WO1997032161A1 - Procede et appareil de production de vapeur surchauffee utilisant la chaleur generee par l'incineration de dechets - Google Patents
Procede et appareil de production de vapeur surchauffee utilisant la chaleur generee par l'incineration de dechets Download PDFInfo
- Publication number
- WO1997032161A1 WO1997032161A1 PCT/JP1997/000573 JP9700573W WO9732161A1 WO 1997032161 A1 WO1997032161 A1 WO 1997032161A1 JP 9700573 W JP9700573 W JP 9700573W WO 9732161 A1 WO9732161 A1 WO 9732161A1
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- WIPO (PCT)
- Prior art keywords
- pyrolysis
- combustion
- waste
- heat
- char
- Prior art date
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G1/00—Steam superheating characterised by heating method
- F22G1/16—Steam superheating characterised by heating method by using a separate heat source independent from heat supply of the steam boiler, e.g. by electricity, by auxiliary combustion of fuel oil
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- 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
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- 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
- F22B31/04—Heat supply by installation of two or more combustion apparatus, e.g. of separate combustion apparatus for the boiler and the superheater respectively
- F22B31/045—Steam generators specially adapted for burning refuse
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- 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
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- 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
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- 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
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- 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
- F23G2201/304—Burning pyrosolids
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/12—Heat utilisation in combustion or incineration of waste
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S423/00—Chemistry of inorganic compounds
- Y10S423/18—Treating trash or garbage
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S588/00—Hazardous or toxic waste destruction or containment
- Y10S588/90—Apparatus
Definitions
- the wood invention refers to an invention in which municipal waste and industrial waste vegetables are incinerated, steam is produced by the heat of the combustion exhaust gas, and for example, superheated steam is produced using the steam for a power generation plant. Furthermore, the present invention relates to an invention in which incinerated ash is melted by utilizing its heat and turned into resources.
- fluidized bed incinerators have often been used for incinerators to incinerate waste such as municipal solid waste, and kagaru units are sand contained on dispersion plates (for example, perforated plates) in fluidized bed incinerators.
- dispersion plates for example, perforated plates
- waste such as municipal waste is injected into the fluidized bed thus formed.
- the combustion gas generated by this combustion is returned to the boiler via a combustion gas output line, and in the boiler, steam is raised by thermal contact with 7K, and the steam is used as a turbine drive source for a power generation plant or the like. Things.
- the waste such as municipal solid waste contains chlorinated organic compounds such as PVC and is contained in combustibles at about 0.2 to 0.5% as C1. Chlorine contained in PVC and other materials mixed into municipal solid waste is converted to HC1 by combustion. (Usually, HC1 of municipal solid waste combustion exhaust gas width is about 500 to 1 OOO.) ppm), which acts on and corrodes the tubes of the steam boiler installed downstream of the incinerator. In particular, when the tube surface temperature is about 350 ° C or more, high corrosion becomes remarkable as the temperature increases.
- the tube surface temperature had to be kept at 350 ° C or lower, and the temperature of the produced steam was limited to about 300 ° C.
- the efficiency of conventional waste incineration is less than about 15%, and the boiler tube temperature can be raised to 500 to 600 ° C using fuel such as LNG, which contains almost no chlorine. It is significantly lower than the power efficiency of the plant, which is about 40%.
- the present invention has been made in view of the above technical problems, and it is an object of the present invention to provide a method and apparatus for producing superheated steam capable of efficiently obtaining high-temperature and high-pressure superheated steam while preventing boiler tubes from being corroded by chlorine. is there.
- Another object of the present invention is to provide a superheated steam capable of efficiently reducing chlorine and obtaining a superheated steam at a high temperature without using expensive high-grade materials as a boiler tube.
- the pyrolysis-thermal decomposition in the T 'stage is efficiently performed while preventing tar adhesion and coking of the pyrolysis gas, reducing dioxin, and reducing NOX. It is an object of the present invention to provide a superheated steam production device capable of efficiently obtaining a superheated steam having a high temperature and a high temperature while reducing chlorine.
- Another object of the present invention is to provide an apparatus for producing superheated steam that enables the steam to be produced stably over a long period of time and that further improves the efficiency m of the pyrolysis gas.
- Another object of the present invention is to provide an apparatus for producing a superheated steam that can produce an aggregate or the like by melting ash obtained by separating the pyrolysis gas or the combustion gas. . Configuration>
- the present invention uses boiler water pressurized so as to have a boiling point of approximately 200 ° to 320 °°, and heating the boiler water in at least two stages. Of multiple stages,
- the heating up to the substantially boiling point temperature is performed with chlorine-containing heat energy
- the method is characterized in that superheating for obtaining superheated steam at a predetermined temperature from the above-mentioned approximate boiling point is performed by using dechlorination heat energy containing no chlorine.
- the boiling point of the boiler water is set to about 200 T: to about 320 ° C. by pressurization, the application of thermal energy to the boiler water by the chlorine-containing pyrolysis gas varies. However, it can be used to absorb the latent heat of the boiler water (in other words, it is used only for the phase conversion from fc to steam and does not act as a rise), so the boiler water heat exchange tube The boiler water or steam with a stable heating temperature can be obtained without the surface temperature of the boiler rising above the chlorine corrosion temperature.
- the heating with the chlorine-containing heat energy is performed by a pyrolysis unit obtained by a pyrolysis unit that supplies waste into a space containing a fluid medium of about 300 ° C. or more to perform a pyrolysis reaction. Heating is performed using the combustion heat energy of the gas, and the heating with the dechlorination heat energy is performed by flowing a mixture of undecomposed residue and flowing sand extracted by the pyrolysis means with air. The thermal energy obtained by the char-combustion hand-killing of burning the undecomposed residue while heating is performed.
- a waste is supplied into a space having a temperature of 30 (TC or higher, preferably, a temperature of 350 to 500 ° C., and a thermal decomposition reaction is performed. Separation of the pyrolysis gas generated by the reaction, the undecomposed residue and the char mixture consisting of the fluidized medium and the incombustibles from each other, for example, pyrolysis using a fluidized bed, one-way kiln, or a mixing tank Means,
- a non-decomposed residue removed by the pyrolysis means and a mixture of medium and a medium composed of a medium are re-flowed by air to burn the un-decomposed residue.
- second steam producing means for converting hot water or steam produced by the first steam producing means into superheated steam by the heat of the combustion gas obtained by the charcoal condensation means. It is.
- the steam heated in the first or second steam production stage or the hot water or steam that is guided to any one of the above means for observation is placed on the high temperature side of the char-combustion means. It is better to introduce it appropriately to the arranged heat exchange means.
- An exchange means is preferably provided.
- a heat medium 7 such as heat exchange hand killing is provided in the fluid medium path block for returning the heated fluid medium to the pyrolysis means, which has been heated by the J-fuel Jft. It is better to interpose a second char combustion means.
- the present invention provides a method for effectively removing non-combustible substances from the pyrolysis means and the char-combustion step.
- a first method for separating the large-sized waste 3 from other wastes by taking out the discharged wastes of the pyrolysis means, and feeding the other wastes to the bottom side of the combustion means. Filter means;
- the discharge discharged from the non-removal outlet of the means is regarded as small incombustible. »Second filter means for separating the J medium and feeding the flowing medium to the combustion chamber 3 ⁇ 4 side;
- a third filter means for separating ash and feeding the fluid medium after the ash separation to the bottom of the purifying means
- the first filter means needs to have a mesh size larger than at least the second filter means.
- the first filter means is 5 mm depending on the size of the waste to be charged.
- the second filter means is set to about 2 mm, which is larger than the maximum diameter of the fluid medium (about 1.0 mm).
- the third filter means is preferably set to about 0.1 mm which is smaller than the minimum value of the flow book (about 0.2 mm).
- a vibrating sieve can be supplied to the front filter stage.
- the mixture of tea separated by the pyrolysis means is substantially free of ⁇ by means of a sword, it is used as a superheat source for the second steam production means. Even if it is configured to obtain superheated steam of ° C or higher, high-temperature corrosion of equipment does not occur.
- the combustion exhaust gas of the pyrolysis gas containing chlorine is used as the heating source for the steam production-final stage of ⁇ 1, but the heat is used to reduce the temperature to about 400 "C or less. 0 0 to 3 2 (Because it manufactures hot water or steam below TC, it heats only below the temperature of hot corrosion, so there is no danger of boiler tube corrosion, and expensive expensive materials are used. No need to use.
