WO2006010324A1 - Procede de production de carburants a partir de dechets de plastiques par craquage catalytique sous pression atmospherique - Google Patents

Procede de production de carburants a partir de dechets de plastiques par craquage catalytique sous pression atmospherique Download PDF

Info

Publication number
WO2006010324A1
WO2006010324A1 PCT/CN2005/001120 CN2005001120W WO2006010324A1 WO 2006010324 A1 WO2006010324 A1 WO 2006010324A1 CN 2005001120 W CN2005001120 W CN 2005001120W WO 2006010324 A1 WO2006010324 A1 WO 2006010324A1
Authority
WO
WIPO (PCT)
Prior art keywords
cracking
components
temperature
producing fuel
waste plastic
Prior art date
Application number
PCT/CN2005/001120
Other languages
English (en)
Chinese (zh)
Inventor
Falai Chen
Qing Lin
Original Assignee
Hefei Lafa Environmental Protection Technology Development Co., Ltd.
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 Hefei Lafa Environmental Protection Technology Development Co., Ltd. filed Critical Hefei Lafa Environmental Protection Technology Development Co., Ltd.
Publication of WO2006010324A1 publication Critical patent/WO2006010324A1/fr

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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal

Definitions

  • the invention relates to a process for continuously producing fuel oil by using waste plastics. Background technique
  • the invention aims to: provide a process method for producing fuel by atmospheric pressure catalytic cracking of waste plastic without cleaning and drying the waste plastic raw materials and having a light oil ratio ⁇ by improving the catalyst and the processing technology.
  • the present invention provides a method for producing fuel oil by atmospheric pressure catalytic cracking of waste plastics, the method comprising the following steps:
  • Heating and plasticizing the broken waste plastic raw material is heated by a screw extruder, wherein the barrel temperature of the screw extruder is 180 ⁇ 220 ° C;
  • Catalytic cracking the raw material which is heated and plasticized is subjected to gas phase catalytic cracking in a cracking vessel packed with a catalyst and a protective filler for 3 to 4 hours to form low molecular hydrocarbons and waste slag, wherein the temperature in the cracking kettle is 380 ⁇ 400°C; wherein the weight ratio of the catalyst to the waste plastic is: 1:6000-7000, the catalyst is a Y-type zeolite molecular sieve; and the protective filler is a ceramic ball;
  • Cooling low molecular steroids are cooled to room temperature and are classified into gas components and liquid components;
  • Fractionation of gasoline component The liquid component is fractionated in a fractionation kettle, wherein the temperature of the fractionation kettle is raised from normal temperature to 180 ° C at a rate of 1 ° C / minute, and the main component is C 4 ⁇ C U
  • the gasoline component of the hydrocarbon, the gasoline component is divided into three components according to the following fractionation temperature: 20 ° C ⁇ 70 ° C, 70 ° C ⁇ 120 ° C and 120 ° C ⁇ 180 ° C;
  • Fractionation of kerosene diesel fuel component the temperature of the fractionation kettle is continuously increased from 180 ° C to 350 ° C at a rate of 2 ° C / min, and the kerosene whose main component is C 12 ⁇ C 2 o hydrocarbon is fractionated. And the diesel component, the diesel component is divided into three components according to the following fractionation temperature: no higher than 300 ° C, 300 ° C ⁇ 330 ° C and 330 ° C ⁇ 350 ° C.
  • the unit cell composition of the Y-type zeolite molecular sieve is Me 56/n [(AlO 2 ) 56 (SiO 2 ) 136 ]-250H 2 O and the oxidation formula is Na 2 OAl 2 O y xSi0 2 -yH 2 0, according to the molecular weight of formula oxide meter is 530 ⁇ 686, Si0 2 / Al 2 0 3> 4.5 and 0.9 pore size molecular sieve - 1 nm, wherein Me represents a cation, The cation is Na+ or Ca 2+ ; n represents the ionic valence of the cation; x is 4.0 to 6.0; and y is 7.0 to 9.0.
  • step (2) of the method further comprises the steps of: after 3 to 4 hours of catalytic cracking, lowering the temperature to below 300 ° C, starting slagging, wherein The slag discharge is carried out through a water-tight slag discharge bin:
  • the exhaust pipe on the slag discharge bin is in an inverted U shape, and the exhaust port is immersed in water.
  • step (4) of the method further comprises the steps of: feeding the three components into the mixed component tank, and adding the concentration to a concentration of 5 to 10% by weight
  • the 3% ⁇ 5% sodium hydroxide solution is washed by a mixer, and then passed through a depth filter to enter the product oil tank to obtain a finished gasoline product.
