Abstract: A gasifier includes a combustion zone where a gas is introduced and fuel is combusted and at least one sensor for measuring a predetermined condition in the gasifier. A grate subsystem contains the fuel and includes at least one grinding mechanism. A controller is responsive to the at least one sensor and controls the grinding mechanism by activating the grinding mechanism if the predetermined condition exists to reduce the collection of non-fuel products on the grate subsystem.

Abstract: A method of producing substitute natural gas (SNG) includes providing at least one steam turbine engine. The method also includes providing a gasification system that includes at least one gas shift reactor configured to receive a boiler feedwater stream and a synthesis gas (syngas) stream. The at least one gas shift reactor is further configured to produce a high pressure steam stream. The method further includes producing a steam stream within the at least one gas shift reactor and channeling at least a portion of the steam stream to the at least one steam turbine engine.

Abstract: A gasifier is disclosed. The gasifier may include a housing and a refractory system contained within the housing. The refractory system may comprise an upper manifold, an intermediate portion, and a lower manifold. The refractory system may also include columnar cavities. The columnar cavities may extend vertically through the intermediate portion and place the upper manifold in communication with the lower manifold.

Abstract: A micro reforming reactor includes a first substrate with a micro channel having a width of less than 1,000 ?m bonded to a second substrate to form a micro tunnel. An adhesive layer is formed on the internal walls of the micro tunnel using a flow coating method. A catalyst may then be optionally formed on the adhesive coated internal walls of the micro tunnel, also using a flow coating method.

Abstract: Disclosed is a cyclonic gasifier and cyclonic gasification method. The cyclonic gasifier and cyclonic gasification method involve a chamber having a first portion proximal to a first end and a second portion proximal to a second end, introducing a first fuel to the first portion of the chamber, introducing a second fuel to the chamber; and introducing a first oxidant to accelerate the velocity of the first fuel and swirl the first fuel from the first portion toward the second portion.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A hydrogen manufacturing system for performing offgas flow control includes: a vaporizer (1) for heating a material mixture containing a hydrocarbon material; a reforming reactor (2) for generating hydrogen-containing reformed gas by reforming reactions of the material; a PSA separator (5) for repeating a cycle of adsorption and desorption, where in the adsorption PSA separation is performed with an adsorption tower loaded with an adsorbent to adsorb unnecessary components in the reformed gas and extract hydrogen-enriched gas out of the tower, and in the desorption the offgas containing the unnecessary components from the adsorbent and remaining hydrogen is discharged from the tower; and a buffer tank (6) for holding the offgas before supplying to the vaporizer. The offgas flow supply from the tank (6) to the vaporizer is changed continuously over time when the cycle time is changed according to load change on the separator (5).

Abstract: In a reactor for gasification of entrained solid and liquid fuels at temperatures between 1,200 and 1,900° C. and at pressures between ambient pressure and 10 MPa using an oxidizing agent containing free oxygen, the cooling screen is connected to the pressure shell in a gastight manner via a sliding seal in order to allow length changes. Continuous gas purging of the annular gap between pressure shell and cooling screen is unnecessary and gasification gas is prevented from flowing behind.

Abstract: In a reactor for the gasification of solid and liquid fuels in the entrained flow at temperatures between 1200 and 1900° C. and pressures between ambient pressure and 10 MPa with an oxidizing agent containing free oxygen, the cooling screen is connected in a gas-tight manner to the pressure shell via a bellows compensator to accommodate linear deformation. Continuous sweeping by gas of the annular gap between pressure shell and cooling screen is unnecessary and backflow by producer gas is prevented.

Abstract: A reactor vessel includes a dipleg connecting a tubular syngas collection chamber and a quench chamber. The collection chamber connects to the dipleg via a slag tap having a frusto-conical part starting from the lower end of the collection chamber and diverging to an opening connected to an interior of the dipleg. The slag tap has a first tubular part connected to the opening of the frusto-conical part and extending in the direction of the dipleg. A second tubular part connects to the frusto-conical part or to the tubular part and extends toward the dipleg. The second tubular part is spaced away from the dipleg to provide an annular space having a discharge conduit. The discharge conduit has a discharge opening located to direct water along the inner wall of the dipleg. At least half of the vertical length of the first tubular part extends below the discharge opening.

Abstract: In certain embodiments, a system includes a gasification system configured to output grey water. The system also includes a grey water zero liquid discharge (ZLD) system configured to receive the grey water and to generate a first stream of distillate. The grey water ZLD system comprises an ammonia stripping system. An amount of water into and out of the grey water ZLD system is approximately equal.

