A process of preparing a solid catalyst component for the production of polypropylene includes a) dissolving a halide-containing magnesium compound in a mixture, the mixture including an epoxy compound, an organic phosphorus compound, and a hydrocarbon solvent to form a homogenous solution; b) treating the homogenous solution with an organosilicon compound during or after the dissolving step; c) treating the homogenous solution with a first titanium compound in the presence of a first non-phthalate electron donor, and an organosilicon compound, to form a solid precipitate; and d) treating the solid precipitate with a second titanium compound in the presence of a second non-phthalate electron donor to form the solid catalyst component, where the process is free of carboxylic acids and anhydrides.

A process of preparing a solid catalyst component for the production of polypropylene includes a) dissolving a halide-containing magnesium compound in a mixture, the mixture including an epoxy compound, an organic phosphorus compound, and a hydrocarbon solvent to form a homogenous solution; b) treating the homogenous solution with an organosilicon compound during or after the dissolving step; c) treating the homogenous solution with a first titanium compound in the presence of a first non-phthalate electron donor, and an organosilicon compound, to form a solid precipitate; and d) treating the solid precipitate with a second titanium compound in the presence of a second non-phthalate electron donor to form the solid catalyst component, where the process is free of carboxylic acids and anhydrides.

A process for producing a hydrogen-rich gas stream from a liquid hydrocarbon stream, the process comprising the steps of introducing the liquid hydrocarbon stream to a dual catalytic zone, the liquid hydrocarbon stream comprises liquid hydrocarbons selected from the group consisting of liquid petroleum gas (LPG), light naphtha, heavy naphtha, gasoline, kerosene, diesel, and combinations of the same, the dual catalytic zone comprises: a combustion zone comprising a seven component catalyst, and a steam reforming zone, the steam reforming zone comprising a steam reforming catalyst; introducing steam to the dual catalytic zone, introducing an oxygen-rich gas to the dual catalytic zone; contacting the liquid hydrocarbon stream, steam, and oxygen-rich gas with the seven component catalyst to produce a combustion zone fluid; and contacting the combustion zone fluid with the steam reforming catalyst to produce the hydrogen-rich gas stream, wherein the hydrogen-rich gas stream comprises hydrogen.

A process for producing a hydrogen-rich gas stream from a liquid hydrocarbon stream, the process comprising the steps of introducing the liquid hydrocarbon stream to a dual catalytic zone, the liquid hydrocarbon stream comprises liquid hydrocarbons selected from the group consisting of liquid petroleum gas (LPG), light naphtha, heavy naphtha, gasoline, kerosene, diesel, and combinations of the same, the dual catalytic zone comprises: a combustion zone comprising a seven component catalyst, and a steam reforming zone, the steam reforming zone comprising a steam reforming catalyst; introducing steam to the dual catalytic zone, introducing an oxygen-rich gas to the dual catalytic zone; contacting the liquid hydrocarbon stream, steam, and oxygen-rich gas with the seven component catalyst to produce a combustion zone fluid; and contacting the combustion zone fluid with the steam reforming catalyst to produce the hydrogen-rich gas stream, wherein the hydrogen-rich gas stream comprises hydrogen.

A method for preparing an active catalyst for high-efficiency denitration is disclosed. The method includes: a catalyst raw material is charged into a denitration reactor, NH.sub.3 and an inert gas are introduced and then heating is performed, and the temperature is held and then natural cooling is performed, thereby obtaining the catalyst. The active catalyst can greatly improve the denitration activity in low temperature range, and can not only improve the denitration efficiency under the condition without SO.sub.2 and H.sub.2O, but also can improve the denitration efficiency under the condition with both SO.sub.2 and H.sub.2O. The service life of the catalyst is prolonged under the premise of not changing the existing catalyst preparation process, and the economic benefit is significant. The denitration efficiency of a powder catalyst can be increased by 25%, and the denitration efficiency of a honeycombed catalyst or a corrugated catalyst can be increased by 20%.

A method for preparing an active catalyst for high-efficiency denitration is disclosed. The method includes: a catalyst raw material is charged into a denitration reactor, NH.sub.3 and an inert gas are introduced and then heating is performed, and the temperature is held and then natural cooling is performed, thereby obtaining the catalyst. The active catalyst can greatly improve the denitration activity in low temperature range, and can not only improve the denitration efficiency under the condition without SO.sub.2 and H.sub.2O, but also can improve the denitration efficiency under the condition with both SO.sub.2 and H.sub.2O. The service life of the catalyst is prolonged under the premise of not changing the existing catalyst preparation process, and the economic benefit is significant. The denitration efficiency of a powder catalyst can be increased by 25%, and the denitration efficiency of a honeycombed catalyst or a corrugated catalyst can be increased by 20%.

A powdered catalyst material on a titanium oxide basis. The powdered catalyst material includes a combined content of at least 90 wt.-% of a hydrated titanium oxide having the general formula TiO.sub.(2-x)(OH).sub.2x, with 0<x≤1, (calculated as TiO.sub.2), and a silicon dioxide and hydrated precursors of the silicon dioxide (calculated as SiO.sub.2). A weight ratio of TiO.sub.2/SiO.sub.2, determined for TiO.sub.2 and SiO.sub.2 respectively, is at least 3 and less than 30. The wt.-% is based on a total weight of the catalyst material after the catalyst material has been dried at 105° C. for at least 2 hours. The powdered catalyst material has a specific surface area of >300 m.sup.2/g and an isoelectric point of from 4.0 to 7.0.

A powdered catalyst material on a titanium oxide basis. The powdered catalyst material includes a combined content of at least 90 wt.-% of a hydrated titanium oxide having the general formula TiO.sub.(2-x)(OH).sub.2x, with 0<x≤1, (calculated as TiO.sub.2), and a silicon dioxide and hydrated precursors of the silicon dioxide (calculated as SiO.sub.2). A weight ratio of TiO.sub.2/SiO.sub.2, determined for TiO.sub.2 and SiO.sub.2 respectively, is at least 3 and less than 30. The wt.-% is based on a total weight of the catalyst material after the catalyst material has been dried at 105° C. for at least 2 hours. The powdered catalyst material has a specific surface area of >300 m.sup.2/g and an isoelectric point of from 4.0 to 7.0.

Provided herein are catalyst materials and processes for processing hydrocarbons. For example, doped ceria-supported metal catalysts are provided exhibiting good activity and stability for commercially relevant dry reforming of methane as well as mixed hydrocarbon feedstocks under process conditions including low temperature and long term operation. Useful doped ceria-supported metal catalysts include nickel dispersed over Ti-doped ceria.

Provided herein are catalyst materials and processes for processing hydrocarbons. For example, doped ceria-supported metal catalysts are provided exhibiting good activity and stability for commercially relevant dry reforming of methane as well as mixed hydrocarbon feedstocks under process conditions including low temperature and long term operation. Useful doped ceria-supported metal catalysts include nickel dispersed over Ti-doped ceria.