EP1284389A1 - Procede et dispositif de traitement de dechets - Google Patents

Procede et dispositif de traitement de dechets Download PDF

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Publication number
EP1284389A1
EP1284389A1 EP00929845A EP00929845A EP1284389A1 EP 1284389 A1 EP1284389 A1 EP 1284389A1 EP 00929845 A EP00929845 A EP 00929845A EP 00929845 A EP00929845 A EP 00929845A EP 1284389 A1 EP1284389 A1 EP 1284389A1
Authority
EP
European Patent Office
Prior art keywords
dust
gas
temperature
concentration
combustible gas
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.)
Withdrawn
Application number
EP00929845A
Other languages
German (de)
English (en)
Other versions
EP1284389A4 (fr
Inventor
Takashi Noto
Akira Nakamura
Seiji Kinoshita
Hajime Akiyama
Takuya Shinagawa
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.)
JFE Engineering Corp
Original Assignee
JFE Engineering Corp
NKK Corp
Nippon Kokan Ltd
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
Application filed by JFE Engineering Corp, NKK Corp, Nippon Kokan Ltd filed Critical JFE Engineering Corp
Publication of EP1284389A1 publication Critical patent/EP1284389A1/fr
Publication of EP1284389A4 publication Critical patent/EP1284389A4/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—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
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/025—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using filters
    • 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
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2207/00—Control
    • F23G2207/30—Oxidant supply
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07002—Injecting inert gas, other than steam or evaporated water, into the combustion chambers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07009—Injection of steam into the combustion chamber