Abstract: A reactor for the recovery of carbon and hydrocarbons from organic input material through pyrolysis includes a vessel with a chamber that is limited outwardly by an outer jacket and by an upper and a lower end-wall section, and in which chamber input material in fragmented form is to be placed; an inlet which for the introduction of heated inert gas into the chamber for passage through the input material comprises several inlet units arranged in areas in the chamber; and an outlet which for the passage out from the chamber of gas that has passed through the input material that has been placed in the chamber comprises number of outlet units arranged in areas in the chamber.

Abstract: An object of the present invention is to provide a reforming apparatus and the like capable of uniformly mixing water (steam) and a raw material together, of preventing the precipitation of carbon without using a temperature controller, and of efficiently heating the water and the mixture by heating gas. Accordingly, the reforming apparatus has the following configuration. The reforming apparatus includes: a first vaporizer (05) that is cylindrically shaped and includes a first flow passage; a second vaporizer (06) that is cylindrically shaped and includes a second flow passage; a duct (027) that connects an outlet of the first flow passage to an inlet of the second flow passage; a raw-material mixing portion (028) formed at a certain point of the duct. The first vaporizer and the second vaporizer are concentrically disposed. An interstice between the first vaporizer and the second vaporizer serves as a heating-gas flow passage (024).

Abstract: A method of producing substitute natural gas (SNG) includes providing a gasification reactor having a cavity defined at least partially by a first wall. The reactor also includes a first passage defined at least partially by at least a portion of the first wall and a second wall, wherein the first passage is in heat transfer communication with the first wall. The reactor further includes a second passage defined at least partially by at least a portion of the second wall and a third wall. The method also includes coupling the cavity in flow communication with the first and second passages. The method further includes producing a first synthetic gas (syngas) stream within the cavity. The method also includes channeling at least a portion of the first syngas stream to the first and second passages.

Abstract: Methods and systems for a gasifier having a partial moderator bypass are provided. The gasifier includes a partial oxidation reactor including an inlet and an outlet and a primary reaction zone extending therebetween, the partial oxidation reactor configured to direct a flow of products of partial oxidation including fuel gases, gaseous byproducts of partial oxidation, and unburned carbon, and a secondary reaction chamber coupled in flow communication with the partial oxidation reactor, the secondary reaction chamber is configured to mix a flow of moderator with the flow of gaseous byproducts of partial oxidation and unburned carbon such that a concentration of fuel gases is increased.

Abstract: A process for preparation of synthesis gas and/or hydrogen by counter-currently providing an oxidation reactant stream through an oxidation chamber and a reforming reactant stream through a steam reforming chamber is described. Also provided is a reactor for conducting the reaction.

Abstract: A process and device for the material utilization of soot from the waste water of a gasification appliance (heavy oil POX) in which a hydrogen- and carbon monoxide-containing (crude synthesis gas) is generated from relatively high-boiling hydrocarbons by partial oxidation, is disclosed. The soot-loaded waste water from the heavy oil POX is mixed with naphtha and is subsequently introduced into a separator (decanter) from which a substantially soot-free water fraction and a substantially water-free naphtha/soot mixture are taken off separately, where the naphtha/soot mixture is fed as feed to a further gasification appliance (naphtha POX), in which appliance predominantly naphtha is converted into a crude synthesis gas by partial oxidation.

Abstract: A controlled zone gasification reactor with an agitator drive assembly for a plasma assisted gasification reaction system is disclosed for converting fuel, such as, but not limited to, biomass, to syngas to replace petroleum based fuels used in power generation. The agitator drive assembly that prevents formation of burn channels with in the fuel. The agitator drive assembly may include a syngas separation chamber configured to produce clean syngas, thereby requiring less filtering. The syngas separation chamber may feed syngas downstream to a syngas heater in a pyrolysis reaction zone in the reactor vessel.

Abstract: A controlled zone gasification reactor for a plasma assisted gasification reaction system is disclosed for converting fuel, such as, but not limited to, biomass, to syngas to replace petroleum based fuels used in power generation. The system may be a modular system housed within a frame facilitating relatively easy transportation. The system may include a reactor vessel with distinct reaction zones that facilitate greater control and a more efficient system. The system may include a syngas heater channeling syngas collected downstream of the carbon layer support and to the pyrolysis reaction zone. The system may also include a syngas separation chamber configured to produce clean syngas, thereby requiring less filtering. The system may further include an agitator drive assembly that prevents formation of burn channels with in the fuel.

