JP5901809B2 - Solid fuel production method and production plant - Google Patents

Description

  The present invention relates to a solid fuel manufacturing method and a manufacturing plant using organic waste such as excess sludge.

  Sewage sludge contains more than 99 wt% (percentage by mass) of water and has a strong odor. Most of the sewage sludge is made into surplus sludge through an aeration process and a precipitation process using the activated sludge method, and then landfilled as industrial waste. Final disposal such as incineration is carried out.

  In recent years, with increasing consideration for the global environment, soil pollution due to surplus sludge reclamation and carbon dioxide emissions into the atmosphere due to incineration of surplus sludge have become problems. In relation to these problems, the production of solid fuel using surplus sludge as a material is expected to reduce the amount of surplus sludge landfilled or reduce carbon dioxide emissions by replacing it with fossil fuel.

  Conventionally, as a method for producing solid fuel using sewage sludge, after drying the sewage sludge to a water content of 0 to 50 wt%, carbonization is performed at a temperature of 250 to 500 ° C. to form sludge carbide. And the technique of mixing waste oil etc. with this sludge carbide and granulating is proposed (refer patent document 1). In the said drying process, after processing a sewage sludge with dehydrators, such as a filter press, and making it a dehydrated sludge, it is dried with the sun or a dryer etc., and the water content is adjusted to 0-50 wt%. In the carbonization process, a screw carbonization furnace, a rotary kiln carbonization furnace, or the like is used.

JP 2006-152097 A

  However, in the conventional method for producing a solid fuel, the sewage sludge is dehydrated with a filter press and then dried with sun or a drier in the drying process. The odor that diffuses when dried with may cause adverse effects on the surrounding environment. In addition to the dehydrator, a sun dryer or a dryer is used for the drying process, so it takes time and labor. In particular, there is a problem that it takes time when performing sun drying. In addition, when a dryer is used for the drying process, since fossil fuel is generally used to generate heat for drying, there are problems that fuel cost increases and carbon dioxide emissions are large. Further, in the carbonization treatment, if fossil fuel is used as the fuel for the carbonization furnace, there are problems that the fuel cost increases and the amount of carbon dioxide emission is large. In this case, there is a problem that the effect of reducing carbon dioxide emissions by using waste is reduced.

  Therefore, the problem of the present invention is that the drying and carbonization of organic waste can be performed in a relatively short time and with a small number of processes while deodorizing, and the amount of fossil fuel used can be reduced. It is to provide a solid fuel manufacturing method and a manufacturing plant that can reduce carbon dioxide emissions and carbon dioxide emissions.

In order to solve the above problems, the solid fuel production method of the present invention includes a reduced-pressure drying step in which organic waste is added with microorganisms and heated in a reduced-pressure environment to form a dried organic matter.
A condensation step of condensing moisture evaporated from the organic waste in the vacuum drying step;
In the condensation process, water is cooled, and the cooling water to which microorganisms are added is mixed with the condensed water produced in the condensation process and the gas containing the odor produced in the reduced pressure drying process, and the cooling water is cooled. A mixing and cooling step;
A carbonization step of heating the dry organic matter in a low oxygen environment to form an organic carbide and generating a combustible gas;
A combustion step of burning the combustible gas generated from the dried organic matter in the carbonization step as a fuel for heating in the vacuum drying step or the carbonization step;
And a mixed molding step of mixing and molding the organic carbide with a binder.

  According to the above configuration, in the reduced pressure drying step, the organic waste is added with microorganisms and heated in a reduced pressure environment to form a dried organic matter. Since microorganisms are added to organic waste and heated in a reduced pressure environment, even if the organic waste has a water content exceeding 90 wt%, such as excess sludge, the odor is suppressed by the action of microorganism decomposition. It can be dried at a relatively low heating temperature by lowering the boiling point. In this way, lowering the boiling point due to reduced pressure makes it possible to lower the heating temperature for drying, so it is possible to use less fuel for heating and prevent the death of microorganisms added to organic waste. And the odor reduction effect can be stably achieved. Here, organic waste refers to a wide variety of industrial production processes, wastewater treatment, or waste that is discharged from urban infrastructure and contains organic matter. For example, excess sludge generated by sludge treatment by the activated sludge method This includes sludge deposited on the bottom of lakes and seas, waste discharged from the agriculture and fisheries industry, food residues discharged from food factories, and garbage discharged from ordinary households.

  Here, in the vacuum drying step, the amount of combustible gas generated from the organic waste can be suppressed by relatively reducing the heating temperature of the organic waste. By suppressing the amount of flammable gas produced in the vacuum drying step, a large amount of flammable gas can be collected in the carbonization step after the vacuum drying step. Therefore, combustible gas can be efficiently generated and collected from organic waste, and it is generated from organic waste in a combustion process in which this combustible gas is burned as fuel for heating in a vacuum drying process or carbonization process. A large amount of the combustible gas produced can be used. That is, the ratio of using the combustible gas generated in the carbonization step can be increased with respect to the fuel necessary for the heating in the vacuum drying step and the carbonization step. As a result, the fossil fuel newly used for the heating can be reduced. As a result, fuel costs can be reduced, and emissions of greenhouse gases and air pollutants associated with the use of fossil fuels can be reduced. Moreover, since the combustible gas produced | generated from organic waste is burned, the odor of organic waste can be reduced effectively.

  Moreover, the water | moisture content evaporated from the organic waste at the said decompression drying process is condensed by a condensation process. The cooling water used in this condensing step, to which the microorganisms are added, is mixed with the condensate water generated in the condensing step and the gas containing the odor generated in the depressurizing drying step. Cool this cooling water. Thereby, while cooling cooling water, the odor contained in condensed water and gas can be decomposed | disassembled by the microorganisms of cooling water and deodorized. Accordingly, it is possible to promote the drying of the organic waste in the reduced pressure drying process and to effectively prevent the diffusion of the odor caused by the drying of the organic waste.

  As described above, according to the method for producing a solid fuel of the present invention, organic waste having a high water content and strong odor, such as excess sludge, can be efficiently and quickly consumed by relatively inexpensive fuel consumption. It is possible to produce a solid fuel with less odor by reducing emissions of greenhouse gases and air pollutants and further drying and carbonizing while preventing odor diffusion.

  In the carbonization step, the low oxygen environment means that the oxygen concentration in the atmosphere where the dry organic matter is placed is 5% or more and 12% or less by volume. Moreover, in the said carbonization process, it is preferable that the heating temperature of dry organic substance is 350 degreeC or more and 500 degrees C or less, and it is preferable that the heating time of dry organic substance is 5 minutes or more and 10 minutes or less. Depending on the conditions of oxygen concentration, heating temperature, and heating time, the dried organic material can be carbonized, and a combustible gas containing, for example, hydrogen, carbon monoxide, and methane can be generated from the dried organic material.

  The manufacturing method of the solid fuel of one Embodiment utilizes the excessive heat of the heating in the said carbonization process for the heating in the said pressure reduction drying process.

  According to the embodiment, the combustible gas generated from the dry organic matter in the carbonization step is burned in the combustion step as a heating fuel in the carbonization step, and the excess heat of heating in the carbonization step is reduced in the vacuum drying step. By using it for heating, heat can be stably supplied to the reduced-pressure drying process that requires a larger amount of heat than the carbonization process. Moreover, wasteful consumption of heat can be reduced as a whole solid fuel production method.

  The manufacturing method of the solid fuel of one Embodiment is provided with the combustion air supply process which supplies the gas produced in the said pressure reduction drying process as combustion air for the heating of the organic waste in this pressure reduction drying process.

  According to the above embodiment, the gas generated in the reduced pressure drying step is supplied to a heat source device such as a burner as combustion air for heating the organic waste in the reduced pressure drying step, whereby the odor component of the gas is supplied. It can be burned with fuel to remove odors produced in the vacuum drying process.

The method for producing a solid fuel according to an embodiment includes a granulation step of granulating the dry organic matter formed in the vacuum drying step before the carbonization step,
In the carbonization step, the granulated dry organic matter is heated.

  According to the said embodiment, since the dry organic substance formed at the pressure reduction drying process is granulated by a granulation process, a dry organic substance is solidified and powdery dry organic substance decreases. Therefore, in the carbonization step of heating the granulated dry organic matter, the amount of powdered dry organic matter and organic carbide discharged together with the exhaust gas is reduced. As a result, it is possible to reduce the loss that occurs during the formation of the organic carbide from the dry organic material, and to increase the yield of the organic carbide. In addition, since the powder discharged together with the exhaust in the carbonization step can be reduced, the dust collector that collects the powder from the exhaust can be reduced in size, and the maintenance of the dust collector can be reduced. As a result, it is possible to reduce costs and labor related to dust collection in the carbonization process.

  In addition, granulation of dry organic substance means forming the dry organic substance formed in the reduced pressure drying step into solid particles of 2 mm or more and 8 mm or less. Granulation can be performed by a granulator such as a so-called pellet mill.

The solid fuel production plant of the present invention is a reduced-pressure drying apparatus that heats organic waste to which microorganisms are added in a reduced-pressure environment to form a dried organic matter,
A carbonization device that heats the dried organic matter in a low oxygen environment to form an organic carbide and generate a combustible gas;
The organic carbide is formed by mixing with a binder and forming, and forming a solid fuel,
The reduced-pressure drying apparatus includes a casing in which organic waste is introduced and decompresses the inside, a stirring unit that is rotatably disposed in the casing and stirs the organic waste, and is disposed in at least a part of the casing for organic waste. A heating unit that heats the product, a condensing unit that condenses the vapor from the organic waste, cooling water supplied to the condensing unit to which microorganisms are added, condensed water generated in the condensing unit, and the organic A suction pump for sucking a gas containing odor generated by drying waste from the casing, and a mixing cooler for mixing the cooling water with the condensed water sucked by the suction pump and the gas and cooling the cooling water And
For heating at least one of the reduced-pressure drying apparatus and the carbonization apparatus, a combustible gas generated from a dried organic substance in the carbonization apparatus is used as a fuel.

  According to the said structure, the organic waste to which microorganisms were added is heated by a reduced pressure drying apparatus in a reduced pressure environment, and a dry organic matter is formed. That is, organic waste is put into a casing whose inside is decompressed, and this organic waste is heated by the heating unit and stirred by the stirring unit. Since microorganisms are added to organic waste and heated in a reduced pressure environment, even if the organic waste has a water content exceeding 98 wt%, such as excess sludge, the odor is suppressed by the action of microorganism decomposition. In addition, the boiling point is lowered and drying is performed at a relatively low heating temperature. As described above, since the heating temperature by the heating unit can be relatively lowered due to the decrease in boiling point due to the reduced pressure, the fuel used for the heat source device of the heating unit can be relatively reduced and the microorganisms added to the organic waste can be killed. This can be prevented, and the effect of reducing odor can be stably achieved. Here, organic waste refers to a wide variety of industrial production processes, wastewater treatment, or waste that is discharged from urban infrastructure and contains organic matter. For example, excess sludge generated by sludge treatment by the activated sludge method This includes sludge deposited on the bottom of lakes and seas, waste discharged from the agriculture and fisheries industry, food residues discharged from food factories, and garbage discharged from ordinary households.

