WO2003098111A1 - Appareil ameliore destine a la gazeification de dechets - Google Patents

Appareil ameliore destine a la gazeification de dechets Download PDF

Info

Publication number
WO2003098111A1
WO2003098111A1 PCT/US2003/016066 US0316066W WO03098111A1 WO 2003098111 A1 WO2003098111 A1 WO 2003098111A1 US 0316066 W US0316066 W US 0316066W WO 03098111 A1 WO03098111 A1 WO 03098111A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasification
chamber
gas
operably connected
interior chamber
Prior art date
Application number
PCT/US2003/016066
Other languages
English (en)
Inventor
Michael G. Pope
Original Assignee
Senreq, Llc
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Senreq, Llc filed Critical Senreq, Llc
Priority to AU2003233631A priority Critical patent/AU2003233631A1/en
Priority to CA002482557A priority patent/CA2482557C/fr
Priority to GB0423188A priority patent/GB2403284A/en
Priority to EP03729070A priority patent/EP1509726A1/fr
Publication of WO2003098111A1 publication Critical patent/WO2003098111A1/fr

Links

Classifications

    • 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
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10J3/06—Continuous processes
    • 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
    • C10J3/06—Continuous processes
    • C10J3/10—Continuous processes using external heating
    • 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
    • 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
    • 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
    • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
    • 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
    • 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
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • 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
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • 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
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/08—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases using flares, e.g. in stacks
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L17/00—Inducing draught; Tops for chimneys or ventilating shafts; Terminals for flues
    • 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
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing 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
    • 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
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1215—Heating the gasifier using synthesis gas as fuel
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1284—Heating the gasifier by renewable energy, e.g. solar energy, photovoltaic cells, wind
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1696—Integration of gasification processes with another plant or parts within the plant with phase separation, e.g. after condensation
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • 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
    • F23G2900/00001—Exhaust gas recirculation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23M—CASINGS, LININGS, WALLS OR DOORS SPECIALLY ADAPTED FOR COMBUSTION CHAMBERS, e.g. FIREBRIDGES; DEVICES FOR DEFLECTING AIR, FLAMES OR COMBUSTION PRODUCTS IN COMBUSTION CHAMBERS; SAFETY ARRANGEMENTS SPECIALLY ADAPTED FOR COMBUSTION APPARATUS; DETAILS OF COMBUSTION CHAMBERS, NOT OTHERWISE PROVIDED FOR
    • F23M2900/00—Special features of, or arrangements for combustion chambers
    • F23M2900/05004—Special materials for walls or lining

