Provided is a method of converting a hydrocarbon using a catalyst/catalyst support including a PST-32 or PST-2 zeolite, which has an effect of increasing the selectivity/yield of a light olefin product and reducing a side reaction to sustain catalytic activity, in various hydrocarbon conversion reactions, in particular, catalytic cracking of diesel.

Provided is a method of converting a hydrocarbon using a catalyst/catalyst support including a PST-32 or PST-2 zeolite, which has an effect of increasing the selectivity/yield of a light olefin product and reducing a side reaction to sustain catalytic activity, in various hydrocarbon conversion reactions, in particular, catalytic cracking of diesel.

In accordance with the present subject matter there is provided a catalyst composition including 70-98% of a non-zeolitic material; and 2-30% of at least one zeolite material, the percentage being based on weight of the catalyst composition. The subject matter also relates to a method for preparation of the catalyst composition. The subject matter further relates to a process for the fluid catalytic cracking of a hydrocarbon feedstock.

In accordance with the present subject matter there is provided a catalyst composition including 70-98% of a non-zeolitic material; and 2-30% of at least one zeolite material, the percentage being based on weight of the catalyst composition. The subject matter also relates to a method for preparation of the catalyst composition. The subject matter further relates to a process for the fluid catalytic cracking of a hydrocarbon feedstock.

The present invention relates to new crystalline zeolite SSZ-52x prepared using a quaternary ammonium cation templating agent, for example, having the structure:

##STR00001##

wherein X.sup.− is an anion which is not detrimental to the formation of the SSZ-52x. SSZ-52x is useful as a catalyst and shows improved durability, particularly with regard to NO.sub.x conversion.

A petroleum refining method for upgrading petroleum products improves the efficiency and reduces the costs of upgrading oils, such as lipids, bitumen, crude oil, fracking oils, synthetic oils, and other feeds, to produce useful fuels and chemical precursor streams. Usage of a specific type of zeolite (ZSM-5) catalyst, supercritical water to control coke formation, and a specific response to phase behavior and other catalytic effects optimize the process. A prescribed set of reactor conditions employing supercritical water increases activity of the catalyst in industrial reactions.

According to one or more embodiments described herein, a method for cracking a hydrocarbon oil may include contacting the hydrocarbon oil with a fluidized cracking catalyst including an ultra-stable Y-type zeolite in a fluidized catalytic cracking unit to produce light olefins, gasoline fuel, and coke. At least 99 wt. % of the hydrocarbon oil may have a boiling point greater than 350° C. The ultra-stable Y-type zeolite may be a framework-substituted zeolite in which a part of aluminum atoms constituting a zeolite framework thereof is substituted with 0.1-5 mass % zirconium atoms and 0.1-5 mass % titanium ions on an oxide basis. The fluidized cracking catalyst may include from 3.5 wt. % to 10 wt. % of one or more Group 7 metal oxides.

According to one or more embodiments described herein, a method for cracking a hydrocarbon oil may include contacting the hydrocarbon oil with a fluidized cracking catalyst including an ultra-stable Y-type zeolite in a fluidized catalytic cracking unit to produce light olefins, gasoline fuel, and coke. At least 99 wt. % of the hydrocarbon oil may have a boiling point greater than 350° C. The ultra-stable Y-type zeolite may be a framework-substituted zeolite in which a part of aluminum atoms constituting a zeolite framework thereof is substituted with 0.1-5 mass % zirconium atoms and 0.1-5 mass % titanium ions on an oxide basis. The fluidized cracking catalyst may include from 3.5 wt. % to 10 wt. % of one or more Group 7 metal oxides.

A process for producing olefins from the hydrocarbon feed includes introducing the hydrocarbon feed into a Solvent Deasphalting Unit (SDA) to remove asphaltene from the hydrocarbon feed producing a deasphalted oil stream, wherein the SDA comprises a solvent that reacts with the hydrocarbon feed, and the deasphalted oil stream comprises from 0.01 weight percent (wt. %) to 18 wt. % asphaltenes; introducing the deasphalted oil stream into a steam catalytic cracking system; steam catalytically cracking the deasphalted oil stream in the steam catalytic cracking system in the presence of steam and a nano zeolite cracking catalyst to produce a steam catalytic cracking effluent; and separating the olefins from the steam catalytic cracking effluent.

Embodiments of catalyst systems and methods of synthesizing catalyst systems are provided. The catalyst system may include a core comprising a zeolite; and a shell comprising a microporous fibrous silica. The shell may be in direct contact with at least a majority of an outer surface of the core. The catalyst system may have a Si/Al molar ratio greater than 5. At least a portion of the shell may have a thickness of from 50 nanometers (nm) to 600 nm.