Abstract: Biomass gasification systems including a biofilter assembly adapted to be disposed within a filter unit of a biomass gasification system are provided. The biofilter assemblies may be adapted to filter particulate matter from a producer gas flowing through the filter unit while allowing a remainder of the producer gas to pass through the biofilter assembly. The biofilter assembly may include a support structure and a biofilter disposed on the support structure and including a biomaterial adapted to be gasified in a biomass gasification reactor of the biomass gasification system.

Abstract: The disclosed embodiments provide systems for the removal and use of tar from a biomass gasification system. For example, in one embodiment, a biomass gasification system includes a reactor configured to gasify a biomass fuel in the presence of air to generate a producer gas. The system also includes an absorber configured to receive a mixture of the producer gas and tar and to absorb the tar into an organic solvent to produce treated producer gas and a rich solvent mixture containing at least a portion of the tar. The system further includes a recycle line configured to direct the rich solvent mixture to a biomass gasifier.

Abstract: An apparatus and method for starved air gasification of solid organic materials, including biomass and other wastes, to convert the chemical energy stored in such materials to thermal energy or gaseous products that may be used in biochemical and/or chemical synthesis. Specifically, the system utilizes a gasifier having a “moving bed of ash” hearth wherein the feedstock is partially oxidized at a low temperature (less than 1500 degrees F.) in a square or rectangular chamber having a vaulted, tapered or flat roof.

Abstract: A gas-generating apparatus (10) includes a reaction chamber (18) containing a solid fuel component (24) and a liquid fuel component (22) that is introduced into the reaction chamber by a fluid path, such as a tube, nozzle, or valve. The flow of the liquid fuel to the solid fuel is self-regulated. Other embodiments of the gas-generating apparatus are also disclosed.

Abstract: A hydrogen manufacturing system for performing offgas flow control includes: a vaporizer (1) for heating a material mixture containing a hydrocarbon material; a reforming reactor (2) for generating hydrogen-containing reformed gas by reforming reactions of the material; a PSA separator (5) for repeating a cycle of adsorption and desorption, where in the adsorption PSA separation is performed with an adsorption tower loaded with an adsorbent to adsorb unnecessary components in the reformed gas and extract hydrogen-enriched gas out of the tower, and in the desorption the offgas containing the unnecessary components from the adsorbent and remaining hydrogen is discharged from the tower; and a buffer tank (6) for holding the offgas before supplying to the vaporizer. The offgas flow supply from the tank (6) to the vaporizer is changed continuously over time when the cycle time is changed according to load change on the separator (5).

Abstract: The invention has its object to arbitrarily adjust an amount of particles to be circulated without changing a flow rate of a gasification agent to thereby enhance gasification efficiency in a fluidized bed gasification furnace. The fluidized bed gasification furnace 107 comprises first and second chambers 113 and 114 in communication with each other in a fluidized bed 105. The hot particles 102 separated in the separator 104 and raw material M are introduced into the first chamber 113. The particles 102 introduced from the first chamber 113 through interior in the fluidized bed 105 to the second chamber 114 are supplied in an overflow manner to the fluidized bed combustion furnace 100.

Abstract: Hydrogen-producing fuel processing systems, hydrogen purification membranes, hydrogen purification devices, fuel processing and fuel cell systems that include hydrogen purification devices, and methods for operating the same. In some embodiments, operation of the fuel processing system is initiated by heating at least the reforming region of the fuel processing system to at least a selected hydrogen-producing operating temperature. In some embodiments, an electric heater is utilized to perform this initial heating. In some embodiments, use of the electric heater is discontinued after startup, and a burner or other combustion-based heating assembly combusts a fuel to heat at least the hydrogen producing region, such as due to the reforming region utilizing an endothermic catalytic reaction to produce hydrogen gas.

Abstract: A quench ring for use with a gasifier system. The quench ring including an annular manifold having a radius, an annular channel coupled in flow communication with said manifold, and at least one inlet coupled in flow communication with said manifold, said at least one inlet having a center line aligned substantially tangentially to said annular manifold.

