JP4265975B2 - Heat recovery method, combustible material processing method, heat recovery system, and combustible material processing apparatus - Google Patents

Description

In the present invention, when processing combustible waste such as municipal waste, waste plastic, shredder dust, construction waste, and waste tires, the heat generated is used to melt ash and effectively recover heat. The present invention relates to a heat recovery method, a combustible material processing method, a heat recovery system, and a combustible material processing apparatus.

  In recent years, the gasification and melting method has attracted attention as a method for incinerating waste such as municipal waste. This gasification and melting method is a method in which waste is partially burned at about 500 ° C. to obtain a pyrolysis gas, and this pyrolysis gas is burned at a high temperature in a melting furnace to melt ash contained in the gas. is there. The pyrolysis gas obtained by this method is obtained by partial combustion of waste, and the combustion gas is mixed in and the calorific value is low. Therefore, in order to obtain a sufficient temperature for melting the ash in the melting furnace, that is, a temperature of about 1200 ° C., it is necessary that the input waste has a calorific value of about 7 to 8 MJ / kg. is there.

  However, waste, especially municipal waste, has a large fluctuation in calorific value, so if the calorific value is insufficient, you must supply auxiliary fuel or use oxygen instead of air as the oxygen source for combustion. Is the actual situation. Therefore, there are problems that the running cost increases and the initial cost increases by installing an oxygen generator.

  The ash contained in the pyrolysis gas flowing into the melting furnace contains silica, alumina, calcia-based materials, low melting point metals, low boiling point metal salts, etc., but melts in the melting furnace. The main components are silica, alumina, and calcia, and low-boiling metal salts and the like flow out of the melting furnace downstream with the combustion gas.

  In addition, in a melting furnace, a swirl flow of gas is formed inside, and in many cases, the ash content in the gas is collided with the wall of the melting furnace by an inertial force by means such as sudden reversal of the gas flow, thereby generating a slag flow. A structure that is formed to increase the melting rate of ash contained in the material to be melted is employed. Accordingly, since particles having a large particle size are trapped in the slag flow, the particle size of ash in the exhaust gas flowing downstream from the melting furnace increases as a result of 10 microns or less.

  As described above, the ash in the gas flowing out downstream of the melting furnace is characterized by a high salt concentration and a very small particle size, which causes various problems. From the high temperature range of 1200 ° C. or higher immediately after melting to the temperature range of about 400 ° C., fine particles melted at each temperature adhere to the heat transfer surface of the equipment provided for heat recovery and the heat transfer coefficient of the heat transfer surface Is drastically reduced.

  As the heat transfer coefficient decreases, the function of the heat recovery device decreases, such as being unable to decrease the gas temperature, so the gas temperature at the heat recovery process outlet rises, such as a bag filter provided downstream of the heat recovery process. The allowable temperature for the dust collection process may be exceeded. In particular, since the filter cloth of the bag filter is vulnerable to heat, the temperature at the entrance of the dust collection process needs to be lower than the allowable temperature. For this reason, a water spray type gas cooling process is provided in advance, or a sufficient heat transfer area is provided on the heat transfer surface of the heat recovery device so that the function of the heat recovery device is sufficiently maintained. It is necessary to prevent the gas temperature at the temperature from exceeding the allowable temperature. This causes high costs due to an increase in equipment.

  FIG. 1 is a diagram showing a process flow of a combustible waste treatment apparatus that employs a conventional gasification melting method (see Patent Document 1). The combustible waste treatment apparatus includes a gasification furnace 101, a melting furnace 102, a boiler 103, an economizer or air preheater 104, a gas cooling tower 105, a bag filter 106, an induction blower 107, a catalyst denitration tower 108, and a chimney 109. . The combustible waste is supplied to the gasification furnace 101 and partially combusted and pyrolyzed to generate pyrolysis gas, tar, char, fly ash and the like. The pyrolysis gas containing tar, char, fly ash and the like is supplied to the melting furnace 102 in its entirety.

  The pyrolysis gas is burned at a high temperature of 1200 ° C. or higher in the melting furnace 102, the ash is melted and discharged out of the furnace as molten slag, and the high-temperature combustion gas emitted from the melting furnace is guided to the boiler 103. The combustion gas is cooled to about 450 ° C. by the boiler 103 and further cooled to about 200 ° C. by the economizer or the air preheater 104.

  The ash contained in the high-temperature combustion gas exiting the melting furnace 102 has a small particle size and a high ratio of metal salts having a relatively low melting point, and thus has high adhesion, and is transferred to the boiler 103, economizer or air preheater 104. Easy to adhere to hot surface. Therefore, as the operation is continued, the heat transfer coefficient is gradually reduced by adhering to the heat transfer surface of the boiler 103, the economizer or the air preheater 104. As time passes, the cooling gradually becomes difficult and the inlet temperature of the bag filter 106 increases.

  In general, since the heat resistance temperature of the bag filter is about 220 ° C., the gas cooling tower 105 must be cooled by spraying water into the combustion gas so that the temperature does not exceed that. However, even if the operation is continued in this manner, the progress of the ash adhesion to the heat transfer surface does not stop, the combustion gas temperature at the inlet of the air preheater gradually increases, and the adhesion becomes further intense. In the temperature range above 450 ° C, the ash is in a semi-molten state, and it is difficult to mechanically scrape or wipe off the adhesion, for example, and stop the progress of ash adhesion without lowering the temperature. Is difficult. That is, once the function of the heat transfer surface is degraded, it is difficult to suppress the progress of ash adhesion in that state.

  Therefore, the conventional combustible waste treatment apparatus has a sufficient safety factor for the heat transfer area of the boiler 103, the economizer or the air preheater 104, which is a heat recovery process, and forces the ash adhering to the heat transfer surface. In addition, a stable operation could not be continued except for providing a means for scraping off. However, if the ash adhering to the heat transfer surface is forcibly scraped off, the surface temperature of the heat transfer surface will change greatly, and the protective film formed will peel off due to thermal shock, which may promote corrosion wear on the heat transfer surface. There is also.

  In addition, in order to return the ash collected by the bag filter 106 to the melting furnace 102 in order to increase the ash melting rate, a large amount of low ash that is not melted into slag in the melting furnace and is transferred to the exhaust gas as it is. Since the melting point material and metal salts circulate in large quantities in the circulation path including the heat exchanger part, there is a risk of accelerating the adhesion of ash to the heat transfer surface of the heat exchanger. There is a problem that the slag conversion rate cannot be increased below a certain limit.

