EP1712839B1 - Procédé de récuperation de la chaleur et appareil de récuperation de la chaleur - Google Patents

Procédé de récuperation de la chaleur et appareil de récuperation de la chaleur Download PDF

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Publication number
EP1712839B1
EP1712839B1 EP04770831.8A EP04770831A EP1712839B1 EP 1712839 B1 EP1712839 B1 EP 1712839B1 EP 04770831 A EP04770831 A EP 04770831A EP 1712839 B1 EP1712839 B1 EP 1712839B1
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EP
European Patent Office
Prior art keywords
gas
heat recovery
heat
fluidized bed
recovery apparatus
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EP04770831.8A
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German (de)
English (en)
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EP1712839A1 (fr
EP1712839A4 (fr
Inventor
Norihisa Miyoshi
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Ebara Corp
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Ebara Corp
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Priority claimed from JP2004012419A external-priority patent/JP4265975B2/ja
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Publication of EP1712839A4 publication Critical patent/EP1712839A4/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/006—Layout of treatment plant
    • 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
    • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
    • 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
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/303—Burning pyrogases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/20—Combustion to temperatures melting waste

Definitions

  • the present invention relates to a heat recovery method and an apparatus for processing a combustible material, which use the generated heat to melt ash and which can recover the heat effectively, when a combustible material such as municipal waste, waste plastic, shredder dust, construction waste, waste tires or biomass is processed.
  • the gasification melting method is a method in which waste is partially combusted at approximately 500°C to obtain pyrolysis gas and the pyrolysis gas is combusted at a high temperature in a melting furnace to melt ash content entrained in the gas. Since the pyrolysis gas which can be obtained in this method is gas produced by partial combustion of waste, it contains combustion product gas and has a low calorific value. Therefore, to achieve a sufficiently high temperature to melt ash in a melting furnace, that is, a temperature of approximately 1200°C, the waste to be dumped needs to have a calorific value of approximately 7 to 8 MJ/kg.
  • the ash content entrained in the pyrolysis gas flowing into the melting furnace contains low-melting point metals, low-boiling point metal salts and so on in addition to silica-, alumina- and calcia-based substances
  • the components which are melt in the melting furnace are mainly the silica-, alumina- and calcia-based substances and the low-boiling point metal salts and so on flow downstream out of the melting furnace together with the combustion product gas.
  • the melting furnace has such a structure that a swirling gas flow can be formed inside thereof and, in many cases, a means for suddenly inverting the flow direction of the gas causes the ash content in the gas to collide with the wall surfaces of the melting furnace by inertia force to form a slag flow in order to increase the melting rate of the ash content contained in the substances to be melted. Therefore, particles with large particle sizes are captured by the slag flow, and, consequently, the ash content in the exhaust gas flowing downstream out of the melting furnace has particle sizes of mainly 10 ⁇ m or smaller.
  • the ash content in the gas flowing downstream out of the melting furnace is characterized by a high content of salts and very small particle sizes as described above, which causes various problems. Fine particles are melted at every temperature in various temperature ranges from a high-temperature range of 1200°C or higher immediately after the melting to a temperature range around 400°C. The melted fine particles adhere to the heat transfer surface of a device installed for heat recovery and significantly lower the heat transfer coefficient of the heat transfer surface.
  • the function of the heat recovery device decreases and it becomes unable to lower the gas temperature, for example.
  • the gas temperature at the exit of the heat recovery step may increase and exceed an allowable temperature of a dust collection step such as a bag filter provided downstream of the heat recovery step.
  • a dust collection step such as a bag filter provided downstream of the heat recovery step.
  • the temperature at the entrance of the dust collection step must be not higher than the permissible temperature. Therefore, it is necessary to provide a water spraying gas cooling step in advance or to provide a sufficiently large allowance to the heat transfer area at the heat transfer surface of the heat recovery device to maintain the function of the heat recovery device sufficiently so that the gas temperature at the entrance of the dust collection step cannot be higher than the allowable temperature. This causes an increase in cost due to increase in equipment.
