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EP1338847B1 - Réacteur vertical à cocourant - Google Patents

Réacteur vertical à cocourant Download PDF

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Publication number
EP1338847B1
EP1338847B1 EP03001006A EP03001006A EP1338847B1 EP 1338847 B1 EP1338847 B1 EP 1338847B1 EP 03001006 A EP03001006 A EP 03001006A EP 03001006 A EP03001006 A EP 03001006A EP 1338847 B1 EP1338847 B1 EP 1338847B1
Authority
EP
European Patent Office
Prior art keywords
zone
reactor according
gas
shaft reactor
gas supply
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
EP03001006A
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German (de)
English (en)
Other versions
EP1338847A1 (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
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Filing date
Publication date
Application filed by Smile Beteiligungs GmbH filed Critical Smile Beteiligungs GmbH
Priority to SI200330322T priority Critical patent/SI1338847T1/sl
Publication of EP1338847A1 publication Critical patent/EP1338847A1/fr
Application granted granted Critical
Publication of EP1338847B1 publication Critical patent/EP1338847B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • 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 specially adapted for furnaces of these types
    • F27B1/16—Arrangements of tuyeres
    • 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
    • C10J3/20—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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C5/00—Disposition of burners with respect to the combustion chamber or to one another; Mounting of burners in combustion apparatus
    • F23C5/08—Disposition of burners
    • F23C5/28—Disposition of burners to obtain flames in opposing directions, e.g. impacting flames
    • 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
    • F23G5/08—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
    • F23G5/24—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
    • 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
    • F23M5/00—Casings; Linings; Walls
    • F23M5/08—Cooling thereof; Tube walls
    • 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 specially adapted for furnaces of these types
    • 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
    • F27D17/30—Arrangements for extraction or collection of waste gases; Hoods 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
    • F27D3/16—Introducing a fluid jet or current into the charge
    • 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
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • C10J2300/0913—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
    • C10J2300/0913—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
    • C10J2300/09—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
    • C10J2300/16—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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/10—Drying by heat
    • 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
    • F23G2204/00—Supplementary heating arrangements
    • F23G2204/10—Supplementary heating arrangements using auxiliary fuel
    • F23G2204/103—Supplementary heating arrangements using auxiliary fuel gaseous or liquid fuel
    • 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
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/50009—Furnace with progressive waste movements in vertical or steeply inclined direction
    • 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
    • F27D19/00—Arrangements of controlling devices
    • F27D2019/0006—Monitoring the characteristics (composition, quantities, temperature, pressure) of at least one of the gases of the kiln atmosphere and using it as a controlling value

