EP0747462B1 - Réacteur à lits fluidisés pour le traitement thermique des déchets - Google Patents

Réacteur à lits fluidisés pour le traitement thermique des déchets Download PDF

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Publication number
EP0747462B1
EP0747462B1 EP96401196A EP96401196A EP0747462B1 EP 0747462 B1 EP0747462 B1 EP 0747462B1 EP 96401196 A EP96401196 A EP 96401196A EP 96401196 A EP96401196 A EP 96401196A EP 0747462 B1 EP0747462 B1 EP 0747462B1
Authority
EP
European Patent Office
Prior art keywords
reactor
fluidised bed
waste
reactor according
dense
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
EP96401196A
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German (de)
English (en)
French (fr)
Other versions
EP0747462A1 (fr
Inventor
Jean-Xavier Morin
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.)
Alstom Power Boiler SA
Original Assignee
Alstom Energy Systems SA
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Filing date
Publication date
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Publication of EP0747462A1 publication Critical patent/EP0747462A1/fr
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Anticipated expiration legal-status Critical
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
    • F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed
    • F22B31/0084—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed with recirculation of separated solids or with cooling of the bed particles outside the combustion bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/08—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form
    • C10B49/10—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated in dispersed form according to the "fluidised bed" technique
    • 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
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/80—Shredding
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/501—Fluidised bed furnace with external recirculation of entrained bed material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/50—Fluidised bed furnace
    • F23G2203/503—Fluidised bed furnace with two or more fluidised beds
    • 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
    • F23G2205/12—Waste feed arrangements using conveyors
    • F23G2205/121—Screw conveyor
    • 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
    • F23G2206/00—Waste heat recuperation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/10—Liquid waste
    • F23G2209/102—Waste oil
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/12—Sludge, slurries or mixtures of liquids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/26—Biowaste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/00001—Exhaust gas recirculation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/70—Incinerating particular products or waste
    • F23G2900/7006—Incinerating used automobiles