Definitions

  • Waste gasification involves supplying the minimum amount of oxygen necessary to cause a thermo-chemical reaction that releases simple combustible gases at a controlled temperature, without supplying enough oxygen to cause combustion.
  • feed stock materials such as MSW
  • feed stock materials that are rich in energy as measured by British thermal units
  • oxygen depleted environment such solid, sludge, or liquid feed stock materials are converted into a heavy vapor gas fuel.
  • Materials that are rich in energy include, but are not limited to, coal, wood, cardboard, paper, industrial scrap, plastics, tires, organic wastes, sewage cake, animal waste, and crop residue, or a combination thereof.
  • the released heavy vapor fuel gas is then mixed with oxygen and burned. Examples of prior gasification systems are shown in U.S. Pat. No. 4,941,415, which is incorporated herein by reference, and U.S. Pat. No. 5,941,184.
  • the material remaining after the completion of the gasification process cycle is composed of incombustible materials, including metals, glass, and ceramics, along with a fine inert salt and mineral power residue, and has a greatly reduced volume that is suitable for remanufacturing into concrete material or land filling. Furthermore, recyclable materials that do not undergo phase transition, such as all recycle glass, aluminum, metals, residual materials and salts, are recoverable after the gasification process, thereby eliminating the need for pre-sorting or processing the in-bound feed stock material.
  • prior art open-looped systems such as U.S. Pat. No. 6,439,135, which is incorporated herein by reference, utilize exhaust stacks that release hot gases from the final combustion step into the atmosphere, or use storage tanks to collect the hot gases for future ancillary purposes, rather than reclaiming at least a portion of the cleaned air for re-introduction into the gasification process.
  • prior art systems do not teach a gasification system that produces a relatively pure carbon dioxide for other industrial purposes or to support the augmentation of vegetation, such as a greenhouse, a carbon dioxide dispersal system, or an aquaculture bed.
  • Current research indicates that increasing the surface area of feed stock material that is exposed to gasification process gas significantly improves the production rate of fuel gas from the feed stock materials.
  • prior art gasification systems such as those illustrated in U.S. Pat. No. 6,439,135 and 5,619,938, utilize reactor chamber configurations that expose only limited feed stock surface area to gasification process gas.
  • Such prior art systems incorporate reactor chamber configurations where only the bottom of the feed stock at grate level, known as the primary reaction zone, and the uppermost surface of the feed stock, known as the secondary reaction zone, are exposed to optimum gasification conditions.
  • gasification of the tons of feed stock material that is not located at either the primary or secondary zones, such as that on the sides and center of the reactor chamber, requires that the temperature and duration of the gasification cycle be increased. Yet, higher gasification temperatures tend to reduce the Btu content of the resulting heavy vapor fuel gas. The high operating temperatures also increase the time required for cooling the gasification chamber to a temperature suitable for the loading and disposal of subsequent loads of feed stock materials.
  • a 2 to 4 inch layer of ceramic fiber blanket is usually inserted between the refractory material and the steel jacket before the refractory layer is installed to offer additional thermal protection for the exterior steel surfaces of the gasification reactor chamber.
  • Application of refractory material is thus labor intensive, time consuming, and a significantly expensive step.
  • the weight of the refractory liner necessitates that the steel vessel be constructed from at least 1/4 inch thick hot rolled A36 steel plate and heavy structurals. This additional superstructure weight further increases the overall cost of manufacturing, shipping, and installation.
  • refractory material An additional problem with the use of refractory material is the length of time required for cooling the gasification reactor chamber before it can be re-used to gasify a subsequent load of MSW. More specifically, a subsequent gasification process typically cannot begin until the gasification reactor chamber has cooled to approximately 150 degrees Fahrenheit. Yet, at the end of a process cycle, the clay refractory material tends to retain heat for a long period of time. Depending on the particular chemistry of the refractory material, this retention of heat may require that the gasification chamber be inoperative for several hours as the temperature of the chamber, and associated refractory material, cools down.
  • gasification reactor chambers typically have a rectangular configuration.
  • the size of the reactor chamber creates problems associated with providing sufficient clearance space away from the prolonged high temperatures of the reactor chamber. This problem typically limits reactor chambers to configurations that are approximately 20 feet high, 20 feet wide, 20 feet long. Such a configuration however has a limited load capacity of approximately 50 tons of feed stock material.
  • problems develop with the side load waste dump arrangement. More specifically, as the rectangular sidewalls extend beyond 20 feet, the angle of repose of the trash spilling out of the garbage truck typically only fills a small portion of the reactor chamber's near sidewalk
  • waste gasification systems must also increase the level of ambient oxygen in the gas produced in the gasification reactor chamber to make it fully flammable. This often requires increasing the oxygen content of the heavy vapor fuel gas to approximately 15% to 20%.
  • Prior art gasification systems increased the oxygen content of the heavy vapor fuel gas by directing the heavy vapor fuel gas through air mixing chambers.
  • These mixing chambers are typically large, cylindrical vessels, with a variety of air induction tubes attached to multiple blower fans that flood the air mixing chambers with outside air using air compressors or high velocity fans. Yet because of the large size of these chambers, they require substantial fabrication and installation time, and as a result are expensive.
  • the use of fans and/or air compressors also increases the initial cost of the system and operating and maintenance expenses.
  • a further disadvantage of traditional air draft systems is that heavy vapor fuel gases have a tendency to linger in the gasification reactor chamber, and become subject to accidental combustion, which ultimately lowers the Btu content of the extracted heavy vapor fuel gas.
  • This problem is exacerbated by the inconsistency of up-draft air movement in a natural draft system. Humidity, wind, barometric pressure and outside temperature all affect the rate of flow through a natural draft system. This inconsistent flow causes the evacuation of gases from the reactor chambers to frequently stall, produces negative results in the process, and adversely effects the total cycle time for the gasification of the feed stock material.
  • the combustion of the heavy vapor fuel gas in a hot water heater, steam boiler, refrigeration unit, or other industrial process produces a relatively high temperature exhaust.
  • prior art systems often vent this hot combusted exhaust into the atmosphere at a temperature between 1200 and 1600 degrees Fahrenheit, thereby wasting a significant thermal resource that could be further captured and directly utilized in other heat dependent applications, thereby preserving natural resources and providing a cost efficient source for heated gas.
  • Hot combusted exhaust that is vented into the atmosphere in prior art systems via an exhaust stack also often contain large quantities of carbon dioxide. While carbon dioxide is not currently regulated as a pollutant from solid waste incinerators, it is subject to various industrial air quality abatement initiatives.
  • the volume of the exhaust decreases.
  • It is another object of the present invention is to provide an inexpensive to build, simple to operate, gasification system that provides the benefits of producing a fuel gas from feed stock material. It is another object of the present invention to provide for improved gas collection that allows for both simpler gasification reactor chamber configurations and an improved gas flow design that allows for better final combustion.
  • the present invention is directed to a system for the gasification of a variety of waste streams, including, but not limited to, agricultural, industrial, and municipal waste streams. More particularly, the invention relates to a gasification system that incorporates a self sustaining gasification chamber that has its own dedicated flare assembly, and which is capable of gasifying large volumes of feed source material without the need for multiple gasification chambers. This self-sustaining gasification chamber and flare assembly are also capable of being used with other self-sustaining chambers to feed at least one common heat recovery device.
  • the present invention is a closed-loop system, which eliminates the need for an exhaust stack, and which recovers heat entrained in hot exhaust, thereby producing a cooled exhaust that is subsequently filtered and separated from carbon dioxide, and which is suitable for re-introduction in the gasification procedure.
  • Removed carbon dioxide may then be used for other industrial operations, or may be used to support the augmentation of vegetation, such as a greenhouse or a carbon dioxide dispersal system, whereby vegetation converts the carbon dioxide into oxygen that may also be recaptured for re- introduction in the system of the present invention.
  • the gasification system is comprised of a gasification reactor chamber, an aspirator, a flare assembly, at least one heat recovery device, an absorber, and an extractor.
  • the reactor chamber is comprised of an interior chamber and an outer shell.
  • the gasification reactor chamber of the present invention may have a number of shapes, including being rectangular, square, or cylindrical
  • the reactor chamber of the preferred embodiment of the present invention has at least five sidewalls and includes perforated conduits or an inner liner.
  • the perforate conduits or inner liner increase the surface area of the feed stock material that is exposed to optimum gasification conditions, thereby decreasing both the gasification cycle time and temperature, while also decreasing the time between additional gasification procedures on subsequently loaded feed stock material.
  • gasification temperature also allows for the fabrication of the gasification chamber from lighter gage material, and eliminates the need for refractory material, thereby reducing the weight of the gasification system and the time and expense associated with its fabrication.
  • gasification conditions may be controlled by a process logic controller, which is used to control the gas content and temperature in the interior chamber.
  • An aspirator assembly through the use of a motor, is used to create a negative pressure in the interior chamber, thereby allowing for the smooth and even evacuation of heavy fuel vapor gas.
  • a suction force is created in the conduit coupling and attached single gas manifold and gas siphon assembly. This suction force pulls the heavy vapor fuel gas from the interior chamber and into the conduit coupling.
  • the efficient extraction of heavy vapor fuel gas afforded by the aspirator assembly also prevents the occurrence of accidental combustion that may lower the Btu content of the desired fuel gas.
  • the ambient air used by the aspirator to create the suction force is mixed with the heavy vapor fuel gas in the conduit coupling, thereby eliminating the need for a separate mixing chamber. Furthermore, control of the motor and the selected size of the tubing and conduit allow for finite control of the volume of gas that moves through, and is mixed by, the aspirator assembly.
  • the aspirator assembly of the present invention also eliminates the need for a damper.
  • the flare assembly includes a targeting nozzle that has a conical funnel configuration.
  • the configuration of the targeting nozzle allows for additional mixing of the gases, increases the velocity of the mixed gas so as to provide back pressure in the system, and creates a focus point for combustion.
