WO2008004357A1 - Équipement permettant de convertir du plastique en huile - Google Patents

Équipement permettant de convertir du plastique en huile Download PDF

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Publication number
WO2008004357A1
WO2008004357A1 PCT/JP2007/054062 JP2007054062W WO2008004357A1 WO 2008004357 A1 WO2008004357 A1 WO 2008004357A1 JP 2007054062 W JP2007054062 W JP 2007054062W WO 2008004357 A1 WO2008004357 A1 WO 2008004357A1
Authority
WO
WIPO (PCT)
Prior art keywords
water vapor
oil
plastic
reaction tank
steam
Prior art date
Application number
PCT/JP2007/054062
Other languages
English (en)
Japanese (ja)
Inventor
Kazuki Kanbara
Atsuo Fukushima
Original Assignee
Orient Instrument Computer Co., Ltd.
Kazuki Industry Ltd.
Nihonseisui Engineering Co.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Orient Instrument Computer Co., Ltd., Kazuki Industry Ltd., Nihonseisui Engineering Co. filed Critical Orient Instrument Computer Co., Ltd.
Publication of WO2008004357A1 publication Critical patent/WO2008004357A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/14—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by treatment with steam or water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B51/00—Destructive distillation of solid carbonaceous materials by combined direct and indirect heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/62—Plastics recycling; Rubber recycling

