US20070266914A1 - Method for gasifying solid organic materials and apparatus therefor - Google Patents

Method for gasifying solid organic materials and apparatus therefor Download PDF

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Publication number
US20070266914A1
US20070266914A1 US11/801,030 US80103007A US2007266914A1 US 20070266914 A1 US20070266914 A1 US 20070266914A1 US 80103007 A US80103007 A US 80103007A US 2007266914 A1 US2007266914 A1 US 2007266914A1
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United States
Prior art keywords
gasifier
solid organic
organic materials
opening
providing
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
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US11/801,030
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English (en)
Inventor
Robert Graham
Dejan Sparica
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Nexterra Systems Corp
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Nexterra Energy Corp
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Publication date
Application filed by Nexterra Energy Corp filed Critical Nexterra Energy Corp
Priority to US11/801,030 priority Critical patent/US20070266914A1/en
Priority to PCT/US2007/011965 priority patent/WO2007136786A1/fr
Priority to BRPI0711715-9A priority patent/BRPI0711715A2/pt
Priority to EP07795052A priority patent/EP2032503A4/fr
Priority to CA002649285A priority patent/CA2649285A1/fr
Assigned to NEXTERRA ENERGY CORPORATION reassignment NEXTERRA ENERGY CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SPARICA, DEJAN, GRAHAM, ROBERT G.
Publication of US20070266914A1 publication Critical patent/US20070266914A1/en
Assigned to NEXTERRA SYSTEMS CORP. reassignment NEXTERRA SYSTEMS CORP. CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). Assignors: NEXTERRA ENERGY CORP.
Priority to US12/860,759 priority patent/US20100313796A1/en
Priority to US13/372,061 priority patent/US20120137582A1/en
Abandoned legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/30—Fuel charging devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/10—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of field or garden waste or biomasses
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/12—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of plastics, e.g. rubber
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/70—Incinerating particular products or waste
    • F23G2900/7003—Incinerating litter from animals, e.g. poultry litter
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/12—Heat utilisation in combustion or incineration of waste
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention disclosed and claimed herein deals with a method for gasifying solid organic materials, the novel apparatus for that purpose, and a system therefor.
  • the instant invention is a unique method and apparatus that produces a high energy, low temperature, and low particulate-laden syngas by controlling the oxygen content in combustion air used for “starved air” combustion of biomass in a unique gasifier. Recirculated flue gas mixed with a predetermined amount of fresh air is utilized for providing the oxygen content therein and for controlling the method.
  • this invention deals with a method for gasifying biomass materials, such as forestry and agricultural residues, industrial waste materials such as saw mill pulp, paper products, fowl litter, such as chicken litter and turkey litter, and hydrocarbon based plastics and the like.
  • biomass materials such as forestry and agricultural residues, industrial waste materials such as saw mill pulp, paper products, fowl litter, such as chicken litter and turkey litter, and hydrocarbon based plastics and the like.
  • This invention also deals with the apparatus that is used to convert the chemical energy into thermal energy or gaseous products, and specifically, syngas, that is also called production gas.
  • Syngas is a compressible synthetic combustible gas containing very little particulate material.
  • this invention can also be viewed as a method of producing syngas.
  • biomass materials are now successfully utilized to some extent as fuel in some very large industrial systems, for example, in firing the power boiler and the recovery boiler in a pulp or paper mill.
  • biomass energy recovery systems has precluded their successful use in small or even medium size energy recovery systems.
  • FIG. 1B is a schematic of embodiments of this invention utilizing gasifiers and methods of this invention showing additional portions of the embodiments.
  • FIG. 2 is a full front view of a circular gasifier of this invention.
  • FIG. 5 is a view in perspective of one configuration of a segmented, round cone feed of this invention.
  • FIG. 6 is a view in perspective of one configuration of a segmented, square cone feed of this invention.
  • FIG. 5A is a view in perspective of a unitary, round cone feed of this invention
  • FIG. 6A is a view in perspective of a unitary, square cone feed of this invention.
  • FIG. 7 is a cross sectional view of the area designated 28 of FIG. 3 , showing the detail of the moveable cone feed and the bottom tuyeres.
  • FIG. 8 is a full front view of a square or rectangular, loaf gasifier of this invention.
  • FIG. 10B is a cross sectional view showing another embodiment of this invention and the detailed construction of the walls and roof without insulation and using air as the insulation.
