WO2009130524A1 - Appareil et procédé pyrolytique - Google Patents

Appareil et procédé pyrolytique Download PDF

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Publication number
WO2009130524A1
WO2009130524A1 PCT/HU2009/000036 HU2009000036W WO2009130524A1 WO 2009130524 A1 WO2009130524 A1 WO 2009130524A1 HU 2009000036 W HU2009000036 W HU 2009000036W WO 2009130524 A1 WO2009130524 A1 WO 2009130524A1
Authority
WO
WIPO (PCT)
Prior art keywords
pyro
gas
reactor
circulated
pyrolysis area
Prior art date
Application number
PCT/HU2009/000036
Other languages
English (en)
Inventor
Sándor LUCZE
Original Assignee
Energum Deutschland Gmbh
LEKRINSZKI, Balázs, Barna
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 Energum Deutschland Gmbh, LEKRINSZKI, Balázs, Barna filed Critical Energum Deutschland Gmbh
Publication of WO2009130524A1 publication Critical patent/WO2009130524A1/fr

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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
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • 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
    • C10B51/00—Destructive distillation of solid carbonaceous materials by combined direct and indirect heating
    • 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
    • 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 relates to a pyrolytic apparatus comprising a reactor unit with heated pyrolysis area and a condensation unit condensing pyro-oil from a pyro-gas by cooling the pyro-gas recovered from a material in the pyrolysis area. Further, the invention relates to a pyrolytic method based on the apparatus.
  • Waste management is more and more becoming a vital industry of our days. Due to our way of life, an immense amount of non-biodegradable, or very slowly biodegradable waste is being produced in a continuous manner. Both storage and disposal of such waste is possible only at high costs, thus it is one objective of waste processing to recover the more and the better quality recyclable material.
  • pyrolysis in which so called pyro-gas and/or pyro-oil is produced by thermal decomposition of waste comprising macromolecule organic compounds (e.g. rubber, plastics).
  • the ratio and the chemical composition of the end product depend on the base materials (i.e. the type of waste) as well as on the conditions of pyrolysis.
  • the pyrolysis first the waste is usually shredded, then introduced into a pyrolysis reactor, where it is heated for a longer period of time in an oxygen-free environment, and the resulting pyro-gas releases (i.e.
  • vapors and gases formed during pyrolysis are conducted into, and condensed in a cooling system, and thus pyro-oil is obtained, which then can be used, for example, as fuel oil or as engine fuel after further processing.
  • the remaining gases may also be put to several uses.
  • the soot remaining after waste evaporation is a recyclable material, that can be used as additive agent, for example, in rubber production.
  • the pyrolysis reactor is filled with waste, serving as base material, and after a certain period of heating, the residual soot and other substances are removed. Within certain boundaries, the reactor is heated, then cooled down, which entails significant loss of energy. Beyond loss of energy, the material of the reactor is likely to fail prematurely due to the fluctuations of heat, in consequence of the frequent changes of shrinking due to the cooling cycle and expansion due to the heating cycle.
  • a disadvantage of known pyrolytic apparatuses and methods is the difficulty of implementing rapid extraction of pyro-gases, which would be necessary for more rapid pyrolysis processes. By keeping the produced pyro-gases in the pyrolysis area will result in the formulation of long-chain molecules, which reduce the quality of pyro-oil.
  • the invention has been achieved in light of the recognition, that after condensation of pyro-oil from the produced pyro-gas a liquid-free pyro-gas remains, which is from all aspects (composition, temperature) suitable for accelerating the extraction of the newly formed pyro-gases rich in liquid by re-circulating it into the pyrolysis area.
  • the invention therefore, relates to a pyrolytic apparatus according to claim 1 , and a pyrolytic method according to claim 7.
  • Preferred embodiments of the invention are defined in the dependent claims.
  • Fig. 1. is a schematic diagram of a pyrolytic apparatus according to the invention.
  • the apparatus has, therefore, been constructed in a way that it comprises three reactors 1 , 2, 3, which can operate at different temperatures.
  • the soot remaining from pyrolysis is a valuable recyclable material, the quality of which is important to be maintained at a most suitable level in the long run.
  • the apparatus has been constructed so that an artificial gas circulation is conducted through the pyrolysis area of the reactors so as to accelerate evaporation of the gases produced in the course of the pyrolysis.
  • the apparatus therefore, comprises a reactor unit 50, which preferably comprises three reactors 1 , 2, 3 arranged one above the other and connected with each other in a series.
  • the reactor unit 50 comprises a waste input joint 7, an output opening 10, a pyro-gas recirculation joint 21, and two gas outlet joints 23, 24.
