JP2006321851A - Apparatus and method for pyrolytic conversion into oil, apparatus for treating waste by pyrolysis, and apparatus for recovering valuable metal - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an apparatus for pyrolytic conversion into oil which can attain a high rate of recovery of hydrocarbon oils from plastic wastes. <P>SOLUTION: This apparatus is provided with a conveying part 18 which is set in a pyrolysis vessel 10 and conveys plastics in a particulate, crushed, semi-molten, or molten state in the direction of the transfer axis of the pyrolysis vessel 10, the pyrolysis vessel 10 which heats the plastics fed on the upstream side of the conveying part 18 inside the pyrolysis vessel 10 to produce a pyrolyzed gas and discharges unpyrolyzed residues on the downstream side, a cooling-type oil recovery part 50 which cools the pyrolyzed gas obtained in the pyrolysis vessel 10 to recover hydrocarbon oils, and a spray-type oil recovery part 60 which sprays the pyrolyzed gas cooled in the cooling-type oil recovery part 50 with an oil to recover hydrocarbon oils. <P>COPYRIGHT: (C)2007,JPO&INPIT

Description

  The present invention relates to a pyrolysis oil converting apparatus and method for thermally decomposing plastic waste containing a halogen-based element such as polyolefin-based thermoplastic plastic, wood chips, vinyl chloride, etc., and taking it out as hydrocarbon oil.

  The present invention also relates to a pyrolytic waste treatment apparatus for effectively treating waste using a composite material of plastic such as glass fiber reinforced plastic (FRP) and heat resistant glass fiber.

  Furthermore, the present invention relates to a valuable metal recovery device for effectively recovering metal from waste using a composite material of plastic and silver (metal) such as X-ray photographic film.

  Regarding the disposal of plastic waste, it is requested to treat it in a waste treatment facility that satisfies the permission standards based on the Waste Treatment Law. And in addition to the conventional incineration process in the law enforcement order based on the Waste Treatment Law, thermal decomposition process (Article 3 No. 2 b). And the structure of the thermal decomposition equipment is prescribed | regulated to the case of producing | generating hydrocarbon oil or a carbide | carbonized_material in the 1st article 2-7 1st of the enforcement regulations of the law.

  In addition, diligent research has been conducted on the practical application of an oil converting device that recycles hydrocarbon oil from plastic waste. In particular, recycled hydrocarbon oil can replace crude oil, and the price of crude oil has risen several times as many as US $ 10 per barrel, several years ago, as in recent years. In Japan, a resource-free country, the importance is increasing not only for waste disposal and environmental measures, but also for resource and energy measures.

  Therefore, for example, as disclosed in Patent Document 1, a plastic oil converting apparatus is known that thermally decomposes plastic waste and converts it into hydrocarbon oil. In this type of plastic oil conversion equipment, plastic waste is put into a decomposition vessel and thermally decomposed, and the resulting pyrolysis gas is led to a catalyst tank, where it is decomposed into low-boiling components and further led to a cooling device for carbonization. A configuration for obtaining hydrogen oil is employed.

JP 2002-30179 A

  However, when the inventor actually used the plastic oil converting apparatus according to Patent Document 1, it was found that the following problems exist. First, the hydrocarbon oil recovery rate from plastic waste is low. Under typical operating conditions of this apparatus, about 0.20 to 0.25 kg of hydrocarbon oil is obtained for 1 kg of the raw plastic. In other words, the hydrocarbon oil recovery rate is as low as about 20-25%, and the regulation value 40% set in the enforcement regulations as an oiling device for pyrolysis treatment (Waste Treatment Law Enforcement Ordinance Article 3 No. 2) There is a problem that cannot be achieved.

  Second, plastic waste contains not only three major plastics such as polyethylene (PE), polypropylene (PP) and polystyrene (PS), but also those containing halogen elements such as vinyl chloride. is there. If separated collection progresses, it is theoretically possible to separate the three major plastics and plastic waste containing halogen-based elements. However, for example, transparent plastic sheets for packaging food and the like include polyethylene-based and poly (vinylidene chloride) -based materials, but it is practically difficult to separate them from dust collected as waste.

  And the hydrocarbon oil containing halogen like chlorine shortens the lifetime of a general purpose burner remarkably. Some large-scale burners used in thermal power plants and the like have a halogen countermeasure that can use heavy oil containing salt as a fuel, and hydrocarbon oils containing halogen such as chlorine (for example, 900 ppm) are also possible. . However, there arises a problem that the cost of collecting hydrocarbon oil from the dust incineration facilities distributed in various places and transporting it to the use facility of the burner for which halogen countermeasures are taken increases. Therefore, it is necessary to reduce the chlorine content of the hydrocarbon oil to the chlorine content standard (for example, 100 ppm) of the hydrocarbon oil set by the Packaging Container Recycling Association. However, the proportion of vinyl chloride or the like contained in plastic waste is not constant, and the installation of a hydrocarbon oil chlorine removal device has a problem that the burden of equipment costs increases.

  Furthermore, glass fiber reinforced plastic (FRP) has been in widespread use for several decades, but waste disposal has become a problem with the end of its useful life. That is, since FRP is a composite material of plastic and heat-resistant glass fiber, the actual situation is that there is only landfill treatment as waste treatment. In a typical case, the glass fiber content is about 50% to 80% and the balance is plastic. In this case, in order to improve heat resistance and durability, a plastic combined with a halogen element such as chlorine is used. Therefore, when trying to incinerate FRP, in addition to the combustion temperature becoming as high as about 1000 degrees C., if the plastic contains a halogen element, the incinerator is severely damaged by the separated halogen element. There is a problem of becoming.

  There is also a large amount of waste using a composite material of plastic and silver (metal) such as X-ray photographic film. However, an apparatus for effectively recovering valuable metals such as metals from a composite material of plastic and silver (metal) has not been sufficiently developed. In general, it is known that a composite material of plastic, heat-resistant glass fiber, and a noble metal such as gold or silver, such as a printed circuit board, has a high noble metal content even compared to a noble metal ore. That is, in the precious metal ore, the precious metal content ratio per ton of the rough ore is known to be about 10 to 20 g in gold ore. On the other hand, some plastic wastes have a higher content ratio than precious metal ores. However, the difference between plastic waste and precious metal ore is that precious metal ore can separate non-precious earth and stone relatively easily, whereas plastic waste is effectively made of non-precious plastic and heat-resistant glass fiber. It cannot be removed.