- the steam heated by the first or second steam producing means or a part of the hot water or steam introduced into the laser producing means is used in the step (1): It may be appropriate to introduce it to the heat exchange means arranged on the side (hereinafter referred to as the first heat exchange means). That is, the char combustion means burns the undecomposed residue while flowing the char mixture by air, so that the combustion gas block is at a high temperature, specifically, at 700 ° C. to 950 ° C. Become.
- the hot gas is used to heat the steam heated by the first or second steam producing means or the hot water introduced into any of the producing means (heat exchange with a part of the steam).
- hot water introduced into the first steam producing means may be introduced into the heat exchanging means to raise the temperature to a certain extent, and hot water or steam introduced into the second steam producing means may be used.
- the amount of heating of the second steam production means can be increased, and a large amount of superheated steam can be obtained.
- the superheated steam heated by the second steam production means is used as the pre-heat exchange means because it is heated to 800 to 950 ° C. in the high temperature range of the above-mentioned char burning means.
- a superheated steam of, for example, 400-520 ° C. which is further heated, and it is possible to obtain a superheated steam which is sufficiently heated.
- the provision of heat exchange means on the high-temperature area side of the above-mentioned char combustion means means that the high-temperature area side, which has become unnecessarily high at 950 to 130 ° C., is passed through the output line as it is.
- the refractory material does not have a temperature, it is 800 to 95 (by dropping it to TC, it is possible to use a normal refractory line. As mentioned above, 800 to 95 (Even if it is dropped to TC, there is no hindrance in maintaining the steam temperature in the second steam production stage-400 to 500 "C.
- the present invention utilizes the high-temperature fluidized medium, and interposes a second charged medium in the circulation of the fluidized medium that has been heated in the above-mentioned char-combustion stage.
- the heat exchange means provided on the first or second steam producing means side is preferably disposed in the combustion medium of the means.
- the heat exchangers installed in the first steam production stage, the second steam production stage, etc. are arranged in series and parallel to increase the temperature by multi-step heating. This makes it possible to obtain a superheated steam that is sufficiently heated, and the fluid medium has a large heat capacity and a stable high temperature can be obtained by its thermal contact.
- the fluid medium in the T 'stage circulates between the pyrolysis stage
- the temperature of the fluidized medium of the char combustion means is approximately 700 to 800 "C, while the temperature of the fluidized medium of the pyrolysis means is 350 to 500 ° C, and the heat drop between the two Therefore, when the fluid medium of the combustion means is directly introduced into the pyrolysis means, there is a possibility that the heat decomposition temperature in the pyrolysis means is locally increased and the heat fluctuation occurs. Therefore, the adjustment of the amount of the fluid medium returned is complicated.
- the present invention provides a second chamber provided with a means for reducing heat exchange-stage heat, etc., in a path of the medium flowing through the fluid medium heated by the chamber combustion means to the thermal decomposition means. ⁇ It's better to let them go through the potato stage.
- the fluid medium heated to 700 to 850 C by the second char combustion means for example, by the first char combustion means, is heated by the heat exchange means by the second char combustion means.
- the temperature of the fluid medium dropped to 500 to 700 CTC by the heat deprived can be returned to the pyrolysis means because the fluid medium dropped to 500 to 700 ° C.
- the thermal decomposition temperature in the thermal decomposition stage is controlled from 35 (TC to 50 (TC around the TC) and the uj ability is stably controlled.
- thermal decomposition means The large-sized non-combustible materials are separated from the discharged materials from the outlet by the first filter means, and only the large-sized non-combustible materials are discharged.
- the material is to be fed to the bottom of the combustion means and used for combustion.
- the waste discharged from the noncombustible material outlet is regarded as small incombustible substance. It is only necessary to separate the fluid medium by the second filter means, and the fluid medium separated by this is fed to the bottom of the stage. Becomes possible.
- the third filter stage is not always necessary, the second filter Only the ash is discharged to the outside while supplementing the liquid sand that has not been caught by the step, which facilitates efficient ash removal and collection of the liquid sand.
- a mixture of undissolved m and the fluid medium flows from the pyrolysis stage side to the rich combustion means side, and a high temperature flows from the first combustion hand-stage side to the pyrolysis means side. Are sent (returned).
- the temperature on the side of the pyrolysis stage is 350 to 50 (TC, while the temperature on the side of the char-combustion means is 700 to 850, so that the temperature difference
- TC temperature on the side of the char-combustion means
- the temperature difference When a fluid medium with a large amount of heat circulates from one side to the other, the temperature fluctuates in each fluidized tank due to the fluctuation of the circulation amount, and the thermal decomposition power on the thermal decomposition killing side.
- the combustion means on the side of the Aya-chamber does not completely burn.
- the boiler water is heated to approximately the boiling point by the pyrolysis of 3 "'salt.
- the thermal energy of the pyrolysis gas obtained in the pyrolysis stage is used in order to perform the superheating to obtain the superheated steam of a predetermined temperature from the above-mentioned boiling point temperature by the dechlorination heat energy obtained by the char combustion means. It is necessary to set the calorie ratio of the heat energy of dechlorination obtained by the combustion means to be about 7: 3 for practical purposes. Les, fluid medium etc. such to maintain the reflux Then the force opening Li ratio.
- a char-passage connecting the thermal decomposition means and the char-combustion means, or a means for preventing backflow of the char or 'J medium is provided on the side of the pyrolysis means and / or the char-combustion means. are doing.
- Such a backflow prevention means may be constituted by a pressure stage: forming stage, or may be constituted by a target conveying means.
- the backflow prevention means is a force difference forming means provided on at least one side of the first combustion stage for returning the fluid medium to the pyrolysis means. It is more preferable to form a pressure difference larger than the pressure difference (PP 2 ) between the pressure P on the pyrolysis means side and the pressure P 2 of the char combustion means.
- the backflow prevention means is constituted by mechanical conveyance means for forcibly conveying the char to the pyrolysis means side or the char combustion means side, preferably from the entrance side of the mechanical conveyance means. It is good to arrange it with the difference of ffi force 11 by inclining upward toward the output 1 side.
- the present invention particularly provides a flow medium path for returning the fluid medium heated by the first combustion stage to the re-pyrolysis means in a fluid medium path, and a means for alleviating heat exchange heat or the like to reduce heat. It is preferable to provide a heat exchange means in the char combustion means, and to provide the above-mentioned backflow prevention means at the outlet of the heat exchange stage.
- the backflow preventing means for preventing the backflow of the flow medium or the flow medium is disposed between the pyrolysis means and the combustion means, the flow having the temperature difference and the large heat capacity is provided. It is possible to prevent a temperature fluctuation, a thermal decomposition, a deterioration of a combustion strip, and the like in the two fluidized tanks caused by the medium and the like without erroneously flowing back between the two fluidized tanks.
- the thermal action of the pyrolysis-stage and the char-combustion stage and the stage-side fluid flow are performed smoothly, respectively, and the thermal energy of the pyrolysis gas obtained by the pyrolysis means and the char-
- Pressure difference ( ⁇ ⁇ ⁇ ⁇ ⁇ ) formation stage which forms a large difference (( ⁇ ,- ⁇ 2 ) between the pressure P t on the pyrolysis means side and the H; force I ⁇ of the char combustion stage Pressure on the pyrolysis means side!
- the pressure of the combustion stage can be automatically adjusted to the set pressure lid ( ⁇ ⁇ ⁇ ⁇ ) when the power exceeds ⁇ 2 units //. +11 Contrary to the combustion means side and the pyrolysis furnace side ⁇ : Force difference is roughly set. J. Force difference ( ⁇ ⁇ .p) can be maintained, which is preferable.
- the invention also specifically specifies the char combustion means.
- air flow the air supplied from below the dispersion plate (hereinafter referred to as air flow) is divided into two parts, or the inside of the fluidized bed is partitioned by an il J plate.
- a fluid tank formed with a circulating means for circulating and flowing the char mixture in the fluidized bed; and a pyrolysis means power supplied to the lower part of the circulating fluid area or the lower part of the upstream area. I have been established for the supply of
- the circulating means may be divided into a plurality of parts so that the inside of the fluidized bed can be circulated, and the circulating means is supplied from below the dispersing plate.
- the plurality of air streams may be used to control the flow rate of the char mixture in the fluidized bed so that the mixture can be circulated.
- ⁇ is as follows.
- the above-mentioned effect is further increased because the floats on the front of the fluidized bed are moved to the bottom of the fluidized bed by the downstream flow.
- the air in the outlet line This prevents the temperature from dropping and prevents the temperature from rising excessively, preventing tar adhesion and caulking, thus enabling stable operation.
- the pyrolysis gas after the primary combustion is further introduced into the pyrolysis gas to burn the pyrolysis gas in a reduced state, thereby reducing the temperature to 0x.
