EP1261827A1 - Reacteur et procede de gazeification et/ou de fusion de matieres - Google Patents

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

Info

Publication number
EP1261827A1
EP1261827A1 EP01911636A EP01911636A EP1261827A1 EP 1261827 A1 EP1261827 A1 EP 1261827A1 EP 01911636 A EP01911636 A EP 01911636A EP 01911636 A EP01911636 A EP 01911636A EP 1261827 A1 EP1261827 A1 EP 1261827A1
Authority
EP
European Patent Office
Prior art keywords
section
reactor
gas
feed
gases
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.)
Granted
Application number
EP01911636A
Other languages
German (de)
English (en)
Other versions
EP1261827B8 (fr
EP1261827B1 (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
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
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Application filed by Masch und Stahlbau GmbH, Maschinen- und Stahlbau GmbH filed Critical Masch und Stahlbau GmbH
Publication of EP1261827A1 publication Critical patent/EP1261827A1/fr
Application granted granted Critical
Publication of EP1261827B1 publication Critical patent/EP1261827B1/fr
Publication of EP1261827B8 publication Critical patent/EP1261827B8/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

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
    • 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
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—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 method for gasifying and / or melting substances.
  • the invention relates to the material and / or energy recovery of any waste, e.g. with predominantly organic components but also special waste.
  • the reactor according to the invention and the method are also suitable for gasifying and melting feedstocks of any composition or for energy generation through the use of organic substances.
  • a special task is to enable simple, inexpensive and environmentally friendly material and / or energy recovery of waste.
  • the aim is to increase the functional reliability of a corresponding reactor by largely avoiding the operational uncertainties associated with the recycle gas flow.
  • Another object of the invention is to significantly reduce the pollution in the excess gas to be extracted, so that the effort in a subsequent gas cleaning can be minimized.
  • the double injection of oxygen or fuel gas (gas mixtures) enables combustion on the one hand of the pyrolysis gases and, on the other hand, allows a sufficiently high temperature to be maintained in the lower reactor section so that the melts which collect there are kept liquid.
  • a reduction section is formed between the two injection means, through which all gases have to flow before suction and in which they are consequently largely reduced.
  • a preheating section is added to the feed section, in which the waste is pre-dried, for example, at temperatures around 100.degree.
  • the feedstocks can also be cooled in this section under certain circumstances if this is useful for the overall process.
  • An advantageous embodiment of the reactor is characterized in that the total length of the feed section and pre-tempering section is several times greater than the diameter of the feed section.
  • the pouring column in the feed and pre-tempering section acts as a plug which closes at the top and prevents large amounts of ambient air from being drawn into the reactor.
  • the reactor can be closed at its upper end by a lock, a double flap system or a similar device. This prevents the uncontrolled entry of ambient air and the escape of gases from the bed even better.
  • the reactor is expediently essentially cylindrical and the gas supply space and the gas extraction space are - D ⁇
  • This embodiment is particularly suitable for recycling predominantly organic feedstocks.
  • Other embodiments e.g. are more expedient for other feedstocks, can have non-cylindrical basic shapes and differently positioned and shaped means for gas extraction and supply.
  • the pyrolysis section of the reactor is also double-walled and a heat transfer medium is guided in the wall cavity.
  • the wall can be cooled thereby, which reduces the material stress, on the other hand, depending on the feedstock used and the resulting heat requirement, additional heat can be supplied to or derived from the bulkhead as required.
  • the process steps essential to the invention can advantageously be further developed by pre-drying the feed material by heating the pouring column above the level in which the shock-like heating takes place to about 100 ° C.
  • water components of the feedstock are largely evaporated, which also improves the desired automatic downward movement of the feedstock.
  • the negative pressure for extracting the excess gases can be regulated, the extraction being carried out in such a way that on the one hand no gas escapes from the top of the reactor and on the other hand only minimal amounts of additional ambient air are sucked in through the bulk column.
  • the aim of minimizing the amount of false air present in the reactor is to reduce the proportion of nitrogen oxides in the excess gas and also to keep the total amount of gas small in order to make the subsequent gas economy simple.
  • the single figure shows a simplified sectional view of a reactor according to the invention.
  • a preferred embodiment of a reactor is described below with reference to FIG. 1.
  • the process steps that occur in the treatment of waste with organic constituents as starting materials in this reactor are also given.
  • the implementation of the method according to the invention is not necessarily linked to the reactor explained, but can also be carried out using modified systems, if necessary.
  • Input materials may be useful modifications of the reactor and / or the process (eg flexible arrangement and design of the technical design of the gas supply and discharge, the heating or cooling of the reactor jacket or the like).
  • different feedstocks can also be combined, for example by adding feedstocks with a higher energy value (e.g. organic waste, contaminated waste wood or the like) when gasifying / melting non-organic feedstocks.
  • the reactor shown in the figure has at its upper end a feed section 1 with at least one feed opening 2, through which the feedstock to be used in terms of material and / or energy is fed.
  • the proportion of organic constituents predominates with this feed material, so that the reactor and the process described are particularly suitable for the treatment of normal household garbage and commercial garbage.
  • combustible constituents of certain feedstock compositions are not high enough to carry out the combustion and gasification processes, combustible additives or energy sources can be added to the feedstock. It is possible to add a certain amount of coke in a conventional manner or to increase the total calorific value by adding wood. Under certain circumstances, it can also be useful to add other additives, for example to influence the pH that is set. Such measures are known to the person skilled in the art 3, however, so that a detailed description is not given here.
  • the feedstock and possibly the aggregates are fed into the feed opening 2 via a suitable delivery device 3 Reactor introduced.
  • a pillar 4 is thus formed.
  • the height of the pouring column 4 is monitored using fill level measuring devices which are not specifically designated. This bed height is to be kept between a minimum and a maximum level. The minimum level is chosen so that the pouring column 4 acts in the upper section of the reactor as a barrier layer, which prevents larger amounts of ambient air from entering the reactor.
  • the pre-tempering section 5 serves to pre-dry the starting materials.
  • the feed section and the pre-tempering section are advantageously cylindrical or conical with a slight increase in cross-section 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 the help of the heat transfer medium, heat can be supplied to the bulkhead in the region of the double-walled predrying section 5, so that the feed material is preheated or predried. Possibly. the wall cavity can be omitted and the heat can be supplied directly from the hotter zones of the reactor, for example by conduction.
  • the heat supply is dimensioned in such a way that the adherence of certain ingredients to the wall is largely excluded.
  • water components can be removed by the pre-drying, so that they do not additionally burden the further gasification process.
  • the pouring column 4 can be tempered to approximately 100 ° C.
  • the pre-tempering section may be omitted entirely if predrying is due to the composition of the Feed material is not required, or the pre-tempering section is used in special cases to cool the feed materials.
  • a pyrolysis section 8 adjoins below the pre-tempering section 5, the cross-section widening abruptly at the transition between the pre-tempering section (or the feed section if the pre-tempering section is omitted) and the pyrolysis section.
  • the free shaft cross section in this transition region is preferably increased by at least twice, which on the one hand reduces the sinking speed of the feed materials and on the other hand forms a pouring cone 9.
  • the pouring cone 9 is fed centrally from the pouring column 4 in the predrying section. At the edge areas the cone flattens out, so that a free space is created there.
  • gas supply means 10 which in the example shown is designed as an annular gas supply space 10 which is opened approximately in the plane of the cross-sectional expansion in the pyrolysis section 8.
  • the purpose of the gas supply space 10 is to bring hot gases to the pouring cone 9.
  • the gas supply means can also be designed as nozzles, wall openings or other devices which enable the supply of hot gases to the pouring column.
  • the burner 12 generates the required hot gas, which is preferably brought tangentially to the debris cone 9 via the combustion chambers and the gas supply space ,
  • multiple combustion chambers or multiple burners can be used if this is for one heating the cone as evenly as possible is desirable.
  • the combustion in burner 12 is expediently carried out with a lack of oxygen, so that an inert combustion gas with temperatures of approximately 1000 ° C. is provided by an almost stoichiometric combustion.
  • the burner will need foreign fuels that are not obtained directly from the reactor.
  • natural gas, oil, the excess gas generated and temporarily stored by a previous gasification process, gas mixture, liquid-gas mixture, dust-gas mixture or other media that are suitable from an energy point of view are used.
  • the burner 12 can also be operated with a possibly previously cleaned excess gas.
  • the feed material present in the cone area is heated in a shock-like manner.
  • the very rapid heating of the material to temperatures between 800 ° C and 1000 ° C causes this material to dry very quickly, avoiding sticking and sticking to the wall. Rather, there is at least some conglomeration of the starting materials.
  • the expulsion of pyrolysis products is already started in this upper section of the reactor. Since the gas supplied is largely inert, these pyrolysis products are only incinerated to a small extent, insofar as air can be sucked in through the pouring column 4 piled above the pouring cone or carried along by the feed material.
  • the feed material then drops further down in the pyrolysis section 8, the pyrolysis being continued, among other things. also with the materials in the center, which are also heated by heat transfer.
  • the wall of the pyrolysis section is preferably heat-insulated and / or double-walled, so that, if necessary, a heat transfer medium can also be guided in the wall cavity formed.
  • the heat insulation or the additional supply of heat with the aid of the heat transfer medium are dimensioned such that the starting materials have a temperature of preferably above 500 ° C. in the lower region of the pyrolysis section 8. The temperature required at this point can be specifically controlled depending on the special feed materials.
  • a melting and superheating section 14 follows below the pyrolysis section 8. This has a cross-sectional constriction on the basis of which the sinking rate of the feed material changes. In the example of the treatment of predominantly organic waste, the cross-section is narrowed by at least 10%, which is generated, for example, by conically drawing in the corresponding shaft part at an angle of approximately 60 ° to the horizontal.
  • upper injection means 15 which in the example shown are formed by a plurality of oxygen lances 16 distributed around the circumference. In order to protect the oxygen lances 16 from overheating, they are water-cooled, for example.
  • nozzles, burners or the like are used as the upper injection means, via which various fuel gases or gas compositions can be supplied in a controlled manner, with the aim of setting the temperature in the melting and superheating zone to a desired value. If the supply of oxygen is not sufficient for this (if, for example, no feedstocks with a sufficiently high energy value are available at this position for a short time), foreign combustion gases or excess gases obtained from the reactor can also be supplied via the injection means. In the specific example, with the aid of the upper injection means 15, the targeted and metered addition of oxygen takes place immediately below the level of the cross-sectional constriction. As a result, a hot zone 17 is formed in the region of the melting and superheating section 14, in which temperatures of from 1500 ° C. to 2000 ° C. preferably prevail, but which must be adapted to the respective feed material.
  • the (inert) combustion gases supplied via the gas supply space 10 and the pyrolysis gases formed in the pyrolysis section 8 are sucked through this hot zone 17.
  • the supply of oxygen in the hot zone is controlled in such a way that combustion takes place in the absence of oxygen, which ultimately leads to a further increase in temperature and to the extensive coking of the residues of the feedstock.
  • the temperature m of the hot zone 17 is set so that slag-forming mineral constituents and metallic constituents are melted in this zone, a certain proportion of pollutants contained in the insert material (eg heavy metals) being dissolved in these melts.
  • the molten metal and the slag melt then drip down.
  • the largely coked residues also continue to decline.
  • a reduction section 20 is then formed below the melting and superheating section 14, in which the coked residues sink further down with a sufficient dwell time.
  • the reduction section 20 comprises a gas extraction space 21, via which excess gases are extracted. All extracted gases must therefore flow through both the hot zone 17 and a reduction zone 22 formed below it by the coked residues.
  • the gases are reduced with the help of the carbon present there. In particular, there is a conversion of carbon dioxide into carbon monoxide, the carbon still contained in the bed being used up in particular and thus being further gasified.
  • the gases are also cooled so that they can be extracted at a technically manageable temperature, preferably about 800 ° C. to 1000 ° C.
  • the extracted excess gases are fed to subsequent (not shown) cooling and / or cleaning stages and a suitable conveying device (compressor or blower).
  • a suitable conveying device compressor or blower.
  • a partial flow of approximately 10% to 20% can be supplied as the own gas to the above-mentioned burner 12 and / or the injection means, the cooling / cleaning for this partial flow being able to be kept to a minimum.
  • the gas extraction chamber 21 is in turn advantageously (but not necessarily) designed in a ring shape, with a connected conveyor device serving to extract the gases.
  • a fireproof-lined stove 25 connects below the gas extraction chamber 21. The metal melts and the slag melts are collected in the hearth 25.
  • lower injection means 26 are provided immediately above the melts and below the gas extraction chamber 21, which in turn have a plurality of oxygen lances 16 (possibly water-cooled) in the example shown.
  • the lower injection means can alternatively be designed and operated, as was explained above for the upper injection means 15.
  • a temperature for the melts is set which is sufficiently high to keep the melts liquid and, after appropriate collection, to be able to discharge them from the reactor via a tap 27. For example, temperatures of about 1500 ° C are appropriate.
  • the distribution of the total amount of oxygen / fuel gas supplied to the combustion chamber 11, the upper injection means 15 and the lower injection means 26 is to be optimized depending on the feed used and on the other process parameters, with the aim of largely utilizing the feed and minimizing the amount of pollutants in the residues.
  • an oxygen-air mixture or an oxygen-fuel gas mixture can be supplied instead of oxygen, for example for reasons of cost reduction.
  • temperature values given by way of example have to be adapted depending on the feed materials to be processed and the desired process speed.
  • the feedstocks may need to be mechanically comminuted before being introduced into the reactor to prevent clogging avoid.
  • certain additives may be required to stabilize the calorific value and to increase the yield of excess gas as well as to improve slag formation, basicity and the slag flow.
  • liquids are also to be converted in the reactor, these can advantageously be supplied via a liquid injection 30 which opens into the gas supply space 10 or is combined with other gas supply means.
  • Water, water vapor or other liquids intended for disposal can be introduced via the liquid injection 30, whereby in addition to the desired disposal, it is also possible to regulate the temperature of the inert combustion gases, the pyrolysis process and / or the composition and the temperature of the excess gases.
  • the dust feed 31 is preferably a metering tube which is guided centrally in the feed section 1 and in the preheating section 5 and which ends in the vicinity of the cone 9. The dusts are therefore transported directly in the vicinity of the shock-like heating of the feed materials, so that when they emerge from the metering tube they are immediately exposed to a high temperature effect, which causes combustion or gasification, without causing deflagrations or the like.