  The said reduced pressure drying apparatus can suppress the production amount of the combustible gas from the said organic waste by setting the heating temperature of the organic waste by a heating part comparatively low. By suppressing the amount of flammable gas produced during the treatment by the reduced pressure drying apparatus, a large amount of flammable gas can be collected when the dry organic matter is treated by the carbonization apparatus. Therefore, it is possible to efficiently generate and collect combustible gas from organic waste. When this combustible gas is burned as fuel for heating a vacuum drying apparatus or as fuel for heating a carbonization apparatus, In addition, a large amount of combustible gas generated from organic waste can be used. That is, it is possible to increase the ratio of using the combustible gas generated in the carbonization apparatus with respect to the fuel necessary for heating the vacuum drying apparatus and the carbonization apparatus. As a result, it is possible to reduce the fossil fuel newly used for heating the vacuum drying apparatus and the carbonization apparatus. As a result, fuel costs can be reduced, and carbon dioxide emissions associated with the use of fossil fuels can be reduced. Moreover, since the combustible gas produced | generated from organic waste is burned, the odor of organic waste can be reduced effectively.

  Moreover, in the said reduced pressure drying apparatus, the water | moisture content evaporated from the organic waste is condensed in a condensation part. The condensed water sucked by the suction pump and the gas in the casing are mixed and cooled by the mixing cooler to the cooling water supplied to the condensing unit and added with microorganisms. Thereby, while cooling water, it can decompose and deodorize condensed water and gaseous odor with the microorganisms of cooling water. Therefore, drying of organic waste can be promoted, and odor diffusion that occurs with drying of organic waste can be effectively prevented.

  As described above, according to the solid fuel production plant of the present invention, for example, organic waste having a high water content and strong odor, such as excess sludge, can be efficiently and quickly dried to reduce the amount of fuel consumed. Originally, it can be carbonized while suppressing the generation of greenhouse gases such as carbon dioxide and the generation of air pollutants such as nitrogen oxides, and while preventing the spread of odors during processing by the vacuum drying device and the carbonization device, A solid fuel with less odor can be produced.

  In the carbonization process by the carbonization apparatus, the low oxygen environment means that the oxygen concentration in the atmosphere in which the dry organic matter is placed is 5% or more and 12% or less by volume. In the carbonization step using the carbonization apparatus, the heating temperature of the dried organic material is preferably 350 ° C. or more and 500 ° C. or less, and the heating time of the dried organic material is preferably 5 minutes or more and 10 minutes or less. Depending on the conditions of oxygen concentration, heating temperature, and heating time, the dried organic material can be carbonized, and a combustible gas containing, for example, hydrogen, carbon monoxide, and methane can be generated from the dried organic material.

  The solid fuel manufacturing plant according to an embodiment supplies and uses surplus heat when the dry organic matter is heated by the carbonization apparatus to the heating unit of the vacuum drying apparatus.

  According to the above-described embodiment, the combustible gas generated from the dry organic matter in the carbonization device is burned as a fuel for heating the dry organic matter in the carbonization device, and excess heat generated when the carbonization device is heated is reduced in pressure. Supplying heat to the heating unit of the drying device to supply heat stably to the vacuum drying device for drying organic waste that requires more heat than carbonizing dry organic matter. Can do. Moreover, wasteful consumption of heat can be reduced as a whole solid fuel production plant.

  The solid fuel production plant of one embodiment sucks the gas in the casing of the vacuum drying apparatus, and supplies the sucked gas as combustion air to the heat source device for heating of the vacuum drying apparatus. Provide a pump.

  According to the above embodiment, the gas generated in the reduced pressure drying apparatus is supplied as combustion air to the heat source device for heating of the reduced pressure drying apparatus by the second suction pump, whereby the odor component of the gas is combusted together with the fuel. Thus, the odor generated in the vacuum drying apparatus can be removed.

  A solid fuel production plant according to an embodiment includes a granulation device that is formed by the reduced-pressure drying device and granulates dry organic matter before being charged into the carbonization device.

  According to the said embodiment, since the dry organic substance formed with the reduced pressure drying apparatus is granulated with a granulation apparatus, dry organic substance is solidified and powdery dry organic substance decreases. Therefore, when the granulated dry organic matter is heated by the carbonization apparatus, the amount of powdered dry organic matter and organic carbide discharged together with the exhaust gas is reduced. As a result, it is possible to reduce the loss that occurs during the formation of the organic carbide from the dry organic material, and to increase the yield of the organic carbide. In addition, since the powder discharged from the carbonization device together with the exhaust gas is small, the dust collector that collects and removes the powder from the exhaust gas can be reduced in size, and the maintenance of the dust collector can be reduced. As a result, it is possible to reduce costs and labor related to dust collection of exhaust gas from the carbonizer.

  In addition, granulation of a dry organic substance means forming the dry organic substance formed with the reduced pressure drying apparatus into the solid particle | grains of 2 mm or more and 8 mm or less. For example, a granulator such as a pellet mill can be used as the granulating device.

  In one embodiment of the solid fuel production plant, the binder includes at least one of a wood material, a paper material, and a plastic material.

  According to the above-described embodiment, a solid fuel capable of stably holding a shape can be manufactured by mixing and molding a binder containing at least one of a wood material, a paper material, and a plastic material with an organic carbide.

  In the solid fuel production plant according to an embodiment, the powder of the wood material is added to the organic waste processed by the vacuum drying apparatus.

  According to the above embodiment, by adding the wood material powder to the organic waste, it is possible to reduce the amount of water to be processed by the reduced pressure drying apparatus, and to quickly generate the dry organic matter. As the wood material powder, sawdust obtained by pulverizing waste wood, thinned wood, or the like can be used.

It is a block diagram which shows the structure of the manufacturing plant of the solid fuel of embodiment. It is a schematic diagram which shows the structure of a mixed waste processing line. It is a schematic diagram which shows the principal part of a rocking | fluctuation type separator. It is a schematic diagram which shows the principal part of a wind power sorter. It is a schematic diagram which shows a washing | cleaning dehydrator. It is a schematic diagram which shows an optical sorter. It is a schematic diagram which shows the structure of an organic waste processing line. It is a schematic diagram which shows the structure of a reduced pressure fermentation drying apparatus. It is a longitudinal cross-sectional view which shows the inside of the casing of a reduced pressure fermentation drying apparatus. It is a schematic diagram which shows a mixing cooler. It is a schematic cross section which shows a carbonization apparatus. It is a schematic diagram which shows the structure of a woody waste processing line. It is a schematic diagram which shows the structure of a solid fuel manufacturing line. It is sectional drawing which shows a part of screw type shaping | molding apparatus. It is a schematic diagram which shows a ring die type shaping | molding apparatus.

  DESCRIPTION OF EMBODIMENTS Hereinafter, embodiments of a solid fuel production plant of the present invention will be described in detail with reference to the accompanying drawings.

  The solid fuel manufacturing plant of the present embodiment processes organic waste to produce organic carbide, and also processes mixed waste in which combustibles and non-combustibles are mixed to extract combustibles. FIG. 1 is a block diagram showing an overall configuration of a solid fuel production plant in which a solid fuel is produced by mixing a combustible material with a carbide as a binder. As shown in FIG. 1, a solid fuel production plant 1 includes a mixed waste processing line 2 for processing mixed waste, an organic waste processing line 3 for processing organic waste, and a wooden waste processing line 4. A solid fuel production line 5 for producing solid fuel and a steam boiler 6 for supplying steam to the organic waste treatment line 3 are provided.

  The mixed waste processing line 2 mainly processes general waste discharged from homes and offices, and is put in a state where combustible and non-combustible materials are mixed. Here, combustible materials include, for example, plant-derived waste materials such as waste paper, natural fibers, and waste wood, and waste plastics such as chemical cloth, food trays, vinyl bags, toys, and stationery. Incombustible materials are, for example, metal products, ceramics, glass bottles, and the like. It should be noted that the combustible material and the non-combustible material may be input in a state of being separately collected, or may be input in a state of being mixed and collected. When the waste is separated, the plant-derived waste and the waste plastic among the combustibles may be further separated or mixed. The mixed waste treatment line 2 separates the combustible material and the incombustible material that have been input, and extracts the combustible material by washing and drying. The combustible material extracted in the mixed waste treatment line 2 is used as a binder for the solid fuel produced in the solid fuel production line 5.

  The organic waste treatment line 3 is for treating organic waste, and in particular, treats high-moisture organic waste whose water content exceeds approximately 80 wt%. Examples of organic waste include excess sludge, food residues discharged from food factories, sludge accumulated on the bottom of lakes and seas, and the like. This organic waste treatment line 3 ferments and dries organic waste in a reduced pressure environment to produce dry organic matter having a water content of approximately 50 wt% or less. Further, in the organic waste treatment line 3, the dry organic matter is carbonized to form an organic carbide. In the present embodiment, the organic waste carbonization method of the present invention is performed in the organic waste treatment line 3. The organic waste treatment line 3 treats excess sludge as organic waste, but garbage or the like may be input in addition to the excess sludge. The organic carbide formed in the organic waste treatment line 3 is used as a solid fuel material produced in the solid fuel production line 5.

  Moreover, the organic waste processing line 3 produces | generates a combustible gas by performing a drying process and a carbonization process to organic waste. This combustible gas contains hydrogen, carbon monoxide, methane, and the like depending on the material of the organic waste. This combustible gas is used as a fuel for heating the carbonization apparatus in the organic waste treatment line 3 and also supplied to the steam boiler 6 as a fuel.

  The woody waste treatment line 4 is for treating woody waste, and waste wood such as thinned wood, thinned wood, and wood timber scraps generated by the dismantling of the building is input. The wooden waste treatment line 4 crushes the wooden waste to form wooden chips and sawdust. The sawdust formed in the wood waste treatment line 4 is mixed with the organic waste treated in the organic waste treatment line 3. The wood chip formed in the wood waste treatment line 4 is used as a wood material in the solid fuel production line 5 and also used as a fuel for the steam boiler 6. Here, the sawdust mixed with the organic waste has a diameter of approximately 4 mm or less, preferably 2.5 mm or less. The solid wood material and the wood chip used as the fuel for the steam boiler 6 have a diameter of approximately 2 to 20 mm.

  The solid fuel production line 5 is formed by mixing the organic carbide generated in the organic waste treatment line 3 with the combustible material including waste plastic extracted from the mixed waste treatment line 2 and plant-derived waste as a binder, and molding the mixture. Thus, solid fuel is produced, and RPF (waste paper waste plastic fuel) as solid fuel is produced. A part of the RPF produced in the solid fuel production line 5 is used as fuel for the steam boiler 6.

  Here, the solid fuel production line 5 is composed of the organic carbide generated in the organic waste treatment line 3 and the waste plastic and plant-derived waste extracted in the mixed waste treatment line 2 in the following proportions. To produce RPF. The plant-derived waste may include a wood chip generated in the wood waste treatment line 4. As an example of the blending ratio of materials for producing RPF, organic carbide is approximately 40 wt%, waste plastic is approximately 40 wt%, and plant-derived waste is approximately 20 wt%. RPF with this blending ratio can generate a calorific value of about 6500 kcal / kg, and has sufficient utility as fuel for various boilers and burners. In addition, when the amount of heat equivalent to coal is sufficient, organic carbide is approximately 60 wt%, waste plastic is approximately 30 wt%, and wood scrap and / or paper scrap may be approximately 10 wt%. The produced RPF has a calorific value of about 5500 kcal / kg.

  The steam boiler 6 generates steam as a heating medium for drying the organic waste in the organic waste treatment line 3, the RPF produced in the solid fuel production line 5, and the wooden waste treatment line 4. And at least one of the combustible gas generated in the organic waste treatment line 3 is used. The steam boiler 6 is supplied with excess heat when carbonizing the dry organic matter in the organic waste treatment line 3 by supplying a high-temperature gas as a heat medium.

