The present invention relates to a catalyst system for olefin metathesis, the catalyst system comprising: a) a first system zone substantially comprising a layered double hydroxide; and b) a second system zone comprising a metathesis catalyst.

A process for preparing a hydroconversion catalyst comprising the steps of: preparing a modified zeolite of the FAU framework type, whose intracrystalline structure presents at least one network of micropores, at least one network of small mesopores with a mean diameter of 2 to 5 nm and at least one network of large mesopores with a mean diameter of 10 to 50 nm; these various networks being interconnected; mixing the zeolite with a binder, shaping the mixture, and then calcining; impregnating the shaped zeolite with at least one compound of a catalytic metal chosen from compounds of a metal from group VIII and/or from group VIB, in acidic medium, provided that at least one compound of a catalytic metal is soluble within said acidic medium and that the acid acts as a complexing or chelating agent for at least one compound of a catalytic metal.

According to one or more embodiments described, a zeolite supported catalyst may be synthesized by a process that includes combining a colloidal mixture with a metal oxide support material to form a support precursor material, processing the support precursor material to form a support material, and impregnating the support material with one or more metals to form the zeolite supported catalyst. The colloidal mixture may include nano-sized zeolite crystals, and the nano-sized zeolite crystals may have an average size of less than 100 nm.

Hydrocarbon (HC) traps are disclosed. The HC trap may include a first zeolite material having an average pore diameter of at least 5.0 angstroms and configured to trap hydrocarbons from an exhaust stream and to release at least a portion of the trapped hydrocarbons at a temperature of at least 225° C. The HC trap may also include a second zeolite material having an average pore diameter of less than 5.0 angstroms or larger than 7.0 angstroms. One or both of the zeolite materials may include metal ions, such as transition, Group 1A, or platinum group metals. The HC trap may include two or more discrete layers of zeolite materials or the two or more zeolite materials may be mixed. The multiple zeolite HC trap may form coke molecules having a relatively low combustion temperature, such as below 500° C.

A catalyst comprises a carbide or nitride of a metal and a promoter element. The metal is selected from the group consisting of Mo, W, Co, Fe, Rh or Mn, and the promoter element is selected from the group consisting of Ni, Co, Al, Si, S or P, provided that the metal and the promoter element are different. The catalyst also comprises a mesoporous support having a surface area of at least about 170 m.sup.2 g.sup.−1, wherein the carbide or nitride of the metal and the promoter element is supported by the mesoporous support, and is in a non-sulfided form and in an amorphous form.

The disclosure provides a process to hydrodearylate the non-condensed alkyl-bridged multi-aromatics at the outlet of the clay tower where such multi-aromatics form rather than performing hydrodearylation on the reject stream of the aromatics complex. Hydrodearylation may feature combining a C.sub.8+ hydrocarbon stream from a clay treater with a hydrogen stream over a catalyst bed comprising a support and an acidic component optionally containing Group 8 and/or Group 6 metals.

In accordance with one or more embodiments of the present disclosure, a catalyst composition includes a catalyst support and at least one hydrogenative component disposed on the catalyst support. The catalyst support includes at least one USY zeolite having a framework substituted with titanium and zirconium. The framework-substituted USY zeolite comprises at least one rare earth element. Methods of making and using such a catalyst in a hydrocracking process are also disclosed.

A supported catalyst has a support and a metal active component disposed on the support. The metal active component is at least one selected from the group consisting of a Group VIB metal element and a Group VIII metal element. The support contains at least one of heat-resistant inorganic oxides and molecular sieves and includes an internal channel penetrating the support. The ratio of the cross-section area of the channel to the cross-section area of the support is 0.05-3:100. The difference R between the water absorption rate and the BET pore volume of the support is not less than 0.2 mL/g. The supported catalyst can be used as a hydrogenation catalyst. When used in the hydrocracking of hydrocarbon oils, it can achieve high catalytic activity and high yield of jet fuels at the same time. The supported catalyst can also be used as a Fischer-Tropsch synthesis catalyst.

The invention relates to a catalyst comprising at least one metal selected from the group formed by metals of group VIB and of group VIII of the periodic table, used alone or as a mixture, and a support comprising at least one zeolite NU-86, at least one zeolite Y and at least one porous mineral matrix containing at least aluminum and/or at least silicon. The invention also relates to a process for hydrocracking of hydrocarbon feeds employing said catalyst.

Catalytic system which can be used in processes for the hydroconversion of heavy oils by means of hydrotreatment in slurry phase, characterized in that it comprises: a catalyst, having the function of hydrogenating agent, containing MoS.sub.2 or WS.sub.2 or mixtures thereof in lamellar form or an oil-soluble precursor thereof; a co-catalyst, having nanometric or micronic particle-sizes, selected from cracking and/or denitrogenation catalysts. The co-catalyst preferably consists of zeolites having small-sized crystals and with a low aggregation degree between the primary particles, and/or oxides or sulfides or precursors of sulfides of Ni and/or Co in a mixture with Mo and/or W.