EP1323809B1 - Réacteur à lit descendant à co-courant - Google Patents

Réacteur à lit descendant à co-courant Download PDF

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Publication number
EP1323809B1
EP1323809B1 EP02027458A EP02027458A EP1323809B1 EP 1323809 B1 EP1323809 B1 EP 1323809B1 EP 02027458 A EP02027458 A EP 02027458A EP 02027458 A EP02027458 A EP 02027458A EP 1323809 B1 EP1323809 B1 EP 1323809B1
Authority
EP
European Patent Office
Prior art keywords
gas
shaft
lock
shaft body
reactor
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.)
Expired - Lifetime
Application number
EP02027458A
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German (de)
English (en)
Other versions
EP1323809A2 (fr
EP1323809A3 (fr
Inventor
Jürgen Möser
Manfred Schulz
Thomas Flick
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.)
Smile Beteiligungs GmbH
Original Assignee
Smile Beteiligungs GmbH
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 Smile Beteiligungs GmbH filed Critical Smile Beteiligungs GmbH
Priority to SI200230833T priority Critical patent/SI1323809T1/sl
Publication of EP1323809A2 publication Critical patent/EP1323809A2/fr
Publication of EP1323809A3 publication Critical patent/EP1323809A3/fr
Application granted granted Critical
Publication of EP1323809B1 publication Critical patent/EP1323809B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • 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
    • C10J3/32—Devices for distributing fuel evenly over the bed or for stirring up the fuel bed
    • 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
    • C10J3/08—Continuous processes with ash-removal in liquid state
    • 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
    • C10J3/06—Continuous processes
    • C10J3/14—Continuous processes using gaseous heat-carriers
    • 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
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • 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
    • F23G5/0276—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using direct heating
    • 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
    • F23G5/04—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment drying
    • 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
    • F23G5/24—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a vertical, substantially cylindrical, 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
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B1/00—Shaft or like vertical or substantially vertical furnaces
    • F27B1/02—Shaft or like vertical or substantially vertical furnaces with two or more shafts or chambers, e.g. multi-storey
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B1/00—Shaft or like vertical or substantially vertical furnaces
    • F27B1/10—Details, accessories, or equipment peculiar to furnaces of these types
    • F27B1/16—Arrangements of tuyeres
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B1/00—Shaft or like vertical or substantially vertical furnaces
    • F27B1/10—Details, accessories, or equipment peculiar to furnaces of these types
    • F27B1/20—Arrangements of devices for charging
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D1/00—Casings; Linings; Walls; Roofs
    • F27D1/0003—Linings or walls
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/001—Extraction of waste gases, collection of fumes and hoods used therefor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D3/00—Charging; Discharging; Manipulation of charge
    • F27D3/0025—Charging or loading melting furnaces with material in the solid state
    • F27D3/0032—Charging or loading melting furnaces with material in the solid state using an air-lock
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D7/00—Forming, maintaining, or circulating atmospheres in heating chambers
    • F27D7/06—Forming or maintaining special atmospheres or vacuum within heating chambers
    • 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
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • 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
    • C10J2300/0903—Feed preparation
    • C10J2300/0909—Drying
    • 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
    • C10J2300/0943—Coke
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • C10J2300/1634—Ash vitrification
    • 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
    • C10J2300/1869—Heat exchange between at least two process streams with one stream being air, oxygen or ozone
    • 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
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/20—Combustion to temperatures melting waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2205/00—Waste feed arrangements
    • F23G2205/16—Waste feed arrangements using chute
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2205/00—Waste feed arrangements
    • F23G2205/18—Waste feed arrangements using airlock systems
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/26—Biowaste
    • F23G2209/261—Woodwaste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/28—Plastics or rubber like materials
    • 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
    • F23G2900/7004—Incinerating contaminated animal meals
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
    • F23J2900/15081—Reheating of flue gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27M—INDEXING SCHEME RELATING TO ASPECTS OF THE CHARGES OR FURNACES, KILNS, OVENS OR RETORTS
    • F27M2001/00—Composition, conformation or state of the charge
    • F27M2001/05—Waste materials, refuse
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27M—INDEXING SCHEME RELATING TO ASPECTS OF THE CHARGES OR FURNACES, KILNS, OVENS OR RETORTS
    • F27M2003/00—Type of treatment of the charge
    • F27M2003/14—Pyrolising

