AU5801500A - A process for producing gasoline and diesel from waste plastics and/or heavy oil - Google Patents
A process for producing gasoline and diesel from waste plastics and/or heavy oil Download PDFInfo
- Publication number
- AU5801500A AU5801500A AU58015/00A AU5801500A AU5801500A AU 5801500 A AU5801500 A AU 5801500A AU 58015/00 A AU58015/00 A AU 58015/00A AU 5801500 A AU5801500 A AU 5801500A AU 5801500 A AU5801500 A AU 5801500A
- Authority
- AU
- Australia
- Prior art keywords
- catalyst
- heavy oil
- reaction
- reactor
- diesel
- 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.)
- Abandoned
Links
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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
-
- 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
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- 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
- C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
-
- 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
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)
- Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
- Catalysts (AREA)
- Liquid Carbonaceous Fuels (AREA)
Description
WO 01/05908 PCT/CNOO/00196 A PROCESS FOR PRODUCING GASOLINE AND DIESEL FROM WASTE PLASTICS AND/OR HEAVY OIL Field of the Invention 5 The present invention relates to a process for producing low-boiling point hydrocarbons from waste plastics and/or heavy oil, and more particularly to a process for producing gasoline and diesel through pyrolysis and catalytic cracking of waste plastics and/or heavy oil. 10 Background of the Invention Many methods for preparing low-boiling hydrocarbons from waste plastics and high-boiling hydrocarbons are known. U.S. Patent No. 4,851,601 and EP-A-0607862 (Applicant: MAZDA MOTOR CORPORATION) disclose a reaction of pyrolysis in a reactor kettle is (vertical or horizontal), wherein the outside wall of the kettle is heated at a high temperature while the materials therein are heated indirectly. In this method, the outside wall is apt to be deformed when the reactor is heated directly at a high temperature. The materials are readily sintered on the inside wall because of local over-heating so that the 20 conversion yield of the reaction and the life of the reactor are greatly decreased. In addition, the coefficient of the reactor's heat transfer is relatively low, it is difficult to drain the reaction residues, and the WO 01/05908 PCT/CNO0/00196 catalytic reaction in the fixed bed needs a separate heat supply. These are the common drawbacks of the reactor kettle in the prior art. A spiral reactor utilized in some special fields is similar to the above. Heat is indirectly transferred when it works. The outside wall of the 5 reactor is heated directly at a very high temperature, making the materials in the reactor indirectly heated. Therefore, the heat transfer coefficient is not satisfactory. Particularly, because the screw therein is apt to be deformed at a high temperature, making it hard to seal the two ends of the screw so that gas generated in the reaction may be exhausted. 10 Summary of the Invention Accordingly, an object of the invention is to provide a process for producing gasoline and diesel from waste plastics and/or heavy oil (including high-boiling hydrocarbons) to overcome the shortcomings in 15 the prior art as described above. The process of the present invention comprises the steps of: (a) mixing waste plastics and/or heavy oil with a first catalyst at a high temperature in a pyrolysis reactor to carry out a reaction of pyrolysis and first catalytic cracking simultaneously; and 20 (b) introducing the products in step (a) into a fixed bed to perform a reaction of second catalytic cracking. 2 WO 01/05908 PCT/CNOO/00196 Said first catalyst is made as follows: powder A1 2 0 3 is mixed with water glass to obtain a slurry, and the resultant slurry is then mixed with catalyst HZSM-5. The resultant mixture is dried, formed, granulated, and heated to obtain the first catalyst. 5 The ratio between powder A1 2 0 3 and water glass is 1:3-5 by weight and that between the slurry and HZSM-5 is 1:0.2-0.5 by weight. According to the process of the invention, the materials can be converted to gasoline and diesel with a high yield, and the requirements for the reactor are not strictly defined because the first catalyst is used to 10 heat the materials directly. Brief Description of the Drawing Figure 1 is an operational flow chart of the process in the invention. 