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WO2023111604A1 - Processus et appareil de conversion de matières à base d'hydrocarbures, de matières plastiques et de déchets plastiques - Google Patents

Processus et appareil de conversion de matières à base d'hydrocarbures, de matières plastiques et de déchets plastiques Download PDF

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Publication number
WO2023111604A1
WO2023111604A1 PCT/HU2022/050087 HU2022050087W WO2023111604A1 WO 2023111604 A1 WO2023111604 A1 WO 2023111604A1 HU 2022050087 W HU2022050087 W HU 2022050087W WO 2023111604 A1 WO2023111604 A1 WO 2023111604A1
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Prior art keywords
reactor
process gas
gas
plastics
plastic waste
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Ceased
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PCT/HU2022/050087
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English (en)
Inventor
Eszter KELEMEN-CSERTA
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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
    • C10G1/10—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
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B51/00—Destructive distillation of solid carbonaceous materials by combined direct and indirect heating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • 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
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • 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
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/03—Pressure vessels, or vacuum vessels, having closure members or seals specially adapted therefor
    • 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
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/04—Pressure vessels, e.g. autoclaves
    • B01J3/048—Multiwall, strip or filament wound vessels
    • 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
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/008—Pyrolysis reactions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B1/00—Retorts
    • C10B1/02—Stationary retorts
    • C10B1/04—Vertical retorts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/12—Applying additives during coking
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/16—Features of high-temperature carbonising processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • 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
    • B01J2219/00051—Controlling the temperature
    • B01J2219/0015—Controlling the temperature by thermal insulation means
    • B01J2219/00153—Vacuum spaces
    • 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
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics

Definitions

  • the invention relates to a process and apparatus for conversion materials of hydrocarbon origin, plastics, and plastic waste.
  • the process comprises the steps of storing, sorting, and crushing the plastics and plastic waste, and feeding them into a reactor.
  • the apparatus comprises a storage unit, a sorting unit, a feed unit, and a reactor.
  • the pyrolysis of materials of hydrocarbon origin and plastic waste is a type of thermal technologies that is suited for conversion these materials into products with properties that are considered favourable in some respects, or into energy.
  • Thermal treatment technologies can be classified into the following groups: low-temperature pyrolysis, low -temperature gasification, pyrolytic gasification, conventional incineration, high-temperature gasification, plasma technology.
  • Siemens process (a combination of pyrolysis and high-temperature incineration).
  • Noel’s conversion process thermal digestion of the waste is performed in an indirectly heated rotary-drum reactor, and then - after grinding the residual coke - the waste is passed on to the flow-type gasification reactor where partial oxidation is applied for energy recovery).
  • the above cited processes have the common feature that at some operational stage all of them include a pyrolysis phase operating at an excess air coefficient of X ).
  • the above referenced pyrolytic processes also have it in common that the generated flue gases come into contact with the process gas, i.e., they are mixed. Translated to heating technology terms this means that the excess air coefficient X T). Because the composition of the waste entering the process is not known in advance, the combustion/oxidation processes are impossible to control in an optimal manner. It is especially dangerous if the composition of additional materials (additives) contained by the plastic waste is not known.
  • a multiple-hearth furnace for the incineration of sewage sludge filter-cake adapted to carry out such a pyrolytic process is disclosed in the patent description EP 0577759B 1.
  • heat introduction is implemented by the oxygen-poor combustion of the gas, which means that the flue gas is mixed with the process gas.
  • the known processes do not provide a solution to the problem of simultaneously providing, in the same reactor space, the temperature required for the combustion of the process gas and fulfilling the temperature requirements of the process of conversion hydrocarbon derivatives. For example, let the temperature of the decomposition/transformation process be 300 °C, while the optimal temperature for the combustion of the process gas is 820-850 °C, at an incubation time of 2-3 s. It is impossible (not feasible) to simultaneously fulfil both conditions inside conventional reactors.
  • the objective of the invention is to eliminate the drawbacks of the technical solutions cited above and provide a process for conversion plastics of hydrocarbon origin and plastic waste into light oil, heavy oil, paraffin-type hydrocarbons, solid carbon-containing powder, and hydrocarbon-containing gas.
  • Our invention therefore relates to a process for conversion materials of hydrocarbon origin, plastics, and plastic waste, the process comprising the steps of storing, sorting, and crushing the plastics and plastic waste, and feeding them into a reactor.
  • the process is characterised by heating the starting material in a reactor to a temperature in the temperature range of 300- 1200°C predetermined depending on the starting material and the final product.
  • the cooled-down process gas is carried away from the reactor, and process gas heated up in a separate space is mixed to it in a controlled manner.
  • the material is directed downwards from the top, causing the material to decompose during the process.
  • the end products of the decomposition process which can be light oil, heavy oil, paraffin-type hydrocarbons, process gases, and carbon-containing powders, are discharged from the reactor.
  • Our invention further relates to an apparatus for conversion materials of hydrocarbon origin, plastics, and plastic waste, the apparatus comprising a storage unit, a sorting unit, a feed unit, and a reactor.
  • the invention is characterised in that the casing of the reactor is constituted by the dual-wall vacuum-insulated top portion and the dual-wall vacuum-insulated bottom portion of a bell furnace, the reactor body being constituted by portions of a multi-tray, multizone multiple hearth furnace that have no casing.
  • a respective separately controllable high-temperature circulation fan is connected to each zone, the circulation fans being connected to a condenser and also to dampers/mixing valves. Furthermore, the dampers/mixing valves are in connection with an energy centre.
  • a carbon discharge stub adapted for carrying away the carbon-containing powder is arranged at the bottom of the bell furnace.
  • Fig. 1 is the schematic flow diagram of the process according to the invention
  • Fig. 2 is a schematic depiction of the components of the apparatus according to the invention
  • Fig. 3 shows a cross-sectional view of the reactor body arranged in a bell furnace
  • Fig. 4 illustrates, in a half-section view, the configuration of the bell furnace.
  • step 2 the materials of hydrocarbon origin, plastics and plastic waste are stored and prepared.
  • step 2 the already homogenous-composition waste is collected in storage bins.
  • the plastic waste is crushed to a given size.
  • step 3 the prepared plastic waste is compacted and is introduced into the reactor 4 at high pressure.
  • the material is heated to a temperature in the temperature range of 300-1200°C predetermined depending on the feedstock and the final product. The temperature is determined depending on the feedstock to be transformed, and on the desired ratio of gas, light and heavy oil to be obtained.
  • the cooled-down process gas is carried away from the reactor 4, with process gas heated up in a separate space being mixed to it in a controlled manner.
  • the separate space is an energy centre 7, wherein, after cleaning the process gas, a portion of the cleaned process gas is combusted, the generated heat being utilised for heating - by means of the heat exchanger of the energy centre 7 - a portion of the process gas coming from the reactor 4.
  • the heated process gas is mixed in a controlled manner with the other portion of the process gas - coming from the direction of the reactor 4 and having lower temperature. The mixing is performed applying dampers/mixing valves 6.1, 6.2, 6.3, and thereafter the heated process gas is reintroduced into the interior space of the reactor 4.
  • the material In the reactor 4, the material is directed downwards from the top, causing the material to decompose during the process.
  • the end product of the decomposition process which can be light oil, heavy oil, paraffin-type hydrocarbons, process gases, and carbon-containing powder, is discharged from the reactor 4.
  • the excess process gas generated in the reactor is passed on to a condenser 8, wherein the gas is separated into fractions while being cooled down.
  • the light condensate oil 8.1 and the heavy condensate oil 8.2 are introduced, respectively, into a light oil container and a heavy oil container that are not shown in the drawings, carrying off the paraffin-type condensates through a condensate storage tank (not shown in the drawing) and then, via a condensate/water separator 8.3, spraying them into the process gas.
