Dow Global Technolgoies LLC

Davy L S Nieskens

Andrzej Malek

Peter E Groenendijk

Glenn Pollefeyt

Aysegul Ciftci Sandikci

Alexey Kirilin

Barry B Fish

Adam Chojecki

Vera P Santos Castro

Brien A Stears

David F Yancey

Edward M Calverley

Joseph F DeWilde

Kyle C Andrews

Dean M Millar

Joseph F Dewilde

A process for preparing C2 to C3 hydrocarbons may include introducing a feed stream including hydrogen gas and a carbon-containing gas comprising carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor, and converting the feed stream into a product stream comprising C2 to C3 hydrocarbons in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst may include a metal oxide catalyst component and a microporous catalyst component comprising 8-MR pore openings less than or equal to 5.1 A and a cage defining ring size less than or equal to 7.45 A, where a C2/C3 carbon molar ratio of the product stream is greater than or equal to 0.7.

Processes for preparing C2 to C3 hydrocarbons in the presence of a hybrid catalyst

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

A method for preparing Cto Cparaffins includes introducing a feed stream including hydrogen gas and a carbon-containing gas selected from carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor. Converting the feed stream into a product stream including Cto Cparaffins in the presence of a hybrid catalyst. The hybrid catalyst includes a microporous catalyst component; and a metal oxide catalyst component selected from (A) a bulk material consisting of gallium oxide, (B) gallium oxide present on a titanium dioxide support material, and (C) a mixture of gallium oxide and at least one promoter present on a support material selected from Group 4 of the IUPAC periodic table of elements.

Methods for producing Cto Cparaffins using a hybrid catalyst comprising gallium metal oxide

A hybrid catalyst including a metal oxide catalyst component comprising chromium, zinc, and at least one additional metal selected from the group consisting of aluminum and gallium, and a microporous catalyst component that is a molecular sieve having 8-MR pore openings. The metal oxide catalyst component includes anatomic ratio of chromium:zinc (Cr:Zn) from 0.35 to 1.00, and the at least one additional metal is present in an amount from 25.0 at % to 40.0 at %. A process for preparing C2 and C3 olefins comprising: a) introducing a feed stream comprising hydrogen gas and a carbon-containing gas selected from the group consisting of carbon monoxide, carbon dioxide, and mixtures thereof into a reaction zone of a reactor; and b) converting the feed stream into a product stream comprising C2 and C3 olefins in the reaction zone in the presence of said hybrid catalyst.

Hybrid catalysts comprising a zeolite and a mixed metal oxide component for converting syngas into Cand Colefins

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 preparing Cto Cparaffins includes introducing a feed stream comprising hydrogen gas and a carbon-containing gas into a reaction zone of a reactor, and converting the feed stream into a product stream comprising Cto Cparaffins in the reaction zone in the presence of a hybrid catalyst. The hybrid catalyst includes a metal oxide catalyst component and a microporous catalyst component. The metal oxide catalyst component satisfies: an atomic ratio of Cu/Zn from 0.01 to 3.00; an atomic ratio of Cr/Zn from 0.01 to 1.50; and percentage of (Al+Cr) from greater than 0.0 at % to 50.0 at % based on a total amount of metal in the metal oxide catalyst component.

Catalyst for converting carbon-containing stream to C2 to C5 paraffins and method using the catalyst

A process for preparing Cto Chydrocarbons includes introducing a feed stream into a reaction zone of a reactor, the feed stream including hydrogen gas and carbon monoxide. An additional stream is introduced into the reaction zone of the reactor, the additional stream comprising water, carbon dioxide, or mixtures thereof. 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 metal oxide catalyst component, and a microporous catalyst component.

Process for preparing C2&#x2014;C5 hydrocarbons using a hybrid catalyst

A process for preparing Cto Colefins includes introducing a feed stream comprising hydrogen and at least one carbon-containing component selected from the group consisting of CO, CO, and mixtures thereof into a reaction zone. The feed stream is contacted with a hybrid catalyst in the reaction zone, and a product stream is formed that exits the reaction zone and includes Cto Colefins. The hybrid catalyst includes a methanol synthesis component and a solid microporous acid component that is selected from molecular sieves having 8-MR access and having a framework type selected from the group consisting of CHA, AEI, AFX, ERI, LTA, UFI, RTH, and combinations thereof. The methanol synthesis component comprises a metal oxide support and a metal catalyst. The metal oxide support includes titania, zirconia, hafnia or mixtures thereof, and the metal catalyst includes zinc.

Hybrid catalyst for selective and stable olefin production

A hybrid catalyst including a metal oxide catalyst component comprising chromium, zinc, and at least one additional metal selected from the group consisting of iron and manganese, and a microporous catalyst component that is a molecular sieve having 8-MR pore openings. The at least one additional metal is present in an amount from 5.0 at % to 20.0 at %.

Hybrid catalysts comprising a mixed metal oxide component for production of C2 and C3 hydrocarbons

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

Catalyst and method for converting carbon-containing stream to C2 to C5 paraffins using it

A process for preparing Cto Colefins includes introducing a feed stream having a volumetric ratio of hydrogen to carbon monoxide from greater than 0.5:1 to less than 5:1 into a reactor, and contacting the feed stream with a bifunctional catalyst. The bifunctional catalyst includes a Cr/Zn oxide methanol synthesis component having a Cr to Zn molar ratio from greater than 1.0:1 to less than 2.15:1, and a SAPO-34 silicoaluminophosphate microporous crystalline material. The reactor operates at a temperature ranging from 350&#xb0; C. to 450&#xb0; C., and a pressure ranging from 10 bar (1.0 MPa) to 60 bar (6.0 MPa). The process has a cumulative productivity of Cto Colefins greater than 15 kg Cto Colefins/kg catalyst.

Process to convert synthesis gas to olefins using a bifunctional chromium/zinc oxide-SAPO-34 catalyst

A process for converting a feed stream to Cto Chydrocarbons includes introducing a feed stream of hydrogen and at least one carbon-containing component selected from CO, CO, and mixtures thereof into a reaction zone at an initial reactor pressure and an initial reactor temperature. The feed stream is contacted to a hybrid catalyst positioned in the reaction zone, and the hybrid catalyst includes a methanol synthesis component and a solid microporous acid material. The pressure within the reaction zone is increased during the contacting of the feed stream to the hybrid catalyst from the initial reactor pressure to a final reactor pressure. A temperature within the reaction zone at any time during the contacting of the feed stream to the hybrid catalyst is within &#xb1;20&#xb0; C. of the initial reactor temperature.

Processes for improving the activity of hybrid catalysts

A process for converting oxygenates to hydrocarbons includes introducing a feed stream having at least one oxygenate into a reaction zone, and introducing a hydrogen gas stream into the reaction zone. In the reaction zone the feed stream and the hydrogen gas stream are simultaneously contacted with a catalyst, and the catalyst includes a solid microporous acid component having 8-MR to 10-MR access. The hydrogen gas stream in the reaction zone has a partial pressure from 1 bar (100 kPa) to 48 bar (4800 kPa), and the reaction zone is at a temperature from 350&#xb0; C. to 500&#xb0; C.

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Terneuzen, Netherlands

Davy L S Nieskens