15 Detailed Description of the Invention The process of the present invention comprises the steps of: (a) mixing waste plastics and/or heavy oil with a first catalyst at a high temperature in a pyrolysis reactor to carry out a reaction of pyrolysis and first catalytic cracking simultaneously; and 20 (b) introducing the products in step (a) into a fixed bed to perform a reaction of second catalytic cracking. The process of the invention further comprises a step of: 3 WO 01/05908 PCT/CNOO/00196 (c) recycling the first catalyst in the reaction. The reaction of pyrolysis and first catalytic cracking may be conducted under the standard atmosphere or higher, and the temperature of the first catalyst may be controlled at 500-1,000'C, preferably 600 5 700'C. The reaction of second catalytic cracking is carried out with a second catalyst in the fixed bed at 300-600'C, preferably 300-450'C. The second catalyst used in the invention may be the commonly used catalyst in the reaction of catalytic cracking in the art. 10 In the invention, the first catalyst after being heated to a high temperature in the combustion chamber the first catalyst is charged into a pyrolysis reactor by using a spiral conveyor. Waste plastics (or heavy oil) are charged into the sealed pyrolysis reactor, and there they are directly mixed with the hot first catalyst to perform a reaction of pyrolysis and 15 first catalytic cracking. The materials are decomposed into gaseous hydrocarbons and residues. The gaseous hydrocarbons then enter a fixed bed in the reactor and are further decomposed into smaller molecules via a second catalytic cracking. Gaseous substances from the reaction are collected by means of the conventional process in the prior art so as to 20 obtain gasoline and diesel. Said first catalyst and residues in the reaction are introduced into a gasification chamber by a screw, and further into a separator by a spiral conveyor. Hot flue gas is led into the separator 4 WO 01/05908 PCT/CNOO/00196 with a blower, which blows said mixture into a cyclone separator so as to collect a solid mixture. Said mixture is introduced into a combustion chamber by a spiral conveyor. In the combustion chamber, organic substances in the mixture are burnt out, while the first catalyst is heated 5 and delivered to the spiral reactor again. In the above-mentioned process, the feedstock is mixed directly with hot first catalyst, and pyrolysis and the first catalytic cracking take place at the same time. The first catalyst is not only used as a heating medium but also as a catalyst, which can be recycled. 10 Said first catalyst is made as follows: powder Al 2 0 3 is mixed with water glass to obtain a slurry, and the resultant slurry is then mixed with catalyst HZSM-5; and the resultant mixture is dried, formed, granulated, and heated at a temperature of 550-800'C. The ratio between powder A1 2 0 3 and water glass to be used is 1:3-5 by weight and that between the 15 slurry and HZSM-5 is 1:0.2-0.5 by weight. Said first catalyst used in the invention is generally of a Mohs' scale of hardness of 7-9 and a diameter of 0.2-0.5mm. In the above process, said pyrolysis and first catalytic cracking may be conducted under standard atmosphere or higher. The reaction 20 temperature, when the first catalyst is transmitted from the combustion chamber to the pyrolysis reactor, is controlled at 500-1000C, preferably 600-700'C. The temperature of the first catalyst is kept at 400-800'C, 5 WO 01/05908 PCT/CN00/00196 preferably 500-600'C when it leaves the pyrolysis reactor. Said second catalytic cracking is carried out in the fixed bed inside the gasification chamber. Heat required in the second catalytic cracking is provided by the gasification chamber itself. The second 5 catalytic reaction is undertaken at 230-600'C, preferably 300-450'C. A particular catalyst DL-1 being composed of (Wt. %): 8% of CHO-l(a commodity produced by China Qilu Petrochemical Factory), 24% of REY, 25% of flokite (silicon/aluminum =12/1) and 43% of catalyst ZSM 5 is used in the second catalytic cracking after being thoroughly mixed 10 and calcined. The present invention will be more distinct with reference to the accompanying drawings. Referring to Fig. 1, a first catalyst 16 in the granular form is charged into a combustion chamber 21 from a storage tank 26 with a spiral 15 conveyor 27. Fuel oil (or recuperated pyrolysis gas) and air are sprayed into the combustion chamber 21 simultaneously via nozzles 18, 19 and 20. The first catalyst 16 in the combustion chamber 21 is heated to 500 1 ,000'C and subsequently led into a storage