  Hereinafter, the configuration of each line and the details of processing performed in each line will be described for each line.

  FIG. 2 is a schematic diagram showing the configuration of the mixed waste treatment line 2. In the mixed waste processing line 2, waste discharged from a home or office is first received by the rough crusher 21. The rough crusher 21 performs rough crushing of waste. When the waste is wrapped in a bag or a container, the rough crusher 21 breaks the bag or the container and breaks the waste into pieces. . The rough crusher 21 accommodates a rotor that is rotationally driven in a casing having a hopper with an inclined side plate that forms a processing space narrowed downward. The rotor has a sack-shaped bag breaking blade arranged in a plurality in the longitudinal direction, and is supported by a bearing at the upper part of the central portion of the upper partition plate arranged in the transverse direction between the bag breaking blades. Below the upper partition plate, a lower partition plate is provided in which a plurality of fixed blade longitudinal members are fixed on an arc surface to form a rough screen. A known hammer crusher or rotary screw crusher may be used as the rough crusher 21. The screw crusher may be either a biaxial type or a uniaxial type.

  The magnetic material such as iron is removed by the magnetic separator 22 while the waste roughly crushed by the rough crusher 21 is being conveyed by the conveyor. The waste from which the magnetic material has been removed is supplied to a uniaxial crusher 23 and crushed to a size of about 150 mm. The waste crushed by the crusher 23 is supplied to the swing type separator 24.

  In the oscillating type separator 24, it is sorted into a lightweight article, a heavy article, and a small-diameter article. A lightweight thing is a thing with comparatively small bulk specific gravity, and among combustibles, sheet-like or plate-like paper, cloth, fiber waste, etc. are contained. Moreover, a sheet-like or thin plate-like resin is contained among waste plastics. A heavy object has a relatively large bulk specific gravity, and includes a piece of wood among combustible substances. In addition, the waste plastic includes a resin container and a bottle. In addition, among non-combustible materials, metals, ceramics, glass and the like having relatively large dimensions are included. Small diameter objects have a relatively large true specific gravity and a small diameter, and include metal grains, ceramic grains, earth and sand, and the like.

  As shown in FIG. 3, the oscillating type separator 24 is provided with a plurality of strip-shaped sieve plates that are installed to be inclined in the longitudinal direction and oscillate so as to feed waste from the bottom to the top. 241 and a crank mechanism 244 that receives the rotational force of the motor 242 via the chain 243 and drives the strip-shaped sieve plate 241 to swing. On the strip-shaped sieve plate 241, a plurality of protrusions 245 for feeding the object to be processed (waste) are provided. As shown by the arrow W1, the waste thrown into the casing in which the main part of the oscillating type sorter 24 is accommodated from the upper side is shown by the arrow W2. On the other hand, the heavy article moves by its own weight to the lower end of the strip-shaped sieve plate 241 as shown by an arrow W3, and the small-diameter article moves downward from the sieve mesh of the strip-like sieve plate 241 as shown by an arrow W4. Fall. In this way, the waste is separated into light, heavy, and small-diameter items. Small-diameter objects are discarded after being stored in the tray.

  The heavy goods separated by the swing type separator 24 are crushed by the single-shaft crusher 25 and then conveyed by the screw conveyor 26. A wind sorter 27 is provided at the end of the screw conveyor 26, and a crushed material is a lightweight piece such as a plastic piece or a wood piece, which is a crush of a resin container or a bottle, a piece of ceramic, a piece of glass or a piece of metal. And so on. As shown in FIG. 4, the wind power sorter 27 is continuously supplied with crushed material as indicated by an arrow W5 from the lower supply port 271a of the bowl-shaped zigzag pipe 271. Sorting into lightweight combustible materials such as plastic pieces and non-combustible materials such as ceramic pieces by the air flowing above. The air flow is supplied to the air supply port 271 b at the lower end portion of the zigzag pipe line 271, flows through the zigzag pipe line 271, and conveys a lightweight combustible material from the upper end part to the cyclone separator 273. The air carrying the light combustible material is sucked into the blower 272 after the light combustible material is separated by the cyclone separator 273. The lightweight combustible material is discharged from the lower end of the cyclone separator 273 via the rotary seal valve as indicated by an arrow W6 and stored in the metering feeder 50 formed integrally with the storage silo. The heavy incombustible is discharged onto the belt conveyor 28 as indicated by an arrow W7.

  While the heavy incombustible material is being conveyed by the belt conveyor 28, the magnetic material such as iron is removed by the magnetic separator 29. The magnetic material is stored in a hopper (not shown) and used as a recycled resource, while the heavy incombustible material from which the magnetic material has been removed is stored in a tray and then discarded.

  On the other hand, the lightweight material sorted by the swing type separator 24 is sent to the washing and dehydrator 30. As shown in the schematic diagram of FIG. 5, the washing and dehydrator 30 is charged with a lightweight object together with water and air, as indicated by an arrow W <b> 8, into an inlet 301 a formed at one end of the casing 301. Deodorizers such as ozone and deodorizing enzymes are added to water. In the casing 301, a plurality of paddles 303 that are attached to a rotating shaft 302 and are driven to rotate so as to feed a lightweight object are arranged. A porous cylinder 304 is disposed in the casing 301 so as to surround the paddle 303. As the lightweight material is sent to the other end side through the perforated tube 304 by the paddle 303, the dirt is removed together with moisture, washed, and dried. The dirt removed together with the water from the lightweight material becomes dirty water and is discharged to the outside of the porous tube 304 and collected at the lower part of the casing 301. The sewage is discharged out of the casing 301 as indicated by an arrow W9 by a discharge conveyor 305 disposed at the lower portion of the casing 301. The sewage discharged to the outside of the casing 301 is input to the organic waste treatment line 3.

  The washed and dried lightweight material is discharged from a discharge port 301b formed at the other end of the casing 301 by a take-out conveyor 306 connected to the discharge port 301b. A vertical tube 307 extending vertically is attached to the end of the takeout conveyor 306, and an air flow is formed by the blower 308 from below to above the connection position of the takeout conveyor 306 of the vertical tube 307. The light that is discharged from the takeout conveyor 306 by the air flowing from the bottom to the top in the vertical tube 307 is made of incombustible material such as paper, plastic, cloth, fiber scraps, and metal particles mixed in the light material. Sorted into things. As indicated by an arrow W <b> 10, the air flow conveys the combustible material from the vertical tube 307 to the cyclone separator 31, and is sucked by the blower 308 after the combustible material is separated by the cyclone separator 31. On the other hand, the incombustible material is discharged by its own weight from the lower end of the vertical tube 307 as indicated by an arrow W11.

  As described above, the washing and dehydrator 30 performs the washing and dehydration by applying the turning force to the lightweight object, so that it is not necessary to heat the lightweight object as the object to be processed. Therefore, since the washing and dehydrator 30 does not require a heat source device such as a boiler or a burner, the equipment cost can be reduced as compared with the conventional case, and the emission of carbon dioxide due to the use of fossil fuel can be prevented.

  The combustible material such as paper and plastic separated by the cyclone separator 31 is sent to the fixed quantity feeder 32 and temporarily stored. The combustible material is supplied from the metering feeder 32 to the vibrating screen 33. The vibrating screen 33 has an inclined screen and a vibrating mechanism that vibrates the screen, and the lower end of the screen is positioned above the transfer device of the optical sorting device 35 as a subsequent chlorine-containing resin removing device. Are arranged as follows. The vibrating screen 33 uniformly discharges the lightweight material introduced from the fixed amount feeder 32 to the upper end portion of the screen in the width direction from the lower end by the vibrating action of the screen. Thereby, a lightweight thing is arranged uniformly on the upper surface of the transfer device of the optical sorting device 35.

  FIG. 6 is a schematic diagram showing the optical sorting device 35. The optical sorting device 35 is disposed in the vicinity of the belt conveyor 351 as a transfer device for transferring the object to be processed and the terminal portion of the belt conveyor 351, and irradiates the object to be processed with near infrared rays as electromagnetic waves, and the reflected wave thereof. An optical unit 352 for receiving the air, an air gun 353 as an injection unit for injecting compressed air to the object to be processed, and a control unit 354 connected to the optical unit 352 and the air gun 353. The air gun 353 is connected to a compressor unit 355 that supplies compressed air. The optical unit 352 includes an irradiation unit 356 as an electromagnetic wave irradiation unit that irradiates a lightweight object on the belt conveyor 351 with a near infrared ray, and a light receiving unit 357 as a reflected wave detection unit that receives a reflected wave of the near infrared ray reflected by the lightweight object. Have The irradiation unit 356 is formed by arranging a plurality of lamps that irradiate near-infrared rays from before and after the belt traveling direction of the belt conveyor 351 in the belt width direction of the belt conveyor 351. A lens of a near-infrared camera 357 as a light-receiving unit is arranged between each pair of lamps of the irradiation unit 356 so as to receive near-infrared light from directly below.

  The belt conveyor 351 is supplied with a light object as an object to be processed from the vibrating screen 33 on the upper surface of the belt, and transfers the light object to the terminal side. When the light object reaches below the optical unit 352, the irradiation unit 356 of the optical unit 352 irradiates the light object with near-infrared light, and reflects the reflected wave formed by reflecting the irradiated near-infrared light with the light object. The lens receives. The near-infrared camera 357 receives the reflected near-infrared wave and outputs information indicating the wavelength and intensity of the reflected near-infrared wave to the control unit 354. Based on the information input from the near infrared camera 357, the control unit 354 analyzes the wavelength and intensity of the reflected wave (near infrared) from each lightweight object, and discriminates the material of the lightweight object based on the spectrum distribution pattern. To do. When the identified material is vinyl chloride as a chlorine-containing resin, the control unit 354 removes the waste plastic, which is a lightweight product made of vinyl chloride, from the belt conveyor 351. That is, at the timing when the waste plastic made of vinyl chloride reaches the end of the belt conveyor 351, the air gun 353 is operated to inject compressed air toward the waste plastic made of vinyl chloride. The waste plastic made of vinyl chloride is blown off by receiving compressed air, and is collected in a collection chamber 358 provided on the side far from the end of the belt conveyor 351. Lightweight materials other than vinyl chloride waste plastic fall downward from the end of the belt conveyor 351 and are collected in a collection chamber 359 provided on the side close to the end of the belt conveyor 351.

  In this manner, after washing and dewatering the lightweight material with the washing dehydrator 30, the resin containing chlorine is discriminated and removed by the optical sorting device 35. It is possible to remove chlorine-containing materials at a low cost by a simple apparatus and fewer steps than when heating is performed to remove chlorine content and paper is washed with water to perform desalting.

  Further, the lightweight object is washed by the washing and dehydrator 30 to remove the deposits, and sent to the optical sorting device 35 in a dried state. Therefore, in the optical sorting device 35, the electromagnetic wave applied to the light object is reflected without being interfered by the adhering substance, so that the material of the light object can be accurately determined. As a result, chlorine-containing resins such as vinyl chloride can be removed from lightweight materials with high accuracy, so that solid fuel that does not generate dioxins when combusted is produced at a high regeneration rate with respect to waste material. Can do.

  The optical sorting device 35 can discriminate various materials other than vinyl chloride based on the spectral distribution of the near-infrared reflected wave. For example, polyethylene, polyethylene terephthalate, and polypropylene can be discriminated, and paper and wood can be discriminated. Therefore, the optical sorting device 35 may discriminate materials other than vinyl chloride from light objects and collect them.

