EP0607862A1 - Méthode d'obtention d'une huile d'hydrocarbures à partir de déchets de plastiques ou du caoutchouc et appareil utilisé pour effectuer cette méthode - Google Patents

Méthode d'obtention d'une huile d'hydrocarbures à partir de déchets de plastiques ou du caoutchouc et appareil utilisé pour effectuer cette méthode Download PDF

Info

Publication number
EP0607862A1
EP0607862A1 EP94100382A EP94100382A EP0607862A1 EP 0607862 A1 EP0607862 A1 EP 0607862A1 EP 94100382 A EP94100382 A EP 94100382A EP 94100382 A EP94100382 A EP 94100382A EP 0607862 A1 EP0607862 A1 EP 0607862A1
Authority
EP
European Patent Office
Prior art keywords
hydrocarbon oil
cracking
catalytic cracking
tank
plastic material
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP94100382A
Other languages
German (de)
English (en)
Inventor
Toshiki Ha-404 1088-1 Nakashima Takahashi
Yoshio Tanimoto
Akemi Muraoka
Tatsuto Fukushima
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mazda Motor Corp
Original Assignee
Mazda Motor Corp
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 Mazda Motor Corp filed Critical Mazda Motor Corp
Publication of EP0607862A1 publication Critical patent/EP0607862A1/fr
Withdrawn legal-status Critical Current

Links

Images

Classifications

    • 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
    • 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
    • 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
    • C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
    • C10G57/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with polymerisation