Definitions

  • the present invention relates to a method and a system for waste treatment.
  • wastes A method for waste treatment in which municipal wastes or industrial wastes (hereinafter referred simply to as wastes) are partially oxidized and gasified, and then are burned has been disclosed in Unexamined Japanese Patents JP-A-7-35322 and JP-A-9-159132.
  • FIG. 10 schematically shows an example of a typical method disclosed in JP-A-7-35322.
  • Wastes are gasified in a partial combustion fluidized bed furnace 1 in a reducing atmosphere with an air ratio of about 0.15 to 0.5 at a fluidized bed temperature of 450 to 650°C, and are introduced into a secondary combustion furnace 3 via a dust collector 2 such as a cyclone and an impact type dust collector.
  • the yielded gas is mixed with secondary air in the secondary combustion furnace 3, and is burned completely at a high temperature of 800 to 1000°C.
  • a desalting agent is supplied to restrain the generation of hydrogen chloride gas, and heat recovery is accomplished.
  • a dust recovery line 6 is provided under the dust collector 2, so that some of the desalting agent and some or all of dust are returned again to the partial combustion fluidized bed furnace 1 after being cooled by a cooler 7.
  • FIG. 11 schematically shows an example of a typical method disclosed in JP-A-9-159132.
  • Exhaust gas generated by the combustion of refuse in a combustion furnace is cooled to a temperature of 450 to 650°C by heated water 20 introduced from a fuel economizer 8 into a waste heat boiler 4, and dust is removed by a filter 9.
  • Some or all of the exhaust gas coming out of the filter 9 is supplied to a heating furnace 10, where the exhaust gas is heated to a high temperature by additional combustion using an auxiliary fuel 21, whereby it is used to overheat saturated steam 22, which comes from the waste heat boiler 4, to a temperature of about 500°C in a steam superheater 11.
  • some of the exhaust gas is discharged from a stack 14 through an induced draft fan 13 after waste heat is recovered by the fuel economizer 8 and an air preheater 12.
  • the above-described waste treatment methods have problems as described below.
  • the concentration of dust is high, so that the methods are disadvantageous in terms of dust removal.
  • the boiler tube is corroded by salt etc. contained in dust, or the amount of unburned gas of the exhaust gas generated in the combustion furnace is small, so that waste heat cannot be recovered effectively in the heating furnace.
  • An object of the present invention is to provide a method and a system for waste treatment in which wastes can be partially oxidized so that the concentration of dust does not increase and heat can be recovered from exhaust gas with high efficiency.
  • the above object can be achieved by a method for waste treatment, comprising the steps of: incompletely burning or partially oxidizing wastes in a partial oxidation furnace in which combustion reaction takes place to yield combustible gas having a concentration converted to Oxygen of -30 to 1% at the outlet of the partial oxidation furnace; introducing the combustible gas into a dust separator at a temperature of 250 to 800°C to reduce the dust concentration to 0.1 g/Nm 3 or lower; and burning the combustion gas, from which dust has been removed, in a combustion furnace at a high temperature.
  • the above object can be achieved by a method for waste treatment, comprising the steps of: incompletely burning or partially oxidizing wastes in a partial oxidation furnace in which combustion reaction takes place to yield combustible gas having a concentration converted to Oxygen of -30 to 1% at the outlet of the partial oxidation furnace; introducing the combustible gas into a dust separator at a temperature of 250 to 800°C to reduce the dust concentration to 0.1 g/Nm 3 or lower; introducing the combustible gas, from which dust is removed, into a wet gas treatment apparatus to reduce the concentration of hydrogen chloride to 20 ppm or lower; and burning the combustible gas subjected to wet gas treatment in a combustion furnace at a high temperature.
  • a system for waste treatment comprising a partial oxidation furnace for incompletely burning or partially oxidizing wastes to yield combustible gas having a concentration converted to Oxygen of -30 to 1% at the outlet of the furnace; a dust separator for reducing the concentration of dust contained in the combustible gas at a temperature of 250 to 800°C to 0.1 g/Nm 3 or lower; and a combustion furnace for burning the combustion gas, from which dust has been removed, at a high temperature, or a system for waste treatment, comprising a partial oxidation furnace for incompletely burning or partially oxidizing wastes to yield combustible gas having a concentration converted to Oxygen of -30 to 1% at the outlet of the furnace; a dust separator for reducing the concentration of dust contained in the combustible gas at a temperature of 250 to 800°C to 0.1 g/Nm 3 or lower; a wet gas treatment apparatus for reducing the concentration of hydrogen chloride contained in the
  • FIG. 1 schematically shows one embodiment of a waste treatment system in accordance with the present invention.
  • This system includes a partial oxidation furnace 1 for incompletely burning or partially oxidizing wastes, a dust separator 2 for decreasing the concentration of dust in combustible gas, a combustion furnace 3 for burning the combustible gas, from which dust has been removed, at a high temperature, and a boiler 4 for recovering heat.
  • Wastes charged in the partial oxidation furnace 1 is partially oxidized by the combustion of gas consisting mainly of air, whose oxygen concentration is controlled by steam or exhaust gas, by which combustible gas is yielded.
  • gas consisting mainly of air
  • the concentration converted to Oxygen of the yielded combustible gas at the outlet of the furnace 1 is lower than -30%, a problem of tar adhesion etc. occurs as a strongly reduced gas.
  • the concentration exceeds 1%, combustion in which dioxin etc. can be decreased sufficiently cannot be produced. Therefore, the concentration must be made in the range of -30 to 1% by regulating the air ratio so as to be, for example, 0.15 to 0.9.
  • the concentration converted to Oxygen so as to be in this range, the danger of explosion caused by combustible components and oxygen is lessened, and also the fluctuations in potential of generated combustible gas is decreased, so that steady operation can be performed.
  • the concentration converted to Oxygen means a value defined by a difference between the oxygen concentration in an atmosphere and the concentration of oxygen supposed to be consumed by a gas to be possibly oxidized.
  • the temperature in the furnace 1 is set at 400 to 800°C, at which temperature wastes is self-combustible and is partially oxidized.
  • the temperature of the yielded combustible gas is controlled so as to be 250 to 800°C according to the residence time in the partial oxidation furnace 1, and the combustible gas is sent to the dust separator 2, where dust is removed until the dust concentration becomes 0.1 g/Nm 3 or lower.