  • FIG. 11 is an enlarged view of a roof of a loaf gasifier of this invention showing two exit ports and how radar is placed thereon.
  • FIG. 12 is a cross sectional view of the roof of FIG. 11 , showing the construction of the roof.
  • FIG. 13 is a top view of the ash collection system of the gasifier of FIG. 8 .
  • FIG. 14 is a side view of a gasifier 1 of this invention with the sides open to show another embodiment of a grate system of this invention.
  • FIG. 15 is a side cross section view of the grates of FIG. 14 through line C-C of FIG. 14 .
  • the sensing device Located at, and associated with the sensing device opening, there is at least one device for sensing the elevation of any mass of any solid organic material contained in the housing, the sensing device being a radar device that is mounted over any sensing device opening and surmounts a non-metallic plate that covers the opening.
  • the gasifier has a device for containing the solid organic materials while above the retention basin and at least one opening in the lower portion of the gasifier to allow movement of non-combustibles out of the gasifier, along with a device in the retention basin for removing non-combustible materials out of the gasifier.
  • the invention deals with a square or rectangular “loaf” gasifier.
  • a gasifier for gasifying solid organic materials comprising a housing, wherein the housing has a lower portion and an upper portion and the housing has four side walls supported by the lower portion and attached to the upper portion, thus differing from the above-mentioned circular gasifier.
  • the floor for the gasifier located in the lower portion of the gasifier, the floor having a top surface and a bottom surface.
  • the floor has at least one opening through it to allow for the passage of solid organic material into the interior of the gasifier, wherein the top surface of the floor has a retaining wall on the outside of each of the floor openings to form a retention basin to retain the solid organic materials in the lower portion of the gasifier to form a floorless hearth.
  • the circular gasifier described Supra is modified to alter the flow of effluent by providing a constriction in the midsection of the gasifier.
  • a gasifier for gasifying solid organic materials comprising a housing wherein the housing has a lower portion having a top part and an upper portion having a bottom part and the housing has a circular side wall supported by the lower portion and attached to the upper portion, wherein the circular side wall has a constricted section where the top part of the lower portion and the bottom part of the upper portion meet and join.
  • an effluent path of flow within the gasifier for a portion of the gaseous effluent to migrate, mix, and react through the heated solid organic materials and the syngas formed thereby is transferred outwardly from the gasifier and any non-combustible solids are transferred out of the gasifier.
  • a further embodiment of this invention is a method of gasifying solid organic material to produce a gaseous effluent and a solid residue, said method comprising providing a supply of solid organic material and providing a loaf gasifier as set forth in this disclosure and introducing the solid organic materials into the gasifier upwardly from a lower portion of the gasifier to provide a mass of solid organic materials in the gasifier.
  • the solid organic materials are ignited and then heated in the gasifier while providing an oxidative gas to the gasifier to provide a gaseous effluent, wherein the oxidative gas is recirculated flue gas from a flue stack located in a system in which the gasifier is operating and, the oxidative gas is flue gas containing a predetermined portion of fresh air.
  • FIG. 1 there is shown therein a full front view of a circular gasifier 1 of this invention having a solid mass feeder 2 and an ash removal system 4 .
  • a gasifier 1 of this invention that is a circular gasifier that is equipped with a solid mass feeder 2 (shown in FIG. 1 ), having a collection bin 5 that is connected by auger feed 3 to the bottom 9 ( FIG. 2 ) of the gasifier 1 .
  • the solid mass feeder 2 runs essentially horizontally 7 beneath the gasifier 1 and then turns essentially ninety degrees vertically 8 and thus feeds the gasifier 1 from the center of the bottom 9 of the gasifier 1 .
  • the solid mass feeder 2 in the horizontal run 7 can be shrouded or it can be an open trough. It is shown as solid mass feed 2 that is covered by a shroud 6 enclosing the auger feed 3 ( FIG. 3 ).
  • the solid mass materials are first comminuted or chopped, if it is forestry product, so that it will flow and be ignited readily. Generally this chopped material is best handled if the pieces are at least 3 inches or less in any dimension. If the solid mass material is chicken litter or turkey litter, then chopping is not required.
  • FIG. 2 is an enlarged front view of a circular gasifier of this invention showing the gasifier 1 , the auger feed 3 , the shroud 6 , the horizontal run 7 and the vertical run 8 .
  • the gasifier per se comprises in combination, a housing 10 that has a circular side wall 11 supported by the lower portion, generally shown as 12 , of the housing 10 .