  On the other hand, as a method not to use auxiliary fuel for melting ash in recent years, rather than introducing the partial combustion type pyrolysis gas to the melting furnace, the heat generation amount of the pyrolysis gas is increased as much as possible to increase the temperature of the melting furnace. In order to make it easier to maintain, there has been proposed a method in which a pyrolysis furnace system is used which is as close to a dry distillation system as possible without using oxygen. FIG. 2 is a diagram showing a process flow of the combustible waste treatment apparatus proposed by the inventors of the present application (see Patent Document 2).

  2, the same reference numerals as those in FIG. 1 denote the same or corresponding parts. The combustible waste treatment apparatus has a gasification furnace and a melting furnace as in the conventional example, but the gasification furnace is an integrated type divided into a pyrolysis chamber 110-1 and a combustion chamber 110-2. A fluidized bed gasification furnace 110 is employed. The combustible waste is mainly supplied to the pyrolysis chamber 110-1 side of the fluidized bed gasification furnace 110, where pyrolysis gas, tar, char, fly ash and the like are generated. Of these, all that does not remain in the fluidized bed is supplied to the melting furnace 102 where it is burned at a high temperature of 1200 ° C. or higher, and the ash is melted.

  On the other hand, the pyrolysis residue remaining in the fluidized bed flows into the combustion chamber 110-2 together with the fluidized medium. Fluidized air and secondary air are supplied so that the fluidized bed in the combustion chamber 110-2 is maintained at about 550 ° C to 700 ° C, and the freeboard portion above the fluidized bed is maintained at 850 ° C to 950 ° C. The ratio is maintained at 1 or more and complete combustion is performed. In some cases, the combustion chamber 110-2 only burns the pyrolysis residue flowing in via the pyrolysis chamber 110-1, but directly supplies waste according to the thermal decomposition characteristics and combustion characteristics of the waste. May be.

  The combustion gas emitted from the combustion chamber 110-2 is introduced into a dust collector 112 such as a cyclone at a temperature of 850 ° C. to 950 ° C., and after being dedusted, is introduced into the boiler 103. The ash particles collected by the dust collector 112 are guided to the melting furnace 102 and melted.

  The combustible waste treatment apparatus having the above-described configuration has an excellent advantage that ash can be melted without using auxiliary fuel even in the case of waste having a low calorific value, but in the gas flowing into the boiler 103, Since the contained particles are collected by the melting furnace 102 on the pyrolysis chamber 110-1 side and the dust collector 112 such as a cyclone on the combustion chamber 110-2 side, the particles are very fine (small particle size). As described above, it is not preferable from the viewpoint of preventing adhesion to the heat transfer surface of the boiler 103, the economizer, or the air preheater 104.

Japanese Patent No. 3153091 Japanese Patent Application No. 2001-271497

The present invention has been made in view of the above points, and even if the calorific value is as low as 6 to 7 MJ / kg, ash can be melted without requiring auxiliary fuel and combustion gas after ash melting is achieved. Even when heat is recovered from the heat source, ash adhesion to the heat transfer surface of the heat recovery device (boiler, economizer, or air preheater) is suppressed to minimize the heat transfer surface margin, and water spray type gas cooling equipment An object of the present invention is to provide a heat recovery method, a combustible material processing method, a heat recovery system, and a combustible material processing apparatus that can eliminate the need for such facilities.

In order to solve the above-mentioned problem, the invention according to claim 1 supplies a combustible material to a fluidized bed gasification furnace composed of a thermal decomposition chamber and a combustion chamber, and thermally decomposes the combustible material in the thermal decomposition chamber. The cracked gas and the pyrolysis residue are generated, the pyrolysis residue is burned in the combustion chamber, the first gas containing a large number of large particles generated in the combustion chamber is generated, and is generated in the pyrolysis chamber . A pyrolysis gas is introduced into a melting furnace and burned to melt the ash to generate a second gas containing a large number of small particles, and has a heat transfer surface for directly exchanging the first gas. It is introduced into the heat recovery device, heat is exchanged between the introduced gas and the heat receiving fluid to recover heat, and then the second gas is more gas than the portion where the first gas is introduced into the heat recovery device. the first gas to the second gas mixture to the heat recovery child introduced into the heat recovery device downstream relative to the flow In heat recovery method comprising.

As described above, heat is recovered from the first gas containing many particles having a large particle size, and then the second gas containing many particles having a small particle size is mixed, so that the particle size in the first gas is large. Due to the polishing function for polishing the heat transfer surface when the particles collide with the heat transfer surface, the particles adhere to the heat transfer surface, particularly the particles having a small particle size that easily adhere to the heat transfer surface in the second gas. Adhesion can be prevented.

Since the first gas discharged from the combustion chamber does not pass through the melting furnace, it contains a large amount of large particles and is supplied to the heat recovery device as it is. In addition, since the first gas is introduced from the upstream side of the second gas and mixed with the second gas, the second gas containing many particles having a small particle size that easily adhere to the heat transfer surface. There is no region where only gas exists. In addition, since the high-temperature second gas is introduced and mixed after the first gas is cooled by the heat recovery device, only the high-temperature second gas containing molten slag particles that easily adhere to the heat transfer surface is used. It will also not make the area where there is.

According to a second aspect of the invention, the heat recovery method of claim 1, the remaining char fluidized bed of the pyrolysis chamber with the fluidized medium by combustion is introduced into the combustion chamber, the combustion chamber The heated fluid medium is caused to flow into a pyrolysis chamber for pyrolyzing the combustible material. With this configuration, the heat generated by burning the char in the combustion chamber can be transferred to the fluid medium, and this heat can be effectively used for the pyrolysis reaction of the combustible material in the pyrolysis chamber.

The invention according to claim 3 is the heat recovery method according to claim 1 or 2 , wherein after mixing the first gas and the second gas, the mixture is cooled to 450 ° C. or lower, and then the mixed gas is collected by a dust collector. The solid content is separated, and the separated solid content is introduced into a melting furnace and melted. The gas temperature after cooling is 450 ° C. or lower, preferably 350 ° C. or lower, more preferably 300 ° C. or lower, and most preferably 250 ° C. or lower.

The invention according to claim 4 supplies a combustible material to a fluidized bed gasification furnace composed of a pyrolysis chamber and a combustion chamber, and pyrolyzes the combustible material in the pyrolysis chamber to produce pyrolysis gas and pyrolysis residue. The pyrolysis residue is burned in the combustion chamber, the first gas containing many particles having a large particle size is generated in the combustion chamber, and the pyrolysis gas generated in the pyrolysis chamber is introduced into the melting furnace. introduced into the heat recovery unit with a heat transfer surface of the small particles to produce a second gas containing a large amount of, for the first gas direct heat exchange from the combustion chamber of the particle size by melting ash is burned Te and performs heat exchange between the introduced gas and the heat receiving fluid heat recovery, the second gas discharged from the solvent Toruro first gas of the gas than portions introduced into the heat recovery device The combustible material is characterized in that it is introduced into the heat recovery device downstream of the flow and mixed with the first gas to recover heat. Some sense way.