Definitions

  • the present invention relates to a DC shaft reactor for melting and gasifying feedstocks of different types and consistency, such as pollutant-free and / or contaminated wood, household and bulky refuse, substitute fuels, pelleted dusts or animal meal, plastics, industrial and commercial waste materials.
  • 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 198 16 864 A1 describes a cycle gas polyol furnace in which an excess gas suction is arranged below the melting and superheating zone. This results in a countercurrent gasification and heat transfer in the upper furnace shaft area, where the gas is sucked by means of large-volume openings and is passed through channels / nozzles in the melting and superheating zone. In the subsequent DC gasification, the gas is reduced at high temperatures and split longer-chain hydrocarbons. This arrangement reduces the negative influence of short-circuit currents.
  • DE 100 07 115 A1 describes a reactor for gasifying and / or melting feedstocks with a feed zone, a degassing and gasification zone and a melting and overheating zone.
  • the degassing and gasification zone has a cross-sectional widening as a gas supply space, into which at least one combustion chamber opens with at least one burner, through which hot combustion gases are supplied 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 the increased reactor surface in the region of the cross-sectional widening of the pyrolysis, since heat losses occur.
  • the hot gases entering the bed in direct current also form preferred flow channels, which results in an inhomogeneous reaction over the reactor cross-section.
  • 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 danger of damage to the direct current shaft reactor during their generation is reduced.
  • 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 vertically arranged shaft body thus has, in the transport direction, successively a drying zone for drying and heating the feedstock, a subsequent degassing zone for degassing the feedstock and a gasification zone for gasifying the feedstock.
  • the shaft body is followed by a receiving body, which serves to receive molten feedstock. Within this body, the melting zone of the reactor is formed.
  • the shaft body and / or the receiving body are equipped with a gas discharge device connected to the discharge of the useful gases generated within the reactor.
  • the discharge device is arranged in the region between the shaft body and the receiving body and designed as a tube.
  • the vertically oriented shaft body has a feeder through which the feedstock is fed to the shaft reactor.
  • a plurality of gas supply units are connected to the shaft body.
  • the gas supply units which are usually nozzles or the like.
  • the lower cylindrical or tapered region of the gasification region may project into the melting zone.
  • the Schütt yarn located above it at least partially, at the same time prevail there high temperatures.
  • cooling takes place according to the invention by means of indirect water cooling in the reactor shaft wall. Since at very high temperatures and the size of the area to be cooled a double-walled design of the reactor shaft wall is disadvantageous due to overheating occurring and destructions caused thereby, this cylindrical or tapered region is formed according to the invention as a coil.
  • a spiral pipe coil, through which a cooling medium flows, is particularly suitable for realizing the cooling in this area. In particular, a targeted cooling is possible.
  • the risk of vapor formation within the coil is very low due to the circulation of the liquid.
  • the coil is preferably connected in several areas with separate inflows and outflows, so that the excessively heated cooling liquid can be discharged directly from the coil.
  • nozzles or burners may be provided between the individual rings or spiral parts of the tube, so that the process control can be controlled very precisely also in this area.
  • the temperature can be controlled precisely in this area, the control is preferably carried out separately and thus independent of the regulation of the other nozzles and burners.
  • the degassing zone can be better utilized, so that degassing of these substances is possible even with different starting materials. Since, in particular, energy and thus heat are introduced into the degassing zone by supplying the gases in the degasification zone, a more uniform heating of the feedstock material can be ensured in the degasification zone over the cross section. Since, according to the invention, a plurality of gas feed units are arranged one behind the other in the transport direction, a preferably continuous heating of the feed material in the transport direction can be ensured. This makes it possible that even difficult-to-degassed feedstocks are degassed in the degassing zone.
  • the degassing thus takes place predominantly in the degassing zone of the DC-shaft reactor according to the invention, degassing of feedstock in the gasification or the melting zone is reduced or avoided. As a result, the efficiency of the shaft reactor can be significantly increased.
  • the shaft reactor according to the invention a high degree of degassing can be realized in the degassing, so that combustible Nutzgase can be generated, which have only a very low particle load.
  • the gas feed units are preferably arranged substantially uniformly distributed.
  • the gas supply units thus have a substantially equal distance from each other.
  • the individual gas supply units or a plurality of feed devices combined in each case into a group or feed unit are connected to a control device.
  • the control device it is possible to control or regulate the individual gas supply units and / or the feed units separately. This can be done, for example, by regulating the amount of gas delivered by the individual gas supply units, the oxygen content of the supplied gas and / or the temperature of the supplied gas.
  • the gas mixture can also be changed.
  • the figure shows a schematic side view of a DC-shaft reactor.
  • 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 melting zone 23 is formed in the upper region of the receiving body 20, the melting zone 23 is formed.
  • 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 collection chamber 24 is provided with an im illustrated embodiment formed as a pipe gas discharge device 26.
  • 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 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 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.
  • the feed material then passes via the lock arrangement 12 into the drying zone 14.
  • the shaft body 10 In the drying zone 14 and the adjoining zones 16, 18, the shaft body 10 is almost completely filled with feedstock during operation. Even in the drying zone 14, no or at most a low pour cone forms near the lock gate 32.
  • the shaft body 10 is thus cylindrical, at least in the region of the degassing zone 16, or is designed to widen without jerking in the transport direction.
  • the shaft inner wall of the shaft body 10 is thus smooth at least in the degassing zone 16 and has no steps or the like. On.
  • a gas supply unit 36 is provided in the region of the drying zone of the shaft body 10.
  • the gas supply unit 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.
  • the feed material in the region of the drying zone 14 preferably supplies hot air, which may possibly be enriched with oxygen, for drying the feedstock via the gas feed unit 36.
  • degassing zone 16 In the subsequent to the drying zone 14 degassing zone 16 are a plurality of gas feeders 46, which are in particular nozzles, is provided.
  • the gas supply means 46 are arranged distributed uniformly.
  • a plurality of gas supply means or nozzles 46 are arranged one after the other.
  • a plurality of nozzles 46 are connected to a feed unit 42.
  • a ring line 44 is provided, for which the nozzles 46 can be supplied together with gas.
  • the ring line 44 is thus connected to a plurality of circumferentially preferably uniformly distributed nozzles 46.
  • each ring line 44 has at least three nozzles.
  • the ring lines 44 which are each arranged in a horizontal plane, together with the nozzles or gas feed devices 46 individual feed units 42. Within the degassing zone 16 more in the illustrated embodiment, four feed units 42 are arranged. It is particularly preferred according to the invention to provide at least two feed units.
  • the individual feed units 42 are arranged offset from one another or rotated, so that nozzles 46 arranged one after the other in the transport direction of the feed material are not arranged above or behind one another, but offset or next to one another.
  • the individual feed units are arranged rotated relative to the feed unit arranged above by the same angle in each case.
  • the size of the rotation angle is preferably dependent on the number of nozzles 46 provided for each feed unit 42, so that a substantially uniform distribution of the nozzles 46 in the degassing zone 16 takes place.
  • the gas feed devices 46 Via the gas feed devices 46, high-energy gases, oxygen, air or other gases suitable for controlling the melting and gasification process can be supplied to the feedstock.
  • 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.
  • a side wall 56 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.
  • the lock assembly 12 has the task of continuous and homogeneous supply of material and the gas-tight seal against the environment.
  • 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.
  • the volume of the lock chamber 34 is fully utilized as possible and falls into the reactor shaft of the same diameter as possible.
  • 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 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 well 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 within the Bulk column. By reducing the size of the shaft cross-section in this area, the rate of descent of the material column can be made uniform, 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 gas flows through the zone of high-temperature gasification in co-current with the feedstock.
  • the longer-chain hydrocarbons resulting from the expired degassing and thermolysis reactions have been 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 tube coil 60 In the lower cylindrical or tapered region of the gasification region 18, which possibly projects into the melting zone 23, the tube coil 60 according to the invention is arranged. It is preferably provided with separate feeds and outlets not shown in the figure. Furthermore, 60 additional nozzles 48 or burner 54 may be provided between the individual rings or spiral parts of the coil. Below the water-cooled region of the gasification region 18, the gas undergoes a deflection by about 180 ° and enters the shake-free space 24. By the above-described endothermic processes, the gas has a temperature of about 1,000 ° C. After a certain gas calming and homogenization, the gas is sucked out of the reactor above.
  • the gas collection chamber 24 is already part of the molten zone 23, which is substantially higher than the projecting gasification zone 18 above, and at least partially surrounds the gasification zone 18.
  • the cylindrical melt zone 23 tapers conically downward and closes with the bottom plate above which the molten phase collects.
  • the melting zone 23 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 23.
  • Integrated into the molten zone 23 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 in the foundry usually via a tap hole and a gutter 72.
  • a design with 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.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Emergency Protection Circuit Devices (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Claims (13)