Abstract: A fixed bed coal gasifier (300) includes a coal gasification chamber with a coal lock above the chamber. A static coal distribution device inside the gasification chamber includes a hollow coal distributor which flares downwardly outwardly with a skirt depending downwardly from an inside of the coal distributor so that a gas collection zone is defined between the skirt and the coal distributor. The gasifier (300) has an ash discharge outlet (606) and a rotatable grate (600) above the outlet (606). The rotatable grate (600) includes at least one upwardly projecting finger or disturbing formation (500) to disturb the ash bed formed in use above and around the grate (600).

Abstract: A gasification reactor vessel comprising a combustion chamber in the upper half of the vessel, provided with a product gas outlet at the bottom end of the combustion chamber, at least two burner openings are present in the wall of the combustion chamber, which burner openings are located at the same horizontal level and are positioned diametrical relative to each other and wherein in each burner opening a burner is present, wherein between the wall of the combustion chamber and the wall of vessel an annular space is provided, wherein the wall of the combustion chamber comprises an arrangement of interconnected tubes (vertical arranged or helical coiled), wherein the product gas outlet at the bottom end of the combustion chamber is fluidly connected to a dip-tube, which partly is submerged in a water bath located at the lower end of the reactor vessel, and wherein at the upper end of the dip-tube means are present to add a quenching medium to the, in use, downwardly flowing mixture of hydrogen and carbon monox

Abstract: A method of cooling hot fluid flowing through a chamber is provided. The method includes channeling cooling fluid through at least one cooling tube that extends through a passage of the chamber, and circulating the hot fluid flowing within the passage around the at least one cooling tube using at least one fluid diverter.

Abstract: A process of generating power utilizing a low level heat from a raw syngas produced in a quench gasifier is disclosed. The process includes a first stage that includes: producing raw syngas at the quench gasifier, making 150 psi saturated steam from the produced raw syngas, superheating the saturated steam, and using the superheated saturated steam in a low pressure steam turbine to generate power. The process includes a second stage that includes: providing the raw syngas and a process condensate stream to a thermal fluid vaporizer to vaporize an organic thermal fluid, and using the vaporized organic thermal fluid in an expander turbine to generate power via an organic Rankine cycle.

Abstract: A gas-generating apparatus includes a reaction chamber having a first reactant, a reservoir having an optional second reactant, and a self-regulated flow control device. The self-regulated flow control device stops the flow of reactant from the reservoir to the reaction chamber when the pressure of the reaction chamber reaches a predetermined level. Methods of operating the gas-generated apparatus and the self-regulated flow control device, including the cycling of a shut-off valve of the gas-generated apparatus and the cycling of the self-regulated flow control device are also described.

Abstract: In a retrofit system for hot solids combustion and gasification, a chemical looping system includes an endothermic reducer reactor 12 having at least one materials inlet 22 for introducing carbonaceous fuel and CaCO3 therein and a CaS/gas outlet 26. A first CaS inlet 40 and a first CaSO4 inlet 64 are also defined by the reducer reactor 12. An oxidizer reactor 14 is provided and includes an air inlet 68, a CaSO4/gas outlet 46, a second CaS inlet 44, and a second CaSO4 inlet 66. A first separator 30 is in fluid communication with the CaS/gas outlet 26 and includes a product gas and a CaS/gas outlet 32 and 34 from which CaS is introduced into said first and second CaS inlets. A second separator 50 is in fluid communication with the CaSO4/gas outlet 46 and has an outlet 52 for discharging gas therefrom, and a CaSO4 outlet from which CaSO4 is introduced into the first and second CaSO4 inlets 62, 66.

Abstract: A method for using a downdraft gasifier comprising a housing and a refractory stack contained within the housing. The refractory stack may comprise various sections. Apertures in the sections may be aligned to form multiple columnar cavities. Each columnar cavity may comprise an individual oxidation zone. The method of use may include the steps of placing a feedstock into an upper portion of the refractory stack, measuring the temperature of each columnar cavity, and adjusting the flow of oxygen to a particular columnar cavity to maintain the temperature of the particular columnar cavity within a particular range.

Abstract: A downdraft gasifier (1) has an oxidant inlet (3), a biomass injector (2), a grate (9), a gas exit port (7), and an ash removal system (11). A sensor (10) maintains the height of the bed and a rotating paddle (5) maintains the top of the bed (4) at an even height. The grate arrangement (9) is preferably a sliding grate arrangement which actively moves ash material through the grate. An in-bed oxidant distributor (6) injects oxidant within the bed.