As described above, the first gas containing a large number of large particles from the combustion chamber is introduced into the heat recovery device to recover the heat, and then this heat is recovered into the recovered gas as particles discharged from the melting furnace. The second gas containing a large number of small-diameter particles is introduced into the heat recovery device downstream of the location where the first gas is introduced into the heat recovery device and mixed with the first gas to heat the gas. Therefore , the particles can be prevented from adhering to the heat transfer surface by the polishing function when the large particle in the first gas collides with the heat transfer surface.

According to a fifth aspect of the present invention, in the method for treating a combustible material according to the fourth aspect , the first gas and the second gas are recovered by a heat recovery device, cooled to 450 ° C. or lower, and then collected. apparatus by separating solids of the gas, and introducing the solids separated in the solvent Toruro, characterized in that to melt. The gas temperature after cooling is 450 ° C. or lower, preferably 350 ° C. or lower, more preferably 300 ° C. or lower, and most preferably 250 ° C. or lower.

The invention according to claim 6 is a method of pyrolyzing a combustible material to produce a pyrolysis gas and a pyrolysis residue, burning the pyrolysis residue, and burning the pyrolysis residue to contain a first gas containing many particles having a large particle size. and fluidized-bed gasification furnace which is composed of a combustion chamber to produce, by melting ash content contained pyrolysis gas produced by thermal decomposition chamber to the pyrolysis gas stream is combusted by introducing into the melting furnace particle size A melting furnace for generating a second gas containing a large amount of small particles, a first inlet for directly introducing the first gas from the fluidized bed gasification furnace, and a second for directly introducing the second gas from the melting furnace. And an exhaust port for exhausting the gas after heat recovery, and heat is recovered by exchanging heat between the gas introduced from the first and second inlets and the heat receiving fluid. A heat recovery device for exchanging heat between the heat receiving fluid and the introduced gas. Provided with a heat transfer surface, on the downstream side for the the flow of gas introduced from the first inlet, in a heat recovery system characterized in that a second inlet.

  As described above, the second introduction port for introducing the second gas containing many particles having a small particle diameter is provided downstream of the first introduction port for introducing the first gas containing many particles having a large particle size. Therefore, due to the polishing function when particles having a large particle diameter in the first gas introduced from the first introduction port collide with the heat transfer surface, the particles are adhered, particularly introduced from the second introduction port. It is possible to prevent adhesion of particles having a small particle diameter in the second gas that easily adheres. In addition, by providing the first inlet on the upstream side of the second inlet, the second gas containing many particles having a small particle size is cooled after the first gas containing many particles having a large particle size is cooled. As a result, gas is mixed in, and as a result, a region in which high-temperature gas containing particles having a small particle diameter that easily adheres to the heat transfer surface exists is not formed as much as possible.

The invention according to claim 7 is the heat recovery system according to claim 6 , wherein the first gas and the second gas are mixed, then cooled to 450 ° C. or lower, and then collected in the mixed gas by a dust collector. The solid content is separated, and the separated solid content is introduced into a melting furnace and melted. The gas temperature after cooling is 450 ° C. or lower, preferably 350 ° C. or lower, more preferably 300 ° C. or lower, and most preferably 250 ° C. or lower.

According to the eighth aspect of the present invention, the combustible material supplied from the combustible material supply means for supplying the combustible material is pyrolyzed to burn the pyrolysis chamber and the pyrolysis residue that generate the pyrolysis gas and the pyrolysis residue. Between a fluidized bed gasification furnace composed of a combustion chamber for generating a first gas containing a large number of particles having a large particle size, and a heat receiving fluid by directly introducing the first gas generated in the combustion chamber A heat recovery device with a heat transfer surface that recovers heat by exchanging heat and a pyrolysis gas generated in the pyrolysis chamber is introduced and burned to melt the ash in the pyrolysis gas to produce particles with a small particle size. in the processing apparatus of combustibles having a melting furnace to produce a second gas containing a large amount, a second gas discharged from the melting furnace, as a transport gas for further generated particles the melting furnace, the with particles 1 downstream of the gas flow from the location where the gas 1 is introduced into the heat recovery device In processor combustibles, characterized in that it comprises a gas introducing means for introducing the heat recovery device.

As described above, the second gas discharged from the melting furnace is used as a transport gas for the particles further generated in the melting furnace, and the gas flow is more than the portion where the first gas is introduced into the heat recovery apparatus together with the particles. Since the gas introduction means for introducing the heat recovery device downstream is provided , the particles having a large particle size in the first gas are adhered to the heat transfer surface by the polishing function. a second attachment grain terminal of gas discharged from the melting furnace comprising small particles of size can be prevented.

The invention according to claim 9 is the combustible material processing apparatus according to claim 8 , wherein the first gas is introduced into the heat recovery device to recover the heat, and the heat is recovered in the recovered gas. It is characterized by comprising at least means for mixing the second gas discharged from the furnace and further recovering heat.

The invention according to claim 10, in the processing apparatus of combustibles according to claim 8 or 9, the fluid medium from the combustion chamber, characterized in that it comprises means for moving the pyrolysis chamber.

An eleventh aspect of the present invention is the combustible material processing apparatus according to the tenth aspect , wherein the second gas from the pyrolysis chamber is introduced into the melting furnace, and the first gas from the combustion chamber is heated. Means for introducing into the recovery device is provided.

A twelfth aspect of the present invention is the combustible material treatment apparatus according to any one of the eighth to eleventh aspects, wherein the heat recovery device is a waste heat boiler.

The invention according to claim 13 is the combustible material processing apparatus according to any one of claims 8 to 12 , wherein the first gas and the second gas are mixed and then cooled to 450 ° C. or lower, The solid content in the mixed gas is separated by a dust collector, and the separated solid content is introduced into a melting furnace and melted. The gas temperature after cooling is 450 ° C. or lower, preferably 350 ° C. or lower, more preferably 300 ° C. or lower, and most preferably 250 ° C. or lower.