- the wood invention narrows the passage area between the two spaces, promotes mixing with air, and reverses the radiant heat. It has an ih function.
- the thermal decomposition means is constituted by a fluidized bed
- the fluidized bed is mainly fluidized by blowing air or combustion exhaust gas from below the dispersion plate containing a fluidized fluid medium.
- the lower side wall of the main fluidized bed may be widened, and a conveying means may be provided at the bottom for conveying solids from the waste input side to the char-mixture extraction side.
- the transporting means functions as a sub-pyrolyzing section, in which thermal decomposition is performed while forcibly transporting non- ⁇ in the direction of the remaining charcoal. It is possible to prevent frustration from remaining, and to substantially completely decompose and gasify and remove chlorine in waste.
- the flow length of the fluidized bed is improved by the partition plate provided in the fluidized bed. Therefore, the waste mixture is mixed with the waste medium and the medium is discharged. The effluent does not blow through to the extraction of the tea mixture 1.1, so the pyrolysis is uniformly performed for more than a predetermined time. Will be retained.
- the power S ′ for performing the thermal decomposition uniformly and sufficiently, and the power i ′ for substantially completely decomposing and gasifying and removing the chlorine in the waste bubble can be obtained.
- the invention provides a method in which between the pyrolysis means and the first steam production means, the primary combustion fuel of the pyrolysis gas removes the heat from the first combustion stage or the fifth heat stage, respectively. It is preferable to provide ash fusion separation means for performing melt separation of ash separated from the above gas, and preferably to provide secondary combustion means for performing secondary combustion of the pyrolysis gas from which the ash has been separated.
- the molten ash can be used to produce aggregate and the like.
- водородн ⁇ е кар ⁇ е кактрол ⁇ ество is performed using pyrolysis gas, and a first steam production stage such as a boiler is disposed in the secondary combustion means, so that secondary heating of boiler water can be performed more efficiently. is there.
- the ash contained in the pyrolysis gas width and the ash contained in the combustion gas are converted into waste. However, it is not necessary to use all of the pyrolysis gas supplied to melt it. Rather, it becomes excessive heat energy.
- the pyrolysis gas obtained by the pyrolysis means be configured to be partly branched and supplied to the secondary combustion means together with the ash melt separation means.
- the present invention preferably provides a pyrolysis reaction by supplying waste to an oxygen-poor space having a temperature of 30 (TC or more) and subjecting the pyrolysis gas generated by the reaction to secondary combustion means or heat.
- a throttle section is provided in the path width, and an air flow through which a small amount of air flows appropriately to the pressure outlets provided respectively on the artificial side and the outlet side of the throttle section.
- An entry means is preferably provided.
- the flow rate of the pyrolysis gas required for melting the ash is measured and, in order to control the pyrolysis gas, a differential pressure gauge such as an orifice is provided in the path of the pyrolysis gas. It is necessary to measure the flow rate (flow velocity).
- a differential pressure gauge such as an orifice in the outlet path from the pyrolysis means, and to measure the flow rate. Since the mouth temperature is around 350 to 500 "C, gas containing tar may come out, and the tar may be confined to the throttle or pressure tap (porous ⁇ Mouth), making smooth flow measurement difficult.
- the air is used as an air-suspension gas containing a supporting gas.
- a portion of the pyrolysis gas obtained in the pyrolysis stage be branched and supplied to the inlet side of the pyrolysis rare.
- the thermal decomposition means is not limited to a fluidized bed only, and is a mechanical transport Z for transporting solids in the thermal decomposition means from the waste input side to the char-mixture removal side.
- a pyrolysis furnace having a stirring function may be used.
- the thermal decomposition means is configured not as a fluidized bed but as the mechanical transport stirring means described above, the thermal decomposition time and the amount of thermal decomposition can be secured on a regular and regular basis as compared with a fluidized bed. And stable pyrolysis can be performed.
- the pyrolysis gas is not released because the fluidizing gas required in the fluidized bed (N 2 as Byeon, an inert gas mainly composed of CO ⁇ H 20 ) is unnecessary. Therefore, it has a high calorific value per unit volume, and can easily generate a high temperature of more than 130 ° C by air or oxygen-enriched gas, as described later for melting ash in gas. It can be used effectively as an energy source.
- N 2 as Byeon, an inert gas mainly composed of CO ⁇ H 20
- the gas is discharged from the char combustion means in a state containing ash, it is preferable that the gas is separated by a cyclone or the like and then introduced into a steam production stage such as a superheater / boiler.
- the ash separated from the gas is melted and granulated, so that the use of aggregate and the like becomes acceptable.
- a pyrolysis gas which is generally a flammable gas, is / ⁇
- the ash contained in the pyrolysis gas and the ash contained in the combustion gas is about 10% of the waste, so it is not always necessary to melt it using all the pyrolysis gas supplied. No, it is rather easy to generate excess heat energy.
- the amount of oxygen-enriched air required to burn all the pyrolysis gas at a high temperature until the ash can be melted increases.
- the thermal decomposition means is to extract only chlorine from waste such as municipal waste. Since the dechlorinated char mixture can be supplied to the char combustion means, there is no need to raise the temperature in particular, and a sufficient force at a temperature of about 250 to 450 ° C.
- ash melting In order to melt the ash, the furnace must be set to a temperature of around 130 ° C. Therefore, the pyrolysis gas used in the ash melting furnace has a higher temperature, in practice 450 to 7 It is preferable to thermally decompose at a temperature around 0 CTC and to actively generate pyrolysis gas instead of simply dechlorinating.
- the present invention provides the above-mentioned pyrolysis means, which comprises a plurality of pyrolysis furnaces appropriately combining a fluidized bed or a mechanical stirrer, and sets the pyrolysis temperature of one pyrolysis furnace to that of another pyrolysis furnace. It may be configured differently for 'decomposition'.
- the temperature is set to about 250 to 45 (TC) to actively produce a dechlorinated char mixture, while the other pyrolysis furnace on the high-temperature side
- the temperature may be set to about 450 to 70 (TC), for example, to generate a pyrolysis gas used in an ash melting furnace.
- the pyrolysis gas generated by the pyrolysis furnace on the high-temperature side is subjected to melting and separation of ash separated from the respective gases extracted by the char-combustion stage or the pyrolysis means.
- Ash melt-separation configured to be fed to a stage.
- the function of the pyrolysis gas is separated, and in one pyrolysis furnace, it is possible to actively produce a dechlorinated tea mixture.
- the pyrolysis gas to be used in the furnace can be generated, and this functional separation makes it possible to generate a more effective and effective char-mixture and to generate the pyrolysis gas.
- FIG. 1 is a system diagram showing a superheated steam production apparatus utilizing waste incineration heat according to a first embodiment of the present invention, in which a subcharging combustion furnace is provided between a cha-fe furnace and a pyrolysis furnace. I have.
- FIG. 2 is a system diagram showing a superheated steam production apparatus utilizing waste heat of incineration according to a second embodiment of the present invention, in which a subcharging combustion furnace is provided independently.
- FIG. 3 shows the procedure for producing superheated steam using the heat of incineration of waste related to this configuration of the present sword.
- FIG. 4 is a system diagram showing an apparatus for producing a superheated steam using waste incineration heat according to a third embodiment of the present invention.
- Finoleta power is attached to each take-out line.
- FIG. 5 is a system diagram showing an apparatus for producing superheated steam using waste incineration heat according to a fourth embodiment of the present invention, in which the sub-charging combustion furnace shown in FIG. It is divided into backflow prevention I means.
- Fig. 6 is a system diagram showing a superheated steam production system using the heat of waste incineration according to the fifth embodiment of the present invention. It is configured as possible.
- FIG. 7 is a schematic diagram in which the backflow prevention means is constituted by mechanical transport means for forcibly transporting the channel from the pyrolysis means side to the char-combustion means side.
- Fig. 8 shows the char-combustion means, sub-char-combustion means and pyrolysis furnace applied to Fig. 5,
- (A) is a plan view
- (B) is a plan view
- FIG. 9 shows the configuration of a fluidized bed obtained by improving the char-firing furnace suitable for each of the above embodiments, (A) is a front view, (B) is a side view, and (C) is an instep figure. is there.
- FIGS. 10A and 10B are three views showing the internal structure of a pyrolysis furnace according to a modification of the pyrolysis furnace suitable for each of the above-described embodiments, where (A) is a metaphysical
- FIG. 11 relates to another improvement of the pyrolysis furnace in which the pyrolysis gas combustion furnace including the combustion ducts shown in each of the above-mentioned embodiments is suspended, and (A) shows the results of the pyrolysis furnace of FIG. ⁇ E duct viewed from the side Figure, (beta) modification of the diaphragm portion, (C) is a positive ⁇ u
- FIG. 12 is a system diagram showing an apparatus for producing a superheated steam using waste incineration heat according to a sixth embodiment of the present invention.