Abstract: A biomass thermochemical gasification apparatus is provided that can manufacture high-quality fuel gas out of solid biomass in an industrial manner. This fuel gas can be used as fuel for a gas engine and a gas turbine for example and also can be used as synthesis gas for methanol synthesis. A high-temperature combustion gas generation apparatus (101) for biomass operates entirely by biomass and the heat source thereof does not depend on fossil fuel. A coarsely-ground powder biomass (205) subjected to gasification and gasification agent (303) are introduced to a primary gasification reaction room (202) and generate gasification reaction by, as reaction heat, radiation heat from a wall face of the primary gasification reaction room (202) heated by combustion gas (109a) generated in the high-temperature combustion gas generation apparatus (101) and are dissolved. Consequently, the biomass (205) is converted to clean and high-quality generated gas.

Abstract: A system and process for gasifying carbonaceous feedstock with staged slurry addition in order to prevent the formation of tar that causes deposition problems. Dry solid carbonaceous material is partially combusted, then pyrolyzed along with a first slurry stream comprising carbonaceous material in two separate reactor sections, thereby producing mixture products comprising synthesis gas. The second slurry stream comprising particulate carbonaceous material is fed to a drying unit downstream of a heat recovery zone along with the mixture product exiting the heat recovery zone The resulting final temperature of the second stage mixture products and dried particulate carbonaceous material is between 450° F. and 550° F., a temperature range that is typically not conducive to the emission of heavy molecular-weight tar species.

Abstract: An entrained bed gasifier for operation with particulate or liquid fuels is provided. A reaction chamber defined by a cold screen and a quenching chamber connected to the reaction chamber using a crude gas and slag outlet, wherein at least the cold screen is enclosed by a pressure-resistant pressure mantle. The annular gap between the cold screen and pressure jacket may be filled with a fluid, for example, water or heat transfer oil. A rough pressure equalization between the gasification chamber and the annual gap may be guaranteed using a connection between the annular gap and the quenching chamber or the crude gas line, hence the pressure in the gasification chamber normally remains slightly higher than in the inner water jacket.

Abstract: Hydrogen-producing fuel processing systems, hydrogen purification membranes, hydrogen purification devices, fuel processing and fuel cell systems that include hydrogen purification devices, and methods for operating the same. In some embodiments, operation of the fuel processing system is initiated by heating at least the reforming region of the fuel processing system to at least a selected hydrogen-producing operating temperature. In some embodiments, an electric heater is utilized to perform this initial heating. In some embodiments, use of the electric heater is discontinued after startup, and a burner or other combustion-based heating assembly combusts a fuel to heat at least the hydrogen producing region, such as due to the reforming region utilizing an endothermic catalytic reaction to produce hydrogen gas.

Abstract: A system and process are disclosed for the controlled combustion of a wide variety of hydrocarbon feedstocks to produce thermal energy, liquid fuels, and other valuable products with little or no emissions. The hydrocarbon feeds, such as coal and biomass, are first gasified and then oxidized in a two-chamber system/process using pure oxygen rather than ambient air. A portion of the intermediate gases generated in the system/process are sent to a Fischer-Tropsch synthesis process for conversion into diesel fuel and other desired liquid hydrocarbons. The remaining intermediate gases are circulated and recycled through each of the gasification/oxidation chambers in order to maximize energy production. The energy produced through the system/process is used to generate steam and produce power through conventional steam turbine technology.

Abstract: Methods and systems for a gasifier having a partial moderator bypass are provided. The gasifier includes a partial oxidation reactor including an inlet and an outlet and a primary reaction zone extending therebetween, the partial oxidation reactor configured to direct a flow of products of partial oxidation including fuel gases, gaseous byproducts of partial oxidation, and unburned carbon, and a secondary reaction chamber coupled in flow communication with the partial oxidation reactor, the secondary reaction chamber is configured to mix a flow of moderator with the flow of gaseous byproducts of partial oxidation and unburned carbon such that a concentration of fuel gases is increased.

Abstract: A system and process for maximizing the generation of marketable products from a variety of hydrocarbon feedstocks. The hydrocarbon feedstocks are first gasified and then oxidized in a two-chamber system and process using oxygen gas rather than ambient air. Intermediate gases generated in the system and process are recirculated and recycled to the gasification and oxidation chambers in order to maximize both energy generation and the resulting stoichiometric reaction products. The energy produced through the system and process is used to generate steam and produce power through conventional steam turbine technology. In addition to the release of heat energy, the hydrocarbon feedstocks are oxidized to the pure product compounds of water and carbon dioxide. The carbon dioxide is subsequently purified and marketed. The water recovered from the system and process is collected and electrolyzed to generate oxygen and hydrogen gases.