Definitions

  • the present invention relates to a method in which waste plastic material or waste rubber material is recycled so as to obtain hydrocarbon oil and an apparatus used for carrying out the method.
  • a vehicle body panel, various interior parts, tires, etc. are formed by polymer such as plastic or rubber material and ratio of plastic material or rubber material used for each motor vehicle has been raised gradually. Therefore, even if only one motor vehicle is scrapped after its service life, a considerable quantity of waste plastic material or waste rubber material is generated. Since a number of motor vehicles are scrapped every day at present, a total quantity of waste plastic material or waste rubber material is enormous.
  • the waste plastic material is subjected to thermal cracking so as to obtain thermal cracking gas and the thermal cracking gas is subjected to catalytic cracking by using proper catalyst so as to obtain catalytic cracking gas and then, the catalytic cracking gas is cooled so as to obtain hydrocarbon oil having relatively low boiling point.
  • thermal cracking of the plastic material is performed in melt phase at a temperature of 390 °C to 500 °C, while catalytic cracking of the thermal cracking gas is performed at a temperature of 200 °C to 350 °C by using zeolite as the catalyst.
  • catalyst such as zeolite used for catalytic cracking of the thermal cracking gas produced through thermal cracking of the waste plastic material or the waste rubber material is maintained at not more than a predetermined temperature lower than a temperature for thermal cracking of the waste plastic material or the waste rubber material so as to prevent heat deterioration of the catalyst. Therefore, the thermal cracking gas produced through thermal cracking of the waste plastic material or the waste rubber material is cooled by the catalyst during catalytic cracking. As a result, high-boiling hydrocarbon component (wax component) contained in the thermal cracking gas adheres to the catalyst, thereby resulting in drop of function of the catalyst.
  • wax component high-boiling hydrocarbon component
  • a method is considered in which content of the high-boiling hydrocarbon component in the thermal cracking gas is lowered by further raising temperature for thermal cracking of the waste plastic material or the waste rubber material such that amount of the high-boiling hydrocarbon component adhering to the catalyst for catalytic cracking is reduced.
  • content of low-boiling hydrocarbon component in the catalytic cracking gas which is kept in gaseous state without being converted to hydrocarbon oil even when being cooled, increases. As a result, recovery of the hydrocarbon oil drops undesirably.
  • an essential object of the present invention is to provide a method of obtaining hydrocarbon oil from waste plastic material or waste rubber material and an apparatus used for carrying out the method, in which when thermal cracking gas obtained by thermal cracking of the waste plastic material or the waste rubber material is subjected to catalytic cracking by using proper catalyst so as to obtain catalytic cracking gas and the catalytic cracking gas is cooled so as to obtain the hydrocarbon oil, not only heat deterioration of the catalyst for catalytic cracking and drop of function of the catalyst for catalytic cracking due to adherence of high-boiling hydrocarbon component thereto can be restrained effectively but recovery of the hydrocarbon oil can be raised.
  • a method of obtaining hydrocarbon oil from waste plastic material or waste rubber material comprises the steps of: subjecting the waste plastic material or the waste rubber material to thermal cracking at a temperature exceeding 450 °C so as to obtain a thermal cracking product; subjecting the thermal cracking product to catalytic cracking by using solid acid catalyst so as to obtain a catalytic cracking product; cooling the catalytic cracking product so as to obtain first hydrocarbon oil and cracking gas component; and subjecting the cracking gas component to oligomerization by using polymerization catalyst so as to obtain second hydrocarbon oil.
  • the catalytic cracking product is obtained at a temperature of 120 °C to 250 °C.
  • an apparatus for producing hydrocarbon oil comprises: a thermal cracking portion in which waste plastic material or waste rubber material is subjected to thermal cracking at a temperature exceeding 450 °C so as to obtain a thermal cracking product; a catalytic cracking portion in which the thermal cracking product is subjected to catalytic cracking by using solid acid catalyst so as to obtain a catalytic cracking product; a cooling portion in which the catalytic cracking product is cooled so as to obtain first hydrocarbon oil and cracking gas component; an oligomerization portion in which the cracking gas component is subjected to oligomerization by using polymerization catalyst so as to obtain second hydrocarbon oil; and a recovery portion for recovering the first and second hydrocarbon oils from the cooling portion and the oligomerization portion, respectively.
  • the catalytic cracking product is obtained in the catalytic cracking portion at a temperature of 120 °C to 250 °C.
  • the waste plastic material or the waste rubber material is subjected to thermal cracking at a relatively high temperature exceeding 450 °C so as to obtain the thermal cracking product and the thermal cracking product is subjected to catalytic cracking at a relatively low temperature of, for example, 120 °C to 250 °C by using the solid acid catalyst so as to obtain the catalytic cracking product. Therefore, content of the high-boiling hydrocarbon component in the thermal cracking product is lowered.
  • the solid acid catalyst for catalytic cracking is maintained at a relatively low temperature, heat deterioration of the solid acid catalyst is restrained effectively.
  • the cracking gas component which is obtained together with the first hydrocarbon oil by cooling the catalytic cracking product is oligomerized by using the polymerization catalyst so as to produce the second hydrocarbon oil. Accordingly, in addition to the first hydrocarbon oil obtained by cooling the catalytic cracking product, the second hydrocarbon oil is obtained by oligomerization of the cracking gas component, so that recovery of the hydrocarbon oil is raised greatly.