Definitions

  • the present invention relates to a DC shaft reactor for melting and gasifying feedstocks of different types and consistencies, such as pollutant-free and / or contaminated wood, domestic and bulky refuse, substitute fuels, pelleted dusts or animal meal, plastics, industrial and commercial waste.
  • a synthesis gas which is suitable for generating electrical energy and heat and / or is used as a basis for synthesis processes can be produced.
  • the solid product formed is a non-leachable slag and a material processable metal phase or a non-recoverable liquid phase, which is available for further processing.
  • DE 43 17 145 C1 describes a method and apparatus for degassing waste materials based on a coke-heated countercurrent shaft furnace.
  • the resulting dust-containing gas is completely removed and burned in the underlying melting and overheating zone with oxygen at high temperatures.
  • the countercurrent flow of the gas through the downwardly moving bed and the suction between the Kreislaufgasausaugung and the recirculation gas supply result in a variety of practical problems.
  • the result is short circuit flows in the shaft and insufficient heat transfer to the upper shaft area, which creates a contaminated gas with tar and dust components.
  • a complex gas treatment and purification is necessary.
  • a coke-heated Kreislaufgaskupolofen for material and / or energy recovery of waste materials is described. It consists of a vertical furnace shaft with below-the-aeration large-volume Kreislaufgasabsaugö réelleen, which are connected by channels and nozzles with the melting and superheating zone, above which a large-volume excess gas discharge level, the resulting gas from the process.
  • the furnace shaft part is narrowed in cross-section between the circulation gas and excess gas suction openings.
  • the heat transfer takes place as well as in DE 43 17 145 C1 by the countercurrent principle to the feedstock rising process gases.
  • the multiple countercurrent flow of the gas through the downwardly moving bed despite some modifications due to cross-sectional constriction in the shaft and cross-sectional widening in the gas outlet does not allow the processing of a wide range of feedstock.
  • a reactor for gasifying and / or melting feedstocks with a feed, pyrolysis, melt and superheat section is described.
  • the pyrolysis section has a cross-sectional widening as a gas feed space, into which at least one combustion chamber opens with at least one burner, through which hot combustion gases are fed to a forming bulk cone.
  • high-energy media are introduced by means of upper and lower injection means in the region of the melting and superheating zone and above the melt by means of oxygen lances and / or nozzles.
  • the disadvantage of this device is increased by the bulk cone
  • US 4,813,179 is a DC-shaft reactor for melting and gasifying feed known
  • the shaft body a Lock area is upstream with locks.
  • the lock area ends at a screw conveyor, which introduces feed into the shaft body.
  • the introduced feed is then conveyed in the vertical direction through a feed opening of the shaft body by means of a further screw conveyor to a rotating distribution plate, which spreads the feed over the entire cross-sectional area of the shaft body.
  • preheated reaction gas is fed for drying the feedstock via a gas supply device.
  • the object of the invention is to provide a direct current shaft reactor, with which useful gases, in particular combustible useful gases with a low particle load, can be produced even when different starting materials are used, the energy content of which can be used for the direct current shaft reactor.
  • the inventive DC-shaft reactor for melting and gasifying feedstock has a vertical shaft body. Within the shaft body, the feedstock is dried, heated and gasified. The shaft body can thus usually be subdivided into the areas of drying zone, degassing zone and gasification zone. The shaft body is followed by a receiving body, which serves to receive molten feedstock. Within this body is the Melting zone of the reactor formed. The shaft body and / or the receiving body are connected to a gas discharge device for discharging the Nutzgase generated within the reactor. In particular, the discharge device is arranged in the region between the shaft body and the receiving body and designed as a tube. Further, the vertically oriented shaft body has a feeder through which the feedstock is fed to the shaft reactor.
  • a gas supply device for supplying gas into the shaft body is connected to the shaft body.
  • the supplied gas which is preferably air or oxygen-enriched air, serves to dry the feedstock.
  • the gas supplied is preheated according to the invention.
  • the gas supply device according to the invention is connected to the gas discharge device.
  • the discharged from the reactor hot gas is thus used according to the invention for preheating the gas supplied to the shaft body.
  • the feed opening of the reactor is followed by a lock arrangement which controls the introduction of the feedstock. In the area of the lock arrangement, at least part of the gas supply device is connected to the lock chamber.
  • the inventive use of the discharged gas as an energy source means that no additional energy is required for preheating the gas and the feed already undergoes a first drying in the lock assembly.
  • the lock arrangement is thereby additionally used for drying the feedstock.
  • Another essential advantage of the invention is that heat is removed from the discharged gas. This simplifies the further processing or use of this gas.
  • the lock arrangement preferably has at least one lock chamber.
  • a first lock gate is opened to introduce the feed into the lock chamber.
  • this first lock gate is closed, so that the lock chamber is closed. In this state, possibly contained air can be sucked out of the lock chamber and / or replaced by another gas.
  • the second lock gate which leads in the direction of the interior of the shaft reactor, opened and the feed material passes from the lock chamber into the reactor.