  • the circular sidewall 11 is attached to the upper portion indicated generally as 13 .
  • the housing 10 is surmounted by a roof 14 , the roof 14 being supported by, and integral with the circular sidewall 11 .
  • FIG. 3 Shown in FIG. 3 is an exit opening 15 through the roof 14 that is used for exiting syngas from the method of this invention. Also shown is a sensing device 16 that is positioned over an opening 17 (shown in FIG. 3 ). The sensing device 16 is a radar that is used to monitor the top of the solid mass 18 shown in FIG. 3 . For purposes of illustration, only one such device 16 is shown, but it is within the scope of this invention to use more than one such device 16 , and it is preferred to use at least three such devices 16 and more preferred to use at least 5 such devices 16 on the gasifier as the height of the solid mass pile 18 is critical to providing particulate free, quality syngas. Details of the construction of the device 16 is shown in 4 and how it may be positioned on the gasifier 1 is shown in FIG. 3
  • the control of pile height is of critical importance for combustion control and the release of gaseous combustibles, i.e., the “product gas”.
  • the location of feed cone(s) 25 and vertical auger(s) are designed to provide a pile having a generous depth, and which has a generally flat upper periphery. This flat, mesa-like upper surface extends over 60 to 70 percent of the floor area, generally filling the lower portion of gasifier 1 , and sharply tapers downward adjacent wall 11 . This downward taper, referred to as the angle of repose, is dependent upon the type of fuel used.
  • a flat fuel pile is key to achieving uniform combustion without bridging.
  • This flat configuration results in a uniform pile depth, which in turn results in uniform air pressure within the pile 18 , thus minimizing channeling of the pile. Maintaining pile depth is very important. About 6 inches or more of ash is maintained below the actively burning portion of the pile so as to prevent heat damage to feed cone 25 and ash removal system 4 .
  • This material moves generally horizontally outward and then downward toward the outer wall and lower floor where it is exposed to further oxidation agents via tuyere arrays 32 and 34 for a more complete reaction, at which time all of the organic constituents of such feed material will gasify and will pass from gasifier 1 as an incompletely oxidized gaseous effluent of combustibles (syngas), the effluent leaving gasifier 1 through an insulated exit duct 52 .
  • the velocity of the effluent above the fuel pile and out the exit duct is kept low, reducing particulate carryover.
  • Feed rate into gasifier 1 is monitored and controlled by monitoring and controlling fuel pile height within gasifier 1 .
  • Suitable instrumentation not shown, is provided to control the rate of the delivery of the feed material into gasifier 1 by the feed assembly as a function of the elevation of the top of the feed material in the height of pile 18 to maintain such elevation at a substantially constant value, and thereby to contain the pile 18 of feed material at a substantially constant shape
  • FIG. 4 there is shown the roof 14 of a circular gasifier 1 upon which is mounted a radar device 16 .
  • the device 16 is housed in an open housing 21 and supported by adjustable fasteners 19 and has the capacity to be adjusted angularly on swiveled fasteners 20 so that the contour of the solid mass 18 in the interior of the gasifier 1 can be sensed.
  • the device 16 in its housing 21 , is mounted over a non-metallic plate 22 .
  • the plates 22 have to be non-metallic so that the device 16 can beam into the interior of the gasifier 1 and sense the top of the solid mass pile 18 .
  • the opening in the gasifier is only an opening in the metal cladding, and not an opening through the firebrick contained in the interior.
  • the solid mass pile 18 burns, it creates a certain amount of ash that must be removed from the gasifier 1 . Therefore, there is at least one trench 24 provided in the gasifier floor featuring one or more devices for removal of ash and combustion residues and for control of the elevation of the “moving bed of ash” hearth.
  • a most adaptable device is an auger 26 shown in FIG. 3 (end view only).
  • FIGS. 2 and 3 there are two trenches 24 , one on either side of a centrally located feed cone 25 that will be described infra.
  • the ash augers 26 in the trenches 24 move the ash towards points of discharge 27 suitably located at the end or bottom of the trenches 24 .
  • the trenches 24 are connected to a bin or a conveyor of suitable design for further disposal of the ash (see FIG. 1 ).
  • the connections are standard connections and are not shown herein.
  • the formation of the ash creates a floorless hearth in the gasifier 1 on which the burning solid mass pile 18 is situated.