  Up to this point, the processing applied to the light-weight items sorted by the swing type sorter 24 has been described. However, the same processing can be applied to the heavy items sorted by the swing type sorter 24. That is, after a heavy-weight combustible material separated by the wind power sorter 27 is washed, dehydrated and separated by a washing dehydrator having the same configuration as the washing dehydrator 30, the cyclone separator Then, the chlorine-containing resin is removed by an optical sorting device having the same configuration as the optical sorting device 35 through a fixed amount feeder and a vibrating screen. As a result, waste plastics such as polyethylene terephthalate containers with relatively large dimensions and combustibles such as wood chips with relatively large dimensions separated as heavy objects by the oscillating separator 24 are extracted without vinyl chloride. can do.

  The lightweight material from which the vinyl chloride has been removed by the optical sorting device 35 and is collected in the collection chamber 359 is conveyed by a screw conveyor 36 connected to the lower end of the collection chamber 359 and sent to a wind power sorter 37 for foreign matter. Is recovered. The combustible material from which the foreign matter has been collected is sent to the crusher with pusher.

  The crusher with pusher 38 has a single rotating shaft with a rotary blade fixed to the peripheral surface in the casing, and the combustible material is pressed toward the rotating shaft by a pusher driven by a hydraulic cylinder. The combustible material pressed by the pusher is crushed by the shearing action of the rotating blade of the rotating shaft and the fixed blade disposed opposite to the rotating blade at the lower portion of the rotating shaft and becomes a crushed piece having a size of 25 to 100 mm. Discharged. The pusher-equipped crusher 38 may be a biaxial crusher. The crushed pieces crushed by the crusher with pusher 38 are conveyed by the screw conveyor 39, and foreign substances are removed by the wind power sorter 40 installed at the end of the screw conveyor 39. The wind power sorter 40 sorts the inside of the bowl-shaped zigzag pipe line 401 into combustibles and foreign substances by the air flowing upward from the bottom by the blower 402, and conveys the combustibles to the cyclone separator 403 by the air flow. The combustible material separated by the cyclone separator 403 is stored in a metering feeder 50 formed integrally with the storage silo via a rotary seal valve.

  In this way, the solid fuel production plant 1 of the present embodiment, from the waste in which combustible materials and incombustible materials are mixed, from the coarse crusher 21, the swing type separator 24, the washing and dehydrator 30, By passing through the optical sorting device 35, it is possible to efficiently remove the chlorine-containing resin that is the cause of dioxins, and to efficiently collect flammable lightweight materials including waste paper and waste plastic.

  FIG. 7 is a schematic diagram showing the configuration of the organic waste treatment line 3. The organic waste treatment line 3 is mainly configured by a reduced-pressure fermentation drying device 44 as a reduced-pressure drying device that performs a drying process on organic waste, and a carbonization device 47 that performs a carbonization treatment. This embodiment demonstrates the case where the excess sludge produced by the activated sludge method is processed as organic waste.

  First, surplus sludge with a moisture content exceeding 98 wt% is received by the receiving hopper 41 and is transported by the transport conveyor 42 from the cutting device below the receiving hopper 41. In addition, the sewage generated by washing the light weight by the swing type separator 24 is put into the receiving hopper 41, mixed with sludge and transported by the transport conveyor 42. Oga powder is added to the excess sludge transported by the transport conveyor 42 by a wood chip supply device 43 installed in the middle of the transport conveyor 42. The sawdust produced in the woody waste processing line 4 described later is supplied to the wood waste supply device 43. In addition, it is not necessary to add the sawdust to the excess sludge. The excess sludge to which the sawdust is added is sent to the reduced-pressure fermentation drying device 44.

  FIG. 8 is a view showing the reduced-pressure fermentation drying apparatus 44. The reduced-pressure fermentation drying apparatus 44 is roughly composed of a drying apparatus main body 410 and a cooling tower 430 as a mixed cooler.

  The drying apparatus main body 410 includes a substantially cylindrical casing 412 having a processing chamber 411 therein, a jacket heater 413 formed on the lower wall surface of the processing chamber 411, and a heating and stirring unit 414 disposed in the processing chamber 411. And a condensing part 415 provided at the upper part in the processing chamber 411.

  An input port 412 a into which the object to be processed is input is formed at the upper part of one end of the casing 412, and a discharge port 412 b through which the object to be processed is discharged is formed at the lower part of the other end of the casing 412. An air lock mechanism connected to the terminal end of the transfer conveyor 42 is connected to the charging port 412 a of the casing 412. A discharge conveyor 451 formed by a screw conveyor is connected to the discharge port 412 b of the casing 412. The terminal end of the discharge conveyor 451 is connected to a discharge device 45 having an air lock mechanism.

  FIG. 9 is a cross-sectional view showing details of the inside of the drying apparatus main body 410. As shown in FIG. 9, the heating and agitating unit 414 includes a rotating shaft 141 supported at both ends by bearing devices 121 and 122 provided on both end surfaces of the casing 412, and a coiled tube 142 fixed to the rotating shaft 141. And a plurality of rectangular blades 143 which are arranged on the outer peripheral side of the coiled tubular body 142 and have a side of 5 to 10 cm. The rotating shaft 141 and the coiled tubular body 142 communicate with each other, and steam as a heat medium is supplied into the rotating shaft 141 and the coiled tubular body 142 via the bearing devices 121 and 122. The heating and stirring unit 414 is driven to rotate by the motor M, heats the object to be processed by the rotating shaft 141 and the coiled tubular body 142, and sends the object to be processed in the casing 412 from the inlet 412a toward the outlet 412b. It is formed to stir while applying. The blade 143 has a surface in which the radial leading edge of the heating and agitating unit 414 is inclined in the rotational direction, and the side edge on the axial discharge port 412b side is inclined in the counter-rotating direction. As a result, as the heating and agitating unit 414 rotates, the blade 143 scrapes the object to be processed in the vicinity of the inner surface of the casing 412. The rotation speed of the heating and stirring unit 414 can be set between 1 rpm and 60 rpm in accordance with the amount of water in the organic waste put into the processing chamber 411.

  The bearing devices 121 and 122 of the casing 412 support the rotating shaft 141 of the heating and agitating unit 414 and supply and discharge steam as a heat medium. The supply-side bearing device 121 includes a rotary joint 124 connected to the steam supply pipe 123 and a sleeve bearing 125 that supports the end of the rotary shaft 141 that includes the steam pipe 141 a connected via the rotary joint 124. The discharge-side bearing device 122 includes a rotary joint 127 connected to the steam discharge pipe 126 and a sleeve bearing 128 that supports the end of the rotary shaft 141 that includes the steam pipe 141 b connected via the rotary joint 127. Steam supplied from the steam boiler 6 to the supply-side bearing device 121 through the steam supply pipe 123 is supplied to the rotary shaft 141 through the rotary joint 124. A part of the steam supplied to the rotating shaft 141 is supplied to the coiled tube 142. The steam supplied to the rotating shaft 141 and the coiled tube 142 undergoes heat exchange with the object to be contacted by the rotating shaft 141 and the coiled tube 142, and then is discharged through the steam tube 141 b and the rotating joint 127. Return to the side of the device 122. The steam that has returned to the discharge-side bearing device 122 is returned to the steam boiler 6 through the steam discharge pipe 126. On the other hand, steam having a lower pressure and temperature than the steam supplied to the heating and agitating unit 414 is supplied to the jacket heater 413 through the supply port 143a and returned to the steam boiler 6 through the discharge port 143b. That is, by supplying steam having a higher pressure and temperature to the heating and stirring unit 414 having a larger contact area than the jacket heater 413 as compared with the steam supplied to the jacket heater 413, The treated product is efficiently dried. Thus, the jacket type heater 413 and the heating stirring unit 414 function as a heating unit of the reduced-pressure fermentation drying apparatus 44.

  The coiled tube 142 of the heating and agitating unit 414 is formed by an upstream coil 144 and a downstream coil 145. The inside of the rotating shaft 141 is in communication with the upstream end 144a and the downstream end 144b of the upstream coil 144 and the upstream end 145a and the downstream end 145b of the downstream coil 145 in sequence. Thereby, the steam supplied to the supply-side bearing device 121 side flows into the upstream coil 144 as indicated by the arrow G1, and then returns to the inside of the rotating shaft 141 as indicated by the arrow G2, It flows into the downstream coil 145 as indicated by an arrow G3, and then returns to the inside of the rotating shaft 141 as indicated by an arrow G4. The steam in the rotating shaft 141 is discharged from the rotating shaft 141 through the steam pipe 141b as indicated by an arrow G5.

  The heating and agitation unit 414 can scrape the object to be processed in the vicinity of the inner surface of the casing 412 with the blade 143 provided on the outer peripheral side of the coiled tube 142. Therefore, it is possible to effectively prevent the problem that the workpiece is fixed to the inner surface of the casing 412 where the jacket heater 413 is formed.

  The condensing unit 415 provided in the upper part of the casing 412 includes a cooling water supply chamber 151 formed on the other end surface of the casing 412 and a cooling water discharge chamber 152 formed on one end surface of the casing 412. A cooling water supply pipe 153 to which cooling water is supplied from the cooling tower 430 is connected to the cooling water supply chamber 151. A cooling water discharge pipe 154 that discharges the cooling water and returns it to the cooling tower 40 is connected to the cooling water discharge chamber 152. Between the cooling water supply chamber 151 and the cooling water discharge chamber 152, a plurality of cooling water pipes 155, 155,... Extending in the axial direction of the casing 412 and communicating at both ends with the supply chamber 151 and the discharge chamber 152.・ ・ Is provided. The plurality of cooling water pipes 155, 155,... Are arranged on both sides in the width direction of the upper part in the casing 412. A water collecting trough 156 for collecting condensed water is provided on the side and the lower side of the plurality of cooling water pipes 155, 155,. A suction pipe 157 that sucks air in the processing chamber 411 together with condensed water communicates with the inside of the water collecting tank 156.

  Microorganisms are added to the organic waste dropped into the casing 412 of the drying apparatus main body 410. As microorganisms, indigenous or fermentative bacteria that inhabit the natural world such as the sea, mountains, and land are collected and cultured. In particular, in order to ferment organic sludge such as excess sludge and perform deodorization, it has been found that various animals and plants and bacteria that inhabit soil are effective. Examples of plants and animals inhabited by fungi include wormwood, wild grass, medicinal herbs, seaside grass, bamboo shoots, bamboo bush soil, mountain forest soil, fish, seaweed, fruits, pineapples, apples, mandarin oranges, loquats and grapes. It is preferable to use the bacteria that inhabit them by culturing with rice bran or sawdust. In this embodiment, the fermenting bacteria are mixed while stirring the workpiece at a temperature of 70 to 90 ° C. for 30 minutes to 2 to 3 hours under a reduced pressure environment of 0.03 to 0.07 MPa. Since deodorization is performed, microorganisms that grow under such conditions are preferred. The microorganism added to the processing chamber 411 is preferably one that produces at least one of the following enzymes. In addition, the substance which each enzyme acts is described in the parenthesis following each enzyme. Alcohol dehydrogenase (alcohol), lactate dehydrogenase (lactose), glucose 6-phosphate dehydrogenase (carbohydrate), aldehyde dehydrogenase (aldehyde), L, aspartate, beta-semialdehyde, NADP Oxdrectase (aldehyde), glutamate dehydrogenase (amino acid), aspartate semialdehyde dehydrogenase (amino acid), NADPH2 cyclochrome C-reactase (NADP), glutathione dehydrogenase (glutathione), Trehalose phosphate synthetase (carbohydrate), polyphosphae kinase (ATP), ethanolamine phosphae cytidyltransferase (CTP), trehalose phosphatase (carbohydrate), metal O-phospho-glycerate phosphatase (glycerin), inulase (inulin), β-mannositase (carbohydrate), uridine nucleositase (amino acid), cytosine diaminase (cytosine), methylcysteine synthetase (amino acid), aspartate synthetase (ATP) ), Succinate dehydrogenase (succinic acid), aconitic acid hydrogenase (citrate), fumarate hydrogenase (malonic acid), maleate dehydrogenase (malonic acid), citrate synthetase (acetyl CouA) , Isocitrate dehydrogenase (citrate), LSNADP oxidase (citrate), monoamine oxidase (amine), histamine (amine), pyruvate decarboxylase (oxoacid), ATPase (ATP), nucleotide pyrophosphatase (nucleic acid), endopolyphosphatase (ATP), ATP phosphohydrolase (ATP), orotidine 5-phosphate decarboxylase (orotidine). By including a microorganism that produces at least one of these enzymes in the object to be treated, it is possible to effectively decompose organic waste composed of many kinds of organic substances.

