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EP1261827B1 - Reacteur et procede de gazeification et/ou de fusion de matieres - Google Patents

Reacteur et procede de gazeification et/ou de fusion de matieres Download PDF

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Publication number
EP1261827B1
EP1261827B1 EP01911636A EP01911636A EP1261827B1 EP 1261827 B1 EP1261827 B1 EP 1261827B1 EP 01911636 A EP01911636 A EP 01911636A EP 01911636 A EP01911636 A EP 01911636A EP 1261827 B1 EP1261827 B1 EP 1261827B1
Authority
EP
European Patent Office
Prior art keywords
section
reactor
gases
gas
melting
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
EP01911636A
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German (de)
English (en)
Other versions
EP1261827A1 (fr
EP1261827B8 (fr
Inventor
Eckhardt Tischer
Frank Wuchert
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.)
KBI INTERNATIONAL Ltd
Original Assignee
Masch und Stahlbau GmbH
Maschinen- und Stahlbau GmbH
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Filing date
Publication date
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Publication of EP1261827B1 publication Critical patent/EP1261827B1/fr
Publication of EP1261827B8 publication Critical patent/EP1261827B8/fr
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Classifications

    • 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
    • F23G5/02—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
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • C10J3/74—Construction of shells or jackets
    • 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
    • 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
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/101—Combustion in two or more stages with controlled oxidant supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/104—Combustion in two or more stages with ash melting stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/106—Combustion in two or more stages with recirculation of unburned solid or gaseous matter into combustion chamber
    • 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
    • F23G2207/00—Control
    • F23G2207/20—Waste supply
    • 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
    • F23G2900/50002—Burning with downwards directed draft through the waste mass

