A method is provided for removing tar from a gas by contacting a first gas containing tar with a second gas containing oxygen for time period sufficient to effect oxidation of at least a portion of the tar in the first gas, thus producing an oxidized product gas that contains less tar than the first gas. The method can also include heating a fluidized particulate material in a combustor, introducing the heated fluidized particulate material from the combustor and a biomass feedstock into a gasifier, such that heat from the heated fluidized particulate material causes the gasification of at least a portion of the biomass feedstock to form a tar-containing product gas, the first gas may contain at least a portion of the tar-containing gas, and the tar-containing gas may be extracted from the gasifier prior to contacting the first gas with the second gas.

A system includes a first reactor that may gasify a first feed to generate a first syngas. The first feed has a first particle size distribution (PSD.sub.1). The system also includes a second reactor that may receive the first feed, a second feed, and at least a portion of the first syngas. The second reactor may gasify the second feed to generate additional syngas, and the second feed has a second particle size distribution (PSD.sub.2) that is different from the first PSD. The second reactor includes an elutriation zone disposed on a first end of the second reactor. The elutriation zone may receive the first and second feed. The second reactor also includes a fluidized bed disposed at a second end of the second reactor that is substantially opposite the first end. The fluidized bed is fluidly coupled to the first reactor and may receive the portion of the first syngas via a syngas inlet. The system also includes a gas-solids separation section fluidly coupled to the first and second reactors. The gas-solids separation section may receive the first feed and partially reacted particles of the second feed from the elutriation zone and may feed a combined feed consisting of the first feed and the partially reacted particles of the second feed to the first reactor.

A system for the pyrolysis of a pyrolysis feedstock utilizes a pyrolysis reactor for producing pyrolysis products from the pyrolysis feedstock to be pyrolyzed. An eductor condenser unit in fluid communication with the pyrolysis reactor is used to condense pyrolysis gases. The eductor condenser unit has an eductor assembly having an eductor body that defines a first flow path with a venturi restriction disposed therein for receiving a pressurized coolant fluid and a second flow path for receiving pyrolysis gases from the pyrolysis reactor The second flow path intersects the first flow path so that the received pyrolysis gases are combined with the coolant fluid. The eductor body has a discharge to allow the combined coolant fluid and pyrolysis gases to be discharged together from the eductor. A mixing chamber in fluid communication with the discharge of the eductor to facilitates mixing of the combined coolant fluid and pyrolysis gases, wherein at least a portion of the pyrolysis gases are condensed within the mixing chamber.

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.

A gasifier start-up method for a gasifier capable of preventing or inhibiting a temporary occurrence of black smoke when a gasifier is started-up. A gasifier start-up method for a gasifier, in which a gasifying agent and a solid carbonaceous fuel are supplied and gasified, includes a start-up burner igniting step of supplying a start-up fuel and oxygen-containing gas to a start-up burner and igniting the start-up fuel and oxygen-containing gas, under an inert atmosphere in which an inside of the gasifier around the start-up burner is filled with inert gas; and an oxygen-containing-gas supply adjusting step of adjusting the supply of the oxygen-containing gas such that combustion gas obtained after the combustion reaction of the start-up fuel and the oxygen-containing gas becomes the inert gas, which contains little oxygen.

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 fluidized bed biogasifier is provided for gasifying biosolids. The biogasifier includes a reactor vessel and a feeder for feeding biosolids into the reactor vessel at a desired feed rate during steady-state operation of the biogasifier. A fluidized bed in the base of the reactor vessel has a cross-sectional area that is proportional to at least the fuel feed rate such that the superficial velocity of gas is in the range of 0.1 m/s (0.33 ft/s) to 3 m/s (9.84 ft/s). In a method for gasifying biosolids, biosolids are fed into a fluidized bed reactor. Oxidant gases are applied to the fluidized bed reactor to produce a superficial velocity of producer gas in the range of 0.1 m/s (0.33 ft/s) to 3 m/s (9.84 ft/s). The biosolids are heated inside the fluidized bed reactor to a temperature range between 900° F. (482.2° C.) and 1700° F. (926.7° C.) in an oxygen-starved environment having a sub-stoichiometric oxygen level, whereby the biosolids are gasified.

A solids discharge system (SDS) is configured to separate solids from product gas. The system includes a solids separation device and at least one solids transfer conduit configured to receive solids from the solids separation device. The solids transfer conduit is selectively partitioned into a plurality of compartments (or “sections”) along its length by isolation valves. A gas supply conduit and a gas discharge conduits are connected to one of the sections to facilitate removal of solids. A filter in fluid communication with that section is configured to prevent solids from passing through the gas discharge conduit so that the solids can be removed from one of the sections of the solids transfer conduit. A product gas generation system incorporates first and second reactors, the latter of which receives products created by the second reactor.

The present disclosure provides a method and an apparatus for integrating pressurized hydrocracking of heavy oil and coke gasification. A coupled reactor having a cracking section and a gasification section is used in the method: a heavy oil feedstock and a hydrogenation catalyst are fed into a cracking section, to generate light oil-gas and coke; the coke is carried by the coke powder into the gasification section, to generate syngas; a regenerated coke powder is returned to the cracking section; the syngas enters the cracking section and merges with light oil-gas, and enters a gas-solid separator, to separate out first-stage solid particles and second-stage particles in sequence, and a purified oil-gas product is collected; oil-gas fractionation of the purified oil-gas product is performed, and a light oil product and a syngas product are collected. Yield and quality of the light oil can be improved by the method.

It is provided a method of converting a carbonaceous material into syngas at a carbon conversion rate of at least 78% comprising gasifying the carbonaceous material in a fluidized bed reactor producing a crude syngas, classifying the crude syngas by particle size and density into a cut sizing device, introducing the classified particle crude syngas into a thermal reformer and reforming the classified crude syngas at a temperature above mineral melting point, producing the syngas.