WO2011009419A1 - Procédé et dispositif destinés à la décomposition thermique de caoutchouc et/ou plastique - Google Patents

Procédé et dispositif destinés à la décomposition thermique de caoutchouc et/ou plastique Download PDF

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Publication number
WO2011009419A1
WO2011009419A1 PCT/CZ2010/000079 CZ2010000079W WO2011009419A1 WO 2011009419 A1 WO2011009419 A1 WO 2011009419A1 CZ 2010000079 W CZ2010000079 W CZ 2010000079W WO 2011009419 A1 WO2011009419 A1 WO 2011009419A1
Authority
WO
WIPO (PCT)
Prior art keywords
outlet
cooler
reaction zone
rubber
thermal decomposition
Prior art date
Application number
PCT/CZ2010/000079
Other languages
English (en)
Inventor
Miroslav DOČKAL
Josef MALlŠ
Radim HOLAŇ
Milan Fikoczek
Original Assignee
Dockal Miroslav
Malls Josef
Holan Radim
Milan Fikoczek
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
Priority claimed from CZ20090473A external-priority patent/CZ2009473A3/cs
Priority claimed from CZ20090472A external-priority patent/CZ2009472A3/cs
Application filed by Dockal Miroslav, Malls Josef, Holan Radim, Milan Fikoczek filed Critical Dockal Miroslav
Priority to EP20100766215 priority Critical patent/EP2456813A1/fr
Publication of WO2011009419A1 publication Critical patent/WO2011009419A1/fr

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Classifications

    • 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
    • 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
    • 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
    • C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
    • C10B47/06—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge in 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
    • 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
    • C08J2300/00—Characterised by the use of unspecified polymers
    • C08J2300/30—Polymeric waste or recycled polymer
    • 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
    • C08J2319/00—Characterised by the use of rubbers not provided for in groups C08J2307/00 - C08J2317/00
    • 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
    • C08J2321/00—Characterised by the use of unspecified rubbers
    • 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
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/62—Plastics recycling; Rubber recycling