- the apparatus shown in FIG. And a ash melting furnace is provided.
- Fig. 13 is a system diagram showing a superheated steam production system using the heat of waste incineration according to the seventh embodiment of the present invention.
- a part of the pyrolysis gas is branched.
- the gas is supplied to a pyrolysis gas combustion furnace.
- Fig. 14 shows the differential pressure measuring means provided in the pyrolysis gas outlet line shown in Fig. 13.
- (A) uses an orifice, a differential pressure measuring means formed by using an orifice, and
- (B) uses a flap-shaped throttle. This is a differential pressure measuring means formed by:
- FIG. 15 is a system diagram showing an apparatus for producing superheated steam using the heat of waste incineration according to the eighth embodiment of the present invention, wherein the-part of the pyrolysis gas obtained by the pyrolysis furnace is ashed. It is configured to circulate to the lower part of the pyrolysis furnace through a branch line on the upstream side of the melting furnace.
- FIG. 16 is a system diagram showing a superheated steam production apparatus utilizing waste incineration heat according to a ninth embodiment of the present invention, in which a pyrolysis furnace is constituted not by a fluidized bed but by mechanical transfer stirring means. ing.
- FIG. 17 is a system diagram showing a superheated steam production apparatus using the heat of waste incineration according to the tenth embodiment of the present invention, which is constituted by a plurality of pyrolysis furnaces.
- FIG. 18 shows a system ⁇ showing a modified example of the superheated steam production apparatus utilizing the heat of incineration of waste according to the first embodiment, in which pyrolysis is performed by a fluidized bed and a mechanical conveying means. Reconfigured.
- Fig. 1 shows a superheated steam production apparatus utilizing the heat of waste incineration according to the first embodiment of the wood invention.
- reference numeral 1 denotes a pyrolysis furnace comprising a fluidized bed, and a dispersion plate such as a perforated plate.
- Fluid medium 2-1 such as flowing sand is stored on the top, and waste supply line 4 Waste such as municipal solid waste is supplied from the sand ring (return) line 5.
- gas inlet 1-1 line 6 (Wood pyrolysis furnace (3 ⁇ 4When wood is not combustion, it is pyrolysis, so the supplied gas is combustion gas that consumes oxygen.)
- air is introduced as needed to control the temperature) to create a fluidized bed space at a temperature of 300 ° C or more, and to carry out the thermal decomposition reaction of waste,
- the pyrolysis gas generated by the reaction is supplied to the pyrolysis gas output line 7 through the pyrolysis gas output line 7, which is composed of unreacted azalea and fluid sand.
- the fuel mixture is separated and taken out from the char mixture take-out line 9 and the non- ⁇ is taken out from the non-combustible material take-out line 8, respectively.
- the pyrolysis gas outlet line 7 on the outlet side of pyrolysis furnace 1 is provided with an air inlet line 21 and the pyrolysis gas extracted from pyrolysis furnace 1 is empty 51 population line 21. If necessary, it is possible to prevent tar adhesion and coking prevention
- a pyrolysis gas incinerator 34 composed of a combustion duct is provided, and from the line 2 ⁇ , the pyrolysis gas is supplied to the pyrolysis gas by Perform complete combustion.
- Reference numeral 10 denotes a char-burning furnace composed of a bubble furnace and a bottom furnace.
- the char-mixture is supplied to the dispersing plate 11 disposed at the bottom of the charcoal-combustion line 9 and the char-mixture supplied from the bottom, and the ⁇ -ring line 19-2 /
- the liquid sand circulated through the subcharging furnace 10B via 19-1 is stored.
- air is supplied from the air supply line 12 below the dispersion plate 11 and heated to 650 to 800 ° C in the fluidized bed 2-3 to burn the undecomposed residue, and further, the fuel is burned in a 10-width region.
- Air is introduced from the air supply line 13 and completely burns, producing fuel gas at about 800 to 1300 ° C, and a second superheater 29-1 in the I-.
- ifi 2 steam production-stage first superheater 20
- superheated superheated steam introduced via line 28-1 together with unnecessarily high combustion around 950-1300 ° C Drop gas to 800-950 ° C.
- the combustion gas temperature is 800 to 95 There is no hindrance in maintaining the steam temperature in the tank 20 at 200-32 O'C. Small incombustibles that are not burned in the char combustion furnace 10 are taken out from the non- ⁇ taking-out line 14.
- the auxiliary combustion furnace 10 is provided with an auxiliary fluid combustion furnace 10 as a sub-fluidized bed in the auxiliary combustion furnace 10, and as shown in FIGS. 1 and 2, a sand circulation line 19-1 2Z19-1 is provided.
- the third superheater 29-2 is arranged in the fluid medium 2-2 of the sub-charging furnace 10 # so as to move with the sand force between the sub-charging combustion furnace 10 # and the second superheater 29-2. Connected to the outlet [:] side of superheater 29-1 via line 28-2.
- the auxiliary charging furnace 10 ⁇ may be provided independently, but as shown in FIG.
- the fluid medium reheated by the charging furnace 10 is supplied to the pyrolysis furnace 1. It is preferable to interpose a sub-charging fiber furnace 10 provided with a ⁇ 3 superheater 29-2 ⁇ in the fluid medium path 191-1-5 returning to the reactor.
- the combustion gas heat-exchanged by the second superheater 29-1 is supplied to the combustion gas outlet line 15 as needed.
- the pyrolysis gas taken from the pyrolysis gas outlet line 7 is a water-cooled boiler 36 power ⁇ inside the built-in pyrolysis gas furnace 34
- the boiler water is also introduced into the water-cooled boiler 36 in the combustion gas combustion furnace 34 via the branch line 26 ', and supplies steam or heated water to the first superheater 20 via the branch line 27'.
- the boiler water C is set around the water-cooled 3 ⁇ 4 boiler 36, 36-2 and the first boiler 24
- the first stage of heating is performed, and the amount is controlled so that the heating temperature is about 309 ° C., which is near the boiling point.
- the tube plastic surface temperature of the water-cooled wall boiler 36 and the first boiler 24 can be maintained at 350 or less following the heated water. Or corrosion does not occur even if it contains HC1.
- the steam / heated water extracted from the outlet line 27 of the first boiler 24 and the steam heated by the water boiler 36 and extracted through the branch steam line 27 ′ Z heating water is injected into the furnace and heated by the combustion gas supplied through the combustion gas line 17 to produce superheated steam, and the steam outlet line 28 1 1 and the second superheater 29 1 Further, the superheated steam superheated to 400 ° C. to 52 ° C. is taken out from the line 282-2 to the third superheater 29-2 in series, respectively, and taken out.
- the waste such as municipal solid waste supplied to the pyrolysis furnace 1 contains chlorine-containing organic compounds such as PVC.
- the combustible width is about 0.2 to 0.5 ° / C1. It is contained.
- municipal solid waste is supplied from the waste supply line 4 and high-temperature circulating fluidized sand is supplied to the pyrolysis furnace 1 from the fluidized sand circulation line 5, and the air in the tank or the combustion gas is supplied to the combustion exhaust gas from the population line 6.
- the temperature was raised to 350 to 50 (by ⁇ tiffl in TC, From the 9 delivery lines, a raw undecomposed residue containing substantially no element is obtained.
- the chlorine contained in the waste is substantially contained in the pyrolysis gas and is discharged to the pyrolysis gas output line 7.
- the large-sized waste separated by the thermal decomposition reaction in the thermal decomposition furnace 1 is taken out of the furnace through a non-takeout line 8.
- the pyrolysis time and the pyrolysis temperature are set so that the thermal calorie ratio of the pyrolysis gas and the char mixture becomes about 7: 3.
- the pyrolysis gas extracted from the pyrolysis gas outlet line 7 of the pyrolysis furnace 1 includes: Power containing gas, oil, tar and HC 1 Outlet line 7 Upstream air Inlet line 21 Partial combustion with a small amount of air supplied from 1 prevents the temperature from dropping in the P direction, and outlet line 7 In addition to preventing tar adhesion and coking in the furnace, air is further introduced into the pyrolysis-gas baking furnace 34 from the line 2 and complete combustion is performed in the pyrolysis gas baking furnace 34.
- the pyrolysis gas was introduced into the water-cooled wall boilers 36, 36-2 and the second boiler 24 to have a boiling point of 200 to 320. Steam to start up to near ° C Can produce a large amount of boiler water.
