Dow Global Technolgoies LLC

Blue Cube IP LLC

Ecocatalytic Inc.

Barry B Fish

Max Markus Tirtowidjojo

Andrzej Malek

David Laitar

Matthew T Pretz

Brien A Stears

Davy L S Nieskens

Peter E Groenendijk

William Jack Kruper, Jr

Alexey Kirilin

Daniel A Hickman

Michael Leo Tulchinsky

William J Kruper

Hangyao Wang

Erich J Molitor

Victor J Sussman

Shawn D Feist

Eric E Stangland

Abraham D Schuitman

John A Sofranko

Richard Michael Wehmeyer

Lin Luo

John G Pendergast, Jr

Garmt R Meima

Adam Chojecki

Matthew Lee Grandbois

Dennis Wade Jewell

Yu Liu

Aysegul Ciftci Sandikci

Mark D Bearden

Soumen Kundu

Patrick H Au-Yeung

Brian W Goodfellow

Manish Sharma

Kevin Blann

David S Laitar

Thomas Davidian

Matthijs Ruitenbeek

David Jean

Elena Y Chung

Jan Willem Verwijs

Stacie L Santhany

Joseph F DeWilde

Hendrik L Pelt

William K Wang

Jon H Siddall

Davy Nieskens

Patrick Ho Sing Au-Yeung

Todd William Toyzan

Haivan D Tran

Aaltje Verwijs-van Den Brink, Legal Representative

Lena Verwijs, Legal Representative

Hendrika Gerrita Verwijs, Legal Representative

Dennis W Jewell

Glenn Pollefeyt

Gerald W Dare

Gerald Dare

Todd Toyzan

David Stephen Laitar

Matthew L Grandbois

Erich Molitor

A process for oxidative dehydrogenation of a hydrocarbon to produce an olefin and water may include contacting, in a fluidized bed, the hydrocarbon with a particulate material, which may include at least one oxygen transfer agent (OTA) and at least one fluidization enhancing additive. During at least a portion of contacting the hydrocarbon with the particulate material, the fluidized bed may be at a temperature at or above a melting point of one or more materials of the oxygen transfer agent. Further, during at least a portion of contacting the hydrocarbon with the particulate material, a surface of at least a portion of the OTA may comprise a molten layer. The fluidization enhancing additive may not undergo reduction in the fluidized bed during contacting the hydrocarbon with the particulate material and may be present in an amount that maintains sufficient fluidization of the particulate material.

Fluidization enhancers for the oxidative dehydrogenation of hydrocarbons

A process for preparing Cto Chydrocarbons includes introducing a feed stream into a reaction zone of a reactor, the feed stream comprising hydrogen gas and carbon monoxide. An additional stream is introduced into the reaction zone of the reactor, the additional stream comprising carbon dioxide. A combined stream that includes the feed stream and the additional stream is converted into a product stream comprising Cto Chydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a mixed metal oxide catalyst component, and a microporous catalyst component. The process operates at a gas hourly space velocity in excess of 2500 hrand effectively yields a net carbon dioxide selectivity of less than 5.0% and a productivity of C-Chydrocarbons greater than 75 g hydrocarbons per kilogram of catalyst per hour.

Synthesis gas to hydrocarbon processes with neutral or negative carbon dioxide selectivity

According to one or more embodiments described herein, a method for dehydrogenating hydrocarbons may include passing a hydrocarbon feed comprising one or more alkanes or alkyl aromatics into a fluidized bed reactor, contacting the hydrocarbon feed with a dehydrogenation catalyst in the fluidized bed reactor to produce a dehydrogenated product and hydrogen, and contacting the hydrogen with an oxygen-rich oxygen carrier material in the fluidized bed reactor to combust the hydrogen and form an oxygen-diminished oxygen carrier material. In additional embodiments, a dual-purpose material may be utilized which has dehydrogenation catalyst and oxygen carrying functionality.

Methods for dehydrogenating hydrocarbons

A method for separating COfrom Cto Calkanes includes introducing a first stream including Cto Calkanes and COinto a first separation zone, the first separation zone including a hydrocarbon solvent, and separating the first stream into a recycle stream and a second stream in the first separation zone. The recycle stream including COand one or more of CO, H, and CH, and the second stream including Cto Calkanes. The method further includes introducing the second stream into a second separation zone, and separating the second stream into a third stream and a fourth stream, wherein the third stream includes Calkanes and the fourth stream includes Cto Calkanes.

Processes and systems for separating carbon dioxide in the production of alkanes

A method for operating an integrated system for producing olefins may include contacting a hydrogenation feed with a first hydrogenation catalyst to produce a hydrogenated effluent, the hydrogenation feed including at least a portion of a first process effluent from a first olefin production process and at least a portion of a second process effluent from a second olefin production process. The hydrogenation feed may include at least hydrogen, ethylene, carbon monoxide, acetylene, methyl acetylene, and propadiene, and the first hydrogenation catalyst may be a hydrogenation catalyst having a temperature operating range of at least 40&#xb0; C. The hydrogenated effluent may include methyl acetylene, propadiene, or both. The method may further include contacting at least a portion of the hydrogenated effluent with a second hydrogenation catalyst, which may cause hydrogenation of at least a portion of the methyl acetylene and propadiene to produce an MAPD hydrogenated effluent.