  • the apparatus K includes a hopper 12 in which recycling material 11 such as waste plastic material including polypropylene or waste rubber material is stored.
  • a screw conveyor 14 is provided in operative association with the hopper 12 so as to, by using a rotating screw 13, grind and deliver to a thermal cracking tank 15 the recycling material 11 supplied from the hopper 12.
  • the thermal cracking tank 15 is constituted by a tank body 15B having an inlet port 15A and a heater 16.
  • a discharge portion of the screw conveyor 14 is coupled with the inlet port 15A such that the recycling material 11 supplied from the inlet port 15A into the tank body 15B is heated for thermal cracking by the heater 16.
  • a temperature sensor 17 for detecting temperature of interior of the tank body 15B is provided on the tank body 15B. Temperature control of the heater 16 is performed on the basis of detection output of the temperature sensor 17 such that thermal cracking temperature in the tank body 15B is maintained at a predetermined temperature exceeding 450 °C.
  • An upper portion of the tank body 15B of the thermal cracking tank 15 is coupled with a gas inlet port 18A of a catalytic cracking tank 18 in which thermal cracking gas obtained, as thermal cracking product, in the tank body 15B is subjected to catalytic cracking.
  • the catalytic cracking tank 18 contains aluminum chloride (AlCl3.6H2O) 19 acting as solid acid catalyst and the thermal cracking gas supplied through the gas inlet port 18A from the tank body 15B is brought into contact with the aluminum chloride 19 so as to be subjected to catalytic cracking.
  • a temperature sensor 20 for detecting temperature of interior of the catalytic cracking tank 18 is provided on the catalytic cracking tank 18.
  • the catalytic cracking tank 18 is heated by a heater (not shown) undergoing temperature control on the basis of detection output of the temperature sensor 20 such that catalytic cracking temperature in the catalytic cracking tank 18 is maintained at a temperature of 120 °C to 250 °C.
  • a duct 21 is connected with a gas outlet port 18B of the catalytic cracking tank 18.
  • the duct 21 is provided with a pressure compensated flow control valve 22 and the other end of the duct 21 is connected with an inlet of a cooler 23 in which catalytic cracking gas obtained, as catalytic cracking product, in the catalytic cracking tank 18 is cooled.
  • An outlet of the cooler 23 is led to a neutralization tank 25 via a duct 24.
  • the neutralization tank 25 stores 20 % sodium hydroxide (NaOH) aqueous solution 26 acting as neutralization liquid and includes a rotary stirrer 27 for stirring the 20 % sodium hydroxide aqueous solution 26.
  • the duct 24 extending from the outlet of the cooler 23 has a distal end dipped into the 20 % sodium hydroxide aqueous solution 26 in the neutralization tank 25.
  • An intermediate portion in the neutralization tank 25 is led, through a duct 28, to a recovery tank 29 for recovering hydrocarbon oil, while an upper portion in the neutralization tank 25 is led to an oligomerization tank 31 by way of a duct 30.
  • the oligomerization tank 31 stores 100 % phosphoric acid (H3PO4) 32 acting as polymerization catalyst and includes a rotary stirrer 33 for stirring the 100 % phosphoric acid 32.
  • the oligomerization tank 31 is heated by a heater (not shown) such that temperature of interior of the oligomerization tank 31 reaches about 130 °C.
  • An intermediate portion in the oligomerization tank 32 is led, via a duct 34, to the recovery tank 29, while an upper portion in the oligomerization tank 31 is led to a blower 36 through a duct 35.
  • the blower 36 is, in turn, led to an accumulator 38 by way of a duct 37 and the accumulator 38 is further led to the heater 16 of the thermal cracking tank 15 via a duct 39.
  • the recycling material 11 stored in the hopper 12 is supplied into the tank body 15B of the thermal cracking tank 15 from the inlet port 15A of the tank body 15B by the screw conveyor 14.
  • the tank body 15B is heated by the heater 16 such that thermal cracking of the recycling material 11 takes place in the tank body 15B.
  • temperature control of the heater 16 is performed on the basis of detection output of the temperature sensor 17 such that thermal cracking temperature in the tank body 15B is maintained at a predetermined temperature exceeding 450 °C.
  • thermal cracking gas which is a thermal cracking product of the recycling material 11 is obtained in the tank body 15B.
  • the thermal cracking gas obtained in the tank body 15B is introduced into the catalytic cracking tank 18 from gas inlet port 18A of the catalytic cracking tank 18 and is brought into contact with the aluminum chloride 19 stored, as solid acid catalyst, in the catalytic cracking tank 18.
  • the thermal cracking gas from the thermal cracking tank 15 is subjected to catalytic cracking in the catalytic cracking tank 18.
  • temperature control of the heater of the catalytic cracking tank 18 is performed on the basis of detection output of the temperature sensor 20 such that catalytic cracking temperature in the catalytic cracking tank 18 is maintained at a temperature of 120 °C to 250 °C.
  • the catalytic cracking gas which is a catalytic cracking product of the thermal cracking gas from the thermal cracking tank 15 is obtained in the catalytic cracking tank 18.
  • the catalytic cracking gas obtained in the catalytic cracking tank 18 is supplied to the cooler 23 through the duct 21 provided with the pressure compensated flow control valve 22 so as to be cooled by the cooler 23.
  • the cooler 23 low-boiling hydrocarbon oil 50 based on the catalytic cracking gas and cracking gas component 51 mainly consisting of polymer having, for example, three to four carbon atoms are obtained.
  • the low-boiling hydrocarbon oil 50 and the cracking gas component 51 which are obtained in the cooler 23 are supplied, through the duct 24, to the 20 % sodium hydroxide aqueous solution 26 stored, as neutralization liquid, in the neutralization tank 25.
  • a layer of the 20 % sodium hydroxide aqueous solution 26 a layer of the low-boiling hydrocarbon oil 50 from the cooler 23 and a layer of the cracking gas component 51 from the cooler 23 are formed sequentially upwardly in this order from a bottom of the neutralization tank 25.