  This invention solves the subject mentioned above, and the 1st objective is to provide the pyrolysis oil-ized apparatus and method with a high oil recovery rate from plastic waste. The second object is to provide a pyrolysis oil conversion apparatus and method in which the recovered hydrocarbon oil has a low chlorine content even if it is a plastic waste containing a halogen-based element such as vinyl chloride.

  A third object is to provide a thermal decomposition waste treatment apparatus for effectively treating waste using a composite material of plastic and heat-resistant glass fibers without incineration. A fourth object is to provide a valuable metal recovery device that effectively recovers valuable metals from a composite material of valuable metals such as plastic and silver without using incineration.

  The pyrolysis oil converting apparatus of the present invention that achieves the first object is, for example, as shown in FIG. 1, a conveying unit 18 installed in the decomposition vessel 10, in a granular, crushed state, and semi-molten state. Alternatively, the molten plastic body is transported in the moving axis direction of the decomposition container 10 and the plastic body charged on the upstream side of the transport section 18 is heated in the decomposition container 10 for thermal decomposition. A cracking vessel 10 that generates gas and discharges residues left by pyrolysis on the downstream side, and a cooling-type oil recovery unit 50 that cools the pyrolysis gas obtained in the cracking vessel 10 and collects hydrocarbon oil. And a spray-type oil recovery unit 60 that recovers hydrocarbon oil by spraying the oil on the pyrolysis gas cooled by the cooling-type oil recovery unit 50.

  In the apparatus configured as described above, the plastic body is in a granular, crushed state, semi-molten state or melted state, so that it can be easily transported by the transport unit 18 provided inside the decomposition container 10 and the decomposition container 10. The pyrolysis gas inside is rapidly generated. The transport unit 18 transports the plastic body in the direction of the moving axis of the decomposition container 10, and heats the inside of the decomposition container 10 to secure a residence time for generating pyrolysis gas, while the pyrolysis solids on the downstream side. The remaining residue in minutes is discharged. In the cooling type oil component recovery unit 50, the pyrolysis gas obtained in the decomposition vessel 10 is cooled to recover hydrocarbon oil. In the spray type oil component recovery unit 60, the oil component is sprayed on the pyrolysis gas cooled by the cooling type oil component recovery unit 50 to recover the hydrocarbon oil. In this manner, pyrolysis gas is generated from the granular, crushed, semi-molten or molten plastic body inside the cracking vessel 10, and the pyrolysis gas is separated from the cooling oil recovery unit 50 and the spray oil recovery unit 60. By collecting in two stages, the recovery rate of hydrocarbon oil from plastic waste is increased.

  In the pyrolysis oil converting apparatus of the present invention, for example, as shown in FIG. 1, an oil content refining unit 70 for refining the hydrocarbon oil recovered by the cooling type oil content recovery unit 50 and the spray type oil content recovery unit 60 is provided. When the hydrocarbon oil refined by the oil refining unit 70 is used for heating the cracking vessel 10, the hydrocarbon oil can be used as a fuel for heating the cracking vessel 10, which contributes to a reduction in operating costs.

  In the pyrolysis oil converting apparatus of the present invention, as shown in FIG. 4, for example, a volume reduction processor 130 for pre-processing a plastic-containing body to be processed by the pyrolysis oil converting apparatus into a granular or semi-molten plastic body is further provided. The plastic body having the pre-processed by the volume reduction processor 130 is supplied to the decomposition container 10. According to such a configuration, even a plastic-containing body including various shapes and inclusions is pre-processed into a granular or semi-molten plastic body by the volume reduction processing machine 130. Can be smoothly carried out, and thermal decomposition in the decomposition vessel 10 of the pyrolysis oil converting apparatus can be performed quickly.

  In the pyrolysis oil converting apparatus of the present invention, in order to achieve the second object, as shown in FIG. 4, for example, the plastic-containing body to be processed by the pyrolysis oil converting apparatus is in a granular or semi-molten plastic. And a halogen separation tank 140 for maintaining the plastic body pretreated by the volume reduction processor 130 at a halogen element separation temperature, and dehalogenated in the halogen separation tank. A granular or semi-molten plastic body is supplied to the decomposition container 10.

  According to such a configuration, even a plastic-containing body including various shapes and inclusions is pre-processed into a granular or semi-molten plastic body by the volume reduction processing machine 130. Can be smoothly carried out, and thermal decomposition in the decomposition vessel 10 of the pyrolysis oil converting apparatus can be performed quickly. Further, since the plastic body pretreated by the volume reduction processor 130 is held at the halogen element separation temperature by the halogen separation tank 140 and dehalogenated, the halogen element contained in the plastic container is the decomposition container 10. Does not corrode, and the halogen element contained in the hydrocarbon oil is also greatly reduced.

  In the pyrolysis oil converting apparatus of the present invention, in order to achieve the second object, for example, as shown in FIG. 4, the plastic containing body or plastic body to be processed by the pyrolysis oil converting apparatus is further limestone. It is good to set it as the structure provided with the calcium supply means 120 which supplies calcium components, such as. Then, when the plastic-containing body is PET (polyethylene terephthalate) and nylon, even if other transparent plastics containing chlorine are mixed, calcium is combined with chlorine gas that separates with thermal decomposition. It becomes calcium chloride, the chlorine component contained in the pyrolysis gas is reduced, and the chlorine component is not mixed into the hydrocarbon oil, so that a high quality hydrocarbon oil can be obtained.

  In the pyrolysis oil converting apparatus of the present invention, in order to further achieve the second object, for example, as shown in FIG. 5, at least one of the cooling oil recovery unit 50 or the spray oil recovery unit 60 is recovered. The hydrocarbon oil may be brought into contact with an alkali metal compound in the pressure / temperature range of the halogen detachment process to provide a desalting unit 160 for detaching the halogen element contained in the hydrocarbon oil. According to such a configuration, the hydrocarbon oil recovered by at least one of the cooling-type oil component recovery unit 50 or the spray-type oil component recovery unit 60 is maintained at the halogen element separation temperature by the desalination processing unit, and dehalogenated. Since it is processed, the halogen element contained in the hydrocarbon oil is greatly reduced. The halogen element separation temperature is typically set to a temperature of 200 ° C. to 300 ° C. and a pressure of 100 atm to 200 atm.