- the pyrolysis gas combustion exhaust gas that has exchanged heat with the water-cooled wall boiler 36 in the pyrolysis gas combustion furnace 34 flows from the first boiler gas inlet 23 together with the combustion exhaust gas from the first superheater gas outlet line 22. Supply to the first boiler 24.
- the gas introduced into the pyrolysis combustion furnace 34 and the first boiler 24 contains HC1 at about 500 to 100 ppm, water flow is controlled by adjusting the flow rate of the boiler water.
- the tube temperature of the plastic boiler 36 and the first boiler 24 is about 35 (TC or less, which is the same level as that of the conventional one, and high corrosion is suppressed. For this reason, the water-cooled plastic boilers 36, 36
- the first boiler 24 cannot generate high-temperature superheated steam. Since it can be heated to about 300 to 320 "C, it can be further heated by the superheaters 29-1, 1, and 2 after the first superheater 20. By heating at 9-12, it is possible to obtain high-temperature superheated steam of about 500-700 "C.
- the tea mixture removal line in the pyrolysis furnace 1 9 One mixture is composed of fluidized sand and undecomposed residue, and a substantially chlorine-free char mixture is supplied to the lower part of the combustion furnace 10 in the char-combustion furnace 10, and the gas supply line 1
- the fuel is heated by air supplied from the dispersing plate 11 through the dispersing plate 11.
- the amount of air supplied from the air supply line 12 is adjusted so that the fluidized sand flows and the undecomposed residue is removed. In some cases, more air may be supplied from the air supply lines 13 and 19-13 for complete combustion.
- the temperature of the flaming furnace 10 rises due to the combustion and exothermic reaction.
- the temperature may be as high as about 100 "to about 1200" C.
- the second superheater 29-1 exchanges heat with the superheated steam of the first superheater 20 through line 28-1 to reduce the combustion gas to 800 to 950. Is easy.
- the water 26 is used to heat the boiler water that is recirculated through the lines 26 ", 27" that branch off the lines 26, 27.
- a wall boiler 36-2 may be provided.
- Incombustibles that have been miniaturized by melting glass, cans, etc. are extracted from the incombustibles take-out line 14.
- the auxiliary combustion furnace 10 B may be provided independently as shown in FIG. 2, but the fluid medium of the combustion furnace 10 circulates with the pyrolysis furnace 1.
- the temperature of the fluidized medium in the charcoal combustion furnace 10 is approximately 700 to 850 ° C, while the temperature of the fluidized medium in the pyrolysis furnace 1 is 350 to 5001:
- the heat drop ⁇ ⁇ ⁇ is large, and therefore, if the fluid medium of the chamber 10 is guided directly to the pyrolysis furnace 1 side, the heat drop will cause the thermal decomposition temperature in the pyrolysis furnace 1 in the part where the pyrolysis temperature is high. If the temperature rises, heat fluctuation may occur, and accordingly, the adjustment of the amount of the returned fluid medium becomes complicated.
- a third superheater 29-2 is placed in the fluid medium path 19-] Z5 for returning the fluid medium reheated by the char combustion furnace 10 to the pyrolysis furnace 1.
- the fluid medium heated to 700 to 800 in the first char-burning furnace 10 is removed from the sub-charging furnace 10B. Then, the temperature of the fluid medium dropped to 500 to 700 ° C.
- the combustion gas formed in the char combustion furnace 10 and having a high temperature of 800 to 95 CTC and containing substantially no chlorine is introduced into the cyclone 16 through the combustion gas outlet line 15 as required, Ash and ash are separated from the outlet line 18, and hakai gas is separated from the gas outlet line 17.
- the high-temperature exhaust gas at 50 ° C is introduced into the first superheater 20 and heats steam Z boiler water at around 200 to 320 ° C produced by the first boiler 24 and water-cooled wall boiler 36. It is then used to produce superheated steam. Since the exhaust gas passing through the gas outlet line 17 does not substantially contain chlorine, even when the surface of the boiler tube of the first superheater 20 is set to 350 ° C or more, high-temperature corrosion is significantly reduced; Therefore, the temperature of the tube inside stream can be set at about 400 to 52 (TC, and it can be set to TC, and the first super boiler boiler steam is output. Is obtained.
- the flow rate of the gas supplied from the fiber exhaust gas input I line 6 is adjusted.
- the auxiliary sand—combustion is performed at a high temperature of about 500 to 700 ”C, which is higher than that of the 10B.
- the part is supplied from the sand circulation line 5 and used as a heat source.
- the air or combustion exhaust gas supplied to the pyrolysis furnace 1 through the exhaust gas inlet line 6 has a low oxygen content in order to efficiently perform pyrolysis in the range of 350 to 500 "C ffl.
- the temperature of the exhaust gas is 150-200 (the exhaust gas that maintains the temperature of TC, specifically, the output of the first boiler 24 [ It is a good idea to use the exhaust gas obtained by removing dust and chlorine from the exhaust gas.
- 3-1, 1 and 3-2 are dispersion plates, and 2-1, 2-2 and 2-3 are fluidized beds.
- FIG. 4 is a system diagram showing a superheated steam production apparatus according to the third embodiment of the present invention, which utilizes the heat of incineration of waste according to the third embodiment of the present invention, and explains the differences from the embodiment of FIG.
- a first filter 291 such as a vibrating sieve having a mesh diameter of about 5 mm, is provided in the refining furnace removal line 8 of the pyrolysis furnace 1, and a large amount of waste discharged from the line 8 is provided. ⁇ and other effluents are separated, and the other effluents are fed via lines 50 and 54 to the bottom of the fluidized bed above the distribution plate 11 of the charcoal combustion furnace 10 It is configured as follows. 51 is a large non- ⁇ extraction line.
- the incombustibles removal line 14 is provided with a second filter 292 having a mesh of about 2 mm, and the small amount 1 and the fluidized sand ash of the discharge discharged from the line 14 are removed. Separate and feed the fluidized sand to the bottom of the fluidized bed above the dispersing plate 11 of the yah furnace 10 via the line 52, the third filter 293, the lines 55 and 54. It is configured as follows. Small incombustibles are discharged outside through line 53.
- the third filter 293 is not necessarily required, but only drains ash to the outside while supplementing the fluid sand not supplemented by the second filter 292;
- the mesh size is set to around 0.1 mm, which is smaller than the minimum diameter (about 0.2 mm).
- the third filter 293 allows the ash alone to be discharged to the outside through the line 56 while being supplemented by the moving sand that has not been supplemented by the second filter 292. This facilitates efficient ash removal and liquid sand recovery.
- the large incombustibles separated by the pyrolysis reaction in the pyrolysis furnace 1 are taken out of the furnace from the incombustibles take-out line 8.
- the power of waste that has been crushed to about 200 mm mfi! As waste The power that is input into the pyrolysis furnace 1 Therefore, the size of the incombustibles removal line 8 of the pyrolysis furnace 1 must be increased to some extent. Therefore, in addition to the large non-combustible material from the above-mentioned I, I line 8, the residual charge flow iM ⁇ and the small non-combustible material are removed.
- the first filter 291 which separates the large amount of non-combustibles from the other substances discharged from the non- ⁇ extraction line 8 of the pyrolysis furnace 1, and discharges only large non-combustible substances, Other emissions can be fed to the bottom of the combustion chamber 10 and used for fuel lamps.
- Fig. 5 is a system diagram showing an apparatus for producing superheated steam using waste incineration heat according to the fourth embodiment of the present invention. And constitute the backflow prevention means.
- the sub-charging combustion furnace 10 B is provided with a partition line between the upper part of the fluidized bed and the lower part of the dispersion plate 3-2 facing the return line (fiT circulation line) 5 for returning the flow medium to the pyrolysis furnace 1. 1 0 0, 1 0 0 Divide by '.
- the lower part of the fluidized bed above the dispersion plate 3-2 is opened, and the fluid in the fluidized bed provided with the third superheater 29-2 (hereinafter referred to as the main fluidized bed 2-2A) is provided.
- the medium is configured to be supplied to the partition (a partition fluidized bed 2-2B partitioned by the plate 100) through the partition plate lower opening I110.
- the partitioning fluidized bed 2-2 B has a dispersion plate 3-2, so that the fuel gas flows through the branch line 6 ′ of the I line 6.
- the return line (sand circulation line) 5 should also be inclined in the direction of the pyrolysis furnace 1 Les ,.
- the fluid medium after the heat is removed by the third superheater 29-2 in the main fluidized bed 2-2A of the sub-chamber combustion furnace 100B passes through the partition plate 100.