  In addition, a combustible waste treatment method includes a pyrolysis process in which a combustible waste is pyrolyzed at a temperature of 350 ° C. or more to obtain char and pyrolysis gas, an unthermally decomposed product generated from the pyrolysis process, tar, Combustion process in which char is combusted at a temperature of 500 ° C. or higher, a pyrolysis gas generated in the pyrolysis process is combusted at 1200 ° C. or higher, and an ash content accompanying the pyrolysis gas is melted. A heat recovery step of recovering sensible heat until the burned combustion gas reaches 450 ° C. or less, and a dust collection step of collecting ash contained in the combustion gas downstream of the heat recovery step. The collected ash is supplied to the melting combustion process and melted.

  Combustion gas generated by incineration of combustible waste contains ash particles, but the size of these particles varies depending on the physical properties of the incinerated materials, chemical changes associated with combustion reactions, combustion gas rises, etc. It depends on various factors. Generally, the ash that is produced by incineration of municipal waste varies depending on the type of incinerator, but the maximum particle size is about several tens to 100 microns, and the ash particles contained in the combustion gas that has passed through the melting furnace. Is almost 10 microns or less.

  The fluidized bed incinerator, which was used as an incineration facility for many municipal wastes before the gasification melting furnace was commercialized, is a highly reliable incineration technology, because it does not have a melting furnace, so silica of ash particles, Because there are many alumina and calcia components and the particle size of the dust accompanying the combustion gas is relatively large, there is little ash adhesion on the heat transfer surface of equipment used in heat recovery processes such as boilers, economizers, air preheaters, It never became a big problem.

  Further, in such a combustible waste treatment method, the combustion gas discharged from the combustion process does not pass through the melting furnace, so the shape of the ash particles in the combustion gas is discharged from the conventional fluidized bed incinerator. It is the same as the shape of the ash particles in the combustion gas, and even if heat recovery is performed in the heat recovery process, there is no risk that it will adhere to the heat transfer surface of the heat recovery facility and cause trouble.

  In the combustible waste treatment method described above, both the pyrolysis step and the combustion step are performed in a fluidized bed furnace, and the amount of heat required for the pyrolysis in the pyrolysis step is the manifestation of the fluidized medium in the fluidized bed furnace in which the combustion step is performed. It is characterized by being covered with heat.

  As described above, the amount of heat required for pyrolysis in the pyrolysis process is covered by the sensible heat of the fluidized medium in the fluidized bed furnace that carries out the combustion process, so an oxygen generator, etc., is required as an auxiliary combustion or oxygen source for combustion. In addition, running costs and initial costs are low.

  In the combustible waste treatment method, the pyrolysis step is maintained at 650 ° C. or lower, preferably 600 ° C. or lower, more preferably 550 ° C. or lower, and the temperature of the combustion step is 900 ° C. or lower, preferably 800 ° C. or lower. More preferably, the temperature is maintained at 700 ° C. or lower.

  As described above, in order to stably pulverize combustible waste such as municipal waste with little fluctuation, it is preferable to carry out at a low temperature of 650 ° C. or less, and by carrying out at 550 ° C. or less, more stable heat Decomposition gasification can be performed. Also, in the pyrolysis process, it is preferable to maintain a low temperature in order to stably burn combustible waste such as municipal waste with little fluctuation, and it is preferable to carry out at a low temperature of 700 ° C. or lower. In addition, at a high temperature of 900 ° C. or higher, there is a problem in heat resistance of a metal part such as a dispersion nozzle.

  In addition, the combustible waste treatment apparatus includes a pyrolysis chamber in which the combustible waste is pyrolyzed at a temperature of 350 ° C. or higher to obtain char and pyrolysis gas, an unpyrolyzed product generated from the pyrolysis chamber, tar A combustion chamber for burning char at a temperature of 500 ° C. or higher, a melting furnace for burning pyrolysis gas generated in the thermal decomposition chamber at 1200 ° C. or higher and melting ash accompanying the pyrolysis gas, and the combustion chamber A heat recovery device that recovers sensible heat until the combustion gas discharged from the reactor reaches 450 ° C. or less, and a dust collector that collects ash contained in the combustion gas downstream of the heat recovery device. The ash collected by the dust device is supplied to the melting furnace to be melted.

  As described above, since the combustion gas discharged from the combustion chamber does not pass through the melting furnace, the shape of the ash particles in the combustion gas is the same as the shape of the ash particles in the combustion gas discharged from the conventional fluidized bed incinerator. Similarly to the first aspect of the present invention, even if heat recovery is performed by the heat recovery device, there is no possibility that it will adhere to the heat transfer surface and cause trouble. In addition, the ash collected by the dust collector downstream of the heat recovery device is supplied to the melting furnace. For example, cyclones are used in the dust collector to collect and circulate the low-boiling substances and metal salts that have become fine particles. Without this, the slag conversion rate can be improved.

  In the combustible waste treatment apparatus, the pyrolysis chamber and the combustion chamber are both constituted by a fluidized bed furnace.

  As described above, the pyrolysis chamber and the combustion chamber are both composed of a fluidized bed furnace, which enables stable pyrolysis gasification of combustible waste in the pyrolysis chamber, and the combustion chamber becomes a fluidized bed incinerator. The combustion gas from here is the same as the shape of the ash particles in the combustion gas discharged from the conventional fluidized bed incinerator, and it adheres to the heat transfer surface of the equipment used even if heat recovery is performed in the heat recovery process There is no fear of trouble.

  In the combustible waste treatment apparatus, the fluidized bed furnace constituting the thermal decomposition chamber and the fluidized bed furnace constituting the combustion chamber are circulated.

  Since the fluidized medium in the fluidized bed furnace constituting the pyrolysis chamber and the fluidized bed furnace constituting the combustion chamber circulates as described above, unheated decomposition products, tar and char remaining in the fluidized bed in the pyrolysis chamber are It moves to the combustion chamber along with the fluid medium, and the unheated decomposition product, tar and char are combusted in the combustion chamber. Then, the fluidized medium in the fluidized bed of the combustion chamber heated by this combustion is moved to the thermal decomposition chamber and used as thermal decomposition gasification heat.

  The combustible waste treatment apparatus is characterized in that water vapor, carbon dioxide gas, nitrogen gas, or combustion exhaust gas is used as the fluidizing gas in the fluidized bed of the fluidized bed furnace constituting the thermal decomposition chamber.