  • the low-boiling hydrocarbon oil 50 which forms the intermediate layer in the neutralization tank 25 as described above is supplied to the recovery tank 29 through the duct 28, while the cracking gas component 51 which forms the uppermost layer in the neutralization tank 25 is supplied, via the duct 30, to the 100 % phosphoric acid 32 stored, as polymerization catalyst, in the oligomerization tank 31. Therefore, in the oligomerization tank 31, oligomerization of the cracking gas component 51 takes place in the 100 % phosphoric acid 32 and thus, low-boiling hydrocarbon oil 52 based on the cracking gas component 51 is obtained.
  • a portion of the cracking gas component 51 remains as unreactive cracking gas component 53. Accordingly, in the oligomerization tank 31, a layer of the 100 % phosphoric acid 32, a layer of the low-boiling hydrocarbon oil 52 produced by oligomerization of the cracking gas component 51 and a layer of the unreactive cracking gas component 53 are formed sequentially upwardly in this order from a bottom of the oligomerization tank 31.
  • the low-boiling hydrocarbon oil 52 which forms the intermediate layer in the oligomerization tank 31 is supplied to the recovery tank 29 through the duct 34. Therefore, the low-boiling hydrocarbon oil 50 supplied from the neutralization tank 25 through the duct 28 and the low-boiling hydrocarbon oil 52 supplied from the oligomerization tank 31 through the duct 34 are recovered, as low-boiling hydrocarbon oil 55, by the recovery tank 29. Meanwhile, the unreactive cracking gas component 53 which forms the uppermost layer in the oligomerization tank 31 is supplied to the blower 36 via the duct 35 and then, is fed to the accumulator 38 through the duct 37 by the blower 36. The unreactive cracking gas component 53 is further supplied from the accumulator 38 to the heater 16 of the thermal cracking tank 15 through the duct 39 so as to be recycled in the heater 16.
  • the low-boiling hydrocarbon oil 55 which is produced from the recycling material 11 so as to be recovered by the recovery tank 29 as described above is discharged from the recovery tank 29 via a duct 56 and is used as, for example, fuel.
  • thermal cracking temperature for thermal cracking of the recycling material 11 is set at a predetermined temperature exceeding 450 °C and catalytic cracking temperature for catalytic cracking of the thermal cracking gas obtained by thermal cracking of the recycling material 11 is set at a temperature of 120 °C to 250 °C on the following grounds. Initially, when thermal cracking temperature for thermal cracking of the recycling material 11 is not more than 450 °C, content of high-boiling hydrocarbon component in the thermal cracking gas obtained by thermal cracking of the recycling material 11 becomes high.
  • the experimental apparatus includes annular ovens 60 and 61 through which a tubular member 62 extends.
  • a tubular member 62 extends.
  • One end of a duct 65 is coupled with one end portion of the tubular member 62 through a plug 63, while one end of a duct 66 is coupled with the other end portion of the tubular member 62 through a plug 64.
  • a mouth of a container 68 is closed by a plug 67 such that the other end of the duct 66 pierces through the plug 67 into the container 68.
  • the plug 67 is also pierced through by one end of a duct 69 and the other end of the duct 69 is inserted into a flask 71 through a plug 70.
  • the flask 71 is disposed in an oil tank 73 placed on a magnetic stirring machine 72.
  • a heater 74 is provided in the oil tank 73.
  • a stirrer 75 which is remotely driven by the magnetic stirring machine 72 is provided in the flask 72.
  • one end of a duct 76 pierces through a plug 77 into the flask 71 and the other end of the duct 76 is open.
  • hydrocarbon oil is produced from waste plastic material in the method of the present invention.
  • 50 g of polypropylene 80 is provided as waste plastic material.
  • a predetermined amount of aluminum chloride 81 is provided as solid acid catalyst.
  • a predetermined amount of 20 % sodium hydroxide aqueous solution 82 acting as neutralization liquid is put into the container 68, while a predetermined amount of 100 % phosphoric acid 83 acting as polymerization catalyst is put into the flask 71.
  • the flask 71 is heated by the heater 74 provided in the oil tank 73 such that interior of the flask 71 is maintained at about 130 °C. Meanwhile, the stirrer 75 in the 100 % phosphoric acid 83 in the flask 71 is remotely driven by the magnetic stirring machine 72. In addition, while nitrogen (N2) gas is being blown into the tubular member 62 through the duct 65, not only temperature in the annular oven 60 is set at 500 °C but temperature in the annular oven 61 is set at 250 °C.
  • N2 nitrogen
  • hydrocarbon oil is produced from waste plastic material in another method other than the method of the present invention.
  • 50 g of polypropylene 80 is provided as waste plastic material and at a location in the tubular member 62, which confronts inside of the annular oven 61, a predetermined amount of aluminum chloride 81 is provided as solid acid catalyst.
  • a predetermined amount of 20 % sodium hydroxide aqueous solution 82 acting as neutralization liquid is put into the container 68.
  • the flask 71, the oil tank 73 and the magnetic stirring machine 72 are eliminated from the experimental apparatus. While nitrogen gas is being blown into the tubular member 62 through the duct 65, not only temperature in the annular oven 60 is set at 500 °C but temperature in the annular over 61 is set at 250 °C.
  • the waste plastic material or the waste rubber material is subjected to thermal cracking at a relatively high temperature exceeding 450 °C and the thermal cracking product obtained by this thermal cracking is subjected to catalytic cracking at a relatively low temperature of, for example, 120 °C to 250 °C by using the solid acid catalyst. Therefore, content of the high-boiling hydrocarbon component in the thermal cracking product is lowered.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)
EP94100382A 1993-01-22 1994-01-12 Méthode d'obtention d'une huile d'hydrocarbures à partir de déchets de plastiques ou du caoutchouc et appareil utilisé pour effectuer cette méthode Withdrawn EP0607862A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP9238/93 1993-01-22
JP5009238A JPH06220461A (ja) 1993-01-22 1993-01-22 廃プラスチック又はゴム材から炭化水素油を得る方法及びその実施に使用される装置