- the fluid is introduced into the fluidized bed 2-2 B and then returned to the pyrolysis furnace 1 via the return line (sand circulation line) 5 while being moved by the flue gas in the branch line 6 ′.
- FIG. 6 shows a configuration in which a sand storage tank 120 is provided in the above-described char combustion furnace 10 in the system of FIG.
- the pyrolysis time needs to be changed according to the refuse quality, supply sand from the shellfish tank 120 to increase the number of sand held in the pyrolysis furnace, Increasing the time and extracting more sand from line 14 will reduce the amount of sand retained in the pyrolysis furnace and shorten the pyrolysis time.
- FIG. 7 shows an embodiment of a backflow prevention stage disposed on the above-mentioned char mixture removal line 9, wherein the power of the pyrolysis furnace 1 is larger than the pressure of the char combustion furnace 10 side.
- the mechanical transport stage 50 mm with the backflow prevention I function is shown by setting to.
- 5 5 is a cutting board.
- FIG. 8 shows a detailed configuration of the sub-charging furnace 10 used in FIGS. 5 and 6, and the sub-charging furnace 10B is, as shown in FIG. From 10 Take in fluid medium i 9-1 and return line to return fluid medium to pyrolysis furnace 1 side Circulation line) 5 Power sub-chamber 1 Furnace 10 Arranged so as to be on the diagonal of B The fluid medium moves from the base side of the third superheater 29-2 to the front side, and is disposed so as to be in sufficient thermal contact. As shown in FIG.
- the pressure difference forming means 50 is formed in the form of a so-called small fluidized bed, and is composed of a sub-charging combustion furnace 10, a fluidized bed 2-2 at the outlet side of B 2, an upper part and a dispersing plate 3-2, a partition plate 10 0, 1 below. Partition at 0 0 '.
- the fluidized bed space on the upper side of the dispersion plate 3-2 has an opening 101, and the flow medium in the sub-charging combustion furnace 10B is opened via the partition plate opening 101. It is configured to be fed to the fluidized bed 51 on the pressure difference forming means 50 side partitioned by the partition plate 100.
- a flow is caused by the combustion exhaust gas and the like supplied from the branch line 6 'of the exhaust gas inlet line 6 from below the dispersion plate 2-2.
- the fluid I The height up to the lower end of 100 (partition plate opening ⁇ 100 1 upper end) should be set to the height of ⁇ ⁇ ⁇ so that no backflow force is generated.
- the flow path for taking in the fluid medium into the sub-charging furnace 10 ⁇ side from the sub-charging furnace 10 0, and the flow from the sub-charging furnace 10 ⁇ side to the pyrolysis furnace 1 side The return lines 5 for returning the medium breaks are formed with slopes ⁇ ⁇ ⁇ ⁇ , each of which is inclined downward toward the I side, and each fluidized bed is gradually lowered in accordance with the inclined surface. ⁇ ! ⁇ (Liquid bed interface of combustion chamber 10 ⁇ !
- Fluid bed interface of combustion furnace 10 2 2 Force ax forming means 50 Partitioning fluidized bed of 50 side 5 1 interface) ⁇ Pyrolysis
- the fluidized bed of each fluidized bed is gradually lowered so as to form a fluidized bed 2-1 in the furnace 1.
- the line 9 for supplying the char mixture from the pyrolysis furnace 1 to the char combustion furnace 10 be constituted by a mechanical conveying means such as a screw feeder.
- Figure 9 shows the configuration of a fluidized bed improved from the char-firing furnace applied to each of the above embodiments.
- (A) is a front view
- (B) is a side view
- (C) is a plan view.
- Such a fluidized bed forms a fluidized bed 2-3 by accumulating a mixture of charcoal on the upper part of the dispersion plate 11 and the three fluidized areas of the left, right, and center 2-3 A so as to be able to circulate in the fluidized bed 2-3.
- / 2—3 BZ2—3 C is provided with an upper partitioning plate 61 A / 62 A, which is divided into 3 C, and the seven-part dividing plate 61 A / 62 A is a fluidized bed 2-3 parts. And the bottom are each questioned.
- a line 9 and a line 19-12 for supplying a char mixture and a fluid medium to the combustion furnace 10 are connected.
- the dispersion plate 11 is downwardly directed toward the incombustible removal line 14.
- a lower partitioning plate 61 B / 62 B is arranged at the same interval as the upper partitioning plate 6 1 AZ62 ⁇ , and is sandwiched between the divided partitioning plates 6 1 B and 62 B. It is more effective if the central part 11-2 of the dispersion plate is formed in a shape.
- Dispersion plates 1 1-1/1 1 1 1 2 1 1 1 1 3 provided by the lower release plates 61 B and 62 B, respectively, are connected to the air supply lines 12 at the bottom of the lower space.
- Lines 12—1 / 12—2—12—3 are connected, and the branch lines 1 2—1 / 1—2—2 / 1—2—3 are each provided with a 64 ⁇ control valve, and are provided with a The air flow supplied to each of the flow areas divided into three by the ⁇ 1 split plate 6 1 ⁇ 62 ⁇ can be controlled.
- the line 19-1 for supplying the fluid medium to the sub-charging furnace 10B is on the fluidized bed 2-3 interface, and the line 19-13 for supplying the combustion gas from the sub-charging furnace 10B is It is located above it.
- the supply port of the line 9 for supplying the mixture of the supplied pyrolysis furnace and the supply of the mixture of the pyrolysis furnace is divided into the three-divided flow area subsection 2-3B (downflow area) or both right and left sides.
- the char mixture supplied from line 9 to the lower part of, for example, the central part of the flow area 2-3B (downflow area) or the flow area 2-3AZ2-3C (h upflow area) is a mountain-shaped dispersion plate 1 1 1 2
- the air flow flows in the flow area 2-3 A 2-3 C on the left and right sides of the central part 2-3 B, and the downward flow force of the flow medium 2-3 B in the central part of the flow area can be generated.
- ⁇ Due to the upward flow, the char mixture and the fluid medium in the fluidized bed are as shown by the arrows in (A). Circulates.
- the lighter specific gravity always moves to the bottom of the bed due to the descending flow area of 2-3 B in the center of the flow area, and circulates through the flow areas 2-3A / 2-3C located on the left and right sides. Therefore, mixing with air is sufficiently performed, and sufficient combustion is possible with an air flow that is smaller by J1 (for example, 0: ⁇ : 1.2 to 1.3).
- the incombustibles not combusted in the fluidized bed move along the direction of the dispersing plate 11 as shown in (B) and (C), and are taken out through the guide plate 14 1 1 1 14 2. Discharged outside line 14.
- FIGS. 10A and 10B are three Ifii diagrams showing the internal construction of a pyrolysis furnace according to the improvement of the pyrolysis furnace applied to each of the above-described embodiments.
- FIG. (C) is a side view.
- the fluidized bed 2-1 such as flowing sand, stored in the pyrolysis furnace 1, specifically, on the dispersion plate 3-1, is fed from the waste input side (the waste supply line 4 side).
- the partition 80 is divided into a plurality of steps by a partition plate 80, and the partition plate 80 is alternately connected between the left and right side walls.
- the openings 81 are formed apart from each other, and the openings 81 are alternately provided at different positions.
- the main fluidized bed 1A is
- the width of the lower side wall of the main fluidized bed 1A is widened, and conveying means for conveying solid rest from the waste input side to the discharge side of the mixture at the bottom of the main fluidized bed 1A.
- conveying means for conveying solid rest from the waste input side to the discharge side of the mixture at the bottom of the main fluidized bed 1A.
- an air or flue gas artificial line 82 that blows air or flue gas directly below the conveying means 1 C, and a sub-fluidized bed section 1 B that fluidizes fluid sand etc. It is equipped with.
- the combustion can be performed while forcibly transporting the unburned material adhering to the incombustible material by the transporting means 1C in the auxiliary fluidized bed portion 1B in the direction of the charcoal.
- unburned matter can be discharged without remaining in the air.
- the actual flow length of the fluidized bed, and more specifically, a mixture of waste and fluidized medium while mixing the waste with the fluidized medium can be long, and the waste does not flow through to the char-mixture removal line 9. be able to.
- the thermal decomposition can be sufficiently performed in a negative manner, and the chlorine in the waste bubble can be substantially completely decomposed and removed by gasification.
- FIG. 11 shows another modification of the pyrolysis furnace in which the pyrolysis gas combustion furnace composed of the combustion ducts shown in the respective embodiments was deactivated, and (A) shows the thermal decomposition furnace of ⁇ 1.