  • Back pressure created by the conical funnel configuration not only aids in the smooth operation of the at least one common heat recovery device, but allows the system to incorporate heat recovery devices that have minimum positive input pressure requirements.
  • the flare assembly is built in, or is a sub-component of, at least one primary heat recovery device.
  • the combustion of the mixed gas by the flare assembly is then used to operate or heat the at least one heat recovery device.
  • hot combusted gas is delivered from the flare assembly to the at least one common heat recovery device.
  • each subsequent heat recovery device further captures the thermal energy that is entrained in the exhaust until the temperature of the exhaust has been reduced to a permissible level for filtering in an absorber.
  • Heat recovery devices include, but are not limited to, boilers, generators, and reverse chiller refrigeration loops.
  • the hot exhaust exiting the at least one heat recovery device may also pass through a geothermal field, in which the exhaust is directed to a subsurface manifold that may be located underground or beneath a body of water. Heat from the exhaust is then used to heat the surrounding ground or water, and may provide a no-operating cost method for heating such things as on-site greenhouses and aquaculture beds.
  • exhaust from the last heat recovery device is diverted into a chilling loop.
  • the exhaust entering the chilling loop has a temperature of approximately 30 degrees Fahrenheit.
  • the cold chill tubes cause the temperature of the through-flowing exhaust air to cool and the moisture to condense.
  • the condensation removes virtually all particulate matter, particularly water-soluble particulate matter, including HCL and SO2, from the exhaust air stream.
  • the water is then removed in a knock-out trap
  • the exhaust gas is filtered for low temperature criteria pollutants, such as, but not limited to, HCL
  • the filtered exhaust then proceeds to an extractor where carbon dioxide is separated from the remaining filtered exhaust, which is comprised mainly of oxygen and water vapor.
  • the oxygen and water vapor may then be re-directed back to the gasification chamber as recycled process gas for re-use in the gasification system, thus providing a closed- loop process.
  • Carbon dioxide may be captured for other industrial purposes, or may be vented for the purpose of facilitating the growth of on-site vegetation, such as a greenhouse. Careful planning in the selection of plants may create an on-site vegetative environment that is capable of converting all of the produced carbon dioxide into oxygen. The converted oxygen may then be captured for re-introduction in the gasification system of the present invention.
  • FIG. 1 shows a process diagram for a multi-cell gasification system in accordance with the present invention.
  • FIG. 2 shows a variant of the process flow of an embodiment of the invention.
  • FIGS. 3A, 3B, and 3C show exterior views of a gasification reactor chamber for use with the present invention.
  • FIG. 3D shows a perspective view of one embodiment of the interior chamber of the gasification reactor chamber for use with the present invention.
  • FIG. 3E shows an exterior perspective view of one embodiment of the interior chamber and an inclined waste disposal configuration of the gasification reactor chamber for use with the present invention.
  • FIG. 4 shows a flare assembly for use in combusting mixed gas with the present invention.
  • FIG. 5A shows a cross sectional top view of the gasification reactor chamber made in accordance with one embodiment of the present invention.
  • FIG. 5B shows a perspective cross sectional view of the gasification reactor chamber made in accordance with one embodiment of the present invention.
  • FIG. 5C shows a perspective cross sectional view of the gasification reactor chamber including an inner liner in accordance with one embodiment of the present invention.
  • FIG. 5D shows a cross sectional side view outer shell and interior chamber for the gasification reactor chamber of the present invention.
  • FIG. 6 shows an aspirator assembly for use with the present invention.
  • FIG. 7 shows a cross-sectional view of a conduit coupling for use with the aspirator assembly shown in FIG. 6.
  • FIG. 8 shows the inclusion of a geothermal field in one embodiment of the present invention.
  • FIG. 9 shows a general operational layout of the present invention.
  • FIG. 10 shows an overview of transporting feed stock material to multiple waste gasification reactor chambers in accordance with the present invention.
  • FIG. 11 shows the use of a greenhouse for absorbing carbon dioxide in accordance with one embodiment of the present invention.
  • FIG. 12 shows the use of a carbon dioxide dispersal system in accordance with one embodiment of the present invention.
  • FIG. 1 shows a closed-loop waste gasification system 100.
  • Waste hauling trucks unload feed stock material either directly into batch waste gasification reactor chambers 101, 102, 103, as shown in Figure 9, or unload the feed stock at a tipping floor area 50, as shown by Figure 10, whereby a variety of conveyors 60 transport the feed stock to the gasification reactor chambers 101, 102, 103.
  • the feed stock material undergoes gasification.
  • Uncombusted heavy vapor fuel gas driven off in the reactor chambers 101, 102, 103 is evacuated by aspirator assemblies 229a, 229b, 229c through collection ducts 107, 108, 109 to the dedicated flare assemblies 210a, 210b, 210c.
  • Radiant and convection heat generated in the flare assemblies 210a, 210b, 210c converge, and are absorbed by at least one heat recovery device, such as a primary heat recovery device 211, which may include, but is not limited to, a steam boiler, heat exchanger, or any other heat sink.
  • a primary heat recovery device 211 which may include, but is not limited to, a steam boiler, heat exchanger, or any other heat sink.
  • Each flare assembly 229a, 229b, 229c may be operably connected to both a single self-sustaining gasification reactor chamber 101, 102, 103 and to the primary heat exchanger 211, as illustrated in Figure 1, whereby the flare assemblies 229a, 229b, 229c produce a hot combusted exhaust that is fed into a primary heat recovery device 211.
  • the dedicated flare assemblies 210a, 210b, 210c may be a sub-component of, or built into, a common or a separate primary heat recovery device 211, whereby, rather than receiving thermal energy in the form of hot combusted gas, the combustion of heavy vapor fuel gas is directly used to power or operate the primary heat recovery device 211.
  • the gasification reactor chambers 101, 102, 103 and their dedicated flare assemblies are operably connected to different primary heat recovery devices.
  • one gasification reactor chamber 101 provides heavy vapor fuel gas for operating a boiler 111 and hot water heater 110, while other gasification reactor chambers 102, 103 independently supply heavy vapor fuel gas to support the operations of a greenhouse 117.
  • Each associated flare assembly then independently satisfies its combustion requirements for the attached heat recovery device.
  • the multiple flare assemblies 210a, 210b, 210c may also be operably connected to a common primary heat recovery device 211, whereby each individual flare assembly 210a, 210b, 210c independently combusts heavy vapor fuel gas from its dedicated reactor chamber 101, 102, 103 in accordance with the designed combustion requirements of the common primary heat recovery device 211.
  • Figure 1 illustrates flare assemblies 210a, 210b, 210c as separate components that are not part of the primary heat recovery device 211, each flare assembly 210a, 210b, 210c may also be built into, or a subcomponent of, the system's 100 primary heat recovery device 211.
  • Additional heat recovery devices such as a secondary heat recovery device 212 may also use exhaust from the primary heat recovery device 211.
  • the secondary heat recovery device 212 is a reverse chiller refrigeration system, the reverse chiller system being comprised of an inlet, a radiator, an induced draft fan, a sump, and an outlet. Hot exhaust is pumped into the radiator from the primary heat recovery device 211, the momentum for the hot exhaust being provided by the in-line induced draft fan that is preferably located on the back out-take side of the radiator loop.
  • exhaust from the primary heat recovery device 211 enters the reverse chiller at approximately 350 degrees Fahrenheit.
  • Water within the radiator then begins to condense, and continues condensing as the exhaust gas is reduced in temperature to preferably 70 degrees Fahrenheit.
  • the rapid cooling of the exhaust from the primary heat recovery device 211 causes particulates, such as HC1 and SO 2 , to condense out of the gas. Accumulated pollutants and condensate are then collected in a sump at the low point of the radiator and removed from the system. Cooled exhaust gas will then be piped back to the gasification reactor via an additional induced draft fan, and directed to a plurality of cooling fins within the reactor chambers 101, 102, 103. The cooled exhaust is then used as a cooling media, which thereby eliminates the need for an exhaust stack, as required by incineration and pyrolysis operations.
  • cooled exhaust may be re-introduced into the gasification chamber through a plurality of process gas inlets and aid the gasification procedure.
  • the at least one heat recovery device has significantly cooled the exhaust gas, it becomes possible to avoid any regulated air emissions by diverting the exhaust to an underground geothermal field 113. Heat from the exhaust passing through the geothermal field 113 may then heat surrounding surfaces, such as soil or a body of water, thereby providing heat to support a number of activities, such as, but not limited to, a greenhouse 117 or an aquaculture bed.
  • the geothermal field 113 is forcibly vented by an induced draft fan 317 to an absorber 115, such as a monolithic lime or sodium carbonate absorber, for the removal of at least a portion of criteria pollutants.
  • an absorber 115 such as a monolithic lime or sodium carbonate absorber
  • the feed stock material contained plastics, or other substances which might cause the formation of either HC1 or SO 2
  • the exhaust leaving the at least one heat recovery device will be diverted to a passive sodium carbonate absorber to reduce any potential for excessive levels of these chemicals in the end recycled process gas product.
  • the filtered gas is pulled from the system and into an extractor 116 a carbon dioxide extractor 116 retrieves gaseous carbon dioxide for a carbon dioxide consumer.
  • Oxygen produced by the consumption of extracted carbon dioxide such as the conversion of carbon dioxide into oxygen by vegetation, may be vented back into the system 100 via a return air line 118 to provide recycled process gas or a cooling medium for the gasification reactor chambers 101, 102, 103.
  • a greenhouse 117, or some other agricultural carbon dioxide dispersal system replaces the carbon dioxide extractor 116. Carbon dioxide is then sequestered before the balance of the filtered exhaust stream is returned to the reactor chambers 101, 102, 103 via the return air line 118 as recycled process gas.
  • FIG 2 illustrates additional detail of the gasification system 100 combustion process loop.
  • Feed stock material is fed into the gasification chamber 101 through the primary access loading door 120, as shown in Figure 3B.
  • the primary access loading door 120 and any other residual removal ports are then sealed, and all gasification process gas intake ports are closed.
  • the aspirator assembly 229 then starts reducing the volume of ambient air within the reactor chamber 101. Following this air purge, which typically for a system containing 50 tons of feed stock material may take 15 minutes, at least one heater that is near the base of the reactor chamber 101 is activated.
  • the heater may include, but is not limited to, a fuel-fired burner or an electric thermal radiant heat assembly.
  • thermocouples are used to determine whether the average ambient temperature has reached the predetermined limit. These thermocouples may be positioned in a variety of locations, such as, but not limited to, below the grate, around the midsection of the reactor chamber 101, at the top of the reactor chamber 101, or in conjunction with additional thermocouples in any combination thereof.
  • a plurality of process gas inlets located below the grate level of the reactor chamber 101 are slowly opened.
