WO2013119187A2 - Procédé de décomposition thermique de matières organiques et équipement pour sa mise en œuvre - Google Patents

Procédé de décomposition thermique de matières organiques et équipement pour sa mise en œuvre Download PDF

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Publication number
WO2013119187A2
WO2013119187A2 PCT/SK2013/000001 SK2013000001W WO2013119187A2 WO 2013119187 A2 WO2013119187 A2 WO 2013119187A2 SK 2013000001 W SK2013000001 W SK 2013000001W WO 2013119187 A2 WO2013119187 A2 WO 2013119187A2
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WIPO (PCT)
Prior art keywords
tubular flow
cracking reactor
type
type cracking
reactor
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PCT/SK2013/000001
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English (en)
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WO2013119187A3 (fr
Inventor
László Farkas
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Farkas Laszlo
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Publication of WO2013119187A2 publication Critical patent/WO2013119187A2/fr
Publication of WO2013119187A3 publication Critical patent/WO2013119187A3/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • 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
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
    • 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
    • C10B57/02—Multi-step carbonising or coking 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • 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
    • F23G7/12—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of plastics, e.g. rubber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/302—Treating pyrosolids
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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 present invention concerns a method of thermal decomposition of organic material and a design of equipment for thermal decomposition of organic material.
  • the said equipment enables continuous processing of organic material and production of alternative second generation energy carriers (chemicals, solid, gaseous and liquid fuels, heating oils) and solid carbon materials by thermal decomposition of specified and/or mixed wastes from used tyres, plastics, biomass, organic portions of municipal waste, using the system of tubular flow-type cracking reactor for the processing of carbon-based waste materials.
  • thermal cracking of used tyres, waste plastics, biomass and municipal waste allows for their thermal degradation without the participation of oxygen/air.
  • thermal cracking the wastes are heated to high temperatures under which their macromolecular structures are cracked to smaller molecules.
  • Products of thermal cracking can be divided to non- condensed gaseous fraction, liquid fraction and solid residues (coke).
  • Thermal cracking of waste further provides a rather wide composition range of hydrocarbons and non- hydrocarbons, including low-molecular gasses (hydrogen, carbon monoxide, carbon dioxide, alkanes and alkenes d - C 5 ) through liquid portions up to coke.
  • Liquid products of thermal cracking are used for the production of valuable types of gasoline, kerosene, diesel fuels, heating oils, alternative oils, as well as valuable chemicals, such as dl-limonene obtained from thermal cracking of used tyres.
  • the most valuable portions of municipal wastes include polymeric materials from industrial or municipal sources.
  • Polymeric materials mainly polyethylene and polypropylene, undergo thermal cracking at 165 to 750 °C and at the atmospheric pressure, generating oil-waxes with the boiling temperature of 30 to 450 °C, containing saturated and non-saturated hydrocarbons numbered C 5 to C 30 . Then the fraction of gasoline's is separated from oil-waxes by the process of distillation at the atmospheric pressure and at the temperature of 30 to 180 °C, and it contains saturated and non-saturated, non-branched and branched hydrocarbons C 5 to Cn.
  • Critical technological parameters with the strongest influence on the composition of reaction products obtained under thermal cracking include chemical composition of feedstock, temperature, heat transfer rate, pressure, reaction time, reactor type, presence of reactive gasses (e.g. oxygen), catalyst, additives contained in the feedstock, gaseous and liquid phase of the process.
  • Reactor type is critical with respect to the heat transfer quality, mixing, retention time in gaseous and liquid phases, and the release of primary decomposition products.
  • Reactor is to be selected mainly on the basis of technical aspects, such as heat transfer and working properties of the feedstock and products.
  • the polymeric material is first dissolved in a polymer melt or wax, or dispersed in a salt bath in order to reduce the melt viscosity.
  • the reactors In order to ensure high efficiency of cracking reactors involving chemical cracking of polyalkenes, the reactors must be built using the flow design. For the same reasons, they should have the capacity to continuously remove coke during the decomposition of plastic waste that involves high generation of coke and mineral residues.