  • step (5) of the method further comprises the steps of: feeding the three components into the mixing component tank, adding the concentration to a concentration of 5-10% by weight
  • the 3% ⁇ 5% sodium hydroxide aqueous solution is washed by a mixer, and then passed through a depth filter to enter the product oil tank to obtain a finished diesel product.
  • the volume accounts for the volume ratio of the total.
  • step (3) of the method further comprises the steps of: introducing the gas component into the gas recovery device, collecting and compressing into a combustible gas for use as a living fuel.
  • step (3) of the method further comprises the steps of: introducing the gas component into the gas recovery device, collecting and compressing into a combustible gas for use as a living fuel.
  • the process of the invention is produced, the catalytic cracking is sufficient, the oil yield is as high as 60-85%, the quality of the oil is good, the gasoline is No. 90, and the diesel is from No. 0 to No. 20.
  • the whole production process is fully enclosed and clean continuous production.
  • the waste plastic raw materials do not need to be classified, cleaned and dried.
  • the pickling and washing are omitted in the production process, and the alkaline washing method is used to achieve automatic neutralization without secondary pollution. Reduced production costs.
  • FIG. 1 is a process flow diagram of the present invention. detailed description
  • the invention relates to a process method for producing fuel by atmospheric pressure catalytic cracking of waste plastic, and the method comprises the following steps:
  • the catalyst is Y zeolite molecular sieve (can be obtained from Nanjing Jinling Petrochemical Plant or Lanzhou Petrochemical Plant)
  • the molecular sieve has a pore size in the range of 0.9 to 1 nanometer, and the unit cell composition of the Y zeolite molecular sieve is Me 56/n [(AlO 2 ) 56 (SiO 2 ) 136 ]_250H 2 O and the oxidation formula is Na 2 OAl 2 .
  • the relative molecular mass according to the oxidation formula is 530-686, Si0 2 /Al 2 0 3 ⁇ 4.5 and the molecular sieve has a pore diameter in the range of 0.9 to 1 nanometer, wherein Me represents a cation, and the cation is Na + or Ca 2+ ; n represents the ionic valence of the cation; x is 4.0 to 6.0; and y is 7.0 9.0; the protective filler is a ceramic ball; and the electrothermal cracking vessel is preheated before feeding, to the electrothermal pyrolysis kettle
  • the set temperature is 350 ° C in the upper part of the kettle, 400 ° C in the lower part of the kettle, 50 CTC at the bottom of the kettle; preheating time 30 minutes
  • the preheating temperature is around 10 (TC);
  • the electrothermal cracking kettle has a deceleration mixer.
  • the speed of the deceleration stirrer is 20 ⁇ 23 rev / min; that is, stirring while heating while feeding;
  • the macromolecular chain When the catalyst is contacted, the macromolecular chain is broken, and the hydrocarbon having a small molecular chain C 2Q or lower flows out through the pores, and the unbroken macromolecular chain is stirred and stirred to continue contact with the catalyst while being heated.
  • a small molecular chain becomes a light oil. It takes 3-4 hours of catalytic cracking reaction. Then, it is cooled to 300 ° C. It starts to slag at high temperature through a high-temperature slag discharger. The vent is immersed in water for 5 mm. Through the water sealing, the slag discharge time is 5 minutes, the carbon residue is screened into high-quality carbon without secondary pollution; then the above-mentioned feeding, heating, reaction and slagging processes are circulated;
  • the cracked low molecular hydrocarbons are cooled by the primary heat exchanger to a liquid at normal temperature, and most of the liquids with a total oil yield of 60 to 85% are passed through a gas-liquid separator, a water separator, and a filter.
  • the device enters the mixing tank; the sight glass is used to observe the oil condition; a small part of the non-solidified gas separated by the gas-liquid separator enters the gas recovery device, and after the second-stage low-temperature heat exchange, the collection is compressed in the collector to be
  • the gas is used as a living fuel without secondary pollution; the partially cracked product is cooled by a desuperheater and sent to a fractionation kettle;
  • the oil of the mixed oil tank is sent to the fractionation kettle through the pipeline.
  • the oil level should not exceed 2/3 of the capacity of the kettle body.
  • the temperature is raised by electric heating. The temperature is between normal temperature and 18CTC, and the temperature is raised at the speed of C/min.