Definitions

  • the present invention relates to a reactor and a Process for gasifying and / or melting substances. Especially the invention relates to the material and / or energetic Utilization of any waste, e.g. with predominantly organic components but also of hazardous waste.
  • the reactor according to the invention and the process are suitable but also for gasification and melting of feedstocks any composition or for energy through the use of organic substances.
  • DE 198 16 864 A1 shows a coke-heated Circulation gas cupola, in which the excess gas suction is arranged below the melting and superheating zone.
  • the excess gas suction is arranged below the melting and superheating zone.
  • An object of the present invention is therefore to an improved reactor and method for gasifying and To provide melts of feedstocks which the Avoid disadvantages of the prior art.
  • a special one The task is simple, inexpensive and environmentally sound material and / or energy recovery of waste to enable.
  • the aim is functional reliability to increase a corresponding reactor, by the associated with the recirculation gas guide Operating uncertainties are largely avoided.
  • a Another object of the invention is the pollution in the suctioned off excess gas significantly reduce the effort in a subsequent gas purification can be minimized.
  • a Pre-tempering section in which the waste For example, predried at temperatures around 100 ° C. become.
  • modified embodiments may in this Section may also be a cooling of the starting materials if this is useful for the overall process.
  • An advantageous embodiment of the reactor is apparent characterized in that the total length of feeding section and Pre-tempering section several times larger than the diameter of the feed section.
  • the reactor can its upper end by a lock, a double flap system or a similar facility. This is the uncontrolled entry of ambient air and the escape of gases from the bed even better avoided.
  • the reactor is substantially cylindrical constructed and the Gaszu 1500raum and the Gasabsaugraum are designed annular, so that the gas supply and the Gas extraction on the entire circumference of the Schüttklale respectively.
  • This embodiment is particularly suitable for Utilization of predominantly organic starting materials.
  • Other Embodiments, e.g. more suitable for other starting materials are non-cylindrical basic shapes and different positioned and shaped gas extraction means and own feeder.
  • the reactor is double-walled and in the wall cavity a heat transfer medium is guided.
  • a heat transfer medium On the one hand can be cooled by the wall, causing the material stress is reduced, on the other hand, depending on used feedstock and the resulting Heat demand of the Schüttklale if necessary additional heat be supplied or derived from this heat.
  • the o.g. Objects of the invention are also by the in Claim 12 specified method for gasification and / or Melting of ingredients dissolved, which u.a. advantageous for material and / or energy recovery of waste and other input materials.
  • the process steps essential to the invention can be advantageous be further developed by a predrying of Feedstock by heating the pouring column above the Level at which the shock-like heating takes place about 100 ° C is made.
  • This will be water shares of Feedstock largely evaporated, which also the desired automatic downward movement of the insert is improved.
  • a modified process variant there is no pre-drying of the starting materials or a Cooling of the starting materials, the latter being expedient can be used to adhere to the hot starting materials Wall of the feed section to avoid.
  • the negative pressure for the extraction of the excess gases is controllable, wherein the Extraction should be done so that on the one hand no gas upwards escapes from the reactor and on the other hand only minimal Sucked additional amounts of ambient air through the pillar become.
  • Minimizing the amount of in the reactor existing false air aims to reduce the proportion of nitrogen oxides to reduce in excess gas and also the total amount of gas keep small to the subsequent gas economy easy to design.
  • the single figure shows a simplified sectional view a reactor according to the invention.
  • the reactor shown in the figure has at its upper end a Zuurerabites 1 with at least one Feed opening 2, via which the material and / or energy is fed to be recycled feedstock.
  • this feedstock Preferably In this feedstock, the proportion of organic predominates Ingredients, so that the reactor and the described method especially for the treatment of conventional Domestic waste and household-type commercial waste is suitable.
  • the flammable ones Components are not sufficiently high to prevent the combustion and to carry out gasification processes, the Feedstock combustible additives or energy sources be added. It is possible in conventional To add a certain amount of coke or the total calorific value to increase by adding wood. In certain circumstances it may also be useful to add other additives, for example, the adjusting pH to influence. Such measures are, however, those skilled in the art known, so that on a detailed presentation of this Job is omitted.
  • a pre-tempering section closes below 5, in the example shown, the pre-drying the feedstock serves.
  • the feeding section and the Vorstemper istsablie are advantageous cylindrical or conically shaped with slight cross-sectional increase downwards.
  • the pre-tempering section 5 has a double Wall, wherein a wall cavity 6 is formed in which a heat transfer medium is guided. With help the heat transfer medium can the Schüttklale in the area of the double-walled predrying section 5 heat be fed so that the feedstock preheated or is pre-dried. Possibly. the wall cavity can be omitted and the heat directly, for example by heat conduction from the hotter zones of the reactor.
  • the Heat input is dimensioned so that adherence of certain Feedstock components on the wall largely excluded is.
  • pre-drying water constituents be discharged, so that these the other Do not add extra weight to the gasification process.
  • the pouring column 4 tempered at about 100 ° C. become.
  • the pre-tempering section may possibly be omitted altogether, if a predrying due to the composition of the Feedstock is not required, or the Vortemper istsabêt is used in special cases for cooling the Feedstocks used.
  • Gas supply 10 which in the example shown as an annular gas supply space 10 is configured, which is approximately in the plane of the cross-sectional widening in the pyrolysis section 8 is open.
  • the purpose of the gas supply space 10 is to introduce hot gases to the bulk cone 9.
  • the gas supply means may also serve as nozzles, wall openings or other devices designed to be the feed allow hot gases to the pouring column.
  • the burner 12 generates the required hot gas, which preferably tangentially over the combustion chambers and the Gaszu 1500raum is brought to the bulk cone 9.