  • control of the “moving bed of ash” level that creates the hearth 30 , and the removal of the ash can be accomplished by a conveyor or conveyors moving across the entire floor, or section thereof, from side to side, or end to end of the gasifier as deemed most suitable for the dimensions and shape of the “moving bed of ash” hearth 30 , or alternatively, a set, or sets, of dump grates can be inserted under the “moving bed of ash” hearth 30 to facilitate and control removal of the ash.
  • the peppermill grate 40 is known in the art and consists of a flat metal plate 39 that is perforated with a multiplicity of holes 41 for allowing the ash to fall through it. Over top of the flat plate 39 is a moveable grate 42 , that essentially covers part of the holes 41 part of the time and allows other of the holes 41 to be open.
  • the grate 42 is also perforated with holes 43 .
  • the ash is caused to fall through the holes 42 into the retention basins 29 below and the augers 26 then move the ash to one end 27 where it is moved out of the retention bins 29 into a conveyor system (see FIG. 1 ) for transfer away from the gasifier 1 .
  • FIG. 14 is a side view of a gasifier 1 of this invention with the sides open to show the grate system 84 .
  • the grate system 84 consists of two grate rings 85 and 86 (see FIG. 15 ) at the bottom of the gasifier 1 .
  • the bottom grate 85 is stationary and it has square openings 87 that are approximately 8 inches wide by 20 inches long.
  • the top grate 86 is moveable, that is, activated by two (not shown) hydraulic cylinders that have a stroke maximum of about 8 inches. Because the grate is round, this stroke rotates the grate.
  • the top grate 86 also has square openings 88 .
  • the hydraulic cylinders stroke the top grate 86 such that it aligns the square openings 87 and 88 and on the back stroke misaligns the openings covering the bottom openings 87 .
  • the top grate 86 has wedge plates 89 mounted on top of it. These plates 89 are installed in such a way that when the top grate 86 is rotating towards the openings 88 , the wedge plates 89 push the ash in front of them towards the openings 87 in the bottom grate 85 .
  • the movement and height of the wedge plates 89 ensure measurable and constant ash removal from the bottom of the pile, preventing the ash bridging above the ash grate openings.
  • the process temperature in the vicinity of the ash discharge thermocouples becomes higher indicating that the system has to wait for the next ash dump.
  • the bottom of the gasifier becomes colder and colder indicating that the ash only is left at the bottom of the gasifier and it is time for a new ash dump.
  • the portion of a segment of a feed cone 25 is shown surmounting the grate 42 .
  • the grate 42 is surmounting the flat plate 39 .
  • At one edge 44 of the grate 42 there is a pin 45 that attaches the grate 42 to the flat plate 39 and the grate 42 partially swings around the pin 45 such that the grate 42 moves in an oscillating motion.
  • the swinging motion of the grate 42 moves the ashes that pile on the grate 42 and the flat table 39 and the ash falls through holes 41 and 43 into a bin below.
  • the bottom tuyeres 34 are also shown.
  • the feed material into the gasifier 1 is soft, easily combustible materials, such as chicken litter, turkey litter, or plastics, and the like.
  • the gasifier 1 has a centrally located feed cone 25 arranged along the centerline of the chamber and protruding above the general elevation of the “moving bed of ash” hearth 30 .
  • the feed cone 25 is serviced by a single, or twin set, of fuel feed augers 31 entering vertically from below.
  • the feed cone 25 is circular (See FIGS. 5 and 5 A) for the circular gasifier 1 shown in FIGS. 2 and 3 and the feed cone 25 is square or rectangular (See FIG. 6 and 6 A) for the loaf type of gasifier described infra.
  • the feed cones 25 be utilized as one single piece, that is a unitary article, for example those shown in FIGS. 5A and 6A , respectively.
  • the feed cones 25 be segmented as shown in FIGS. 5 and 6 so that they can more easily be moved into and out of the gasifier 1 for servicing, maintenance and repair.
  • the segmented feed cones 25 can be simply set in place adjacent each other, or they can be mortared together, or glued together to hold them in place.
  • the segmented feed cones 25 shown in 5 A and 6 A are those used in the moveable feed cone described infra.
  • feed cones 25 are non-moveable articles when in use in the gasifier.
  • feed cones 25 that are moveable, that is are moveable in a partial circular motion within the gasifier 1 , such that they oscillate. (See FIGS. 5 and 6 ).
