An integrated hydrotreating and hydrocracking process includes contacting a hydrocarbon oil stream with a hydrogen stream and a hydrotreating catalyst in a moving-bed hydrotreating reactor, thereby producing a hydrocarbon product stream and a spent hydrotreating catalyst; contacting the hydrocarbon product stream with a second hydrogen stream and a hydrocracking catalyst in a hydrocracking reactor, thereby producing a hydrocracked hydrocarbon product stream; processing the spent hydrotreating catalyst to produce regenerated hydrotreating catalyst; and recycling the regenerated hydrotreating catalyst to the moving-bed hydrotreating reactor.

Methods for processing paraffinic naphtha include contacting a paraffinic naphtha feedstock with a catalyst system in a dehydrogenation reactor. The catalyst system includes a framework-substituted ultra-stable Y (USY)-type zeolite to produce a dehydrogenated product stream. The catalyst system includes a framework-substituted ultra-stable Y (USY)-type zeolite. The framework-substituted USY-type zeolite has a modified USY framework. The modified USY framework includes a USY aluminosilicate framework modified by substituting a portion of framework aluminum atoms of the USY aluminosilicate framework with substitution atoms independently selected from the group consisting of titanium atoms, zirconium atoms, hafnium atoms, and combinations thereof. A dehydrogenation catalyst for dehydrogenating a paraffinic naphtha includes the framework-substituted ultra-stable Y (USY)-type zeolite.

A modified Y-type molecular sieve contains 0.5-2 wt. % of Na.sub.2O based on the total amount of the modified Y-type molecular sieve. In the modified Y-type molecular sieve, the ratio between the total acid amount measured by pyridine and infrared spectrometry and total acid amount measured by n-butyl pyridine and infrared spectrometry is 1-1.2. The total acid amount measured by pyridine and infrared spectrometry of the modified Y-type molecular sieve is 0.1-1.2 mmol/g. The acid center sites of the molecular sieve of the modified Y-type molecular sieve are distributed in the large pore channels. The molecular sieve is used in the hydrocracking reaction process of a wax oil.

A method for producing a hydrocracking catalyst includes preparing a framework substituted Y-type zeolite, preparing a binder, co-mulling the framework substituted Y-type zeolite, the binder, and one or more hydrogenative metal components to form a catalyst precursor, and calcining the catalyst precursor to generate the hydrocracking catalyst. The framework substituted Y-type zeolite is prepared by calcining a Y-type zeolite at 500° C. to 700° C. to form a calcined Y-type zeolite. Further, the framework substituted Y-type zeolite is prepared by forming a suspension containing the calcined Y-type zeolite, the suspension having a liquid to solid mass ratio of 5 to 15, adding acid to adjust the pH of the suspension to less than 2.0, adding and mixing one or more of a zirconium compound, a hafnium compound, or a titanium compound to the suspension, and neutralizing the pH of the suspension to obtain the framework substituted Y-type zeolite.

Disclosed is a hydrocracking catalyst, a preparation method and an application thereof. The catalyst comprises a carrier, silicon dioxide and active ingredients loaded on the carrier, wherein the carrier comprises Y molecular sieves and SAPO-34 molecular sieves. The preparation method of the hydrocracking catalyst comprises the following steps: (1) mixing materials comprising Y molecular sieves and SAPO-34 molecular sieves, and then subjecting the mixture to molding, drying and calcinating to obtain a carrier; (2) introducing silane and the active ingredients into the carrier prepared in the step (1), subsequently performing the drying and calcinating to prepare the hydrocracking catalyst. The catalyst prepared with the method can be used for hydrocracking reaction, thereby significantly increase yield of jet fuel.

A process for the upgrading of hydrocarbon streams, i.e., processing any hydrocarbon feed streams rich in benzene and sulphur compounds. The process for simultaneous hydrodesulfurization and benzene conversion to higher alkylated aromatic molecules (C.sub.7 to C.sub.10 aromatics), without need of prior treatment like distillation, or sulfur removal. The hydrocarbon feed streams are processed over sulfided metal catalyst impregnated on acid support simultaneously desulfurizes and alkylates the benzene molecules.

Provided is a novel catalyst comprised of an alumina, silica-alumina, and a zeolite containing base impregnated with Ni, Mo, and W. In one embodiment, the trimetallic catalyst is layered with a conventional hydrocracking pretreat catalyst to provide a catalyst combination useful in hydrotreating a feed to a hydrocracking stage.

The present invention relates to a process for the direct conversion of cellulose into glycols by using a non noble metal supported zeolite catalyst selected from Al—Ni—W/HY, Al—Ni—W/NaY and Al—Ni—W/Na-ZSM-5, wherein the ratio of the metal in the catalyst is in the range of 15%-12%-30% to 0%-3%-5%.

A method for converting an alcohol to a hydrocarbon, the method comprising contacting said alcohol with a metal-loaded zeolite catalyst at a temperature of at least 100° C. and up to 550° C., wherein said alcohol can be produced by a fermentation process, said metal is a positively-charged metal ion, and said metal-loaded zeolite catalyst is catalytically active for converting said alcohol to said hydrocarbon.

Embodiments of the present disclosure are directed to hydrocracking catalysts and methods of making same. The hydrocracking catalyst comprises a platinum encapsulated zeolite having a crystallinity greater than 20% determined by X-ray powder diffraction analysis.