- a combustion duct 40 is formed above a fluidized bed furnace block constituting the pyrolysis furnace 1 through a throttle section 4 11 1 and a diffuser nozzle 4 2 is formed in the throttle section 4 1. Further, an air inlet 43 for guiding air is provided above the combustion duct 40. As shown in FIGS. 11 (A) and 11 (C), the constricted portion 4 1 1 has an air diffuser nozzle 4 2 extending horizontally in the central area of the constricted portion 4 1 1 along the extending direction. Alternatively, the outlet may be formed with a narrower width, and as shown in ( ⁇ ), the intersecting portion 411 may be reduced in diameter to a circle, and the reduced portion may be formed.
- the air inlets 21 and 21 may be provided at vertically symmetric positions so that a swirling air flow can be introduced into the air inlet.
- the pyrolysis gas generated in the pyrolysis furnace 1 is guided into the duct 40 through the throttle section 4 1 1, introduced through the ⁇ air introduction line 2 1, and rejected by the diffuser nozzle 4 2.
- Primary combustion of pyrolysis gas in a reducing atmosphere with air (excess air ratio 0.6 to 0.
- the throttle section 4 11 is provided between the duct 40 and the pyrolysis furnace 1, the mixing with air is promoted, and the flow of heat below the thermal power at the time of reburning in the fuel duct 40 is improved.
- the preferred thermal decomposition can be achieved in the thermal furnace 1 without radiation between the floors and, as a result, without burning of the charcoal.
- FIG. 12 is a system diagram showing a superheated steam production apparatus using waste heat of incineration according to a sixth embodiment of the present invention, in which the char-burner of FIG. 2 is divided into two fluidized beds via a partition plate. It is divided to form backflow prevention means, and an ash melting furnace is provided.
- FIG. 13 is a system diagram showing an apparatus for producing superheated steam using incineration heat of waste vegetables according to the seventh embodiment of the present invention.
- a part of the pyrolysis gas is branched.
- the pyrolysis gas is supplied to the fiber furnace.
- Fig. 14 shows the differential pressure gauge installed in the pyrolysis gas outlet line shown in Fig. 13: a measuring means, (A) a differential pressure measuring stage formed using an orifice, and (B) a The formed differential pressure measurement stage.
- the pyrolysis gas from the pyrolysis gas ili I 1 line 7 is introduced into the ash melting furnace 31.
- the pyrolysis gas from the pyrolysis gas outlet line 7 is branched and then introduced into the ash melter 31.
- the ash melting furnace 31 introduces, for example, a swirling stream, dust or ash from the line 29, air or oxygen-enriched air together with the pyrolysis gas from the line 30, and Dust and ash are melted by heat at a temperature of 1300 ° C. or more, and the melted dust and ash are dropped into the water storage section 32 A via the molten ash outlet line 32 to reduce the size of several mm A water-cooled slag is generated, and the slag is configured to be used as building aggregate.
- Ash is guided to the ash melting furnace 31 via an output II line 18 dust line 29 of a cyclone 16 and an incombustible material and / or a bubble filter of a line 14. These can also be lysed, such as — and ash collected by an electric dust collector.
- pyrolysis gas 'fibre furnaces' composed of fuel ducts, and a line 21 A for supplying air which is small to the pyrolysis gas. And complete combustion of the pyrolysis gas.
- the pyrolysis gas extracted from the pyrolysis gas outlet line 7 of the pyrolysis furnace 1 is introduced into the ash melting furnace 31 before being introduced into the fuel 34.
- the ash separated by the bag filter provided in the downstream of the cyclone 16 ⁇ ⁇ ⁇ exhaust gas line 25 and the incombustibles of Z or line 14 should be introduced into the ash melter 31 described above. This makes it possible to produce aggregates and the like using the molten ash.
- the pyrolysis gas outlet line 7 is branched as lines 7 ′ and 7-1 as shown in FIG. 13, it is necessary to measure the branch flow rate by the differential pressure measuring means 100.
- This differential pressure measuring means 100 is used to measure the flow rate of the pyrolysis gas removed from the pyrolysis furnace 1.
- FIG. 14 (A) shows the orifice formed by ⁇ 3 ⁇ ⁇ : measurement means, 101, 101 'is the pipe forming the outlet line 7, 102 is the flange, 103 is the orifice plate , 104 is a differential pressure gauge, 105, 106, 107, 108 is an air inlet pipe, 109 is a pressure tap as a pressure outlet, 110 is a throttle part, 1 1 1 is an air-conditioning valve, and 1 1 2 is a flow meter or other flow meter.
- four pressure tubs 109 are provided at positions that are changed by 90 ”in the circumferential direction.
- FIG. 14 (B) shows a difference measuring means 100 formed by using a trumpet-shaped narrowing portion 110, and its configuration is the same as that of FIG. 14 (A).
- FIG. 15 is a system diagram showing an apparatus for producing a superheated steam using the heat of incineration of waste according to the eighth embodiment of the present invention, wherein part of the pyrolysis gas obtained by the pyrolysis furnace 1 is ash-melted.
- a configuration may also be adopted in which the upstream side of the furnace 31 is supplied through a branch line 7-2 to the lower inlet side of the dispersion plate 31-1 of the pyrolysis furnace.
- This I reline 7-1 pyrolysis gas force ⁇ fluidizing gas because they are not diluted with (N 2, C 0 2, H 2 0 principal component of the inert gas) becomes high power port Rigas, Hai ⁇ ifc ⁇ 3
- the temperature of 1 can be easily adjusted to 130 to 150 ° C.
- FIG. 16 is a system diagram showing a superheated steam production apparatus utilizing waste incineration heat according to the ninth embodiment of the present invention. Has formed.
- 1A is a mechanical transport for transporting the solid content in the pyrolysis means from the waste input side to the char mixture removal side.
- a means for performing a stirring function for example, a rotary kiln or a horizontal screw stirring tank is provided.
- a fluid medium such as sand is discharged, and waste such as sand and municipal waste is fed into the waste supply line 4 and the T-ring line 5 to enter air or fuel exhaust gas. Agitated at a temperature of 300 ° C or more by air or combustion exhaust gas supplied from 1 line 6.
- the thermal decomposition be performed so that the thermal calorie ratio of the pyrolysis gas and the char mixture becomes “about 7 (pyrolysis gas): about 3 (char mixture) J”. is there.
- an empty line iA port 21 is attached to line 1 for the pyrolysis gas output from the pyrolysis furnace 1A exit side, and the pyrolysis gas extracted from the pyrolysis furnace 1A is an air population line. 2 Introduce air from 1 to partially burn the tar and the like contained in the pyrolysis gas block, and to prevent tar adhesion and coking prevention at the outlet line 7, and then expand the pyrolysis gas. It is introduced into the ash melting furnace 31 before being introduced into the furnace 34.
- Figure 17 shows the superheated steam produced by using the heat of incineration of waste according to the tenth embodiment of Honshu.
- Fig. 3 is a system diagram showing a manufacturing apparatus, which is composed of a plurality of pyrolysis furnaces.
- a plurality of the thermal decomposition furnaces are provided, and the thermal decomposition furnace is constituted by a fluidized thermal decomposition furnace having a fluidized bed with a V ⁇ deviation.
- Each of the fluidized-bed pyrolysis furnaces 1 and 2 has a fluidized medium 2-1 and 2-1 'such as fluidized sand stored on a dispersion plate 3-1 and 3-1' such as a perforated plate. Wastes such as municipal waste and fluidized sand are supplied from the waste supply lines 4 and 4 'and the 3 ⁇ 4Ht ring (return) lines 5 and 5', and the waste gas is supplied from the flue gas inlet lines 6 and 6 '.
- the fluidized-bed pyrolysis furnace 1 (first pyrolysis furnace) actively generates a tea mixture by performing the pyrolysis reaction of waste in a fluidized bed space of a temperature of 250 to 45 (TC). The mixture is taken out from the removal line 9 and supplied to the furnace 10.
- the pyrolysis gas generated by the reaction is sent to the pyrolysis gas outlet line 7 to the pyrolysis gas combustion furnace 34 and non-flammable. The object is not!
- the other fluidized pyrolysis furnace ⁇ (second pyrolysis furnace) performs the pyrolysis reaction of waste in a fluidized bed space with a temperature of about 450 to 700 ”C, and actively heats it together with dechlorination.
- the cracked gas is fed to the ash melting furnace 3 1 from the pyrolysis gas outlet line 7 ′, while the unreacted char — mixture (the char-burning furnace 10, non-flammable ash from the iii ii ⁇ The object is separated into _, respectively, from the unloading line 8 'and taken out.
