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WO2024256366A1 - Appareil d'hydrocraquage de plastiques pour procédé en continu et son utilisation - Google Patents

Appareil d'hydrocraquage de plastiques pour procédé en continu et son utilisation Download PDF

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Publication number
WO2024256366A1
WO2024256366A1 PCT/EP2024/066022 EP2024066022W WO2024256366A1 WO 2024256366 A1 WO2024256366 A1 WO 2024256366A1 EP 2024066022 W EP2024066022 W EP 2024066022W WO 2024256366 A1 WO2024256366 A1 WO 2024256366A1
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
melting element
plastic
outlet
melting
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.)
Pending
Application number
PCT/EP2024/066022
Other languages
English (en)
Inventor
Felix Daniel BOBBINK
Antoine VAN MUYDEN
Christopher Marc HUNSTON
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.)
Plastogaz Sa
Original Assignee
Plastogaz Sa
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 Plastogaz Sa filed Critical Plastogaz Sa
Priority to CN202480035938.9A priority Critical patent/CN121219386A/zh
Publication of WO2024256366A1 publication Critical patent/WO2024256366A1/fr
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

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
    • 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
    • C10G1/10—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
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • C10G47/16—Crystalline alumino-silicate carriers
    • C10G47/18—Crystalline alumino-silicate carriers the catalyst containing platinum group metals or compounds thereof
    • 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
    • C10G47/36—Controlling or regulating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00162—Controlling or regulating processes controlling the pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00193—Sensing a parameter
    • B01J2219/00195—Sensing a parameter of the reaction system
    • B01J2219/00198—Sensing a parameter of the reaction system at the reactor inlet
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00193—Sensing a parameter
    • B01J2219/00195—Sensing a parameter of the reaction system
    • B01J2219/002—Sensing a parameter of the reaction system inside the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00211—Control algorithm comparing a sensed parameter with a pre-set value
    • B01J2219/00213—Fixed parameter value
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00222—Control algorithm taking actions
    • B01J2219/00227—Control algorithm taking actions modifying the operating conditions
    • B01J2219/00229—Control algorithm taking actions modifying the operating conditions of the reaction system
    • B01J2219/00231—Control algorithm taking actions modifying the operating conditions of the reaction system at the reactor inlet
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/12—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only