  • FIG. 1 is a view illustrating the process flow of an apparatus for processing a combustible material employing a conventional gasification melting method (see JP-B-3153091 ).
  • the apparatus for processing a combustible material has a gasification furnace 101, a melting furnace 102, a boiler 103, an economizer or an air preheater 104, a gas cooling tower 105, a bag filter 106, an inducing blower 107, a catalyst denitration tower 108 and a stack 109.
  • the combustible material is supplied to the gasification furnace 101, and is combusted partially and pyrolyzed to generate pyrolysis gas, tar, char, fly ash and so on.
  • the pyrolysis gas entraining the tar, char, fly ash and so on is all supplied to the melting furnace 102.
  • the pyrolysis gas is combusted at a high temperature of 1200°C or higher in the melting furnace 102, and ash content is melted and discharged out of the furnace as molten slag.
  • High-temperature combustion product gas discharged from the melting furnace is directed to the boiler 103.
  • the combustion product gas is cooled to approximately 450°C in the boiler 103 and further cooled down to approximately 200°C in the economizer or air preheater 104.
  • the ash content entrained in the high-temperature combustion product gas flowing out of the melting furnace 102 has high adhesivity since it has small particle sizes and contains a large proportion of metal salts with relatively low melting points. Thus, it easily adheres to the heat transfer surfaces of the boiler 103 and the economizer or air preheater 104. Therefore, since it gradually adheres to the heat transfer surfaces of the boiler 103 and the economizer or air preheater 104 and decreases the heat transfer coefficients thereof during operation, the combustion product gas, which can be sufficiently cooled immediately after the start of operation, becomes gradually less able to be cooled with elapse of operation time and the entrance temperature of the bag filter 106 increases correspondingly.
  • the maximum allowable temperature of a bag filter is approximately 220°C.
  • spray water into the combustion product gas in the gas cooling tower 105 so that the gas temperature cannot exceed it.
  • the adhesion of ash to the heat transfer surfaces is not stopped.
  • the combustion product gas temperature at the entrance of the air preheater gradually increases and the adhesion of ash further increases.
  • the temperature range exceeding 450°C the ash is in a semi-molten state and difficult to be scraped or to be brushed off mechanically, and it is difficult to stop adhesion of ash without lowering the temperature. In other words, once the function of the heat transfer surfaces is lowered, it is difficult to suppress adhesion of ash in that state.
  • FIG. 2 is a view illustrating the process flow of another apparatus for processing a combustible material.
  • Combustion product gas discharged from the combustion chamber 110-2 is introduced into a dust collector 112 such as a cyclone at a temperature of 850°C to 950°C and subjected to dust removal, and then is introduced into the boiler 103.
  • the ash content particles trapped by the dust collector 112 are directed into the melting furnace 102 and melted therein.
  • the heat recovery method preferably further comprises the steps of: combusting the char in a combustion chamber 22, and introducing a fluidized medium from the combustion chamber 22 to a pyrolysis chamber 21 for pyrolyzing the combustible material 34 (D, E).
  • the heat generated by combusting the char in the combustion chamber can be transferred to the fluidized medium and the heat can be used for the pyrolysis reaction of the combustible material in the pyrolysis chamber effectively.
  • Another method for processing a combustible material comprises the steps of, as shown in FIG. 3 for example, generating first gas G2 and second gas G1 both entraining particles in a fluidized bed gasification furnace 1; introducing the first gas G2 from the fluidized bed gasification furnace 1 into a heat recovery apparatus 3; recovering heat by heat exchange between the introduced gas G2 and a heat receiving fluid; introducing the second gas G1 from the fluidized bed gasification furnace 1 into a melting furnace 2 to melt ash content in the particles; and introducing the gas G3 in which the ash content has been melted into the heat recovery apparatus 3.
  • the first gas from the fluidized bed gasification furnace is introduced into the heat recovery apparatus to recover heat therefrom and the second gas from the fluidized bed gasification furnace is introduced into the melting furnace and the gas discharged from the melting furnace is introduced into the same heat recovery apparatus as described above, the first gas is gas entraining particles mostly with large particle sizes. Adhesion of particles to the heat transfer surface can be therefore prevented by the grinding function which the particles exhibit when colliding with the heat transfer surface.
