EP1707614A1 - Thermisches oder katalytisches Spaltverfahren für Kohlenwasserstoffeinsätze und entsprechendes System - Google Patents

Thermisches oder katalytisches Spaltverfahren für Kohlenwasserstoffeinsätze und entsprechendes System Download PDF

Info

Publication number
EP1707614A1
EP1707614A1 EP05460034A EP05460034A EP1707614A1 EP 1707614 A1 EP1707614 A1 EP 1707614A1 EP 05460034 A EP05460034 A EP 05460034A EP 05460034 A EP05460034 A EP 05460034A EP 1707614 A1 EP1707614 A1 EP 1707614A1
Authority
EP
European Patent Office
Prior art keywords
reaction
zone
gas
hydrocarbons
cracking
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Withdrawn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
EP05460034A
Other languages
English (en)
French (fr)
Inventor
Miroslaw Konopka
Lilia Maciukiewicz-Sosnowska
Tadeusz Chrapek
Zbigniew Packowski
Roman Kempinski
Wieslawa Fila
Slawomir Szumacher
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.)
Osrodek Badawczo-Rozwojowy Przemyslu Rafineryjnego
Original Assignee
Osrodek Badawczo-Rozwojowy Przemyslu Rafineryjnego
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 Osrodek Badawczo-Rozwojowy Przemyslu Rafineryjnego filed Critical Osrodek Badawczo-Rozwojowy Przemyslu Rafineryjnego
Publication of EP1707614A1 publication Critical patent/EP1707614A1/de
Withdrawn legal-status Critical Current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
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/22—Non-catalytic cracking in the presence of hydrogen
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils

Definitions

  • the subject-matter of the invention is the technology of hydrocarbons feedstock processing using the method of thermal or catalytic cracking and the installation of hydrocarbons feedstock processing based on the method of thermal or catalytic cracking designed for hydrocarbons with lower molecular weights. Both the technology and the installation are useful especially in processing of waste raw-materials - used ones, impure or being the residues received in various technological processes.
  • waste raw-materials contain waste plastics, including polyethylene, polypropylene, polystyrene and polyvinyl chloride (PVC), used lubricating oils and lubricants, distillation residues, impure heavy hydrocarbon fractions of various origin or used and fresh vegetable and animal fats as applicable in production of fuels.
  • the above methods contain also methods consisting in conversion of waste into high-value hydrocarbon products received in such processes as hydro cracking, thermal and catalytic cracking.
  • hydro cracking thermal or catalytic cracking bond cleavage occurs to raw-materials molecules and the mixture of hydrocarbons with lower molecular weights is received.
  • the most required products in the process are hydrocarbons fractions corresponding to petrol fractions and diesel oil fractions.
  • German patent No 100 49 377 the technology as well as the installation for production of diesel oil and petrol (but mainly diesel oil) by cracking of mixtures composed of various kinds of used oils and lubricants, mineral and biological oils, heavy oils being distillation residues with the addition of plastics waste has been presented.
  • the oil products submitted to processing have the boiling point within the range of 350-550°C.
  • the sodium aluminosilicate is being used as a catalyst.
  • the process itself is conducted under such conditions, in which a part of the reaction mixture from the reactor equipped with a mechanical mixer passes through a tubing into the inter-tubular space of the jacket - tubular vaporizer; then - the reaction mixture is heated by combustion gas having a very high temperature equal to 1100-1200°C at the inlet to vaporizer tubes and through the tubing is turned back to the reactor enabling to maintain the temperature in the reactor at the level of 410-460° C.
  • a low pressure of 30-150 millibars generated in a vacuum pump is employed.
  • the combustion gas is produced during combustion of solid, liquid or gas fuels; at the same time impurities collected at the bottom of the reactor are introduced into the combustion chamber situated in the lower part of the vaporizer. Directly on the reactor, the fractionating column for products is situated centrically.
  • the subject-matter of the invention as referred to in the Polish patent application No 332762 is conversion of polyolefin's waste at the temperature not exceeding 600°C and in the presence of the specified catalysts.
  • the reactor (similarly to the other discussed solutions) is heated by means of indirect exchange of heat with hot combustion gas.
  • the reactor is surrounded by the combustion chamber provided with burners, in which the fuel obtained as the product of reaction is being burnt; from the combustion chamber passage heating tubes are led out passing through the reactor inside and through which combustion gas from the combustion chamber is flowing out.
  • the reactor is provided with the mixer.
  • the subject-matter of the invention as referred to in the Polish patent application No 337413 is the processing of liquid fuels with waste of polyolefin's plastics; the essence of the invention is application of the mixture composed of wastes and technological oil (most frequently - the used one) as a raw-material, mixed according to the weight ratio of oil to plastics waste as 100:1 1 to 1: 1, as well as the equipment for melting of wastes before their mixing with oil.
  • the goal to be attained in numerous technical solutions with respect to the processes of thermal or catalytic cracking of plastics waste and heavy hydrocarbons feedstock not suitable for processing in other known technological processes is to design the process characterized by effectiveness sufficient to guarantee an economic profitability of the process after its implementation on the industrial scale.
  • the effectiveness of the process depends on efficiency of the main products i.e. petrol fraction and diesel oil fraction as well as on costs incurred for their production.
  • the essential factor reflecting on the level of costs is consumption of energy during the process as well as duration of time, over which the installation is under continuous operation.
  • reaction mixture determines the mixture of melted plastics and/or other processed hydrocarbons feedstock as well as products with a different degree of cracking, which is contained within the process system. This mixture, especially when processing of plastics or other raw-materials with plastics, is characterized by high viscosity and low heat conduction.
  • New technological solutions are being sought for all the time, application of which could result in lowering of consumption of process energy, increase in productivity of petrol fractions and diesel oil fractions as well as in facilitating and simplifying of exploitation services referring to the process in question, running of which is not easy in the industrial practice.
  • the method according to the invention consists in that the cracking process is conducted under the reaction system containing the first reaction zone and the second reaction zone.
  • hydrocarbons feedstock in a liquid state is introduced and - in the case of catalytic process - also a catalyst.
  • this zone the temperature specific for running of a cracking reaction is maintained, and obtained products in a form of vapours are carried away from the upper part of the first reaction zone.
  • the liquid reaction mixture from the lower part of the first zone flows into the mentioned second reaction zone situated near by; the formed liquid-gas mixture is heated when flowing upwards by indirect exchange of heat with the heating medium and then the heated mixture flowing out up above from the mentioned second zone is turned back into the first reaction zone, preferably above the level of the liquid reaction mixture where the reaction mixture flowing in from below is divided in numerous streams flowing upwards.
  • a stream of gas is introduced from below which, along with the reaction mixture, forms a liquid-gas mixture closed in this zone.
  • the products carried away up above from the first zone are submitted to fraction separation.
  • the products of reaction are at first separated into hydrocarbons fraction with the boiling point of up to 350°C and hydrocarbons fraction with the boiling point of over 350°C.
  • the boiling fraction of over 350°C is turned back into the reaction system, preferably to the first reaction zone.
  • the boiling fraction of up to 350°C contains petrol fractions and diesel oil fractions.
  • the system according to the invention designed for processing of hydrocarbons feedstock consists of the tank-type reactor and tubular reactor provided with an inlet for feeding raw-material and catalyst, an outlet for receiving products from the upper part of the reactor and an outlet for receiving impurities from the lower part of the reactor.
  • the tubular reactor situated next to the tank-type reactor is provided with parallel tubes mounted in the casing and directed from below to the top. These tubes along with the lower chamber combining the lower open ends of the above tubes and with the upper chamber combining the upper open ends of the tubes form a separate tubular space, which is connected with the tank-type reactor by means of pipes.
  • One pipe connects the lower part of the tank-type reactor with the lower chamber of the tubular space, whereas the second pipe connects the upper chamber of the tubular space with the tank-type reactor, where the inlet of the mentioned second pipe leading to the tank-type reactor is situated above the mentioned lower part of the said reactor.
  • Each tube of the tubular reactor has a small tube installed on its lower end, with an inlet directed into the tube's inside and in principal - coaxially to the tube's surface; the diameter of the small tube is significantly less than the diameter of the tube. Small tubes are led out from the common collector.
  • the casing of the tubular reactor has accordingly an inlet and an outlet to feed and carry away the heating medium.
  • the tubular reactor in its lowest point of the tubular space may be additionally provided with an outlet for removal of impurities.
  • Combustion gas used as the heating medium may be produced by combustion of fuels in a separate furnace or by combustion in appropriate burners mounted in the casing of the tubular reactor.