  • a flexible connection is ensured by compensators between reactors 1-3. All three reactors 1-3 are equipped with a device to ensure material forwarding from the waste input in the direction of output.
  • the material to be pyrolyzed preferably waste, examples of which may contain automotive rubber tires, plastic foils, plastic objects, parts or an arbitrary mixture thereof, is shredded into 2-5 cm pieces prior to feed.
  • the material to be pyrolyzed, i.e. waste to be processed is continually introduced into the waste input joint 7 located on the body of reactor 1.
  • the material to be pyrolyzed passes from the waste input joint in the direction of the output opening 10 along the marked arrows.
  • a material forwarding means is arranged, which is preferably formed as a spiral belt mounted onto a mandrel, and by the means of which the waste is conveyed longitudinally in one direction (from left to right in the drawing), whilst being turned and stirred by mixing blades mounted on the spiral belt.
  • waste passes through a flow profile 8 by means of gravitation into reactor 2.
  • Preferably identical spiral belts are arranged in reactors 1 and 2; in the case of reactor 2 waste is forwarded thereby from right to left.
  • the material passes from reactor 2 into reactor 3 through a flow profile 9.
  • reactor 3 contrary to the above, mixing blades fixed to mixing arms mounted onto the mandrel carry out the intense stirring, as well as force linear movement of the material from left to right.
  • the evaporated waste which has been transformed into soot, reaches the temporary collector tank connected to the output opening 10 of reactor 3.
  • the waste entering the reactor unit 50 has to pass through the entire length of reactor chambers 1a-3a so as to pass into a lower chamber through the gravitational flow profiles 8, 9. From the collector tank the soot is periodically emptied into further units through a valve.
  • Pyrolysis takes place in a continuous manner in the reactor unit 50, whilst the waste is forwarded by means of the material forwarding means arranged within the reactor chambers, and the material passes from the upper chambers into lower arranged chambers via gravitation.
  • the period of time spent in the individual chambers as well as the temperature set in the individual chambers greatly depend on the type of waste.
  • the temperature of pyrolysis is typically in the range between 400 and 800 °C, which may differ in the individual chambers and the period of time spent in the individual chambers typically lasts between 15 and 25 minutes, however, these values may significantly differ depending on the type of material to be pyrolysed.
  • the reactor unit 50 is heated by means of the heating mantles 4-6 positioned on the reactors 1-3.
  • heating mantles 4-6 are in communicating connection with each other, however are not in communicating connection with the pyrolysis area.
  • Heating of the reactors 1-3 is conducted from heating pipe inputs 11 of reactor 3, and from a heating pipe input 13 of reactor 2 to a flue gas output joint 15 along the arrows marked in the heating mantles 4-6.
  • Pyrolysis takes place in the longitudinal chambers 1a-3a of the reactors 1-3, comprising part of the pyrolysis area.
  • the reactor chambers 1a-3a are 3-10 m in length with an inner diameter of preferably between 20 cm and 1 m.
  • the reactors 1-3 require different temperature settings.
  • Reactor 1 requires the lowest, while reactor 3 requires the highest temperature.
  • reactors 1-3 are heated via heating of mantles 4-6 surrounding the bodies of reactors 1-3, via distributing heating pipes by means of forced circulation.
  • the main supply heating pipe is divided into three parts, two of which are connected to reactor 3 via the heating pipe inputs 11.
  • the non-utilized heat passes through the connection profile 12 arranged on the upper part of the heating mantle 6 into reactor 2, where flue gas is freshened through heating pipe input 13 by a third heating pipe.
  • the heating flue gas passes by means of forced circulation into reactor 1 through connection profile 14 without being freshened. Flue gas leaves reactor 1 through the upper flue gas output joint 15. In this way, reactor 1 is able to utilize the waste heat, that reactor 2 is unable to utilize.
  • Heating of the reactor unit 50 is supplied by a thermic afterburner 33 comprising a burner, in this way keeping contamination of flue gas to a minimum level.
  • the heating energy is produced from the gas recovered through pyrolysis.
  • the initial operation of the system requires the use of, for example, pipeline gas. After a few hours of operation, however, pipeline gas is no longer necessary, since sufficient amount of pyro-gas will be produced for the system to become self-supporting.
  • the hot flue gas passes along the heating route 40, via the main pipe to the reactor unit 50, where divided into three portions, of which two branches are connected to the heating pipe input 11 of the reactor 3, whilst the remaining branch is connected to the heating pipe input of reactor 2.
  • flue gas leaves through the flue gas output joint 15.
  • the outside mantle heating is preferably formed as an interrelated system comprising at least one burner, heating the reactor chambers 1a-3a.