  • the purpose for the moveable feed cones 25 is for providing oxidative gases through the burning solid mass pile 18 evenly so that creation of gas channels can be voided. Periodic movement of the cone will prevent oxidative gas from burning holes between the gas sources and the surface of the pile.
  • a partial primary method is one in which the combustion is carried out sub-stoichiometrically with the application of an oxidizing agent, which in this invention is flue gas mixed with a predetermined portion of fresh air, wherein the solid organic materials are transferred continuously or intermittently to the gasifier 1 at a predetermined rate to maintain a mass of solid organic materials in the gasifier, and further wherein the oxidant is continuously added to the gasifier 1 to continuously gasify the solid organic materials in the mass, and still further the solid residue (non-combustibles) are transferred out of the gasifier.
  • an oxidizing agent which in this invention is flue gas mixed with a predetermined portion of fresh air
  • the oxidizing agent is administered through a set or sets of suitable ducts connected to nozzles, preferably tuyeres and injection points located within, around and between the feed cones 25 , and to a row, or line of nozzles and/or tuyeres in the surrounding walls of the gasifier 1 .
  • the upper tuyeres 32 are fed through a common manifold 35 and the lower tuyeres 33 are also fed through a common manifold 36 .
  • the tuyeres 32 are linked to the manifold 35 by feed tubes 37 and the tuyeres 33 are linked to the manifold 36 by feed tubes 38 .
  • the manifolds 35 and 36 are fed from a flue gas return system, generally 48 , that consists of a duct 49 and an air motor 50 .
  • the inlet 51 of the air motor is attached to the system 60 ( FIG. 1 ) for supplying fresh air-modified flue gas to the air motor 50 .
  • the gasifier 1 is equipped with an opening 15 for the movement of the syngas produced by the method.
  • the opening 15 has surmounted on it, a fixture 52 for allowing the attachment of components that are used to handle the syngas, which will be described infra.
  • probes 53 can be used to monitor the level of moving ash bed defined by the upper elevation of the accumulated ash.
  • probes 53 there are used thermo elements in pairs located one above the other, distanced sufficiently such that the level of the moving ash bed will be in between them, and capable of characterization by the difference in temperatures and the temperature of the material above the moving ash bed while in operation. Said temperature difference will then be the offset that will dictate the degree of auger 26 movement required to control the level of the moving ash bed between the probes.
  • gasifier 1 is equipped with several sets of probes 53 , inserted through openings 55 , around the perimeter of the chamber and an average of probe 53 input data will determine the auger 26 movements.
  • the floor 57 for the gasifier is located in the lower portion 12 of the gasifier 1 , the floor 57 having a top surface and a bottom surface.
  • the floor 57 has at least one opening through it to allow for the passage of the solid organic material into the interior of the gasifier 1 .
  • the feed assembly 3 is activated to form the pile 18 of feed material in the gasifier 1 in preparation of development of a “moving ash bed” above bottom 9 .
  • the pile 18 of feed material is ignited.
  • fuel oil or other readily combustible supplemental fuel may be added to it. As an example, this may be done manually through an opening 54 provided in the wall of the gasifier 1 .
  • the moderately slow burning lower portion of the pile will serve to establish a quiet oxidation zone whereby entrainment of particulate matter and fly ash is minimized.
  • Syngas with a maximum of combustible gaseous components and a minimum of particulate matter is one key objective of this invention.
  • FIG. 8 which is a full front view of a loaf type of gasifier 60
  • FIG. 9 that is a full cross sectional view of a gasifier 60 of FIG. 8 through line B-B
  • the gasifier 60 is defined by four vertical side walls 61 , giving the chamber a square or rectangular cross section and forming an enclosure 62 ( FIG. 9 ) which has an irregularly shaped bottom 63 and which has at its top a roof 64 , which in cross section may be vaulted, tapered or flat or any combination hereof.
  • Wall 61 is made up of a multiplicity of layers.
  • the innermost layer 65 is an insulating layer of a high-temperature resistant type refractory that is capable of withstanding the elevated temperatures that will develop within gasifier 60 , for example, temperatures in the range of approximately 2300° F. to approximately 2500° F., and that is capable of withstanding the operational temperature variations as well as the corrosive, erosive effects of the gaseous materials produced by the oxidation of the biomass feed material that is delivered into gasifier 60 .
  • Wall 61 may also include an insulating layer 66 on the outside of the wall layer 65 to further prevent loss of heat through the wall 61 of gasifier 60 .