  • the lock arrangement is designed so that the introduction of feed into the DC shaft reactor takes place almost free of freeze or low-shear. This reduces the risk of larger pieces of feedstock rolling to the reactor wall and segregation of the feedstock.
  • the adverse consequences of demixing, such as melting of Ofenausmautation, emergence of flow channels for the incoming gases and fluctuating gas qualities due to different reaction zones are thereby greatly reduced.
  • a low-shear introduction of material into shaft reactors can be achieved, for example, by the fact that the reactor shaft, which follows the lock arrangement, has a similar cross-sectional geometry.
  • the drop height of the supplied goods should be as low as possible. In particular not higher than three times the height of the feed in the lock arrangement.
  • the second floodgate should open as quickly as possible, so that the underside of the falling feed remains as horizontal as possible.
  • the feedstock in the lock assembly should not as far as possible already contain a bulk cone.
  • the first lock gate is designed as a slide with cutting edge in an advantageous manner.
  • the feedstock to be introduced almost corresponds to the geometry of the lock chamber and in particular has almost no bulk cone on.
  • the second lock gate can be opened as quickly as possible, it is carried out in an advantageous manner as a flap or slide.
  • the DC shaft reactor has a shaft body 10.
  • the shaft body 10 can be subdivided into a lock arrangement 12, a drying zone 14 adjoining the lock arrangement 12, a degassing zone 16 adjoining the drying zone 14, and a gasification zone 18 connected thereto.
  • a receiving body 20 connects, which serves to receive molten feedstock 22.
  • the cross-section of the receiving body is widened, so that an annularly formed gas collecting space 24 is formed, which surrounds the lower part of the gasification zone 18.
  • the gas collecting space 24 is connected to a gas discharge device 26 designed as a pipe in the illustrated embodiment.
  • the feed is introduced through a supply port 28 into the well body 10 via the gate assembly 12.
  • the feeding of the feed material takes place via the lock arrangement 12 in order to prevent the introduction of large amounts of ambient air, by means of which the melting and gasification process can be influenced in an uncontrolled manner.
  • the lock arrangement 12 has two lock devices or lock gates 30, 32, between which the lock chamber 34 is formed, the lock chamber 34 already being part of the shaft body 10.
  • a gas supply device 36 is provided in the region of the drying zone 14 of the shaft body 10.
  • the gas supply device 36 has a ring conduit 38 surrounding the shaft body 10, which is connected to a plurality of nozzles 40 distributed uniformly around the circumference.
  • About the gas feeder 36 is the feed in Area of the drying zone 14 preferably hot air, which may optionally be enriched with oxygen, fed to dry the feedstock.
  • a further gas supply means 42 is arranged, which also has a surrounding the shaft body 10 ring line 44.
  • the ring line 44 is connected to a plurality of circumferentially preferably uniformly distributed nozzle 46.
  • High-energy gases, oxygen, air or other gases suitable for controlling the melting and gasification process can be supplied to the feedstock via the gas feed device 42.
  • nozzles 48 are provided in the gasification zone 18. High-energy gas or other gases or substances controlling the melting and gasification process can in turn be supplied via the nozzles 48. Likewise, instead of the nozzles 48, it is also possible to provide burners which directly supply heat to the feedstock in the gasification zone 18.
  • the end region of the shaft body 10, which is rotationally symmetrical with respect to the longitudinal axis 50, has a slightly tapered conical shape, so that the feed material is retained somewhat in the region of the gasification zone 18.
  • a plurality of circumferentially distributed nozzles 54 are further arranged.
  • the nozzles 54 serve to introduce high-energy gases or corresponding substances. By the nozzles 54 it is ensured that the melt 22 remains liquid. Likewise, burners may be provided instead of the nozzles 54.
  • the gas supply device 36 is connected to the gas discharge device 26.
  • the tube of the gas discharge device 26 through which the hot gases produced in the reactor are discharged, to a heat exchanger 56.
  • the discharged gases or Nutzgase flow through the heat exchanger 56 and are then discharged from a pipe 58 preferably for further processing.
  • a Pipeline 60 connected. Through the pipe 60, air or other gas is passed into the heat exchanger 56, takes in the heat exchanger 56 heat from the useful gas and is discharged through a pipe 62 back out of the heat exchanger.
  • the tube 62 is then connected via a heater 64 and a pipe 66 to the ring line 38 of the gas supply device 36.
  • the heating of the gas supplied to the feed material by the gas feed device 36 in the region of the drying zone 14 is thus preferably preheated in operation exclusively by the heat of the useful gases with the aid of the heat exchanger 56.
  • the heating device 64 which may be, for example, an electric heater or a burner, the gas to be supplied via the gas supply device can be additionally heated.
  • the heater 64 can be used to heat the gas.
  • a part 35 of the gas feed device 36 is connected to the shaft body 10 in the region of the lock arrangement 12. Through this connection, the feedstock is already subjected to a first drying in the lock assembly 12.
  • a side wall 68 of the lock assembly 12 is double-walled.
  • heating and thus drying of the feed material in the lock chamber 34 can be achieved by passing a hot medium through the double-walled side wall 68.
  • This is preferably air or another gas, which is likewise preheated by the useful gas, preferably with the aid of the heat exchanger 56.
  • the ideal material input preferably requires a homogeneous mixture, in particular when adding additives such as coke and lime.
  • the entry is carried out according to the invention centrally on the axis of the reactor. Of the Reactor should be kept as full as possible during operation. A level monitoring is therefore preferably mounted directly below the lock gate 32. The filling takes place in a high clock rate.
