The present application pertains to family of new crystalline molecular sieves designated SSZ-92. Molecular sieve SSZ-92 is structurally similar to sieves falling within the ZSM-48 family of molecular sieves and is characterized as having magnesium.

A hydroisomerization catalyst comprising a molecular sieve belonging to the ZSM-48 family of zeolites; an inorganic oxide support; one or more first modifiers selected from Groups 8 to 10; and one or more second modifiers selected from the group consisting of calcium (Ca), chromium (Cr), magnesium (Mg), lanthanum (La), barium (Ba), praseodymium (Pr), strontium (Sr), potassium (K) and neodymium (Nd). The molecular sieve comprises: a silicon oxide to aluminum oxide mole ratio of about 40 to about 220; at least about 70% polytype 6 of the total ZSM-48-type material present in the product; and an additional EUO-type molecular sieve phase in an amount of between about 0 and about 7.0 percent by weight of the total product. The molecular sieve has a morphology characterized as polycrystalline aggregates comprising crystallites collectively having an average aspect ratio of between about 1 and about 8.

Systems and methods are provided for oligomerization of olefins to distillate boiling range products while also recycling naphtha boiling range olefins as part of the feed. By performing the olefin oligomerization while also recycling naphtha boiling range olefins, it has been discovered that the resulting distillate boiling range products can have an unexpected improvement in diesel combustion quality, such as an unexpected improvement in cetane rating. In order to manage coke formation and maintain consistent activity profile for the oligomerization catalyst, the reaction can be performed in a moving bed reactor. Additional temperature control can be maintained by the recycling of the naphtha boiling range portions of the oligomerization product back to the reactor.

Systems and methods are provided for oligomerization of olefins to distillate boiling range products while also recycling naphtha boiling range olefins as part of the feed. By performing the olefin oligomerization while also recycling naphtha boiling range olefins, it has been discovered that the resulting distillate boiling range products can have an unexpected improvement in diesel combustion quality, such as an unexpected improvement in cetane rating. In order to manage coke formation and maintain consistent activity profile for the oligomerization catalyst, the reaction can be performed in a moving bed reactor. Additional temperature control can be maintained by the recycling of the naphtha boiling range portions of the oligomerization product back to the reactor.

Systems and methods are provided for upgrading of methane and/or small alkanes to distillate boiling range hydrocarbons. The upgrading is performed using a reaction system where various types of integration are provided from downstream reaction stages to upstream reaction stages. Such integration can include recycle of various reaction products as well as thermal integration. Having a reaction system that begins with reforming of hydrocarbons and finishes with production of distillate can enable unexpected synergies between downstream reaction stages and upstream reaction stages.

Processes are provided for preparing molecular sieves for use as catalysts. The process involves preparing a synthesis mixture for the molecular sieve wherein the synthesis mixture includes a morphology modifier which may be selected from cationic surfactants having a single quaternary ammonium group comprising at least one hydrocarbyl group having at least 12 carbon atoms, nonionic surfactants, anionic surfactants, sugars, and combinations thereof.

Methods are provided for performing selective hydrodesulfurization on a naphtha boiling range stream naphtha boiling range portion of a feed. It has been unexpectedly discovered that hydrodesulfurization with improved octane retention can be performed by using a catalyst that comprises CoMo supported on a catalyst support that includes a zeotype framework. By using a catalyst support including a zeotype framework, an unexpectedly high amount of octane in the naphtha boiling range portion of the hydrodesulfurized effluent is maintained.

A family of new crystalline molecular sieves designated SSZ-91 is disclosed, as are methods for making SSZ-91 and uses for SSZ-91. Molecular sieve SSZ-91 is structurally similar to sieves falling within the ZSM-48 family of molecular sieves, and is characterized as: (1) having a low degree of faulting, (2) a low aspect ratio that inhibits hydrocracking as compared to conventional ZSM-48 materials having an aspect ratio of greater than 8, and (3) is substantially phase pure.

A catalyst system for dewaxing of a hydrocarbon feedstock comprising a mixture of a first dewaxing catalyst composition and a second dewaxing catalyst composition, wherein the first dewaxing catalyst composition is a ZSM-12 zeolite based catalyst composition and the second dewaxing catalyst composition is a EU-2 and/or ZSM-48 zeolite based catalyst composition, and wherein a concentration gradient of the mixture is achieved within a single catalyst bed, such that the concentration of the first dewaxing catalyst is decreasing and the concentration of the second dewaxing catalyst is increasing through the catalyst bed; and a process for dewaxing of a hydrocarbon feedstock comprising contacting the hydrocarbon feedstock with said catalyst system.

Process for preparing a catalyst composition containing a modified crystalline aluminosilicate and a binder, wherein the catalyst composition comprises from 5 to 95% by weight of crystalline aluminosilicate as based on the total weight of the catalyst composition, the process being remarkable in that it comprises a step of steaming said crystalline aluminosilicate: at a temperature ranging from 100° C. to 380° C.; under a gas phase atmosphere containing from 5 wt % to 100 wt % of steam; at a pressure ranging from 2 to 200 bars; at a partial pressure of H.sub.2O ranging from 2 to 200 bars; and said steaming being performed during at least 30 min and up to 144 h;
and in that the process also comprises a step of shaping, or of extruding, the crystalline aluminosilicate with a binder, wherein the binder is selected to comprise at least 85 wt % of silica as based on the total weight of the binder, and less than 1000 ppm by weight as based on the total weight of the binder of aluminium, gallium, boron, iron and/or chromium.