An apparatus and method for producing hydrocarbons including aromatic hydrocarbons and lower olefins including propylene from CH.sub.4 and CO.sub.2 through CO and H.sub.2 with high activity and high selectivity. The apparatus is provided with: a synthetic gas production unit to which a gas containing CH.sub.4 and CO.sub.2 is supplied from a first supply unit, and which generates a synthetic gas containing CO and H.sub.2 while heating a first catalyst structure; a production unit to which the synthetic gas is supplied and which generates hydrocarbons including aromatic hydrocarbons having 6-10 carbon atoms and lower olefins including propylene while heating a second catalyst structure; and a detection unit which detects propylene and the aromatic hydrocarbons discharged from the production unit, in which the first catalyst structure includes first supports having a porous structure and a first metal fine particle in the first supports, the first supports have a first channels, the first metal fine particle is present in the first channels, the second catalyst structure includes second supports having a porous structure and a second metal fine particle in the second supports, the second supports have a second channels, and a portion of the second channels have an average inner diameter of 0.95 nm or less.

Embodiments of the disclosure include processes for ring-opening of hydrocarbon species comprising aromatic and cycloparaffinic rings in hydrocarbon feeds to produce ring-opened products. In particular, the process comprises contacting hydrocarbon species comprising aromatic and cycloparaffinic rings with hydrogen in the presence of a ring-opening catalyst comprising a noble metal on a low-acidity crystalline material containing external pockets to facilitate ring-opening of the hydrocarbon species comprising aromatic and cycloparaffinic rings. The processes are useful in the transformation of polynuclear aromatic hydrocarbons (PAHs) to ring-opened products.

A hydrocracking process for converting a petroleum feed to lower boiling products. The process comprises hydrotreating a petroleum feed in a pre-treating zone in the presence of hydrogen to produce a hydrotreated effluent stream comprising a liquid product. At least a portion of the hydrotreated effluent stream is then passed to an MMS catalyst zone, and then to a hydrocracking zone. In one embodiment, the MMS catalyst zone comprises a self-supported multi-metallic catalyst prepared from a precursor in the oxide or hydroxide form. The percentage work of the hydrotreating in the pre-treating zone is maintained at a level of at least 56%.

Nickel and copper catalyst, and an alumina support: nickel distributed both in the core of and on a crust at the periphery of the support, crust thickness being 2% to 15% of catalyst diameter; nickel density ratio between the crust and the core greater than 3; crust contains more than 25% by weight of nickel element relative to total weight of nickel in the catalyst; mole ratio between nickel and copper is 0.5 to 5, at least one portion of nickel and copper is a nickel-copper alloy; nickel content in the nickel-copper alloy is 0.5% to 15% by weight of nickel element relative to total weight of the catalyst; size of the nickel particles in the catalyst is less than 7 nm.

The invention relates to a process for producing energy products, notably fuel, by catalytic cracking of a hydrocarbon-based solid material without coke formation, in which a cracking dispersion (40) is heated, said dispersion comprising: a solid material (1) in divided form containing at least one hydrocarbon-based compound; a liquid (30) which is inert with respect to catalytic cracking;
so that the cracking dispersion (40) reaches a temperature suitable for allowing catalytic cracking of at least one hydrocarbon-based compound;
characterized in that the cracking temperature is reached by mixing an amount of cracking dispersion (40) and an amount of inert liquid (30) brought to a temperature above the cracking temperature, such that the mixture formed reaches a temperature above the cracking temperature and below the temperature for formation of coke, dioxin and furan. The invention also relates to a device for performing such a process.

Disclosed are processes for conversion of a feedstock comprising C.sub.8+ aromatic hydrocarbons to lighter aromatic products in which the feedstock and optionally hydrogen are contacted in the presence of the catalyst composition under conversion conditions effective to dealkylate and transalkylate said C.sub.8+ aromatic hydrocarbons to produce said lighter aromatic products comprising benzene, toluene and xylene. The catalyst composition comprises a zeolite, a first metal, and a second metal, and is treated with a source of sulfur and/or a source of steam.

The invention relates to a process for adding an organic compound to a porous solid wherein the porous solid and the organic compound in the liquid state are brought together simultaneously, without physical contact between the solid and the organic compound in the liquid state, at a temperature below the boiling point of the organic compound and under pressure and time conditions such that a fraction of said organic compound is transferred gaseously to the porous solid.

Methods for producing ethylene using nanowires as heterogeneous catalysts are provided. The method includes, for example, an oxidative coupling of methane catalyzed by nanowires to provide ethylene.

Isobutanol may be converted into predominantly C.sub.12+ olefin oligomers under specified conditions. Such methods may comprise: contacting a feed comprising isobutanol with a zeolite solid acid catalyst having a MWW framework under conditions effective to convert the isobutanol into a product comprising C.sub.4n olefin oligomers, wherein n is an integer having a value of two or greater and about 80 wt. % or greater of the C.sub.4n olefin oligomers are larger than C.sub.8.

A regeneration method for catalytic cracking reaction, the method is applied in a catalytic reaction process of petroleum hydrocarbon materials, and the method comprises: feeding the regenerated and semi-regenerated catalyst from a regenerator separately into different positions of a reactor for reaction. A part of the semi-regenerated catalyst is firstly processed in a purification cooler for removing carried nitrogen, oxygen, carbon dioxide and impurity gases before being fed into the reactor. Spent catalyst or the purified and cooled semi-regenerated catalyst is fed into a catalyst mixing section of the reactor for controlling the temperature of the catalyst being contact with the oil material to be gasified, thereby achieving a three stage cycle of the catalyst in the reactor and a three stage control for the reaction outlets of the oil material gasification zone and the cracking reaction zone and the catalyst taking part in the reaction.