  • the main component is C 4 ⁇ C U hydrocarbon, which is a component of gasoline; the components of gasoline are fractionated by temperature during fractionation: 30 ° C ⁇ 70 ° C, 70 ° C ⁇ 120 ° C 120 ° C ⁇ 180 ° C, respectively accounted for 10%, 50%, 90% of the total volume ratio (V accumulation / V total), the fractionated gasoline passed through the gasoline primary heat exchanger, used to observe Liquid mirror, gas-liquid separator, oil-water separator, filter, after entering the gasoline component tank, through the flow meter, component mixing tank, and then adding the concentration of 3% ⁇ 5 according to the weight ratio of 5 ⁇ 10% % sodium hydroxide alkali solution is refined in the refiner, and then passed through the depth filter to enter the gasoline product oil tank;
  • the main component of this range of fractionation is C 12 ⁇ C 2C hydrocarbons, is a component of kerosene and diesel; Kerosene and excess component oil are used as fuel; the components of diesel are also fractionated by temperature during the fractionation process: one set is not higher than 300 °C, and the second group is 330 °C ⁇ .330 °C.
  • C is the third group, which accounts for the total volume ratio (V accumulation / V total) 50%, 90%, 95% of the fractionated diesel oil passes through the diesel primary heat exchanger, the sight glass used to observe the liquid discharge condition, the filter, the diesel fuel component tank, the flow meter, the component mixing tank Then, add 5 to 10% by weight to the concentration of 3% ⁇ 5% sodium hydroxide solution in the refiner, and then go through the depth filter into the diesel product tank.
  • the Y-type zeolite molecular sieve is a catalyst of a silica-alumina molecular sieve having a pore diameter of 0.9 to 1 nanometer; the filler ceramic sphere has a diameter ranging from 8 to 12 mm. '
  • the whole production process is completely closed and clean production, and the slag discharge is carried out by water sealing without secondary pollution.
  • the exhaust pipe on the slag discharge bin is inverted U-shaped, and the exhaust port is immersed in water 5 mm, carbon
  • the slag is separated into high-quality carbon black by a screening device; the exhaust gas is collected and compressed by a gas recovery device, and the compressed gas is collected for use as a daily life fuel.
  • the test method is to use an electric pyrolysis kettle and a fractionation kettle for continuous production for 72 hours. Before the feed is completed, 10 kg of catalyst (Y-type molecular sieve, obtained from Nanjing Jinling Petrochemical Plant) is placed in the catalytic tower at the top of the electrothermal reactor.
  • catalyst Y-type molecular sieve, obtained from Nanjing Jinling Petrochemical Plant
  • the set temperature of the cracking kettle is: The upper temperature of the autoclave is 350 °C, the lower temperature of the kettle is 40 (TC, the bottom of the kettle is 500 ⁇ ; the preheating time is 30 minutes, pre The heat temperature is about 100 ° C; at the same time, the feeder barrel is preheated for 30 minutes, the set temperature is 200 ° C, and the feed enters the cracker at a feed rate of 150 kg per hour.
  • the stirrer on the kettle is 20 per minute. The rotation speed was continuously stirred.
  • the feed was stirred while heating, and the feed was suspended after 30 hours of continuous feeding, and the set temperatures of the cracking kettle were changed to 380 ° C, 400 ° C, and 550 ° C, respectively.
  • the pyrolysis kettle be kept at 380 ° C ⁇ 400 ° C for 3 ⁇ 4 hours catalytic cracking reaction, at this time the material in the kettle is vaporized, the small molecular chain in the vaporization, that is, the hydrocarbon below C 2 o can pass through the Y molecular sieve
  • the aperture flows into the pipeline and is cooled to become light oil, while the large fraction Chain C 2G is more hydrocarbons can not be 0.9-1 nm pore size molecular sieves, which upon contact with the catalyst macromolecular chains to be interrupted, into smaller hydrocarbon molecules chain C 5 -C 2Q by aperture
  • the macromolecular chain that has flowed out and is not interrupted continues to contact with the catalyst while stirring, and breaks into a small molecular chain to become a
  • °C takes one hour and then drains for 5 minutes. Thereafter, it is produced according to the above procedure: feeding, heating, reaction, slagging, and the like.
  • the cracked low molecular hydrocarbons are mostly liquid when cooled to normal temperature, and the oil yield is 75%. Most of the liquid enters the oil tank through the gas-liquid separator, oil-water separator and filter; small part ⁇ C 4
  • the flammable gas is separated into a gas recovery device by a gas-liquid separator and then cooled and compressed by a secondary refrigeration system to be converted into a civil liquefied gas.