Definitions

  • a transfer element (2) is provided in fluid connection with the outlet of the melting element (1 ) and in fluid connection with the inlet of reactor (3) and comprises at least one first switching valve (22) adapted to either convey the molten plastic feedstock to the inlet of reactor (3) or to a tank (8);
  • the pressure at the outlet of the melting element (1 ) is higher than the pressure at the inlet of the melting element (1 );
  • the reactor (3) is provided with a pressure sensor adapted for sensing the pressure inside the reaction chamber of reactor (3) and for automatically controlling
  • the at least one first switching valve (22) such as to convey the flow of molten plastic feedstock towards the tank (8) when the pressure in the reaction chamber of reactor (3) exceeds a predetermined level;
  • FIG.1 Schematic representation of an example of a plastic hydrocracking apparatus according to the invention.
  • FIG.2 Graph showing the evolution of the feed rate and the pressure difference over time during the safety assessment of Example 1 .
  • hydrocracking refers to reacting a hydrocarbon substance with hydrogen over a bifunctional catalyst having both an acidic site (performing a cracking reaction) and a redox site (able to perform a hydrogenation/dehydrogenation and/or a hydrogenolysis reaction). Considering that different quantities of these active sites on the catalyst can be present and that activity of such sites differs depending on the applied conditions, the reaction involved is either catalytic cracking, hydrogenolysis or hydrogenation. Therefore, the present invention encompasses an apparatus and a process for continuous hydrocracking, hydrogenolysis and/or hydrogenation of plastic. [0020] The invention relates to a continuous plastic hydrocracking apparatus having improved safety. Continuous processes are by nature associated with higher risks than batch processes.
  • the present invention advantageously provides an apparatus provided with means for cross-control of the different parts of the apparatus, enabling key parts of the production line to regulate the flux of the feedstock, thus making it possible to regulate precisely the pressures at every key point of the production line (apparatus).
  • any type of plastic can be continuously processed in the plastic hydrocracking apparatus of the present invention, including single plastic sources or mixed plastic sources, such as mixed waste plastics.
  • suitable plastics polymers that can be used as starting material in the continuous hydrocracking process include polyolefins, ethylene vinyl alcohol (EVOH), poly lactic acid (PLA), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polytrimethylene terephthalate (PTT), polyethylene isosorbide terephthalate (PEIT), polyethylene furanoate (PEF), polyamide (PA), polyamide-6 or Poly(e-caprolactam) or polycaproamide (PA6), polyamide-6, 6 or Poly(hexamethylene adipamide) (PA6,6), Poly(l I- aminoundecanoamide) (PA11 ), polydodecanolactam (PA 12), poly(tetramethylene adipamide) (PA4,6), poly(pentamethylene sebacamide) (
  • the polyolefin is selected from the group consisting of polyethylene, polypropylene, polymethylpentene, polybutene-1 , polyisobutylene, ethylene propylene rubber, ethylene propylene diene monomer rubber, polystyrene polyvinylchloride and polyvinylidene chloride.
  • the plastic feedstock is preferably heated enough to be at least partially molten when it leaves the melting element (1 ) through the melting element (1 ) outlet. Since the plastic feedstock is composed of different materials, part of the plastic feedstock can remain in the solid state within the molten plastic feedstock, thus forming a viscous paste (slurry).
  • the melting element (1 ) possesses one or more addition port(s) (11) adapted to add substances to the melting element (1 ) and/or one or more extraction port(s) (12) adapted to extract substances from the melting element (1 ).
  • the substances that can be added to or extracted from the melting element (1) are solids, such as catalysts, liquids, such as water, and gases, such as hydrogen, air or steam, or slurries.
  • Preferred materials that can be added to the melting element (1 ) through one or more addition port(s) (11 ) include hydrogen, water, steam, a catalyst or materials originating from the reactor element (3), such as unreacted or partially reacted materials.
  • the pressure at the outlet of the melting element (1 ) is higher than the pressure at the inlet of the melting element (1 ). This is for example achieved when the melting element (1 ) comprises a screw that compresses the plastic feedstock towards the end of the screw element, at the outlet of the melting element (1 ).
  • the melting element (1 ) comprises one or more pressure sensor(s) adapted to increase the flow of the plastic feedstock from the inlet of the melting element (1 ) to the outlet of the melting element (1 ) when the pressure at the outlet of the melting element (1) drops below a predetermined level and/or one or more pressure sensor(s) adapted to decrease the flow of the plastic feedstock from the inlet of the melting element (1 ) to the outlet of the melting element (1 ) when the pressure at the outlet of the melting element (1 ) exceeds a predetermined level.
  • the reactor (3) is preferably provided with at least one means for controlling the temperature inside the reactor, preferably at least one heating means and/or at least one cooling means.
  • the temperature and the pressure in the reactor are adequate to perform the hydrocracking of the plastic feedstock.
  • the liquid level sensor of the reactor element (3) is advantageously adapted to control the means for conveying the plastic feedstock from the inlet of the melting element (1 ) to the outlet of the melting element (1 ) to reduce or stop the conveying of molten plastic feedstock from the melting element (1 ) to the reactor (3) and/or to control the second switching valve (21) to redirect the flow of plastic feedstock to the tank (8) when the level of the reaction mixture inside the reaction chamber exceeds a predetermined level.
  • the level sensor is also advantageous to monitor the progress of the hydrocracking reaction. This cannot be achieved by the pressure sensor.
  • the beneficial role of the level sensor is due to the fact that various indicators of the reaction progress can be detected by a level sensor and not by a pressure sensor. Firstly, the level sensor can detect volume increase due the amount of hydrogen being sparged within the melt ( ⁇ 40% difference). In addition, it can provide a direct measure of the rate at which the plastic inside the reactor is consumed. Furthermore, the monitoring of the reaction progress by the level sensor is not affected by the density of the mixture, which is unknown and evolves over time. Therefore, operation of a continuous hydrocracking line is improved when the level sensor is present in addition to the pressure sensor.