Definitions

  • the invention concerns thermal decomposition of rubber and/or plastic and solves ecological processing of waste containing rubber and/or plastic and their transformation to again usable raw materials.
  • Reaction products are drawn off outside the reaction zone, where they are cooled, whereas the condensed liquid is drawn off into an expansion tank heated to 40 0 C, and residual gases are delivered into the combustion chamber.
  • Disadvantage of this technique is that processed material must be crushed in advance, as unequal heating of greater pieces results to unwanted prolongation of processing time.
  • the next disadvantage is unequal heating.
  • document CZ 18799 U the device for continual ecological rubber waste disposal is described. This device contains a swinging heated chamber provided with a hole for charge insertion and with a hole for removal of indecomposable residue. Due to swinging motion of the chamber, the charge stepwise moves from chamber inlet side to chamber outlet side, whereas it undergoes to thermal decomposition.
  • pyrolytic gases are drawn off outside the chamber, where they are separated to gas fraction, liquid fraction and solid impurities after cooling-down.
  • the gas fraction is burnt in the course of chamber heating. Disadvantage of this device is that the processed rubber waste must be crushed in advance. This increases costs in particular when used tires are processed.
  • CA 2584557 a device for thermal decomposition of rubber waste containing an exchangeable reaction chamber provided with heating elements and an off-take tube is described, with which arisen pyrolytic gases are drawn off into a condenser. In the condenser cooling down of pyrolytic gases and liquefaction of liquefiable fraction occur. The gas fraction is drawn off into the combustion equipment, while the liquid fraction is conducted into the reservoir.
  • the charge formed with crushed tires is subjected to temperature 550-800 °C, namely in reduction gas atmosphere, whereat the liquefiable fraction is separated from released gases.
  • a part of the gas fraction is burnt and the rest is after preheating inducted back into reactor.
  • it acts as a heat source for further thermal decomposition.
  • Disadvantage of this technology is that there occurs not only releasing of substances, which are not liquid under standard conditions, but also gas arises, whereas a part of gas, which was cooled down in the course of condensation of liquefiable fraction, must be reheated before entering the reaction zone.
  • CZ 17601 U is described the device for separation of pyrolytic oil for processing of waste rubber. This device comprises the reaction chamber, in which the charge is inserting.
  • the reaction chamber is provided with outlet for off-take of pyrolytic gases outside the reaction chamber, where the pyrolytic gases are cooled down, whereas condensation of liquid fraction occurs.
  • the non-condensed gas fraction is forced back into the reaction chamber, while the liquid fraction is collected in the receiving tank.
  • Disadvantage of this device is that the not liquefied gases forced into the pyrolytic chamber are cool. They uselessly cool down both, the chamber and the charge. Heat delivered for pyrolysis ensuring is then uselessly extracted by condensation of liquefiable substances.
  • inorganic salts forming the molten bath represents, after depletion of the bath, a waste, which is technologically difficult to treat. If the hot bath is made of melt metals, this bath is very expensive in case that the device should have higher capacity. Furthermore, operation of such bath, if it contains lead, endangers health of operating staff. The device is thanks to mechanical forcing of the charge under hot bath surface very complicated, and therefore it is also maintenance-intensive.
  • the base of method is that the charge containing rubber and/or plastic is inserted into the reaction zone, which is a part of the working area, the working area is separated from ambient atmosphere and the charge is subjected to temperature in the range of 100 up to 600 0 C. Through temperature effect there occurs releasing of pyrolytic gases, which are drawn off from the working area. However, at least a part of gases located in the working area circulates, whereas it is repeatedly directed to the vicinity of heat source, where it is heated to temperature at most 600 0 C, and flow of these gases is led in direction to the charge or under its surface and gases drawn off from the reaction zone are subsequently cooled down up to at least partial liquefaction.
  • the reaction zone is advantageously cooled down, at best with air from ambient atmosphere, which is delivered into the area between the reaction zone and thermal-insulating layer, with which the reaction zone is at least partially surrounded.
  • the reaction zone can be also cooled down with gas delivered into the reaction zone.
  • the base of the device is that it consists of the working chamber, the walls of which are at least partially provided with thermal-insulating material.
  • the working chamber is provided with at least one outlet of pyrolytic gases and at least one lockable hole.
  • the reaction zone for placing of the charge containing rubber and/or plastic and heating elements, which at least partially surround the reaction zone.
  • the fan for assuring of circulation of at least a part of gases located in the working chamber, and at least one slat for flow directing of gases.
  • At least one outlet of the working chamber is connected with the inlet of at least one first cooler, which is provided with the outlet of the first cooler for first liquid fraction and with the gas fraction outlet, whereas the gas fraction outlet is connected with the inlet of at least one second cooler, which is provided with the first outlet of the second cooler for second liquid fraction and at least one second outlet of the second cooler for not liquefied residue.
  • the cooling zone there can be further located inside the working chamber the cooling zone, provided with cooling medium inlet and the cooling medium outlet.
  • the second cooling zone is alternatively located from inner side of the cover for closing of the lockable hole.
  • at least one tank for placing of the charge in the reaction zone is alternatively a part of the device.
  • the slats can at least partially surround the reaction zone. From inner side of the cover for closing the lockable hole the second cooling zone can be alternatively located.
  • working chamber is further provided with inlet of gas, which is connected with the second outlet of the second cooler for not liquefied residue, whereas with advantage there are located the auxiliary cooler and/or the desludger between the second outlet of the second cooler for not liquefied residue and the inlet of gas into the working chamber.
  • the second outlet of the second cooler for not liquefied residue can be connected with the inlet of the suction pump, the outlet of which is connected with the cogeneration unit and/or with the tank of not liquefied residue, whereas with advantage there are located the auxiliary cooler and or desludger between the second outlet of the second cooler for not liquefied residue and the inlet of the suction pump.