  • the insulating layer 66 may be a single layer of insulating firebrick, block insulation, or blanket insulation.
  • the outer casing of the wall 61 is a structural layer or shell 67 of sheet metal, for example, plate steel, which is airtight and provides the necessary strength and rigidity for the wall.
  • FIG. 10B A second embodiment of wall 61 is shown in FIG. 10B , wherein insulating layer 66 is not used, and a vacant layer or space 58 is provided between refractory innermost layer 65 and steel shell 67 .
  • the air which fills vacant layer 68 acts as an insulator between refractory layer 65 and steel shell 67 .
  • This warmed air can also be used as a source of preheated air for injection into gasifier 60 and recovery and regeneration equipment 96 and 98 .
  • the biomass feed material from the storage hopper assembly (not shown) is introduced into gasifier 60 from below gasifier 60 through at least one feed cone 59 located along the centerline of bottom 63 of gasifier 60 .
  • the feed material rises over the top of the feed cone(s) 59 and rests on the hearth 70 .
  • Hearth 70 is made up of ash and other solid combustion residues, until it forms a pile 71 of such material, which is the normal or equilibrium condition of gasifier 60 .
  • This self-generated hearth 70 is the “moving ash bed” configuration, that is an essential part of this invention and which is described Supra with regard to gasifier 1 . As primary oxidation progresses, this bed continues to elevate and the ash must be removed at essentially the same rate it is formed to maintain the appropriate fuel pile height.
  • exit ducts 69 are positioned so that it vents gasifier 60 through roof 64 .
  • prior art loaf gasifiers required that the exit for the produced gases must be through the sidewall so as to minimize the flow of particulate materials along with the gas.
  • sidewalls 61 are provided in a height which allows any air-borne particulate to fall back to pile 71 rather that exit via duct 69 .
  • the positioning of exit duct 69 within gasifier 60 can be as shown in FIGS. 8 or 9 , and may be sloped or vertical, and is selected to be practical and suitable for the specific application.
  • the oxidizing agent is administered through a set or sets of suitable ducts connected to nozzles, preferably tuyeres and injection points located within, around and between the feed cones 59 , and to a row, or line of nozzles and/or tuyeres in the surrounding walls of the gasifier 1 .
  • the modified flue gas return system useful in gasifier 60 shown in FIGS. 8 and 9 can also be observed in FIG. 2 , and this system is adaptable and useful in the gasifier 60 .
  • the manifolds 76 and 77 of FIGS. 8 and 9 are fed from a flue gas return system as shown in FIG. 8 , generally 48 , that consists of a duct 49 and a fresh air motor 50 .
  • the inlet 51 of the air motor is attached to the system 60 ( FIG. 1 ) for supplying fresh air-modified flue gas to the air motor 50 .
  • the details of the movement of the fresh air modified flue gas from the flue stack to the gasifier is set forth in detail infra.
  • the upper part of the lower portion 12 and the lower part of the upper portion 13 of the gasifier are modified from prior art devices in that, there is a constriction 80 of the interior of the gasifier 60 .
  • This constriction 80 is built into the firewall brick 65 , or it can be formed from a plate that is set at an angle into the firebrick 65 .
  • the purpose of this constriction 80 is to slow down the product gas in its flow upward which results in another method by which particulate material does not tend to reach the exits ports 69 .
  • Feed rate into gasifier 60 is monitored and controlled by monitoring and controlling fuel pile height within gasifier 60 using the same radar devices 16 as set forth Supra. Suitable instrumentation, not shown, is provided to control the rate of the delivery of the feed material into gasifier 60 by the feed assembly as a function of the elevation of the top of the feed material in the height of pile 71 to maintain such elevation at a substantially constant value, and thereby to contain the pile 71 of feed material at a substantially constant size.
  • FIG. 11 there is shown an enlarged view of roof 64 for the loaf gasifier 60 , that shows the two exit ports 69 for syngas located on the roof 64 . Also shown is a placement of a radar device 16 on the roof 64 , between the two exit ports 69 . The dotted lines 84 illustrate the beam of the radar 16 into the interior of the gasifier 1 .
  • FIG. 12 shows the roof 64 and the construction of the walls of the roof 64 . There is thus shown the outside, or steel wall 67 , the insulating layer 66 and the interior firebrick wall 65 .
  • the component 82 is a flange that is useful for fitting the roof to the sidewalls of the gasifier 60 .