Definitions

  • the present invention relates to the treatment thermal waste.
  • heat treatment is meant not only the destruction of waste, but also their recovery by recovering most of it of their heat energy.
  • An object of the present invention is to define a reactor capable of receiving all types of waste, including settling sludge, without the need for prior sorting and contenting itself with a summary fragmentation.
  • Another object of the present invention is to define a reactor in which the heat exchange zone, by example with the tubes of the superheaters of a energy recovery, free of chlorine.
  • the subject of the invention is a fluidized bed reactor for heat treatment of waste and exchange between the solids in circulation and an organ heat exchange, such as an evaporator and / or a superheater, the reactor being of the type comprising a bed fluidized circulating axial and at least a first and a second dense lateral fluidized beds established respectively on along first and second walls of the envelope reactor, characterized in that the supply of waste is carried out at at least one point on said first wall, above said first dense lateral fluidized bed, said reactor further comprising at least one conduit extraction of heavy non-fluidizable elements, located the base of said first fluidization bed.
  • the heat exchange is preferably carried out in said second dense lateral fluidized bed.
  • the heavy elements extraction duct includes an inclined part arranged in the extension of a sole inclined of said first dense lateral fluidized bed, nozzles supply air, directing a directional flow, flush on the surface of said sole.
  • Said extraction duct is provided with means adjustable air injection to regulate the flow of solids passing through said conduit.
  • the base of the second dense fluidized bed is connected by at least one extraction duct at the base of said fluidized bed circulating.
  • Said extraction duct is provided with means adjustable air injection to regulate the flow of solids passing through said conduit.
  • the circulating fluidized bed and the first fluidized bed dense lateral are fluidized by a mixture of primary air and recycled smoke.
  • the second dense lateral fluidized bed is fluidized by a mixture of air and dechlorinated recycled fumes.
  • Air called tertiary air
  • injectors with adjustable flow at an altitude higher than that of the waste introduction points, through each of the reactor walls.
  • the tertiary air is mixed with recycled fumes and dechlorinated at least for the tertiary air injected into the wall where the dense fluidized exchange bed is located thermal.
  • the base of the reactor includes extraction means inert materials.
  • Said non-heavy element extraction duct fluidizable is associated with a sorting device and extraction of said inert elements.
  • the reactor has a third fluidized bed lateral, the heat exchange being carried out with at least one of said second and third lateral fluidized beds.
  • Reactor includes third and fourth beds lateral fluidized, heat exchange being carried out with at least one of said second, third and fourth beds lateral fluidized.
  • the reactor includes means for feeding the bed fluidized waste supply with some of the materials from at least one heat exchange bed.
  • the reactor is connected to a hot cyclone, the wall where is carried out the connection of the reactor to the cyclone being opposite the wall where the waste is fed.
  • the reactor walls have exchange tubes thermal.
  • the reactor has an annexed fluidized bed, containing a heat exchange member, supplied by part of the solids of the second dense fluidized bed, provided with means fluidization, at least one return line for solids down the circulating fluidized bed, and a vent directing the gases up the circulating fluidized bed.
  • the reactor is supplied with waste made up of a mixture of urban residues and / or waste chosen in particular from settling sludge, biomass residues, industrial waste and refuse grinding, and / or fossil fuels chosen in particular among coal and petroleum residues.
  • Fig. 1 represents schematically and in a way simplified part of the thermal installations of a waste treatment unit according to the invention.
  • the turbine steam and the electric generator are not represented.
  • FIG. 1 a 1-bed reactor fluidized, subject of this patent application, powered in products to be treated.
  • This reactor is connected by its part higher than the upper part of a hot cyclone 2 in which performs the separation between gases and essentials of the solid materials with which they are charged, the latter returning to the reactor.
  • the gases leaving the heat exchange unit 3 are sent to a gas-solid separator 4 where the gases are separated from the coarse fraction C of the fly ash which are collected at the base of cyclone 4.
  • the gases, thus separated from said fraction, are sent to a TF smoke treatment device from where they are extracted by a VT draft fan and sent to the base of a CH chimney.