  • the mixture of polyalkenes and used tyres gets charged into a batch reactor equipped with a special agitator.
  • the reactor is charged using a screw extruder or other equipment.
  • Material is batched to this semi-continuous reactor for a certain period of time, with gaseous and liquid fractions, as well as a mixture of carbon black, mineral impurities and coke being generated as the main products.
  • the production cycle is finished, the process stops and the reverse run of the agitator starts. In this cycle the agitator blades scrape the coke off the inner walls of the reactor.
  • the main disadvantage of this solution resides in the semi-continuously working reactor with a relatively low production capacity and a problem using the cracking catalyst.
  • the agitator blades have exactly the same shape and size as the inside of the reactor.
  • the solid material deposited inside the reactor is being scraped off the hot reactor walls.
  • the scraped off coke falls down and is evacuated from the reactor bottom together with a portion of reaction products through an exhaust pipe.
  • the main products of thermal cracking are the gaseous fractions (suitable for heating), gasoline and light heating oil, and paraffin fractions.
  • a batch reactor equipped with a screw feeder and an agitator is described in another American patent, the U.S. Patent No. 5738025.
  • Special grating is installed inside the reactor above the melted mixture of waste plastics being cracked. Waste plastics charged into the cracking reactor are melted on the special grating and then fall down to the reaction mixture.
  • an agitator having a specially designed shape, scraping the coke off the reactor walls down to a specially shaped reactor bottom, from where it is removed by means of a screw conveyor. The temperature in this process reaches 450 °C.
  • Granules of the coke being removed fall down to a container at the end of the reactor terminal section, while the hydrocarbon vapours proceed through air coolers and water coolers to separators in order to separate gasses from liquids.
  • Laboratory experiments (0.3 - 2 kg) and semi-operation equipment with the capacity of 20 - 30 kg/h have shown that this type of reactors can be suitable for commercial application if used with a flow design.
  • the main advantage of this solution is the continuous removal of coke from the reaction tubes.
  • the reactor cracking unit will comprise six or more tubes equipped with inner agitators, enabling either the thermal or catalytic cracking of waste polyalkenes. It appears that cracking reactors with a fluid bed (thermal or catalytic) are the best solution in terms of their industrial application.
  • Material in the liquid state is then heated and decomposes from higher polymeric structures to low-molecular structures depending on the decomposition temperature. Gaseous components are cooled down to products of standard composition. Composition of the obtained products and their molecular weight largely depends on the decomposition temperature. The aspect that is important for the resulting composition of the obtained products is the development of cracking reactions in the liquid state.
  • the most important task is to ensure thermal cracking of carbon materials to be realized in such a way that the gaseous, rather reactive components (mainly the non-saturated ones) - released by the decomposition of liquid portions - are taken away from the reaction zone as quickly as possible in order to prevent them from being subject to intensive and long heating.
  • the liquid components are transported in a high- density form after liquefaction. Retaining such liquids in the reaction zone results in the formation of high amounts of coke.
  • the generated thin layer made of polymers has low thermal conductivity, which can lead to wrong temperature control in the centre of the reactor and thus to deteriorated control over the composition of the obtained products.
  • the subject-material of the invention which eliminates the above stated deficiencies is the method of producing alternative second generation energy carriers (chemicals, solid, gaseous and liquid fuels, heating oils) and solid carbon materials by thermal decomposition of specified and/or mixed wastes from used tyres, plastics, biomass and organic portions of municipal waste.
  • the present solution consists in providing a new design of a tubular flow-type cracking reactor enabling continuous processing of waste carbon materials.
  • the thermal cracking takes place in a hermetically enclosed flow apparatus.
  • the feedstock material transformed to crushed material, shreds or chippings with the size of up to 350 mm is transported to a batching hopper.
  • the modified feedstock material is transported by a spiral-type batching conveyor through a decomposition oil filling, which constitutes an input oil seal, to a tubular flow-type cracking reactor equipped with a shifting spiral conveyor.
