A process and apparatus are provided for gasification of a carbonaceous material. The process produces a raw syngas that can be further processed in a tar destruction zone to provide a hot syngas. The process includes contacting said carbonaceous material with molecular oxygen-containing gas in a gasification zone to gasify a portion of said carbonaceous material and to produce a first gaseous product. A remaining portion of the carbonaceous material is contacted with molecular oxygen-containing gas in a burn-up zone to gasify additional portion of the carbonaceous material and to produce a second gaseous product and a solid ash. The first gaseous product and said second gaseous product are combined to produce a raw syngas that includes carbon monoxide (CO), carbon dioxide (CO.sub.2) and tar. The raw syngas is contacted with molecular oxygen containing gas in a tar destruction zone to produce said hot syngas.

A multi-stage product gas generation system converts a carbonaceous material, such as municipal solid waste, into a product gas which may subsequently be converted into a liquid fuel or other material. One or more reactors containing bed material may be used to conduct reactions to effect the conversions. Unreacted inert feedstock contaminants present in the carbonaceous material may be separated from bed material using a portion of the product gas. A heat transfer medium collecting heat from a reaction in one stage may be applied as a reactant input in another, earlier stage.

A pulverized coal gasification furnace with multi-level feeding of high speed circulating gasification agent which includes a pulverized coal gasification furnace and a gasification method. The present invention solves the existing problems in short life of burner, uneven slag deposition on the surface of the gasification device which causes burning and corrosion, and uneven temperature distribution along the height direction. The steps are: 1. setting parameters for the gasification chamber; 2. feeding pulverized coal; 3. burning pulverized coal to form molten slag; 4. gasification process of molten slag inside the gasification furnace; 5. removing slag. In the present invention, the furnace body is divided into different levels for the gasification agent, the internal temperature of the furnace along the height direction is evenly distributed, and the furnace is applicable to the coal types which has severe change in ash viscosity in response to temperature changes.

Combining multiple subsystems involving biomass processing, biomass gasification of the processed biomass where a synthesis gas is produced then converted to hydrogen fuels or other transportation fuels for use in coupled transportation systems sized to consume all the transportation fuel produced. Carbon in the biomass is converted to CO.sub.2 in the conversion process and a portion of that CO.sub.2 is captured and sequestrated for long term storage.

A feedstock conversion system including an integrated two-stage fluid bed thermochemical reaction apparatus (50) has first and second reaction chambers (110, 120) side-by-side and physically separated from one another in one vessel (100) by a partition (130). One or more clusters of heat pipes (400) pass through the partition (130) between the first and second chambers (110, 120) for efficient indirect heat transfer between first and second fluid bed reaction stages (200, 300) and materials therein. The system includes devices for solids transfer between the two reaction chambers (110, 120) to enhance feedstock conversion.

An apparatus is provided that receives waste and generates electrical power or thermal energy with minimal NOx emissions. A gasifier is provided that receives the waste and air to produce fuel gas for delivery to a fluidly coupled reformer. The reformer receives the fuel gas, recycled flue gas, and air to auto-thermally produce a reformed fuel gas and destroy fuel gas pollutants at a first temperature without a catalyst. A burner is fluidly coupled to the reformer and receives recycled flue gas and air to oxidize the reformed fuel gas at a second temperature that prevents nitrogen oxide formation, the second temperature being lower than the first temperature. A quench chamber is fluidly coupled to the burner and receives flue gas from the burner for quenching with recycled flue gas. A heat recovery system is fluidly coupled to the reformer, burner, and quench chamber to extract usable energy.

Processes and systems are provided for converting a carbonaceous feedstock into a reaction gas and a syngas, involving a step of pyrolysing and methanating the feedstock in a pyrolysis chamber to produce the reaction gas and a step of gasifying unconverted feedstock in the presence of a reactant to produce a syngas.

A system and method for producing Syngas from the CO.sub.2 in a gaseous stream, such as an exhaust stream, from a power plant or industrial plant, like a cement kiln, is disclosed. A preferred embodiment includes providing the gaseous stream to pyrolysis reactor along with a carbon source such as coke. The CO.sub.2 and carbon are heated to about 1330° C. and at about one atmosphere with reactants such as steam such that a reaction takes place that produces Syngas, carbon dioxide (CO.sub.2) and hydrogen (H.sub.2). The Syngas is then cleaned and provided to a Fischer-Tropsch synthesis reactor to produce Ethanol or Bio-catalytic synthesis reactor.

The present invention demonstrates a solid fuel grade gasification-combustion dual bed poly-generation system, comprising a combustion system, a gasification system, a synthesized gas cooling and purifying system and a synthesized gas methanization system. The combustion system is connected with the gasification system through a circulating material return system. The gasification system mainly adapts the circulating fluidized-bed combustion mode. The gasification system adapts the fluidized-bed incomplete gasification method and the generated semi-coke is returned to the combustion system for re-utilization. The synthesized gas purifying and cooling unit adapts water cycling and combustible recycling. The by-products, CO.sub.2 and steam, in the methanization unit can be recovered, so the maximum utilization rate of energy in this system is realized.

A temperature measurement system for a gasifier may employ a first stage gasifier with a refractory wall that defines a first stage gasifier volume. A protruding refractory brick may protrude from the first stage refractory wall and into a gaseous flow path of the first stage gasifier volume. The temperature sensor may reside completely through the refractory wall, which may be a plurality of brick layers, except for a tip end of a temperature sensor that may reside in a blind or non-through hole within the protruding refractory brick. The protruding refractory brick protrudes beyond a normal wall surface of the plurality of brick layers that defines the first stage gasifier volume. The protruding refractory brick may have a face that forms an angle that is not 90 degrees, such as 45 degrees, relative to the gaseous flow path of the fluid stream through the first stage gasifier volume.