  • the plurality of process gas inlets act as valves to keep the average internal temperature of the reactor chamber 101 within a predetermined range and prevent the incursion of ambient air, which may increase the oxygen level of the process air and cause combustion, from entering into the reactor chamber 101.
  • this predetermined temperature range is within approximately 350 and 750 degrees Fahrenheit, while the oxygen level is 4% to 11% of ambient.
  • the plurality of process gas inlets may be opened by a common electric motor that is controlled through the use of a process logic controller.
  • Oxygen and temperature sensors sample the interior environmental air and relay the information to the process logic controller.
  • the process logic controller may also be connected to data recorders and digital display panels in the system control cabinet. Such sensors may be located in a variety of positions, including, but not limited to, heavy vapor fuel gas evacuation ducts in the ceiling of the reactor and in a reinforced stainless steel cage located on the interior wall of the reactor chamber.
  • the aspirator assembly 229 begins extracting heavy vapor fuel gas out from the reactor chamber 101 through an aspirator assembly 229.
  • the aspirator assembly 229 uses impelled ambient air passing through a conduit coupling to create a negative back pressure in the reactor chamber 101 and the gas siphon assembly 225. This negative pressure creates a suction force that draws heavy vapor fuel gas from the reactor chamber 101 into the gas siphon assembly 225.
  • the gas siphon assembly 225 extends into and out of the reactor chamber 101, as shown in Figure 5 A.
  • a portion of the gas siphon assembly 225 that extends into the reactor chamber 101 is perforated and mounted along the ceiling of the reactor chamber 101. At least a portion of the gas siphon assembly 225 outside of the reactor chamber 101 is insulated.
  • the aspirator assembly 229 also mixes ambient air with the collected heavy vapor fuel gas, thereby creating a mixed gas.
  • Heavy vapor fuel gas extracted from the reactor chamber 101 will preferably enter the gas siphon assembly 225 at a temperature of approximately 800 degrees Fahrenheit. However, because the aspirator assembly 229 mixes the hot heavy vapor fuel gas with ambient air, the mixed fuel gas released from the aspirator assembly 229 will preferably have a temperature of approximately 600 degrees Fahrenheit, and is delivered to the flare assembly 210 at a rate of approximately 540 CFM.
  • the flare assembly 210 is operably connected to at least one burner 220 that initiates combustion of the mixed gas.
  • the at least one burner 210 consists of, but is not limited to, two 2 inch propane burners that utilize pilot igniters. Additionally, the combustion temperatures in the preferred embodiment are operated at approximately 1600 degrees Fahrenheit.
  • the flare temperature will be 1857 degrees Fahrenheit, and will produce total gas output of 47,903 lb/hr, a sensible heat content of 25,011,241 Btu/hr (ref. 77 degrees Fahrenheit), and a latent heat content of 5,337,774 Btu/hr.
  • a primary heat recovery device 211 a secondary heat recovery device 212, and a geothermal field 213 recover heat entrained in the combusted gas.
  • the primary heat recovery device 211 is configured to operate on the power or heat generated by the combustion of the heavy vapor fuel gas by the flare assembly 210.
  • the flare assembly may be built into, or a subcomponent of, the primary heat recovery device 211.
  • hot exhaust produced by the combustion of the heavy vapor fuel gas by the flare assembly 229 may be delivered to, and utilized by, the primary heat recovery device 211.
  • Exhaust from the primary heat recovery device 211 typically has a temperature in the range of 350 degrees to 500 degrees Fahrenheit.
  • the secondary heat recovery device 212 operates on the combusted exhaust provided by the primary heat recovery device 211. In the preferred embodiment, the secondary heat recovery device 212 further cools the combusted exhaust to the range of 200 degrees to 300 degrees Fahrenheit. hi the preferred embodiment, exhausted combusted gas from the secondary heat recovery device 212 is delivered to the geothermal field 213, which provides a final cooling stage. An induced draft fan 214 preferably provides momentum for combusted gas to pass through the geothermal field 213. The geothermal field will typically produce a final exhaust temperature of 60 degrees to 80 degrees Fahrenheit, which are approximately ambient conditions. In one embodiment of the invention, carbon dioxide separation may be provided at early stage by separator 216 that is operably connected to the geothermal field 213.
  • Filtered exhaust exiting the absorber 215 is typically comprised of water dioxide and carbon dioxide.
  • a carbon dioxide extractor 116 such as, but not limited to, a Wittmann carbon dioxide extractor, is employed to remove the carbon dioxide molecules from the filtered exhaust.
  • the extractor 116 is replaced by a greenhouse 117, or by an agricultural carbon dioxide dispersion system, whereby carbon dioxide is sequestered from the filtered exhaust.
  • the remaining filtered gas is then re-directed to the reactor chambers 101, 102, 103, where it is re-introduced into the gasification cycle as recycled process gas, and thereby eliminates the need for an exhaust stack.
  • Extracted carbon dioxide gas may be used for other industrial purposes, or to support vegetation, such as replenishing the carbon content of soil of an agricultural field by passing extracted carbon dioxide through a carbon dioxide dispersal system or venting it into a greenhouse.
  • oxygen that has been converted from extracted carbon dioxide may be recaptured and reintroduced into the gasification chamber as a cooling medium for the chambers 101, 102, 103, or as part of the ambient process gas intake.
  • Figures 3 and 5 show details of the waste gasification reactor chamber 101 of the present invention.
  • the capacity of the gasification reactor chamber 101 can be configured to hold a wide range of feed stock material, such as, but not limited to, as little as one ton or as much as one thousand tons of feed stock material.
  • Figures 5A and 5B illustrate the basic configuration of the gasification reactor chamber 101 of the preferred embodiment.
  • the gasification reactor chamber 101 incorporates a double walled configuration, in which the interior chamber 126 is sleeved inside the outer shell 127.
  • the interior chamber 126 of the present invention is capable of having a rectangular, square, or cylindrical configuration
  • the preferred embodiment of the present invention has at least five side walls, such as an octagonal or hexagonal shape, and is a continuously welded container of 1/2 inch thick, 316 or 304 stainless steel plate or cast iron.
  • a reactor chamber 101 an octagonal reactor chamber that is designed to hold approximately 50 tons of feed stock material will be approximately 24 feet tall and 8 feet wide on the sides.
  • At least one burner 220 is operably connected to the interior chamber 126, the at least one burner 220 providing heat to elevate the temperature inside the interior chamber 126.
  • two openings are positioned beneath grate level, each opening being operably connected to at least one natural gas or LPG-burner, thermal lance, electrical resistance heat generator, or other heat generating device.
  • Figure 5D illustrates a cross sectional side view of the gasification reactor chamber in accordance with one embodiment of the present invention.
  • the outer surface of the interior chamber 126 includes a plurality of aluminum convective cooling fins 130 that dissipate heat away from the surface of the interior chamber 126. Between the cooling fins 130 and the interior surface of the outer shell 127 is at least one layer of insulation 129.
  • the preferred embodiment of the invention utilizes an insulative jacket that is comprised of two layers of insulation, with the first layer 77, which covers the cooling fins, being a 2 inch thick blanket of ceramic fiber.
  • the preferred embodiment of the invention also includes vents 131 located on the sides of outer shell 127, as illustrated in Figure 5B. Because of the temperature gradient between the cooler outside ambient air and the elevated temperatures of the gasification reactor chamber 101, these vents 131 allow for outside air to rise into the space between the interior chamber 126 and the outer shell 127, and through the at least one layer of insulation 129, thereby providing cooling air flow through the mineral wool. In the preferred embodiment of the present invention, such vents 131 could allow for a sustainable external temperature of approximately 100 degrees Fahrenheit.
  • each wall of the interior chamber 126 has at least one process gas inlet 112.
  • each process gas inlet 112 has a 6 inch diameter.
  • at least two of these process gas inlets 112 are preferably operably connected to a common air supply manifold 125.
  • the manifolds 125 are comprised of 8 inch diameter tubing that circumscribes the outside diameter of the interior chamber 126, the tubing having a first end and a second end, the first end being connected to a variable speed blower that is located outside of the reactor chamber 101, and the second end being completely occluded.
  • a damper is preferably operably positioned between the blower and the manifold, the damper configured to control the introduction of the limited process gas necessary to maintain the gasification cycle and to prevent the inclusion of unwanted ambient air in the interior chamber 126.
  • Recycled process gas may be returned to the gasification reactor chamber 101 via a return air line 118.
  • the recycled process gas may be used as a cooling media for the reactor chamber 101, in which the recycled process gas flows between the insulative jacket and the outer shell 127.
  • the return air line 118 provides a path for the controlled introduction of the recycled process gas into the gasification cycle, the return air line being operably connected to the plurality of process gas inlets 112.
  • FIGS 3A, 3B, and 3C illustrate the outer shell 127 of the preferred embodiment.
  • the outer shell 127 is preferably constructed from A36 hot rolled structural shapes and steel sheet, that may be similar to painted metal ribbed panels, and provides mechanical support for the loaded reactor vessel.
  • the outer shell 126 may also provide attachment points for monitoring, ducting, insulation, and other gasification operating equipment.
  • Feed stock is loaded into the reactor chamber 101 through an access loading door 120, as shown in Figure 3 A, and placed on a grate 70, as illustrated in Figure 3D.
  • the gasification reactor chamber 101 may also include an additional opening near the floor of the chamber that is just below the highest edge of the bottom grate, and which allows for access for maintenance and repairs.
  • the maintenance opening is bolted and gasket into place.
  • Removal of residual solid waste after gasification is accomplished through a disposal opening 119, and is preferably lead away from the reactor chamber 101 via a conveyor 321.
  • the exact arrangement of the conveyor system is not critical and any arrangement for conveniently removing solid byproducts is acceptable as long as the reactor chamber 101 can be sealed off from outside ambient air during the gasification cycle.
  • the grate 70, which supports feed stock material within the reactor chamber 101 may have a sloped configuration that is designed to facilitate the movement of solid waste product remaining after the gasification process towards the disposal opening 119, as illustrated in Figure 3D.
  • Figure 3E illustrates another embodiment of the present invention, which includes at least one inclined surface beneath the grate 70 that tapers inward towards the disposal opening 119, the disposal opening 119 being located at the base of the reactor chamber 101.
  • Adjacent to the disposal opening 119 is a slatted discharge conveyor.
  • the slatted discharge conveyor is preferably positioned in a trench in the concrete floor and is configured to receive and remove any remaining debris from the reactor chamber 101 after the completion of the gasification cycle.
  • An air lock at the exit point of the slatted discharge conveyor is used to prohibit the unwanted incursion of ambient air into the reactor chamber 101.
  • both the disposal opening 119 and the primary access loading door 120 are hydraulically activated doors that are formed from 1/8 inch thick type 304 stainless steel, and are insulated with a ceramic blanket and/or mineral wool fiber. A seal insures an air-tight fit between the door and the top of the reactor.