  • modified Embodiments may include multiple combustors or several burners are used, if this is for one As uniform as possible heating of the bulk cone desirable is.
  • the combustion in the burner 12 is expediently carried out under oxygen deficiency, so that by a nearly stoichiometric Combustion of an inert combustion gas at temperatures of about 1000 ° C is provided. At least during start-up operation the burner will need foreign fuels that are not immediately be recovered from the reactor. For example, come Natural gas, oil obtained from a previous gasification process generated and cached excess gas, gas mixture, Liquid-gas mixture, dust-gas mixture or others under energetic aspects suitable media used. As soon as the reactor its operating condition described below has taken the burner 12 can also with an optionally operated previously purified excess gas.
  • the Supply of combustion gas which under suitable control is largely composed of carbon dioxide and water vapor, the in the bulk cone area existing feed shock-like heated.
  • the feed then continues to sink in the pyrolysis section 8 down, pyrolysis being continued, i.a. also at the materials kept in the center by heat transfer also heated.
  • the wall of the pyrolysis section is preferably thermally insulated and / or double-walled formed so that, if necessary, in the formed wall cavity also a heat transfer medium are performed can.
  • the heat insulation or the additional heat with Help of the heat transfer medium are dimensioned so that the starting materials in the lower part of the pyrolysis section 8 a temperature of preferably over 500 ° C. exhibit. The temperature desired at this point may be in Dependent on the specific feed materials targeted be managed.
  • a melting point closes. and overheating section 14. This has a cross-sectional narrowing due to which the sinking rate changed the feedstock.
  • a cross-sectional narrowing by at least 10% for example by conical indentations of the corresponding shaft part in an angle of about 60 ° to the horizontal is generated.
  • upper injection means 15 in the example shown formed by a plurality of circumferentially distributed oxygen lances 16 are. To prevent the oxygen lances 16 from overheating protect, for example, these are water cooled.
  • nozzles, burners or the like used as upper injection means over which controlled supplied various fuel gases or gas compositions with the aim of reducing the temperature in the melting and overheating zone to a desired value. If the supply of oxygen is not sufficient for this (If, for example, no starting materials with sufficiently high energy value at this position stand), can also external fuel gases or from the reactor obtained excess gases supplied via the injection means become.
  • using the top Eindüsungsmitell 15 the targeted and metered addition of Oxygen just below the plane of cross-sectional narrowing. This forms in the area of melting and Overheating section 14 of a hot zone 17, in which preferably temperatures of 1500 ° C to 2000 ° C, but which are to be matched to the respective feedstock.
  • the over the Gaszu 1500raum 10 supplied (inert) combustion gases and the pyrolysis gases formed in the pyrolysis section 8 are sucked through this hot zone 17.
  • the oxygen supply in the hot zone is controlled so that combustion takes place under oxygen deficiency, the finally to a further increase in temperature and to extensive coking of the residues of the feed to lead.
  • the temperature in the hot zone 17 is adjusted that slag-forming mineral constituents and metallic constituents melted in this zone being a certain proportion of in the feedstock contained pollutants (e.g., heavy metals) in these Melting is solved.
  • pollutants e.g., heavy metals
  • the reduction section 20 includes a Gasabsaugraum 21, sucks over which excess gases become. All extracted gases must therefore both the hot Zone 17 as well as one under this by the coked residues flow through trained reduction zone 22.
  • the gases using the existing there Reduced carbon. In particular, it comes to Conversion of carbon dioxide into carbon monoxide, taking in particular The carbon still contained in the bed is used up and thus continue to be gassed.
  • the gases are also cooled so that they with a technically controllable temperature, preferably about 800 ° C to 1000 ° C, can be aspirated.
  • the sucked off Excess gases will be following (not shown) Cooling and / or cleaning stages and a suitable Conveyor (compressor or blower) supplied. at the gasification of waste with predominantly organic components After that, for example, about 80% to 90% of the Excess gases as fuel gas for a material and / or energetic Usage available. It can be a partial flow of about 10% to 20% as own gas the o.g. Burner 12 and / or be fed to the Eindüsungsstoffn, wherein the Cooling / cleaning for this partial flow to a minimum can be limited.
  • the Gasabsaugraum 21 is in turn advantageous (but not mandatory) ring-shaped, a connected conveyor of the suction of the Gases serves.
  • the lower injection means may alternatively designed and operated as above for the top Injection means 15 has been explained.
  • About the injection of a suitable amount of oxygen, gas, fuel gas o.ö. becomes one Temperature set for the melts that sufficient is high to keep the melts fluid and after corresponding collection via a tap 27 from the reactor to be able to leave. For example, temperatures of about 1500 ° C appropriate.
  • the division of the total amount of supplied oxygen / fuel gas to the combustion chamber 11, the upper injection means 15 and the lower injection means 26 is dependent on the feed used and to optimize from the other process parameters, with the The aim of the extensive utilization of the feedstock and the Minimization of pollutant content in the residues.
  • liquids are also to be reacted in the reactor, These can be advantageous via a remplisstechniksseindüsung 30th be fed, which opens into the gas supply chamber 10 or with other gas supply means is combined.
  • About the liquid injection 30 may be water, water vapor or others Disposal certain liquids are introduced, wherein in addition to the desired disposal, a regulation of Temperature of the inert combustion gases, the pyrolysis process and / or the composition and temperature of the excess gases becomes possible.
  • the dust feed 31 is preferably a center in the Feeding section 1 and guided in the pre-tempering section 5 Metering tube, which ends in the vicinity of the bulk cone 9.
  • the dusts are therefore immediately in the vicinity of the shock-like Heat the feedstock transported so that they Exiting the metering tube immediately a high temperature effect are exposed to a burning or gasification causes, without causing deflagration or the like.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Furnace Details (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Catalysts (AREA)