  The cooling tower 430 cools the cooling water supplied to the condensing unit 415 of the drying device main body 410 and cools the condensed water generated by the condensing unit 415 of the drying device main body 410 and the gas in the drying device main body 410. Deodorizing by mixing with water. The cooling water is guided from the cooling water discharge chamber 152 in the drying apparatus main body 410 to the cooling tower 430 as shown by an arrow W1 in FIG. 8 and cooled, and then is indicated by the cooling water pump P by an arrow W2 in FIG. Thus, the cooling water supply chamber 151 of the drying apparatus main body 410 is returned. Moreover, the condensed water produced | generated in the condensation part 415 of the drying apparatus main body 410 and the gas which has the odor produced in the process chamber 411 with the drying of organic waste are attracted | sucked by the vacuum pump VP, and the arrow of FIG. As indicated by V, it is guided to the cooling tower 430.

  As shown in FIG. 10, the cooling tower 430 includes a casing 431 having an air circulation port at an upper part and a lower part, a water tank 432 installed at a lower end of the casing 431, and guides water in the water tank 432 to an upper part in the casing 431. Sprinkling pipe 433, sprinkling pump SP provided in sprinkling pipe 433, a plurality of sprinkling nozzles 433a, 433a,... Provided at the branched end of sprinkling pipe 433, and sprayed from sprinkling nozzle 433a. A contact body 435 in which water flows down and contacts, and a fan 436 provided at the upper end of the casing 431 are provided. The casing 431 is provided with a conduit 434 that guides the condensed water and air discharged from the drying apparatus main body 410 as indicated by an arrow V in FIG. A plurality of discharge nozzles 434a, 434a,... Are provided at the branched tip end portion of the conduit 434 so that condensed water and gas guided by the conduit 434 are discharged toward the flow of water discharged from the watering nozzle 433a.・ ・ Is provided. The contact body 435 is provided with a porous filler made of resin and serves as a carrier for microorganisms. A cooling water pipe 437 for returning the cooling water in the water tank 432 to the drying apparatus main body 410 is connected to the water tank 432, and the cooling water is circulated between the cooling tower 430 and the condensing unit 415 in the cooling water pipe 437. A cooling water pump P is interposed.

  Microorganisms are added to the cooling water circulating between the cooling tower 430 and the condensing unit 415. This microorganism is obtained by collecting and cultivating indigenous bacteria, fermenting bacteria, and the like that inhabit the natural world such as the sea, mountains, and land, in the same manner as the microorganisms introduced into the processing chamber 411. The microorganism added to the cooling water may be any microorganism that produces at least one enzyme among a plurality of enzymes produced by the microorganism added to the processing chamber 411 described above. By adding microorganisms to the cooling water, the odor component contained in the condensed water and the odor component contained in the gas sucked from the processing chamber 411 can be decomposed and removed. The decomposition of odor components by microorganisms is performed while cooling water circulates in a circulation path formed between the cooling tower 430 and the condensing unit 415. Further, when the cooling water comes into contact with the contact body 435 and flows down, the odor is decomposed by the microorganisms supported on the contact body 435.

  Since this reduced-pressure fermentation drying apparatus 44 reduces the concentration of odor components as a whole by mixing condensed water and gas with cooling water, there is a risk that the processing capacity of microorganisms may be exceeded even if condensed odor or gaseous odor components increase. Therefore, the decomposition process with stable odor can be performed. Further, since the inside of the processing chamber 411 is depressurized, the temperature rise of the cooling water when the cooling water exchanges heat with room air in the condensing unit 415 is relatively small, and the temperature of the cooling water is approximately 40 to 45 ° C. become. Thereby, the disadvantage that the microorganisms in the cooling water are killed by the high temperature is prevented, the microorganisms are stably activated, and the condensed water and gas can be stably deodorized by the microorganisms.

  Further, in the cooling tower 430, the evaporation of the cooling water is promoted, so that almost no overflow occurs. Moreover, since condensed water and gaseous odor components are diluted with cooling water, they are highly decomposed and removed. Therefore, it is possible to effectively prevent the inconvenience that the odor diffuses outside the reduced-pressure fermentation drying apparatus 44.

  When the organic waste is dried by the reduced pressure fermentation drying apparatus 44, the air inside the processing chamber 411 is sucked by the vacuum pump VP to reduce the pressure to a pressure lower than the atmospheric pressure. Here, the boiling point of water can be reduced to about 90-68 degreeC by making the pressure reduction value of the process chamber 411 into 0.03-0.07 MPa. Note that the reduced pressure value refers to a difference in pressure that is reduced from atmospheric pressure.

  As a heating medium supplied to the heating unit of the drying apparatus main body 410, steam of 0.2 to 0.3 MPa and 130 ° C. is used for the jacket type heater 413, while 0.7 to 0.8 MPa is used for the heating and stirring unit 414. In addition, steam at 170 ° C. is used. Thus, by supplying a heating medium having a temperature higher than that of the jacket type heater 413 that performs heating in a stationary state to the heating and stirring unit 414 that performs heating in a rotationally driven state, the heating and stirring unit 414 and the jacket type Each of the heaters 413 can efficiently heat the object to be processed at a high temperature at which the object to be processed adheres and does not burn. Further, since the inside of the processing chamber 411 is depressurized, the temperature of the heat medium can be set lower than drying at normal pressure. Therefore, the generation energy of the steam as the heat medium can be reduced. In addition, since the heating temperature of the object to be processed is low, it is possible to prevent the microorganisms that are added to the processing chamber 411 and deodorize from being killed, and the deodorization can be performed effectively. For example, the dried organic matter that has been dried and deodorized by the drying apparatus main body 410 is discharged from the outlet 412b at a temperature of about 60 ° C. In this way, the organic waste of the object to be treated is heated to a relatively low temperature, so that the microorganisms can be effectively activated to perform deodorization. Can be dried.

  According to this reduced-pressure fermentation drying apparatus 44, a high-moisture organic waste having a water content of 80 to 99.5 wt% is dried, and the water content is 10 wt% or more and 25 wt% or less in a processing time of 2 to 6 hours. Can be reduced.

  Thus, since the reduced-pressure fermentation drying apparatus 44 performs fermentation and drying of organic waste in a reduced-pressure environment, sludge can be dried with a small amount of heat due to a decrease in boiling point accompanying reduced pressure. In addition, the organic waste is decomposed by microorganisms in the reduced-pressure fermentation dryer 44, and the condensed water and gas are decomposed by the microorganisms of the cooling water, so that the odor of the organic waste can be effectively reduced, and the surrounding environment can be reduced. Odor diffusion can be prevented. In addition, by adding a known chlorinase in the treatment chamber 411, chlorine-containing substances contained in the organic waste can be removed, and generation of dioxins can be prevented.

  The dried organic matter whose organic waste has been dried by the reduced-pressure fermentation dryer 44 and whose water content has become 10 wt% or more and 25 wt% or less is discharged from the discharge port 412 b on the other end side of the lower portion of the casing 412. The dried organic matter discharged from the discharge port 412b is conveyed by the discharge conveyor 451, and is sent to the fixed amount feeder 46 formed integrally with the storage silo via the discharge device 45 having an air lock mechanism.

  The dry organic matter once stored in the metering feeder 46 is sent to the carbonizer 47.

  FIG. 11 is a schematic cross-sectional view showing the carbonization apparatus 47. The carbonization device 47 is configured by an externally heated rotary kiln. The carbonization apparatus 47 includes a casing 471 into which a heat transfer gas is supplied, a rotary furnace 472 housed in the casing 471, and a dry organic material to be processed that is connected to one end of the rotary furnace 472 to rotate the rotary organic substance 472. It has a supply conveyor 476 that feeds into the interior and a discharge chamber 477 that communicates with the other end of the rotary furnace 472 and discharges the processed object and combustible gas. A heating chamber 473 for introducing a heat medium and heating the rotary furnace 472 from the outside is formed between the casing 471 and the rotary furnace 472. Inside the rotary furnace 472 is a carbonization chamber 474 that performs dry distillation and carbonization of the dry organic matter with the heat of the heat medium supplied to the heating chamber 473 while sending the dry organic matter introduced into one end by the supply conveyor 476 to the other end. Is formed. On the inner peripheral surface of the carbonization chamber 474, a spiral guide (not shown) for sending the object to be processed to the other end is provided. The discharge chamber 477 is in communication with the carbonization chamber 474. The discharge chamber 477 discharges the organic carbide, which is carbonized in the carbonization chamber 474, by the discharge conveyor 452 connected to the lower end, while drying in the carbonization chamber 474. The combustible gas produced | generated from the organic substance is discharged | emitted from the exhaust port 479 provided in the upper end. The exhaust port 479 is connected to a combustible gas pipe 480 for deriving a combustible gas. The downstream end of the combustible gas pipe 480 is connected to a carbonizer pipe 481 connected to the heating chamber 473 side of the carbonizer 47 and steam. Branching to a boiler pipe 482 connected to the burner of the boiler 6. The carbonization apparatus pipe 481 is connected to a gas burner 487 installed in the heating chamber 473 of the carbonization apparatus 47 so that a flame opening is desired. The carbonizer piping 481 and the boiler piping 482 are provided with electromagnetically driven on-off valves 483 and 484, respectively. The on-off valves 483 and 484 are controlled to be opened and closed by a control unit 485 described in detail later. Further, a blower (not shown) is connected to the exhaust pipe connected to the exhaust port 479. The blower sucks air in the carbonization chamber 474, and the air containing the combustible gas is supplied to the carbonizer pipe 481 and the boiler. It is sent to the pipe 482. By sucking the air in the carbonizing chamber 474 with this blower, the inside of the carbonizing chamber 474 is made into a low oxygen environment having an oxygen concentration of 5% or more and 12% or less by volume. Thereby, the dry organic substance heated in the carbonization chamber 474 is effectively carbonized, and a combustible gas such as carbon monoxide is efficiently generated. The heating temperature of the dry organic substance in the carbonization chamber 474 is preferably 350 ° C. or more and 500 ° C. or less, and the heating time of the dry organic substance is preferably 5 minutes or more and 10 minutes or less.