  • the dampers/mixing valves 6.1, 6.2, 6.3 that can be seen in Fig. 2 are applied for mixing the hot gas (having a temperature of 700-750 °C) coming from the direction of the energy centre 7 to a portion of the cooled-off process gas coming from the reactor 4 in such a manner that the resulting temperature of the gas is 600 °C.
  • water fed to the reactor 4 by a water pump 16 leaves the heat exchangers 9 as water vapour and is fed into the reactor 4 along a water vapour feed path 14, with the transformation process taking place in the reactor 4 in its presence.
  • a pressure of 10’ 3 bar is provided between the dual walls of the bell furnace and is continuously monitored applying a pressure sensor.
  • the decomposition process is halted, and the reactor space is deluged with CO2 gas.
  • the essential component of the apparatus adapted for carrying out the process is the modified multiple-hearth furnace, which has been modified to enable it to perform tasks related to conversion plastic waste.
  • the apparatus is known in the English-, German-, and Hungarian- language literature of the field as “Multiple-Hearth Furnace”, “Mehretagenofen”, and “Tobbszintu pbrkblokemence”, respectively.
  • the furnace modified in such a manner will hereinafter be called a reactor 4.
  • the reactor body 4.3 which differs from the multi-tray multiple-hearth furnaces in that it does not have the casing and heating system of the latter.
  • the casing of the reactor 4 is constituted by the dual-wall, vacuum-insulated top portion 4.1 and the dual-wall, vacuum- insulated bottom portion 4.2 of a bell furnace.
  • the pressure between the dual walls of the bell furnace is 10’ 3 bar, with the inside surface of the external wall facing the vacuum space being covered by thermal-insulating ceramic fibre material, with a heat-reflective layer being disposed on the layer’s surface.
  • the top portion 4.1 of the bell furnace is lifted and lowered by a lifting machine.
  • the reactor body 4.3 depicted in Fig. 3 has a “self-supporting” design.
  • the force ensuring gas-tightness between the top portion 4.1 and the bottom portion 4.2 of the bell furnace is provided by the own weight of the bell furnace.
  • the top portion 4.1 of the bell furnace comprises refractory masonry 4.1.1.
  • a water seal that is 4.22 depicted in Fig. 4 and is adapted for improving the gas-tightness and safety of the furnace space is disposed along the bottom edge of the bell furnace.
  • the dual-wall medium-pressure vacuum space is adapted to provide thermal insulation but also plays a safety role. It performs its safety function such that in the event that the vacuum is lost it immediately indicates that the surface of the bell furnace has been damaged. If the vacuum is lost, a pressure sensor triggers an alarm and immediately stops the process.
  • the multilevel, multi-tray core of the reactor body 4.3 depicted in Fig. 3 consists of a plurality of zones. Each zone consists of two trays, with hot gas arriving to the upper tray of each zone, and with the cooled-off process gas leaving the particular zone near the tray situated underneath it. The number of zones is determined in the design phase based on technological requirements.
  • Fig. 3 there can be observed how the process gas 4.3.1 is introduced into the first zone and how the process gas 4.3.4 is exhausted therefrom; how the process gas 4.3.2 is introduced into the second zone and how the process gas 4.3.5 is exhausted therefrom; and also, how the process gas 4.3.3 is introduced into the third zone and how the process gas 4.3.6 is exhausted therefrom.
  • the carbon-containing residues of the transformed hydrocarbon derivatives are carried off into a residual carbon storage tank 11 (shown in Fig. 2) through a carbon discharge stub 4.21 that can be seen in Fig. 4.
  • a respective separately controllable high-temperature circulation fan 5.1, 5.2, 5.3 is connected to each zone of the reactor 4.
  • the circulation fans 5.1, 5.2, 5.3 are connected to a condenser 8 and also to dampers/mixing valves 6.1, 6.2, 6.3 that can be seen in Fig. 2, said dampers/mixing valves 6.1, 6.2, 6.3 further being in connection with an energy centre 7 that can be seen in Fig. 2.
  • the dampers/mixing valves 6.1, 6.2, 6.3 are adapted for mixing the cooled-down process gas coming from the direction of the reactor 4 and the hot process gas coming from the direction of the energy centre 7.
  • the task of heating the process gas is performed by an external energy centre 7, with the heated process gas supplying the required energy to the reactor 4 that is in indirect connection with the flue gas.
  • the dampers/mixing valves 6.1, 6.2, 6.3 disposed upstream of each input level are applied for mixing the heated process gas to the cooled-off gas coming from the reactor 4 space in a controlled manner, such that the required temperature can be provided at the points of introduction of the process gas 4.3.1, 4.3.2, 4.3.3.
  • the energy centre 7 obtains the heat required for heating the process gas by burning a portion of the already cleaned process gas in a combustion chamber 7.1.
  • the energy centre 7 comprises a process gas superheater 7.2.
  • the excess quantity of the process gas is fed into a storage container 18 and is subsequently utilised outside the apparatus for other purposes.
  • the thermal energy required for starting the transformation process is provided by burning utility natural gas in a natural gas-fired supporting burner 12.
  • the combustion processes are controlled such that the temperature of the flue gas leaving the energy centre 7 in the direction of the flue gas stack is 820-850 °C.
  • the excess process gas generated in the reactor 4 is passed on to the condenser 8, wherein the gas is separated into fractions while being cooled down.
  • the light condensate oil 8.1 and the heavy condensate oil 8.2 coming from the condenser 8 are stored in a light oil storage container and in a heavy oil storage container, respectively.
  • the paraffin-type condensates are discharged via a condensate storage tank, which is followed by spraying them into the process gas coming from the direction of the circulation fans 5.1, 5.2, 5.3 via the condensate/water separator 8.3, or reintroducing them into the feed unit 3 ’ .
  • the feed paths of the plastic and the hot flue gas into the reactor 4, and the path along which the cooled- off flue gas is reintroduced therein are indicated by the reference numerals 3.1, 3.2, and 3.3, respectively.
  • the energy centre 7 is an apparatus that is adapted to bum gases of various grades, and also pre-heated oils/heavy oils/paraffin-type hydrocarbons.
  • the apparatus comprises a process gas cleaner 13.
  • the gas coming from the process gas cleaner 13 is burned in a recuperative process gas burner 17.
  • the heat exchangers 9 are adapted for feeding warm air to the gas- fired supporting burner 12 and the recuperative process gas burner 17 with the help of an air fan 15.
  • the high-temperature flue gas of the gases burned in the burners is passed through the heat exchanger of the energy centre 7 and is exhausted into the surrounding atmosphere via the heat exchangers 9 and a flue gas stack 10.
  • thermolysis/gasification is applied for decomposing the plastics; the process gas and the flue gas do not come into direct contact. We were able to implement this due to the separation/relocation of the energy supply location from the process space to a separate energy centre.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • General Chemical & Material Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)