  By using water vapor, carbon dioxide gas, nitrogen gas as the fluidizing gas of the fluidized bed of the fluidized bed furnace constituting the pyrolysis chamber as described above, there is no partial combustion of combustible waste supplied to the pyrolysis chamber, Since there is no heating of the fluid medium by this combustion, the heat of the fluid medium from the combustion chamber can be effectively absorbed. In addition, since there is no partial combustion of combustible waste in the pyrolysis chamber, a gas with a high calorific value is obtained from the pyrolysis chamber without the combustion gas being contained in the pyrolysis gas. Thus, high-temperature combustion at 1200 ° C. or higher can be performed without supplying auxiliary fuel in the melting furnace.

  As described above, according to the invention described in each claim, the following excellent effects can be obtained.

According to the first to third aspects of the present invention, heat is recovered from the first gas containing many particles having a large particle size, and then the second gas containing many particles having a small particle size is mixed. Due to the polishing function for polishing the heat transfer surface when a particle having a large particle size in the gas 1 collides with the heat transfer surface, the particle is likely to adhere to the heat transfer surface in the second gas, in particular. It is possible to provide a heat recovery method capable of preventing adhesion of small particles to the heat transfer surface.

According to invention of Claim 4 thru | or 5 , the 1st gas from a combustion chamber is introduce | transduced into a heat recovery apparatus, heat | fever is collect | recovered, pyrolysis gas from a thermal decomposition chamber is introduce | transduced into a melting furnace, and this melting | fusing Since the second gas discharged from the furnace is introduced into the heat recovery device, the first gas is a gas containing many particles having a large particle size, and therefore the polishing function when the particles collide with the heat transfer surface. Thus, it is possible to provide a method for treating a combustible material that can prevent the particles from adhering to the heat transfer surface.

According to the inventions described in claims 4 to 5 , the first gas containing a large amount of particles having a large particle diameter from the combustion chamber is introduced into the heat recovery device to recover the heat, and then the gas from which the heat has been recovered In addition, the heat recovery is performed by mixing the second gas containing many particles having a small particle size discharged from the melting furnace, so that the particles having a large particle size in the first gas collide with the heat transfer surface. A combustible treatment method that can further prevent particles from adhering to the heat transfer surface can be provided by the polishing function.

According to the invention described in claims 6 to 7 , the second gas containing many particles having a small particle diameter is provided downstream of the first inlet for introducing the first gas containing many particles having a large particle diameter. Since the second introduction port to be introduced is provided, due to the polishing function when the particles having a large particle size in the first gas introduced from the first introduction port collide with the heat transfer surface, the adhesion of the particles, particularly It is possible to provide a heat recovery system that can prevent adhesion of particles having a small particle diameter in the second gas that is easily introduced from the second introduction port. In addition, by providing the first inlet on the upstream side of the second inlet, the second gas containing many particles having a small particle size is cooled after the first gas containing many particles having a large particle size is cooled. As a result, gas is mixed in, and as a result, a region in which high-temperature gas containing particles having a small particle diameter that easily adheres to the heat transfer surface exists is not formed as much as possible.

According to the invention described in claims 8 to 13, the second gas discharged from the melting furnace is used as a transport gas for the particles further generated in the melting furnace, and the first gas is introduced into the heat recovery apparatus together with the particles. Since the gas introduction means for introducing the gas into the heat recovery apparatus is provided downstream of the gas flow with respect to the gas flow, the polishing function when particles having a large particle size in the first gas collide with the heat transfer surface is provided. it can provide a processing apparatus combustibles which can prevent the adhesion of the second grain terminal of gas discharged from the melting furnace including a small grain terminal of easy particle size adhering deposition of particles, in particular.

  Embodiments of the present invention will be described below with reference to the drawings. FIG. 3 is a diagram showing a process flow of the combustible waste treatment apparatus according to the present invention. As shown in the figure, the combustible waste treatment apparatus includes a gasification furnace 1, a melting furnace 2, a boiler 3, a heat recovery device 4 such as an economizer or an air preheater, a dust collector 5 such as a cyclone, a gas cooling tower 6, a bug The filter 7, the induction blower 8, the catalyst denitration tower 9, and the chimney 10 are provided. The gasification furnace 1 employs an integrated fluidized bed gasification furnace divided into a pyrolysis chamber 1-1 and a combustion chamber 1-2.

  The combustible waste is mainly supplied to the pyrolysis chamber 1-1 side of the gasification furnace 1, where it is pyrolyzed to generate pyrolysis gas, tar, char, fly ash and the like. Of these, pyrolysis gas G1 containing tar, char, fly ash, etc. not staying in the fluidized bed is all supplied to the melting furnace 2 and burned at a high temperature of 1200 ° C. or higher in the melting furnace 2, and the ash is melted. It becomes molten slag and is discharged out of the melting furnace 2.

  On the other hand, the pyrolysis residue remaining in the fluidized bed of the pyrolysis chamber 1-1 of the gasification furnace 1 flows into the combustion chamber 1-2 together with the fluidized medium. Fluidized air and secondary air are supplied so that the fluidized bed in the combustion chamber 1-2 is maintained at about 550 ° C. to 700 ° C., and the free board portion at the top of the fluidized bed is maintained at 850 ° C. to 950 ° C. The air ratio is maintained at 1 or more and complete combustion is performed. The combustion chamber 1-2 may only burn the pyrolysis residue that flows through the pyrolysis chamber 1-1, but the combustible waste is directly combustible depending on the pyrolysis characteristics and combustion characteristics of the combustible waste. Goods may be supplied.

  The combustion gas G2 emitted from the combustion chamber 1-2 of the gasification furnace 1 flows into the boiler 3 at a temperature of 850 ° C. to 950 ° C., cooled to about 700 ° C., and then discharged from the melting furnace 2. Is mixed with the combustion gas G3. At the mixing position at this time, the mixed gas is mixed at such a point that the gas temperature after mixing does not exceed 1100 ° C., preferably 1050 ° C., more preferably 1000 ° C.

  The mixed combustion gas G4 is cooled to about 450 ° C. by the boiler 3, further cooled to about 200 ° C. by a heat recovery device 4 such as an economizer or an air preheater, and dedusted by a dust collector 5 such as a cyclone. Is done. The ash 11 collected by the dust collector 5 is returned to the melting furnace 2 and melted in the melting furnace 2. A heat exchanger such as an economizer or an air preheater may be omitted, in which case dust is collected at a temperature of 450 ° C. or lower. The dust collection temperature is preferably 350 ° C. or less, more preferably 300 ° C. or less, and most preferably 250 ° C. or less. The conditions of 350 ° C. or lower are preferable because inexpensive carbon steel can be used as the material of the dust collector and the corrosion conditions are greatly relaxed. Further, as the temperature decreases to 300 ° C. or lower and 250 ° C. or lower, the probability that a low melting point metal exists in a solid state increases, so troubles due to low melting point metals in the dust collector are reduced. In the combustible waste treatment apparatus, the dust-burned combustion gas G4 is finally dedusted by the bag filter 7 through the gas cooling tower 6. In the present invention, this gas cooling tower is used. 6 can often be omitted.