  • the application of the method according to the invention makes it possible to unexpectedly efficiently eliminate problems and noxiousness connected with the said process. Thanks to the introduction of gas into the streams of the reaction mixture at the inlet to the tubes of the tubular reactor constituting the second reaction zone and the following formation of the mentioned liquid-gas mixture characterized by the lower mean specific gravity than the weight of reaction mixture flowing in from the first reaction zone, in the second zone the flow rate of the mixture moving upwards is increased and a specific circulation of the reaction mixture is arranged within both zones; respectively also effectiveness of heat reception from the heating medium as well as the effectiveness of heat transfer to the first reaction zone is increased.
  • the reaction system in order to feed the reaction system with the necessary heat volume it is enough to apply the heating medium with moderately high temperatures.
  • reaction mixture in the second reaction zone is usually heated up to the temperature by 2 up to 50°C higher than the temperature maintained within the first reaction zone. It turned out also that a favourable change of the character of flow and heat exchange in the second reaction zone can be reached with a relatively smaller volume of gas introduced into the reaction mixture flowing in from the first reaction zone.
  • the gas applied to form a liquid-gas mixture in the second reaction zone may be the gas being a product of the cracking process or the gas originating from any other source e.g. natural gas, liquefied petroleum gas, vaporized light hydrocarbons including hydrocarbons received in the cracking process or inert gases not containing oxygen.
  • the gas introduced into the reaction mixture does not require any preheating; for example, it can have a temperature equal to the ambient temperature or, in the case of gas received by means of hydrocarbons vaporization, equal to the vaporization temperature.
  • the heating medium in the second reaction zone is combustion gas obtained as a result of combustion in burners using the gas being the product of cracking or combustion of any other fuel originating from outer sources, including also solid fuels.
  • the hot combustion gas in the second reaction zone is passed co currently or counter-currently (preferably counter-currently) in relation to the direction of flow of the liquid-gas mixture.
  • the source of heat fed in the second zone may be also electric energy.
  • the method according to the invention which can be completed with the application of the system according to the invention, is suitable for processing of a wide range of hydrocarbons feedstock: used lubricating oils and lubricants, residues obtained in various technological processes, distillation residues, vegetable fats and animal fats both used and fresh applicable in production of fuels as well as plastics waste, the most difficult mixtures to process.
  • the process according to the invention is suitable for processing mixtures of polymer wastes such as: polyethylene, polypropylene, polybutene, polystyrene.
  • the mixture of wastes submitted to processing may contain some quantity of other plastics such as e.g.
  • ethylene polyterephthalate as well as multi-layer products containing, despite the above mentioned, also other kinds of polymers such as: polyamides or polyesters and these containing layers of glue, paper or layers of thin foil or sprinkled with powder e.g. aluminium.
  • waste preparation e.g. disintegration, washing and drying
  • the way of waste preparation should correspond to the kind of waste and degree of its impurity. All materials which will be not cracked, will fall down to the bottom of the cracking installation and will be removed by means of the appropriate equipment.
  • the process according to the invention envisaging the system for removal of chloride and chloroorganic compounds out of cracking products, may be applied in processing of raw-materials containing chloride such as polyvinyl or any other waste hydrocarbons feedstock containing this element.
  • chloride and chloroorganic compounds any well-known method can be applied.
  • the method and the system according to the invention is also applied in hydrocarbons feedstock processing using the method of the catalytic cracking conducted in the presence of hydrogen.
  • Fig.1 presents schematic technological installation containing the system of hydrocarbons feedstock processing based on the cracking method
  • Fig.2 presents the system of hydrocarbons feedstock processing based on the cracking method.
  • the installation presented in the Fig.1 is applied to conduct processing of plastics waste or other hydrocarbons feedstock of any consistence, both liquid and solid ones, or mixtures of both above mentioned kinds of raw-materials.
  • Raw-materials in a liquid state are introduced into the tank-type reactor 1.
  • Raw-materials, which have been disintegrated and dried and then melted in the electrically heated extruder (shown in the Fig.2) are introduced into the reactor 1 through the inlet 2.
  • Other raw-materials after their melting (where it is required taking into consideration the kind of raw-material submitted to processing) are introduced into the reactor 1 by the inlet 3 .
  • the catalyst is introduced into the reactor together with the raw-material. In the reactor 1 , the temperature of 350-450°C is maintained.
  • the reaction mixture flows in from the lower part of the reactor 1 through the pipe 4 into the tubular reactor 5.
  • the reaction mixture flows in into the reactor 5 from below, into the lower chamber 6a and then flows at the top through the vertical tubes 6 to the reactor.
  • the stream of gas being the product of the process is introduced into the reaction mixture through each tube 6 at its lower end.
  • the gas is introduced by means of small tubes 7 mounted in such a way that their outlets are directed towards the tubes 6 inside and gas is flowing out from them vertically upwards.
  • the inlet ends of the small tubes 7 are connected with the collector 8.
  • the gas and the reaction mixture form the liquid-gas mixture which, when flowing upwards through the tubes 6 , is heated thanks to indirect exchange of heat with combustion gas.
  • the hot combustion gas is obtained by combustion of gas being the product of the process in the furnace 9 .
  • the combustion gas is introduced into the inter-tubular space of the reactor 5 through the pipe 10 and is carried away from the reactor through the pipe 11 .
  • the combustion gas is flowing counter-currently in relation to the direction of flow of the liquid-gas mixture.
  • the heated mixture is received through the pipe 12 from the upper chamber 6b of the tubular reactor 5 and is turned back to the tank-type reactor 1.
  • the products of cracking are received at the top, from the tank-type reactor, and through the pipe 13 are introduced into the column 14 , where they are separated into the first portion containing hydrocarbons boiling at the temperature of up to 350°C and into the second portion - containing hydrocarbons boiling at the temperature of over 350°C.
  • the second portion as mentioned above is turned back into the tank-type reactor (as a whole or a part of it) using the pump 15 and the pipe 16 .
  • the first portion as mentioned above is cooled in the air cooler 17 and through the pipe 18 is introduced into the separator 19 , where liquid products are separated from gas products.
  • the liquid products constituting the main product of the process are the hydrocarbons mixture with the boiling point range corresponding to that of petrol fractions and diesel oil fractions. They are passed to the storage tank 22 through the pump 20 and the pipe 21. These products are next submitted to further processing consisting mainly in separation and hydrogenation (on spot or at the consignee). A part of the liquid product from the separator 19 is passed as a reflux to the column 14 through the pipe 23.
  • the gas products from the separator 19 are suck in and slightly compressed by means of the blower 24 and then, through the pipe 25 , they are introduced into the furnace 9 in order to produce combustion gas whereas through the pipe 26 they are introduced into the tubular reactor 5 in order to produce liquid-gas mixture; through the pipe 27 they are introduced into the column 14 as the stripping gas.
  • Impurities collected at the bottom of the tank-type reactor 1 are removed by means of the equipment 28 . Impurities, which may possibly be collected also at the lowest point of the pipe 4 and/or at the bottom of the chamber 6a, may be removed through the outlets 29 and 30.
EP05460034A 2004-12-06 2005-12-06 Thermisches oder katalytisches Spaltverfahren für Kohlenwasserstoffeinsätze und entsprechendes System Withdrawn EP1707614A1 (de)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PL371564A PL205461B1 (pl) 2004-12-06 2004-12-06 Sposób przetwarzania surowców węglowodorowych metodą termicznego lub katalitycznego krakingu i układ do przetwarzania surowców węglowodorowych metodą termicznego lub katalitycznego krakingu

