Dow Global Technolgoies LLC

Aysegul Ciftci Sandikci

Andrzej Malek

Peter E Groenendijk

Davy L S Nieskens

Edward M Calverley

Glenn Pollefeyt

Barry B Fish

Adam Chojecki

Alexey Kirilin

Vera P Santos Castro

Kyle C Andrews

Davy Nieskens

Barry Brent Fish

Davy LS Nieskens

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 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

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.

Method for stable operation of microporous structures in an oxygenate conversion process

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 for preparing C2 and C3 olefins comprises contacting a feedstream including hydrogen, carbon monoxide, and a bifunctional catalyst in a reaction under certain specified conditions. The catalyst includes as components (1) chromium oxide and zinc oxide mixed metal oxides, and (2) a SAPO-34 molecular sieve. The resulting product of the reaction is relatively high in the target lower olefins and relatively low in less desirable products, including C2 and C3 paraffins, C4+ hydrocarbons, oxygenates, and methane, thereby reducing or eliminating the need for certain previously common and costly separations. The bifunctional catalyst as used in the inventive process also offers improvements in catalyst life in comparison with some methanol-to-olefins catalysts. The process may be carried out as a single unit operation.

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Eindhoven, Netherlands

Aysegul Ciftci Sandikci