  The combustion gas generated from incineration of combustible waste such as municipal waste, waste plastic, shredder dust, construction waste, and waste tires contains ash particles, but the size of these particles is It depends on various factors such as physical properties, chemical changes accompanying combustion reactions, and rising combustion gases. Generally, the ash that is generated by incineration of municipal waste varies depending on the type of incinerator, but the maximum particle size is about several tens of microns to 100 microns, but it is included in the combustion gas that has passed through the melting furnace 2. Ash particles are almost 10 microns or less.

  The fluidized bed incinerator, which was used as an incineration facility for many municipal wastes before the gasification melting furnace was commercialized, is a highly reliable incineration technology and has been introduced into the exhaust gas treatment process because it does not have a melting furnace. The ash particles contained in the exhaust gas contained a large amount of silica, alumina, and calcia components, and the particle diameter was relatively large. Therefore, ash adhesion to the heat transfer surface of equipment used in the heat recovery process such as a boiler, an economizer, and an air preheater is small and does not become a big problem.

  Since the combustion gas G2 discharged from the combustion chamber 1-2 of the gasification furnace 1 in the combustible waste treatment apparatus of this embodiment does not pass through the melting furnace 2, the properties and shapes of the ash particles in the combustion gas G2 are It is the same as the nature and shape of the ash particles in the combustion gas discharged from the conventional fluidized bed incinerator, and the transmission of equipment used in the heat recovery process of the heat recovery equipment 4 such as the boiler 3 and the economizer or the air preheater. There is no risk of sticking to the hot surface and causing trouble.

  The pyrolysis gas G1 from the pyrolysis chamber 1-1 of the gasification furnace 1 is combusted in the melting furnace 2, and the combustion gas G3 discharged from the melting furnace 2 passes through the melting furnace 2, so that the conventional gasification melting furnace is used. The combustion gas contains fine ash particles in the same manner as the combustion gas discharged from the gas. According to the results of tests conducted by the present inventors, the gasification furnace 1 is an integrated fluidized bed gasification furnace. When municipal waste is treated, the ratio of the amount of pyrolysis gas G1 from the pyrolysis chamber 1-1 and the amount of combustion gas G2 from the combustion chamber 1-2 is about 1: 3 and the combustion chamber Since the combustion gas G2 from 1-2 is more, the ash particle size distribution of the gas after mixing in the boiler 3 is relatively close to that of the conventional fluidized bed incinerator, such as the boiler 3 and the economizer or air preheater. There is a risk of causing trouble by adhering to the heat transfer surface of equipment used in the heat recovery process of the heat recovery equipment 4 Less.

  As described above, ash particles having a small particle size are mixed in the combustion gas G3 discharged from the melting furnace 2. Since the small particle size ash particles of the combustion gas G3 adhere to the heat transfer surface of the boiler 3, when only the combustion gas G3 is introduced into the boiler 3, the ash adhesion to the heat transfer surface is promoted. Then, the combustion gas G2 discharged | emitted from the combustion chamber 1-2 of the gasification furnace 1 is also introduce | transduced into the boiler 3. FIG. Since ash particles having a large particle size are mixed in the combustion gas G2, this ash particle having a large particle size has a function of polishing the portion when it collides with the heat transfer surface, and the adhesion of the ash particles. There is an effect to prevent. Therefore, when introducing the combustion gas G2 from the combustion chamber 1-2 and the combustion gas G3 from the melting furnace 2 into the boiler 3, the combustion gas G2 is introduced together with the combustion gas G3, or the combustion gas G2 is introduced. By providing the inlet upstream from the inlet of the combustion gas G3 and introducing the combustion gas G2 from the upstream side of the combustion gas G3, a region where only the combustion gas G3 into which ash particles having a small particle size are present does not exist. It is necessary to do so.

  Further, by providing the inlet for the combustion gas G2 upstream of the inlet for the combustion gas G3, the combustion gas G2 from the combustion chamber 1-2 is cooled in the boiler 3 and then the high temperature from the melting furnace 2 is increased. As a result, the combustion gas G3 is mixed, and as a result, a region where high-temperature gas containing molten slag particles that easily adhere to the heat transfer surface is present is not formed as much as possible.

  FIG. 4 is a diagram showing a process flow of another combustible waste treatment apparatus according to the present invention. As shown in the drawing, here, the ash 13 collected by the bag filter 12 disposed downstream of the gas cooling tower 6 is supplied to the melting furnace 2 and melted. In this case, if the total amount of the collected ash 13 is supplied to the melting furnace 2, fine ash is trapped in the system and may circulate. Therefore, the operation of the control valves V1 and V2 causes a part 13a of the ash 13 to be Pull out. Activated carbon 14 is added to the combustion gas G4 emitted from the bag filter 12 to adsorb harmful substances on the activated carbon 14, and the activated carbon 14 adsorbing the harmful substances is collected and removed by the bag filter 7.

  FIG. 5 is a diagram illustrating a configuration example of an integrated fluidized bed gasification furnace which is an example of the gasification furnace 1. The gasification furnace 1 includes a pyrolysis chamber 21 (corresponding to the pyrolysis chamber 1-1), a combustion chamber 22 (corresponding to the combustion chamber 1-2), and a heat recovery chamber 23. The combustible waste 34 supplied to the pyrolysis chamber 21 is pyrolyzed to generate pyrolysis gas, tar, char, fly ash and the like. The pyrolysis gas G1 containing tar, char, fly ash, etc. flows into the melting furnace 2 as shown in FIGS. Unheated decomposition products such as tar and char remaining in the fluidized bed of the pyrolysis chamber 21 flow into the combustion chamber 22 from the opening 26 of the partition wall 25 as indicated by an arrow A along with the fluidized medium. The unheated decomposition product such as char flowing from the thermal decomposition chamber 21 into the combustion chamber 22 in this manner is burned in the combustion chamber 22 to generate combustion gas G2, and the fluidized medium is heated by the combustion heat. The combustion gas G2 flows into the boiler 3 as shown in FIGS.