  • the temperature of combustible gas sent to the dust separator 2 is 250°C or lower, tar etc. sticks in the system, and if the temperature thereof is 800°C or higher, salt melted in the dust sticks. Therefore, the temperature thereof must be controlled so as to be in the range of 250 to 800°C, preferably 250 to 650°C.
  • dust can be removed without excessive cooling effected by using an attemperator or other equipment.
  • FIG. 2 shows the relationship between the dust concentration after dust removal and the useful life of boiler tube provided on the downstream side. This figure reveals that if the dust concentration after dust removal is 0.1 g/Nm 3 or lower, the useful life of boiler tube increases remarkably. The reason for this is that the amount of salt in dust decreases, so that the corrosion of boiler tube etc. is restrained.
  • a bag filter, ceramic filter, high-temperature electrical dust collector, inertial dust collector, high-performance cyclone, centrifugal dust collector, etc. are used according to the temperature of combustible gas. Also, it is desirable to use a filter type dust collector provided with a filter element of a candle type ceramic filter or filter cloth as shown in FIG. 3, or a honeycomb type ceramic filter with an opening of 10 mm or smaller.
  • a gas with an oxygen concentration of 5% or lower or nitrogen gas for the purpose of restraining the oxidation of combustible gas and avoiding a danger of unnecessary explosion and combustion.
  • the gas with an oxygen concentration of 5% or lower can be obtained by utilizing exhaust gas recirculation, or the pressure swing adsorption process or membrane separation process.
  • the conditions of brushing-off method be such that the gas pressure is 1 kg/cm 2 , the brushing-off time interval is several seconds to several hours, and the brushing-off period of time is 0.02 second to several tens of seconds.
  • the temperature of gas for brushing off dust be not lower than the temperature of the combustible gas to prevent the temperature of the combustible gas from decreasing.
  • the coating layer on the surface of the dust collector may sometimes be peeled off by the blow of gas for brushing off dust.
  • this phenomenon can be prevented completely if the gas is blown at the time when the pressure difference between the front and rear of the dust collector reaches a certain preset value.
  • the combustible gas is burned in the combustion furnace 3 so as to have a high temperature of about 1000°C.
  • the combustion furnace 3 since combustion is provided by mixing an oxidizer, complete combustion is accomplished. Therefore, the discharge of unburned gas such as CO is restrained almost completely. Also, since dust has been removed from the combustion gas in advance, the concentration of aromatic organic compounds that is affected by soot is low. As a result, the concentration of dioxins and furan, which are incomplete combustion products, is also decreased.
  • the boiler 4 is disposed on the downstream side of the combustion furnace 3, heat can be recovered from the combustion gas with high efficiency, so that a high-temperature and high-pressure boiler with a temperature of 300°C or higher and a pressure of 20 ata or higher can be provided. Also, high-temperature air can be recovered as necessary.
  • the boiler 4 is disposed on the downstream side of the combustion furnace 3 in the example shown in FIG. 1, the boiler 4 can be disposed within the combustion furnace 3.
  • a dust combustion furnace 15 is provided in the waste treatment system shown in FIG. 1 to burn the dust brushed off in the dust separator 2, and the brushed-off dust is burned at a temperature of 400 to 750°C with a gas containing oxygen, the concentration of unburned gas can be decreased to a certain value (for example, 6 wt%) or lower while the salt contained in the dust is fixed as it is. Also, since the gas generated at the time of combustion contains unburned gas, if the gas is introduced into the partial oxidation furnace 1 by means of a conduit pipe etc., the effective utilization of energy can be achieved.
  • FIG. 5 schematically shows another embodiment of a waste treatment system in accordance with the present invention.
  • a wet gas treatment apparatus 5 is provided between the dust separator 2 and the combustion furnace 3 in the system shown in FIG. 1.
  • the combustible gas is introduced into this wet gas treatment apparatus 5, where the concentration of a neutralizer such as caustic soda is changed, and the concentration of hydrogen chloride is reduced to 20 ppm or lower.
  • FIG. 6 schematically shows still another embodiment of a waste treatment system in accordance with the present invention.
  • the configuration of this system is the same as that of the system shown in FIG. 1, with the exception that a fluidized bed furnace 1 is used as the partial oxidization furnace.
  • Municipal refuse which is waste, was supplied, at a rate of 1 t/h, to the fluidized bed furnace 1 with a fluidized air temperature of 20 to 650°C and a sand layer temperature of 400 to 700°C, and was subjected to partial oxidation by controlling the air ratio in the range of 0.2 to 0.8, by which combustible gas was yielded.
  • the combustible gas was supplied to the dust separator 2 at a temperature of 250 to 800°C, and dust was removed by using a candle type ceramic filter.
  • the candle type ceramic filter is formed of SiO 2 , Al 2 O 3 , SiC, Cordurite, and a composite of these materials, or inorganic materials similar to these materials, and is of a ceramic fiber type or a porous type.
  • a gas that was obtained by recirculation of exhaust gas and has an oxygen concentration of 5% or lower and nitrogen gas were used.
  • the brushing-off pressure was set at 3 to 7 kg/cm 2
  • the brushing-off time interval was set at 5 seconds to 50 minutes
  • the brushing-off period of time was set at 0.1 to 20 seconds.
  • the dust concentration which had been 5 to 20 g/Nm 3 before the combustible gas had flowed into the dust separator 2, was decreased to 0.1 g/Nm 3 or lower.
  • the removed dust etc. were subjected to decharacterizing treatment in a melting furnace and an incinerator after being recovered.
  • the combustible gas was burned in the combustion furnace 3 so as to have a temperature of 900 to 1000°C.
  • heat could be recovered in the boiler 4 on the downstream side of the combustion furnace 3 by using steam with a temperature of 350 to 540°C and a pressure of 50 to 100 ata.
  • the boiler tube stainless steel, Inconel, and other ally steels were used, with the result that remarkable corrosion etc. were not found, and the corrosion resistance such that the boiler tube could be used for a plurality of years was confirmed depending on the material.
  • high-temperature air was recovered. As a result, it was found that high-temperature air with a temperature of 350 to 700°C could be recovered.
  • FIGS. 7A and 7B schematically show still another embodiment of a waste treatment system in accordance with the present invention.
  • FIG. 7A The configuration of the system shown in FIG. 7A is the same as that of the system shown in FIG. 1, with the exception that a grate furnace 1 is used as the partial oxidation furnace.