  The pyrolysis oil conversion method of the present invention that achieves the above first object is, for example, as shown in FIG. 2, in the granular, crushed state, and semi-molten state upstream of the conveying unit 18 installed in the decomposition vessel 10. Alternatively, a molten plastic body is charged (S102), while the plastic body is transported to the downstream side of the transport section 18, heating is performed to generate pyrolysis gas (S106), and the plastic body remains on the downstream side of the transport section 18 (S108), the pyrolysis gas obtained in the cracking vessel 10 is cooled to recover hydrocarbon oil (S114), and the oil is sprayed onto the cooled reformed gas to obtain hydrocarbon oil. Is recovered (S118).

  The pyrolysis waste disposal apparatus of the present invention that achieves the third object includes a crushing means 110 for crushing fiber reinforced plastic and a fiber reinforced plastic crushed by the crushing means 110, as shown in FIG. A plastic body attached to the crushed fiber, which is a volume reduction processing machine 130 that pre-treats into a granular or semi-molten state, and a conveying unit 18 installed inside the decomposition vessel 10, and crushed fiber The plastic body attached to the minute is transported in the direction of the moving axis, and the plastic body charged on the upstream side of the transport section 18 is heated inside the decomposition container 10 to generate pyrolysis gas. At the same time, a decomposition vessel 10 that discharges the crushed fibers remaining in the pyrolysis on the downstream side, and a cooling-type oil collection unit 50 that cools the pyrolysis gas obtained in the decomposition vessel 10 and collects hydrocarbon oil. , The pyrolysis gas that has been cooled in the cooling type oil recovery unit 50, and a spray-type oil recovery unit 60 for recovering the hydrocarbon oil by spraying the oil.

  According to such a configuration, the fiber reinforced plastic is crushed by the crushing means 110 and is attached to the fiber crushed by the volume reduction processor 130, and is pretreated in a granular or semi-molten state. Therefore, the conveyance in the conveyance part 18 can be performed smoothly, and the thermal decomposition in the decomposition container 10 of the pyrolysis oil converting apparatus can be performed quickly. Moreover, since the fiber content contained in the residue is shortened and the plastic component is a small proportion of the pyrolyzed solid content, it is easy to dispose of and regenerate the fiber content. Further, the plastic body contained in the fiber reinforced plastic is recovered as hydrocarbon oil by the cooling oil recovery unit 50 and the spray oil recovery unit 60.

  The valuable metal recovery apparatus of the present invention that achieves the fourth object described above, for example, as shown in FIG. 4, is a volume reduction process for pre-processing a plastic-containing body containing a valuable metal into a granular or semi-molten plastic body. Machine 130, a transport unit 18 installed inside decomposition container 10, a transport unit 18 that transports the plastic body in the direction of the moving axis, and a plastic body introduced upstream of transport unit 18. The decomposition vessel 10 is heated inside the decomposition vessel 10 to generate pyrolysis gas, and the decomposition vessel 10 that discharges residues containing valuable metals remaining on the downstream side, and the pyrolysis obtained in the decomposition vessel 10 Cooling-type oil recovery unit 50 that cools gas and recovers hydrocarbon oil, and spray-type oil recovery that recovers hydrocarbon oil by spraying oil on the pyrolysis gas cooled by cooling-type oil recovery unit 50 Part 60 and From the residue containing the discharged valuable metals by the decomposition container 10 is for recovering valuable metals.

  According to such a configuration, since the plastic-containing body containing valuable metals is pre-processed into a granular or semi-molten plastic body by the volume reduction processing machine 130, the transport in the transport unit 18 can be performed smoothly. At the same time, the thermal decomposition in the decomposition vessel 10 of the pyrolysis oil converting apparatus can be performed quickly. Moreover, the ratio of the valuable metal contained in the residue increases. Therefore, the valuable metal can be easily recovered and recycled. Further, the plastic-containing body is recovered as hydrocarbon oil by the cooling type oil content recovery unit 50 and the spray type oil content recovery unit 60.

  According to the pyrolysis oil converting apparatus and method of the present invention, since the plastic body is granular, crushed, semi-molten or melted, it can be smoothly transported by the transport unit 18 and the decomposition container of the pyrolysis oil converting apparatus. Pyrolysis at 10 can be done quickly. In addition, pyrolysis gas is generated from granular, crushed, semi-molten or melted plastic bodies inside the cracking vessel, and this pyrolysis gas is recovered in two stages, a cooling oil recovery unit and a spray oil recovery unit. By doing so, the recovery rate of hydrocarbon oil from plastic waste is increased.

  According to the pyrolysis oil converting apparatus of claim 4, even if the plastic containing body includes various shapes and inclusions, the plastic body pretreated by the volume reduction processing machine by the halogen separation tank, Since the dehalogenation treatment is performed while maintaining the element separation temperature, the decomposition vessel is not corroded by the halogen element contained in the plastic body, and the halogen element contained in the hydrocarbon oil is greatly reduced. Also according to the pyrolysis oil converting apparatus of claim 6, the desalination treatment unit holds the hydrocarbon oil recovered at least one of the cooling type oil recovery unit or the spray type oil content recovery unit at the halogen element separation temperature, Since the dehalogenation treatment is performed, the halogen elements contained in the hydrocarbon oil are greatly reduced.

  Hereinafter, embodiments of the present invention will be described with reference to the drawings.

  The plastic waste to be processed by the pyrolysis oil converting apparatus of the present invention is preferably a granular plastic body such as RDF (refuse derived fuel) or a semi-molten plastic body. If the plastic waste has a large shape or is a molded product made of fiber reinforced plastic, it cannot be treated with the rotary kiln that constitutes the decomposition container 10 as it is, so it is pretreated with a crusher or volume reduction processor. Thus, it is preferable to form a plastic body in a granular, crushed state, semi-molten state or molten state. The granular form is, for example, processed into a pellet having a diameter of about several centimeters and a length of about several centimeters. In the case of RDF, for example, it is a cylinder having a diameter of 50 mm and a length of 100 mm. The crushed state refers to a state in which plastic waste is crushed into a shape of about several centimeters, and includes a pulverized state in which the crushed state is granular.

  The main plastic waste is polyethylene, polypropylene, polystyrene, polyethylene terephthalate, polyamide resin, and the like. Examples of polyethylene include high density polyethylene, low density polyethylene, and linear low density polyethylene. Polypropylene melting point 160 ° C-170 ° C, polystyrene melting point 240 ° C (decomposition temperature 300 ° C), polyethylene terephthalate melting point 264 ° C, nylon 66 melting point 265 ° C, nylon 6 melting point 215 ° C, plastic waste Shifts to a molten state at about 260 ° C.