  • the feedstock carbon material undergoes thermal cracking in a tubular flow-type cracking reactor at the temperature of 165 to 750 °C, at the atmospheric pressure ranging from 100834.6675 Pa to 101815.3325 Pa (i.e.
  • the tubular flow-type cracking reactor is heated by a heating furnace consisting of two sections, the first stage and the second stage, namely by means of heat transfer from combustion products generated by the combustion in furnace burners of cleaned cooled gas brought in from the process of thermal cracking with preheated air from the recuperator.
  • the feedstock material is preheated already in the initial stage of batching, namely by heat from the oil filling generated by a condensate of high-boiling portions of decomposition oil running down from the area of the tubular flow-type cracking reactor by the force of gravity.
  • the tubular flow-type cracking reactor is positioned on a metal frame at a certain angle relative to the horizontal plane.
  • the tubular flow-type cracking reactor houses a shifting spiral conveyor with its bottom part being submerged in an oil seal. The top part is enclosed by a water seal, with the oil and water seals hermetically enclosing it.
  • the oil and water seals constitute essential and indispensable parts of the tubular flow-type cracking reactor. Thermal decomposition of carbon materials taking place inside the tubular flow-type cracking reactor is thus realized at the atmospheric pressure ranging from 100834.6675 Pa to 101815.3325 Pa (i.e. at the atmospheric pressure ranging from -50 mm up to +50 mm of water column). With the said configuration, at which there is no overpressure generated in the tubular flow-type cracking reactor, the oil and water levels are stable.
  • the spectrum and quality of products depend to a great extent on the reactions that take place.
  • the first ones which are prevailing, include primary cracking of carbon materials to low-molecular products.
  • the second ones include secondary condensation reactions, thermal alkylations, oligomerizations, polymerizations and cyclizations of primary products that can even result in carboids (coke). It derives from the equilibrium composition that thermal decomposition supports the overall pressure reduction in the reaction system thermodynamically. Unlike the decomposition reactions, the secondary reactions are of a higher than the first order. They are supported by a higher concentration of reactive components, such as alkenes, acetylene, dienes, aromates and by pressure. Higher pressure is therefore not desirable during cracking also due to kinetics.
  • condensations resulting in a concentrated liquid phase are not desirable either. Condensations, which eventually lead to coke formation, are therefore even more sensitive to temperature fluctuations in the reactor and exchangers. More distinct are the molecular condensation reactions, such as Diels-Alder syntheses. Polyenes, polyaromates, tar and coke become gradually formed in case of these reactions.
  • coke becomes deposited on the inner surface of the reactor on regular basis. Opinions concerning the coke formation mechanism differ. There probably exist two mechanisms. In case of the first one, the coke-forming substances become adsorbed directly from the gaseous phase on the active points of the surface, where they become transformed to coke by gradual reactions with radicals from the gaseous phase and through the subsequent polymerizations and condensations. In case of the second one, the given interactions, polymerizations and condensations take place in the gaseous phase up to the formation of aerosol. The resulting droplets settle on the surface and through further reactions they turn to coke. The coke formed in the second case is fibrous.
  • the form of the coke depends on weather the droplets drench the surface or not. If they do, it results in the formation of an amorphous coke surface. Otherwise it is the globular (spheroidal) coke that becomes formed.
  • Important precursors include vinyl and phenyl radicals, as well as polyenes, polyacetylenes and polyaromates generated from these radicals. Effect of the surface composition is rather important.
  • the advantage of reduced pressure (not overpressure) in the reactor is that it limits the development of secondary reactions of gaseous carbons.
  • the method of producing alternative second generation energy carriers (chemicals, solid, gaseous and liquid fuels, heating oils) and solid carbon materials in a tubular flow-type cracking reactor provides an original technology using waste carbon polymeric materials from municipal wastes with universal application to produce environmentally friendly quality fuels.
  • the universal character of a tubular flow-type cracking reactor consists primarily in the fact that it enables to recycle varied feedstock materials, such as used tyres, waste plastics, biomass and municipal wastes.