  1. Réacteur à cuve à cocourant pour fondre et gazéifier du matériau, comprenant
    un corps de cuve (10) vertical avec une zone de séchage (14) pour sécher et chauffer le matériau, une zone de dégazage (16) adjacente à la zone de séchage (14) pour dégazer le matériau, et une zone de gazéification (18) pour gazéifier le matériau, le matériau étant transporté de la zone de séchage (14) à travers la zone de dégazage (16) dans la zone de gazéification (18),
    un corps de réception (20) adjacent au corps de cuve (10) pour recevoir du matériau fondu (22), et
    un dispositif d'évacuation de gaz (26) relié au corps de cuve (10) et/ou au corps de réception (20) pour évacuer des gaz générés,
    plusieurs unités d'amenée de gaz (42) reliées au corps de cuve (10) étant prévues successivement dans la direction de transport du matériau, dans la zone de dégazage (16) pour amener des gaz dans la zone de dégazage (16),
    caractérisé en ce qu'un serpentin (60) est prévu dans la paroi de la cuve du réacteur dans la zone de passage entre la zone de gazéification (18) et la zone de fusion (23) pour guider la température.
  2. Réacteur à cuve à cocourant selon la revendication 1, caractérisé en ce que le serpentin (60) présente une forme spiralée.
  3. Réacteur à cuve à cocourant selon la revendication 1 ou 2, caractérisé en ce que le serpentin (60) forme une zone qui se rétrécit, en particulier de manière conique, dans la direction de transport du matériau.
  4. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 3, caractérisé en ce que dans plusieurs zones le serpentin (60) est relié à des entrées et sorties séparées.
  5. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 4, caractérisé en ce que les dispositifs d'amenée de gaz (46) sont pour l'essentiel répartis régulièrement.
  6. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 5, caractérisé en ce qu'au moins trois dispositifs d'amenée de gaz (46) sont prévus successivement dans la direction de transport.
  7. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 6, caractérisé en ce que plusieurs dispositifs d'amenée de gaz (46) sont disposés dans un plan horizontal.
  8. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 7, caractérisé en ce que les dispositifs d'amenée de gaz (46) disposés dans un plan sont reliés par une conduite en boucle (44) pour former une unité d'amenée (42).
  9. Réacteur à cuve à cocourant selon la revendication 8, caractérisé en ce que les dispositifs d'amenée de gaz (46) d'unités d'amenée (42) disposées successivement dans la direction de transport sont décalés les uns par rapport aux autres.
  10. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 4, caractérisé en ce qu'entre les différentes boucles ou parties spiralées du serpentin (60) des buses (48) ou brûleurs (54) supplémentaires sont prévus qui sont en particulier réglables séparément.
  11. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 10, caractérisé en ce que les dispositifs d'amenée de gaz (46) et/ou les unités d'amenée (42) sont reliés à un dispositif de commande.
  12. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 11, caractérisé en ce que des dispositifs d'amenée de gaz (46, 48) supplémentaires sont prévus dans la zone de séchage (14) et/ou la zone de gazéification (18).
  13. Réacteur à cuve à cocourant selon l'une quelconque des revendications 1 à 12, caractérisé en ce que le corps de cuve (10), du moins dans la zone de dégazage (16), présente une forme cylindrique ou s'évasant sans saut dans la direction de transport.
EP03001006A 2002-01-23 2003-01-17 Réacteur vertical à cocourant Expired - Lifetime EP1338847B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
SI200330322T SI1338847T1 (sl) 2002-01-23 2003-01-17 Reaktor z jaskom za enosmerni tok