  • Reactor 1 which is the subject of this invention, is shown in more detail in Fig. 2 and 3.
  • the example described, without limitation, is that of a reactor with two dense lateral fluidized beds.
  • the reactor includes a casing 10, which can have a rectangular section and thus present four walls 11, 12, 13 and 14.
  • the lower part 16 of the reactor is in the form of inverted pyramid trunk, or in the form of a pseudo-pyramid inverted with two parallel faces, or in the shape of a trunk cone; it is in this part that is installed a bed of axial circulating fluidization comprising a part lower 18 surmounted by an upper part 18 ', as it was explained in the second of the above documents and to which the reader is referred.
  • the lower part 18 of the bed circulating fluidized is supplied with pyrolyzed fuel notably due to the overflow of the dense lateral bed 28, as will be seen later.
  • a grid 19, at the base of part 18 of the bed, is equipped with nozzles 20 allowing to inject air, called primary air, identified in the drawing by the arrow AP, which can possibly be mixed with fumes taken at the inlet El of the TF smoke treatment.
  • Above grid 19 are arranged arrivals secondary air AS which can also be optionally mixed with fumes taken at input E1 of the treatment TF smoke.
  • Reactor preheating means not represented, located above the grid 19, allow to reheat the entire reactor from a cold state or lukewarm, and bring it to the temperature required for ensure the combustion of waste.
  • an extraction device 22 residues such as a cooled screw extractor or dry extractor.
  • the reactor comprises two dense lateral fluidized beds 28 and 48.
  • the lateral fluidized bed 28, installed against the wall 11, comprises a sole 29, preferably inclined and in which are placed blowing nozzles 30 directional, that is to say the direction of the flow of blowing can be oriented between a direction perpendicular to the plane of the sole and a direction parallel to this plane. Nozzles are supplied with air (reference AF), possibly mixed with fumes recycled from point E1.
  • the dense fluidized bed 28 is partially contained by an overflow wall 31 raised at the end of the floor 29 parallel to the wall 11.
  • the dense fluidized bed 28 is supplied with waste to be treated which, according to a fundamental characteristic of the invention, are injected into the dense fluidized bed in several points of the wall 11, preferably at a height greater than that of the upper part of the wall of overflow 31.
  • the feeding is carried out from shears 33 or 34 who carry out a summary fragmentation of the waste at a maximum size between 200 and 400 mm.
  • the fragmented waste is introduced either by conduits 35 provided with injection screws such as screw 36, either by simple gravity in the conduits 37. Means conventional not shown allow to adjust the flow waste introduced.
  • conduit 39 (or more conduits if necessary) collecting heavy non-fludisable elements such as scrap, bottles, pieces of glass, etc. or items that have not been pyrolyzed. These elements are sent to the base of part 18 of the circulating fluidized bed, with, possibly, prior passage through a sorting device 40 from which are extracted the elements which do not come disturb the fluidization at the base of the fluidized bed circulating 18.
  • recycled smoke for example taken in E1 upstream of the TF smoke treatment, can be injected into the conduits 39.
  • the conduits 39 are provided, in the vicinity of the grid 29, means for regulating the flow rate of solids passing through in these conduits. These means can be arrivals 39 'adjustable air.
  • the wall 11 where the waste is introduced is protected by a coating of silicon carbide or any other material resistant to reducing medium; the usefulness of this coating will be shown later.
  • a second fluidized bed dense lateral 48 is installed along the wall 12 which, in the example described, is the wall opposite wall 11. It includes an overflow wall 51, a grid 52 and air nozzles 53 supplied with air (referenced AF), possibly with the addition of recycled smoke dechlorinated, for example from an E2 outlet downstream TF smoke treatment.
  • the base of the dense bed 48 is connected by conduits 59 to the lower part 18 of the circulating fluidized bed.
  • Means for adjusting the flow of solids are provided flowing in these conduits 59; these means can be consisting of air inlets with adjustable flow.
  • the exchange member SHT thermal which can include evaporators and / or high temperature steam superheaters.
  • the reactor is completed by air injectors 54, said tertiary air, which are arranged on the four sides of the reactor at a height higher than that of fluidized beds dense lateral. Again tertiary air can be mixed to recycled smoke from the E1 socket for this which is injectors placed on the dense bed supply 28 and dechlorinated from outlet E2 for the dense exchange bed 48.
  • the temperature in the center of the reactor is higher at 850 ° C and generally between 850 and 950 ° C for comply with the regulations concerning the combustion of waste.