  FIG. 1 is a block diagram for explaining a pyrolysis oil converting apparatus as a first embodiment of the present invention. In the figure, the pyrolysis oil converting apparatus includes a cracking vessel 10, a cooling oil recovery unit 50, a spray oil recovery unit 60, and an oil / water separator 70 as an oil refining unit as main components. The plastic body is preferably in a granular or semi-molten state. Here, the plastic body is sent to the input port 20 of the decomposition container 10 by the input hopper 2, blower 4, shooter 6, and transport pipe 8. By providing the charging hopper 2, it is possible to facilitate the charging of the plastic body, and for example, a fixed amount is supplied using a conveyor or the like. The blower 4 is a device that generates high-pressure air and serves as an air source for conveyance. The shooter 6 serves as a pump, generates a negative pressure on the upper side of the shooter 6, takes a plastic body falling from the charging hopper 2, and sends it to the transport pipe 8. In addition to the granular or semi-molten plastic body, the transport pipe 8 can also supply a crushed or molten plastic body to the inlet 20 of the decomposition vessel 10.

  The decomposition container 10 includes an outer casing 12, a kiln outer cylinder part 14, a kiln inner cylinder part 16, and a convex blade (screw) 18 as a conveying part. The outer casing 12 is, for example, a cylinder having a rectangular cross section, a horseshoe shape, or a circular shape that extends horizontally, and a heat insulating material is attached to the outer wall to reduce heat dissipation. Inside the outer casing 12, a kiln outer cylinder part 14, a kiln inner cylinder part 16, and a convex blade 18 constituting a rotary kiln are housed. The kiln outer cylinder portion 14 is a rotating outer cylinder portion, and a driving force is supplied from an electric motor 32 via a power transmission mechanism 30 such as a belt, a chain, or a gear. The kiln inner cylinder part 16 is formed integrally with the kiln outer cylinder part 14 on the outer peripheral side, and has convex blades 18 formed on the inner peripheral side, such as carbon steel or stainless steel with anticorrosion measures. It is made of a structural material that has high heat resistance and is easy to weld. The convex blade 18 conveys the granular, crushed state, semi-molten state or molten state plastic body introduced from the introduction port 20 to the discharge port 22, for example, 3 to 3 in the inner circumferential direction of the kiln inner cylinder portion 16. About 8 are formed.

  The heating chamber 15 is a space surrounded by the kiln outer cylinder portion 14 and the kiln inner cylinder portion 16 and covers the outer periphery of the kiln inner cylinder portion 16. Superheated air of about 350 ° C. to 500 ° C. is supplied from the hot stove 34 to the heating chamber 15, and the periphery of the kiln inner cylinder portion 16 is maintained at about 300 ° C. to 400 ° C. Then, the temperature of the convex blade | wing 18 is also hold | maintained at the temperature about several to several tens of degrees C lower than the kiln inner cylinder part 16. The blower 36 supplies air to the hot stove 34. The kiln inner cylinder part 16 may be heated by installing an external heat source such as an electric heater in the heating chamber 15 or by installing a burner on the discharge port 22 side to send hot air from the burner to the kiln inner cylinder. A format in which the data is sent into the portion 16 may be used.

  The rotary kiln may be substantially horizontal at the charging port 20 and the discharging port 22 as shown in the figure, but the charging port 20 so that the heat supplied from the wall surface of the kiln inner cylinder part 16 is efficiently transmitted to the plastic body. The position may be lower than that of the discharge port 22. When the rotary kiln is tilted in this way, the plastic body is lifted up by the convex blades 18 as the kiln inner cylinder portion 16 rotates, so that the plastic body is effectively mixed and the temperature distribution becomes uniform. The rotary kiln may be appropriately designed according to the processing capacity of plastic waste. For example, in the case of 200 [kg / hr], the rotary kiln has a shape with a diameter of about 1 m and a length of about 8 m.

  In addition, for example, plastic waste enters a molten state at about 260 ° C., and further, thermal decomposition is promoted at about 300 ° C., so temperature management is important. The temperature at which chlorine is separated from chloride plastic such as vinyl chloride resin is, for example, 280 ° C. to 320 ° C., preferably about 300 ° C. On the other hand, depending on the type of plastic, the thermal decomposition reaction may proceed abruptly. Therefore, it is preferable to remove in advance the plastic having an unstable property that is not suitable for the thermal decomposition treatment in the plastic contained in the plastic body.

  Further, a catalyst (for example, zeolite) for cutting a chain of carbon atoms may be applied to the back side of the blade of the convex blade 18. The convex blade 18 is disposed in the kiln inner cylinder portion 16 and has a temperature suitable for a reaction for breaking the carbon atom chain of the pyrolysis gas by zeolite. Further, the plastic waste is pushed forward on the front side of the convex blade 18, and if it is on the back side, the applied catalyst is unlikely to fall off. In this way, a reaction for breaking the carbon atom chain of the pyrolysis gas can be caused in the kiln inner cylinder portion 16, and the plastic waste is a compound having a long carbon chain. The oiling efficiency is improved as a whole device.

The insertion port 20 is provided at one end of the rotary kiln, and has a structure that can ensure a sealed state of the rotary kiln even when plastic waste is supplied from the transport pipe 8. The discharge port 22 is located at the other end of the convex blade 18 of the rotary kiln, and the pyrolysis gas and pyrolysis solid content pyrolyzed by the kiln inner cylinder portion 16 are separated by gravity. The pyrolysis gas outlet 24 is an outlet for sending the pyrolysis gas from the discharge port 22 to the cooling oil recovery unit 50. The pyrolysis gas is mainly hydrocarbon gas CnHm (n and m are integers m≈2n to 2n + 2), but when CO + H ₂ O in which pyrolysis has progressed or plastic waste contains elemental nitrogen Includes nitrogen.

  In the residue discharge port 26, pyrolyzed solid content that has not been thermally decomposed in the kiln inner cylinder portion 16 is sent to the residue cooling chamber 40, and here, drop by gravity is used. For example, moisture remains in the residue cooling chamber 40, and the pyrolyzed solid content that has fallen is cooled in the residue cooling chamber 40, and particulates of the pyrolyzed solid content are captured by the cooling water, and dust is scattered, etc. The problem is not to occur. The pyrolysis solid content cooled in the residue cooling chamber 40 is discharged to the outside of the residue cooling chamber 40 by the conveyor 42 using the driving force of the motor 44. Since the pyrolysis solid content is a residue of plastic waste, it may be a valuable or a non-valueable component. Therefore, in the case of valuable materials, the pyrolysis solid content is recycled, and in the case of non-value items, final disposal processing such as landfill is performed.