Abstract

L'invention concerne un processus de conversion de matières d'origine hydrocarburée, de matières plastiques et de déchets plastiques. Le processus comprend les étapes consistant à stocker, à trier et à broyer les matières plastiques et les déchets plastiques, et à les introduire dans un réacteur. Le processus est caractérisé par le chauffage du matériau dans un réacteur jusqu'à une température dans la plage de températures de 300 à 1 200 °C prédéterminée en fonction du matériau de départ et du produit final. Afin de fournir la chaleur requise par le processus de décomposition, le gaz de traitement refroidi est évacué du réacteur, et le gaz de traitement chauffé dans un espace séparé est mélangé à celui-ci de manière régulée. Dans le réacteur, le matériau est dirigé vers le bas depuis la partie supérieure, ce qui provoque la décomposition du matériau pendant le processus. Le produit final du processus de décomposition, qui peut être du pétrole léger, du pétrole lourd, des hydrocarbures de type paraffine, des gaz de traitement et de la poudre contenant du carbone, est évacué du réacteur. L'invention concerne également un appareil pour la mise en œuvre du processus, ledit appareil comprenant une unité de stockage, une unité de tri, une unité d'alimentation et un réacteur.
PCT/HU2022/050087 2021-12-15 2022-12-12 Processus et appareil de conversion de matières à base d'hydrocarbures, de matières plastiques et de déchets plastiques Ceased WO2023111604A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
HUP2100435 2021-12-15
HUP2100435A HU231697B1 (hu) 2021-12-15 2021-12-15 Eljárás és berendezés szénhidrogénből származó anyagok, műanyagok, műanyag hulladékok átalakítására

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060112639A1 (en) * 2003-11-29 2006-06-01 Nick Peter A Process for pyrolytic heat recovery enhanced with gasification of organic material
WO2019069107A1 (fr) * 2017-10-05 2019-04-11 Horge Technologies Kft Appareil et procédé permettant de produire un gaz de synthèse
WO2021211529A1 (fr) * 2020-04-13 2021-10-21 Eastman Chemical Company Pyrolyse de déchets plastiques dans un réacteur à film

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060112639A1 (en) * 2003-11-29 2006-06-01 Nick Peter A Process for pyrolytic heat recovery enhanced with gasification of organic material
WO2019069107A1 (fr) * 2017-10-05 2019-04-11 Horge Technologies Kft Appareil et procédé permettant de produire un gaz de synthèse
WO2021211529A1 (fr) * 2020-04-13 2021-10-21 Eastman Chemical Company Pyrolyse de déchets plastiques dans un réacteur à film

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Publication number Publication date
HUP2100435A1 (hu) 2023-06-28
HU231697B1 (hu) 2025-10-28

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