Saudi Arabian Oil Company

Aramco Services Company

Brian S Hanna

Michele Louisa Ostraat

Sergio Fernandez

Sohel K Shaikh

Munir D Khokhar

Noor A Sulais

Mohammed R Alalouni

Timothy J Kucharski

Ke Zhang

Sibo Lin

Maxim Bukhovko

Douglas P Theberge

Sufeng Cao

Michael J Forte

A method of converting a liquid hydrocarbon stream to lower boiling point hydrocarbons may include converting the liquid hydrocarbon stream to an aerosolized hydrocarbon particle stream, and subjecting the aerosolized hydrocarbon particle stream to reaction conditions. Reaction conditions may include a temperature from 25° C. to 1,000° C. and a pressure from 1 bar to 15 bar. The method may further include forming the lower boiling point hydrocarbons in the aerosolized hydrocarbon particle stream and separating the lower boiling point hydrocarbons from the aerosolized hydrocarbon particle stream. The lower boiling point hydrocarbons may comprise at least C—Colefins.

Conversion of an aerosolized hydrocarbon stream to lower boiling point hydrocarbons

A method of converting a liquid hydrocarbon stream to lower boiling point hydrocarbons includes converting the liquid hydrocarbon stream to an aerosolized hydrocarbon particle stream, introducing a charge to the aerosolized hydrocarbon particle stream to produce a charged aerosolized hydrocarbon particle stream including positively charged aerosolized hydrocarbon particles or negatively charged aerosolized hydrocarbon particles, contacting the aerosolized hydrocarbon particle stream with an aerosolized reaction catalyst, subjecting the aerosolized hydrocarbon particle stream to reaction conditions, thereby forming the lower boiling point hydrocarbons, and separating the lower boiling point hydrocarbons from the charged aerosolized hydrocarbon particle stream. The reaction conditions include a temperature of from 25&#xb0; C. to 1,000&#xb0; C. and a pressure of from 0 bar to 15 bar. The lower boiling point hydrocarbons includes at least C-Colefins.

Conversion of an aerosolized and charged hydrocarbon stream to lower boiling point hydrocarbons

According to embodiments described herein, a method of processing a whole crude oil feed stream may include passing a whole crude oil feed stream into a fluid catalytic cracking unit and contacting the whole crude oil feed stream with an adsorbent material and a cracking catalyst. The adsorbent material may adsorb at least a portion of the sulfur of the whole crude oil feed stream and at least a portion of the whole crude oil feed stream may be catalytically cracked to produce coke disposed on the cracking catalyst. The method may further include passing the adsorbent material and the cracking catalyst to a regenerator, wherein the adsorbent material and the cracking catalyst contact an oxygen-containing gas at a temperature sufficient to remove at least a portion of the sulfur on the adsorbent material and combust at least a portion of the coke on the catalyst.

Methods of processing whole crude oils that include sulfur

A method of converting a liquid hydrocarbon stream to lower boiling point hydrocarbons may include converting the liquid hydrocarbon stream to an aerosolized hydrocarbon particle stream, and subjecting the aerosolized hydrocarbon particle stream to reaction conditions. Reaction conditions may include a temperature from 25&#xb0; C. to 1,000&#xb0; C. and a pressure from 1 bar to 15 bar. The method may further include forming the lower boiling point hydrocarbons in the aerosolized hydrocarbon particle stream and separating the lower boiling point hydrocarbons from the aerosolized hydrocarbon particle stream. The lower boiling point hydrocarbons may comprise at least C-Colefins.

Conversion of an aerosolized hydrocarbon stream to lower boiling point hydrocarbons utilizing a fibrous filter

Supported catalysts include a solid support, a metal-ligand complex tethered to a surface of the solid support through at least two surface reactive moieties of the metal-ligand complex, and a conformationally stable molecular pore defined between the metal-ligand complex and the surface of the solid support. The metal-ligand complex includes a catalytic metal center, such as a transition metal, coordinated with multiple monodentate ligands, a multidentate ligand, or a combination thereof. The ligands include a tethering portion that is terminated by a surface reactive moiety tethered to the surface of the solid support by a surface interaction. By tailoring the tethering portion, a volume of the molecular pore may be provided that is selective and suitable for a chosen reactant or a chosen reaction type.

Surface supported catalysts with pore size control

A multi-functional composite catalyst includes a catalyst support material, a preformed catalyst material at least partially secured in the catalyst support, and at least one catalytically active compound supported by the catalyst support, the preformed catalyst material, or both. The catalyst support material may include fumed silica, alumina, fumed alumina, fumed titania, or combinations of these. A catalytic activity of the catalytically active compound may be different than a catalytic activity of the preformed catalyst material. The composite catalyst may be catalyst for producing propene from 2-butene and may include a zeolite as the preformed catalyst material and a metal oxide, such as tungsten oxide, as the catalytically active material. A method of making the composite catalyst may include aerosolizing a catalyst precursor mixture that includes a preformed catalyst material, catalyst support precursor, and catalytically active compound precursor, and drying the aerosolized catalyst precursor mixture.

Multi-functional composite catalyst materials and methods of synthesizing the catalyst materials

One or more embodiments presently disclosed is directed to a method for reacting a chemical stream which may include contacting the chemical stream with a catalyst to produce a product stream. The catalyst may include alumina, silica, and a catalytically active compound such as tungsten.

Methods for reacting chemical streams with catalysts comprising silica, alumina, and tungsten

Embodiments of methods of synthesizing a metathesis catalyst system, which include impregnating tungsten oxide on silica support in the presence of a precursor to produce a base catalyst; calcining the base catalyst; dispersing a solid metal-based co-catalyst onto the surface of the base catalyst to produce a doped catalyst; and calcining the doped catalyst to produce a metathesis catalyst system. Further embodiments of processes for the production of propylene, which include contacting a hydrocarbon feedstock comprising a mixture of 1-butene and 2-butene with embodiments of the metathesis catalyst system to produce, via metathesis conversion, a product stream comprising propylene.

Catalyst systems that include metal co-catalysts for the production of propylene

Embodiments of methods of synthesizing a metathesis catalyst system, which include impregnating tungsten oxide on silica support in the presence of a precursor to produce a base catalyst; calcining the base catalyst; impregnating a metal oxide co-catalyst comprising a metal oxide onto the surface of the base catalyst to produce a doped catalyst; and calcining the doped catalyst to produce a metathesis catalyst system. Further embodiments of processes for the production of propylene, which include contacting a hydrocarbon feedstock comprising a mixture of 1-butene and 2-butene with embodiments of the metathesis catalyst system to produce, via metathesis conversion, a product stream comprising propylene.

Catalyst systems that include metal oxide co-catalysts for the production of propylene

Catalysts systems that include metal co-catalysts for the production of propylene

Embodiments of a method of synthesizing a metathesis and isomerization catalyst or metathesis catalyst or isomerization catalyst comprises forming a catalyst precursor solution comprising a diluent and a catalyst precursor where the catalyst precursor comprises at least one of a silica precursor and an alumina precursor for the isomerization catalyst and additionally an oxometallate precursor or metal oxide precursor for the metathesis catalyst or the metathesis and isomerization catalyst, where the catalyst precursor solution is absent a surfactant; aerosolizing the catalyst precursor solution; drying the aerosolized catalyst precursor mixture to form a dried catalyst precursor; and reacting the dried catalyst precursor to yield the metathesis and isomerization catalyst or the metathesis catalyst or the isomerization catalyst, the metathesis and isomerization catalyst comprising a silica and alumina support with an oxometallate or a metal oxide distributed within the silica and alumina support.

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Somerville, MA, United States of America

Brian S Hanna