  • the process in terms of the present invention is efficient also due to the recovery of waste heat in order to pre-heat the air. Before entering the burners, the air is heated in recuperators.
  • the heating medium is constituted by combustion gases.
  • the waste heat from the process is also used for preheating the incoming feedstock that accepts the heat from the oil seal.
  • a benefit provided by the method of thermal decomposition in terms of the present invention is also its technical simplicity in the connection of the reactor cracking tube with the batching hopper through the input oil seal, while the tubular cracking reactor is equipped with a conveyor for solid products and an out-feed conveyor in its upper part.
  • the cracking tubular reactor is designed in such a way that the gaseous and solid products can leave the reaction zone as quickly as possible. This prevents their overheating and the development of secondary reactions leading to coke formation.
  • the method of thermal decomposition in terms of the present invention is a process that is energy and material unintensive. Recycling of carbon polymeric wastes protects the environment while enabling to produce quality and environmentally friendly alternative fuels of second generation. This substitutes a part of fossil fuels, mainly petroleum, which has to be imported by many countries (including Slovakia).
  • Fig. 1 shows the equipment for thermal decomposition of organic material.
  • Fig. 2 shows a detail of the oil seal, and
  • Fig. 3 shows a detail of the water seal.
  • the technological process of thermal decomposition of carbon materials is realized in a tubular flow-type cracking reactor.
  • the universal character of a tubular cracking reactor consists primarily in the fact that it enables to recycle varied feedstock materials, such as used tyres, waste plastics, biomass and municipal wastes.
  • the technological equipment consists of three sections: a batching section, a reactor section (hot section) and an output section (cold unloading section).
  • the tubular flow-type cracking reactor is schematically represented in Figure 1.
  • Feedstock material batching is located in the bottom part of the tubular flow-type cracking reactor l a. It ensures the input of feedstock material through the batching hopper 15 in conjunction with the batching spiral-type conveyor 6 that contains a decomposition oil filling constituting the input hydraulic seal 8. Connection between the spiral conveyor 16 and the tubular flow-type cracking reactor l a forms an angle of 90 to 125 degrees. Feedstock material batching is provided by a spiral-type batching conveyor 16 with an electric drive 18 of the batching spiral-type conveyor.
  • the basis of the hot section is constituted by the tubular flow-type cracking reactor 1a positioned on the frame 32 at an angle of 8 to 38 degrees relative to the horizontal plane.
  • the tubular flow-type cracking reactor la is made of stainless steel with the inner diameter of up to 550 mm and the length of up to 16.0 m, containing a spiral conveyor 2 to transport feedstock material and products along the tubular flow-type cracking reactor la. Drive 3 of the spiral conveyor is placed at the bottom part of the reactor.
  • the other parts of the hot section include a heating furnace 4 of the first stage of the tubular flow-type cracking reactor and a heating furnace 5 of the second stage of the tubular flow-type cracking reactor, a gas burner 12, an air pre-heater 6, an input oil seal 8 at the feedstock inlet, and a water cooler for solid residues 7.
  • the tubular flow- type cracking reactor has two consecutive stages with different operating temperatures. Temperature in the first part of the heating furnace 4 is maintained at 165 to 500 °C, temperature in the second part of the heating furnace 5 is at 520 to 750 °C, with the temperature being controlled in relation to the feedstock material.
  • Tubular flow-type cracking reactor is positioned in the heating furnace of the first 4 stage and heating furnace of the second 5 stage of the tubular flow-type cracking reactor with heat insulation.
  • the tubular flow-type cracking reactor l a is heated with the heat from hot combustion products flowing from the gas burner 12, which is located in the second stage heating furnace 5, in the opposite direction against the feedstock material movement.
  • the decomposition gas generated by thermal cracking of the injected feedstock material is burned in the gas burner 12 together with air. Combustion products from the heating furnace 4 of the first stage are drawn away through point 11. They are led through the air pre-heater 6 to the stack 29.