  • Hydrocracking of the plastic feedstock refers to the reaction between the said plastic feedstock, hydrogen, and a catalyst.
  • the overall combination of the apparatus and catalyst makes it possible to control product composition ranging from C1 to C24 products, such as any hydrocarbon from methane to naphtha, including LPG and aromatics. Reaction conditions and catalyst composition can be adapted to obtain the desired products.
  • the following preferred embodiments provide a preferred set-up for the purification of light hydrocarbon products, preferably of hydrocarbon products having 1 to 16 carbon atoms.
  • the solid and liquid outlet (42) can be in fluid connection to one addition port (11 ) of the melting element (1 ), to a liquid injection element (32), to a solid addition port (33) and/or to a storage tank.
  • the solids and liquids outlet (42) is in fluid connection to one addition port (11 ) of the melting element (1 ) and/or to a liquid injection element (32) of the reactor element (3). This is advantageous when the intended products are gases, as the solids and liquids can be re-introduced into the system for further reaction.
  • the condenser element (5) has a gas inlet in fluid connection to the gas outlet element (4). Such gas inlet enables expansion of the gas and separation of gas and liquid products.
  • the condenser element (5) comprises an inner structure adapted to facilitate the condensation of liquid products.
  • the condenser element (5) preferably has a liquid outlet (52) located at the bottom and a gas outlet (51 ) located towards the top of the condenser element (5).
  • the liquid products extracted from the condenser element (5) through the liquid outlet (52) are then preferably directed towards a degassing element (6) or a storage tank (b) and the gas products extracted from the condenser element (5) through the gas outlet (51) are preferably directed towards a gas burner element (9) or towards a gas addition port (35) of the reactor element (3), so that such products can be further reacted.
  • the apparatus of the invention further comprises one or more degassing element(s) (6) comprising a liquid inlet in fluid connection to the liquid outlet (52) of the condenser element (5).
  • the liquid inlet of the degassing element (6) is adapted to enable extraction of the dissolved gases from the liquids originating from the condenser element (5).
  • the degassing element (6) is adapted to depressurize and cool the liquid products originating from the condenser element (5).
  • the degassing element (6) is adapted to degas hydrocarbons with less than five carbon atoms (in the gas state) from larger hydrocarbon products (which remain in the liquid state).
  • the degassing element (6) is preferably provided with one or more liquid outlet(s) (62) located towards the bottom of the degassing element (6) and/or with one or more gas outlet (61 ) located towards the top of the degassing element (6).
  • the degassing element (6) comprises one or more structured element(s) adapted to prevent the liquid product from escaping the degassing element (6) via the gas outlet (61 ).
  • the liquid products extracted from the degassing element (6) via the liquid outlet (62) are pumped towards a storage tank (b) or to a liquid/liquid separation element (7).
  • the gas products extracted from the degassing element (6) via the liquid outlet (61 ) are preferably directed towards a compressing unit (10).
  • the apparatus of the present invention comprises a liquid/liquid separating element (7) in fluid connection to the liquid outlet (62) of the degassing element (6) or to the liquid outlet (52) of the condenser element (5), preferably in fluid connection to the liquid outlet (62) of the degassing element (6).
  • the liquid/liquid separating element (7) is adapted to separate the lighter liquid hydrocarbon products from the heavier hydrocarbon products and the aqueous phase.
  • the liquid/liquid separating element (7) preferably comprises a lighter hydrocarbon outlet (71 ) located at the top of the liquid/liquid separation element (7) and a heavier hydrocarbon outlet (72) located at the bottom of the liquid/liquid separation element (7).
  • the reactor (3) was equipped with a liquid level sensor by means of a multipoint thermocouple. Other means of measuring the level such as radio waves or sonar detection can also be used. However, a differential pressure detector cannot be used as a liquid level sensor, because the density of the mixture is not known at any point in time, hence the reading would not match the volume of the reactor.
  • a level switch was installed at the top of the reactor (3) to stop the incoming flow of plastic once the reaction medium touches the switch.
  • the first switching valve (21 ) was set to direct the polymer towards the tank (8) as soon as a differential pressure lower than 5 bar between the pressure sensor at the outlet of the melting element (1 ) and the pressure sensor inside the reactor (3) was detected.
  • a level sensor was set to switch the first switching valve (21 ) towards the tank (8) to prevent overfilling the reactor upon reaching a particular level.
  • the first switching valve (21 ) was set to direct the melt into the tank (8).
  • the first switching valve (21 ) was adjusted manually to set the pressure above the reactor pressure (Ap ⁇ 10-20 bar).
  • the first switching valve (21 ) was switched to feed the plastic into the reactor (3). The continuous feeding was maintained until the reaction was stopped, or one of the safety mechanisms was triggered; either by a decrease in melt pressure at the outlet of the melting element (1 ), or by the multipoint thermocouple indicating that the maximum level was reached, or by the level sensor switch being in contact with the reactive medium.
  • the extruder barrel temperatures in the melting element (1 ) were set in the range 200-240°C.
  • the set rotating speed of the screws was adjusted based on the dosing rate of the plastic from the gravimetric dosing unit. For instance, the rotating speed was set to 600 rpm.
  • the vacuum port pressure was set to 600 mbar.
  • plastic foils i. where used, residue-emptied, system compatible items made of plastic foil, area > DIN A4 such as bags, carrier bags and shrink films, incl. secondary components such as closures, labels, etc, ii. where the purity is higher or equal to 92.0 wt%, iii.
  • the maximum total of impurities is less or equal to 8.0 wt% where the impurities are describes as Glass, PCC composites (e.g. liquid, cartons), foreign materials (e.g. rubber, stones, wood, textiles, diapers), compostable waste (e.g. food, garden waste), paper, cardboard and carton are less or equal to 1 .0 wt%, iv. where other impurities are less or equal than 4.0 wt%, here other plastic items are less or equal to 4.0 wt%, v. where the colorless transparent foils greater than DIN A3 are higher or equal to 42.0 wt%, and vi. where the following substances are excluded metallic or mineral impurities with a unit weight is higher than 100 g..