  A heating medium gas is supplied from an oil burner 475 to the heating chamber 473 of the carbonization device 47 when the carbonization device 47 is started. The oil burner 475 is connected to a heavy oil fuel tank 488 that uses A heavy oil as liquid fuel and supplies A heavy oil. The oil burner 475 is controlled by the control unit 485, burns the combustible gas supplied from the discharge chamber 477, and supplies the combustion gas at 500 to 700 ° C. to the heating chamber 473 as a heat transfer gas. When the temperature in the carbonization chamber 474 is sufficiently increased by the combustion gas as the heating medium gas supplied from the oil burner 475 to the heating chamber 473, the dry organic matter in the carbonization chamber 474 is heated, and hydrogen, carbon monoxide, and methane are heated. A flammable gas containing etc. is produced. When the generation of the combustible gas is started in the carbonization chamber 474, the control unit 485 stops the combustion of the oil burner 475 and the on-off valve 483 of the carbonization apparatus pipe 481 is controlled to change from the closed state to the open state. Driven. As a result, the supply of the heating medium gas from the oil burner 475 is stopped in the heating chamber 473, while the combustible gas is supplied from the carbonizer piping 481 to start the gas burner 487, and the combustible gas is Combustion and combustion gas as heat medium gas are supplied to the heating chamber 473. Thus, heating in the carbonization chamber 474 is continued. Combustion gas obtained by burning combustible gas in the heating chamber 473 is discharged from the heating chamber 473 and guided to the heat exchanger of the steam boiler 6 of the vacuum fermentation drying apparatus 44 as a heat transfer gas. Since the combustion gas discharged from the heating chamber 53 has a temperature of 250 to 500 ° C., it can be reused in order to generate steam to be supplied to the vacuum fermentation drying apparatus 44 by the steam boiler 6. As described above, the combustion gas of the carbonization device 47 is supplied to the steam boiler 6 as a heat transfer gas, and the surplus heat when the dried organic matter is heated by the carbonization device 47 is reused by the steam boiler 6. Yes. Dust is removed from the combustion gas used for generating steam in the heat exchanger of the steam boiler 6 and exhausted.

  Thus, by carbonizing the dry organic matter by the carbonization device 47, the odor of the dry organic matter derived from the excess sludge can be effectively reduced. Further, since the combustible gas generated by heating the dry organic matter in the carbonization device 47 is guided to the gas burner 487 and the steam boiler 6 and burned, the odor generated along with the carbonization of the dry organic matter can be removed. .

  Further, by carbonizing the dry organic matter with the carbonization device 47, the amount of heat at the time of burning the dry organic matter can be increased. For example, when the organic waste is woody waste such as wood chips, the fuel formed by molding the organic waste without carbonizing has a heat quantity of approximately 3800 kcal / kg. On the other hand, the fuel obtained by carbonizing the wood waste with the carbonization device 47 and molding the carbide has a calorific value of 7000 to 8000 kcal / kg. Moreover, the surplus sludge as organic waste is carbonized to form an organic carbide, and the fuel obtained by molding the organic carbide has a calorific value of 5000 to 6000 kcal / kg.

  Moreover, since the combustion gas of the carbonization apparatus 47 is supplied to the heat exchanger of the steam boiler 6 as a heat transfer gas and the dried organic matter is heated by the carbonization apparatus 47, the steam boiler 6 uses the surplus heat. The combustible gas generated by the carbonization of the dry organic matter in the apparatus 47 can be used for heating the carbonization apparatus 47 and also for heating the vacuum fermentation drying apparatus 44 for drying the organic waste. Therefore, the fossil fuel used for the drying and carbonization treatment of organic waste can be effectively reduced. As a result, greenhouse gas emissions such as carbon dioxide and air pollutants such as nitrogen oxides can be effectively eliminated. Can be reduced.

  Moreover, the said steam boiler 6 is comprised so that a part of combustible gas produced | generated from the dry organic substance with the carbonization apparatus 47 may be supplied as a fuel. Specifically, when combustible gas is generated from the dry organic matter in the carbonization chamber 474, the control unit 485 opens the on-off valve 484, and the combustible gas is supplied to the burner of the steam boiler 6 through the boiler pipe 482.

  In this way, in the organic waste treatment line 3, in order to dry the organic waste, in addition to the excess heat of the carbonization device 47, the use of fossil fuel by using the combustible gas generated in the carbonization device 47 is used. Organic waste can be efficiently dried while reducing the amount.

  The organic carbide treated by the carbonization device 47 is conveyed by a discharge conveyor 452, and is sent to a fixed amount feeder 49 formed integrally with a storage silo via a discharge device 48 having an air lock mechanism. The organic carbide once stored in the metering feeder 49 is sent to the solid fuel production line 5.

  FIG. 12 is a schematic diagram showing the configuration of the wooden waste treatment line 4. Woody waste treatment line 4 is filled with woody waste such as waste wood, thinned wood, and wood lumber, and forms wood chips and sawdust as wood waste.

  The wooden waste thrown into the wooden waste processing line 4 is crushed by the crusher 61. Here, wood waste that has been dried, such as waste wood, is crushed with a hammer-type crusher, while wood waste that has not been dried, such as thinned lumber and timber ends, is shredded with a chipper-type crusher. Crush.

  The wood waste crushed by the crusher 61 is conveyed by the conveyor 62, and after heavy objects such as nails and metal fittings are removed by the drum type magnetic separator 63, it is sent to the swivel sieve 64. The swivel sieve 64 is configured to drive a swivel body in a slanted surface in a slanted state, with a sieve body formed by spanning a two-stage sieve net inside a bottomed sieve frame. The swivel sieve 64 classifies the wooden waste put into the sieve main body into three types of small diameter, medium diameter and large diameter according to each sieve mesh. Specifically, the two-stage sieve mesh of the sieve body is composed of a large mesh having a large mesh size provided in the upper stage and a small mesh having a small mesh dimension provided in the lower stage. The crushed pieces of wooden waste introduced from above the upper omentum are sequentially sieved into the sieving body by the omentum and the omentum, and the crushed pieces having a diameter larger than 20 mm and a diameter of 2 to 20 mm. It classifies into a crushed piece with a medium diameter and a crushed piece with a diameter smaller than 2 mm.

  Among the crushed pieces of wood waste classified by the swivel sieve 64, the crushed pieces having a medium diameter of 2 to 20 mm are conveyed by the screw conveyor 65, and the wind sorter 66 connected to the end of the screw conveyor 65 is used. Heavy objects are removed. The wind power sorter 66 includes a separation pipe line 661 that is repeatedly bent in a zigzag shape, a cyclone separator 662, and a blower 663, and an object to be processed is conveyed upward along the separation pipe line 661 by wind generated by the blower 663. Separate heavy objects during the process. The wind sorter 66 removes heavy objects such as sand from the medium-sized crushed pieces, and the medium-sized crushed pieces separated from the conveying wind by the cyclone separator 662 are stored in the quantitative feeder 51 as wooden chips. The

  Further, among the crushed pieces of wood waste classified by the swivel sieve 64, small crushed pieces having a diameter of less than 2 mm are conveyed by a screw conveyor 67, and by a wind power sorter 68 connected to the end of the screw conveyor 67. Heavy objects are removed. The wind power sorter 68 includes a separation pipe 681, a cyclone separator 682, and a blower 683. A heavy object is conveyed while the object to be processed is conveyed upward through the separation pipe 681 by the wind generated by the blower 683. To separate. The wind sorter 68 removes heavy objects such as sand from the small-diameter crushed pieces, and the small-diameter crushed pieces separated from the conveying wind by the cyclone separator 682 are stored in the quantitative feeder 69 as sawdust.

  Further, among the crushed pieces of wooden waste classified by the swivel sieve 64, the crushed pieces having a large diameter exceeding 20 mm are returned to the crusher 61 by a return conveyor (not shown) and crushed again.

  The wood chips stored in the fixed quantity feeder 51 are mainly supplied to the steam boiler 6 as fuel. By using the wood chip as the fuel for the steam boiler 6, the amount of fossil fuel used in the steam boiler 6 can be reduced, and the emission amount of greenhouse gases such as carbon dioxide can be reduced. Moreover, the wood chip | tip stored by the fixed quantity supply machine 51 is supplied to the solid fuel production line 5 as a plant-derived waste of the material of RPF as needed. On the other hand, sawdust stored in the quantitative feeder 69 is sent to the organic waste treatment line 3, added to sludge by the sawdust feeder 43, and put into the reduced-pressure fermentation dryer 44. By adding sawdust to the sludge to be dried by the reduced-pressure fermentation dryer 44, the moisture content of the sludge and the nitrogen component can be reduced. Note that the sawdust stored in the metering feeder 69 may be put into the solid fuel production line 5 together with the wood chips.

  FIG. 13 is a schematic diagram showing the configuration of the solid fuel production line 5. The solid fuel production line 5 uses the combustible material containing the waste plastic extracted in the mixed waste treatment line 2 and the organic carbide produced in the organic waste treatment line 3 to produce RPF as a solid fuel. .

  In the solid fuel production line 5, the combustible material including the waste plastic extracted in the mixed waste treatment line 2 and stored in the fixed quantity supply machine 50 is unwound from the fixed quantity supply machine 50 and conveyed by the screw conveyor 70. The organic carbide is supplied from the quantitative feeder 49 of the organic waste processing line 3 to the combustible material including the waste plastic conveyed by the screw conveyor 70 and merges. In addition, wood chips are added to the screw conveyor 70 from the quantitative feeder 51 of the wood waste processing line 4. In addition, it is not necessary to use a wooden chip | tip for the material of solid fuel, without adding a wooden chip | tip to the screw conveyor 70. FIG.

  This solid fuel production line 5 includes organic carbide produced in the organic waste treatment line 3, waste plastic extracted in the mixed waste treatment line 2, paper waste and woody waste extracted in the mixed waste treatment line 2. RPF is manufactured by blending the wood-derived chip or the plant-derived waste material containing sawdust produced in the material treatment line 4 in the following ratio. That is, RPF in which organic carbide is approximately 40 wt%, waste plastic is approximately 40 wt%, and plant-derived waste is solidified at a ratio of approximately 20 wt% is manufactured. This RPF can generate a calorific value of about 6500 kcal / kg and has sufficient utility as a fuel for various boilers and burners.

  As shown in FIG. 13, in the solid fuel production line 5, a mixed material of organic carbide, waste plastic, and plant-derived waste is supplied to the molding device 71 by the screw conveyor 70. The molding device 71 performs mixing, kneading, heating, and extruding steps of materials, and solidifies organic carbide, paper, fibers, and woody components with the molten plastic waste component to produce RPF. As the molding device 71, a screw type molding device or a ring die type molding device can be used.

  FIG. 14 is a cross-sectional view schematically showing a part of a molding apparatus 71 used in the solid fuel production plant 1 of the present embodiment. The molding device 71 is a screw-type molding device including a pair of screw blades 712 whose rotation axes are arranged substantially in parallel. The screw-type molding device 71 kneads, compresses and molds the material while preventing the backflow of the material by a pair of screw blades 712, and generates frictional heat generated by the compression and kneading of the material. It is configured to perform heating, compression and molding with high efficiency.

  The molding apparatus 71 accommodates a pair of screw blades 712 and 712 for kneading and compressing a material in a casing 711 having an input port 711a for an object to be processed. FIG. 14 shows a state in which one screw blade 712 of the pair of screw blades 712 and 712 is observed from a direction perpendicular to the rotation axis.