Publications (1)

Publication Number Publication Date
EP1707614A1 true EP1707614A1 (de) 2006-10-04

Family

ID=36000833

Family Applications (1)

Application Number Title Priority Date Filing Date
EP05460034A Withdrawn EP1707614A1 (de) 2004-12-06 2005-12-06 Thermisches oder katalytisches Spaltverfahren für Kohlenwasserstoffeinsätze und entsprechendes System

Country Status (2)

Country Link
EP (1) EP1707614A1 (de)
PL (1) PL205461B1 (de)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009065271A1 (en) * 2007-11-21 2009-05-28 Global Power And Energy Company Limited Apparatus and process for pyrolysis of scrap tyres and the like
EP2135923A1 (de) * 2008-06-19 2009-12-23 Martin Bajus Die Herstellung von Brennstoffen für Kraftfahrzeuge aus polymeren Materialien
WO2010106399A3 (en) * 2009-03-14 2010-12-23 Clariter Poland Sp. Zo. O. Apparatus for conducting thermolysis of plastic waste and method of thermolysis in continuous manner
US8020499B2 (en) 2007-11-09 2011-09-20 Overseas Capital Assets Limited Apparatus and method for pyrolysis of scrap tyres and the like
US8664458B2 (en) 2010-07-15 2014-03-04 Greenmantra Recycling Technologies Ltd. Method for producing waxes and grease base stocks through catalytic depolymerisation of waste plastics
US10000715B2 (en) 2013-01-17 2018-06-19 Greenmantra Recycling Technologies Ltd. Catalytic depolymerisation of polymeric materials
US10472487B2 (en) 2015-12-30 2019-11-12 Greenmantra Recycling Technologies Ltd. Reactor for continuously treating polymeric material
US10597507B2 (en) 2016-02-13 2020-03-24 Greenmantra Recycling Technologies Ltd. Polymer-modified asphalt with wax additive
US10723858B2 (en) 2018-09-18 2020-07-28 Greenmantra Recycling Technologies Ltd. Method for purification of depolymerized polymers using supercritical fluid extraction
US10870739B2 (en) 2016-03-24 2020-12-22 Greenmantra Recycling Technologies Ltd. Wax as a melt flow modifier and processing aid for polymers
US11072676B2 (en) 2016-09-29 2021-07-27 Greenmantra Recycling Technologies Ltd. Reactor for treating polystyrene material
CN114460057A (zh) * 2022-02-23 2022-05-10 宋东芹 一种便携式硫氯氮元素一体测定仪