Claims (16)

  1. Réacteur de gazéification et/ou de fusion de matières de charge, comprenant :
    une section d'apport (1) présentant une ouverture d'apport (2) par laquelle les matières de charge sont introduites par le haut dans le réacteur ;
    une section de pyrolyse (8) qui fait suite à la section (1, 5) située en amont et qui présente un élargissement de section transversale de telle manière qu'un cône de remplissage (9) de matière de charge puisse s'y former ;
    des moyens d'apport de gaz (10) qui débouchent dans la section de pyrolyse (8) à peu près au niveau de l'élargissement de section transversale et permettent d'apporter des gaz chauds au cône de remplissage (9) ;
    une section de fusion et de surchauffe (14) qui fait suite à la section de pyrolyse (8) et qui présente un rétrécissement de section transversale ;
    des moyens supérieurs d'injection (15) qui permettent d'introduire dans la section de fusion et de surchauffe (14) un fluide énergétique directement au-dessous du niveau du rétrécissement de la section transversale ;
    une section de réduction (20) qui fait suite à la section de fusion et de surchauffe (14) et qui comprend des moyens d'aspiration des gaz (21) permettant d'aspirer les excédents de gaz ;
    une sole (25) comportant un dispositif de déchargement (27) en dessous de la section de réduction (20) qui permet de récolter et d'évacuer le métal en fusion et le laitier en fusion ;
    des moyens inférieurs d'injection (26) permettant d'apporter un fluide énergétique directement au-dessus des fusions et au-dessous des moyens d'aspiration des gaz (21) afin d'empêcher toute solidification des fusions.
  2. Réacteur selon la revendication 1,
    caractérisé en ce qu'
    une section de pré-conditionnement thermique (5) est disposée entre la section d'apport (1) et la section de pyrolyse (8).
  3. Réacteur selon la revendication 2,
    caractérisé en ce que
    la section de pyrolyse (8) et la section de pré-conditionnement thermique (5) sont conçues, au moins par sections avec une double paroi qui crée une cavité (6) dans laquelle circule un fluide caloporteur.
  4. Réacteur selon l'une des revendications 1 à 3,
    caractérisé en ce que
    les moyens d'apport de gaz sont conçus sous forme de chambre d'apport de gaz (10) dans laquelle débouche au moins une chambre à combustion (11) équipée d'au moins un brûleur (12) procurant des gaz chauds, d'une température d'environ 1 000 °C, au cône de remplissage (9) par l'intermédiaire de la chambre de combustion et de la chambre d'expansion, les moyens d'apport de gaz (10) et les moyens d'aspiration de gaz (21) étant de conception circulaire sur la circonférence du réacteur.
  5. Réacteur selon l'une des revendications 1 à 4,
    caractérisé en ce que
    la section d'apport (1), ou la section de pré-conditionnement thermique (5), la section de pyrolyse (8) et la section de réduction (20) sont de conception cylindrique ou légèrement évasée vers le bas, la longueur totale de la section d'apport (1) et de la section de pré-conditionnement thermique (5) est au moins trois fois plus importante que le diamètre de la section d'apport à l'extrémité supérieure, et la section transversale de la section de pyrolyse (8) est au moins deux fois plus importante que la section transversale de l'extrémité inférieure de la section de pré-séchage.
  6. Réacteur selon l'une des revendications 1 à 5,
    caractérisé en ce que
    les moyens supérieurs et/ou inférieurs d'injection (15, 26) comportent plusieurs lances à oxygène (16) ou buses, disposées de manière circulaire sur la circonférence du réacteur, servant à apporter de l'oxygène ou un mélange de gaz combustibles.
  7. Réacteur selon l'une des revendications 1 à 6,
    caractérisé en ce que
    les moyens d'apport de gaz (10) sont reliés à une alimentation de liquide (30) servant à l'apport de liquides ou de vapeurs.
  8. Réacteur selon l'une des revendications 1 à 7,
    caractérisé en ce qu'
    en outre un dispositif d'apport de substances pulvérulentes (31) est prévu pour l'apport direct de substances pulvérulentes au niveau de l'élargissement de la section transversale entre la section d'apport (5) et la section de pyrolyse (8).
  9. Réacteur selon l'une des revendications 1 à 8,