  • the areas of the lock arrangement 12, the drying zone 14 and the degassing zone 16 are preferably cylindrical or slightly conically widening down to the gasification zone 18.
  • the transition between the zones takes place without a step-shaped or sudden cross-sectional enlargement, i. the transition is the same cross-section and without formation of shake-free cavities, steps or edges.
  • the drying zone 14 can also be designed with double walls, in particular for larger types. This allows indirect heating of the Gutcicle inside or ensuring a uniform temperature on the wall and a reduction of condensation phenomena on the inside.
  • the heat transfer medium is preferably also hot air used. The use of standing up at the end of the process flue gas is also possible.
  • the degassing zone 16 can also be designed double-walled in continuation of the drying zone 14.
  • the double-walled version can be replaced by a silicate brick lining.
  • the gasification zone 18 is the main reaction zone within the shaft reactor. Here, at temperatures of 1,200 to 1,400 ° C, the material and energetic conversion of the solids. The solid fuel produces gases and solid products from coke to ash. For the complete and uniform reaction, it is crucial that a homogeneous bed is flowed through uniformly by the degassing gas already produced and the gasification agent to be introduced here.
  • the gasification zone 18 must have a sufficient height for these reasons. This is achieved in that the gasification zone 18 is formed as a straight cylindrical portion with transition into a conical reduction of the cross section or immediately as an increasing taper. Since the material grain is reduced by the material transformations and related destructive forces, the cavities increase within the pouring column. By reducing the size of the shaft cross section in this area, the sinking speed of the Material column are evened out, flow channels are destroyed and the formation of larger voids in the bed is avoided.
  • the region of the gasification is likewise lined with a silicate mass.
  • the lower cylindrical or tapered region of the gasification region 18 projects into the molten zone 20.
  • the Schütt yarn located above it at least partially, at the same time prevail there high temperatures.
  • cooling takes place by means of indirect water cooling in the shaft wall 70.
  • the longer-chain hydrocarbons formed from the expired degassing and thermolysis reactions were thermally split here and at the same time participated in the gasification processes taking place.
  • the result is a combustible gas average calorific value with the main components carbon monoxide, carbon dioxide, hydrogen and water vapor without constituents of condensable hydrocarbons. Many of the chemical reactions that have taken place are endothermic. The temperature of the gas as well as the bed thus decreases.
  • the gas undergoes a deflection by about 180 ° and enters the shake-free space 24.
  • the gas has a temperature of about 1,000 ° C.
  • the gas collection chamber 24 is already part of the melting zone 20, which is substantially further up than the projecting gasification zone 18 above.
  • the Cylindrical melt zone 20 tapers conically downward and closes with the bottom plate above which the molten phase collects.
  • the melting zone 20 is provided in its entirety with a multi-layer ramming mass or equipped with a lining. The reason for this is the necessary high temperatures. Only in the area of the gas collection room a lining may not be necessary.
  • the completely degassed and coked solid is already partially sintered or melted and sinks from the gasification zone 18 into the molten zone 20.
  • Integrated into the molten zone 20 is a plane with a plurality of oxygen nozzles or injectors and / or oxidatively operated burners 54, which are also distributed symmetrically on the axis.
  • the molten material collects as a melt at the bottom of the reactor.
  • the emptying of this liquid melt takes place as usual in the foundry via a tap hole and a gutter 72.
  • a design with a forehearth or siphon is possible.
  • the melt With sufficiently large design and appropriate residence time of the melt, the melt will separate into a heavy metal-containing phase and a slag floating on it.
  • the product slag contains no organic substances and the inorganic components are stably incorporated into a silicate matrix.
  • the use as a material for harbor, landfill and road construction are known, as is possible the production of special molds and products, as they are common in the glass industry.
  • a preferred embodiment of the lock arrangement 12 is that the second lock gate 32 is designed as a quick-opening slide ( Fig. 2 ).
  • the floodgate 32 is designed in particular in several pieces.
  • the feed material contained in the lock chamber 34 falls evenly into the drying zone 14 of the shaft body 10. Previously, the feed was pre-dried with the part 35 of the gas feeder 36 connected to the lock chamber 34.
  • designed as a slide second lock gate 32 is advantageously provided with a cutting edge. As a result, the part of the feed material protruding into the lock chamber 34 can be cut off when the second lock gate 32 is closed, as a result of which the lock chamber 34 can be closed again.
  • the lock chamber 34 is completely filled and the part of the feed material which does not fit in is cut off.
  • the first lock gate 30 is designed as a slide with a cutting edge, which separates the upper part of the feed from the lock chamber 34.
  • the first lock gate 30 can also be made in several pieces in this embodiment.
  • the second lock gate 32 is initially closed and the first lock gate 30 is opened. As a result, feed material enters the lock chamber 34. After closing the first lock gate 30, the second lock gate 32 is opened, whereby the feed material falls into the shaft body 10. At the same time, additional feed material can already be introduced through the feed opening 28 which is provided on the first lock gate 30. Thereafter, the filling cycle begins again.