  • Figures 3D and 3E also illustrate the perforated grate 70 within the interior reactor chamber 126, in which the perforated grate 70 acts as a primary reaction zone.
  • the perforations in the grate 70 are configured to allow the bottom portion of the feed stock material to be exposed to gasification process gas.
  • the perforations in the grate 70 may be configured to allow any remaining debris to fall below the grate for eventual removal from the reactor chamber 101, as illustrated in Figure 3E.
  • interior chamber includes at least one inclined surface, the at least one inclined surface 132 having a first portion and a second portion.
  • the first portion of the inclined surface 132 is operably connected to the bottom of the interior chamber, and tapers inwards to the second portion.
  • the second portion is operably positioned in proximity to the disposal opening 119.
  • the present invention increases the primary and secondary reaction zones through the incorporation of at least one perforated conduit 75, as illustrated in Figures 3D, 3E, and 5A.
  • the perforated conduit 75 extends from the base of the perforated grate 70 towards, but not reaching, the ceiling of the reactor chamber 101.
  • the at least one perforated conduit 75 is preferably positioned in proximity to the intersection of the reactor chamber walls, and extends outwards towards the center of the interior chamber 126.
  • the plurality of process gas inlets 112 passing through the walls of the interior chamber 126 are positioned relative to the location of the at least one perforated conduit 75.
  • the perforated conduit 75 then provides a passageway that permits process gas to travel in an upward direction along the perforated conduit 75. This configuration prevents the flow of process gas from being occluded by feed stock material covering the plurality of process gas inlets 112.
  • These perforations 76 are then configured to allow for the exposure of additional feed stock surface area to gasification process gas, with at least a portion of the perforated conduit 75 adding to the total surface area of the primary reaction zone, and the remaining exposed surface area adding to the total surface area of the secondary reaction zone.
  • the at least one perforated conduit 75 may be also positioned at a variety of locations, including, but not limited to, being offset away from the walls and towards the center of the feed stock, at various locations along the walls of the reactor chamber 101, through the center of the feed stock, and all other positions that would be understood and appreciated by one of ordinary skill in the art.
  • the at least one perforated conduit having a one foot by one foot construction and extends to within four feet of the top of the interior chamber 126, with the top being sealed with a solid cap.
  • perforated conduits 75 and/or an inner linear 76 also allows the gasification reactor chamber to have a column configuration that includes at least five sidewalls.
  • This column configuration and perforated conduits 75 and/or an inner linear 76 configuration eliminates the 50 ton capacity limitation of prior art gasification reactor chambers.
  • feed stock material may be top loaded into the column configuration, and therefore eliminate the repose fill problems associated with side loading a rectangular reactor chamber configuration, and allows feed stock material to be top loaded through the use of a conveyor.
  • Figure 5C illustrates an alternative embodiment of the gasification reactor chamber 101, in which an inner liner 76 is placed within the interior chamber 126, and preferably is position so as to leave a gap between the interior sidewalls of the interior chamber 126 and the inner liner 76, as illustrated in Figures 5C and 5D.
  • the inner liner 76 which may be constructed from heavy wire mesh, has a plurality of perforations that permit the flow of gasification process gas to the feed stock material.
  • the inner liner 76 is a 1 inch by one inch stainless steel mesh fabricated from 5/8 inch stainless steel wire and positioned 2 to 4 inches away from interior surface of the interior chamber 126.
  • Process gas is then able to circulate in and around the feed stock material along the sides of the inner liner 76, thereby allowing the side surfaces of the feed stock material to become part of the primary reaction zone. Additionally, because the inner liner 76 physically contains the feed stock material, the walls of the interior chamber 126 do not have any mechanical contact with the feed stock material. This lack of contact allows the walls of the interior chamber 126 to be fabricated from substantially thinner material, thereby further reducing the weight and fabrication expenses of the reactor chamber 101.
  • an octagonal reactor chamber of the present invention that is designed to hold the same 50 tons of feed stock material, and which includes eight perforated conduits 75, has a primary reaction zone of 498 feet at the sloped perforated grate 70, plus an additional 384 square feet from at least the lower portion of the perforated conduits 75, for a total primary reaction zone of 882 square feet.
  • an additional 782 square feet of secondary reaction zone is created, which is comprised of 384 square feet from at least a portion of the perforated conduits 75, and 398 square feet from the upper surface area of the feed stock.
  • the total primary and secondary reaction zone surface area is therefore 1,664 square feet, roughly 1.78 times that of conventional rectangular reactors.
  • gasification cycle time is a function of surface exposure to the process gas supply
  • an increase in the surface area of the primary and secondary reaction zones represents a significant reduction in the rate of reaction necessary for gasification, and thus reduces the cycle time required for a single charge of feed stock.
  • the maximum anticipated volume of heavy vapor fuel gas produced from feed stock material in the present invention could be reduced to less than 12 hours, instead of the 18 to 24 hour cycle times of prior art systems.
  • the present invention further eliminates the need to rely on multiple reactor chambers to meet system volume capacity requirements.
  • this configuration substantially reduces the external surface temperature of the gasification reactor chamber 101 during operation, thereby making the environment around the system safer for workers.
  • the lower operating temperature within the reactor of the present invention also improves the ultimate air quality of the final system exhaust. Constant cooling of the reactor interior chamber 126 by convection helps stabilize the reactor temperatures to as low as 750 degrees Fahrenheit. At this temperature level, there is insufficient thermal energy to create many of the complex chemical reformation reactions that occur in mass burn incinerators, some pyrolysis systems, some high temperature gasifiers, and plasma systems from the various materials that comprise the feed stock material within the reactor. Depression of the optimum operating temperature also inhibits the volatilization of most metals, thus virtually eliminating the metal content in exhaust air from the total system.
  • the simplified single gasification reactor chamber 101 of the present invention also has significant financial benefits over large, multi-celled fixed systems, in terms of flexibility, portability, and economics of installation, operation, and maintenance.
  • Faster gasification cycles at lower temperatures permit the gasification reactor chamber 101 to be fabricated from lighter and less expansive material.
  • the lightness of both the gauge of the material and insulative layers produces a significant reduction in the overall weight of the system. This reduction in weight translates into both lower material and installation expenses.
  • the time required for fabricating and installing such a system is greatly reduced by the elimination of refractory materials and associated refractory hanger installation.
  • the absence of the weight attributable to refractory material also allows for the use of lighter structural steel members.
  • repair and maintenance profiles for a stainless steel system are far superior to hot rolled steel structures that are painted. Additionally, the relative small size of the present invention allows a single gasification system to be economically and efficiently sited at the location of the fuel demand, such as the location of the at least one heat recovery device. These benefits allow a single reactor supplying energy from this alternative fuel-generating reactor to be economically and efficiently sited at the location of the fuel demand.
  • FIG. 6 illustrates details of the gas extraction assembly of the present invention.
  • the extraction scheme includes an aspirator assembly 229 that replaces the air-mixing chamber of the prior art.
  • the aspirator assembly 229 is capable of both evenly withdrawing heavy vapor fuel gas from the interior chamber 126 and completely mixing impelled ambient air with the extracted oxygen-deficient heavy vapor fuel gas, thereby creating an oxidized mixed gas.
  • the aspirator assembly 229 can also provide transport of the mixed gas over greater distances than conventional methods, thereby making the whole system more adaptable than current designs, especially for multiple cell systems.
  • a damper assembly which is the norm in prior art gasification systems, has been eliminated in the present invention in favor of employing a variable speed motor 227 as the driving device for extracting gas from the reactor chamber 101.
  • the motor 227 forces ambient air through a second passageway 228 and into an impeller 224, which subsequently supplies impelled air through a passageway 223 and into a conduit coupling 230.
  • a 10 hp motor 227 is mounted approximately 7 feet above floor level, the motor 229 being operably connected to a shutoff valve that is located thirty feet above floor level.
  • Figure 7 illustrates the preferred embodiment of the conduit coupling 230, which is shown as having a "Y" configuration, but may have a number of configurations, including a "T" shape, as would be understood and appreciated by one of ordinary skill in the art.
  • the conduit coupling 230 readily available from an industrial supply source.
  • the conduit coupling 230 is comprised of a first leg 141, a second leg 142, and a stem 143. High velocity impelled air passing along the first leg 141 and through the stem 143 of the conduit coupling 230 creates a suction force in the second leg 142, the attached single manifold pipe 226, and the gas siphon assembly 225, thereby creating a slight negative pressure in the interior chamber 126.
  • the gas siphon assembly 225 is sized according to the type of feed stock material and designed for the capacity of the chamber 101. In the preferred embodiment of the invention, the gas siphon assembly 225 is comprised of 3 inch diameter 316 stainless steel, schedule 40 piping.
  • the pipes are preferably mounted along the ceiling of interior chamber 126, and terminate at a single manifold pipe 226, with at least a portion of the piping inside the reactor chamber 101 being perforated so as to permit heavy vapor fuel gas to pass into the gas siphon assembly 225.
  • the suction force created by the aspirator assembly 229 allows for smooth and even extraction of heavy vapor fuel gases from the interior chamber 126, and increases the quantity of extracted heavy vapor fuel gas.
  • This even and smooth extraction provides a number of benefits, including: causing the gasification process to work with less fluctuation in gas volume removal from the reactor chamber 101 as the gasification process works its way through the raw feed stock material; reduces the total primary gasification process cycle time; and supplies a more homogenous and regulated flow of heavy vapor fuel gas product to the ultimate burner system that will combust the gas in the employed heat recovery strategy of the present invention.
  • the aspirator assembly 229 also overcomes problems associated with accelerating mixed gas for use in ancillary systems, hi the preferred embodiment, the gas siphon assembly 225, single manifold pipe 226, passageway 223, conduit coupling 230, and downstream pipe 231 are constructed from small diameter tubing, which, in conjunction with the motor 227, increases both the velocity and turbulence of the passing ambient air and heavy vapor fuel gas. As compared to the mixing obtained through conventional prior art methods, the increased velocity and turbulence created by the present invention significantly contributes to increasing the mixing of the gases, which improves the completeness of the combustion event.