Definitions

  • the present invention relates to a plastic oil making apparatus that directly decomposes plastic with superheated steam to generate oil.
  • Patent Document 1 discloses a water vapor or inert gas supply path, a waste plastic supply path, a horizontal pyrolysis furnace, a pyrolysis residue outlet, and a cooling device for converting pyrolysis gas into oil. It is characterized by comprising a combustion device that burns the pyrolysis gas and a heat recovery device that is heated by the combustion and introduces a gas or liquid into a jacket provided in the pyrolysis furnace.
  • a waste plastic thermal decomposition apparatus is disclosed.
  • Patent Document 1 Japanese Patent Laid-Open No. 6-298994
  • the present invention has been made in view of the above-mentioned problems existing in the prior art, and the object of the present invention is that the reaction with superheated steam is performed under normal pressure without using a catalyst.
  • One aspect of the present invention for achieving the above object includes a reaction vessel for decomposing plastic, a heating chamber in which the reaction vessel is provided, a heating device, water vapor, A plastic oil making apparatus having a discharge part for discharging the decomposition product of plastic into the reaction tank,
  • the reaction tank has a water vapor introduction layer that covers at least a part of the reaction tank on the outside in the heating chamber
  • the plastic oil converting apparatus includes an introduction unit that introduces water vapor into the water vapor introduction layer, and the water vapor
  • the apparatus further comprises a water vapor jet nozzle for ejecting water vapor from the introduction layer into the reaction tank, and the heating device superheats the water vapor introduced into the water vapor introduction layer, and the superheated water vapor is By ejecting from the introduction layer into the reaction tank through the water vapor ejection nozzle, the plastic is decomposed in the vapor phase in the reaction tank, and the oil produced by the decomposition is introduced into the reaction tank through the water vapor ejection nozzle.
  • a plastic oil making apparatus characterized in that it is discharged to the outside of the reaction tank through the discharge part together with the jetted water vapor.
  • the target plastic is charged into the reaction tank, water vapor is introduced into the water vapor introducing layer from the water vapor supply source, and the heating device is used.
  • the water vapor introduced into the water vapor introduction layer in the heating chamber is heated and the reaction vessel is heated.
  • the water vapor introduced into the water vapor introduction layer is supplied to the water vapor introduction layer! It is overheated and ejected into the reaction tank through the water vapor ejection nozzle.
  • the plastic reacts with the superheated steam that is superheated in the steam introduction layer and jets into the reaction tank through the steam jet nozzle, and does not require the use of a catalyst at normal pressure.
  • the oil produced by the decomposition is transported by water vapor ejected into the reaction tank via the water vapor ejection nozzle, and discharged to the outside of the reaction tank via the discharge part, so that it can be safely taken out.
  • a plurality of the water vapor ejection nozzles are provided.
  • a plurality of steam jet nozzles are provided, so that a plurality of force heated steams can be brought into contact with the plastic in the reaction tank. Therefore, superheated steam and plastic react efficiently in the reaction tank, and the plastic decomposes efficiently in the steam gas phase.
  • a part or all of the inside of the reaction vessel is a plastic container, and the plastic thereof.
  • the plurality of steam jet nozzles are arranged so that superheated steam is sprayed evenly to the storage chamber.
  • the water vapor introduced into the water vapor introduction layer is superheated by the water vapor introduction layer V, and is uniformly overheated to the plastic container in the reaction tank via a plurality of water vapor ejection nozzles. Water vapor spouts out. Therefore, the superheated steam and the plastic react efficiently in the plastic container in the reaction tank, and the plastic is efficiently decomposed in the steam gas phase.
  • the weight of water vapor can be made 10 times or less the weight of the oil.
  • the apparatus further includes an inclined plate separation device into which oil discharged to the outside of the reaction tank together with water vapor is introduced, and moisture and oil are separated in the inclined plate separation device.
  • the apparatus further includes an inclined plate separation device into which oil discharged to the outside of the reaction tank together with water vapor is introduced.
  • the inclined plate separating apparatus moisture and oil are separated.
  • an upper end plate portion and a lower end plate portion in the vertical direction are respectively provided at the upper end and the lower end of the inclined plate included in the inclined plate separating apparatus.
  • the oil-containing water is rectified by the upper end plate portion and the lower end plate portion provided in the vertical direction at the upper end and the lower end of the inclined plate, respectively, and the flow of the oil-containing water is biased in the inclined plate. This prevents the oil / water separation efficiency from being lowered.
  • a dechlorination device is provided between the discharge portion and the inclined plate separator.
  • the dechlorination device is interposed between the discharge part and the inclined plate separation device, the inclined plate is removed after being dechlorinated by the dechlorination device even when the plastic containing chlorine is liquefied. Water and oil are separated in the separation device. As a result, generation of chlorine-containing harmful substances such as hydrogen chloride is prevented.
  • the plastic reacts with the superheated steam that is superheated in the steam introduction layer and jetted into the reaction tank through the steam jet nozzle, so that it is not necessary to use a catalyst under normal pressure.
  • the plastic decomposes efficiently in the vapor phase of steam.
  • the generated oil is transported by the steam ejected into the reaction tank through the steam ejection nozzle and discharged outside the reaction tank through the discharge section, so that it can be safely taken out.
  • FIG. 1 is a schematic cross-sectional view of a main part showing a front part of a plastic oil making apparatus according to an embodiment of the present invention.
  • FIG. 2 is a schematic cross-sectional view of a main part showing a rear part of the plastic oil making apparatus according to the embodiment of the present invention.
  • FIG. 3 is a flow diagram including a dechlorination apparatus.
  • the plastic oil making apparatus 1 is mainly composed of a pre-stage portion mainly composed of a reaction vessel 10 and a heating chamber 12, and an inclined plate separating device 28. When It consists of the latter part.
  • the plastic oil making apparatus 1 includes a reaction vessel 10 having a rectangular parallelepiped shape (not limited to this shape) for decomposing plastic, and the reaction vessel 10 provided therein.
  • a heated heating chamber 12 is provided.
  • target plastics include PET, polyethylene, polyacrylamide, and salt gel. It is pretty easy to process two or more types at once.
  • the upper part of the reaction tank 10 faces the outside of the heating chamber 12, and the side surface and the bottom surface of the reaction tank 10 are located in the heating chamber 12.
  • the lower part of the reaction vessel 10 is supported against the bottom of the heating chamber 12.
  • the heating chamber 12 is covered with a heat insulating wall 14.
  • the reaction vessel 10 has a water vapor introduction jacket 16 (water vapor introduction layer) that covers a pair of side and bottom portions facing each other.