  • the first gas entraining particles mostly with large particle sizes from the fluidized bed gasification furnace is introduced into the heat recovery apparatus to recover heat and then the gas from which heat has been recovered is mixed with the second gas entraining particles mostly with small particle sizes and discharged from the melting furnace to recover heat as described above, adhesion of particles to a heat transfer surface can be prevented by the grinding function which the particles with large particle sizes in the first gas exhibit when colliding with the heat transfer surface.
  • a heat recovery apparatus comprises, as shown in FIG. 3 for example, a first introduction port for introducing first gas G2 entraining particles mostly with large particle sizes; a second introduction port located downstream of the first introduction port along the flowing direction of the gas G2 introduced through the first introduction port for introducing second gas G3 entraining particles mostly with small particle, wherein first gas G2 and second gase G3 flow in the heat recovery apparatus first in a downward direction with respect to gravity as they mix and then in an upward direction with respect to gravity after a change of direction at the bottom of the heat recovery apparatus; a discharge port for discharging gas G4 from which heat has been recovered; and a heat transfer surface for allowing heat exchange between the gases G2,G3 introduced through the first and second introduction ports and a heat receiving fluid to recover heat from the gases G2,G3.
  • the first gas G2 is gas generated in a fluidized bed furnace 1 by supplying a combustible material to the fluidized bed furnace 1
  • the second gas G3 is gas obtained by introducing the gas G2 generated in the fluidized bed furnace 1 into a melting furnace 2 and melting ash content entrained in the gas.
  • the gas generated in the fluidized bed furnace by supplying a combustible material to the fluidized bed furnace is gas entraining particles mostly with large particle sizes and the gas obtained by introducing the gas generated in the fluidized bed furnace into the melting furnace and melting ash content therein is gas entraining particles mostly with small particle sizes, the same effect can be achieved by introducing the gas generated in the fluidized bed furnace into the heat recovery apparatus through the first introduction port as the first gas and the gas obtained in the melting furnace into the heat recovery apparatus through the second introduction port as the second gas.
  • the second gas generated in the fluidized bed gasification furnace is introduced into the melting furnace and gas discharged from the melting furnace is introduced into the heat recovery apparatus, which receives the first gas generated in the fluidized bed gasification furnace and entraining particles and recovers heat therefrom, as described above, adhesion of particles, especially the particles with small particle sizes in the gas discharged from the melting furnace, which tend to adhere, can be prevented by the grinding function which the particles in the first gas exhibit when colliding with the heat transfer surface.
  • the heat recovery apparatus for heat exchange with the first gas and the heat recovery apparatus for heat exchange with the mixed gas of the first gas and the second gas may be the same apparatus or different apparatuses.
  • the fluidized bed gasification furnace 1 preferably comprises a pyrolysis chamber 21 for pyrolyzing the combustible material 34 to generate the second gas G1, a combustion chamber 22 for combusting char to generate the first gas G2, and a passage D,E for directing a fluidized medium from the combustion chamber 22 to the pyrolysis chamber 21.
  • the apparatus for processing a combustible material preferably further comprises, as shown in FIG. 3 for example, a passage for introducing the second gas G1 from the pyrolysis chamber 1-1 to the melting furnace 2; and a passage for introducing the first gas G2 from the combustion chamber 1-2 to the heat recovery apparatus 3.
  • the heat recovery apparatus 3 preferably is a waste heat boiler.
  • a fluidized bed gasification furnace 1 for gasifying a combustible material to generate first gas G2 and second gas G1 both entraining particles
  • a solid separator 12 for trapping the particles in the first gas G2 generated in the fluidized bed gasification furnace 1
  • a melting furnace 2 for combusting the second gas G1 generated in the fluidized bed gasification furnace 1 to melt the particles trapped by the solid separator 12 and to generate combustible gas
  • the solid separator for trapping the particles includes a device which separates solid matter from gas by the difference in density such as a cyclone and so on as well as a filter for filtering the first gas to tap the particles therein when the first gas entraining the particles passes through.
  • a device which separates solid matter from gas by the difference in density such as a cyclone and so on as well as a filter for filtering the first gas to tap the particles therein when the first gas entraining the particles passes through.
  • a combustible material having a low calorific value of, for example, 6 to 7 MJ/kg can be combusted at a high temperature of 1200°C or higher and the ash content can be melted without using auxiliary fuel.