tank 17. A spiral conveyor 29 is started by a motor 1 to push the first catalyst 16 continuously into a 20 pyrolysis reactor 14. At the same time, the materials to be treated are pushed by a screw (or reciprocating) extruder 4 into a spiral reactor 14. If the materials are heavy oils, they may be pumped into the sealed 6 WO 01/05908 PCT/CNOO/00196 pyrolysis reactor 14 via an inlet 28. The materials are mixed directly with the first catalyst 16 in the reactor 14 to undergo a pyrolytic reaction and a first catalytic cracking. Rotated and pushed by the spiral conveyor 2, gaseous hydrocarbons generated from the reaction and residues move 5 forward to enter a vaporizer 13. Gaseous hydrocarbons enter a fixed bed 12 in the vaporizer 13 through the vaporization region, and react with a second catalyst to generate gaseous hydrocarbons with small molecules, which will be fractionated in a fractional column 9 to obtain gasoline and diesel by means of the conventional process. A mixture 10 of reaction 10 residues and the first catalyst 16 entering the bottom of the vaporizer 13 is driven into a separator 8 via a spiral conveyor 2. A blower 3 is employed to push the high-temperature flue gas into the separator 8 via an entrance 6. Solid mixture 25 containing the first catalyst are flown up to enter a cyclone 24 because they are lighter. Other heavy residues enter is the bottom of the separator 8 and are discharged from a hole 7. Thus, the solid mixture 25 in the cyclone 24 drops into a storage tank 26, and then is charged into the combustion chamber 21 by the spiral conveyor 27. In the combustion chamber 21, organic substances in the mixture 25 are burnt out and inorganic dusts are extracted together with high 20 temperature flue gas. The first catalyst 16 is hereby recovered and falls into the storage tank 17, subsequently. The heated first catalyst is then charged into the reactor 14 by the spiral conveyor 29. 7 WO 01/05908 PCT/CN00/00196 The invention is further described by the following examples. Example 1 5 Water glass (1,600kg, modulus>3) and powder A1 2 0 3 (400kg) were completely mixed to obtain a slurry. The slurry was mixed with catalyst HZSM-5 (800kg). The resultant mixture was dried, formed, granulated, and heated at 800'C for 4 hours to obtain the first catalyst with a Mohs' scale of hardness of 8.5 and a diameter of 0.4 mm. 10 2,000 kg of the first catalyst prepared as indicated above was charged into the combustion chamber 21, and simultaneously sprays 0" diesel (or recuperated pyrolysis gas) and air were led into the combustion chamber 21 to bum. The first catalyst was heated up to 600-700'C and then led into the pyrolysis reactor 14. The screw (or reciprocating) extruder 4 was is used to push 1,400kg of waste plastics (PP25%, PS25%, and PE50%) into the reactor 14 to perform the reaction. The temperature at the stock inlet of the reactor 14 was controlled at 600-700'C, whereas the temperature at the residue outlet thereof was controlled at 500-600'C. The catalyst DL-1 was arranged in the fixed bed 12, and the second catalytic reaction was 20 conducted therein. The reaction pressure was kept at 0.05-0.1 MPa. Gasoline and diesel were obtained from the fractional column 9. The mixture of the first catalyst and residues was charged into the combustion 8 WO 01/05908 PCT/CNO0/00196 chamber 21 and was heated up to 600-700 0 C therein to separate the first catalyst. The recovered first catalyst was introduced into the reactor 14 for heat supply. 5 Products generated from this Example are listed below: 1. Gasoline, 630kg, RON=93.5, components (by wt%): paraffin 19.9%, cyclanes 12%, olefin 48%, arenes 9.9%, others 10.2%; 2. Diesel, 420kg, cetane value=52, components (by wt%): paraffin 15%, cyclanes 8%, olefin 55%, arenes 10%, others 12%; 10 3. Inorganic residues 140kg; 4. Flammable gas 2 10kg. 15 20 9
Claims (10)
1. A process for producing gasoline and diesel from waste plastic and/or heavy oil comprises the steps of: 5 (a) mixing waste plastic and/or heavy oil with a first catalyst in a pyrolysis reactor at high temperature to carry out a pyrolytic reaction and a first catalytic cracking ; and (b) introducing the products in step (a) into a fixed bed to perform a second catalytic cracking with a second catalyst. 10
2. A process as claimed in Claim 1, wherein said first catalyst is made as follows: powder A1 2 0 3 is mixed with water glass to obtain a slurry, and the resultant slurry is then mixed with catalyst HZSM-5; and resultant mixture is dried, formed, granulized, and heated at 550-800'C.
