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.

Catalysts for the hydrogenolysis of butane are described. A supported catalyst for hydrogenolysis of butane to ethane can include a support and a catalytic crystalline bimetallic composition that can include a molybdenum-iridium (Mo—Ir) crystalline composition attached to the support. The supported catalyst has a BET specific surface area of at least 100 m.sup.2/g, preferably 100 m.sup.2/g to 500 m.sup.2/g. Method of use and methods of making the catalyst are also described.

Process P.sup.1 for the manufacture of a secondary fatty alcohol, said process P.sup.1 comprising synthesizing an internal ketone K1 by a process P.sup.0 comprising the decarboxylative ketonization reaction of a fatty acid or the like in a liquid phase with a metal compound as catalyst in a reaction medium, wherein a ketone K.sup.2 at liquid state, which is identical or similar to the internal ketone K.sup.1, is introduced into the reaction medium, and subjecting the internal ketone K.sup.1 to a hydrogenation reaction with hydrogen gas as hydrogenating agent to form the secondary fatty alcohol. Use of the secondary fatty alcohol manufactured by the process P.sup.1 for the manufacture of an internal olefin or of an internal olefin sulfonate.

The present disclosure relates to gallium-based dehydrogenation catalysts that further include additional metal components, and to methods for dehydrogenating hydrocarbons using such catalysts. One aspect of the disclosure provides a calcined dehydrogenation catalyst that includes a gallium species, a cerium species, a platinum promoter, and a silica-alumina support. Optionally, the composition can include a promoter selected from the alkali metals and alkaline earth metals.

There is provided a catalyst having an average electronegativity of 2.1 or more and 2.8 or less.

Paraffin compositions including mainly even carbon number paraffins, and a method for manufacturing the same, is disclosed herein. In one embodiment, the method involves contacting naturally occurring fatty acid/glycerides with hydrogen in a slurry bubble column reactor containing bimetallic catalysts with equivalent particle diameters from about 10 to about 400 micron. The even carbon number compositions are particularly useful as phase change material.

A method for producing a three-dimensional porous transition alumina catalyst monolith of stacked catalyst fibers, comprising: a) Preparing a paste in a liquid diluent of hydroxide precursor particles and/or oxyhydroxide precursor particles of transition alumina particles, all particles in the suspension having a number average particle size in the range of from 0.05 to 700 μm, b) extruding the paste nozzle(s) to form fibers, and depositing the extruded fibers to form a three-dimensional porous catalyst monolith precursor, c) drying the precursor to remove the liquid diluent, d) performing a temperature treatment of the dried porous catalyst monolith precursor to form the transition alumina catalyst monolith, wherein no temperature treatment of the porous catalyst monolith precursor or porous catalyst monolith at temperatures above 1000° C. is performed and wherein no further catalytically active metals, metal oxides or metal compounds are applied to the surface.

A modified Y-type molecular sieve has a rare earth content of about 4% to about 11% by weight on the basis of the oxide, a phosphorus content of about 0.05% to about 10% by weight on the basis of P.sub.2O.sub.5, a sodium content of no more than about 0.5% by weight on the basis of sodium oxide, a gallium content of about 0.1% to about 2.5% by weight on the basis of gallium oxide, and a zirconium content of about 0.1% to about 2.5% by weight on the basis of zirconia; and the modified Y-type molecular sieve has a total pore volume of about 0.36 mL/g to about 0.48 mL/g, a percentage of the pore volume of secondary pores having a pore size of 2-100 nm to the total pore volume of about 20% to about 40%.

A catalyst for non-oxidative dehydrogenation of alkanes and a method for making and using the same is disclosed. The catalyst can include vanadium oxide derived from vanadyl oxalate. More particularly the catalyst is prepared by a method comprising the steps of: (a) contacting a transition alumina support with an aqueous solution comprising a vanadium carboxylate material solubilized therein; (b) heating the contacted alumina support to remove the water and produce a catalyst precursor material in solid form; and (c) heating the solid catalyst precursor material in the presence of an oxidizing source at a temperature of 500 to 800° C. to produce an alumina supported catalytic material comprising vanadium oxide. The catalyst can be further modified with an alkali metal oxide like potassium oxide, the precursor thereof being introduced with the impregnation solution.

A modified Y-type molecular sieve has a rare earth content of about 4-11% by weight on the basis of rare earth oxide, a sodium content of no more than about 0.5 wt % by weight on the basis of sodium oxide, a zinc content of about 0.5-5% by weight on the basis of zinc oxide, a phosphorus content of about 0.05-10% by weight on the basis of phosphorus pentoxide, a framework silica-alumina ratio of about 7-14 calculated on the basis of SiO.sub.2/Al.sub.2O.sub.3 molar ratio, a percentage of non-framework aluminum content to the total aluminum content of no more than about 10%, and a percentage of the pore volume of secondary pores having a pore size of 2-100 nm to the total pore volume of about 20-40%. The modified Y-type molecular sieve has a high crystallinity and a high thermal and hydrothermal stability, and is rich in secondary pores.