  • Heat is recovered from the first gas entraining particles mostly with large particle sizes and then the first gas is mixed with the second gas entraining particles mostly with small particle sizes. Therefore, there can be provided a heat recovery method in which adhesion of particles, especially adhesion of the particles with small particle sizes which tend to adhere to a heat transfer surface, in the second gas to the heat transfer surface can be prevented by the grinding function to grind the heat transfer surface which the particles with large particle sizes in the first gas exhibit when colliding with the heat transfer surface.
  • the first gas from the fluidized bed gasification furnace is introduced into the heat recovery apparatus to recover heat therefrom, and the second gas from the fluidized bed gasification furnace is introduced into the melting furnace and gas discharged from the melting furnace is introduced into the heat recovery apparatus. Since the first gas is gas entraining particles mostly with large particle sizes, there can be provided a method for processing a combustible material in which adhesion of particles to a heat transfer surface can be prevented by the grinding function which the particles exhibit when colliding with the heat transfer surface.
  • the first gas entraining particles mostly with large particle sizes from the fluidized bed gasification furnace is introduced into the heat recovery apparatus to recover heat therefrom. Then the gas from which heat has been recovered is mixed with the second gas discharged from the melting furnace and entraining particles mostly with small particle sizes and heat is recovered from the mixture. Therefore, there can be provided a method for processing a combustible material in which adhesion of particles to a heat transfer surface can be further prevented by the grinding function which the particles with large particle sizes in the first gas exhibit when colliding with the heat transfer surface.
  • the second introduction port for receiving the second gas entraining particles mostly with small particle sizes is located downstream of the first introduction port for receiving the first gas entraining particles mostly with large particle sizes. Therefore, there can be provided a heat recovery apparatus in which adhesion of particles, especially the particles with small particle sizes in the second gas introduced through the second introduction port, which tend to adhere to a heat transfer surface can be prevented by the grinding function which the particles with large particle sizes in the first gas introduced through the first introduction port exhibit when colliding with the heat transfer surface.
  • the second gas entraining particles mostly with small particle sizes is introduced after the first gas entraining particles mostly with large particle sizes has been cooled, resulting in the prevention of formation of a region with high-temperature gas entraining particles with small particle sizes, which tend to adhere to the heat transfer surface.
  • the second gas generated in the fluidized bed gasification furnace is introduced into the melting furnace and gas discharged from the melting furnace is introduced into the heat recovery apparatus, which receives the first gas generated in the fluidized bed gasification furnace and entraining fine particles and recovers heat therefrom. Therefore, there can be provided an apparatus for processing a combustible material in which adhesion of particles, especially the fine particles with small particle sizes in the gas discharged from the melting furnace, which tend to adhere to a heat transfer surface, to the heat transfer surface can be prevented by the grinding function which the particles in the first gas exhibit when colliding with the heat transfer surface.
  • the second gas generated in the fluidized bed gasification furnace and entraining fine particles and particles with large particle sizes entrained in the first gas generated in the fluidized bed gasification furnace are introduced into the melting furnace and ash content is melted therein. Therefore, the ash content can be melted with a combustible material with a low calorific value without using auxiliary fuel.
  • the combustible material is mainly supplied from the combustible material supplying means 36 to the pyrolysis chamber 1-1 side in the gasification furnace 1 and is pyrolyzed therein to generate pyrolysis gas, tar, char, fly ash and so on.
  • Pyrolysis gas G1 entraining the tar, char, fly ash and so on among those generated, which do not remain in the fluidized bed, is all supplied to the melting furnace 2 and combusted at a high temperature of 1200°C or higher in the melting furnace 2.
  • the ash content is melted and discharged out of the melting furnace 2 as molten slag.
  • fluidizing air is supplied from under the furnace and secondary air is supplied to the part above the free board. The air ratio is maintained at one or higher as a whole to ensure complete combustion.
  • the mixed combustion product gas G4 is cooled to approximately 450°C in the boiler 3 and further cooled to approximately 200°C in the heat recovery device 4 such as an economizer or air preheater, and then is subjected to dust removal in the dust collector 5 such as a cyclone.