Publications (1)

Publication Number Publication Date
EP0607862A1 true EP0607862A1 (fr) 1994-07-27

Family

ID=11714827

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94100382A Withdrawn EP0607862A1 (fr) 1993-01-22 1994-01-12 Méthode d'obtention d'une huile d'hydrocarbures à partir de déchets de plastiques ou du caoutchouc et appareil utilisé pour effectuer cette méthode

Country Status (2)

Country Link
EP (1) EP0607862A1 (fr)
JP (1) JPH06220461A (fr)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999009116A1 (fr) * 1997-08-13 1999-02-25 Li Xing Procede de production d'huile hydrocarbonee a partir de matieres organiques ou de matieres de rebut de masse moleculaire elevee et appareillage correspondant
WO2000018852A1 (fr) * 1998-09-24 2000-04-06 Zhou, Dingli Procede et appareil de production d'hydrocarbures a partir de dechets urbains et/ou de dechets organiques
WO2000064997A1 (fr) * 1999-04-23 2000-11-02 Jiang Tianfu Procede et installation pour convertir des dechets de matieres plastiques en hydrocarbures combustibles
WO2001005908A1 (fr) * 1999-07-16 2001-01-25 Enercon Technologies, Inc. Procede d'obtention d'essence et de diesel a partir de dechets plastiques et/ou de petrole lourd
EP1122294A2 (fr) * 2000-02-02 2001-08-08 Shuzo Matsumura Procédé et appareillage pour la pyrolyse de gas hydrocarboné
CN1074447C (zh) * 1999-06-08 2001-11-07 周鼎力 用废塑料和或重油生产汽油柴油的方法和设备
WO2003010258A1 (fr) * 2001-07-23 2003-02-06 Yuanmo Zhang Procede et appareil de production d'essence et de gazole a partir de dechets plastiques et/ou de petrole lourd
FR2845391A1 (fr) * 2002-10-07 2004-04-09 Inst Francais Du Petrole Procede et installation de production d'un gaz de synthese depollue a partir d'une charge riche en matiere organique
US6774271B2 (en) * 2001-01-22 2004-08-10 Tianfu Jiang Method and system of converting waste plastics into hydrocarbon oil
CN102205341A (zh) * 2011-01-30 2011-10-05 福州索源智能装备技术开发有限公司 智能化固体有机废弃物微波裂解系统及其生产工艺
CN101812314B (zh) * 2009-02-20 2013-06-19 上海金匙环保科技股份有限公司 一种弃废轮胎高值利用的低温催裂解方法
EP2443216A4 (fr) * 2009-06-19 2015-12-16 Innovative Energy Solutions Inc Craquage thermo-catalytique pour la conversion d'hydrocarbures supérieurs en hydrocarbures inférieurs
WO2022067251A1 (fr) * 2020-09-28 2022-03-31 Chevron Phillips Chemical Company Lp Produits chimiques ou polymères circulaires à partir de déchets plastiques pyrolysés et utilisation de bilan massique pour permettre de créditer les produits résultants sous forme circulaire