- the temperature range of the fluidized bed can be widened to 250 to 450 ° C, and as a result, the amount of char mixture can be increased. I can do it.
- the ash melting furnace 31 since a high-temperature gas of 450-700 ° C. and sufficiently thermally decomposed and high in calories is introduced, it is introduced into the ash melting furnace 31. oxygen A high temperature of 130 ° C. can be maintained even if the enriched air is reduced.
- FIG. 18 is a system diagram showing a modified example of the superheated steam production apparatus using the heat of incineration of waste according to the eleventh embodiment, in which a pyrolysis furnace is constituted by a fluidized bed and mechanical conveying means. are doing.
- one of the fluidized pyrolysis furnaces 1 (first pyrolysis furnace) in FIG. 17 is left as it is, and the other fluidized pyrolysis furnace ⁇ (first pyrolysis furnace) is mechanically heated as shown in ⁇ 16.
- Cracking furnace 1 A, ⁇ a stirrer with a mechanical transport / stirring function, such as a rotary kiln or a horizontal screw, which moves the rest in the pyrolysis furnace from the waste input side to the char-mixture removal side. It consists of pyrolysis with one agitation.
- a is the gas for fluidization (main and to N 2, C 0 2, H 2 0 main component of I ⁇ : gas) it is not Therefore, since the pyrolysis gas is not released, the heat per unit volume is high. It can be effectively used as an energy source for melting the ash content of gas bubbles, and is more preferable than the fluidized bed pyrolysis furnace 1.
- a low-temperature pyrolysis furnace for producing a char mixture is formed in a fluidized bed ⁇ , and a high-temperature pyrolysis furnace 1 ′ for producing high-calorie pyrolysis gas is mechanically transported.
- the ⁇ gas introduced into the ash melting furnace 31 can be enriched with oxygen.
- a part of the pyrolysis gas obtained by the other pyrolysis furnace 1 ′ is supplied to the pyrolysis gas combustion furnace 34 via the branch line 7 ′ on the upstream side of the ash melting furnace 31. are doing.
- the amount of ash contained in the pyrolysis gas or the combustion gas is about 10% of the waste, and it is not always necessary to use the entire pyrolysis gas supplied to melt it.
- the ash melting furnace 31 branched from the pyrolysis gas outlet line 7 and the upstream / branch line ⁇ ′ are placed before the ⁇ / K measurement ⁇ stage 100 shown in Fig. 14 Then, it is necessary to adjust the owl.
- the present invention particularly employs a backflow prevention step for preventing a backflow of a fluid or a fluid medium and gas between the pyrolysis means and the char combustion-stage, so that the flow having the temperature ⁇ and a large heat capacity is provided.
- Medium strength s' Prevents temperature fluctuations, thermal decomposition, deterioration of combustion conditions, etc. in both fluidized tanks due to these without erroneous backflow in both fluidized tanks.
- the PJ lubrication function is performed on the pyrolysis means side and the char combustion means side, respectively, and the thermal energy of the pyrolysis gas obtained by the pyrolysis means and the chlorine obtained by the char
- the calorie ratio and the chlorine content of the combustion gas (dechlorination heat energy) that is not contained can be obtained according to the desired purpose without variation.
- the thermal decomposition in the thermal decomposition means it is possible to prevent tar adhesion and coking of the pyrolysis gas, to reduce dioxin, to reduce C ⁇ , and to reduce NOx. In comparison with this, it is possible to obtain a superheated steam having a higher H level while reducing chlorine.
- the thermal decomposition means is constituted not by a fluidized bed but by a mechanical conveyance stirring means, the thermal decomposition time and the amount of thermal decomposition are more timely compared to a fluidized bed.
- the pyrolysis gas can be stably performed and the pyrolysis gas is not diluted, so that the calorific value per unit volume can be increased.
- the pyrolysis means is constituted by a plurality of pyrolysis furnaces each having a fluidized bed or a combination of mechanical stirring tanks as appropriate, and the pyrolysis temperature of one pyrolysis furnace is reduced by another pyrolysis furnace. Since the pyrolysis temperature of the cracking furnace was made different, one of the pyrolysis furnaces on the low-temperature side The temperature is set to about crc, and i3 ⁇ 4s of the positively dechlorinated char mixture is performed, while the other pyrolysis furnace on the high temperature side is set to about 450 to 700 "C, For example, the pyrolysis gas used in the ash melting furnace
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Gasification And Melting Of Waste (AREA)
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP97903617A EP0823590B1 (en) | 1996-02-29 | 1997-02-27 | Method and apparatus for producing superheated steam using heat generated through incineration of wastes |
DE69732394T DE69732394T2 (de) | 1996-02-29 | 1997-02-27 | Verfahren und vorrichtung zur erzeugung von überhitztem dampf mittels wärme von abfallverbrennung |
KR1019970707702A KR100264723B1 (ko) | 1996-02-29 | 1997-02-27 | 폐기물의소각열을이용한과열증기제조방법과그장치 |
US08/945,591 US6133499A (en) | 1996-02-29 | 1997-02-27 | Method and apparatus for producing superheated steam using heat from the incineration of waste material |
Applications Claiming Priority (10)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP8/69067 | 1996-02-29 | ||
JP06909096A JP3285752B2 (ja) | 1996-02-29 | 1996-02-29 | 廃棄物の焼却熱を利用した過熱蒸気製造装置 |
JP06938896A JP3310853B2 (ja) | 1996-02-29 | 1996-02-29 | 廃棄物の焼却熱を利用した過熱蒸気製造装置 |
JP8/69090 | 1996-02-29 | ||
JP8/69388 | 1996-02-29 | ||
JP8/69383 | 1996-02-29 | ||
JP8/69393 | 1996-02-29 | ||
JP06906796A JP3276286B2 (ja) | 1996-02-29 | 1996-02-29 | 廃棄物の焼却熱を利用した過熱蒸気製造装置 |
JP06938396A JP3322557B2 (ja) | 1996-02-29 | 1996-02-29 | 廃棄物の焼却熱を利用した過熱蒸気製造装置 |
JP06939396A JP3408686B2 (ja) | 1996-02-29 | 1996-02-29 | 廃棄物の焼却熱を利用した過熱蒸気製造装置 |
Publications (1)
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WO1997032161A1 true WO1997032161A1 (fr) | 1997-09-04 |
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PCT/JP1997/000573 WO1997032161A1 (fr) | 1996-02-29 | 1997-02-27 | Procede et appareil de production de vapeur surchauffee utilisant la chaleur generee par l'incineration de dechets |
Country Status (6)
Country | Link |
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US (1) | US6133499A (ja) |
EP (1) | EP0823590B1 (ja) |
KR (1) | KR100264723B1 (ja) |
DE (1) | DE69732394T2 (ja) |
SG (1) | SG96183A1 (ja) |
WO (1) | WO1997032161A1 (ja) |
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EP2011972B1 (de) | 2007-07-03 | 2013-07-31 | clm technologie ag | Anlage, Verfahren und Vorrichtung zur Erzeugung eines überhitzten Mediums |
FI123180B (fi) * | 2007-10-11 | 2012-12-14 | Valtion Teknillinen | Laitteisto pyrolyysituotteen valmistamiseksi |
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ITBO20080008A1 (it) * | 2008-01-04 | 2009-07-05 | Samaya S R L | Impianto per il trattamento di rifiuti in discarica |
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-
1997
- 1997-02-27 SG SG9904761A patent/SG96183A1/en unknown
- 1997-02-27 WO PCT/JP1997/000573 patent/WO1997032161A1/ja active IP Right Grant
- 1997-02-27 US US08/945,591 patent/US6133499A/en not_active Expired - Fee Related
- 1997-02-27 DE DE69732394T patent/DE69732394T2/de not_active Expired - Fee Related
- 1997-02-27 EP EP97903617A patent/EP0823590B1/en not_active Expired - Lifetime
- 1997-02-27 KR KR1019970707702A patent/KR100264723B1/ko not_active IP Right Cessation
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JPS59215503A (ja) * | 1983-05-20 | 1984-12-05 | 堺市 | ごみ焼却炉 |
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Also Published As
Publication number | Publication date |
---|---|
EP0823590A4 (en) | 2001-03-21 |
KR100264723B1 (ko) | 2000-09-01 |
DE69732394D1 (de) | 2005-03-10 |
DE69732394T2 (de) | 2006-03-30 |
EP0823590A1 (en) | 1998-02-11 |
SG96183A1 (en) | 2003-05-23 |
EP0823590B1 (en) | 2005-02-02 |
KR19990008177A (ko) | 1999-01-25 |
US6133499A (en) | 2000-10-17 |
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