  • a steam introduction section 20 for introducing steam from an external boiler 18 (which is an example of a steam supply source, but is not limited to this) for supplying steam into the reaction vessel 10.
  • An external boiler 18 which is an example of a steam supply source, but is not limited to this
  • a portion of the reaction vessel 10 excluding the upper end is a plastic container 11.
  • a number of steam ejection nozzles 22 are provided so that superheated steam is evenly ejected from the inner wall force of the steam introduction jacket 16 to the plastic container 11 in the reaction tank 10. Yes.
  • the steam introduction jacket 16 can cover the entire outer surface and bottom surface of the reaction vessel 10 in the heating chamber 12 or can cover a part thereof.
  • an openable / closable inlet 24 for introducing the target plastic P such as waste plastic into the reaction tank 10, water vapor and plastic decomposition products (liquid, solid, (Or a gaseous substance) is provided with a discharge hole 26 (discharge section) for discharging from the reaction vessel 10.
  • a discharge pipe 30 is connected between the discharge hole 26 and the introduction portion of the inclined plate separator 28.
  • the plastic decomposition process by the plastic oil converting apparatus 1 can be a continuous process or an intermittent process in addition to a batch process. In the case of continuous or intermittent treatment, it is desirable to shield the air with water vapor in order to exclude air from entering the reaction tank 10 when the target plastic P is charged into the reaction tank U.
  • a panner 32 (heating device) is provided at one end of the heating chamber 12. Pana 32 is heated The water vapor introduced into the water vapor introduction jacket 16 in the chamber 12 is heated and the reaction tank 10 is heated. Heating to the reaction vessel 10 can be performed directly or indirectly through a steam introduction jacket 16.
  • the temperature of superheated steam is, for example, about 200 ° C-500 ° C for PET bottles. It is preferable to use about 2 to 5 times the weight of the plastic to be decomposed as superheated steam.
  • One or more pruners can be installed.
  • the temperature of the superheated steam sprayed into the reaction tank 10 is always controlled within a fluctuation range within 10% of the set temperature, for example.
  • the quality of the product oil can be suitably maintained.
  • Such temperature control of the superheated steam can be performed, for example, by providing a temperature sensor in the reaction tank 10 and controlling the combustion of the paran 32 by an appropriate method based on the detected temperature.
  • the target plastic P When plastic is processed in the plastic oil converting apparatus 1, the target plastic P is charged into the reaction vessel 10, steam is introduced from the boiler 18 into the steam introduction jacket 16, and the burner 32 is used. The steam introduced into the steam introduction jacket 16 in the heating chamber 12 is heated and the reaction vessel 10 is heated. Then, the water vapor introduced into the water vapor introduction jacket 16 is overheated in the water vapor introduction jacket 16 and is uniformly ejected to the plastic container 11 in the reaction tank 10 through the many water vapor ejection nozzles 22. In the reaction vessel 10 heated by the PANA 3 2, the target plastic P reacts efficiently with the superheated steam jetted into the reaction vessel 10, and efficiently decomposes in the vapor gas phase under normal pressure without the need for a catalyst. Is done.
  • the oil produced by the decomposition is transported in a state of floating in the steam or in another state by the water vapor jetted into the reaction tank 10 through the water vapor jet nozzle 22, and is sent through the discharge hole 26 to the reaction tank 10 Since it is discharged to the outside, it can be safely removed. If cracked gases and other substances are generated by the decomposition of the plastic, they can also be discharged from the discharge holes 26.
  • the water vapor and the oil in the water vapor can be discharged and transported by the pressure of water vapor jetted into the reaction tank 10 or by providing a suction fan or the like in addition to the pressure of water vapor.
  • the weight of water vapor is preferably 10 times or less the weight of oil.
  • the plastic oil making apparatus 1 of the present embodiment is provided with a dechlorination apparatus.
  • Fig. 3 is a flow diagram including the dechlorination unit. As shown in FIG. 3, in this embodiment, a dechlorination device 34 is provided between the discharge hole 26 of the reaction tank 10 and the inclined plate separation device 28.
  • the temperature of the mixture of water vapor and cracked product oil supplied to the dechlorination unit 34 is preferably 100 ° C-250 ° C.
  • a heat exchange device can be provided between the reaction vessel 10 and the dechlorination device 34 as necessary.
  • the residence time of the mixture of water vapor and cracked product oil in the dechlorination unit 34 is preferably about 0.5 seconds to 180 seconds.
  • the inclined plate separating device 28 shown in FIG. 2 is divided into two sections that are adjacent in the horizontal direction except for the lower part.
  • an oil / water receiver 38 in which the downward tip of the discharge pipe 30 is located.
  • the second section 40 is formed with a separating portion 44 in which a large number of inclined plates 42 are provided in parallel over the entire horizontal direction from the lower portion to the middle portion.
  • an upper end plate portion 46 and a lower end plate portion 48 in the vertical direction are provided, respectively.
  • a separation water outlet 50 is provided in a side wall portion below the separation portion 44 in the second section 40. Further, a separation oil outlet 54 is provided on the side wall portion of the second section where the separation oil layer 52 is formed above the separation portion 44.
  • the oil that is transported by water vapor and discharged to the outside of the reaction tank 10 through the discharge hole 26 is removed by the discharge pipe 30 through the dechlorination apparatus 3 4 (Fig. After passing through 3), it is introduced into the inclined plate separator 28, where water and oil are separated.
  • the oil-containing water is rectified by the upper end plate portion 46 and the lower end plate portion 48 provided in the vertical direction at the upper end and the lower end of the inclined plate 42, respectively. Therefore, the flow of the oil-containing water is biased at the inclined plate 42mm. This prevents the oil / water separation efficiency from being lowered.
  • the upper end plate portion 46 and the lower end plate portion 48 are provided on the inclined plate 42, but the upper end plate portion and the lower end plate portion may be omitted.
  • the residence time of the liquid cracked product oil and water in the inclined plate separator 28 can be 20 minutes to 480 minutes. Preferably 40 minutes-180 minutes.
  • the inclined plate separator 28 may be provided with a drain fan, a suction fan for introducing a mixture of water vapor and oil, and the like.
  • the dechlorination device 34 is provided between the discharge hole 26 of the reaction tank 10 and the inclined plate separation device 28, but the dechlorination device 34 is not provided.
  • the discharge hole 26 and the inclined plate separating device 28 can be directly connected to each other.
  • Recycled oil (pyrolytic oil) Unit Measurement method Kinematic viscosity (40 ° C) 2.268 mm 2 / s JIS K 2283 Kinematic viscosity (30 ° C) 2.777 mm 2 / s JIS K 2283 Pour point -7.5 ° C JIS K 2269 Flammability Point (PM method) 34.0.
  • C JIS K 2265 Residual carbon content 0.16 mass% JIS K 2270 Moisture (KP vaporization method) 0.07 mass% JIS K 2275 Ash 0.001 mass% JIS K 2272
  • Total calorific value (actual measurement) 41.93 MJ / kg JIS K 2279 Inorganic chlorine content ⁇ 7r 3 ⁇ 4 Mass ppm Silver nitrate measurement method