  • FIG. 13 is a cross sectional view of the specifics of the ash handling system of the loaf gasifier as shown in FIG. 8 .
  • the ash handling system 81 that includes the removable peppermill grates 42 , the increasing flight ash augers in the collection bin and retention bin 29 , and the castable tuyere panels 83 .
  • the exit of the centered feed cone 59 is also shown.
  • FIGS. 1A and 1B a description of a “system” of this invention, there is shown a schematic of a gasifier 1 of this invention and its interconnection to the various components that can make up the system wherein the numbers in pentagons are the flow paths and various components of the system as describe infra.
  • FIGS. 1A and 1B show a gasifier 1 that is fed a solid mass material 2 using an auger feed 3 . Shown also is an ash removal system 4 .
  • Syngas 90 that is produced by the pyrolysis and gasification of the solid mass material 2 exits the gasifier 1 through exit port 15 and into a syngas burner 91 and into a syngas blower 92 .
  • the syngas 90 is controlled by draft controls 93 .
  • the syngas burner 91 is aided in combustion using a combustion air blower 94 that provides air 95 to the syngas burner 91 .
  • the syngas 90 is provided to the syngas burner 91 at a temperature of about 500° F. to about 600° F. and is in a starved air condition.
  • This part of the system is unique to this type of gasifier system in that the normal temperature of the air from prior art devices is in the range of 1200° F. to 1400° F., and in prior art systems, this air is not “starved air”, and before the prior art air can be used, it has to be cooled and compressed, which means that additional and expensive equipment has to be added to the system in prior art processes.
  • the syngas burner 91 heats and combusts the syngas 90 up to a temperature in the range of 1200° F. to 1400° F. before the heated air 97 is provided to a low NO x oxidizer 96 .
  • the syngas 90 can be provided to a kiln 98 using a syngas blower 99 that moves the syngas 90 to a nozzle mix syngas burner 100 . Thereafter the syngas 90 is moved through the nozzle mix syngas burner 100 into the kiln 98 . The heated air (about 2200° F.) from the kiln 98 is moved to the low NO x oxidizer 96 and combined with the starved air coming from the syngas burner 91 .
  • the heating and movement of the heated air in the kiln 98 is aided by passing heated air 101 from a heat exchanger 102 (see FIG. 1B ) and also mixing the heated air 103 with heated ambient air 105 being bleed into the nozzle mix syngas burner 100 using a preheated combustion air blower 104 , along with additional heated air 101 from the heat exchanger 102 that is bled 106 directly into the kiln 98 .
  • the heated air 107 from the kiln 98 is fed into the low NO x oxidizer 96 and mixed therein with the air 97 being fed into the top portion of the low NO x oxidizer 96 .
  • the low NO x oxidizer 96 is fed ambient air 108 using a combustion/tempering air fan 109 , through manifolds 110 and tuyeres (not shown) and the air 111 that exits the low NO x oxidizer 96 does so at about 2000° F. and passes to the heat exchanger 102 shown in FIG. 1B .
  • FIG. 1B there is shown the heat exchanger 102 into which the heated air 111 has been passed and the exchanged air 112 is then passed to a metal heat exchanger 113 at about 1400° F., the metal heat exchanger 113 being useable because of the lower temperature of the air 112 .
  • Air 114 is moved to the heat exchanger 102 and the heated air is that used in the heat exchanger 102 for the exchange. The movement of the air 114 is aided by the introduction of fresh air 124 using an air blower 125 .
  • Exchanged air having a temperature in the range of about 400° F. to 1200° F. is the air 101 that is passed back to the kiln 98 .
  • the air 101 has to be occasionally vented in order to control the temperature and pressure of the air 101 and this is shown at 116 .
  • the heat-exchanged air 127 from the metal heat exchanger 113 is moved to an induction draft fan 115 before it enters the stack 117 .
  • a portion of the flue gas 120 Prior to air exiting 122 the flue stack 117 , a portion of the flue gas 120 is withdrawn from the stack 117 and moved to a flue gas eductor 118 , which is aided by a an induced draft fan 119 .
  • fresh air 128 is inducted and mixed with the flue gas 120 and it is this flue gas modified with fresh air 121 that is moved back to the gasifier 1 as the oxidative gas for use in the gasifier 1 .
  • a sampling port 129 Also shown in FIG. 1B is .