  • the apparatus operates at nearly atmospheric pressure.
  • decomposition by pyrolysis process takes place in an artificially produced gas circulation.
  • the gas route 41 illustrating the passing of gas is marked by a dashed line in Fig. 1. It is a benefit of the present invention, that by continuous, controlled gas circulation the formed gases can be eliminated quickly and formation of long-chain molecules is reduced, thereby improving the quality of other by-products, such as of pyro-oil, for example.
  • the pyrolytic apparatus therefore, comprises a reactor unit 50 comprising heated pyrolysis area and a condensation unit 51 condensing pyro-oil from pyro-gas by cooling down pyro-gas recovered from the material in the pyrolysis area.
  • a condensation unit 51 condensing pyro-oil from pyro-gas by cooling down pyro-gas recovered from the material in the pyrolysis area.
  • the reactor chamber 3a of reactor 3 which forms a part of the pyrolysis area, is equipped with a pyro-gas re-circulating joint 21 , through which the liquid-free, so-called ,,dry" pyro-gas conducted through the condensation unit 51 is re-circulated and introduced in a controlled manner by means of a ventilator 30.
  • a ventilator 30 By taking hold of the pyro-gas rich in liquid formed in reactor chamber 3a, the pyro-gas passes through the connection gas pipe 22 arranged for unhindered flow into reactor chamber 2a, where taking hold additional pyro-gas rich in liquid, it leaves through the gas output joint 23.
  • the gas is circulated in a countercurrent to the material to be pyrolysed and bumps against several surfaces, resulting in the condensation of the major part of the granule particles while the gas passes on.
  • the gas leaving through the gas output joint 23 reaches the condensation unit 51 through a vapor pipe being accelerated by the suction effect of the ventillator's 30 suction side, thereby realizing a circular connection.
  • the gas formed in reactor chamber 1a reaches through a separately arranged gas output joint into a cyclone 25 known per se, where water being evaporated from the waste and transported by pyro-gas condenses. Decomposition does not yet take place in reactor chamber 1a.
  • the gas leaving the cyclone 25 also enters the condensation unit 51 through the above mentioned vapor pipe.
  • the condensation unit 51 illustrated on the figure comprises a first and a second oil condensation column 26, 27.
  • the pyro-gas enters the column 26, where moving upwards from the bottom of the tower and bumping into the wall of the liquid-cooled column, first the fraction of high boiling-point condenses and accumulates in the so-called ,,boiler" part. From the gas passing on, the condensing fraction already with lower boiling-point re-drips into a drip tray arranged at the upper part of the column 26.
  • the pyro-gas emerging from the upper part of the column 26 passes into the bottom of the column 27 through a connection pipe. By moving upwards from the bottom of column 27 and passing two drip trays, the gas cools down to such an extent that no additional liquid material condenses.
  • the gas emerging from the upper half of column 27 is conducted through a transfer pipe into a scrubber 28. Moving upwards in the gas scrubber, and passing through a caustic solution injected at two levels of jet dispersers, the gas is decontaminated.
  • the gas emerging from the scrubber 28 is conducted into the cyclone 29, where the taken water drops condense.
  • the gas pipeline connected to the discharge side of the ventilator 30 divides into two branches, where a part of the gas passing through a control-valve towards the pyro-gas re-circulating joint 21 of the reactor 3 re-enters the cycle.
  • the other part of the gas enters the compressor 31 , from where in a compressed state it passes towards a gas tank 32.
  • the gas passes into a thermic afterburner 33, where it is burned, thereby providing thermic energy for the serial reactor, i. e. the portion of pyro-gas, which is not re-circulated into the pyrolysis area is used for heating the reactor unit 50.
  • the soot-cooler completes the cooling of soot to a processable temperature.
  • the soot-cooler is a batch operating apparatus. Cooled through its outer mantle by a cooling-liquid, an inside stirring unit completes the turning of soot.
  • soot-cooler Locking up of the soot-cooler locks the filling- valve, and intense stirring starts, while a controlled amount of water accumulated by the technology is vaporised onto the soot. After a few minutes of cooling, the soot is discharged into the throat positioned underneath the soot-cooler 34, from where the soot is forwarded, after being measured, for further processing by means of, for example, a worm-conveyor.
  • the reactor chambers 1a-3a are arranged directly one above the other, which carries the benefit of a compact, space- and material-saving construction, however, it is evident, that the benefits according to the present invention can also be realized in the cases of any arbitrarily arranged chambers. Also it is not absolutely necessary that the reactor chambers of 1a-3a should be arranged horizontally, or that they should be parallel to each other. The number of pyrolysis reactor chambers 1a-3a may also vary according to specific needs.