  • Gaseous fission products generated by thermal cracking of carbon materials leave the tubular flow-type reactor through the opening 13 in the first part.
  • Decomposition gas generated in the process of radical cracking leaves the tubular flow-type reactor also through the opening 14 in the second part of the reactor.
  • the upper part of the reactor contains an opening 19 designated for the discharge of solid products (coke, steel cords from tyres).
  • the emerging decomposition gas is taken away from the tubular flow-type cracking reactor through the first outlet 13 and the second outlet 14 to undergo condensation. It passes through a two-stage condensation system. In the first condensation step it enters a quench column. The decomposition gas vapours are quenched by the emerging decomposition oil to the temperature of 65 to 80 °C. In the second condensation step the gas product vapours are cooled down to the temperature of 30 to 35 °C when mainly the hydrocarbons C 4 and C 5 are condensed. Water becomes separated from light heating oil in the separator. The condensed water is collected in an intermediate store and is returned back to the technological process. The decomposition gasses are compressed into storage tanks.
  • Inclination of the tubular flow-type cracking reactor l a serves the following functions: it naturally provides for the required input oil seal 8 in the bottom part of the tubular cracking reactor l a; it enables easy and trouble-free movement of feedstock material even in the form of crushed material, shreds, as well as of the reaction intermediate and final products (coke, steel cords) along the tubular flow-type cracking reactor l a; it ensures fluent and easy transfer of heat and material for decomposition gases, liquids and coke during the decomposition process; it enables natural flow of residual decomposition oils into the oil seal.
  • an in-feed spiral conveyor 20 for solid products including a drive 21 of the in-feed spiral conveyor, and an out-feed spiral conveyor 22 with a drive 23.
  • an output water seal 9 Between the in-feed spiral conveyor 20 for solid products and the out-feed spiral conveyor 22 there is an output water seal 9.
  • the level 24 of the output water seal provides a barrier that prevents the outside from entering the inert environment inside the reactor.
  • the water intake to the water seal is at point 25.
  • Connection between the conveyor 26 for solid products and the out-feed screw conveyor 22 forms an angle of 90 to 125 degrees.
  • the input oil seal 8 located at the input-batching section of the tubular flow-type cracking reactor la and the output water seal 9 located at the output section of the tubular flow-type cracking reactor constitute essential and indispensable parts of the reaction system.
  • the oil and water fillings provide hermetic enclosure of the reaction zone. Thermal decomposition taking place inside the tubular flow-type cracking reactor la is thus realized at the atmospheric pressure. With the given configuration the oil 10 and water 24 levels are stable. A sudden release of vapours of the emerging products (decomposition process bubble theory) sometimes results in an overpressure inside the reactor area.
  • the liquid seals enable the gas overpressure to become relieved into the air and thus to prevent the increasing pressure of the emerging gases from exceeding the safe limit.
  • the method of thermal decomposition within the production of alternative second generation liquid carriers of energy (chemicals, gaseous and liquid fuels, heating oils) and solid carbon materials by thermal cracking while using specified and/or mixed wastes from used tyres, plastics, paper, textiles, biomass and organic portions of municipal waste in the equipment for thermal decomposition of organic material by means of a tubular flow-type cracking reactor in terms of the present invention is mainly applicable for recycling of waste carbon materials in small-scale as well as large-scale power engineering. It enables to use in a flexible way either the minor facilities with an annual processing capacity of 20 000 tons built on green-field sites, or the large- capacity facilities at oil refineries enabling to valorize the obtained products to an even greater extent.