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20010087776A (ko) * 2001-04-18 2001-09-26 김전열 촉매에 의한 증류유화기술
CN104371750B (zh) * 2013-08-12 2017-03-08 上海金匙环保科技股份有限公司 热解反应装置及其系统与方法
CN108239552B (zh) * 2018-02-11 2019-09-17 北京石油化工学院 一种处理废塑料和纤维素的方法
CN108251146B (zh) * 2018-02-11 2019-09-17 北京石油化工学院 一种废塑料和纤维素共处理的方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2357630A1 (fr) * 1976-07-05 1978-02-03 Erap Procede perfectionne de craquage catalytique
US4851601A (en) * 1988-01-19 1989-07-25 Mobil Oil Corporation Processing for producing hydrocarbon oils from plastic waste
EP0392590A1 (fr) * 1989-04-11 1990-10-17 Shell Internationale Researchmaatschappij B.V. Procédé de conversion d'une charge hydrocarbonée

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2357630A1 (fr) * 1976-07-05 1978-02-03 Erap Procede perfectionne de craquage catalytique
US4851601A (en) * 1988-01-19 1989-07-25 Mobil Oil Corporation Processing for producing hydrocarbon oils from plastic waste
EP0392590A1 (fr) * 1989-04-11 1990-10-17 Shell Internationale Researchmaatschappij B.V. Procédé de conversion d'une charge hydrocarbonée

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999009116A1 (fr) * 1997-08-13 1999-02-25 Li Xing Procede de production d'huile hydrocarbonee a partir de matieres organiques ou de matieres de rebut de masse moleculaire elevee et appareillage correspondant
WO2000018852A1 (fr) * 1998-09-24 2000-04-06 Zhou, Dingli Procede et appareil de production d'hydrocarbures a partir de dechets urbains et/ou de dechets organiques
AU760143B2 (en) * 1998-09-24 2003-05-08 Dingli Zhou Process and apparatus for producing hydrocarbons from city garbage and/or organic waste material
WO2000064997A1 (fr) * 1999-04-23 2000-11-02 Jiang Tianfu Procede et installation pour convertir des dechets de matieres plastiques en hydrocarbures combustibles
CN1074447C (zh) * 1999-06-08 2001-11-07 周鼎力 用废塑料和或重油生产汽油柴油的方法和设备
WO2001005908A1 (fr) * 1999-07-16 2001-01-25 Enercon Technologies, Inc. Procede d'obtention d'essence et de diesel a partir de dechets plastiques et/ou de petrole lourd
EP1228165A1 (fr) * 1999-07-16 2002-08-07 Xing, Li Procede d'obtention d'essence et de diesel a partir de dechets plastiques et/ou de petrole lourd
EP1228165A4 (fr) * 1999-07-16 2004-01-28 Xing Li Procede d'obtention d'essence et de diesel a partir de dechets plastiques et/ou de petrole lourd
EP1122294A2 (fr) * 2000-02-02 2001-08-08 Shuzo Matsumura Procédé et appareillage pour la pyrolyse de gas hydrocarboné
EP1122294A3 (fr) * 2000-02-02 2002-03-06 Shuzo Matsumura Procédé et appareillage pour la pyrolyse de gas hydrocarboné
US6921517B2 (en) 2000-02-02 2005-07-26 Shuzo Matsumura Process and apparatus for the pyrolysis of hydrocarbon gas
US6774271B2 (en) * 2001-01-22 2004-08-10 Tianfu Jiang Method and system of converting waste plastics into hydrocarbon oil
WO2003010258A1 (fr) * 2001-07-23 2003-02-06 Yuanmo Zhang Procede et appareil de production d'essence et de gazole a partir de dechets plastiques et/ou de petrole lourd
FR2845391A1 (fr) * 2002-10-07 2004-04-09 Inst Francais Du Petrole Procede et installation de production d'un gaz de synthese depollue a partir d'une charge riche en matiere organique
CN101812314B (zh) * 2009-02-20 2013-06-19 上海金匙环保科技股份有限公司 一种弃废轮胎高值利用的低温催裂解方法
EP2443216A4 (fr) * 2009-06-19 2015-12-16 Innovative Energy Solutions Inc Craquage thermo-catalytique pour la conversion d'hydrocarbures supérieurs en hydrocarbures inférieurs
US9480963B2 (en) 2009-06-19 2016-11-01 Innovative Energy Solutions, Inc. Thermo-catalytic cracking for conversion of higher hydrocarbons into lower hydrocarbons
CN102205341A (zh) * 2011-01-30 2011-10-05 福州索源智能装备技术开发有限公司 智能化固体有机废弃物微波裂解系统及其生产工艺
WO2022067251A1 (fr) * 2020-09-28 2022-03-31 Chevron Phillips Chemical Company Lp Produits chimiques ou polymères circulaires à partir de déchets plastiques pyrolysés et utilisation de bilan massique pour permettre de créditer les produits résultants sous forme circulaire
US11479726B2 (en) 2020-09-28 2022-10-25 Chevron Phillips Chemical Company, Lp Circular chemicals or polymers from pyrolyzed plastic waste and the use of mass balance accounting to allow for crediting the resultant products as circular
US11518942B2 (en) 2020-09-28 2022-12-06 Chevron Phillips Chemical Company Lp Circular chemicals or polymers from pyrolyzed plastic waste and the use of mass balance accounting to allow for crediting the resultant products as circular
US11746297B2 (en) 2020-09-28 2023-09-05 Chevron Phillips Chemical Company Lp Circular chemicals or polymers from pyrolyzed plastic waste and the use of mass balance accounting to allow for crediting the resultant products as circular
US11781073B2 (en) 2020-09-28 2023-10-10 Chevron Phillips Chemical Company Lp Circular chemicals or polymers from pyrolyzed plastic waste and the use of mass balance accounting to allow for crediting the resultant products as circular
US12077713B2 (en) 2020-09-28 2024-09-03 Chevron Phillips Chemical Company Lp Circular chemicals or polymers from pyrolyzed plastic waste and the use of mass balance accounting to allow for crediting the resultant products as circular