Claims (10)

  1. Réacteur à lit descendant à co-courant (10) pour fondre et gazéifier d'un matériau d'enfournement, comprenant
    un corps de puits vertical (10) pour sécher, chauffer et gazéifier le matériau d'enfournement, le corps de puits (10) comprenant une ouverture d'alimentation (28) pour l'alimentation en matériau d'enfournement,
    un corps récepteur (20) joignant le corps de puits (10) pour recevoir de matériau d'enfournement (22) fondu,
    un moyen de décharge de gaz (26) raccordé au corps de puits (10) et/ou au corps récepteur (20) pour décharger des gaz formés,
    un moyen d'alimentation en gaz (36), raccordé au corps de puits (10), pour alimenter de gaz le corps de puits (10) pour sécher le matériau d'enfournement, le moyen d'alimentation en gaz (36) étant raccordé au moyen de décharge de gaz (26) pour chauffer le gaz, et
    un ensemble de sas (12) comprenant au moins une chambre de sas (34),
    caractérisé en ce que
    l'ensemble de sas (12) est positionné en aval de l'ouverture d'alimentation (28), et
    au moins une partie (35) du moyen d'alimentation en gaz (36) et/ou au moins une partie du moyen de décharge de gaz (26) est raccordée à la chambre de sas (34).
  2. Réacteur à lit descendant à co-courant selon la revendication 1, caractérisé en ce que le moyen d'alimentation en gaz (36) et le moyen de décharge de gaz (26) sont raccordés l'un à l'autre par un échangeur de chaleur (56).
  3. Réacteur à lit descendant à co-courant selon la revendication 1 ou 2, caractérisé en ce que le moyen d'alimentation en gaz (36) est raccordé à un moyen de chauffage (64).
  4. Réacteur à lit descendant à co-courant selon l'une des revendications 1-3, caractérisé en ce que l'ensemble de sas (12) est disposé sensiblement axialement symétrique par rapport au corps de puits (10).
  5. Réacteur à lit descendant à co-courant selon l'une des revendications 1-4, caractérisé en ce qu'une paroi latérale (68) du corps de puits (10) est configurée à double paroi, spécialement dans la région de l'ensemble de sas (12), pour chauffer le matériau d'enfournement.
  6. Réacteur à lit descendant à co-courant selon la revendication 5, caractérisé en ce que la paroi latérale double (68) est raccordée au moyen d'alimentation en gaz (36).
  7. Réacteur à lit descendant à co-courant selon l'une des revendications 1-6, caractérisé en ce que la superficie de la section du corps de puits (10) dans la région de la zone de séchage (14) est similaire à la superficie de la section de l'ensemble de sas (12).
  8. Réacteur à lit descendant à co-courant selon l'une des revendications 1-7, caractérisé par une première porte de sas (30), façonnée particulièrement comme un coulisseau avec une arête coupante, et/ou une deuxième porte de sas (32) à ouverture rapide, façonnée particulièrement comme un coulisseau avec une arête coupante.
  9. Réacteur à lit descendant à co-courant selon la revendication 8, caractérisé en ce que la première porte de sas (30) et/ou la deuxième porte de sas (32) sont façonnées en plusieurs parties.
  10. Réacteur à lit descendant à co-courant selon l'une des revendications 1-9, caractérisé en ce que la hauteur de chute du matériau d'enfournement introduit à travers l'ensemble de sas (12) ne dépasse pas trois fois la hauteur de la chambre de sas (34).
EP02027458A 2001-12-14 2002-12-10 Réacteur à lit descendant à co-courant Expired - Lifetime EP1323809B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SI200230833T SI1323809T1 (sl) 2001-12-14 2002-12-10 Sotočni jaškasti reaktor