Abstract

L'invention concerne un appareil pyrolytique qui comprend une unité réacteur (50) comportant une région de pyrolyse chauffée, et une unité de condensation (51) qui est destinée à condenser de l'huile pyrolytique à partir d'un gaz pyrolytique en refroidissant le gaz pyrolytique récupéré d'un matériau dans la région de pyrolyse. Selon l'invention, après que le gaz pyrolytique est passé à travers l'unité de condensation (51), au moins une partie de ce dernier est remise en circulation dans la région de pyrolyse de l'unité réacteur (50). L'invention se rapporte en outre à un procédé pyrolytique mis en oeuvre à l'aide de l'appareil.
PCT/HU2009/000036 2008-04-24 2009-04-23 Appareil et procédé pyrolytique WO2009130524A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
HUP0800261 2008-04-24
HU0800261A HUP0800261A2 (en) 2008-04-24 2008-04-24 Pyrolysis reactor and method

Publications (1)

Publication Number Publication Date
WO2009130524A1 true WO2009130524A1 (fr) 2009-10-29

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Application Number Title Priority Date Filing Date
PCT/HU2009/000036 WO2009130524A1 (fr) 2008-04-24 2009-04-23 Appareil et procédé pyrolytique

Country Status (2)

Country Link
HU (1) HUP0800261A2 (fr)
WO (1) WO2009130524A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015040256A1 (fr) * 2013-09-17 2015-03-26 Huguet Farré Jordi I Procédé d'élimination de plastiques contenus dans des résidus urbains et industriels, et installation pour la mise en pratique de celui-ci
ES2553679A1 (es) * 2015-07-20 2015-12-10 Madison Solutions S.L. Planta y proceso para la producción de gasóleo a partir de residuos industriales y urbanos
WO2018014922A1 (fr) * 2016-07-21 2018-01-25 Syntes One - Engineering Group Aps Système et procédé de pyrolyse
WO2021120219A1 (fr) * 2019-12-20 2021-06-24 李素芳 Procédé de fonctionnement d'un four de pyrolyse et dispositif associé
CN115326910A (zh) * 2022-07-07 2022-11-11 华中科技大学 一种热解三态产物的分析系统