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  • 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)
  • Crystallography & Structural Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)

Abstract

La présente invention concerne le domaine de l'hydrocraquage de plastiques et concerne en particulier un appareil qui peut être utilisé pour la production continue de produits hydrocarbonés, tels que des hydrocarbures liquides et gazeux, ou une charge d'alimentation pour des vapocraqueurs, par exemple des alcanes, à partir de plastique et en particulier de plastique mixte, par exemple de déchets plastiques. L'appareil de la présente invention est caractérisé par une sécurité améliorée relativement à la mise en oeuvre du processus d'hydrocraquage d'une manière continue.
PCT/EP2024/066022 2023-06-12 2024-06-11 Appareil d'hydrocraquage de plastiques pour procédé en continu et son utilisation Pending WO2024256366A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202480035938.9A CN121219386A (zh) 2023-06-12 2024-06-11 用于连续式加工的塑料氢化裂解装置及其用途

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
EP23178602 2023-06-12
EP23178602.1 2023-06-12
EP24153255.5 2024-01-22
EP24153255 2024-01-22

Publications (1)

Publication Number Publication Date
WO2024256366A1 true WO2024256366A1 (fr) 2024-12-19

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ID=91539820

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2024/066022 Pending WO2024256366A1 (fr) 2023-06-12 2024-06-11 Appareil d'hydrocraquage de plastiques pour procédé en continu et son utilisation

Country Status (2)

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CN (1) CN121219386A (fr)
WO (1) WO2024256366A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012076890A1 (fr) 2010-12-08 2012-06-14 The University Of Manchester Procédé de recyclage des matières plastiques
US20180282648A1 (en) 2013-01-17 2018-10-04 Greenmantra Recycling Technologies Ltd. Catalytic Depolymerisation of Polymeric Materials
US20180346683A1 (en) 2016-02-13 2018-12-06 Greenmantra Recycling Technologies Ltd. Polymer-Modified Asphalt With Wax Additive
WO2020104385A1 (fr) 2018-11-19 2020-05-28 Ecole Polytechnique Federale De Lausanne (Epfl) Conversion directe de matières plastiques en méthane et/ou en combustibles liquides
DE102021105810A1 (de) 2021-03-10 2022-09-15 Kurt Reschner Verfahren und Anlage zur Depolymerisation von Kunststoffmaterial

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012076890A1 (fr) 2010-12-08 2012-06-14 The University Of Manchester Procédé de recyclage des matières plastiques
EP2649121A1 (fr) * 2010-12-08 2013-10-16 The University Of Manchester Procédé de recyclage des matières plastiques
US20180282648A1 (en) 2013-01-17 2018-10-04 Greenmantra Recycling Technologies Ltd. Catalytic Depolymerisation of Polymeric Materials
US20180346683A1 (en) 2016-02-13 2018-12-06 Greenmantra Recycling Technologies Ltd. Polymer-Modified Asphalt With Wax Additive
WO2020104385A1 (fr) 2018-11-19 2020-05-28 Ecole Polytechnique Federale De Lausanne (Epfl) Conversion directe de matières plastiques en méthane et/ou en combustibles liquides
DE102021105810A1 (de) 2021-03-10 2022-09-15 Kurt Reschner Verfahren und Anlage zur Depolymerisation von Kunststoffmaterial

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