Methods for operating integrated chemical processing systems for producing olefins

A process for converting a feed stream having carbon to Cto Colefins, includes introducing a feed stream including methane and oxygen to a first reaction zone, reacting the methane and oxygen in the first reaction zone to form a first reaction zone product stream having a mixture of Cto Calkanes, transporting the mixture of Cto Calkanes to a second reaction zone, introducing a fresh stream of at least one of ethane and propane to the second reaction zone, converting the Cto Calkanes to Cto Colefins in the second reaction zone, producing one or more product streams in the second reaction zone, where a sum of the one or more product streams includes Cto Colefins, and producing a recycle stream comprising hydrogen in the second reaction zone, where the recycle stream is transported to the first reaction zone.

Processes for improving the efficiency of hydrocarbon production

A process and system for preparing Cto Chydrocarbons includes introducing a feed stream containing hydrogen gas and a carbon-containing gas selected from carbon monoxide, carbon dioxide, and mixtures thereof into a first reaction zone, contacting the feed stream and a hybrid catalyst in the first reaction zone, introducing a reaction zone product stream into a water removal zone that is downstream from the first reaction zone, and introducing a product stream from the water removal zone into a second reaction zone, resulting in a final stream comprising Cto Chydrocarbons. The hybrid catalyst includes a methanol synthesis component and a microporous solid acid component; the microporous solid acid component is a molecular sieve having 8-MR access. The water removal zone removes at least a portion of water from the reaction zone product stream.

Processes and systems for achieving high carbon conversion to desired products in a hybrid catalyst system

A process is provided for the chlorination of ethane using chlorine as the chlorinating agent to produce ethylene, hydrogen chloride (HCl) and vinyl chloride monomer (VCM).

Process for the production of ethylene, hydrogen chloride, and vinyl chloride from ethane

Process for the production of hydrogen chloride, ethylene and vinyl chloride from ethane

A process is provided for the chlorination of ethane using chlorine as the chlorinating agent to produce vinylidene (1,1-dichloroethylene), hydrogen chloride and ethylene.

Process for the production of ethylene, vinylidene, and hydrogen chloride from ethane

A feedstream comprising hydrogen and a gas selected from carbon monoxide, carbon dioxide, or a combination thereof is converted to a product mixture containing a combination of saturated and unsaturated two carbon atom and three carbon atom hydrocarbons via contact with a mixed catalyst comprising a mixed metal oxide catalyst selected from a copper oxide, copper oxide/zinc oxide, copper oxide/alumina, copper oxide/zinc oxide/alumina catalyst, a zinc oxide/chromium oxide catalyst, or a combination thereof, in admixture with a molecular sieve catalyst having a CHA, AEI, AEL, AFI, BEA, or DDR framework type, or a combination of such molecular sieves. Exemplary molecular sieve catalysts include SAPO-34, SAPO-18, SAPO-5, and Beta. Advantages include reduced production of C1 hydrocarbons, C4 and higher hydrocarbons, or both; long catalyst lifetimes; desirable conversions; and desirable proportions of C2 and C3 paraffins.

Conversion of carbon monoxide, carbon dioxide, or a combination thereof over hybrid catalyst

Processes for the production of chlorinated propenes are provided. The processes make use of 1,2-dichloropropane as a starting material and subject a feedstream comprising the same to an ionic chlorination process. At least a portion of any tri- and tetrachlorinated propanes not amenable to ionic chlorination conditions are removed from the ionic chlorination product stream, or, are subjected to chemical base dehydrochlorination step. In this way, recycle of intermediates not amenable to ionic chlorination reactions is reduced or avoided, as is the buildup of these intermediates within the process. Selectivity and, in some embodiments, yield of the process is thus enhanced.

Process for the production of chlorinated propenes

Processes for the production of chlorinated propenes are provided. The present processes make use of a feedstock comprising 1,2,3-trichloropropane and chlorinates the 1,1,2,3-tetrachloropropane generated by the process prior to a dehydrochlorination step. Production of the less desirable pentachloropropane isomer, 1,1,2,3,3-pentachloropropane, is thus minimized. The present processes provide better reaction yield as compared to conventional processes that require dehydrochlorination of 1,1,2,3-tetrachloropropane prior to chlorinating the same. The present process can also generate anhydrous HCl as a byproduct that can be removed from the process and used as a feedstock for other processes, while limiting the production of waste water, thus providing further time and cost savings.

Growing community of inventors

Lake Jackson, TX, United States of America

Barry B Fish