  The fluidized medium heated in the combustion chamber 22 and heated by the combustion of unheated decomposition products such as tar and char passes over the upper end of the partition wall 24 as shown by the arrow B and flows into the heat recovery chamber 23 to recover the heat. After being absorbed by the in-layer heat transfer tube 27 disposed so as to be positioned below the interface in the chamber 23 and cooled, the combustion chamber again passes through the lower opening 28 of the partition wall 24 as indicated by an arrow C. 22 flows in. Further, the fluid medium heated in the combustion chamber 22 flows into the settling chamber between the partition wall 29 and the partition wall 30 over the upper end of the partition wall 29 as indicated by an arrow D, and as indicated by an arrow E. It flows into the pyrolysis chamber 21 through the lower opening 31 of the partition wall 30.

  FIG. 6 is a diagram showing a configuration example of a two-column fluidized bed type fluidized bed gasification furnace which is an example of the gasification furnace 1. As shown in the figure, the gasifier 1 includes a pyrolysis fluidized bed furnace 41 (corresponding to the pyrolysis chamber 1-1) and a combustion fluidized bed furnace 42 (corresponding to the combustion chamber 1-2). The furnace is connected by two inclined pipes 43 and 44, and the fluid medium is circulated between the two layers through the inclined pipes 43 and 44, thereby supplementing the amount of heat necessary for thermal decomposition.

  That is, when combustible waste is supplied to the pyrolysis fluidized bed furnace 41, it is pyrolyzed to generate pyrolysis gas, tar, char, fly ash and the like. The pyrolysis gas G1 containing char, fly ash, etc. flows into the melting furnace 2 as shown in FIGS. The unheated decomposition product such as char remaining in the fluidized bed of the pyrolysis fluidized bed furnace 41 flows into the combustion fluidized bed furnace 42 through the inclined pipe 43 along with the fluidized medium, and combusts and burns here. The heated fluid medium is heated by the combustion heat, and the heated fluid medium flows into the pyrolysis fluidized bed furnace 41 through the inclined tube 44 and is used as a heat source for the pyrolysis of combustible waste. The

  The combustion gas G2 is supplied to the boiler 3 as shown in FIGS. In this two-column fluidized bed gasification furnace, the pyrolysis gas G1 contains no combustion gas, so that a pyrolysis gas G1 having a high gas calorific value is obtained. As the fluidized gas 45 in the fluidized bed of the pyrolysis fluidized bed furnace 41, a gas not containing oxygen, for example, water vapor, carbon dioxide, or nitrogen gas is used, and as the fluidized gas 46 in the fluidized bed of the combustion fluidized bed furnace 42, air. A gas containing oxygen such as is used.

  FIG. 7 is a diagram illustrating a configuration example of the melting furnace 2. The melting furnace 2 includes a primary combustion chamber 51, a secondary combustion chamber 52, and a tertiary combustion chamber 53. As shown in FIGS. 3 and 4, the pyrolysis gas G1 flows from the gasification furnace 1 into the primary combustion chamber 51 of the melting furnace 2, and the combustion gas (air, oxygen-enriched air, oxygen) 55 flows in. , Mixed while forming a swirl flow, burned and moved to the secondary combustion chamber 52 and combusted at a high temperature (1200 ° C. to 1400 ° C., preferably 1350 ° C.), and the combustion gas G 3 is a combustion gas 55 in the tertiary combustion chamber 53. And is completely burned and discharged as a combustion gas G3. As a result of this high-temperature combustion, the ash contained in the pyrolysis gas G1 is melted and discharged as molten slag 56 from the slag discharge port 57 to the outside of the furnace.

  FIG. 8 is a diagram showing a process flow of another combustible waste treatment apparatus according to the present invention. As shown in FIG. 4, as in FIG. 4, the ash 13 collected by the bag filter 12 disposed downstream of the gas cooling tower 6 is supplied to the melting furnace 2 and melted. In this case, if the total amount of the collected ash 13 is supplied to the melting furnace 2, fine ash is trapped in the system and may circulate. Therefore, the operation of the control valves V1 and V2 causes a part 13a of the ash 13 to be Pull out.

Melting furnace 2 Low calorie from the pyrolysis gas G1 from the pyrolysis chamber 1-1 of the gasification furnace ^{1 (1000~1500kcal / Nm 3 (dry} )) or medium calorie ^{(2500~4500kcal / Nm 3 (dry)} ) of It is a melting furnace for obtaining gas. When the pyrolysis gas G1 from the pyrolysis chamber 1-1 flows into the melting furnace 2 and is gasified at a high temperature at 1300 ° C. or higher, char and tar contained therein are completely gasified, and ash is melted as slag outside the furnace. Discharge. Here, the melting furnace 2 is supplied with gas selected from oxygen-enriched air, steam, oxygen or a mixed gas thereof separately or together into the furnace. The oxygen amount of this gasification gas is adjusted to the pyrolysis gas G1, and the total oxygen amount is in the range of 0.1 to 0.6 when the theoretical oxygen amount necessary for completely burning the object to be processed is 1. Then, the low calorie or medium calorie fuel gas G5 can be obtained from the melting furnace 2.

This low calorie or medium calorie fuel gas G5 contains many useful gas components such as CO and H ₂ . The fuel gas G5 from the melting furnace 2 is heat-recovered through the heat recovery device 15 and passed through the scrubber 16, whereby the industrial fuel gas or the chemical industry raw material gas 17 is obtained.

  The above example is one embodiment of the present invention, and the invention described in each claim is not limited to this, and within the scope of the same technical idea as the invention described in each claim. Variations are possible.

It is a figure which shows the process flow of the conventional combustible waste processing apparatus. It is a figure which shows the process flow of the conventional combustible waste processing apparatus. It is a figure which shows the process flow of the combustible waste processing apparatus which concerns on this invention. It is a figure which shows the process flow of the combustible waste processing apparatus which concerns on this invention. It is a figure which shows the structural example of the integrated fluidized bed gasification furnace used for the combustible waste processing apparatus which concerns on this invention. It is a figure which shows the structural example of the two-column type fluidized bed gasification furnace used for the combustible waste processing apparatus which concerns on this invention. It is a figure which shows the structural example of the melting furnace used for the combustible waste processing apparatus which concerns on this invention. It is a figure which shows the process flow of the combustible waste processing apparatus which concerns on this invention.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Gasification furnace 2 Melting furnace 3 Boiler 4 Heat recovery equipment 5 Dust collector 6 Gas cooling tower 7 Bag filter 8 Attraction blower 9 Catalytic denitration tower 10 Chimney 11 Ash 12 Bag filter 13 Ash 14 Activated carbon 15 Boiler 16 Scrubber 17 Raw material gas 21 Pyrolysis chamber 22 Combustion chamber 23 Heat recovery chamber 24 Partition wall 25 Partition wall 26 Opening 27 Heat transfer tube in the layer 28 Lower opening 29 Partition wall 30 Partition wall 31 Lower opening 32 Fluidized gas 33 Fluidized gas 41 Pyrolysis fluidized bed furnace 42 Combustion Fluidized Bed Furnace 43 Inclined Tube 44 Inclined Tube 45 Fluidized Gas 46 Fluidized Gas 51 Primary Combustion Chamber 52 Secondary Combustion Chamber 53 Tertiary Combustion Chamber 55 Combustion Gas 56 Molten Slag 57 Slag Discharge Port