  An end face plate 713 is attached to the end face of the casing 711 on the front end side of the pair of screw blades 712 and 712. A plurality of molding nozzles 714, 714,... Are attached to the end face plate 713 for molding and discharging the compressed material into a rod shape having a circular cross section.

  The screw blades 712 and 712 accommodated in the casing 711 are attached to the distal ends of a pair of rotating shafts 715 and 715 installed by being inserted from the outside to the inside of the casing 711 on the base end side of the screw blades 712 and 712. ing. Attachment portions 715a and 715a having a hexagonal cross section are formed at the tips of the rotation shafts 715 and 715, and screw blades 712 and 712 are fitted on the outer peripheral sides of the attachment portions 715a and 715a.

  The screw blade 712 includes a shaft portion that is attached to the attachment portion 715a of the rotating shaft 715 and a spiral blade portion that is formed on the peripheral surface of the shaft portion. The pair of screw blades 712 and 712 attached to the pair of rotating shafts 715 and 715 are arranged so that the spiral blade portions are formed in the opposite directions, and the spiral blade portions are overlapped when viewed from the extending direction of the rotating shaft. Has been. The pair of rotating shafts 715 and 715 are rotationally driven in directions opposite to each other, whereby the pair of screw blades 712 and 712 sandwich the material charged from the charging port 711a into the casing 711, and knead and compress the end plate. It is formed to be transferred to the 713 side.

  A cutting machine (not shown) that cuts the rod-shaped material discharged from the forming nozzle 714 of the end face plate 713 is attached to the end face of the casing 711. This cutting machine includes a rotary blade that is rotatably arranged at the outlet of the forming nozzle 714 and a motor that drives the rotary blade.

  The pair of screw blades 712, 712 are arranged in order from the inlet 711a side in the casing 711 toward the end face plate 713 side in the first spiral shaft 712a, the second spiral shaft 712b, and the third spiral shaft 712c. Is formed. Each helical shaft 712a, 712b, 712c is formed of a shaft portion connected to the rotation shaft 715 and a spiral blade portion fixed to the outer peripheral surface of the shaft portion. The first spiral shaft 712a, the second spiral shaft 712b, and the third spiral shaft 712c are formed such that the diameter of the shaft portion is increased in this order, and the pitch of the spiral blade portion is decreased in this order. Yes. Furthermore, the thickness of the spiral blade portion is increased in this order. Thereby, the volume of the processing chamber formed between the surface of each spiral shaft and the inner surface of the casing 711 is set to the above-described first spiral shaft 712a, second spiral shaft 712b, and third spiral shaft 712c. In order to make it smaller. As a result, the first spiral shaft 712a, the second spiral shaft 712b, and the third spiral shaft 712c reliably transfer the material to the subsequent stage without causing any inconvenience such as biting, and sequentially apply a large compressive force to the material. be able to. The screw blade 712 compresses a material having a bulk specific gravity of 0.025 at the time of charging so that the bulk specific gravity is approximately between 0.45 and 0.5 when discharged from the molding nozzle 714 of the end face plate. it can. Further, a material having a bulk specific gravity of 0.025 at the time of charging can be compressed to an extent that the true specific gravity is approximately between 0.8 and 1 when discharged from the forming nozzle 714.

  The third spiral shaft 712c has a flat surface at the tip of the spiral blade portion, and the flat surface portion is disposed close to the inner surface of the end face plate 713, and the third spiral shaft 712c is rotationally driven to compress at a high density. The formed material is surely extruded from the forming nozzle 714 of the end face plate 713. The third helical shaft 712c gives the material the maximum compressive force among the compressive forces given by the helical shafts 712a, 712b, and 712c. Therefore, a tungsten carbide-based material, for example, is formed on the base portion made of chromium steel and the surface of the base portion. And a built-up portion formed using a wear-resistant material such as.

  In the casing 711, a plurality of lining blocks 717, 717,... Surrounding the second and third spiral shafts 712b, 712c are arranged. A material processing chamber is formed between the plurality of lining blocks 717 and the outer surfaces of the second and third helical shafts 712b and 712c.

  The end face plate 713 is provided with a plurality of through holes in a region through which the flat portion at the tip of the third spiral shaft 712c passes and a molding nozzle 714 is inserted into the through hole. The end face plate 713 incorporates a resistance heating type heater, and heats the material discharged through the forming nozzle 714 to maintain the flexibility of the material.

  The molding device 71 molds the solid fuel as follows.

  First, after supplying electric power to the heater of the end face plate 713 and preheating the end face plate 713, a motor (not shown) is started to rotate the pair of rotating shafts 715 and 715 in the opposite directions, and a pair of screw blades 712 and 712 are rotated in opposite directions. The rotational speed of the screw blade 712 is preferably rotated at a relatively low speed of, for example, 30 rpm to 60 rpm. Subsequently, the mixed material of the organic carbide, the waste plastic, and the plant-derived waste is transported and input to the input port 711 a of the casing 711 by the screw conveyor 70.

  In the casing 711, the charged material is sandwiched between the pair of first spiral shafts 712a, kneaded, and reliably transferred to the second spiral shaft 712b side by a powerful sandwiching force. The second spiral shaft 712b guides the material into the processing chamber formed between the second spiral shaft 712b and the lining block 717, and kneads and compresses the material. The material guided into the processing chamber is kneaded and compressed while being fed to the end face plate 713 side by the rotation of the second helical shaft 712b, thereby effectively preventing the back flow of the material. Subsequently, the third spiral shaft 712c guides the material into the processing chamber formed between the third spiral shaft 712c and the lining block 717, and performs further kneading and compression. The first, second, and third spiral shafts 712a, 712b, and 712c are formed such that the diameter of the shaft portion is increased in this order, the pitch of the spiral blade portion is increased, and the thickness of the spiral blade portion is increased. Therefore, the material can be effectively kneaded and compressed without inconvenience such as biting of the material and a decrease in density.

  The first, second, and third helical shafts 712a, 712b, and 712c are capable of effectively generating compression heat and frictional heat in the material by sequentially applying a large compressive force to the material and performing kneading. In addition, it is possible to effectively melt a melt such as waste plastic contained in the combustible material. Thus, since the melt can be sufficiently melted by the compression heat and frictional heat of the material, the melt in the material can be sufficiently melted only by auxiliary heating with the heater of the end face plate 713.

  The material guided to the third spiral shaft 712c and compressed at a high pressure is extruded in a rod shape from the forming nozzle 714 of the end face plate 713 in a state where the melt is melted. The extruded rod-shaped material is cut into a predetermined length by a cutting machine, and as the temperature falls, the melt is solidified to obtain a solid fuel.

  FIG. 15 is a diagram showing a main part of a ring die type molding apparatus 102 as another example of the molding apparatus. This ring die type molding device 74 is a so-called pellet mill, which extrudes an object to be processed from the inside of a rotating cylindrical body 740 that is rotationally driven through a die hole 740a provided in a body portion. A pellet-shaped RPF is produced.

  This ring die type forming apparatus 74 includes a rotating cylindrical body 740 provided with a die hole 740a and two rolling cylinders 741, 741 whose outer surfaces are disposed close to the inner side surface of the rotating cylindrical body. With. The two rolling cylinders 741 are arranged at opposing positions on the diameter of the rotating cylindrical body 740, and on the surface of the rolling cylinder 741, a large number of slips of the object to be processed are reduced to facilitate uptake. An axial groove is formed. In a state where the rotating cylindrical body 740 and the rolling cylindrical bodies 741 and 741 are rotationally driven in directions indicated by arrows R1 and R2, respectively, organic carbide, waste plastic, and plant-derived waste are disposed in the rotating cylindrical body 740. The material mixed with the product is charged. The charged material is sandwiched between the inner side surface of the rotating cylindrical body 740 and the outer side surface of the rolling cylindrical body 741 and compressed, and is pushed out from the die hole 740a in the body portion of the rotating cylindrical body 740. . The extruded material is cut to a predetermined length by fixed blades 742 and 742 arranged to face the body portion of the rotating cylindrical body 740 to obtain a pellet-shaped RPF. The ring die type molding device 74 is suitable for producing a relatively small diameter solid fuel having a diameter of up to about 10 mm, and the amount of water in the workpiece before molding is small, and heating of the workpiece is not required. Is preferable.

  In addition, as a shaping | molding apparatus, although the above screw type shaping | molding apparatuses 71 and the ring die type shaping | molding apparatus 74 can be used, other types of shaping | molding apparatuses, such as a flat die type shaping | molding apparatus, can also be used, for example. Here, as a flat die type molding apparatus, a planar flat die in which a plurality of die holes are formed over an annular region, and a revolution shaft provided at the center of the annular region in which the die holes of the flat die are formed A roller that is driven to revolve around and has a roller that pushes the material supplied between the peripheral surface and the surface of the flat die into a state where the peripheral surface slides or rolls on the surface of the flat die. Can be used.

  Thus, the RPF manufactured by the screw-type molding device 71, the ring die-type molding device 74, etc. is cooled by the cooler 72 and stored in the storage silo 73. The RPF stored in the storage silo 73 is sold as fuel for various uses such as for boilers and for heating. A part of the RPF of the storage silo 73 is supplied to the steam boiler 6 as fuel.

  The steam boiler 6 of the present embodiment supplies steam as a heating medium to the vacuum fermentation drying apparatus 44 of the organic waste treatment line 3. The steam boiler 6 has a burner and a steam boiler body, and is supplied from the storage silo 73 of the solid fuel production line 5 and the fixed quantity feeder 51 of the wood waste processing line 4 as fuel for the burner. A wood chip and the combustible gas supplied from the carbonization apparatus 47 are used. The fuel of the steam boiler 6 may be at least one of these RPF, wood chips, and combustible gas. These fuels are burned by a burner, and the steam generated by the steam boiler by this combustion heat is supplied to the reduced-pressure fermentation drying apparatus 44 of the organic waste treatment line 3.

  The steam boiler 6 is formed so that indoor air is supplied as combustion air from the processing chamber 411 of the vacuum fermentation drying apparatus 44. Air in the processing chamber 411 is supplied to the burner of the steam boiler 6 by a blower (not shown). In addition, you may isolate | separate only indoor air from the condensed water and indoor air which were attracted | sucked with the vacuum pump VP of the vacuum fermentation drying apparatus 44, and you may supply to the burner of the steam boiler 6. FIG. Thereby, the air which has the odor in the process chamber 411 can be burned with a burner, and an odor can be removed. Therefore, the processing chamber 411 of the reduced pressure fermentation drying apparatus 44 can be decompressed without odor spreading to the surrounding environment.

  As described above, according to the solid fuel production plant 1 of the present embodiment, the microorganisms are added to the organic waste and heated in the reduced pressure environment by the reduced pressure fermentation drying device 44 of the organic waste treatment line 3, so that the excess sludge High-moisture organic wastes such as these can be effectively dried with a small amount of fuel consumption while reducing odor with microorganisms. Moreover, since the organic waste can be dried at a relatively low temperature of 100 ° C. or less by the reduced-pressure fermentation dryer 44, the amount of combustible gas generated from the organic waste can be suppressed. Therefore, the carbonization apparatus 47 can collect a large amount of combustible gas from the dried organic matter, and can increase the amount of fuel derived from the organic waste in the organic waste treatment line 3. As a result, the ratio of the fossil fuel to the fuel used in the organic waste treatment line 3 can be reduced, the fuel cost can be effectively reduced, and the carbon dioxide emission can be effectively reduced. Moreover, since the combustible gas produced | generated from organic waste is burned with the oil burner 475 of the carbonization apparatus 47, and the burner of the steam boiler 6, the spreading | diffusion of the odor produced from organic waste can be prevented effectively.