    caractérisé en ce que
    la section d'apport (1) est obturée vers le haut de manière essentiellement étanche aux gaz, l'apport en matières de charge se faisant par l'intermédiaire d'un sas de chargement.
  10. Procédé de gazéification et/ou de fusion de matières de charge, comprenant les étapes consistant à :
    former dans un réacteur en forme de puits une charge (4) essentiellement protégée des conditions ambiantes ;
    chauffer soudainement la charge (4) en apportant des gaz chauds dans la partie supérieure afin de déclencher une pyrolyse des matières de charge ;
    produire une zone chaude plus basse (17) présentant des températures supérieures à 1 000 °C par apport de fluides énergétiques ;
    brûler les produits de pyrolyse, faire fondre les composants métalliques et minéraux éventuellement contenus et cokéfier essentiellement le reste des matières de charge dans la zone chaude (17) ;
    faire descendre tous les gaz par aspiration dans la charge (4), dans la zone chaude (17) et dans une zone de réduction plus basse (22) ;
    évacuer les excédents de gaz réduits hors du réacteur au niveau de la zone de réduction (22) ;
    récolter dans la section la plus basse du réacteur le métal en fusion et/ou le laitier en fusion éventuellement présents ;
    introduire des fluides énergétiques directement au-dessus des fusions récoltées afin de les maintenir à l'état liquide ;
    couler les fusions si nécessaire.
  11. Procédé selon la revendication 10,
    caractérisé en ce que
    comme fluides énergétiques, on introduit de l'oxygène, des gaz combustibles, des portions de l'excédent de gaz aspiré, des combustibles liquides ou pulvérulents.
  12. Procédé selon la revendication 10 ou 11,
    caractérisé par
    en outre les étapes consistant à :
    surveiller le niveau de remplissage du réacteur afin que la hauteur de la charge soit en permanence comprise entre une valeur minimale et une valeur maximale ;
    régler la valeur minimale de manière à ce que, au-dessus du point de chauffage soudain, la charge soit protégée des conditions ambiantes par une matière de charge relativement condensée.
  13. Procédé selon l'une des revendications 10 à 12,
    caractérisé par
    en outre les étapes consistant à :
    pré-sécher les matières de charge en chauffant la charge au-dessus du point de chauffage soudain à environ 100 °C ;
    réguler la dépression pour l'aspiration des gaz de manière à ce que pratiquement aucun gaz ne s'échappe du réacteur vers le haut et que seules des quantités minimales d'air ambiant supplémentaire soient aspirées par le haut à travers la charge.
  14. Procédé selon l'une des revendications 10 à 13,
    caractérisé par
    en outre les étapes consistant à :
    produire les gaz chauds servant au chauffage soudain de la charge par combustion de combustibles extérieurs dans la phase initiale du procédé ;
    produire les gaz chauds servant au chauffage soudain de la charge par combustion des excédents de gaz, au moins partiellement réduits, purifiés, qui sont évacués du réacteur, éventuellement combinés avec les combustibles extérieurs ;
    effectuer la combustion sous manque d'oxygène de manière à produire un gaz de combustion inerte composé en grande partie de dioxyde de carbone et de vapeur d'eau.
  15. Procédé selon l'une des revendications 10 à 14,
    caractérisé par
    en outre les étapes consistant à :
    apporter à une installation aval de traitement de gaz les excédents de gaz évacués pour leur refroidissement et/ou purification ;
    apporter des substances pulvérulentes à exploiter à proximité immédiate du chauffage soudain de la charge.
  16. Procédé selon l'une des revendications 10 à 15,
    caractérisé en ce qu'
    on emploie un réacteur selon l'une des revendications 1 à 9.
EP01911636A 2000-02-17 2001-02-13 Reacteur et procede de gazeification et/ou de fusion de matieres Expired - Lifetime EP1261827B8 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE10007115 2000-02-17
DE10007115A DE10007115C2 (de) 2000-02-17 2000-02-17 Verfahren und Reaktor zum Vergasen und Schmelzen von Einsatzstoffen mit absteigender Gasführung
PCT/EP2001/001581 WO2001061246A1 (fr) 2000-02-17 2001-02-13 Reacteur et procede de gazeification et/ou de fusion de matieres