  • a boiler 3A is also provided within the combustion furnace 3 of the system shown in FIG. 7A.
  • Municipal refuse which is waste, was supplied to the grate furnace 1 with an oxidizing air temperature of 20 to 250°C and an upper part temperature of 500 to 800°C, and was subjected to partial oxidation by controlling the air ratio in the range of 0.3 to 0.9, by which combustible gas was yielded.
  • the combustible gas was supplied to the dust separator 2 at a temperature of 250 to 800°C, and dust was removed by using a candle type ceramic filter and a honeycomb type ceramic filter.
  • the ceramic filter is formed of SiO 2 , Al 2 O 3 , SiC, Cordurite, and a composite of these materials, or inorganic materials similar to these materials, and is of a ceramic fiber type or a porous type.
  • nitrogen gas was used to brush off dust in the dust separator 2.
  • the brushing-off pressure was set at 3 to 7 kg/cm 2
  • the brushing-off time interval was set at 10 seconds to 20 minutes
  • the brushing-off period of time was set at 0.05 to 15 seconds.
  • the dust concentration which had been 1 to 5 g/Nm 3 before the combustible gas had flowed into the dust separator 2, was decreased to 0.1 g/Nm 3 or lower.
  • the removed dust etc. were subjected to decharacterizing treatment in a melting furnace and an incinerator after being recovered.
  • the combustible gas was burned in the combustion furnace 3 so as to have a temperature of 900 to 1100°C.
  • the combustible gas was burned continuously by always placing an ignition source using a pilot burner (not shown) to avoid a danger of explosion etc.
  • the output of the burner was several ten thousand to several hundred thousand kilo-calories per hour, and natural gas or kerosene was used as a fuel for the burner.
  • FIG. 8 schematically shows still another embodiment of a waste treatment system in accordance with the present invention.
  • the configuration of this system is the same as that of the system shown in FIG. 5, with the exception that a fluidized bed furnace 1 is used as the partial oxidation furnace.
  • Municipal refuse which is waste, was supplied, at a rate of 1 t/h, to the fluidized bed furnace 1 with a fluidized air temperature of 20 to 650°C and a sand layer temperature of 400 to 700°C, and was subjected to partial oxidation by controlling the air ratio in the range of 0.2 to 0.8, by which combustible gas was yielded.
  • the combustible gas was supplied to the dust separator 2 at a temperature of 250 to 800°C, and dust was removed by using a candle type ceramic filter.
  • the candle type ceramic filter is formed of SiO 2 , Al 2 O 3 , SiC, Cordurite, and a composite of these materials, or inorganic materials similar to these materials, and is of a ceramic fiber type or a porous type.
  • a gas that was obtained by recirculation of exhaust gas and has an oxygen concentration of 5% or lower and nitrogen gas were used.
  • the brushing-off pressure was set at 3 to 7 kg/cm 2
  • the brushing-off time interval was set at 5 seconds to 50 minutes
  • the brushing-off period of time was set at 0.1 to 20 seconds.
  • the dust concentration which had been 5 to 20 g/Nm 3 before the combustible gas had flowed into the dust separator 2, was decreased to 0.1 g/Nm 3 or lower.
  • the removed dust etc. were subjected to decharacterizing treatment in a melting furnace and an incinerator after being recovered.
  • the combustible gas was introduced into the wet gas treatment apparatus 5, where the concentration of hydrogen chloride was reduced from 400 ppm, which had been the concentration before hydrogen chloride in the gas had been treated, to 20 ppm or lower.
  • the combustible gas in which the concentration of hydrogen chloride had been reduced was burned in the combustion furnace 3 so as to have a temperature of 900 to 1000°C.
  • heat could be recovered in the boiler 4 on the downstream side of the combustion furnace 3 by using steam with a temperature of 350 to 540°C and a pressure of 50 to 100 ata.
  • the boiler tube a stainless steel was used, with the result that remarkable corrosion etc. were not found, and the corrosion resistance such that the boiler tube could be used for a plurality of years was confirmed depending on the material.
  • high-temperature air was recovered. As a result, it was found that high-temperature air with a temperature of 350 to 700°C could be recovered.
  • FIGS. 9A and 9B schematically show still another embodiment of a waste treatment system in accordance with the present invention.
  • FIG. 9A The configuration of the system shown in FIG. 9A is the same as that of the system shown in FIG. 5, with the exception that a grate furnace 1 is used as the partial oxidation furnace.
  • a boiler 3A is also provided within the combustion furnace 3 of the system shown in FIG. 9A.
  • Municipal refuse which is waste, was supplied to the grate furnace 1 with an oxidizing air temperature of 20 to 250°C and an upper part temperature of 500 to 800°C, and was subjected to partial oxidation by controlling the air ratio in the range of 0.3 to 0.9, by which combustible gas was yielded.
  • the combustible gas was supplied to the dust separator 2 at a temperature of 250 to 800°C, and dust was removed by using a candle type ceramic filter and a honeycomb type ceramic filter.
  • the ceramic filter is formed of SiO 2 , Al 2 O 3 , SiC, Cordurite, and a composite of these materials, or inorganic materials similar to these materials, and is of a ceramic fiber type or a porous type.
  • nitrogen gas was used to brush off dust in the dust separator 2.
  • the brushing-off pressure was set at 3 to 7 kg/cm 2
  • the brushing-off time interval was set at 10 seconds to 20 minutes
  • the brushing-off period of time was set at 0.05 to 15 seconds.
  • the dust concentration which had been 1 to 5 g/Nm 3 before the combustible gas had flowed into the dust separator 2, was decreased to 0.1 g/Nm 3 or lower.
  • the removed dust etc. were subjected to decharacterizing treatment in a melting furnace and an incinerator after being recovered.
  • the combustible gas was introduced into the wet gas treatment apparatus 5, where the concentration of hydrogen chloride was reduced from 250 ppm, which had been the concentration before hydrogen chloride in the gas had been treated, to 20 ppm or lower.
  • the combustible gas in which the concentration of hydrogen chloride had been reduced was burned in the combustion furnace 3 so as to have a temperature of 900 to 1100°C.
  • the combustible gas was burned continuously by always placing an ignition source using a pilot burner (not shown) to avoid a danger of explosion etc.
  • the output of the burner was several ten thousand to several hundred thousand kilo-calories per hour, and natural gas or kerosene was used as a fuel for the burner.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Incineration Of Waste (AREA)
  • Gasification And Melting Of Waste (AREA)
EP00929845A 2000-05-24 2000-05-24 Procede et dispositif de traitement de dechets Withdrawn EP1284389A4 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/JP2000/003306 WO2001090645A1 (fr) 2000-05-24 2000-05-24 Procede et dispositif de traitement de dechets