  • This accelerated velocity may also provide back pressure to the supply lines, which allows for the proper functioning of attached heat recovery devices. In some instances, this higher velocity delivery makes the heat recovery device more efficient. Additionally, unlike prior art induced draft systems, the increased mixed gas velocity allows the invention to operate equipment that requires higher positive gas input pressures, such as common bottoming cycle electrical power generation turbines, boilers, carburetors, and other fuel consuming devices that require a given amount of supply line gas pressure in order to function properly. Unlike the current invention, prior art designs were typically unable to satisfy such positive pressure requirements, either because of the inability to pressurize the gas because of dependence on a natural draft-driven processes or because of problems and expense associated with the application of high temperature, in-line, induced draft fans.
  • process efficiency in gasification is directly related to the ability to control various functions through equipment sub-sets in the gasification process.
  • prior art damper assemblies typically guess at the amount of flow volume moving through the damper valve body.
  • the vacuum power and mixing air percentage of the aspirator assembly 229 of the present invention can undergo a wide range of adjustment through the modification of the ducting size for both the evacuated heavy vapor fuel gas and the ambient air intake line. Further refinements in air mix and flow can be achieved by varying the speed of the impeller 224.
  • damper assembly affords the present invention finite control over the extraction rate of the heavy vapor fuel gas from the reactor chamber 101 and the mixing event, and affords direct control over the exact flow volume through the system. Additionally, functions of the aspirator assembly 229 may be even more accurately controlled through the use of process control logic. These improvements allow for a finite level of process control which has not been possible in prior art natural draft systems.
  • the gasification reactor chamber described herein simplifies prior designs and is a significantly less costly assembly, providing both a smaller space requirement for such equipment and fewer parts than are represented in prior art systems.
  • the size of the aspirator assembly 229 may be up to 90% smaller than a conventional air-mixing chamber, which dramatically decreases fabrication costs, and installation time.
  • the elimination of a centralized gas collection duct, which is common to most prior art waste gasification systems, makes not only the entire configuration of multiple gasification reactor chambers at a given facility more flexible, but also makes a multi- cell configuration simpler and less expensive to operate. Since there is no longer reliance on the central collection duct, the gasification vessels can be arranged independently, or along different vertical planes than previous designs allowed. Furthermore, the flexibility of the present invention does not suffer from the prior art's cumbersome and difficult methods of moving the heavy vapor fuel gas from its point of formation to the point of combustion.
  • the single flare assembly of the prior art is usually a cylinder, approximately 6 feet in interior diameter, and is made of a spun ceramic fiber or refractory casting liner that is position inside a steel exterior jacket. Piercing the sides of this assembly along alternating left and right ports are four to eight pilot igniters. These igniters provide an open flame for the purpose of facilitating the combustion of the incoming mixed gasses.
  • the gasification system of U.S. Pat. No. 6,439,135 utilizes a single flare assembly wherein the heavy vapor fuel gas from multiple reactor chambers converges for combustion, and in which the combusted exhaust is typically subsequently vented into the atmosphere via an exhaust stack.
  • the present invention incorporates a dedicated flare assembly 210a, 210b, 210c for each reactor chamber 101, 102, 103, as illustrated in Figure 1.
  • FIG. 4 illustrates the preferred embodiment of the flare assembly 210.
  • the flare assembly is comprised of a targeting nozzle 243, thermal insulation 241, a housing 240, and at least one burner 220.
  • the targeting nozzle 243 has a conical funnel configuration that is constructed from cast ceramic and is enclosed in a stainless steel housing 240.
  • the conical funnel configuration of the targeting nozzle 243 is configured to restrict the incoming flow of mixed gas 239 from the aspirator assembly 229 into a combustion focus point 242.
  • the conical funnel design of the targeting nozzle 237 supplements the mixing of the heavy vapor fuel gas and ambient air received from the aspirator assembly 229, thereby further improving the combustibility of the mixed gas 239.
  • the conical design of the targeting nozzle 237 accelerates the velocity of the mixed gas through the nozzle.
  • at least one burner 220 that provides an ignition spark or raw flame to ignite the incoming mixed gas.
  • the at least one burner 220 is comprised of two Maxon Kinemax 2 inch diameter burners.
  • the flare assembly 210 of the present invention has a number of benefits.
  • the number of igniter burners 220 required to adequately combust the mixed gas is reduced. Reduction in the number of igniter burners 220 substantially reduces the consumption of supplemental fuel by the system.
  • the configuration of the targeting nozzle 237 offers better control for mixed gas flaring, and can also be used as an injection point for the processing of waste oil, paints, or other volatile liquids.
  • the flare assembly 210 is also much smaller than conventional flares. This saves on fabrication and installation expenses, and reduces the overall size of the system.
  • a primary heat recovery device 211 utilizes the combustion of the mixed gas, thereby relying on the fuel content of the heavy vapor fuel gas for operation.
  • the flare assembly may be built into, or be a sub-component of, the primary heat recovery device 211.
  • the primary heat recovery device may receive hot combusted exhaust gas from the flare assembly 210, as illustrated in Figure 2.
  • These combusted gases may be directly supplied as the primary fuel source for powering or heating primary heat recovery devices 211 such as, but not limited to, hot water heaters, boilers, refrigeration systems, dryers, omnivorous fuelMnternal combustion engines, and turbines.
  • primary heat recovery devices 211 such as, but not limited to, hot water heaters, boilers, refrigeration systems, dryers, omnivorous fuelMnternal combustion engines, and turbines.
  • Such use of heavy vapor fuel gases would provide an alternative to the expense and conservation issues associated with the production, supply, and consumption of fossil fuels for powering such above-mentioned devices.
  • exhaust from the primary heat recovery device 211 typically has a temperature in the range of 350 degrees to 500 degrees Fahrenheit.
  • a secondary heat recovery device 212 may be utilized to further to recapture and reutilize the thermal energy entrained in the exhaust from the primary heat recovery device 211, and via subsequent use, provide a further cooled exhaust that preferably has a temperature in the range of 200 degrees to 300 degrees Fahrenheit.
  • the closed-loop system includes a geothermal field 113 that utilizes the entrained hot air exhaust from the primary or secondary heat recovery devices 211, 212.
  • the geothermal field 113 provides a very low cost and maintenance-free system for final thermal energy recovery.
  • This geothermal field 113 also provides a no-operating cost method of reducing exhaust temperatures to meet intake requirements of emission absorbers 115 and carbon dioxide extractors 116.
  • Figure 8 illustrates the operation of one embodiment of the geothermal field 113.
  • An induced draft fan 317 provides momentum for intake exhaust 310 from a primary and/or secondary heat recovery device 211, 211 to flow through both a subsurface manifold piping system 315 and a geothermal loop 114.
  • the subsurface manifold piping system 315 may be located underground or beneath a body of water, and is comprised of inlet piping 316 and ventilation tubing 318.
  • a manifold piping system 315 that is comprised of four PVC inlet pipes 316 located six feet below ground or water, and twelve inch diameter ventilation tubing 318, can reduce an intake exhaust 310 heat of 500 degrees Fahrenheit to approximately 200 degrees Fahrenheit.
  • the geothermal loop 114 When the geothermal loop 114 is placed under a greenhouse 117, it warms surrounding soil, which transfers heat to the greenhouse. Ventilation fans may then distribute heat throughout the greenhouse. In winter months, heat provided from the geothermal field 113 is sufficient to maintain environmental temperatures within growing limits, with only minimal supplemental heat needed on the coldest days. This may serve to significantly reduce wintertime costs of greenhouse operations.
  • the use of a greenhouse 117, or other vegetative supporting system also allows for the option of venting extracted carbon dioxide from the extractor 116 to the greenhouse via piping 311.
  • the greenhouse 117 or other vegetative system may also replace the extractor 116, and be used to sequester carbon dioxide out from the filtered exhaust produced by the absorber 115.
  • one embodiment of the invention includes an absorber 115, such as, but not limited to, a monolithic lime absorber.
  • An absorber 115 such as a monolithic lime absorber absorbs HC1 molecules from exhaust gas that is passed through and around it, thereby reducing the HC1 concentration in the gas that is eventually returned to the chamber reactor 101.
  • pollutants may be removed by passing the exhaust stream through a chilled radiator, whereby the pollutants are collected and condensed in water vapor.
  • the filtered gas When the filtered gas leaves the absorber 115, it is basically comprised of water vapor, oxygen, hydrogen, nitrogen, carbon dioxide, and minimal trace elements.
  • the filtered gas is pulled from the system and into an extractor 116, such as a Wittmann carbon dioxide extractor, which removes the carbon dioxide molecules from the filtered gas.
  • an extractor 116 such as a Wittmann carbon dioxide extractor, which removes the carbon dioxide molecules from the filtered gas.
  • the cooled filtered exhaust may be vented into a greenhouse 117, where vegetation converts the carbon dioxide of the filtered gas into oxygen.
  • the filtered gas may be delivered to a carbon dioxide dispersal system, as previously discussed.
  • the resulting recycled process gas is then mainly comprised of water vapor and air that is delivered through a return line 118 and manifold system back to the gasification reactor chambers 101, 102, 103 for use in the gasification process.
  • the recycled process gas may be as a cooling media for the reactor chamber 101.
  • the now cooled filtered exhaust also represents a significant source for clean carbon dioxide.
  • carbon dioxide extraction could provide environmental and economic advantages.
  • piping 311 from the system 100 may deliver and vent accumulated carbon dioxide for facilitating plant growth.
  • Properly selected greenhouse plants could easily consume all of the extracted carbon dioxide in a reasonable time, thereby allowing the present invention to emit zero carbon dioxide emission from the disposal of MSW feed stock.
  • Current research indicates that increasing the Carbon dioxide level in a greenhouse 117 from ambient to as much as 1,500 ppm can increase the productivity of tomatoes, green peppers and lettuce by as much as 35%.
  • extracted carbon dioxide may be vented in a carbon dioxide dispersal system 400, in which carbon dioxide is passed through distribution chambers 410 located beneath, among other things, porous fill materials 411, filter fabric 412, topsoil 413, and vegetation 413. In addition to the vegetation converting the dispersed carbon dioxide into oxygen, released carbon dioxide also replenishes the carbon content of soil.
  • the foregoing system provides a low cost, closed-loop MSW gasification system with that allows for complete material recovery and recycling of metals, glass, minerals and salts. Furthermore, the present invention may efficiently recapture expended thermal energy while preventing overt discharge of air, solids, or waste water from the disposal of solid waste materials.