  The thermometer 28 measures the temperature of the kiln inner cylinder portion 16, and uses a temperature measuring element that can measure the temperature up to about 1000 ° C., such as a thermocouple or a resistance temperature detector. The operation control device (CTL) 29 controls the temperature measured by the thermometer 28 to be a set temperature, for example, 270 ° C. to 300 ° C. For example, when the furnace temperature is lower than the set temperature, the thermal energy supplied from the hot stove 34 to the heating chamber 15 is increased, or the granular, crushed state, semi-molten state or molten state from the transport pipe 8 is increased. Feedback control is performed to reduce the supply amount of the plastic body or to reduce the conveying speed of the convex blade 18. The temperature control of the kiln inner cylinder part 16 is an important control element that determines the decomposition rate of pyrolysis oil conversion, and most of the input plastic body is converted into pyrolysis gas to be recovered as pyrolysis oil. Determine as follows. It is not desirable for the residue to be recycled or disposed of that the residue should be separated as a pyrolysis gas.

  For example, a heat exchanger is used for the cooling type oil recovery unit 50, and the pyrolysis gas flowing in the pipe of the heat exchanger and the cooling water flowing in the outer wall of the pipe of the heat exchanger exchange heat, and the pyrolysis gas. Is cooled and condensed to produce a recovered oil containing hydrocarbon oil. The recovered oil take-out conduit 52 is provided at the lower part of the cooling type oil content collector 50, and the generated recovered oil content is sent to the recovered oil content tank 56. The cooling fan 54 cools the inside of the cooling type oil recovery unit 50, and cancels out the thermal energy accompanying the pyrolysis gas. In addition, although the case where there is one cooling type oil recovery unit is shown, it can be appropriately arranged according to the processing capacity and the oil recovery rate, for example, two or more units may be connected in series, or in parallel You may connect to.

  The oil spray tower (oil scrubber) 60 is provided downstream of the cooled oil recovery unit 50, and performs oil recovery by spraying the oil on the uncondensed carbon compound in the cooled pyrolysis gas. At the same time, dust is removed. The spray-recovered oil take-out conduit 62 is provided at the lower part of the oil spray tower 60, and the recovered oil containing hydrocarbon oil recovered by the oil sprayed by the oil spray tower 60 is sent to the recovered oil tank 56. It is done.

  The reducing device 64 reduces the off gas discharged from the oil spray tower 60 with an alkaline solution such as limestone. The off-gas contains various combustible gases such as carbon monoxide, methane, and hydrogen in addition to water vapor. The off-gas combustion furnace 66 emits exhaust gas detoxified in the atmosphere by burning with off-gas reduced by the reducing device 64 and external air.

  The recovered oil stored in the recovered oil tank 56 contains hydrocarbon oil and moisture. The oil / water separators 70a and 70b remove water contained in the recovered oil and purify it into hydrocarbon oil. Preferably, a filter is provided to remove particulate components such as dust contained in the recovered oil. For example, a centrifugal separator is used as the oil / water separators 70a and 70b, and the oil / water separators 70a and 70b are separated using a difference in specific gravity between water and oil. For example, a light component having a specific gravity of 0.85 or less is sent to the hydrocarbon oil tank 72 as extracted oil, and a heavy component having a specific gravity of 0.85 or more is sent to the waste liquid tank 78 as waste liquid. The waste oil in the waste liquid tank 78 contains pitch and heavy oil, and is incinerated, for example. The water contained in the waste oil in the waste liquid tank 78 is separated from the waste oil due to the difference in specific gravity.

  The hydrocarbon oil tank 72 stores the hydrocarbon oil refined by the two-stage oil / water separators 70a and 70b. The hydrocarbon oil circulation pipe 76 is a pipe connecting the hydrocarbon oil tank 72 and the oil spray pipe of the oil spray tower 60. The hydrocarbon oil stored in the hydrocarbon oil tank 72 is circulated and used as oil to be sprayed by the oil spray tower 60 by the circulation pump 74 and the hydrocarbon oil circulation pipe 76.

  The operation of the apparatus configured as described above will be described. FIG. 2 is a flowchart for explaining the pyrolysis oil conversion method of the present invention. First, plastic waste is carried in by, for example, a dump truck (S100). For the plastic waste, a granular, crushed, semi-molten or molten plastic body is used so that it can be separated into pyrolysis gas and residue within the rotary kiln-type decomposition vessel 10 and the kiln residence time. Preferably, plastic waste is limited to those made of polyethylene, polypropylene, polystyrene, polyethylene terephthalate, polyamide resin, etc., which are the main targets of thermal decomposition, and does not contain unstable substances that cause rapid thermal decomposition. Like that.

  Next, the carried plastic waste is sent to the input port 20 of the decomposition container 10 by the input hopper 2, the blower 4, the shooter 6, and the transfer pipe 8 (S102). The thrown plastic waste is slowly conveyed downstream in the kiln inner cylinder portion 16 by the convex blade 18 (S104). At this time, since the kiln inner cylinder portion 16 and the convex blades 18 are maintained at the thermal decomposition temperature of about 300 ° C. by the heating chamber 15, the plastic waste is also heated to the thermal decomposition temperature and within the kiln stay time. It is separated into pyrolysis gas and residue (S106). The kiln staying time is, for example, about 30 minutes to 1 hour. The length of the kiln outer cylinder part 14 and the kiln inner cylinder part 16 and the substantial conveyance of the plastic waste by the rafting accompanying the rotation of the convex blade 18 are achieved. Determine the speed.

  Since plastic waste contains glass fiber and metal foil, there is a residue as a pyrolytic solid even after the plastic is pyrolyzed and gasified. The pyrolyzed solid content adheres to the inner surface of the kiln inner cylinder portion 16, but is immediately scraped off by the blades of the convex blades 18 and sent downstream. Thus, the pyrolysis solid content is finally sent from the residue discharge port 26 to the residue cooling chamber 40, cooled, and discharged as a residue from the pyrolysis oil converting apparatus by the conveyor 42 (S108). The residue is collected if there is a valuable material and discarded if it is a non-valueable material (S110).