  • the above devices are connected by passages for the combustion product gas constituted of pipes and so on. Ash 11 collected by the dust collector 5 is returned to the melting furnace 2 through a passage constituted of a pipe and so on and melted in the melting furnace 2.
  • the heat exchanger such as an economizer or air preheater may be omitted. In this case, the dust collection is performed at a temperature of 450°C or lower.
  • the ash particles in the gas mixed in the boiler 3 has a particle size distribution which is relatively close to that of gas from a conventional fluidized bed incinerator and has little possibility of causing a trouble by adhering to the heat transfer surfaces of the devices for use in the heat recovery step such as the boiler 3 and the heat recovery device 4 such as an economizer or air preheater.
  • FIG. 4 is a view illustrating the process flow of another apparatus for processing a combustible material according to the present invention.
  • ash 13 trapped by a bag filter 12 as a solid separator located downstream of the gas cooling tower 6 is supplied to the melting furnace 2 and melted therein.
  • a solid separator such as a cyclone may be provided instead of the bag filter 12.
  • Activated carbon 14 is added to the combustion product gas G4 discharged from the bag filter 12 to cause the activated carbon 14 to adsorb harmful substances, and the activated carbon 14 having adsorbed the harmful substances is trapped and removed by a bag filter 7.
  • FIG. 5 is a view illustrating an example of the constitution of an integrated fluidized bed gasification furnace as an example of the gasification furnace 1.
  • the gasification furnace 1 has a pyrolysis chamber 21 (corresponding to the pyrolysis chamber 1-1), a combustion chamber 22 (corresponding to the combustion chamber 1-2), and a heat recovery chamber 23.
  • a combustible material 34 supplied to the pyrolysis chamber 21 is pyrolyzed while being agitated by a fluidized medium revolving in the pyrolysis chamber 21 as indicated by arrows F in the drawing to generate pyrolysis gas, tar, char, fly ash and so on.
  • the molten slag 56 is cooled and pulverized in the water tank into granular slag.
  • the granular slag having sunk in the water tank is transported out of the system on a conveyor installed in the water tank.
  • the gas G3 in the melting furnace is water-sealed by water in the water tank and cannot leak out of the system.
  • the low-calorie or intermediate-calorie combustible gas G5 contains a large amount of useful gas components such as carbon monoxide CO and hydrogen H 2 .
  • a heat recovery device 15 such as a boiler to recover heat therefrom and passed through a scrubber 16
  • gas 17 as industrial fuel gas or raw materials for chemical industry can be obtained.
  • the above method for processing a combustible material is characterized in that the pyrolysis step and the combustion step are both conducted in a fluidized bed furnace, and the amount of heat necessary for the pyrolysis in the pyrolysis step is obtained from the sensible heat of a fluidized medium in the fluidized bed furnace in which the combustion step is conducted.
  • the above method for processing a combustible material is characterized in that the pyrolysis step is maintained at 650°C or lower, preferably 600°C or lower, more preferably 550°C or lower, and the temperature in the combustion step is maintained at 900°C or lower, preferably 800°C or lower, more preferably 700°C or lower.
  • the pyrolysis and gasification are preferably performed at a low temperature of 650°C or lower as described above. When the pyrolysis and gasification are performed at 550°C or lower, they can be performed more stably. It is also preferred to maintain the pyrolysis step at a low temperature to combust a combustible material such as municipal waste stably with little fluctuation.
  • the combustion is preferably performed at a low temperature of 700°C or lower. At a high temperature of 900°C or higher, there arises a problem in the heat resistance and so on of metal parts, especially, of the dispersion nozzle or the like.
  • the lower limit of the temperature in the pyrolysis step depends on the type of the combustible material. For example, when the combustible material is only biomass, the lower limit is 280°C or higher, preferably 300°C or higher, since the decomposition temperature of typical lignin is 280°C. When plastic is contained in the combustible material, the lower limit is 390°C or higher, preferably 400°C or higher, since the decomposition temperature of typical high-density polyethylene HDPE is 390°C.
  • the above apparatus for processing a combustible material is characterized in that the pyrolysis chamber and the combustion chamber are both constituted of a fluidized bed furnace.
  • the gas is supplied to the melting furnace, even a combustible material with a low calorific value of, for example, 6 to 7 MJ/kg can be combusted at a high temperature of 1200°C or higher without using auxiliary fuel in the melting furnace and ash content can be melted.