Abstract

L'invention concerne un système de gazéification qui comprend une chambre de réacteur de gazéification (101) pourvue de conduits perforés ou d'une enveloppe interne qui augmente la surface exposée de matériaux déchets aux conditions de gazéification, ce qui réduit la température de gazéification, le temps et la période de refroidissement entre les processus de gazéification consécutifs. Une fois qu'un aspirateur ait retiré et oxydé le gaz combustible de la chambre réacteur, un ensemble à renflement (229b) brûle le gaz combustible mélangé pour céder de la puissance ou de la chaleur à au moins un dispositif de récupération de chaleur (111). Le ou les dispositif(s) de récupération de chaleur recapture(nt) l'énergie thermique entraînée dans le gaz d'échappement, ce qui réduit la température et rend superflu toute cheminée d'échappement. Un absorbeur purifie le gaz d'échappement et un extracteur (117) retire le dioxyde de carbone. Une partie du dioxyde de carbone retiré peut être utilisée à des fins industrielles ou comme agent favorable à la végétation. Au moins une partie du gaz d'échappement restant est renvoyée à la chambre de réacteur en tant que gaz de procédé recyclé, ce qui complète un processus en boucle fermée.
PCT/US2003/016066 2002-05-17 2003-05-16 Appareil ameliore destine a la gazeification de dechets WO2003098111A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
AU2003233631A AU2003233631A1 (en) 2002-05-17 2003-05-16 Improved apparatus for waste gasification
CA002482557A CA2482557C (fr) 2002-05-17 2003-05-16 Appareil ameliore destine a la gazeification de dechets
GB0423188A GB2403284A (en) 2002-05-17 2003-05-16 Improved apparatus for waste gasification
EP03729070A EP1509726A1 (fr) 2002-05-17 2003-05-16 Appareil ameliore destine a la gazeification de dechets

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US38195802P 2002-05-17 2002-05-17
US60/381,958 2002-05-17

Publications (1)

Publication Number Publication Date
WO2003098111A1 true WO2003098111A1 (fr) 2003-11-27

Family

ID=29550170

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2003/016066 WO2003098111A1 (fr) 2002-05-17 2003-05-16 Appareil ameliore destine a la gazeification de dechets

Country Status (6)

Country Link
US (1) US20040103831A1 (fr)
EP (1) EP1509726A1 (fr)
AU (1) AU2003233631A1 (fr)
CA (1) CA2482557C (fr)
GB (1) GB2403284A (fr)
WO (1) WO2003098111A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005108894A1 (fr) * 2003-10-02 2005-11-17 The Boeing Company Générateur de gaz de synthèse refroidi par régénération

Families Citing this family (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060051274A1 (en) * 2004-08-23 2006-03-09 Wright Allen B Removal of carbon dioxide from air
JP3906313B2 (ja) * 2004-08-31 2007-04-18 株式会社加来野製作所 減圧式乾燥機及びそれを用いた木材の乾燥方法
US7621226B2 (en) 2005-07-01 2009-11-24 Natural Resource Recovery, Inc. System and method for recycling waste into energy
US9266051B2 (en) 2005-07-28 2016-02-23 Carbon Sink, Inc. Removal of carbon dioxide from air
EP2409753B1 (fr) * 2005-07-28 2017-07-19 Carbon Sink Inc. Suppression du dioxyde de carbone de l'air
US7641770B2 (en) 2006-08-30 2010-01-05 Natural Resource Recovery, Inc. System for recovery of hydrocarbons from tar sands
RU2008139902A (ru) 2006-03-08 2010-04-20 ГЛОБАЛ РИСЕРЧ ТЕКНОЛОДЖИЗ, ЭлЭлСи (US) Воздухозаборное устройство с функционализированной ионообменной мембраной для улавливания co2 из внешней среды
WO2008042919A2 (fr) * 2006-10-02 2008-04-10 Global Research Technologies, Llc Procédé et appareil permettant d'extraire le dioxyde de carbone de l'air
AU2008242845B2 (en) 2007-04-17 2012-08-23 Carbon Sink, Inc. Capture of carbon dioxide (CO2) from air
EP2212009A1 (fr) 2007-11-05 2010-08-04 Global Research Technologies, LLC Elimination de dioxyde de carbone contenu dans de l'air
CA2703551A1 (fr) 2007-11-20 2009-05-28 Global Research Technologies, Llc Collecteur d'air avec membrane echangeuse d'ions fonctionnalisee pour capturer le co<sb>2</sb> ambiant
CA3047633C (fr) * 2008-02-19 2023-08-01 Carbon Sink Inc. Extraction et sequestration de dioxyde de carbone
WO2009149292A1 (fr) 2008-06-04 2009-12-10 Global Research Technologies, Llc Capteur d’air d’écoulement laminaire avec matériaux sorbants solides pour capturer le co2 ambiant
CA2728705A1 (fr) 2008-06-26 2009-12-30 Casella Waste Systems, Inc. Systeme et procede pour le stockage de dechets integre
US8747500B2 (en) 2010-11-15 2014-06-10 Adaptivearc, Inc. Plasma assisted gasification system with internal syngas heater
US8747499B2 (en) 2010-11-15 2014-06-10 Adaptivearc, Inc. Modular plasma assisted gasification system
WO2012167070A1 (fr) 2011-06-03 2012-12-06 Dingrong Bai Systèmes et procédés de fabrication de charges d'alimentation de combustibles modifiés à partir de déchets
US9546760B2 (en) 2012-09-28 2017-01-17 Adaptivearc, Inc. Sealing system for a continuous feed system of a gasifier
WO2017130388A1 (fr) * 2016-01-29 2017-08-03 株式会社キンセイ産業 Procédé d'incinération de déchets par distillation sèche-gazéification
CA3069942C (fr) 2017-08-04 2023-05-09 Graymont (Pa) Inc. Systemes et procedes d'elimination du mercure ou de l'acide chlorhydrique a partir de flux gazeux a l'aide de particules contenant du calcium
WO2019161114A1 (fr) 2018-02-16 2019-08-22 Carbon Sink, Inc. Extracteurs à lit fluidisé pour la capture de co2 à partir d'air ambiant
US11286436B2 (en) 2019-02-04 2022-03-29 Eastman Chemical Company Feed location for gasification of plastics and solid fossil fuels
US11447576B2 (en) 2019-02-04 2022-09-20 Eastman Chemical Company Cellulose ester compositions derived from recycled plastic content syngas
US11939406B2 (en) 2019-03-29 2024-03-26 Eastman Chemical Company Polymers, articles, and chemicals made from densified textile derived syngas
EP3951265A4 (fr) * 2019-05-08 2022-11-23 Kinsei Sangyo Co., Ltd. Dispositif de traitement d'incinération par distillation à sec et gazéification
CN115261073B (zh) * 2022-07-28 2023-06-13 赣州市怡辰宏焰能源科技有限公司 一种炉内活动料仓的气化炉