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EP1261827A1 EP1261827A1 (fr) 2002-12-04
EP1261827B1 true EP1261827B1 (fr) 2005-11-16
EP1261827B8 EP1261827B8 (fr) 2006-01-25

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DE (2) DE10007115C2 (fr)
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EP3660132A1 (fr) 2018-11-28 2020-06-03 Waste & Energy Solutions GmbH Réacteur et procédé de gazéification et/ou de fusion de matériaux d'alimentation
WO2020110061A1 (fr) 2018-11-28 2020-06-04 African Rainbow Minerals Limited Réacteur et procédé de gazéification et/ou de fusion de matériaux de charge
WO2020109425A1 (fr) 2018-11-28 2020-06-04 Kbi Invest & Management Ag Réacteur et procédé de gazéification et/ou de fusion de matériaux de charge
EP4026885A1 (fr) 2021-01-06 2022-07-13 KBI Invest & Management AG Réacteur et procédé de gazéification et/ou de fusion de matières d'alimentation et de production d'hydrogène

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Publication number Priority date Publication date Assignee Title
EP3660132A1 (fr) 2018-11-28 2020-06-03 Waste & Energy Solutions GmbH Réacteur et procédé de gazéification et/ou de fusion de matériaux d'alimentation
WO2020110061A1 (fr) 2018-11-28 2020-06-04 African Rainbow Minerals Limited Réacteur et procédé de gazéification et/ou de fusion de matériaux de charge
WO2020109425A1 (fr) 2018-11-28 2020-06-04 Kbi Invest & Management Ag Réacteur et procédé de gazéification et/ou de fusion de matériaux de charge
EP4026885A1 (fr) 2021-01-06 2022-07-13 KBI Invest & Management AG Réacteur et procédé de gazéification et/ou de fusion de matières d'alimentation et de production d'hydrogène

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KR100770889B1 (ko) 2007-10-26
BR0108578A (pt) 2003-04-29
CY1105497T1 (el) 2010-04-28
EA004195B1 (ru) 2004-02-26
JP4426150B2 (ja) 2010-03-03
ZA200206571B (en) 2003-06-12
EP1261827A1 (fr) 2002-12-04
HUP0300690A2 (en) 2003-07-28
WO2001061246A1 (fr) 2001-08-23
SK12912002A3 (sk) 2005-06-02
JP2003527554A (ja) 2003-09-16
AU4061501A (en) 2001-08-27
CN1404566A (zh) 2003-03-19
CZ305021B6 (cs) 2015-04-01
WO2001061246A8 (fr) 2001-11-15
PL357563A1 (en) 2004-07-26
KR20020093806A (ko) 2002-12-16
EP1261827B8 (fr) 2006-01-25
DE10007115A1 (de) 2001-09-06
DK1261827T3 (da) 2006-07-03
CA2400234A1 (fr) 2001-08-23
US6662735B2 (en) 2003-12-16
BR0108578B1 (pt) 2009-12-01
ES2253356T3 (es) 2006-06-01
US20030010267A1 (en) 2003-01-16
EA200200854A1 (ru) 2002-12-26
HU228016B1 (en) 2012-08-28
DE50108084D1 (de) 2005-12-22
SK288020B6 (sk) 2012-11-05
ATE310208T1 (de) 2005-12-15
CZ20022908A3 (cs) 2003-01-15
MXPA02007967A (es) 2004-04-05
DE10007115C2 (de) 2002-06-27
CN1212487C (zh) 2005-07-27
PL193225B1 (pl) 2007-01-31

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