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
PL218782B1 (pl) 2009-04-08 2015-01-30 Bl Lab Spółka Z Ograniczoną Odpowiedzialnością Układ do termolizy odpadowych tworzyw sztucznych i sposób termolizy odpadowych tworzyw sztucznych

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3108048A (en) * 1960-09-12 1963-10-22 Universal Oil Prod Co Apparatus for contacting of different density fluids
DE4112977A1 (de) * 1991-04-20 1992-10-22 Gfk Kohleverfluessigung Gmbh Verfahren zur hydrierung von kohlenstoffhaltigen abfaellen
FR2675499A1 (fr) * 1991-04-17 1992-10-23 Inst Francais Du Petrole Procede et dispositif de vapocraquage d'une charge hydrocarbonee comportant un generateur a gaz et un reacteur echangeur de chaleur.
DE10049377A1 (de) * 2000-10-05 2002-04-18 Evk Dr Oberlaender Gmbh & Co K Katalytische Erzeugung von Dieselöl und Benzinen aus kohlenwasserstoffhaltigen Abfällen und Ölen

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3108048A (en) * 1960-09-12 1963-10-22 Universal Oil Prod Co Apparatus for contacting of different density fluids
FR2675499A1 (fr) * 1991-04-17 1992-10-23 Inst Francais Du Petrole Procede et dispositif de vapocraquage d'une charge hydrocarbonee comportant un generateur a gaz et un reacteur echangeur de chaleur.
DE4112977A1 (de) * 1991-04-20 1992-10-22 Gfk Kohleverfluessigung Gmbh Verfahren zur hydrierung von kohlenstoffhaltigen abfaellen
DE10049377A1 (de) * 2000-10-05 2002-04-18 Evk Dr Oberlaender Gmbh & Co K Katalytische Erzeugung von Dieselöl und Benzinen aus kohlenwasserstoffhaltigen Abfällen und Ölen

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8020499B2 (en) 2007-11-09 2011-09-20 Overseas Capital Assets Limited Apparatus and method for pyrolysis of scrap tyres and the like
WO2009065271A1 (en) * 2007-11-21 2009-05-28 Global Power And Energy Company Limited Apparatus and process for pyrolysis of scrap tyres and the like
EP2135923A1 (de) * 2008-06-19 2009-12-23 Martin Bajus Die Herstellung von Brennstoffen für Kraftfahrzeuge aus polymeren Materialien
WO2010106399A3 (en) * 2009-03-14 2010-12-23 Clariter Poland Sp. Zo. O. Apparatus for conducting thermolysis of plastic waste and method of thermolysis in continuous manner
US8680349B2 (en) 2009-03-14 2014-03-25 Clariter Ip S.A. Apparatus for conducting thermolysis of plastic waste in a continuous manner
US9376632B2 (en) 2009-03-14 2016-06-28 Clariter Ip S.A. Apparatus for conducting thermolysis of plastic waste and method of thermolysis in continuous manner
US8664458B2 (en) 2010-07-15 2014-03-04 Greenmantra Recycling Technologies Ltd. Method for producing waxes and grease base stocks through catalytic depolymerisation of waste plastics
US10457886B2 (en) 2013-01-17 2019-10-29 Greenmantra Recycling Technologies Ltd. Catalytic depolymerisation of polymeric materials
US10000715B2 (en) 2013-01-17 2018-06-19 Greenmantra Recycling Technologies Ltd. Catalytic depolymerisation of polymeric materials
US10472487B2 (en) 2015-12-30 2019-11-12 Greenmantra Recycling Technologies Ltd. Reactor for continuously treating polymeric material
US11072693B2 (en) 2015-12-30 2021-07-27 Greenmantra Recycling Technologies Ltd. Reactor for continuously treating polymeric material
US11739191B2 (en) 2015-12-30 2023-08-29 Greenmantra Recycling Technologies Ltd. Reactor for continuously treating polymeric material
US10597507B2 (en) 2016-02-13 2020-03-24 Greenmantra Recycling Technologies Ltd. Polymer-modified asphalt with wax additive
US11279811B2 (en) 2016-02-13 2022-03-22 Greenmantra Recycling Technologies Ltd. Polymer-modified asphalt with wax additive
US10870739B2 (en) 2016-03-24 2020-12-22 Greenmantra Recycling Technologies Ltd. Wax as a melt flow modifier and processing aid for polymers
US11072676B2 (en) 2016-09-29 2021-07-27 Greenmantra Recycling Technologies Ltd. Reactor for treating polystyrene material
US11859036B2 (en) 2016-09-29 2024-01-02 Greenmantra Recycling Technologies Ltd. Reactor for treating polystyrene material
US10723858B2 (en) 2018-09-18 2020-07-28 Greenmantra Recycling Technologies Ltd. Method for purification of depolymerized polymers using supercritical fluid extraction
CN114460057A (zh) * 2022-02-23 2022-05-10 宋东芹 一种便携式硫氯氮元素一体测定仪