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4145979A (en) * 1978-01-23 1979-03-27 Envirotech Corporation Afterburner assembly
US4295331A (en) * 1978-03-07 1981-10-20 Uriel Rekant Process for the production of energy from solid hydrocarbon fuels
US4305732A (en) * 1980-02-19 1981-12-15 Brennstoffinstitut Freiberg Gasification apparatus with pressure relieving means
US4448588A (en) * 1980-07-28 1984-05-15 Cheng Shang I Integrated gasification apparatus
US4878440A (en) * 1987-08-03 1989-11-07 Siemens Aktiengessellschaft Method and plant for thermal waste disposal
US5425317A (en) * 1992-10-21 1995-06-20 Metallgesellschaft Aktiengesellschaft Process for gasifying waste materials which contain combustible constituents

Family Cites Families (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US624388A (en) * 1899-05-02 siemens
US685539A (en) * 1899-03-30 1901-10-29 William Swindell Gas-furnace.
US2808012A (en) * 1952-03-10 1957-10-01 Babcock & Wilcox Co Fuel burning apparatus
NO145893C (no) * 1979-07-05 1982-06-16 Norsk Hydro As Metode og anordning for forbrenning av fast og flytende avfall
US4398475A (en) * 1981-06-15 1983-08-16 Ssk Corporation Hazardous waste incineration system
US4941415A (en) * 1989-11-02 1990-07-17 Entech Corporation Municipal waste thermal oxidation system
US5159899A (en) * 1990-06-18 1992-11-03 Zbigniew Dobrzynski Obtaining energy from waste products by the pyrolysic process using exhaust gas from an internal combustion engine or turbine
US5222446A (en) * 1991-05-29 1993-06-29 Edwards A Glen Non-polluting incinerator
US5313894A (en) * 1991-07-23 1994-05-24 Kankyouhozen Kotobuki-Seisakusyo Co., Ltd. Structure of incinerator plant
US5279234A (en) * 1992-10-05 1994-01-18 Chiptec Wood Energy Systems Controlled clean-emission biomass gasification heating system/method
AU667977B2 (en) * 1992-11-27 1996-04-18 Pilkington Glass Limited Glass furnaces
GB9224852D0 (en) * 1992-11-27 1993-01-13 Pilkington Glass Ltd Flat glass furnaces
JPH0719008A (ja) * 1993-06-30 1995-01-20 Aisin Seiki Co Ltd スターリングエンジン用加熱装置
JP2909393B2 (ja) * 1994-09-22 1999-06-23 株式会社キンセイ産業 廃棄物の乾留ガス化焼却処理方法
US5823122A (en) * 1994-09-30 1998-10-20 Alternative Energy Development, Inc. System and process for production of fuel gas from solid biomass fuel and for combustion of such fuel gas
US5791266A (en) * 1996-11-25 1998-08-11 International Technology Corporation Combustion apparatus for highly energetic materials
US6439135B1 (en) * 1997-11-25 2002-08-27 International Environmental Technologies, Inc. Organic waste gasification processing and the production of alternative energy sources

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4145979A (en) * 1978-01-23 1979-03-27 Envirotech Corporation Afterburner assembly
US4295331A (en) * 1978-03-07 1981-10-20 Uriel Rekant Process for the production of energy from solid hydrocarbon fuels
US4305732A (en) * 1980-02-19 1981-12-15 Brennstoffinstitut Freiberg Gasification apparatus with pressure relieving means
US4448588A (en) * 1980-07-28 1984-05-15 Cheng Shang I Integrated gasification apparatus
US4878440A (en) * 1987-08-03 1989-11-07 Siemens Aktiengessellschaft Method and plant for thermal waste disposal
US5425317A (en) * 1992-10-21 1995-06-20 Metallgesellschaft Aktiengesellschaft Process for gasifying waste materials which contain combustible constituents

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2005108894A1 (fr) * 2003-10-02 2005-11-17 The Boeing Company Générateur de gaz de synthèse refroidi par régénération

Also Published As

Publication number Publication date
CA2482557C (fr) 2009-12-29
GB2403284A (en) 2004-12-29
GB0423188D0 (en) 2004-11-24
US20040103831A1 (en) 2004-06-03
AU2003233631A1 (en) 2003-12-02
CA2482557A1 (fr) 2003-11-27
EP1509726A1 (fr) 2005-03-02

Similar Documents

Publication Publication Date Title
US6938562B2 (en) Apparatus for waste gasification
CA2482557C (fr) Appareil ameliore destine a la gazeification de dechets
US20170218274A1 (en) Waste Incinerator
US7906695B2 (en) Biomass conversion by combustion
US20060219139A1 (en) Mobile solid waste gasification unit
CN207081009U (zh) 一种农村生活垃圾热解气化系统
US6485296B1 (en) Variable moisture biomass gasification heating system and method
US20170218284A1 (en) SYSTEM AND METHOD FOR PRODUCING LOW NOx AIR EMISSIONS FROM GASIFICATION POWER PLANTS
RU2353590C2 (ru) Способ и система для термической утилизации отходов и их применение для обработки отходов с высоким содержанием воды
EP1269077B1 (fr) Procede et dispositif permettant de bruler un combustible solide
US6715431B1 (en) Multifunctional disposal apparatus
AU2001244880A1 (en) Method and device for combustion of solid fuel, especially solid waste
CN109631042A (zh) 一种垃圾热解减容方法
CN100432532C (zh) 一种垃圾组合焚烧处理方法及专用立式富氧连续焚烧风火炉
JP3128784U (ja) 有機汚泥を燃料とする熱分解給湯装置
CN104100980B (zh) 一种小型垃圾炭化燃烧炉
US4706645A (en) Method and system to provide thermal power for a power plant
CA2522384C (fr) Conversion de la biomasse par combustion
WO2012066179A1 (fr) Procédé et four pour l&#39;incinération d&#39;un combustible solide
CN217535927U (zh) 一种新型回转式气化炉
CN217464436U (zh) 一种垃圾热解气化炉
CA2486318A1 (fr) Appareil et methode pour gazeifier des matieres organiques solides
JP2991638B2 (ja) 廃棄物焼却装置
JP2005121342A (ja) 循環流動層炉の運転方法
JPH0694228A (ja) 炭化式ゴミ焼却装置

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NI NO NZ OM PH PL PT RO RU SC SD SE SG SK SL TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IT LU MC NL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

ENP Entry into the national phase

Ref document number: 0423188

Country of ref document: GB

Kind code of ref document: A

Free format text: PCT FILING DATE = 20030516

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWE Wipo information: entry into national phase

Ref document number: 2482557

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 2003233631

Country of ref document: AU

WWE Wipo information: entry into national phase

Ref document number: 2003729070

Country of ref document: EP

WWP Wipo information: published in national office

Ref document number: 2003729070

Country of ref document: EP

WWW Wipo information: withdrawn in national office

Ref document number: 2003729070

Country of ref document: EP

NENP Non-entry into the national phase

Ref country code: JP

WWW Wipo information: withdrawn in national office

Country of ref document: JP