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GB668808A (en) * 1949-09-17 1952-03-19 California Research Corp Process for retorting shale
AU456936B2 (en) * 1973-05-08 1974-12-16 Occidental Petroleum Corporation Process for production and recovery of fuel values from coal
US4056461A (en) * 1976-06-25 1977-11-01 Chevron Research Company Retorting process utilizing a flexible, helical shaped conveyor
US4324643A (en) * 1980-08-26 1982-04-13 Occidental Research Corporation Pyrolysis process for producing condensed stabilized hydrocarbons
US4419185A (en) * 1981-07-16 1983-12-06 American Carbons, Inc. Pyrolysis system with hot gas recirculation
US4781796A (en) * 1983-09-13 1988-11-01 Canadian Patents And Development Limited Apparatus for the conversion of sludges
US4983278A (en) * 1987-11-03 1991-01-08 Western Research Institute & Ilr Services Inc. Pyrolysis methods with product oil recycling
WO1999018171A1 (fr) * 1997-10-06 1999-04-15 Barsi Peter Systeme de pyrolyse fonctionnant en continu en boucle fermee permettant de traiter les rebuts de caoutchouc
WO2000011110A1 (fr) * 1998-08-21 2000-03-02 Ershag Bengt Sture Procede de recuperation de carbone et de combinaisons d'hydrocarbures a partir de polymeres, de preference sous forme de pneus uses, par pyrolyse dans un reacteur de pyrolyse
WO2008075105A1 (fr) * 2006-12-19 2008-06-26 Used Tyre Distillation Research Limited Système et procédé pour recycler des matériaux contenant du carbone

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB668808A (en) * 1949-09-17 1952-03-19 California Research Corp Process for retorting shale
AU456936B2 (en) * 1973-05-08 1974-12-16 Occidental Petroleum Corporation Process for production and recovery of fuel values from coal
US4056461A (en) * 1976-06-25 1977-11-01 Chevron Research Company Retorting process utilizing a flexible, helical shaped conveyor
US4324643A (en) * 1980-08-26 1982-04-13 Occidental Research Corporation Pyrolysis process for producing condensed stabilized hydrocarbons
US4419185A (en) * 1981-07-16 1983-12-06 American Carbons, Inc. Pyrolysis system with hot gas recirculation
US4781796A (en) * 1983-09-13 1988-11-01 Canadian Patents And Development Limited Apparatus for the conversion of sludges
US4983278A (en) * 1987-11-03 1991-01-08 Western Research Institute & Ilr Services Inc. Pyrolysis methods with product oil recycling
WO1999018171A1 (fr) * 1997-10-06 1999-04-15 Barsi Peter Systeme de pyrolyse fonctionnant en continu en boucle fermee permettant de traiter les rebuts de caoutchouc
WO2000011110A1 (fr) * 1998-08-21 2000-03-02 Ershag Bengt Sture Procede de recuperation de carbone et de combinaisons d'hydrocarbures a partir de polymeres, de preference sous forme de pneus uses, par pyrolyse dans un reacteur de pyrolyse
WO2008075105A1 (fr) * 2006-12-19 2008-06-26 Used Tyre Distillation Research Limited Système et procédé pour recycler des matériaux contenant du carbone

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2015040256A1 (fr) * 2013-09-17 2015-03-26 Huguet Farré Jordi I Procédé d'élimination de plastiques contenus dans des résidus urbains et industriels, et installation pour la mise en pratique de celui-ci
ES2533141A1 (es) * 2013-09-17 2015-04-07 Jordi HUGUET I FARRÉ Procedimiento de eliminación de plásticos contenidos en residuos urbanos e industriales e instalación para la puesta en práctica del mismo.
ES2553679A1 (es) * 2015-07-20 2015-12-10 Madison Solutions S.L. Planta y proceso para la producción de gasóleo a partir de residuos industriales y urbanos
WO2018014922A1 (fr) * 2016-07-21 2018-01-25 Syntes One - Engineering Group Aps Système et procédé de pyrolyse
WO2021120219A1 (fr) * 2019-12-20 2021-06-24 李素芳 Procédé de fonctionnement d'un four de pyrolyse et dispositif associé
CN115326910A (zh) * 2022-07-07 2022-11-11 华中科技大学 一种热解三态产物的分析系统
CN115326910B (zh) * 2022-07-07 2024-04-05 华中科技大学 一种热解三态产物的分析系统

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Publication number Publication date
HU0800261D0 (en) 2008-06-30
HUP0800261A2 (en) 2009-10-28

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