  • the oil in the oil tank is sent to the fractionation tank through the pipeline.
  • the oil level should not exceed 2/3 of the capacity of the kettle body, and then the temperature is raised by electric heating.
  • the main component fractionated is C 4 ⁇ C n hydrocarbon, which is a component of gasoline; the components of gasoline are fractionally distilled into three components during the fractionation process, and are respectively entered into three component tanks of different temperature ranges. Distillation according to the gasoline process standard (less than 70 ° C, 70 ° C ⁇ 120 ° C, 120 ° C ⁇ 180 ° C, respectively, the total volume ratio (V accumulation / V total) 10%, 50%, 90%. Enter the mixed component tank, add 5 ⁇ 10% weight ratio, add 3%-5% sodium hydroxide solution automatically, and then pass through the depth filter to enter the finished gasoline tank. 90#.
  • the feed is heated while stirring; when the feed is finished, the temperature is reset.
  • the limits are 380 ° C, 400 ° C, 550 ° C.
  • the material in the kettle is vaporized, the small molecular chain in the vaporization, that is, the hydrocarbon below C 20 can pass through the Y molecular sieve
  • the pore size flows into the pipeline to be cooled into a light oil, and the large molecular chain, that is, the hydrocarbon above C 2Q cannot pass through the pore size of the molecular sieve of 0.9-1 nm, and the macromolecular chain is broken when it contacts the catalyst.
  • the hydrocarbon chain which becomes a small molecular chain C 5 -C 2C flows out through the pores, and the unbroken macromolecular chain continues to contact with the catalyst while stirring, and breaks into a small molecular chain, becoming light.
  • the oil is then cooled rapidly by the fan, and the temperature is reduced from 40CTC to 300'C and then discharged automatically. It takes 5 minutes to drain the slag. Then, the production process is cycled according to the above procedure, and the preheating process can be omitted.
  • the cracked low molecular hydrocarbons are cooled, the oil yield is 80%, and most of the liquid becomes liquid through the gas-liquid separator, oil-water separator, and filter into the oil tank; a small part of Q ⁇ C 4 flammable gas is gas
  • the liquid separator is separated into a gas recovery device and then cooled and compressed by a secondary refrigeration system to be converted into a civil liquefied gas with a yield of 5%.
  • the oil in the oil tank is sent to the fractionation tank through the pipeline.
  • the oil level should not exceed 2/3 of the capacity of the kettle body, and then the temperature is raised by electric heating. The temperature rises from normal temperature to 180 °C, and the temperature rises at 1 °C/min.
  • the main component of this range is C 4 ⁇ C
  • Cincinnati hydrocarbon which is a component of gasoline; the components of gasoline are fractionally distilled into three components during the fractionation process, and enter the component tanks of three different temperature zones. Distillation according to the gasoline process standard (less than 70 ° C, 70 ° C ⁇ 120 ° C, 120 ° C ⁇ 180 ° C, respectively, accounting for 10%, 50%, 90% of the total volume). , and then automatically cleaned by adding 3% ⁇ 5% alkali solution in a weight ratio of 5 ⁇ 10%, and then into the finished gasoline tank through the depth filter, the output gasoline number is 90#.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé permettant de produire des carburants à partir de déchets de plastiques par craquage catalytique sous pression atmosphérique. Ledit procédé consiste en une mise à température d'une alimentation, un craquage catalytique et un fractionnement. Le catalyseur est du type tamis moléculaire zéolitique, la charge étant constituée de billes de porcelaine. Dans le procédé de l'invention, le craquage catalytique peut s'effectuer de manière suffisante, le rapport de sortie des carburants pouvant atteindre 60 à 85 %, et la qualité de ces carburants étant élevée, 90# pour l'essence et 0# à 20# pour le diesel. Le procédé de production globale est complètement fermé, propre et continu; le matériau brut de déchets de plastiques ne nécessite pas de tri, de purge et de séchage; la neutralisation automatique peut s'effectuer par lavage caustique tout en éliminant une seconde pollution et réduisant les coûts de production.
PCT/CN2005/001120 2004-07-26 2005-07-26 Procede de production de carburants a partir de dechets de plastiques par craquage catalytique sous pression atmospherique WO2006010324A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN200410041527.5 2004-07-26
CN 200410041527 CN1597848A (zh) 2004-07-26 2004-07-26 废塑料裂解生产燃油的工艺方法

