Chinese Academy of Sciences

Dalian Institute of Chemical Physics, Cas

Basf Se Corporation

Basf Mobile Emissions Catalysts LLC

Xiulian Pan

Xinhe Bao

Feng Jiao

Ulrich Mueller

Dirk De Vos

Feng-Shou Xiao

Hermann Gies

Bernd Marler

Ute Kolb

Trees De Baerdemaeker

Yong Wang

Chuan Shi

Na Li

Stefan Maurer

Mathias Feyen

Weiping Zhang

Xiangju Meng

Toshiyuki Yokoi

Gen Li

Robert McGuire

Yu Dai

Xiaoguang Guo

Guangzong Fang

Dali Tan

Yuxiang Chen

Jinjing Li

Minzheng Ding

Yifeng Zhu

Junhao Yang

Qinqin Yu

Jingheng Meng

A method for preparing liquid fuel by direct conversion of syngas uses the syngas as reaction raw material and conducts a catalytic conversion reaction on a fixed bed or a moving bed. The catalyst is a composite catalyst formed by compounding component I and component II in a mechanical mixing mode. The active ingredient of the component I is a metal oxide, and the component II is at least one of zeolites with one-dimensional ten-membered ring porous channels; and a weight ratio of the active ingredient in the component I to that in the component II is 0.1-20. The reaction process has high product yield and selectivity. The selectivity for liquid fuel composed of C-Ccan reach 50-80%. The selectivity for aromatic hydrocarbon is less than 40% in C-C, while the selectivity for methane side product is less than 15%.

Catalyst and method for preparing low aromatic hydrocarbon liquid fuel through direct conversion of syngas

A composite catalyst containing heteroatom-doped zeolite for preparing light olefin using direct conversion of syngas is formed by compounding component I and component II in a mechanical mixing mode. The active ingredient of component I is a metal oxide, and the component II is a heteroatom-doped zeolite. The zeolite topology is CHA or AEI, and the skeleton atoms include Al—P—O or Si—Al—P—O; the heteroatoms is at least one of divalent metal Mg, Ca, Cr, Mn, Fe, Co, Ni, Cu, Zn, Sr, Zr, Mo, Cd, Ba and Ce, trivalent metal Ti and Ga, and tetravalent metal Ge. A weight ratio of the active ingredient in the component I to the component II is 0.1-20. The reaction process has high light olefin selectivity; the sum selectivity of the light olefin including ethylene, propylene and butylene can reach 50-90%, while the selectivity of a methane side product is less than 7%.

Method for preparing light olefin through catalytic syngas with high selectivity by heteroatom-doped zeolite

A supported catalyst for preparing light olefin using direct conversion of syngas is a composite catalyst and formed by compounding component I and component II in a mechanical mixing mode. The active ingredient of component I is a metal oxide; and the component II is a supported zeolite. A carrier is one or more than one of hierarchical pores AlO, SiO, TiO, ZrO, CeO, MgO and GaO; the zeolite is one or more than one of CHA and AEI structures; and the load of the zeolite is 4%-45% wt. A weight ratio of the active ingredients in the component I to the component II is 0.1-20. The reaction process has an extremely high light olefin selectivity; the sum of the selectivity of the light olefin comprising ethylene, propylene and butylene can reach 50-90%, while the selectivity of a methane side product is less than 7%.

Supported catalyst and method for preparing light olefin using direct conversion of syngas

A catalyst containing LF-type B acid preparing ethylene using direct conversion of syngas is a composite catalyst and formed by compounding component A and component B in a mechanical mixing mode. The active ingredient of the component A is a metal oxide; the component B is a zeolite of MOR topology; and a weight ratio of the active ingredients in the component A to the component B is 0.1-20. The reaction process has an extremely high product yield and selectivity, with the selectivity for light olefin reaching 80-90%, wherein ethylene has high space time yield and can reach selectivity of 75-80%. Meanwhile, the selectivity for a methane side product is extremely low (&#x3c;15%).

Catalyst containing LF-type B acid and method for preparing ethylene using direct conversion of syngas

A catalyst for preparing light olefin using direct conversion of syngas is a composite catalyst and formed by compounding component I and component II in a mechanical mixing mode. The active ingredient of component I is a metal oxide; and the component II is one or more than one of zeolite of CHA and AEI structures or metal modified CHA and/or AEI zeolite. A weight ratio of the active ingredients in the component I to the component II is 0.1-20. The reaction process has high product yield and selectivity, wherein the sum of the selectivity of the propylene and butylene reaches 40-75%; and the sum of the selectivity of light olefin comprising ethylene, propylene and butylene can reach 50-90%. Meanwhile, the selectivity of a methane side product is less than 15%.

Catalyst and method for preparing light olefin using direct conversion of syngas

An organic base modified composite catalyst for producing ethylene by hydrogenation of carbon monoxide is a composite catalyst and formed by compounding component I and component II in a mechanical mixing mode. The active ingredient of the component I is a metal oxide; the component II is an organic base modified zeolite of MOR topology; and a weight ratio of the active ingredients in the component I to the component II is 0.1-20, and preferably 0.3-8. The reaction process has an extremely high product yield and selectivity. The selectivity of C-Colefins is as high as 78-87%; the selectivity of hydrocarbon products with more than 4 C atoms is less than 10%; the selectivity of a methane side product is extremely low (&#x3c;9%); and meanwhile, the selectivity of the ethylene is 75-82%.

