A system and method for processing unconditioned syngas first removes solids and semi -volatile organic compounds (SVOC), then removes volatile organic compounds (VOC), and then removes at least one sulfur containing compound from the syngas. Additional processing may be performed depending on such factors as the source of syngas being processed, the products, byproducts and intermediate products desired to be formed, captured or recycled and environmental considerations.

The high efficiency supercritical carbon dioxide power generation system and the method therefor according to the present invention comprises: a hydrogen separation unit for receiving a gaseous fuel and separating the same into carbon monoxide and hydrogen; a combustion processing unit for receiving carbon monoxide and non-condensing gas discharged from the hydrogen separation unit to generate combustion gas; a carbon dioxide high purity unit for separating carbon dioxide from the combustion gas discharged from the combustion processing unit; a compression unit for pressurizing the carbon dioxide discharged from the carbon dioxide high purity unit; and a turbine unit for receiving the pressurized carbon dioxide from the compression unit to generate electricity, wherein the carbon dioxide discharged from the turbine unit may be supplied to the combustion processing unit again.

Processes for producing high biogenic concentration Fischer-Tropsch liquids derived from the organic fraction of municipal solid wastes (MSW) feedstock that contains a relatively high concentration of biogenic carbon (derived from plants) and a relatively low concentration of non-biogenic carbon (derived from fossil sources) wherein the biogenic content of the Fischer-Tropsch liquids is the same as the biogenic content of the feedstock.

Processes for producing high biogenic concentration Fischer-Tropsch liquids derived from the organic fraction of municipal solid wastes (MSW) feedstock that contains a relatively high concentration of biogenic carbon (derived from plants) and a relatively low concentration of non-biogenic carbon (derived from fossil sources) wherein the biogenic content of the Fischer-Tropsch liquids is the same as the biogenic content of the feedstock.

This invention is directed to novel mixed transition metal iron (II/III) catalysts for the extraction of oxygen from CO.sub.2 and the selective reaction with organic compounds.

The present invention provides a process for producing one or more products for use as a transportation or heating fuel. In various embodiments the process comprises treating a cellulosic feedstock in one or more processing steps that release extractives from the feedstock. A solids-liquid separation is subsequently conducted on the process stream comprising the extractives and solids. An aqueous stream comprising one or more of the extractives may be fed to an anaerobic digester to produce crude biogas from which one or more impurities may optionally be removed. In various embodiments the process further comprises providing a solids stream to a thermal process. A product produced or derived from the thermal process may displace a product made from fossil fuel. One or more products obtained or derived from at least one of the foregoing process steps are provided for use as a transportation or heating fuel. In various embodiments the process enables advantaged fuel credit generation.

The present disclosure provides a process for forming a biogenic carbon-based fuel or a fuel intermediate from biogenic carbon dioxide and hydrogen. At least a portion of the biogenic carbon dioxide and hydrogen is subjected to a reverse water gas shift reaction that produces at least carbon monoxide. The carbon monoxide so produced, the biogenic carbon dioxide and the hydrogen are introduced, together or separately, to a biologic or chemical conversion process to produce the fuel or fuel intermediate.

Disclosed are a quick-start system for preparing hydrogen via aqueous methanol, and hydrogen preparation method. The system comprises a liquid storage container, a raw material feeding device, a quick-start device, a hydrogen preparation equipment and a membrane separation device; the quick-start device comprises a first start device and a second start device; the first start device comprises a first heating mechanism and a first gasification pipeline, the first gasification pipeline is wound around the first heating mechanism; one end of the first gasification pipeline is connected to the liquid storage container, and methanol is fed into the first gasification pipeline via the raw material feeding device, for the first heating mechanism to heat and gasify; the hydrogen preparation equipment comprises a reforming chamber; the second start device comprises a second gasification pipeline, a main body of the second gasification pipeline is disposed in the reforming chamber; the methanol output by the first gasification pipeline and/or the second gasification pipeline heats the second gasification pipeline while heating the reforming chamber, to gasify the methanol in the second gasification pipeline. The present invention can be quickly started, while having less energy consumption and good practicability.

Novel redox based systems for fuel and chemical production with in-situ CO.sub.2 capture are provided. A redox system using one or more chemical intermediates is utilized in conjunction with liquid fuel generation via indirect Fischer-Tropsch synthesis, direct hydrogenation, or pyrolysis. The redox system is used to generate a hydrogen rich stream and/or CO.sub.2 and/or heat for liquid fuel and chemical production. A portion of the byproduct fuels and/or steam from liquid fuel and chemical synthesis is used as part of the feedstock for the redox system.

The invention relates to a process for the catalytic cracking of a gasoline feedstock for the production of light olefins, in which said gasoline feedstock is brought into contact with a catalyst comprising at least one zeolite NU-86, alone or in a mixture with at least one other zeolite, at a temperature comprised between 500 and 700 C., at an absolute pressure comprised between 10 and 60 MPa, and with a contact time of the feedstock on said catalyst comprised between 10 milliseconds and 100 seconds.