  On the other hand, the pyrolysis gas exits from the kiln inner cylinder portion 16 through the pyrolysis gas outlet 24, and is sent to the cooling oil recovery unit (heat exchanger) 50 (S112). The pyrolysis gas flows in the pipe as the heat exchanger and is cooled by touching the cooling water on the outer wall of the pipe. Therefore, the pyrolysis gas is separated into hydrocarbon oil and uncondensed gas by the cooling type oil recovery unit 50 (S114). The uncondensed gas is sent to the oil spray tower 60 (S116), and the non-condensed gas is separated into hydrocarbon oil and off-gas by the oil spray tower 60 (S118). The off-gas is sent to the reducing device 64 to remove the chlorine component, and the off-gas combustion process is performed in the off-gas combustion furnace 66 to discharge to the atmosphere (S120).

  The hydrocarbon oil is obtained together with the water condensed in the cooling type oil recovery unit 50 and is also recovered from the oil spray tower 60. Therefore, since the hydrocarbon oil is a mixed solution with moisture, the hydrocarbon oil is separated into oil and water using the oil / water separators 70a and 70b (S122), and a high-quality oil component having a low specific gravity is stored in the hydrocarbon oil tank 72. (S124). When the chlorine content of the recovered hydrocarbon oil is low, for example, 100 ppm or less, it can be used as fuel for the hot stove 34 or the like, and can also be used as spray oil for oil recovery of the oil spray tower 60. Furthermore, since the hydrocarbon oil can be refined and used for various purposes, as is the case with petroleum used in the ordinary petrochemical industry, it can be weighed and shipped to customers (S126).

  FIG. 3 is a configuration diagram illustrating an example of an oil spray tower. The oil spray tower 60 is, for example, a cylindrical body having a total length of about 5000 mm extending in the vertical direction. The tower is provided with a packing (terrarette) and injects oil as a solvent into the sealed internal space. A number of nozzles N,.

  When a large amount of chlorine component is contained in the uncondensed gas, a chlorine removal tank 61 may be provided at the lower stage of the oil spray tower 60. The chlorine removal tank 61 desalinates the recovered oil containing the hydrocarbon oil recovered by the oil sprayed by the oil spray tower 60 and supplies the recovered oil to the recovered oil tank 56 via the spray recovered oil take-out pipeline 62. send. That is, when water is also injected from the nozzles N,... Of the oil spray tower 60, hydrogen chloride as an acidic gas introduced into the tower is adsorbed and dissolved, and an acidic solution having a pH of about 1.5, That is, it becomes hydrochloric acid and flows out into the chlorine removal tank 61. Therefore, if the chlorine removal tank 61 has a function of performing neutralization using limestone or the like, the recovered oil stored in the recovered oil tank 56 does not contain hydrochloric acid, and the corrosion resistance of the oil / water separators 70a and 70b and various pipes is reduced. Is less.

  FIG. 4 shows a second embodiment of the present invention, which is a combination of a pyrolysis oil converting apparatus and a plastic waste pretreatment apparatus. The plastic waste pre-processing equipment processes plastic waste into a granular, crushed, semi-molten or melted plastic body, and at the same time removes halogen elements contained in the plastic waste in advance, and pyrolyzes it. This reduces the burden of desalting on the oil generator side.

  In the figure, the plastic waste that has been carried in is fed into the pulverizer 110 by the charging hopper 102 and the conveyor 104. The start / stop switch 106 is an on / off command for conveying the conveyor 104, but may have a function of adjusting the conveying speed. The crusher 110 crushes plastic waste to a particle size of about several mm. In order to facilitate the pulverization by the pulverizer 110, the plastic waste is preferably dried after removing moisture in advance. The pulverized plastic waste is temporarily stored in the pulverized material storage 112. At this time, for transportation from the pulverizer 110 to the pulverized material storage place 112, for example, a transporter suitable for powder transportation such as a blower may be used, or a belt conveyor may be used.

  The pulverized plastic waste is fed from the pulverized material storage area 112 into the funnel port 116 by the handler 114. For example, a robot arm is used as the handler 114, and the plastic waste of the pulverized material storage place 112 is grasped by the grip part at the tip, and the plastic waste is rotated from the pulverized material place 112 to the funnel port 116 and is grasped by the grip part. It drops to the funnel port 116 and rotates again from the funnel port 116 to the crushed material storage area 112. The funnel port 116 is provided at the entrance of the quantitative charging machine 118, and plastic waste is charged therein. The fixed amount feeder 118 conveys the plastic waste that has been input to the funnel-type supply port 132 in a predetermined amount. For conveyance, for example, a blower suitable for powder transportation may be used.

The limestone feeder 120 is used in the case of PET (polyethylene terephthalate) and nylon as plastic waste, and puts limestone (calcium carbonate: CaCO ₃ ) into the funnel port 116. Originally, polyethylene terephthalate and nylon do not contain chlorine, but when recovered as plastic waste, the fact is that other transparent plastics containing chlorine are mixed. Therefore, calcium contained in limestone is combined with chlorine gas that is separated along with the thermal decomposition of plastic waste to become calcium chloride, and the chlorine component in the pyrolysis oil converting apparatus is reduced. Calcium carbonate is theoretically composed of 56% calcium oxide (CaO) and 44% carbon dioxide (CO ₂ ), but limestone contains some impurities such as magnesium, alumina, silicic acid and iron. Yes.

  The funnel-type supply port 132 sends plastic waste or a mixture of plastic waste and limestone to the input port 134 of the volume reduction processor 130. The volume reduction processing machine 130, such as an RDF forming machine, is preferably one that solidifies the pulverized plastic waste again into a pellet, and the plastic waste is softened so that it can be easily molded as necessary. For example, it is preferable to raise the temperature to about 80 ° C. to 100 ° C., for example. The plastic waste solidified into pellets by the volume reduction processor 130 is sent to the chlorine separation tank 140 through the transport pipeline 136. The transport pipeline 136 is heated to about 200 ° C. in order to promote softening of the plastic waste solidified into pellets.

  The chlorine separation tank 140 holds the plastic waste sent from the transport pipeline 136 at the chlorine element separation temperature. The chlorine element separation temperature is, for example, 270 ° C to 300 ° C. As described above, the chlorine element separation temperature exceeds the melting point of heat-resistant plastics such as three major plastics and polyethylene terephthalate / nylon, which constitute plastic waste. Therefore, the plastic waste is in a semi-molten or molten plastic body and is sent to the inlet 20 of the pyrolysis oil converting apparatus. Note that the chlorine gas separated in the chlorine separation tank 140 is subjected to a desalting treatment of the exhaust gas separately because the air pollutants are being removed. The fluidity of the semi-molten plastic body varies depending on the amount of impurities contained in the plastic waste. For example, when a large amount of glass fiber such as FRP is contained, the fluidity is poor. On the other hand, when the majority is plastic like a plastic film, it becomes a semi-molten state very close to the molten state, and the fluidity is Remarkably high.