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE20120189U 2001-12-14
DE20120189U DE20120189U1 (de) 2001-12-14 2001-12-14 Gleichstrom-Schacht-Reaktor

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EP1323809A2 EP1323809A2 (fr) 2003-07-02
EP1323809A3 EP1323809A3 (fr) 2004-01-02
EP1323809B1 true EP1323809B1 (fr) 2009-04-01

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AT (1) ATE427347T1 (fr)
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Families Citing this family (7)

* Cited by examiner, † Cited by third party
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DE10226862B3 (de) * 2002-06-15 2004-01-29 Gesellschaft für Nachhaltige Stoffnutzung mbH Verfahren und Vorrichtung zur Erzeugung eines Brenngases aus Biomassen
DE10327178B3 (de) * 2003-06-17 2005-05-04 Hans Ulrich Feustel Anlage zur Herstellung von Metall- und Schlackeschmelzen sowie von Synthesegas
EP1493799A1 (fr) * 2003-07-04 2005-01-05 von Görtz & Finger Technische Entwicklungs Ges.m.b.H. Gazéification à vapeur instantanée de biomasse
FR2903168B1 (fr) * 2006-06-30 2008-08-22 Fayard Eliane Bruleur pour realiser la combustion de substances reputees difficilement combustibles
MD3959C2 (ro) * 2007-07-04 2010-04-30 Dinano Ecotechnology Llc Dispozitiv de încărcare a instalaţiei pentru prelucrarea materiei prime ce conţine carbon
GB2453111B (en) * 2007-09-25 2010-12-08 Refgas Ltd Gasification
DE102013218521A1 (de) * 2013-09-16 2015-03-19 Sgl Carbon Se Schachtofen und Verfahren zum Aufarbeiten von einem Fluor enthaltenden Abfallprodukt