3. A process as claimed in Claim 2, wherein the ratio between powder 15 A1 2 0 3 and water glass is 1:3-5 by weight and that between the slurry and HZSM-5 is 1:0.2-0.5 by weight.
4. A process as claimed in Claim 3, wherein said first catalyst is of a Mohs' scale of hardness of 7-9, and a diameter of 0.2-0.5mm.
5. A process as claimed in Claim 1, wherein the process further comprises 20 the step of: c) recycling the first catalyst in the reaction.
6. A process as claimed in Claim 1, wherein said catalyst in the fixed bed 10 WO 01/05908 PCT/CNOO/00196 comprises 8% of CHO-1, 24% of REY, 25% of flokite and 43% of catalyst ZSM-5, by weight.
7. A process as claimed in Claim 1, wherein the process is performed under the standard atmosphere or higher. 5
8. A process as claimed in Claim 1, wherein the temperature of the first catalyst is controlled at 500-1,000'C before entering the pyrolysis reactor, and is controlled at 400-800'C while leaving the pyrolysis reactor.
9. A process as claimed in Claim 1, wherein the first catalyst advances in the same flow direction as that of the waste plastics and/or heavy oil.
10 11
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN99216787 | 1999-07-16 | ||
CN99216787U CN2408118Y (en) | 1999-07-16 | 1999-07-16 | Equipment for producing gasoline and diesel oil by using waste plaste and/or heavy oil |
PCT/CN2000/000196 WO2001005908A1 (en) | 1999-07-16 | 2000-07-13 | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
Publications (1)
Publication Number | Publication Date |
---|---|
AU5801500A true AU5801500A (en) | 2001-02-05 |
Family
ID=5297315
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
AU58015/00A Abandoned AU5801500A (en) | 1999-07-16 | 2000-07-13 | A process for producing gasoline and diesel from waste plastics and/or heavy oil |
Country Status (8)
Country | Link |
---|---|
EP (1) | EP1228165A4 (en) |
JP (1) | JP2003528937A (en) |
KR (1) | KR20020052168A (en) |
CN (1) | CN2408118Y (en) |
AU (1) | AU5801500A (en) |
BR (1) | BR0012623A (en) |
CA (1) | CA2379529A1 (en) |
WO (1) | WO2001005908A1 (en) |
Families Citing this family (35)
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KR20010087776A (en) * | 2001-04-18 | 2001-09-26 | 김전열 | distillation- emulsifying technology through catalyst |
KR20020048350A (en) * | 2002-05-20 | 2002-06-22 | 박준호 | The catalytic composition to stimulate cracking reaction in oil process of utilizing waste synthetic resins |
FR2845391B1 (en) * | 2002-10-07 | 2006-05-12 | Inst Francais Du Petrole | PROCESS AND PLANT FOR PRODUCING SYNTHESIS GAS DEPOLLUED FROM A CHARGE RICH IN ORGANIC MATERIAL |
PL199825B1 (en) * | 2003-02-17 | 2008-11-28 | Zbigniew Tokarz | Method for continuous processing of organic wastes and a system designed for continuous processing of organic wastes |
US20060287560A1 (en) * | 2003-06-24 | 2006-12-21 | Fusheng Xie | Process and a device for producing gasoline, kerosene and diesel oil from waste plastic, rubber and machine oil |
MXPA06010339A (en) * | 2004-03-14 | 2007-01-23 | Ozmotech Pty Ltd | Process and plant for conversion of waste material to liquid fuel. |
WO2007122967A1 (en) * | 2006-04-19 | 2007-11-01 | Kusatsu Electric Co., Ltd. | Method of decomposing waste plastic/organic substance, decomposition apparatus, and decomposition system |
US7776284B2 (en) * | 2006-04-19 | 2010-08-17 | Kusatsu Electric Co., Ltd. | Apparatus of catalyst-circulation type for decomposing waste plastics and organics, and system thereof |