  The operation of the apparatus configured as described above will be described. The carried plastic waste is pulverized by the pulverizer 110 to a particle size of about several mm and sent to the volume reduction processor 130. At this time, when it is expected that chloride is mixed into the plastic waste, limestone is mixed by the limestone feeder 120. Then, the plastic waste pulverized by the volume reduction processor 130 is solidified again into a pellet and sent to the chlorine separation tank 140. In the chlorine separation tank 140, the chlorine element separation temperature is maintained, the chlorine separation treatment is performed, and the plastic body is made into a semi-molten or molten state. The semi-molten or molten plastic body is then sent from the chlorine separation tank 140 to the inlet 20 of the pyrolysis oil converting apparatus. In the pyrolysis oil converting apparatus, the point that hydrocarbon oil is recovered by pyrolysis is as described in the first embodiment.

  As a result of experiments conducted by the present inventor, 80% to 95% of the chlorine components contained in the plastic waste were removed when the chlorine separation tank 140 was retained for a sufficient time. Therefore, on the pyrolysis oil converting apparatus side, the remaining 20% to 5% may be subjected to a desalting treatment.

  FIG. 5 shows a third embodiment of the present invention, which is a combination of a desalination treatment apparatus in the latter stage of the pyrolysis oil converting apparatus. The hydrocarbon oil stored in the hydrocarbon oil tank 72 is desalted by the desalting apparatus 160. The desalinization processing device 160 causes the hydrocarbon oil stored in the hydrocarbon oil tank 72 to come into contact with an alkali metal compound in the pressure / temperature region of the halogen desorption process to desorb halogen elements contained in the hydrocarbon oil. The pressure / temperature region of the halogen desorption process is, for example, a temperature range of 200 ° C. to 300 ° C. and a pressure range of 100 atm to 200 atm. As the alkali metal compound, for example, an alkali metal hydroxide compound such as caustic soda (NaOH) is used.

  The supply of thermal energy to the desalting apparatus 160 is performed by the superheated furnace 152 and the superheated furnace burner fan 154, and for example, steam at 400 ° C. is supplied. The hydrocarbon oil stored in the hydrocarbon oil tank 72 is supplied to the desalting apparatus 160 via the pump 162. Caustic soda is stored in the chemical tank 164 and supplied to the desalting apparatus 160 via the pump 166.

  Since the hydrocarbon oil desalted by the desalination treatment device 160 is at a high temperature of 200 ° C. to 300 ° C., it is cooled to about several tens of degrees by heat exchange with the cooler 168 and sent to the tank 170. . In the oil / water separation / circulation tank 172, the hydrocarbon oil is sent to the oil / water separation processor 176 via the pump 174, and the hydrocarbon oil having a light specific gravity is returned to the oil / water separation / circulation tank 172 by centrifugal separation. Thus, since the light hydrocarbon oil as the supernatant is refined in the oil / water separation / circulation tank 172, the refined hydrocarbon oil is transferred to the refinement tank 173 and stored. The oil / water separation processor 176 separates moisture with a high specific gravity, and the separated moisture is stored in the separation water tank 178. When the purification of the hydrocarbon oil stored in the oil / water separation / circulation tank 172 is completed and transferred to the purification tank 173, the unrefined hydrocarbon oil is transferred from the tank 170. Since the refined hydrocarbon oil is stored in the refining tank 173, the hydrocarbon oil is shipped or used for internal use in the pyrolysis oil converting apparatus.

  In order to cool the hydrocarbon oil desalted by the cooler 168, the coolant stored in the water storage tank 180 is sent to the cooler 168 by the pump 182. The cooling water whose temperature has been increased by exchanging heat with the cooler 168 is cooled by the cooling tower 184 and returned to the water storage tank 180.

  Next, a case will be described in which a system in which a plastic waste pretreatment device is combined with the pyrolysis oil converting device shown in FIG. 4 is used as the pyrolysis waste treatment device. Plastic waste includes waste using a composite material of plastic such as glass fiber reinforced plastic (FRP) and heat-resistant glass fiber. Therefore, the case where the glass fiber reinforced plastic is subjected to pyrolytic waste treatment will be described using the apparatus shown in FIG. First, a fiber reinforced plastic is pulverized by a pulverizer 110 and attached to the fiber crushed by the volume reduction processor 130, and is pretreated in a granular or semi-molten state.

  The plastic body attached to the crushed fiber is conveyed in the direction of the kiln movement axis by the convex blades 18 installed inside the decomposition vessel 10. The plastic body is heated inside the decomposition vessel 10 and separated into pyrolysis gas and pyrolysis solids that have not been pyrolyzed by the kiln inner cylinder portion 16. The pyrolysis gas is effectively recovered as hydrocarbon oil by the cooling oil recovery unit 50 and the spray oil recovery unit 60. In addition, the crushed fiber is sent as a residue from the residue discharge port 26 to the residue cooling chamber 40, cooled, and discharged from the pyrolysis oil generator as a residue by the conveyor 42. Since the fiber contained in the residue is shortened and the plastic component remains only as pyrolytic solids, the fiber can be easily discarded or regenerated.

  Next, a case where a system in which a plastic waste pretreatment device is combined with the pyrolysis oil converting device shown in FIG. 4 is used as a valuable metal recovery device will be described. Plastic waste includes waste using a composite material of plastic and silver (metal) such as an X-ray photographic film. Therefore, the plastic-containing body containing valuable metals is also effectively processed using the apparatus of FIG. That is, the plastic-containing body containing the valuable metal is pretreated into a granular or semi-molten plastic body by the volume reduction processor 130. If the volume reduction processing of the plastic-containing body can be performed by the volume reduction processing machine 130, installation of the pulverizer 110 may be omitted.

  And the point by which a plastic body is collect | recovered as hydrocarbon oil is the same as that of description of a pyrolysis oil-ized apparatus. Further, the residue containing valuable metal remaining after pyrolysis is sent as a residue from the residue discharge port 26 to the residue cooling chamber 40, cooled, and discharged from the pyrolysis oil converting apparatus as a residue by the conveyor 42. Residues containing valuable metals have a markedly increased content of valuable metals compared to ordinary waste, making it easier to collect and reuse valuable metals.