Publications (1)

Publication Number Publication Date
WO2006010324A1 true WO2006010324A1 (fr) 2006-02-02

Family

ID=34665120

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2005/001120 WO2006010324A1 (fr) 2004-07-26 2005-07-26 Procede de production de carburants a partir de dechets de plastiques par craquage catalytique sous pression atmospherique

Country Status (2)

Country Link
CN (1) CN1597848A (fr)
WO (1) WO2006010324A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102061185B (zh) * 2009-11-13 2013-10-09 环拓科技股份有限公司 连续式裂解系统及其应用
WO2015012676A1 (fr) 2013-07-25 2015-01-29 Newpek S.A. De C.V. Procédé et équipement pour la production d'hydrocarbures par décomposition catalytique de déchets plastiques en un seul passage
CN106609144A (zh) * 2015-10-23 2017-05-03 湖南杰能环保科技有限公司 一种混合废有机物的裂解处理方法
WO2018104401A1 (fr) * 2016-12-07 2018-06-14 Solvay Sa Processus de conversion par craquage de plastique en gaz, combustibles liquides et cires
CN112694552A (zh) * 2020-12-31 2021-04-23 扬州天诗新材料科技有限公司 一种具有较低分子量分布指数的聚乙烯蜡的制备方法

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1597848A (zh) * 2004-07-26 2005-03-23 合肥来发环保科技开发有限公司 废塑料裂解生产燃油的工艺方法
CN101260309B (zh) * 2008-04-28 2011-03-09 同济大学 混合型废塑料连续催化裂解生产燃油的方法
CN102311749B (zh) * 2011-08-05 2013-09-18 浙江国裕资源再生利用科技有限公司 固体超强酸催化裂解造纸废渣制备燃料油的方法
CN102517063A (zh) * 2011-11-22 2012-06-27 言显志 塑料垃圾转化成燃料油的转化系统
CN103159613B (zh) * 2011-12-15 2015-09-23 上海华谊丙烯酸有限公司 回收设备和使用该设备的回收方法
CN103450932A (zh) * 2012-05-31 2013-12-18 青岛神源生物质能科技有限公司 焦油常压催化裂解生产燃油的工艺方法
CN102757801B (zh) * 2012-06-27 2014-12-24 北京神雾环境能源科技集团股份有限公司 一种油页岩流化床蒸气低温干馏方法及系统
CN103589454A (zh) * 2013-11-21 2014-02-19 南开大学 一种废塑料热解油制备清洁燃料油的方法
CN105038851B (zh) * 2015-08-04 2017-03-15 陕西延长石油（集团）有限责任公司榆林炼油厂 一种dcc裂解轻油加工工艺
CN108503092A (zh) * 2018-05-29 2018-09-07 青岛德清源环保科技有限公司 废塑料裂解燃油燃气再生水的后期处理工艺
CN116000047A (zh) * 2021-10-22 2023-04-25 中国石油化工股份有限公司 一种废塑料的联合预处理方法和系统

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4948495A (en) * 1988-07-26 1990-08-14 The United States Of America As Represented By The United States Department Of Energy High liquid yield process for retorting various organic materials including oil shale
EP0414439A2 (fr) * 1989-08-17 1991-02-27 Mobil Oil Corporation Conversion de matières plastiques
JPH0559372A (ja) * 1991-09-02 1993-03-09 Sanwa Kako Kk ポリオレフイン系樹脂から燃料油を製造する方法
CN1266042A (zh) * 1999-03-09 2000-09-13 李智范 用废旧聚乙烯和聚丙烯塑料生产液态烯烃的方法
CN1492024A (zh) * 2003-09-30 2004-04-28 吴克斌 废塑料炼油工艺及设备
CN1597848A (zh) * 2004-07-26 2005-03-23 合肥来发环保科技开发有限公司 废塑料裂解生产燃油的工艺方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4948495A (en) * 1988-07-26 1990-08-14 The United States Of America As Represented By The United States Department Of Energy High liquid yield process for retorting various organic materials including oil shale
EP0414439A2 (fr) * 1989-08-17 1991-02-27 Mobil Oil Corporation Conversion de matières plastiques
JPH0559372A (ja) * 1991-09-02 1993-03-09 Sanwa Kako Kk ポリオレフイン系樹脂から燃料油を製造する方法
CN1266042A (zh) * 1999-03-09 2000-09-13 李智范 用废旧聚乙烯和聚丙烯塑料生产液态烯烃的方法
CN1492024A (zh) * 2003-09-30 2004-04-28 吴克斌 废塑料炼油工艺及设备
CN1597848A (zh) * 2004-07-26 2005-03-23 合肥来发环保科技开发有限公司 废塑料裂解生产燃油的工艺方法