Abstract

Cette invention concerne un procédé de décomposition thermique de matières organiques issues de déchets spécifiés et/ou en mélange provenant de pneus usés, plastiques, papier, textiles, biomasse et fraction organique de déchets municipaux dans une atmosphère inerte sans participation d'oxygène/air, ledit procédé de décomposition thermique étant mis en œuvre en continu dans un appareil de décomposition thermique de type à écoulement hermétiquement clos. La charge modifiée sous la forme de matières concassées, déchiquetées ou de copeaux d'une taille jusqu'à 350 mm est transportée jusqu'à la trémie d'alimentation (15), puis acheminée au moyen d'un convoyeur (16) de type spirale après passage dans un bain d'huile de décomposition (17), qui constitue le joint étanche à l'huile (8) d'entrée, jusqu'au réacteur de craquage (1a) de type à écoulement tubulaire au moyen d'un convoyeur (2) de type spirale déportée, où le craquage thermique de la charge s'opère à la température de 165 à 750°C et à une pression atmosphérique allant de 100834,6675 à 101815,3325 Pa (à savoir, à la pression atmosphérique allant de -50 jusqu'à +50 mm de colonne d'eau) pour obtenir des produits gazeux, liquides et solides. Les produits de décomposition gazeux sont ensuite transportés de la première partie (1b) du réacteur de craquage de type à écoulement tubulaire par l'orifice de sortie (13) et par l'orifice de sortie (14) de la seconde partie (1c) du réacteur de craquage de type à écoulement tubulaire jusqu'au système de condensation, puis les produits solides sont transportés jusqu'à la seconde partie (1c) du réacteur de craquage de type à écoulement tubulaire au moyen du convoyeur en spirale (2) après passage dans le refroidisseur à eau (7) par l'ouverture de sortie (19) des produits solides jusqu'au joint étanche à l'eau de sortie (9) constituant le joint hydraulique, d'où les produits solides sont récupérés au moyen du convoyeur d'introduction de charge (20) et du convoyeur de sortie de charge (22). L'équipement de décomposition thermique (1) de matières organiques destiné à mettre en œuvre le procédé de décomposition thermique selon l'invention comprend le réacteur de craquage (1a) de type à écoulement tubulaire monté sur le carter (32) à un angle de 8 à 38° par rapport au plan horizontal, tandis que le réacteur de craquage (1a) de type à écoulement tubulaire renferme un convoyeur en spirale déportée (2) dont la partie inférieure est immergée dans le joint étanche à l'huile d'entrée (8), la seconde partie (1c) du réacteur de craquage de type à écoulement tubulaire étant confinée dans le joint étanche à l'eau de sortie (9).
PCT/SK2013/000001 2012-02-06 2013-02-01 Procédé de décomposition thermique de matières organiques et équipement pour sa mise en œuvre WO2013119187A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SK5004-2012A SK288338B6 (en) 2012-02-06 2012-02-06 Method of thermal decomposition of organic material and device for implementing this method
SKPP5004-2012 2012-02-06

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WO2013119187A2 true WO2013119187A2 (fr) 2013-08-15
WO2013119187A3 WO2013119187A3 (fr) 2013-11-14

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Publication number Priority date Publication date Assignee Title
CN106145107A (zh) * 2016-06-24 2016-11-23 北京神雾环境能源科技集团股份有限公司 一种芦竹生产活性炭、生物油联产发电的系统和方法
WO2021016877A1 (fr) * 2019-07-30 2021-02-04 李媛媛 Dispositif de manipulation de matériau
CN114702980A (zh) * 2022-04-11 2022-07-05 攀枝花市金开圆科技有限公司 一种废轮胎热裂解反应釜排渣装置
EP4212602A1 (fr) * 2022-01-12 2023-07-19 Itelyum Regeneration S.p.A. Procédé d'élimination de pneus

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CN106145107A (zh) * 2016-06-24 2016-11-23 北京神雾环境能源科技集团股份有限公司 一种芦竹生产活性炭、生物油联产发电的系统和方法
WO2021016877A1 (fr) * 2019-07-30 2021-02-04 李媛媛 Dispositif de manipulation de matériau
EP4212602A1 (fr) * 2022-01-12 2023-07-19 Itelyum Regeneration S.p.A. Procédé d'élimination de pneus
CN114702980A (zh) * 2022-04-11 2022-07-05 攀枝花市金开圆科技有限公司 一种废轮胎热裂解反应釜排渣装置

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