Organic base modified composite catalyst and method for producing ethylene by hydrogenation of carbon monoxide

Direct conversion of syngas produces liquid fuels and light olefins. The catalytic reaction is conducted on a fixed bed or a moving bed. The catalyst comprises A and B components. The component A is composed of active metal oxides, and the active ingredients of the component B are zeolites with a MEL structure. The distance between the geometric centers of catalyst A and catalyst B particles is 2 nm-10 mm; a weight ratio of the catalyst A to the catalyst B is 0.1-20. The pressure of the syngas is 0.1-10 MPa; reaction temperature is 300-600&#xb0; C.; and space velocity is 300-10000 h. The reaction mainly produces gasoline with high octane number, and co-generates light olefins. Meanwhile, the selectivity for a methane byproduct is low (less than 10%).

Catalyst and method for preparing liquid fuel and light olefins by direct conversion of syngas

A process for direct synthesis of light olefins uses syngas as the feed raw material. This catalytic conversion process is conducted in a fixed bed or a moving bed using a composite catalyst containing components A and B (A+B). The active ingredient of catalyst A is metal oxide; and catalyst B is an oxide supported zeolite. A carrier is one or more of AlO, SiO, TiO, ZrO, CeO, MgO and GaOhaving hierarchical pores; the zeolite is one or more of CHA and AEI structures. The loading of the zeolite is 4%-45% wt. A weight ratio of the active ingredients in the catalyst A and the catalyst B is within a range of 0.1-20, and preferably 0.3-5. The total selectivity of the light olefins comprising ethylene, propylene and butylene can reach 50-90%, while the selectivity of a methane byproduct is less than 15%.

Catalyst and method for preparing light olefins by direct conversion of syngas

A zeolitic material having framework type CHA, comprising a transition metal M and an alkali metal A, and having a framework structure comprising a tetravalent element Y, a trivalent element X and O, wherein the transition metal M is a transition I metal of groups 7 to 12 of the periodic table, A is one or more of K and Cs, Y is one or more of Si, Ge, Ti, Sn and Zr, and X is one or more of Al, B, Ga and In. A process for preparing such a zeolitic material. Use of such a zeolitic material.

Zeolitic material having framework type CHA and comprising a transition metal and one or more of potassium and cesium

Direct conversion of syngas to light olefins is carried out in a fixed bed or a moving bed reactor with a composite catalyst A+B. The active ingredient of catalyst A is active metal oxide; and catalyst B is one or more than one of zeolite of CHA and AEI structures or metal modified CHA and/or AEI zeolite. A spacing between geometric centers of the active metal oxide of the catalyst A and the particle of the catalyst B is 5 &#x3bc;m-40 mm. A spacing between axes of the particles is preferably 100 &#x3bc;m-5 mm, and more preferably 200 &#x3bc;m-4 mm. A weight ratio of the active ingredients in the catalyst A and the catalyst B is within a range of 0.1-20 times, and preferably 0.3-5.

Catalyst and method for direct conversion of syngas to light olefins

A process for preparing a zeolitic material containing YOand XO, where Y and X represent a tetravalent element and a trivalent element, respectively, is described. The process includes (1) a step of preparing a mixture containing one or more structure directing agents, seed crystals, and a first zeolitic material containing YOand XOand having FAU-, GIS-, MOR-, and/or LTA-type framework structures; and (2) a step of heating the mixture for obtaining a second zeolitic material containing YOand XOand having a different framework structure than the first zeolitic material. The mixture prepared in (1) and heated in (2) contains 1000 wt % or less of HO based on 100 wt % of YOin the framework structure of the first zeolitic material. A zeolitic material obtainable and/or obtained by the process and its use are also described.

Process for the production of a zeolitic material via solvent-free interzeolitic conversion

A reactor configuration comprises an inlet section I, a preheating section II, a transition section III, a reaction section IV and an outlet section V; except for the preheating section II and the reaction section IV, the existence of the inlet section I, the transition section III and the outlet section V depends on reaction conditions; and the process realizes no coke deposition synthesis of methane and high selectivity synthesis of ethylene. The methane conversion rate is 20-90%; ethylene selectivity is 65-95%; propylene and butylene selectivity is 5-25%; aromatic hydrocarbon selectivity is 0-30%; and coke deposition is zero.

Catalytic reactor configuration, preparation and method of direct synthesis of ethylene through oxygen-free catalysis of methane

Synthesis of aromatic hydrocarbons from synthesis gas in a fixed bed or a moving bed reactor loaded with a composite catalyst comprising Catalyst Component A and Catalyst Component B mixed via a mechanical mixing mode, wherein the active ingredient of the Catalyst Component A is active metal oxides; and the Catalyst Component B is one or both of ZSM-5 zeolite and metal modified ZSM-5; the pressure of the synthesis gas is 0.1-6 MPa; the reaction temperature is 300-600&#xb0; C.; and the space velocity is 500-8000 h. The reaction process has a high product yield and selectivity, with the selectivity of aromatics reaching 50-85%, while the selectivity of the methane byproduct is less than 15%.

Catalyst and method for synthesis of aromatic hydrocarbons through direct conversion of synthesis gas

The present invention discloses catalyst and method for producing light olefins directly from synthesis gas by a one-step process, and particularly relates to method and catalyst for directly converting synthesis gas into light olefins by a one-step process. The provided catalysts are composite materials formed of multicomponent metal oxide composites and inorganic solid acids with hierarchical pore structures. The inorganic solid acids have a hierarchical pore structure having micropores, mesopores and macropores. The metal composites can be mixed with or dispersed on surfaces or in pore channels of the inorganic solid acid and can catalyze the synthesis gas conversion to a C-Clight hydrocarbon product containing two to four carbon atoms. The single pass conversion of CO is 10%-60%. The selectivity of light hydrocarbon in all hydrocarbon products can be up to 60%-95%, wherein the selectivity of light olefins (C&#x2014;C) is 50%-85%.

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Dalian, China

Xiulian Pan