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DE966459C (de) * 1952-06-29 1957-08-08 Paul Hahnel Dr Ing Verfahren zur oxydierenden und reduzierenden Behandlung oxydischer Erze in Schachtoefen
DE2633128C3 (de) * 1976-07-23 1980-06-26 Kernforschungsanlage Juelich, Gmbh, 5170 Juelich Feuerungsrost für eine Einrichtung zum Verbrennen von Abfallstoffen
BR7706858A (pt) * 1976-10-26 1978-07-04 Union Steel Corp South Africa Processo e aparelho para a producao continua de um gas redutor contendo monoxido de carbono e hidrogenio
US4530702A (en) * 1980-08-14 1985-07-23 Pyrenco, Inc. Method for producing fuel gas from organic material, capable of self-sustaining operation
US4584947A (en) * 1985-07-01 1986-04-29 Chittick Donald E Fuel gas-producing pyrolysis reactors
FR2596409B1 (fr) * 1986-04-01 1988-07-08 Distrigaz Sa Procede et appareil de gazeification de charbon en cocourant
FR2610087B1 (fr) * 1987-01-22 1989-11-24 Aerospatiale Procede et dispositif pour la destruction de dechets solides par pyrolyse
DE3734988A1 (de) * 1987-10-15 1989-04-27 Voest Alpine Ind Anlagen Verfahren zum kontinuierlichen betreiben einer waermerueckgewinnungsanlage und vorrichtung zur durchfuehrung des verfahrens
CA2036581C (fr) * 1990-02-23 1998-09-22 Gunter H. Kiss Methode de transport, de stockage intermediaire et de valorisation energetique et materielle de dechets de tous geres et dispositif associe
DE4030554A1 (de) * 1990-09-27 1992-04-09 Bergmann Michael Dr Verfahren und vorrichtung zur thermischen behandlung von abfallstoffen
DE4317145C1 (de) * 1993-05-24 1994-04-28 Feustel Hans Ulrich Dipl Ing Verfahren und Einrichtung zur Entsorgung unterschiedlich zusammengesetzter Abfallmaterialien
DE19816864C2 (de) * 1996-10-01 2001-05-10 Hans Ulrich Feustel Koksbeheizter Kreislaufgas-Kupolofen zur stofflichen und/oder energetischen Verwertung von Abfallmaterialien unterschiedlicher Zusammensetzung
DE19640497C2 (de) * 1996-10-01 1999-01-28 Hans Ulrich Dipl Ing Feustel Koksbeheizter Kreislaufgaskupolofen zur stofflichen und/oder energetischen Verwertung von Abfallmaterialien
DE10007115C2 (de) * 2000-02-17 2002-06-27 Masch Und Stahlbau Gmbh Rolan Verfahren und Reaktor zum Vergasen und Schmelzen von Einsatzstoffen mit absteigender Gasführung
DE10127138C2 (de) * 2000-06-23 2003-12-24 Nachhaltige Stoffnutzung Mbh G Verfahren und Vorrichtung zur Erzeugung eines Brenngases aus Biomassen
JP2002081624A (ja) * 2000-09-05 2002-03-22 Kawasaki Heavy Ind Ltd 廃棄物ガス化溶融炉と同溶融炉の操業方法

Also Published As

Publication number Publication date
DE50213409D1 (de) 2009-05-14
SI1323809T1 (sl) 2009-08-31
EP1323809A2 (fr) 2003-07-02
ATE427347T1 (de) 2009-04-15
EP1323809A3 (fr) 2004-01-02
DE20120189U1 (de) 2003-04-24

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