  Further, the moisture evaporated from the organic waste is condensed in the condensing unit 415 by the reduced-pressure fermentation drying apparatus 44, and the condensed water condensed in the condensing unit 415 and the air in the processing chamber 411 are added to the microorganisms. Since it mixes with the cooling water supplied to the condensation part 415, the spreading | diffusion of the odor which arises in the drying process of an organic waste can be prevented. In addition, since the cooling tower 430 has a deodorizing function, organic waste with a large amount of water can be effectively dried with a small apparatus configuration, and the odor diffusion of the organic waste can be prevented.

  In addition, the reduced-pressure fermentation drying apparatus 44 heats in a reduced-pressure environment to evaporate water, and condenses and recovers the water evaporated from the organic waste in the condensing unit 415. Therefore, excess sludge with a water content exceeding 98 wt%, etc. The organic waste can be quickly dried with a relatively small amount of fuel consumption without dehydration by a dehydrator. Therefore, since the process of dewatering excess sludge with a dehydrator can be eliminated, the apparatus configuration of the solid fuel production plant 1 can be simplified, and the labor of the solid fuel production process can be reduced.

  In this way, a solid fuel with less odor using an organic carbide whose odor has been reduced by carbonization can be produced while preventing odor diffusion even in the production process.

  Moreover, since the washing and dehydrator 30 of the mixed waste treatment line 2 performs the washing and dehydration by applying the turning force to the lightweight object, it is not necessary to add quick lime to dry the papers as in the past. . Therefore, the solid fuel manufactured in the solid fuel manufacturing plant 1 according to the present invention can generate less ash than the conventional ash.

  In addition, since the washing and dehydrator 30 does not heat the object to be treated, the chlorine-containing resin such as vinyl chloride contained in the object to be treated is melted by heating and adheres to other waste materials such as waste paper and waste plastic. There is nothing to do. Therefore, the adhesion of the chlorine-containing resin prevents other light weights from being used as the material for the solid fuel, thereby preventing the disadvantage that the recycling rate of the waste to the solid fuel is reduced.

  The solid fuel manufacturing plant 1 includes a mixed waste processing line 2 that processes mixed waste and extracts combustibles and waste plastics. Therefore, the waste that is input to the manufacturing plant 1 is combustible. And it does not have to be separated into incombustibles and waste plastics. Therefore, both the waste discharger and the recovery person can reduce the labor and cost for sorting the waste.

  Further, part of the RPF produced in the solid fuel production line 5 and the wood chips produced in the wood waste treatment line 4 are used as fuel for the steam boiler 6 which is a heat source device of the organic waste treatment line 3. The fuel required for drying organic waste can be reduced. In the organic waste treatment line 3, the combustible gas generated from the organic waste by the carbonization device 47 is used as fuel for the oil burner 475, and excess heat of the heat transfer medium gas discharged from the heating chamber 473 is vaporized. Since the boiler 6 is reused, the fuel of the oil burner 475 and the steam boiler 6 can be reduced. Thus, the fuel consumed in the solid fuel production plant 1 is produced from the waste put into the solid fuel production plant 1, and the surplus heat is reused in the solid fuel production plant 1. Overall, the amount of fossil fuel used can be reduced, and the increase in carbon dioxide emissions can be effectively reduced.

  The solid fuel production plant 1 of the present embodiment processes waste from a home or office in the mixed waste treatment line 2 and also generates sludge generated in a sewage treatment facility, a building site, a food factory, or the like. Is processed in the organic waste processing line 3, waste discharged in the area where the solid fuel production plant 1 is installed can be processed in a lump.

  In the above embodiment, the dried organic material obtained by drying the organic waste in the reduced-pressure fermentation drying device 44 is charged into the carbonization device 47 and carbonized. However, the dried organic material charged into the carbonization device 47 is formed into a granular shape. It is preferable to do this. The granular dry organic matter can be formed using a granulator similar to the ring die type molding device 74 of FIG. The granular dry organic material is preferably formed to have a thickness of 2 mm to 8 mm, and more preferably 4 mm to 6 mm. In addition to the ring die type molding device, other types of granulators such as a flat die type molding device can also be used. The dried organic matter granulated by the granulator is temporarily stored in a fixed amount feeder integrally formed with the storage silo, and a predetermined amount is unwound to the carbonizer 47.

  In this way, the dry organic material granulated by the granulator is carbonized by the carbonization device 47, and the dry organic material that is solidified and has few fine particles is heated in the carbonization chamber 474 of the carbonization device 47. Thereby, the fine particle of the dry organic substance and carbide mixed in the combustible gas discharged | emitted from the exhaust port 479 can be decreased. Accordingly, the combustible gas pipe 480, the carbonizer piping 481 and the boiler piping 482 for supplying the combustible gas to the heating chamber 473 and the steam boiler 6 and the heat collector of the steam boiler 6 from the heating chamber 473 to the dust collector 486 are supplied. Dust accumulated in the path of the combustion gas to reach can be reduced. That is, by drying and solidifying the dry organic matter carbonized by the carbonization device 47, dust of the combustible gas recovered by the carbonization device 47 can be reduced. As a result, combustion or heating of the combustible gas in the heating chamber 473 can be achieved. The above-mentioned combustible gas can be used for a plurality of uses, such as reusing the surplus heat burned in the chamber 473 in the steam boiler 6 and burning the combustible gas in the steam boiler 6. Moreover, by solidifying the dry organic substance carbonized with the carbonization apparatus 47 into a granular form, the loss by the production | generation of dry organic substance and the dust of organic carbide can be reduced, and the yield of organic carbide can be raised.

  Moreover, in the said embodiment, while throwing a general waste into the mixed waste treatment line 2 and extracting a combustible material and forming a binder, an organic waste is thrown into the organic waste treatment line 3 and organic carbide is made into Organic matter such as garbage that has been formed but extracted from the mixed waste in the mixed waste treatment line 2 is put into the reduced-pressure fermentation drying device 44 of the organic waste treatment line 3 to perform the drying treatment, and then the carbonization device The carbonized organic material may be formed by carbonization at 47.

  In the above embodiment, a part of the combustible gas generated by the carbonization device 47 of the organic waste treatment line 3 is used as the fuel for the steam boiler 6, but the combustible gas generated by the carbonization device 47 is used as the fuel for the steam boiler 6. It does not have to be used for.

  Further, in the above embodiment, surplus sludge is used as organic waste, but as organic waste, sludge accumulated on the bottom of lakes and seas, waste discharged in the agricultural and fisheries industry, and discharged from food factories. You may use the organic substance with high water | moisture content produced with the production process and waste water treatment of various industries, such as food residue and garbage discharged | emitted from a general household.

  Further, in the present embodiment, waste plastics and plant-derived wastes such as waste paper and wood chips are used as the binder to be mixed with the organic carbide. However, the binder only needs to contain at least a thermoplastic plastic component. .

  In the said embodiment, although the organic carbide was formed with the carbonization method of the organic waste of this invention in the organic waste processing line 3, and the solid fuel was manufactured using this organic carbide, the organic waste of this invention was illustrated. The organic carbide formed by the carbonization method may be used as a fertilizer, a flocculant, an adsorbent, a filter medium, a soil conditioner, a snow melting agent, or a reducing agent in addition to fuel.

DESCRIPTION OF SYMBOLS 1 Production plant of solid fuel 2 Mixed waste processing line 3 Organic waste processing line 4 Wood waste processing line 5 Solid fuel production line 44 Low pressure fermentation drying apparatus 47 Carbonization apparatus 71 Molding apparatus

Claims (10)

The organic waste is heated in a reduced pressure environment with the addition of microorganisms, thereby reducing the amount of combustible gas produced from the organic waste and forming a dry organic matter,
A condensation step of condensing moisture evaporated from the organic waste in the vacuum drying step;
In the condensation process, water is cooled, and the cooling water to which microorganisms are added is mixed with the condensed water produced in the condensation process and the gas containing the odor produced in the reduced pressure drying process, and the cooling water is cooled. A mixing and cooling step;
A carbonization step of heating the dry organic matter in a low oxygen environment to form an organic carbide and generating a combustible gas;
The flammable gas generated from the drying organics above carbonization step, the carbonization combustion process for burning as a fuel for heating in the upper Kisumi step,
A combustion process for drying that combusts a combustible gas generated from a dry organic substance in the carbonization process as a fuel for heating in the vacuum drying process , and a mixed molding process that mixes and molds the organic carbide with a binder A method for producing a solid fuel. In the manufacturing method of the solid fuel of Claim 1,
A method for producing a solid fuel, wherein excess heat of heating in the carbonization step is used for heating in the vacuum drying step. In the manufacturing method of the solid fuel of Claim 1,
A method for producing a solid fuel, comprising: a combustion air supply step for supplying the gas generated in the vacuum drying step as combustion air for heating organic waste in the vacuum drying step. In the manufacturing method of the solid fuel of Claim 1,
Before the carbonization step, comprising a granulation step of granulating the dry organic matter formed in the vacuum drying step,
A method for producing a solid fuel, comprising heating the granulated dry organic matter in the carbonization step. A reduced-pressure drying device that forms dry organic matter by suppressing the amount of combustible gas generated from the organic waste by heating the organic waste to which microorganisms are added in a reduced-pressure environment;
A carbonization device that heats the dried organic matter in a low oxygen environment to form an organic carbide and generate a combustible gas;
The organic carbide is formed by mixing with a binder and forming, and forming a solid fuel,
The reduced-pressure drying apparatus includes a casing in which organic waste is introduced and decompresses the inside, a stirring unit that is rotatably disposed in the casing and stirs the organic waste, and is disposed in at least a part of the casing for organic waste. A heating unit that heats the product, a condensing unit that condenses the vapor from the organic waste, cooling water supplied to the condensing unit to which microorganisms are added, condensed water generated in the condensing unit, and the organic A suction pump for sucking a gas containing odor generated by drying waste from the casing, and a mixing cooler for mixing the cooling water with the condensed water sucked by the suction pump and the gas and cooling the cooling water And
For heating of the upper Kisumi KaSo location, generated from dry organics above carbonization apparatus combustible gas with Ru it is used as a fuel, for heating the vacuum drying device, produced from dried organics above carbonization apparatus A solid fuel production plant, wherein a combustible gas is used as a fuel. In the solid fuel manufacturing plant according to claim 5,
A solid fuel production plant characterized in that surplus heat generated when the dried organic matter is heated by the carbonization apparatus is supplied to the heating section of the reduced-pressure drying apparatus and used. In the solid fuel manufacturing plant according to claim 5,
A solid fuel comprising a second suction pump for sucking the gas in the casing of the vacuum drying apparatus and supplying the suctioned gas as combustion air to a heat source device for heating the vacuum drying apparatus Production plant. In the solid fuel manufacturing plant according to claim 5,
A solid fuel production plant comprising a granulation device formed by the vacuum drying device and granulating dry organic matter before being charged into the carbonization device. In the solid fuel manufacturing plant according to claim 5,
The solid fuel manufacturing plant, wherein the binder includes at least one of a wood material, a paper material, and a plastic material. In the solid fuel manufacturing plant according to claim 5,
A solid fuel production plant, characterized in that a wood material powder is added to the organic waste processed by the vacuum drying apparatus.

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