Landscapes

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

Abstract

L'invention concerne un réacteur de gazéification et/ou de fusion de matières comprenant: une section d'alimentation (1) permettant l'introduction des matières; une section pyrolyse (8) qui prolonge la section précédente avec une section transversale élargie; des moyens d'alimentation en gaz (10) qui débouchent dans la section pyrolyse (8) approximativement au niveau du plan d'élargissement de la section transversale et qui permettent l'alimentation en gaz chauds d'un cône de versement (9); une section de fusion et de surchauffe (14) qui prolonge la section pyrolyse (8); des moyens de pulvérisation supérieurs (15) qui introduisent un agent à haute énergie dans la section de fusion et de surchauffe (14); une section de réduction (20) qui abrite des moyens d'aspiration de gaz (21) destinés à l'aspiration des surplus de gaz; un foyer (25) placé sous la section de réduction (20) et destiné à collecter et à dériver les métaux en fusion et le laitier en fusion; et des moyens de pulvérisation inférieurs (26) qui permettent l'alimentation d'un agent à haute énergie juste au-dessus des masses en fusion et sous les moyens d'aspiration de gaz (21).
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
DE10007115A DE10007115C2 (de) 2000-02-17 2000-02-17 Verfahren und Reaktor zum Vergasen und Schmelzen von Einsatzstoffen mit absteigender Gasführung
DE10007115 2000-02-17
PCT/EP2001/001581 WO2001061246A1 (fr) 2000-02-17 2001-02-13 Reacteur et procede de gazeification et/ou de fusion de matieres

Publications (3)

Publication Number Publication Date
EP1261827A1 true EP1261827A1 (fr) 2002-12-04
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CA2400234A1 (fr) 2001-08-23
KR20020093806A (ko) 2002-12-16
JP4426150B2 (ja) 2010-03-03
ATE310208T1 (de) 2005-12-15
MXPA02007967A (es) 2004-04-05
JP2003527554A (ja) 2003-09-16
CZ20022908A3 (cs) 2003-01-15
AU4061501A (en) 2001-08-27
EA200200854A1 (ru) 2002-12-26
CN1212487C (zh) 2005-07-27
HUP0300690A2 (en) 2003-07-28
PL193225B1 (pl) 2007-01-31
SK12912002A3 (sk) 2005-06-02
PL357563A1 (en) 2004-07-26
CN1404566A (zh) 2003-03-19
EA004195B1 (ru) 2004-02-26
HU228016B1 (en) 2012-08-28
SK288020B6 (sk) 2012-11-05
DK1261827T3 (da) 2006-07-03
ZA200206571B (en) 2003-06-12
DE10007115A1 (de) 2001-09-06
EP1261827B8 (fr) 2006-01-25
ES2253356T3 (es) 2006-06-01
EP1261827B1 (fr) 2005-11-16
CZ305021B6 (cs) 2015-04-01
CA2400234C (fr) 2010-01-12
WO2001061246A1 (fr) 2001-08-23
CY1105497T1 (el) 2010-04-28
DE50108084D1 (de) 2005-12-22
KR100770889B1 (ko) 2007-10-26
WO2001061246A8 (fr) 2001-11-15
US20030010267A1 (en) 2003-01-16
BR0108578A (pt) 2003-04-29
DE10007115C2 (de) 2002-06-27
US6662735B2 (en) 2003-12-16
BR0108578B1 (pt) 2009-12-01

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