatment on first-stage treated water to obtain second-stage reverse osmosis product water and second-stage reverse osmosis concentrated water; and adding oxidant to second-stage reverse osmosis concentrated water for oxidation treatment to obtain directly discharged effluent water. The obtaining of effluent water may further comprise subjecting liquid after oxidation treatment to adsorption treatment. The above method can recycle 75-85 wt % of water, and operates easily. Thereby, improvement to overall utilization rate of water, and treatment of little remaining water is met to effluent standard for reduction of environmental pollution and economic investment.