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  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Gasification And Melting Of Waste (AREA)

Claims (9)

  1. Procédé de récupération de chaleur, comprenant les étapes de :
    récupérer de la chaleur, en utilisant un appareil de récupération de chaleur (3), d'un premier gaz (G2) entrainant des particules de grandes dimensions ; et
    récupérer de la chaleur, en utilisant l'appareil de récupération de chaleur (3), d'un mélange gazeux, dans lequel un second gaz (G3) entrainant des particules de petites dimensions est mélangé avec le premier gaz (G2) duquel de la chaleur a été récupérée pour former le mélange gazeux,
    fournir un matériau combustible (34) à une chambre de pyrolyse (1-1, 21) ayant un lit fluidisé dans lequel une substance fluidisée tourne, et pyrolyser le matériau combustible (34) dans le lit fluidisé, pour générer du charbon et un gaz de pyrolyse (G1) entrainant des particules incluant de la cendre ;
    bruler le charbon dans un lit fluidisé dans une chambre de combustion (1-2, 22) ayant le lit fluidisé dans lequel une substance fluidisée tourne, pour générer le premier gaz (G2) ; and
    générer le second gaz (G3) en introduisant le gaz de pyrolyse (G1) dans un four de fusion (2) et en fondant la cendre ;
    dans laquelle le premier gaz (G2) est introduit dans l'appareil de récupération de chaleur (3), de façon que le premier gaz (G2) soit introduit dans l'appareil de récupération de chaleur (3) avec les particules dans le premier gaz (G2),
    dans laquelle le second gaz (G3) est introduit dans l'appareil de récupération de chaleur (3) en aval d'un flux du premier gaz (G2) dans l'appareil de récupération de chaleur (3) de façon que le second gaz (G3) soit mélangé avec le premier gaz (G2) ; et
    le second gaz (G3) est mélangé avec le premier gaz (G2) en aval du flux du premier gaz (G2) dans l'appareil de récupération de chaleur (3).
  2. Procédé de récupération de chaleur selon la revendication 1, comprenant en outre l'étape de :
    introduire la substance fluidisée de la chambre de combustion (1-2, 22) à la chambre de pyrolyse (1-1, 21).
  3. Procédé de récupération de chaleur selon l'une quelconque des revendications 1 ou 2, comprenant en outre l'étape de :
    refroidir le mélange gazeux à 450°C ou moins ;
    séparer la matière solide du gaz refroidi avec un collecteur de poussière (5) ; et
    introduire la matière solide séparée dans le four de fusion (2) et y fondre la matière solide.
  4. Procédé de récupération de chaleur selon l'une quelconque des revendications 1 à 3, comprenant en outre l'étape de :
    introduire le premier gaz (G2) et le second gaz (G3) dans l'appareil de récupération de chaleur (3) de façon que le premier gaz (G2) et le second gaz (G3) s'écoulent dans l'appareil de récupération de chaleur (3) d'abord dans une direction descendante par rapport à la gravité puis dans une direction montante par rapport à la gravité après un changement de direction au fond de l'appareil de récupération de chaleur (3).
  5. Appareil de traitement d'un matériau combustible, comprenant :
    un appareil de récupération de chaleur (3) ayant :
    un premier orifice d'introduction pour introduire un premier gaz (G2) ;
    un second orifice d'introduction pour introduire un second gaz (G3) entrainant des particules, le second orifice d'introduction étant situé en aval du premier orifice d'introduction le long d'une direction d'écoulement du premier gaz (G2) introduit à travers le premier orifice d'introduction ;
    un orifice de décharge pour décharger un gaz duquel de la chaleur a été récupérée ; et
    un surface d'échange de chaleur pour permettre un échange de chaleur entre les premier et second gaz (G2, G3) ;
    une chambre de pyrolyse (1-1, 21) ayant un lit fluidisé dans lequel une substance fluidisée tourne, et pyrolysant un matériau combustible (34) dans le lit fluidisé, pour générer du charbon et un gaz de pyrolyse (G1) entrainant des particules incluant de la cendre ;
    une chambre de combustion (1-2, 22) ayant un lit fluidisé dans lequel une substance fluidisée tourne, pour bruler le charbon dans le lit fluidisé et générer le premier gaz (G2), le charbon ayant été généré dans la chambre de pyrolyse (1-1, 21) ;
    un four de fusion (2) pour générer le second gaz (G3) en y introduisant le gaz de pyrolyse (G1) et en fondant la cendre ;
    un passage d'introduction de gaz connecté au second orifice d'introduction pour introduire le second gaz déchargé du four de fusion (2) dans l'appareil de récupération de chaleur (3) ;
    un passage connecté au premier orifice d'introduction pour introduire le premier gaz (G2) dans l'appareil de récupération de chaleur (3) de façon que le premier gaz (G2) soit introduit dans l'appareil de récupération de chaleur (3) avec les particules dans le premier gaz (G2).
  6. Appareil de traitement d'un matériau combustible selon la revendication 5, comprenant en outre :
    un second appareil de récupération de chaleur (4) pour refroidir un mélange gazeux du premier gaz (G2) et du second gaz (G3) à 450°C ou moins, après que le premier gaz (G2) et le second gaz (G3) aient été mélangés,
    un collecteur de poussière (5) pour séparer la matière solide dans le mélange gazeux ; et
    un passage à poussière pour introduire le solide séparé dans le four de fusion (2) pour y fondre la matière solide.
  7. Appareil de traitement d'un matériau combustible selon la revendication 5 ou 6, comprenant en outre :
    un passage pour diriger la substance fluidisée de la chambre de combustion (1-2, 22) à la chambre de pyrolyse (1-1, 21).
  8. Appareil de traitement d'un matériau combustible selon la revendication 6 ou 7, dans lequel l'appareil de récupération de chaleur (3) est constitué de façon que le premier gaz (G2) et le second gaz (G3) soient introduits dans l'appareil de récupération de chaleur (3) de façon que le premier gaz (G2) et le second gaz (G3) s'écoulent dans l'appareil de récupération de chaleur (3) d'abord dans une direction descendante par rapport à la gravité puis dans une direction montante par rapport à la gravité après un changement de direction au fond de l'appareil de récupération de chaleur (3).
  9. Appareil de traitement d'un matériau combustible selon l'une quelconque des revendication 5 à 8,
    dans lequel l'appareil de récupération de chaleur (3) est une chaudière à chaleur perdue.
EP04770831.8A 2004-01-20 2004-07-20 Procédé de récuperation de la chaleur et appareil de récuperation de la chaleur Active EP1712839B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2004012419A JP4265975B2 (ja) 2003-01-20 2004-01-20 熱回収方法、可燃物の処理方法、熱回収システム及び可燃物の処理装置
PCT/JP2004/010320 WO2005068909A1 (fr) 2004-01-20 2004-07-20 Procede de recuperation de la chaleur, procede de traitement de materiau combustible, appareil de recuperation de la chaleur et appareil de traitement de materiau combustible

