Dow Global Technolgoies LLC

Georgia Tech Research Corporation

Brien A Stears

Andrzej Malek

Matthew T Pretz

Barry B Fish

Lin Luo

Mark William Stewart

Peter E Groenendijk

Davy L S Nieskens

Eric E Stangland

Brian W Goodfellow

Madhusudhan Kodam

Max Markus Tirtowidjojo

Howard W Clark

Richard Michael Wehmeyer

Victor J Sussman

Alexey Kirilin

Richard A Pierce

Albert E Schweizer, Jr

Susan B Domke

William Jack Kruper, Jr

William John Koros

Robert G Bowman

William J Kruper

Isa K Mbaraka

Ben J Freireich

Duncan Paul Coffey

Manish Sharma

Guido Capone

Kevin Blann

John G Pendergast, Jr

Mark P Kaminsky

Kurt Frederick Hirsekorn

Dean M Millar

Liren Xu

Mark K Brayden

Mark E Jones

Dennis Wade Jewell

Debashis Chakraborty

Marcos V Martinez

Yu Liu

Don F Shaw

Mark D Bearden

Daniela Ferrari

Adrianus Koeken

Jan Willem Verwijs

Devon C Rosenfeld

Hendrik L Pelt

Yang Yang

Mark A Siddoway

Jon H Siddall

Phillip W Dellinger

Aaltje Verwijs-van Den Brink, Legal Representative

Dennis W Jewell

Luis Bollmann

Lena Verwijs, Legal Representative

Haivan D Tran

Simon G Podkolzin

Mark Siddoway

Martin A Cogswell

Hendrika Gerrita Verwijs, Legal Representative

William L Jackson, Jr

Mark W Stewart

Madhusudhan M Kodam

Jr Albert Schweizer

William J Koros

Barry Brent Fish

Davy LS Nieskens

William L Jackson

Andrzej M Malek

According to one or more embodiments of the present disclosure, a method for producing olefins includes contacting a hydrocarbon-containing feed with a catalyst in a reactor portion of a reactor system to form an olefin-containing effluent, separating at least a portion of the olefin-containing effluent from the catalyst, passing the catalyst to a catalyst-processing portion of the reactor system and processing the catalyst to produce a processed catalyst and a combustion gas, passing the processed catalyst from the catalyst-processing portion to the reactor portion, and introducing a combustion additive to the reactor system when the combustion gas comprises one or more hydrocarbons in an amount greater than 5% of an LFL of the combustion gas at a temperature and pressure of the catalyst processing portion. The catalyst may include from 1 ppmw to 150 ppmw platinum. The combustion additive may include from 150 ppmw to 1,000 ppmw platinum.

Methods for producing olefins

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 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 for recovery of Cand Ccomponents in an on-purpose propylene production system includes utilizing a packed rectifier with a countercurrent stream to strip Cand Ccomponents from a combined de-ethanizer overhead lights vapor and cracked gas vapor stream.

Process for increasing ethylene and propylene yield from a propylene plant

According to one or more embodiments, a fluid catalytic reactor may include a riser, a lower reactor portion, a transition portion, and a flow director. The riser may include a cross-sectional area, and the lower reactor portion may include a cross-sectional area. The transition portion may attach the riser to the lower reactor portion. The cross-sectional area of the riser may be less than the cross-sectional area of the lower reactor portion such that the transition portion is tapered inward from the lower reactor portion to the riser. The flow director may be positioned at least within an interior region of the transition portion. The flow director may include a body which affects the velocity profile of fluids moving from the lower reactor portion to the riser.

Fluid catalytic reactors which include flow directors

According to one or more embodiments of the present disclosure, a fluid catalytic reactor may be scaled-up by a method that includes one or more of constructing, operating, observing, or obtaining data related to a template fluid catalytic reactor comprising a template riser, a template lower reactor portion, and a template transition portion connecting the template riser and the template lower reactor portion. The method may further include one or more of constructing or operating a scaled-up fluid catalytic reactor based on the template fluid catalytic reactor.

Methods for designing scaled-up fluid catalytic reactors

Manage sulfur present as sulfur or a sulfur compound in a hydrocarbon feedstream while effecting dehydrogenation of hydrocarbon(s) (e.g. propane) contained in the hydrocarbon feedstream to its/their corresponding olefin (e.g. propylene where the hydrocarbon is propane) without subjecting the feedstream to desulfurization before it contacts a fluidizable dehydrogenation catalyst that is both a desulfurant and a dehydrogenation catalyst and comprises gallium and platinum on an alumina or alumina-silica catalyst support with optional alkali or alkaline earth metal such as potassium. Contact with such a catalyst yields a desulfurized crude olefin product that corresponds to the hydrocarbon and has a reduced amount of sulfur or sulfur compounds relative to the sulfur or sulfur compounds present in the hydrocarbon feedstream prior to contact with the catalyst.

Propane dehydrogenation sulfur management

Increase propane dehydrogenation activity of a partially deactivated dehydrogenation catalyst by heating the partially deactivated catalyst to a temperature of at least 660&#xb0; C., conditioning the heated catalyst in an oxygen-containing atmosphere and, optionally, stripping molecular oxygen from the conditioned catalyst.

Reactivating propane dehydrogenation catalyst

A catalyst comprising a Group IIIA metal, a Group VIII noble metal, and an optional promoter metal, on a support selected from silica, alumina, silica-alumina compositions, rare earth modified alumina, and combinations thereof, doped with iron, a Group VIB metal, a Group VB metal, or a combination thereof, offers decreased reactivation time under air soak in comparison with otherwise identical catalysts. Reducing reactivation time may, in turn, reduce costs, both in inventory and capital.

Catalyst composition and reactivation process useful for alkane dehydrogenations

A heterogeneous catalyst suitable for use in alkane dehydrogenation has an active layer that includes alumina and gallia. The active layer is dispersed on a support such as alumina or silica-modified alumina.

Heterogeneous alkane dehydrogenation catalyst

Convert dichloroisopropyl ether into a halogenated derivative by contacting the dichloroisopropyl ether with a source of hydrogen and a select heterogeneous hydrogenation catalyst under process conditions selected from a combination of a temperature within a range of from 50 degrees centigrade (&#xb0; C.) to 350&#xb0; C., a pressure within a range of from atmospheric pressure (0.1 megapascals) to 1000 pounds per square inch (6.9 MPa), a liquid feed volume flow to catalyst mass ratio between 0.5 and 10 L/Kg*h and a volume hydrogen/volume liquid ratio between 100 and 5000 ml gas/ml liquid. The halogenated derivative is at least one of 1-chloro-2-propanol and 1,2-dichloropropane 1, and glycerin monochlorohydrin.

Process for hydrogenating dichloroisopropyl ether

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League City, TX, United States of America

Brien A Stears