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE20200935U 2002-01-23
DE20200935U DE20200935U1 (de) 2002-01-23 2002-01-23 Gleichstrom-Schacht-Reaktor

Publications (2)

Publication Number Publication Date
EP1338847A1 EP1338847A1 (fr) 2003-08-27
EP1338847B1 true EP1338847B1 (fr) 2006-03-29

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EP03001006A Expired - Lifetime EP1338847B1 (fr) 2002-01-23 2003-01-17 Réacteur vertical à cocourant

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EP (1) EP1338847B1 (fr)
AT (1) ATE321978T1 (fr)
DE (2) DE20200935U1 (fr)
ES (1) ES2261800T3 (fr)
SI (1) SI1338847T1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102004020919B4 (de) * 2004-04-28 2009-12-31 Kbi International Ltd. Reaktor zur thermischen Abfallbehandlung mit Eindüsungsmitteln
US20130142723A1 (en) * 2011-12-06 2013-06-06 General Electric Company Biomass gasification systems having controllable fluid injectors
DE102014106901A1 (de) * 2014-05-16 2015-11-19 Steenova UG (haftungsbeschränkt) & Co. KG Vergaser und Verfahren zur Erzeugung eines brennbaren Gases aus kohlenstoffhaltigen Einsatzstoffen
NL2030051B1 (en) * 2021-12-07 2023-06-22 Pronovation B V Down-draft co-current reduction furnace (DCR Furnace)

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE50910C (de) * — W. F. M. Mc. CARTY, 501 Seventh Street, North-West, W. H. ASHTON, 3432 P. Street, North-West, und H. D. WALBRIDGE, 902 Fourteenth Street, North-West, sämmtlich in City and County of Washington, District of Columbia, V. St. A Vorrichtung und Verfahren zur unmittelbaren Gewinnung von Eisen aus Erzen
US2634116A (en) * 1949-09-26 1953-04-07 Witt Joshua Chitwood Method of and apparatus for clinkering cement raw materials and the like
DE1152653B (de) * 1958-11-25 1963-08-08 Rheinische Kalksteinwerke Schachtoefen zum Brennen von Kalkstein oder sonstigen Karbonaten mit Abgasumwaelzung
US3355158A (en) * 1966-04-26 1967-11-28 Harbison Walker Refractories Shaft kiln
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
DE4022535C1 (fr) * 1990-04-12 1992-01-02 Thermoselect Ag, Vaduz, Li
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
DE19608826C2 (de) * 1996-03-07 1998-03-26 Walter Kuntschar Gleichstrom-Vergasungsreaktor
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
TW409172B (en) * 1999-01-27 2000-10-21 Sumitomo Metal Ind Waste gasification melting furnace and gasification melting method
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
DE10051648A1 (de) * 2000-02-25 2001-09-13 Mitteldeutsche Feuerungs Und U Verfahren und Schacht-Schmelz-Vergaser zur thermischen Behandlung und Verwertung von Abfallstoffen
DE10030778C2 (de) * 2000-06-23 2002-11-14 Nachhaltige Stoffnutzung Mbh G Verfahren und Vorrichtung zur Erzeugung eines Brenngases aus Biomassen

Also Published As

Publication number Publication date
DE50302772D1 (de) 2006-05-18
ES2261800T3 (es) 2006-11-16
ATE321978T1 (de) 2006-04-15
DE20200935U1 (de) 2003-05-28
EP1338847A1 (fr) 2003-08-27
SI1338847T1 (sl) 2006-10-31

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