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Sustainable Development (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)

Abstract

La présente invention concerne un équipement permettant de convertir du plastique en huile, dans lequel le plastique peut subir un craquage efficace afin d'obtenir de l'huile grâce à une réaction à base de vapeur surchauffée, dans des conditions de pression normales et sans catalyseur, et qui permet de retirer l'huile obtenue en toute sécurité et de séparer efficacement l'huile extraite de l'eau. L'équipement comprend une chambre de chauffage (12), une cuve à réaction (10) installée dans la chambre (12), une chemise de vapeur (16) couvrant l'extérieur de la cuve (10) et de nombreuses buses de pulvérisation de vapeur (22) destinées à pulvériser de la vapeur dans la cuve (10) à partir de la chemise (16). La vapeur introduite dans la chemise (16) est surchauffée, puis pulvérisée dans la cuve (10) par les buses de pulvérisation de vapeur (22). Le plastique présent dans la cuve (10) subit ensuite un craquage en phase vapeur afin de produire de l'huile. Pour finir, l'huile et la vapeur pulvérisée dans la cuve (20) par les buses (22) sont évacuées de la cuve (10) par un orifice de sortie (26).
PCT/JP2007/054062 2006-07-03 2007-03-02 Équipement permettant de convertir du plastique en huile WO2008004357A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2006183653A JP2009221236A (ja) 2006-07-03 2006-07-03 プラスチック油化装置
JP2006-183653 2006-07-03

Publications (1)

Publication Number Publication Date
WO2008004357A1 true WO2008004357A1 (fr) 2008-01-10

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Application Number Title Priority Date Filing Date
PCT/JP2007/054062 WO2008004357A1 (fr) 2006-07-03 2007-03-02 Équipement permettant de convertir du plastique en huile

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JP (1) JP2009221236A (fr)
WO (1) WO2008004357A1 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP6022745B2 (ja) * 2010-03-23 2016-11-09 太平洋セメント株式会社 廃棄物の処理方法
JP5737623B2 (ja) * 2011-07-27 2015-06-17 住友大阪セメント株式会社 廃プラスチックの油化方法
KR102354474B1 (ko) * 2021-02-17 2022-01-20 김동관 폐기물 유화장치
KR20240037190A (ko) 2021-07-16 2024-03-21 가즈키 감바라 플라스틱 유화장치 및 방법

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH06298994A (ja) * 1993-04-12 1994-10-25 Sanwa Kako Co Ltd 廃プラスチックの熱分解装置
JP3042771U (ja) * 1997-04-22 1997-10-31 レイボルド株式会社 含油水の油水分離装置
JP2004359897A (ja) * 2003-06-06 2004-12-24 Kazuki Kogyo:Kk プラスチック廃棄物の処理方法及び処理装置

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH06298994A (ja) * 1993-04-12 1994-10-25 Sanwa Kako Co Ltd 廃プラスチックの熱分解装置
JP3042771U (ja) * 1997-04-22 1997-10-31 レイボルド株式会社 含油水の油水分離装置
JP2004359897A (ja) * 2003-06-06 2004-12-24 Kazuki Kogyo:Kk プラスチック廃棄物の処理方法及び処理装置

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