Abstract: A method for gasification of fuel in an entrained flow of a gasification reactor. The method includes jointly gasifying a mixture of at least two different fuels having different degrees of coalification, including those of differing coal qualities such as brown coals and stone coals. The method also includes pulverizing the coals forming the mixture in specific grain bands and drying the coals forming the mixture to a specific residual water content.

Abstract: A method for controlling the purity of hydrogen in a reforming apparatus is described where in the apparatus includes a fuel processor, a purification unit and a system controller. The controller determines a calculated flow of reformate from the fuel processor and operates the purification unit based on the calculated flow. The calculated flow is derived from a process model of the fuel processor and known feed(s) to the fuel processor. The calculated flow of reformate is used to control the flow of reformate to adsorbent beds within the purification unit and can be used to control other materials flows within the apparatus. Means for reducing fluctuations in the pressure and/or flow rate of reformate flowing from the fuel processor to the purification unit are also disclosed. The purity of the hydrogen produced can be maintained by adjusting the operation of the purification unit in response to changes in reformate composition, pressure and/or flow rate.

Abstract: A gasifier 10 includes a first chemical process loop 12 having an exothermic oxidizer reactor 14 and an endothermic reducer reactor 16. CaS is oxidized in air in the oxidizer reactor 14 to form hot CaSO4 which is discharged to the reducer reactor 16. Hot CaSO4 and carbonaceous fuel received in the reducer reactor 16 undergo an endothermic reaction utilizing the heat content of the CaSO4, the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and a CO rich syngas. The CaS is discharged to the oxidizer reactor 14 and the syngas is discharged to a second chemical process loop 52. The second chemical process loop 52 has a water-gas shift reactor 54 and a calciner 42. The CO of the syngas reacts with gaseous H2O in the shift reactor 54 to produce H2 and CO2. The CO2 is captured by CaO to form hot CaCO3 in an exothermic reaction.

Abstract: A gasifier and gasifier system based on the gasifier, which contains as a major component, a novel feed system for feeding organic materials into the burn pile of the gasifier. The gasifier feed system is a horizontal auger driven feed system that feeds directly through a ceramic elbow into the furnace without having to auger the feed through significant vertical elevations.

Abstract: A down-draft fixed bed gasifier is disclosed that produced clean producer or synthesis gas. The gasifier can be installed at a stationary location or can be scaled down to enable placing the gasifier on a trailer that can be moved to the site of biomass generation. The gasifier is vertically oriented and generally cylindrical, and the design allows for a continual input of feedstock into the gasifier with less clogging and without lowering the gas pressure inside the gasifier. The design incorporates an internal catalyst to clean tars from the produced gas, and uses heat from the combustion chamber of the gasifier to heat the catalyst. The flow of air may be either positive flow or negative flow.

Abstract: A gas-generating apparatus (10) includes a reaction chamber (18) containing a solid fuel component (24) and a liquid fuel component (22) that is introduced into the reaction chamber by a fluid path, such as a tube, nozzle, or valve. The flow of the liquid fuel to the solid fuel is self-regulated. Other embodiments of the gas-generating apparatus are also disclosed.

Abstract: A method of producing a synthetic gas (syngas) includes injecting a plurality of reactant streams into a gasification reactor via at least one injection device having a plurality of injection annuli, an inner portion that extends annularly about a centerline extending through the at least one injection device, and an outer portion extending substantially annularly about the inner portion. At least a portion of the outer portion is oriented obliquely with respect to the at least one injection device centerline. The method also includes mixing at least a portion of each of the streams together such that a plurality of recirculation zones is defined by the streams. The method further includes producing a syngas within the recirculation zones via mixing at least a portion of each of the streams. The injection device includes an inner portion that extends annularly about a centerline extending through the injection device.

Abstract: A tube and shell heat exchanger for a gasification system is provided. The heat exchanger includes a first shell-side inlet positioned proximate to a heat exchanger tube-side inlet. The first shell-side inlet is configured to receive a first portion of a scrubbed syngas flow therethrough. This first scrubbed syngas portion facilitates substantially preventing fouling at the heat exchanger inlet. The heat exchanger also includes a second shell-side inlet positioned proximate to a heat exchanger tube-side outlet. The second shell-side inlet is configured to receive a second portion of a scrubbed syngas flow therethrough.