Also Published As

Publication number Publication date
JPH06220461A (ja) 1994-08-09

Similar Documents

Publication Publication Date Title
EP0607862A1 (fr) Méthode d'obtention d'une huile d'hydrocarbures à partir de déchets de plastiques ou du caoutchouc et appareil utilisé pour effectuer cette méthode
US5414169A (en) Method of obtaining hydrocarbon oil from waste plastic material or waste rubber material and apparatus for carrying out the method
US4820463A (en) Process of degassing and pelletizing polyolefins
US4584421A (en) Method for thermal decomposition of plastic scraps and apparatus for disposal of plastic scraps
JP5016750B2 (ja) 熱分解反応器中での熱分解による重合体、好ましくは廃棄タイヤ形態の重合体からのカーボンおよび炭化水素混合物の回収方法
WO2012076890A1 (fr) Procédé de recyclage des matières plastiques
US20120165583A1 (en) Modified Zeolites and their Use in the Recycling of Plactics Waste
US7824523B2 (en) Catalytically activated vacuum distillation system
KR20180128951A (ko) 석유 제품들을 생산하기 위한 프로세스, 장치, 제어기, 및 시스템
EP3491052B1 (fr) Appareil et procédé de défabrication thermique de pneus et d'autres déchets
JPH11514020A (ja) ゴム脱硫方法
US6881303B2 (en) Method and system for pyrolyzing plastic and pyrolysate product
CN212199124U (zh) 废旧橡胶裂解及回收设备
US6046370A (en) Process for the treatment of used rubber and plastics
EP1618140B1 (fr) Reduction de caoutchouc
US20020070104A1 (en) Tandem batch feed and tandem batch collection apparatus for continuous pyrolysis of rubber and/or other hydrocarbon-based material
CA1045750A (fr) Methode de recuperation de dechets du caoutchouc cuit
US3457248A (en) Polyolefin recovery from solution by flashing and chopping
US3461109A (en) Process for the polymerization of conjugated dienes
US3544540A (en) Temperature control system
JPH06228568A (ja) 廃プラスチック又はゴム材から炭化水素油を得る方法及びその実施に使用される装置
US4188367A (en) Manufacture of red phosphorus
JPH06220460A (ja) 廃プラスチック又はゴム材から炭化水素油を得る方法及びその実施に使用される装置
US8664284B2 (en) Depolymerization of polymers
US2735828A (en) Recovery of carbon black

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DE FR GB

17P Request for examination filed

Effective date: 19950103

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 19960731