Publications (3)

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EP1712839A1 EP1712839A1 (fr) 2006-10-18
EP1712839A4 EP1712839A4 (fr) 2012-12-19
EP1712839B1 true EP1712839B1 (fr) 2018-11-21

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ITPI20070039A1 (it) * 2007-04-10 2008-10-11 Delca S P A Impianto e metodo per la produzione di energia elettrica
NL2001501C2 (nl) * 2008-04-18 2009-10-20 Dhv B V Werkwijze voor het vervaardigen van energie en synthetische bouwmaterialen, zoals basalt, grind, bakstenen, tegels enzovoort en dergelijke materialen uit hoogcalorisch afval en minerale reststoffen.
CN102671410B (zh) * 2012-05-29 2014-12-24 上海锅炉厂有限公司 一种带有灰渣捕捉的防结渣及沾污的显热回收装置

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JP3276274B2 (ja) * 1995-09-13 2002-04-22 三菱重工業株式会社 廃棄物の焼却熱を利用した過熱蒸気製造装置
JP3091197B1 (ja) * 1999-12-03 2000-09-25 川崎重工業株式会社 チャー分離方式ごみガス化溶融装置におけるダイオキシン類の低減方法及び装置
JP3839709B2 (ja) * 2001-09-07 2006-11-01 株式会社荏原製作所 ガス供給装置、ガス供給利用システム、ガス化溶融システム及びガス供給方法

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EP1712839A1 (fr) 2006-10-18
EP1712839A4 (fr) 2012-12-19

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