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Publication Number Publication Date
EP1284389A1 true EP1284389A1 (fr) 2003-02-19
EP1284389A4 EP1284389A4 (fr) 2005-03-16

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EP (1) EP1284389A4 (fr)
KR (1) KR100447009B1 (fr)
WO (1) WO2001090645A1 (fr)

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WO2006123018A1 (fr) * 2005-05-18 2006-11-23 Foster Wheeler Energia Oy Procede et appareil pour la gazeification de materiaux carbones
EP1816396A1 (fr) * 2004-11-26 2007-08-08 Nippon Steel Engineering Co., Ltd Procede de traitement et appareil de traitement pour gaz combustible dans un four de fusion de dechets
CN102200284A (zh) * 2011-05-04 2011-09-28 绍兴市德华制氧技术研究所 一种环保型垃圾燃烧装置及其处理工艺
CN103104922A (zh) * 2013-02-06 2013-05-15 西安宇清环境工程科技有限责任公司 一种垃圾焚烧烟气余热回收装置

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KR101420167B1 (ko) * 2014-03-18 2014-08-13 엔솔 주식회사 오염방지장치가 구비된 친환경적 폐탄약 밀폐기폭처리장치 및 그 방법
CN107044648A (zh) * 2016-11-30 2017-08-15 刘剑 秸秆快速环保处理方法及装置
CN107044644A (zh) * 2016-11-30 2017-08-15 刘剑 秸秆环保处理装置

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CN102200284B (zh) * 2011-05-04 2012-10-10 绍兴市德华制氧技术研究所 一种环保型垃圾燃烧装置及其处理工艺
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