WO2008007384A1 (en) * | 2006-07-10 | 2008-01-17 | Sarjerao Nivrutti Sutar | Depolymerization op waste rubber and thermoplastics including pvc or pet into hydrocarbon fuels |
US7893307B2 (en) | 2007-02-23 | 2011-02-22 | Smith David G | Apparatus and process for converting feed material into reusable hydrocarbons |
WO2008131600A1 (en) * | 2007-04-28 | 2008-11-06 | Bin Niu | A process and a device for continuous cracking waste plastics |
KR101536156B1 (en) * | 2007-10-19 | 2015-07-13 | 쿠사츠 일렉트릭 컴퍼니 리미티드 | Catalyst circulating waste plastic/organic matter decomposition apparatus and decomposition system |
JP5638746B2 (en) * | 2008-08-20 | 2014-12-10 | 堺化学工業株式会社 | Catalyst and method for pyrolyzing organic matter and method for producing such a catalyst |
US8722958B2 (en) | 2008-08-20 | 2014-05-13 | Kusatsu Electric Co., Ltd. | Method of decomposing waste plastic/organic material using titanium oxide granule with optimal particle property |
US10131847B2 (en) | 2009-12-22 | 2018-11-20 | Plastic Energy Limited | Conversion of waste plastics material to fuel |
CN101805630A (en) * | 2010-05-21 | 2010-08-18 | 雪合来提 | Fluidizing bed type waste plastic continuous oil refining device with environment protection and high efficiency |
CN102382668B (en) * | 2010-09-01 | 2014-07-02 | 中国石油化工股份有限公司 | Coal cracking and heavy oil cracking joint production method |
CN102382669B (en) * | 2010-09-01 | 2014-07-02 | 中国石油化工股份有限公司 | Coal cracking and heavy oil cracking joint production method |
US8895790B2 (en) | 2013-02-12 | 2014-11-25 | Saudi Basic Industries Corporation | Conversion of plastics to olefin and aromatic products |
US9447332B2 (en) | 2013-02-12 | 2016-09-20 | Saudi Basic Industries Corporation | Conversion of plastics to olefin and aromatic products using temperature control |
US9428695B2 (en) * | 2013-02-12 | 2016-08-30 | Saudi Basic Industries Corporation | Conversion of plastics to olefin and aromatic products with product recycle |
WO2014145223A1 (en) * | 2013-03-15 | 2014-09-18 | Battelle Memorial Institute | Vapor phase catalytic reactor for upgrade of fuels produced by fast pyrolysis of biomass |
US20170247617A1 (en) | 2013-09-26 | 2017-08-31 | Biobtx B.V. | Process for the Preparation of Aromatic Compounds |
PL229433B1 (en) * | 2014-09-05 | 2018-07-31 | Realeco Spolka Z Ograniczona Odpowiedzialnoscia | Mineral additive, preferably to be used in the process of continuous processing of plastic scrap, method in which this additive is used and the said additive and the device for the execution of this method |
EP3858951A1 (en) | 2014-12-17 | 2021-08-04 | Pilkington Group Limited | Furnace |
CN105567309B (en) * | 2015-12-18 | 2018-01-09 | 云南新昊环保科技有限公司 | Waste mineral oil circulation flash distillation catalytic pyrolysis reclaimer |
ES2618857B1 (en) * | 2015-12-21 | 2018-07-27 | Neoliquid Advanced Biofuels And Biochemicals, S.L. | Thermochemical procedure, and installation, to transform polymeric materials |
EP3976732A4 (en) | 2019-05-24 | 2023-05-17 | Eastman Chemical Company | Blend small amounts of pyoil into a liquid stream processed into a gas cracker |
CN110330996B (en) * | 2019-07-19 | 2021-10-29 | 华东理工大学 | Method and device for hydrocracking mineralized refuse pyrolysis oil |
CN114585710A (en) | 2019-10-24 | 2022-06-03 | 埃克森美孚化学专利公司 | Direct steam cracking process for liquids produced from plastic waste |