Claims (13)

Combustible material is supplied to a fluidized bed gasification furnace composed of a pyrolysis chamber and a combustion chamber, and the combustible material is pyrolyzed in the pyrolysis chamber to generate a pyrolysis gas and a pyrolysis residue. The residue is burned in the combustion chamber, and a first gas containing a large amount of large particles generated in the combustion chamber is generated.
The pyrolysis gas generated in the pyrolysis chamber is introduced into a melting furnace and burned to melt the ash to generate a second gas containing a large number of small particles,
Introducing into the heat recovery device having a heat transfer surface for direct heat exchange of the first gas, heat is exchanged between the introduced gas and the heat receiving fluid, heat is recovered,
Next, the second gas is introduced into the heat recovery device downstream from the portion where the first gas is introduced into the heat recovery device with respect to the gas flow, and the second gas is added to the first gas. A heat recovery method characterized by mixing heat and recovering heat. The heat recovery method according to claim 1 , wherein the char remaining in the fluidized bed of the pyrolysis chamber is introduced into the combustion chamber along with the fluidized medium and burned, and the fluidized medium heated from the combustion chamber is combusted. A heat recovery method characterized by flowing into a pyrolysis chamber for thermal decomposition. 3. The heat recovery method according to claim 1 , wherein after mixing the first gas and the second gas, the mixture is cooled to 450 ° C. or lower, and then a solid content in the mixed gas is separated by a dust collector. A heat recovery method, wherein the separated solid content is introduced into the melting furnace and melted. Supplying combustible materials to a fluidized bed gasifier consisting of a pyrolysis chamber and a combustion chamber ;
Pyrolyzing the combustible in a pyrolysis chamber to produce pyrolysis gas and pyrolysis residue ;
Burning the pyrolysis residue in the combustion chamber, generating a first gas containing a large number of large particles in the combustion chamber ;
The pyrolysis gas generated in the pyrolysis chamber is introduced into a melting furnace and burned to melt the ash to generate a second gas containing many small particles ,
Introducing into the heat recovery device having a heat transfer surface for directly exchanging the first gas from the combustion chamber , heat exchange is performed between the introduced gas and the heat receiving fluid, heat recovery ,
The first gas is introduced into the heat recovery device downstream of the first gas and the second gas to the flow of gas than portions introduced into the heat recovery device to be discharged from the pre-Symbol melting furnace A method for treating a combustible material, wherein the heat is recovered by mixing with a mixture. 5. The method for treating a combustible material according to claim 4 , wherein the first gas and the second gas are heat-recovered by the heat recovery device, cooled to 450 ° C. or lower, and then collected by the dust collector. A method for treating a combustible material, comprising: separating a solid content, introducing the separated solid content into the melting furnace, and melting the solid content. Combustible materials by thermal decomposition, is composed of a combustion chamber to produce a first gas containing a large amount of large particles having a particle size by burning the pyrolysis residue and pyrolysis chamber to produce pyrolysis gas and pyrolysis residue and fluidized-bed gasification furnace,
Melting furnace to produce a second gas to melt the ash included in the pyrolysis gas stream is combusted by introducing pyrolysis gas produced by the pyrolysis chamber to the melting furnace containing a large amount of small particles of particle size When,
A first inlet for directly introducing the first gas from the fluidized bed gasification furnace; and a second inlet for directly introducing the second gas from the melting furnace. A discharge port for discharging, a heat recovery device for recovering heat by exchanging heat between the gas introduced from the first and second inlets and the heat receiving fluid;
Together with the heat recovery device comprises a heat transfer surface for heat exchange with the gas introduced with the heat receiving fluid, to the downstream side against the Re said first flow of gas introduced from the inlet of the A heat recovery system provided with a second introduction port. The heat recovery system according to claim 6 , wherein after mixing the first gas and the second gas, after cooling to 450 ° C. or less, the solid content in the mixed gas is separated by a dust collector, and separated. A heat recovery system, wherein the solid content is introduced into the melting furnace and melted. Combustible material supplied from the combustible material supply means for supplying combustible material is thermally decomposed to generate a pyrolysis gas and a pyrolysis residue, and the pyrolysis residue is burned to contain a large number of large particles. A fluidized bed gasification furnace composed of a combustion chamber for generating a first gas ;
A heat recovery device having a heat transfer surface for directly introducing the first gas generated in the combustion chamber and exchanging heat with the heat receiving fluid to recover the heat;
Combustible material provided with a melting furnace for introducing a pyrolysis gas generated in the pyrolysis chamber and burning it to melt the ash in the pyrolysis gas and generate a second gas containing a large number of small particles In the processing apparatus of
The second gas discharged from the melting furnace is used as a transport gas for the particles further generated in the melting furnace, and the gas flows more than the portion where the first gas is introduced into the heat recovery apparatus together with the particles. A combustible material processing apparatus comprising gas introducing means for introducing the heat recovery apparatus downstream. The combustible material processing apparatus according to claim 8 , wherein the first gas is introduced into a heat recovery device to recover heat, and the heat recovered gas is discharged from the melting furnace to the second furnace . An apparatus for treating a combustible material, comprising at least means for recovering heat by mixing the gas. In the processing apparatus of combustibles according to claim 8 or 9, pre-Symbol processor combustibles which the fluidized medium characterized by comprising a means for moving the pyrolysis chamber from the combustion chamber. The combustible material processing apparatus according to claim 10 , wherein the second gas from the pyrolysis chamber is introduced into the melting furnace, and the first gas from the combustion chamber is introduced into the heat recovery device. An apparatus for treating a combustible material, characterized by comprising means for the above. The combustible material processing apparatus according to any one of claims 8 to 11 , wherein the heat recovery device is a waste heat boiler. The combustible material processing apparatus according to any one of claims 8 to 12 , wherein the first gas and the second gas are mixed, cooled to 450 ° C or lower, and then mixed with the dust collector. A combustible material processing apparatus, comprising: separating a solid content therein; introducing the separated solid content into the melting furnace;

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