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102061185B (zh) * 2009-11-13 2013-10-09 环拓科技股份有限公司 连续式裂解系统及其应用
WO2015012676A1 (fr) 2013-07-25 2015-01-29 Newpek S.A. De C.V. Procédé et équipement pour la production d'hydrocarbures par décomposition catalytique de déchets plastiques en un seul passage
US10240093B2 (en) 2013-07-25 2019-03-26 Newpek S.A. De C.V. Method and equipment for producing hydrocarbons by catalytic decomposition of plastic waste products in a single step
CN106609144A (zh) * 2015-10-23 2017-05-03 湖南杰能环保科技有限公司 一种混合废有机物的裂解处理方法
CN106609144B (zh) * 2015-10-23 2018-06-19 湖南杰能环保科技有限公司 一种混合废有机物的裂解处理方法
WO2018104401A1 (fr) * 2016-12-07 2018-06-14 Solvay Sa Processus de conversion par craquage de plastique en gaz, combustibles liquides et cires
CN108603122A (zh) * 2016-12-07 2018-09-28 索尔维公司 用于通过裂化将塑料转化为气体、液体燃料和蜡的方法
CN112694552A (zh) * 2020-12-31 2021-04-23 扬州天诗新材料科技有限公司 一种具有较低分子量分布指数的聚乙烯蜡的制备方法

Also Published As

Publication number Publication date
CN1597848A (zh) 2005-03-23

Similar Documents

Publication Publication Date Title
WO2006010324A1 (fr) Procede de production de carburants a partir de dechets de plastiques par craquage catalytique sous pression atmospherique
KR100322663B1 (ko) 폐플라스틱을 이용한 휘발유, 등유 및 경유의 연속식제조방법 및 그 시스템
TW294686B (fr)
KR101289583B1 (ko) 폐기물 물질의 액체 연료로의 전환 방법 및 이를 위한 장치
EP1707614A1 (fr) Procédé de craquage thermique ou catalytique de charges hydrocarbures et système correspondant
CA2367937C (fr) Procede de transformation des dechets de polyolefines en hydrocarbures, et usine de traitement
CN114507542B (zh) 一种废塑料制备轻质油品的方法及系统
CN106635115A (zh) 利用混合废塑料垃圾高效清洁制油的方法及水热反应系统
CN1031199C (zh) 用废塑料生产燃料的方法及其装置
CN113122300A (zh) 一种高分子聚合废物热解制油工艺方法及装置
CN103597057B (zh) 有关产品物流分离的改进
CN101260309B (zh) 混合型废塑料连续催化裂解生产燃油的方法
WO2005028593A1 (fr) Procede industrialise et dispositif servant a la production d'essence et de gazole a partir de dechets de plastique
WO2005017069A1 (fr) Procede et dispositif pour produire de l'essence, du kerosene, et du diesel a partir de dechets de plastique, de caoutchouc et d'huiles de machines
KR0176743B1 (ko) 폐 플라스틱을 이용한 연료제조방법 및 장치
Buekens et al. Technical methods in plastics pyrolysis
CN1077479A (zh) 用废聚烯烃塑料制造烃油的方法
WO2021012838A1 (fr) Procédé et appareil d'hydrocraquage d'huile de pyrolyse de déchets minéralisés
AU697420B2 (en) Method for making fuel oil from waste plastic and device therefor
CN2397116Y (zh) 一种用废轮胎和或有机废弃物制取烃油的设备
JP2023532532A (ja) プラスチック廃棄物材料を処理するための方法およびシステム
CN207159148U (zh) 一种含煤粉煤焦油的净化系统
CN208346097U (zh) 一种餐厨垃圾催化裂解炼油系统
KR100517898B1 (ko) 폐합성수지를 원료로 하는 촉매 하행식 크래킹반응기 및 이를 이용한 휘발유·경유의 제조방법
WO1995006682A1 (fr) Procede et appareil de production d'essence et de gazole a partir de dechets plastiques

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KM KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NG NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SM SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): BW GH GM KE LS MW MZ NA SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LT LU LV MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase