Sabic Global Technologies B.v.

Dow Global Technolgoies LLC

Other

Dow Technology Investments LLC

Istvan Lengyel

David H West

Aghaddin Mamedov

Wugeng Liang

Sagar Sarsani

James Lowrey

Byeongjin Baek

John Robert Briggs

Dustin Fickel

Hector Antonio Perez

Jessica L Klinkenberg

Larry G Wright

Krishnan Sankaranarayanan

Sarah E House

Jean Paul Chauvel, Jr

Helene N Launay

Marcel C Van Engelen

Georg Bar

Wilma Hansen

John R Briggs

Christopher P Christenson

Bruce D Hook

Dick Alan Nagaki

Neeta Kulkarni

Timothy Charles Frank

Anil Mehta

Vidya Sagar Reddy Sarsani

Lei Chen

Sreekanth Pannala

Robert R Broekhuis

Emiel Van Kimmenade

Dan Tirtowidjojo

Vladimir Shtern

Zhun Zhao

Heng Shou

Katherine Barton

Steve Gluck

Frank Koester

Sunil K Chaudhary

Celio Lume Pereira

Glenn Lord

Christine Lundstroem

Annett Horn

Zdravko I Stefanov

Wilma Hensen

Abraham Gonzalez

Julia Fuertes Cabello

Julia Cabello Fuertes

Myat Noe Zin Myint

C William Gundlach, Iv

Derek Falcone

Zdravko Ivanov Stefanov

Jr Chauvel Jean Paul

C William Gundlach Iv

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/g, preferably 100 m/g to 500 m/g. Method of use and methods of making the catalyst are also described.

Supported catalyst for butane hydrogenolyis, method of producing the supported catalyst and method to produce ethane

Processes for the hydrogenolysis of butane are described. A process can include (a) introducing a butane feed and hydrogen to a first hydrogenolysis reactor comprising a hydrogenolysis catalyst, and (b) contacting the butane feed and hydrogen with the hydrogenolysis catalyst at conditions sufficient to produce a first hydrogenolysis product stream. The introduction of the butane feed stream and hydrogen to the first hydrogenolysis reactor can be controlled to maintain a hydrogen to butane molar ratio in the reactor inlet of 0.3:1 to 0.8:1.

Methods of butane hydrogenolysis under hydrogen-lean conditions

A reactor () and method for the conversion of hydrocarbon gases utilizes a reactor () having a unique feed assembly () with an original vortex disk-like inlet flow spaces (), a converging-diverging vortex mixing chamber (), and a cylindrical reactor chamber (). This design creates a small combustion zone and an inwardly swirling fluid flow pattern of the feed gases that passes through a converging conduit () with a constricted neck portion (). This provides conditions suitable for efficient cracking of hydrocarbons, such as ethane, to form olefins.

Method and reactor for conversion of hydrocarbons

A mixed oxide catalyst for the oxidative coupling of methane can include a catalyst with the formula ABCDO, wherein: element A is selected from alkaline earth metals; elements B and C are selected from rare earth metals, and wherein elements B and C are different rare earth metals; the oxide of at least one of A, B, C, and D has basic properties; the oxide of at least one of A, B, C, and D has redox properties; and elements A, B, C, and D are selected to create a synergistic effect whereby the catalytic material provides a methane conversion of greater than or equal to 15% and a Cselectivity of greater than or equal to 70%. Systems and methods can include contacting the catalyst with methane and oxygen and purifying or collecting Cproducts.

Mixed oxide catalyst for the oxidative coupling of methane

Use a solvent blend that contains 1-methoxy-2,7-octadiene and an alkanols rather than the alkanols by itself to prepare a catalyst precursor suitable for use in butadiene telomerization.

Butadiene telomerization catalyst precursor preparation

A metal oxide catalyst capable of catalyzing an oxidative coupling of methane reaction is described. The metal oxide catalyst includes a lanthanum (La) cerium (Ce) metal oxide and further including a lanthanum hydroxide (La(OH)) crystalline phase. The catalyst is capable of catalyzing the production of C+ hydrocarbons from methane and oxygen. Methods and systems of using the metal oxide catalyst to produce C+ hydrocarbons from a reactant gas are also described.

Methane oxidative coupling with La&#x2014;Ce catalysts

Disclosed is a process for producing C+ hydrocarbons, and systems for implementing the process, that includes providing a reactant feed that includes methane and an oxygen containing gas to a first reaction zone, wherein the temperature of the reactant feed is less than 700&#xb0; C. contacting the reactant feed with a first catalyst capable of catalyzing an oxidative coupling of methane reaction (OCM) to produce a first product stream that includes C2+ hydrocarbons and heat, and contacting the first product stream with a second catalyst capable of catalyzing an OCM reaction to produce a second product stream that includes C+ hydrocarbons, wherein the produced heat is at least partially used to heat the first product stream prior to or during contact with the second catalyst, wherein the amount of C+ hydrocarbons in the second product stream is greater than the amount of C+ hydrocarbons in the first product stream.

Low inlet temperature for oxidative coupling of methane

An oxidative coupling of methane (OCM) catalyst composition comprising one or more oxides doped with Ag; wherein one or more oxides comprises a single metal oxide, mixtures of single metal oxides, a mixed metal oxide, mixtures of mixed metal oxides, or combinations thereof; and wherein one or more oxides is not LaOalone. A method of making an OCM catalyst composition comprising calcining one or more oxides and/or oxide precursors to form one or more calcined oxides, wherein the one or more oxides comprises a single metal oxide, mixtures of single metal oxides, a mixed metal oxide, mixtures of mixed metal oxides, or combinations thereof, wherein the one or more oxides is not LaOalone, and wherein the oxide precursors comprise oxides, nitrates, carbonates, hydroxides, or combinations thereof; doping the one or more calcined oxides with Ag to form the OCM catalyst composition; and thermally treating the OCM catalyst composition.

Silver promoted catalysts for oxidative coupling of methane

A method for producing Chydrocarbons and Hcomprising (a) introducing to a reactor a reactant mixture comprising methane, (b) heating the reactant mixture to a preheating temperature to yield a heated mixture, (c) generating free radicals in the heated mixture to form a primary effluent mixture comprising free radicals, Chydrocarbons, H, and unreacted methane, (d) reacting the primary effluent mixture in a secondary reaction zone to form a secondary effluent mixture comprising Chydrocarbons, H, free radicals, and unreacted methane, at a secondary reaction zone temperature that is greater than the preheating temperature, wherein a free radicals amount in the primary effluent mixture is greater than a free radicals amount in the secondary effluent mixture, (e) cooling the secondary effluent mixture to a quench temperature lower than the secondary reaction zone temperature to yield a product mixture comprising Chydrocarbons and H, and (f) recovering the product mixture.

Method for producing hydrocarbons by non-oxidative coupling of methane

Process and apparatus for reducing organic content of brine comprising subjecting a brine solution to at least two purification treatments selected from electrochemical treatment, chlorinolysis, or other chemical oxidation treatment, carbon adsorption, extraction, biological treatment and chrystallizing treatment; wherein the organic content of purified brine is sufficiently low to enable sense of the purified brine in an industrial process.

Brine purification

The present invention provides a process for producing low color glycols that comprises altering at least one condition of a reaction component and/or process stream within the process to be unfavorable for the formation of at least one color-producing contaminant intermediate. As such, such intermediates may be reduced in concentration, or even eliminated entirely, from glycols produced by the process. Since they are not present, or are present in reduced number, the intermediates cannot form color-producing contaminants in the glycols, and low color glycols are provided to the customer. Any condition that can discourage the formation of color forming contaminant intermediates can be adjusted, although conditions that can be adjusted by materials or equipment already utilized in the process, e.g., temperature, pressure, pH, concentration of a color-forming contaminant precursor, the presence of one or more solvents or catalysts favorable for the production of the color-producing contaminant or contaminant intermediate, and the like, are preferred.

Process for producing low color glycols

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Lake Jackson, TX, United States of America

Istvan Lengyel