Also Published As

Publication number Publication date
PL205461B1 (pl) 2010-04-30
PL371564A1 (pl) 2006-06-12

Similar Documents

Publication Publication Date Title
EP1707614A1 (de) Thermisches oder katalytisches Spaltverfahren für Kohlenwasserstoffeinsätze und entsprechendes System
CN105219406B (zh) 一种设备和用于转化含烃材料的方法
US7847136B2 (en) Device and method for recovering fractional hydrocarbons from recycled plastic fractions and/or oily residues
CN1247743C (zh) 由废塑料连续地制备汽油、煤油和柴油的方法和***
KR101280875B1 (ko) 로터리 킬른 타입의 고분자 폐기물 유화장치
CN104105781A (zh) 用于转化聚合物废物的区域-划定的热解设备
JP2007529574A (ja) 廃材を液体燃料に転換するための方法及びプラント
US20220204861A1 (en) Process for pvc-containing mixed plastic waste pyrolysis in a reactor handling three phases of products
CN101223261A (zh) 烃热解排出物的加工方法
CN1392224A (zh) 废塑料炼油工艺及设备
EP2432853A2 (de) Vorrichtung und verfahren zur kontinuierlichen thermolyse von kunststoffabfall
EP3946667B1 (de) Verfahren zur verarbeitung von pyrolysegas aus kunststoffabfällen
WO2022130052A1 (en) Process for depolymerization of solid mixed plastic
WO2013119187A2 (en) Method for thermal decomposition of organic material and equipment for implementation of this method
CN102268287B (zh) 一种高酸原料油深度脱酸的延迟焦化方法
US20200331169A1 (en) Heat and Energy Integrated Continuous Process for Plastic Waste Recovery
KR100517898B1 (ko) 폐합성수지를 원료로 하는 촉매 하행식 크래킹반응기 및 이를 이용한 휘발유·경유의 제조방법
EP2792729A1 (de) Verfahren zur Wasserverarbeitung einer Flüssigkeitszufuhr mit Kohlenwasserstoffen in Kraftstoffkomponenten
CN102268289B (zh) 一种含酸原料油的延迟焦化方法
WO2013036151A2 (en) Method for the manufacture of liquid hydrocarbons and plant for the manufacture of liquid hydrocarbons
RU2804969C1 (ru) Способ получения жидких углеводородов из отходов термопластов и устройство для его осуществления
RU2701860C1 (ru) Способ пиролиза жидких и газообразных углеводородов и устройство для его осуществления
NL2033250B1 (en) Method of heating plastics for the production of oil
US20230332051A1 (en) Integrated mixed plastic pyrolysis with heavy oil product thermal cracking
CN102268288A (zh) 一种高酸原料油深度脱酸的延迟焦化工艺

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): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR

AX Request for extension of the european patent

Extension state: AL BA HR MK YU

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

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

17P Request for examination filed

Effective date: 20070404

18W Application withdrawn

Effective date: 20070427

AKX Designation fees paid

Designated state(s): AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LI LT LU LV MC NL PL PT RO SE SI SK TR