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  • Combustion & Propulsion (AREA)
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US11/801,030 2006-05-18 2007-05-08 Method for gasifying solid organic materials and apparatus therefor Abandoned US20070266914A1 (en)

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Application Number Priority Date Filing Date Title
US11/801,030 US20070266914A1 (en) 2006-05-18 2007-05-08 Method for gasifying solid organic materials and apparatus therefor
PCT/US2007/011965 WO2007136786A1 (fr) 2006-05-18 2007-05-17 Procédé de gazéification de matières organiques solides et appareil associé
BRPI0711715-9A BRPI0711715A2 (pt) 2006-05-18 2007-05-17 aparelho para gaseificar material orgánico, e, método para gerar gás de sìntese a partir de material orgánico
EP07795052A EP2032503A4 (fr) 2006-05-18 2007-05-17 Procédé de gazéification de matières organiques solides et appareil associé
CA002649285A CA2649285A1 (fr) 2006-05-18 2007-05-17 Procede de gazeification de matieres organiques solides et appareil associe
US12/860,759 US20100313796A1 (en) 2006-05-18 2010-08-20 Biomass gasification in atmospheres modified by flue gas
US13/372,061 US20120137582A1 (en) 2006-05-18 2012-02-13 Biomass gasification in atmospheres modified by flue gas

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US11/801,030 US20070266914A1 (en) 2006-05-18 2007-05-08 Method for gasifying solid organic materials and apparatus therefor

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US12/860,759 Abandoned US20100313796A1 (en) 2006-05-18 2010-08-20 Biomass gasification in atmospheres modified by flue gas
US13/372,061 Abandoned US20120137582A1 (en) 2006-05-18 2012-02-13 Biomass gasification in atmospheres modified by flue gas

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IT201800003927A1 (it) * 2018-03-26 2019-09-26 Francesco Barbagli Generatore di gas da biomasse e/o rifiuti.
IT201800003922A1 (it) * 2018-03-26 2019-09-26 Francesco Barbagli Generatore di gas da biomasse e/o rifiuti.
CN110586008A (zh) * 2019-10-21 2019-12-20 刘文娟 一种便于排渣清理型氧化装置
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US20110104575A1 (en) * 2008-06-25 2011-05-05 Nexterra Systems Corp. Generating clean syngas from biomass
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CN101995836A (zh) * 2010-11-01 2011-03-30 广州迪森热能技术股份有限公司 生物质气给料放散自动控制系统以及生物质气化反应系统
WO2012122622A1 (fr) * 2011-03-17 2012-09-20 Nexterra Systems Corp. Système et procédé à chauffe direct
US8882493B2 (en) * 2011-03-17 2014-11-11 Nexterra Systems Corp. Control of syngas temperature using a booster burner
US20140004471A1 (en) * 2011-03-17 2014-01-02 Nexterra Systems Corp. Control of syngas temperature using a booster burner
US20170234529A1 (en) * 2012-03-27 2017-08-17 Daniel R. Higgins Method and apparatus for improved firing of biomass and other solid fuels for steam production and gasification
US10627105B2 (en) * 2012-03-27 2020-04-21 Daniel R Higgins Method and apparatus for improved firing of biomass and other solid fuels for steam production and gasification
GB2513143B (en) * 2013-04-17 2015-11-11 Chinook End Stage Recycling Ltd Improvements in waste processing
GB2513143A (en) * 2013-04-17 2014-10-22 Chinook End Stage Recycling Ltd Improvements in waste processing
US10577550B2 (en) * 2017-09-26 2020-03-03 Catherine J. Chagnot Continuously operable mechanical or electrical power source fueled by gas or solid fuel including gas from improved biomass downdraft gasifier
IT201800003927A1 (it) * 2018-03-26 2019-09-26 Francesco Barbagli Generatore di gas da biomasse e/o rifiuti.
IT201800003922A1 (it) * 2018-03-26 2019-09-26 Francesco Barbagli Generatore di gas da biomasse e/o rifiuti.
CN110586008A (zh) * 2019-10-21 2019-12-20 刘文娟 一种便于排渣清理型氧化装置

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EP2032503A1 (fr) 2009-03-11
US20100313796A1 (en) 2010-12-16
WO2007136786A1 (fr) 2007-11-29
BRPI0711715A2 (pt) 2011-12-06
EP2032503A4 (fr) 2011-04-06
US20120137582A1 (en) 2012-06-07
CA2649285A1 (fr) 2007-11-29

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