  • the ratio of section S2 measured above the overflow walls 31 and 51 in section S1 measured between these overflow walls is between 1.05 and 2.
  • the speed of the fluidizing gases in the part lower axial 18 is, in empty barrel, between 3 and 12m / s.
  • the surface velocity of the fluidizing gases, in was empty, in the dense side beds is between 0.3 and 2.5 m / s.
  • the operation of the reactor is as follows.
  • This pyrolysis effect is obtained by mixing the waste introduced and solids falling into the wall under form of a dense layer as a result of the functioning of the upper part 18 'in circulating fluidized bed.
  • the dense fluidized bed 48 is fed by the dense layer of circulating solids resulting from the 18-18 'circulating fluidized bed operation.
  • the dense bed 48 is fluidized by a mixture of air and dechlorinated fumes, as mentioned above.
  • This bed 48 is therefore free of chlorinated products. It is therefore possible to house the SHT heat exchange member; this organ will be placed in a medium whose temperature is 870 ° C approximately so that steam will be obtained superheated to 450 or 500 ° C (instead of 360 ° C in the prior art reactors since one cannot place the exchanger in a medium at a temperature above 600 ° C. without very rapid corrosion).
  • heat exchange members having external exchange coefficients of 450 W / m 2 ° K (instead of 35 W / m 2 ° K in the prior art) and a DTLM (much larger mean log temperature difference) (450 ° C instead of 250 ° C.
  • Fluidized reactor can operate with excess overall air, in relation to the stoecchiometric conditions, limited to 1.4, which has the double advantage of being compliant with regulations and more economical than certain facilities that require for their operating air excess of 1.8 or 1.9.
  • the circulating fluidized beds inherently generate low nitrogen oxides by the low temperature, the air staging and the low air flow; if necessary, an injection of ammonia upstream of the hot cyclone 2 can be envisaged. In this way, the limitation to 200 mg / m 3 can be easily respected.
  • the adjustable air injection serves as auxiliary air for combustion with volatile combustible materials released by pyrolysis-flash; this air allows rapid mixing of gases of the upper part of the reactor which favors chlorine removal.
  • a terminal air injection can possibly be planned upstream of cyclone 2.
  • the wall in which the connection is made between reactor 1 and the cyclone 2, here the wall 12, is chosen opposite the wall 11 where the reactor is fed.
  • the invention also applies to treatment simultaneous waste increased by a certain proportion of sludge from wastewater treatment plants, biomass residues, as well as ordinary industrial waste and the refusal to automotive grinding.
  • the invention also applies to treatment simultaneous waste with fossil fuels of the type coal or petroleum residue. These are introduced in bottom of the lower zone of the circulating fluidized bed 18-18 ', 18 for example by the return pipe of cyclone 2.
  • the reactor may include injection means agents for fixing the sulfur contained in the fumes, such as than limestone.
  • the temperature of the bed dense introduction of waste is desired lower that 870 to 900 ° C, it is possible to feed the dense bed 28 waste introduction with part of the products of the heat exchange bed 48.
  • Reactor walls can be fully cased or in part.
  • the tubes some of which are represented and referenced 60 are traversed by a mixture of water and steam from and returning to the boiler tank.
  • the reactor will include a third dense lateral fluidized bed, the heat exchange being carried out with at least one of the second and third dense lateral fluidized beds.
  • the reactor according to the invention will include third and fourth fluidized beds lateral, the heat exchange being carried out with at least one of the second, third and fourth fluidized beds lateral.
  • Fig. 4 illustrates a variant in which solids collected by the dense bed 48 are transferred into an annex 70 fluidized bed exchanger before being reinjected into the zone 18 by means of conduits 71 provided air flow 71 'flow control. It is in this bed 70 that is placed the heat exchange member SHT.
  • the fluidization gases from bed 70 are reinjected by a conduit 72 to the upper part 18 'of the bed 18-18'.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Dispersion Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Processing Of Solid Wastes (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Crucibles And Fluidized-Bed Furnaces (AREA)
  • Treating Waste Gases (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP96401196A 1995-06-07 1996-06-05 Réacteur à lits fluidisés pour le traitement thermique des déchets Expired - Lifetime EP0747462B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR9506707 1995-06-07
FR9506707A FR2735041B1 (fr) 1995-06-07 1995-06-07 Reacteur a lits fluidises pour le traitement thermique des dechets