US11319262B2 (en) | 2019-10-31 | 2022-05-03 | Eastman Chemical Company | Processes and systems for making recycle content hydrocarbons |
US11945998B2 (en) | 2019-10-31 | 2024-04-02 | Eastman Chemical Company | Processes and systems for making recycle content hydrocarbons |
CN114650981A (en) | 2019-11-07 | 2022-06-21 | 伊士曼化工公司 | Recovery of the components alpha-olefin and fatty alcohol |
US20230002681A1 (en) * | 2021-06-30 | 2023-01-05 | Encina Development Group, LLC | Apparatus and processes for pyrolysis of plastic feeds |
US11859132B2 (en) | 2021-08-05 | 2024-01-02 | Indian Oil Corporation Limited | Process and an apparatus for conversion of waste plastic pyrolysis oil into valuable products |
Family Cites Families (11)
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JPS63178195A (en) * | 1987-01-20 | 1988-07-22 | 工業技術院長 | Production of low boiling point hydrocarbon oil from polyolefinic plastic |
US5079385A (en) * | 1989-08-17 | 1992-01-07 | Mobil Oil Corp. | Conversion of plastics |
US5368723A (en) * | 1992-02-10 | 1994-11-29 | Mazda Motor Corporation | Method of and apparatus of producing low boiling point hydrocarbon oil from waste plastics or waste rubbers |
CN1075328A (en) * | 1992-02-12 | 1993-08-18 | 赵太平 | Method and apparatus for continuous production of petroleum products from waste plastics |
JPH06220461A (en) * | 1993-01-22 | 1994-08-09 | Mazda Motor Corp | Production of hydrocarbon oil from waste plastic or rubber material and equipment for use therein |
JP3383374B2 (en) * | 1993-08-26 | 2003-03-04 | 触媒化成工業株式会社 | Catalyst composition for catalytic cracking of hydrocarbons and method for producing the same |
US5686055A (en) * | 1993-12-27 | 1997-11-11 | Mazda Motor Corporation | Process for recovering phthalic anhydride and hydrogen chloride from plastic materials |
CN1145395A (en) * | 1995-08-08 | 1997-03-19 | 周鼎力 | Method and appts. for prodn. gasoline, diesel oil and carbon black by utilizing wasted rubber |
JPH09310075A (en) * | 1996-05-22 | 1997-12-02 | Densen Sogo Gijutsu Center | Treatment of rubber/plastic waste and system therefor |
JPH1161158A (en) * | 1997-08-20 | 1999-03-05 | Ishikawajima Harima Heavy Ind Co Ltd | Reformation of plastic into oil and installation therefor |
CN1068032C (en) * | 1998-08-27 | 2001-07-04 | 邢力 | Hydrocarbon preparing method and equipment using household refuse and/or organic waste |
-
1999
- 1999-07-16 CN CN99216787U patent/CN2408118Y/en not_active Expired - Fee Related
-
2000
- 2000-07-13 JP JP2001511126A patent/JP2003528937A/en active Pending
- 2000-07-13 KR KR1020027000608A patent/KR20020052168A/en not_active Application Discontinuation
- 2000-07-13 CA CA002379529A patent/CA2379529A1/en not_active Abandoned
- 2000-07-13 BR BR0012623-3A patent/BR0012623A/en not_active Application Discontinuation
- 2000-07-13 AU AU58015/00A patent/AU5801500A/en not_active Abandoned
- 2000-07-13 EP EP00943524A patent/EP1228165A4/en not_active Withdrawn
- 2000-07-13 WO PCT/CN2000/000196 patent/WO2001005908A1/en not_active Application Discontinuation
Also Published As
Publication number | Publication date |
---|---|
KR20020052168A (en) | 2002-07-02 |
EP1228165A1 (en) | 2002-08-07 |
BR0012623A (en) | 2003-04-08 |
JP2003528937A (en) | 2003-09-30 |
CA2379529A1 (en) | 2001-01-25 |
WO2001005908A1 (en) | 2001-01-25 |
EP1228165A4 (en) | 2004-01-28 |
CN2408118Y (en) | 2000-11-29 |
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