  Further, the system in which the thermal decomposition oil conversion apparatus described in the second embodiment is combined with the plastic waste pretreatment apparatus is provided at the subsequent stage of the thermal decomposition oil conversion apparatus described in the third embodiment. Alternatively, the desalting apparatus 160 may be combined. If comprised in this way, since the desalination process of a plastic waste is made | formed as a pre-processing and a post-processing with respect to a pyrolysis oil conversion apparatus, it is not necessary to improve corrosion resistance as a pyrolysis oil conversion apparatus, and is collect | recovered. Since the hydrocarbon oil is refined, it becomes easy to use the hydrocarbon oil.

It is a block diagram explaining the pyrolysis oil-ized apparatus as the 1st Embodiment of this invention. It is a flowchart explaining the pyrolysis oil conversion method of this invention. It is a block diagram explaining an example of an oil-spraying tower and a circulating oil tank. The 2nd Embodiment of this invention is shown, Comprising: The pre-processing apparatus of a plastic waste is combined with the pyrolysis oil conversion apparatus. 3 shows a third embodiment of the present invention, which is a combination of a desalinization treatment apparatus in the latter stage of a pyrolysis oil conversion apparatus.

Explanation of symbols

10 Decomposition container (rotary kiln)
12 Exterior casing 14 Kiln outer cylinder part 16 Kiln inner cylinder part 18 Conveying part (convex blade)
20 Input port 22 Outlet port 50 Cooling oil recovery unit (heat exchanger)
56 Recovered oil tank 60 Oil spray tower (spray type oil recovery unit)
70a, 70b Oil-water separator 72 Hydrocarbon oil tank 110 Crusher (crushing means)
120 Alkali supply means (limestone supply machine)
130 Volume reduction processor 140 Halogen separation tank (chlorine separation tank)
160 Desalination processing equipment

Claims (9)

A transport unit installed inside the decomposition container, wherein the transport unit transports the granular, crushed, semi-molten or molten plastic body in the direction of the axis of movement of the decomposition container;
The decomposition container that heats the plastic body charged on the upstream side of the transport unit to generate pyrolysis gas inside the decomposition container and discharges the residue left by the pyrolysis on the downstream side When,
A cooling type oil recovery unit that cools the pyrolysis gas obtained in the decomposition vessel and recovers hydrocarbon oil;
A spray-type oil recovery unit that recovers hydrocarbon oil by spraying oil to the pyrolysis gas cooled in the cooling-type oil recovery unit;
A pyrolysis oil converting apparatus. Furthermore, an oil content refining unit for refining the hydrocarbon oil recovered by the cooling type oil content recovery unit and the spray type oil content recovery unit,
The pyrolysis oil converting apparatus according to claim 1, wherein the hydrocarbon oil refined by the oil refiner is used for heating the cracking vessel. In the pyrolysis oil converting apparatus according to claim 1 or 2,
Furthermore, it has a volume reduction processing machine for pre-processing the plastic-containing body to be processed in the pyrolysis oil converting apparatus into a granular or semi-molten plastic body,
A pyrolysis oil converting apparatus, wherein the plastic body pretreated by the volume reduction processor is supplied to the decomposition container. In the pyrolysis oil converting apparatus according to claim 1 or 2,
Furthermore, the volume reduction processing machine which pre-processes the plastic containing body processed with a pyrolysis oil converting apparatus into the granular or semi-molten plastic body,
A halogen separation tank for maintaining the plastic body pretreated by the volume reduction processing machine at a halogen element separation temperature;
And supplying a plastic body dehalogenated in the halogen separation tank to the decomposition vessel. In the pyrolysis oil converting apparatus according to claim 3 or 4,
Furthermore, the pyrolysis oil-ized apparatus characterized by including the calcium supply means which supplies a calcium component with respect to the plastic containing body processed by a pyrolysis oil-ized apparatus or a plastic body. In the pyrolysis oil conversion apparatus according to any one of claims 1 to 5,
Further, the hydrocarbon oil recovered at least one of the cooling type oil component recovery unit or the spray type oil component recovery unit is brought into contact with an alkali metal compound in the pressure / temperature region of the halogen desorption process, and is contained in the hydrocarbon oil. A pyrolysis oil converting apparatus comprising a desalting treatment section for releasing a halogen element. Put a granular, crushed, semi-molten or molten plastic body upstream of the transport unit installed inside the decomposition vessel;
While conveying the plastic body to the downstream side, the pyrolysis gas is generated by heating and the residue remaining on the downstream side of the conveyance unit is discharged;
Cooling the pyrolysis gas obtained in the cracking vessel to recover hydrocarbon oil;
Oil is sprayed on the cooled reformed gas to recover hydrocarbon oil;
A pyrolysis oil conversion method comprising a step. Crushing means for crushing fiber reinforced plastic;
A volume reduction processing machine for pre-treating the fiber-reinforced plastic crushed by the crushing means, which is attached to the crushed fiber, into a granular or semi-molten state,
A transport unit installed inside the decomposition container, the transport unit transporting a plastic body attached to the crushed fiber in a moving axis direction;
The plastic body introduced on the upstream side of the transport unit is heated inside the decomposition vessel to generate pyrolysis gas, and discharges the crushed fibers remaining from the pyrolysis on the downstream side. Said disassembly container,
A cooling type oil recovery unit that cools the pyrolysis gas obtained in the decomposition vessel and recovers hydrocarbon oil;
A spray-type oil recovery unit that recovers hydrocarbon oil by spraying oil to the pyrolysis gas cooled in the cooling-type oil recovery unit;
A pyrolysis waste treatment apparatus. A volume reduction processing machine for pretreating a plastic-containing body containing a valuable metal into a granular or semi-molten plastic body;
A transport unit installed inside the decomposition container, the transport unit transporting the plastic body in a moving axis direction; and
The plastic body charged on the upstream side of the transport unit is heated inside the decomposition vessel to generate a pyrolysis gas, and a residue containing valuable metals left by the pyrolysis on the downstream side The decomposition container to be discharged;
A cooling type oil recovery unit that cools the pyrolysis gas obtained in the decomposition vessel and recovers hydrocarbon oil;
A spray-type oil recovery unit that recovers hydrocarbon oil by spraying oil to the pyrolysis gas cooled in the cooling-type oil recovery unit;
And a valuable metal recovery device that recovers the valuable metal from the residue containing the valuable metal discharged in the decomposition container.

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