Publications (2)

Publication Number Publication Date
EP0747462A1 EP0747462A1 (fr) 1996-12-11
EP0747462B1 true EP0747462B1 (fr) 2000-01-12

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ID=9479704

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EP96401196A Expired - Lifetime EP0747462B1 (fr) 1995-06-07 1996-06-05 Réacteur à lits fluidisés pour le traitement thermique des déchets

Country Status (17)

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US (1) US5954001A (cs)
EP (1) EP0747462B1 (cs)
JP (1) JPH10506985A (cs)
KR (1) KR970704858A (cs)
CN (1) CN1077130C (cs)
AT (1) ATE188726T1 (cs)
CA (1) CA2196808A1 (cs)
CZ (1) CZ21797A3 (cs)
DE (1) DE69606093T2 (cs)
DK (1) DK0747462T3 (cs)
ES (1) ES2140798T3 (cs)
FR (1) FR2735041B1 (cs)
HU (1) HU220428B (cs)
PL (1) PL179698B1 (cs)
PT (1) PT747462E (cs)
SK (1) SK17297A3 (cs)
WO (1) WO1996040837A1 (cs)

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FR2758748B1 (fr) * 1997-01-30 1999-04-02 Gec Alsthom Stein Ind Installation de valorisation energetique de dechets urbains et assimiles
FR2758747B1 (fr) * 1997-01-30 1999-04-02 Gec Alsthom Stein Ind Installation de valorisation energetique de dechets urbains et assimiles
JPH10253011A (ja) * 1997-03-13 1998-09-25 Hitachi Zosen Corp 燃焼装置
US6367395B1 (en) * 2000-11-06 2002-04-09 Tommy D. Masek Method of disposing of animal waste
US20040100902A1 (en) * 2002-11-27 2004-05-27 Pannalal Vimalchand Gas treatment apparatus and method
FR2918160A1 (fr) 2007-06-28 2009-01-02 Inst Francais Du Petrole Procede de preparation d'une charge mixte contenant de la biomasse et une coupe hydrocarbonnee lourde en vue d'une gazeification ulterieure.
DE102008064321A1 (de) * 2008-09-19 2010-04-01 Ecoenergy Gesellschaft Für Energie- Und Umwelttechnik Mbh Externe Frischluftvorwärmung bei Feststofffeuerungen
CN103506056B (zh) * 2012-06-28 2015-09-30 广东先导稀材股份有限公司 无筛板的流化床及三氯化硼的制备方法
CN106594747B (zh) * 2017-01-26 2018-06-15 严志谋 改进的无害化垃圾焚烧炉

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US4165717A (en) * 1975-09-05 1979-08-28 Metallgesellschaft Aktiengesellschaft Process for burning carbonaceous materials
GB2070960B (en) * 1980-01-15 1984-06-06 Flameless Furnaces Ltd Fluidised bed combustors
US4335662A (en) * 1980-09-12 1982-06-22 Combustion Engineering, Inc. Solid fuel feed system for a fluidized bed
JPS57501646A (cs) * 1980-09-23 1982-09-09
DE3322971C3 (de) * 1983-06-25 1994-07-28 Lentjes Ag Wirbelschichtreaktor
DE3721341C1 (de) * 1987-06-27 1988-11-17 Bbc Brown Boveri & Cie Verfahren zum thermischen Zersetzen von Abfallmaterial sowie Wirbelschicht-Pyrolysereaktor zur Durchfuehrung des Verfahrens
US4992245A (en) * 1988-03-31 1991-02-12 Advanced Silicon Materials Inc. Annular heated fluidized bed reactor
US5091156A (en) * 1989-02-13 1992-02-25 A. Ahlstrom Corporation Waterwalls in a fluidized bed reactor
FR2661113B1 (fr) * 1990-04-20 1993-02-19 Stein Industrie Dispositif de realisation d'une reaction entre un gaz et un materiau solide divise dans une enceinte.
FR2690512B1 (fr) * 1992-04-27 1994-09-09 Stein Industrie Réacteur à lit fluidisé circulant comportant des échangeurs extérieurs alimentés par la recirculation interne.
US5325823A (en) * 1992-12-24 1994-07-05 Foster Wheeler Energy Corporation Large scale fluidized bed reactor
FI93274C (fi) * 1993-06-23 1995-03-10 Ahlstroem Oy Menetelmä ja laite kuuman kaasuvirran käsittelemiseksi tai hyödyntämiseksi

Also Published As

Publication number Publication date
KR970704858A (ko) 1997-09-06
DE69606093D1 (de) 2000-02-17
HUP9700364A2 (hu) 1998-05-28
CZ21797A3 (en) 1997-05-14
CN1155897A (zh) 1997-07-30
WO1996040837A1 (fr) 1996-12-19
DK0747462T3 (da) 2000-06-26
HU220428B (hu) 2002-01-28
EP0747462A1 (fr) 1996-12-11
ES2140798T3 (es) 2000-03-01
HUP9700364A3 (en) 1999-11-29
JPH10506985A (ja) 1998-07-07
CN1077130C (zh) 2002-01-02
DE69606093T2 (de) 2000-08-24
SK17297A3 (en) 1997-07-09
FR2735041A1 (fr) 1996-12-13
US5954001A (en) 1999-09-21
PT747462E (pt) 2000-04-28
CA2196808A1 (fr) 1996-12-19
PL318505A1 (en) 1997-06-23
PL179698B1 (pl) 2000-10-31
ATE188726T1 (de) 2000-01-15
FR2735041B1 (fr) 1997-07-11

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