  • the first outlet of the second cooler for the second part of liquid fraction can be inducted under the level of the second liquid fraction, which is located in the sedimentation tank, which is advantageously connected through the overflow with the reservoir of the second part of the liquid fraction, and the outlet of the first cooler for the first part of liquid fraction can be inducted under the level of the first liquid fraction part, which is located in the settler.
  • the inlet of the cooling zone is connected to the outlet of cooling unit, namely advantageously through the first fan.
  • thermal decomposition of rubber and/or plastic is that the charge is equally heated so that there occurs no local overheating, which could result in releasing of such substances, which could not be subsequently liquefied and would have to be ecologically disposed, for example with combustion.
  • reaction zone cooling is quick termination of thermal decomposition, which enables opening of device interior without releasing of undesirable substances into atmosphere. If the reaction zone is cooled by air, which cannot mix with gases located in the reaction zone, no its contamination occurs and it can be released back into ambient atmosphere. Thanks decreasing of cooling time, increasing of the capacity of the device occurs.
  • Figures 1, 2, 5, and 6 in enclosed drawings refer to exemplary embodiment according to the example 1, whereas Figure 5 shows a diagram of the whole device in phase of thermal decomposition of the charge, and Figure 6 shows a diagram of the whole device in cooling phase.
  • Figures 1 and 2 represent in more detail this part of embodiment according to the example 1, in which thermal decomposition of the charge is carried out, whereas Figure 1 shows the section B - B from Figure 2, but with the inserted charge, and Figure 2 shows the section A - A from Figure 1, but without the charge.
  • Figures 3 and 4 are equivalents of Figures 1 and 2 according to the example 2, whereas Figure 3 shows the section D - D from Figure 4, but with the inserted charge, and Figure 4 shows the section C - C from Figure 3, but without the charge.
  • the device according to the example 1 is intended for thermal decomposition of rubber from used tires, which are processed without any previous treatment and which form the charge 9.
  • the device consists of the working chamber I 3 the walls 2 of which are provided with the thermal-insulating material 21.
  • the working chamber I is provided with the first outlet JJ . of pyrolytic gasses, the second outlet 15 of pyrolytic gases and with the lockable hole J2, which serves for filling the working chamber I with the charge 9 and for removal of not gasifiable residues.
  • the lockable hole 12 is closed in the course of thermal decomposition of the charge 9 with the cover 121.
  • the reaction zone 3 for placing the charge 9, heating elements 4, at least partially surrounding the reaction zone 3, the fan 5_ for assuring of circulation of gases, which have not been drawn off through the outlets H, 15 of pyrolytic gases until now and which are located in the working chamber 1, and the slats 6 for flow directing of circulating gases, which also surround the reaction zone 3.
  • the slats 6 are horizontally oriented and are fitted on the supporting structure 61.
  • the fan 5 is located above the reaction zone 3, is rotating on vertically oriented axis and is connected with the motor 5JL of fan located outside the working chamber 1.
  • the cooling zone 7, provided with the cooling medium inlet H and the cooling medium outlet 14.
  • This cooling zone 7 is delimited with the partition wall JO located in the working chamber 1 and the walls 2 of the working chamber 1. Furthermore, in the reaction zone 3 there are located supports 9J. for placing of tires, forming the charge 9.
  • the working chamber 1 is also provided with the inlet J6 of gas, through which cold gas is delivered in cooling phase, advantageously not yet liquefied residue of pyrolytic gases.
  • the outlets H, 15 of pyrolytic gases from the working chamber 1 are connected with the inlet 73 of the first cooler 79, which is provided with the outlet 72 of the first cooler 79 for first part of liquid fraction and the gas fraction outlet 77.
  • the gas fraction outlet 77 is connected with the inlet 24 of the second cooler 29.
  • the second cooler 29 is provided with the first outlet 23 of the second cooler 29 for second part of liquid fraction and the second outlet 22 of second cooler 29 for not liquefied residue.
  • the second outlet 22 of second cooler 29 for not liquefied residue is connected through the auxiliary cooler 42, through the first valve 421 and through the second fan 161 with the inlet 16 of gas into the working chamber I.
  • the outlet of the auxiliary cooler 42 is also connected with the inlet 311 of the suction pump H, namely through the second valve 422.
  • the outlet 312 of the suction pump 31 is connected with the cogeneration unit 4L
  • the cogeneration unit 41 there can be alternatively also to the outlet 312 of the suction pump 3_1 connected the reservoir for gas storage or the distribution pipeline to other gas appliances, in this case to appliances of not liquefied residue of pyrolytic gases.
  • the first outlet 23 of the second cooler 29 for second part of liquid fraction is inducted under level of the second part of liquid fraction, which is located in the sedimentation tank 52.
  • the sedimentation tank 52 is connected via the overflow 5_3 with the reservoir 62 of the second part of liquid fraction.
  • the outlet 72 of the first cooler 79 for the first part liquid fraction is inducted under level of the first liquid fraction, which is located in the settler 82.
  • the settler 82 For the purpose of assuring of sufficient level in the first part of the settler 82, the settler 82 is divided with the partition wall 83 of the settler 82 into two parts. The second part of the settler 82 is provided with the outlet hole 84- For the purpose of maintenance of the first part of liquid fraction in sufficient liquid state, the settler 82 is in contact with the heating element 8L
  • the inlet H of the cooling zone 7 is connected through the third fan 132 to the outlet of the cooling unit 100.
  • the first sensor 191 for monitoring of temperature and composition of pyrolytic gases is located.
  • the third sensor 193 for monitoring of temperature and chemical composition of gases is located, and in the reaction zone 3 of the working chamber I the second sensor 192 for temperature monitoring is located. All sensors 191. 192. 193. same as the fans 132, 161 and the valves 421, 422 are connected to a not shown control unit.
  • Method in accordance with the invention is carried out according to this example as follows. Used tires forming the charge 9 are put on the supports £1 for pacing tires, which are located in the reaction zone 3, which is a part of the working are. Afterwards, the working chamber 1 is closed with the cover 121, wherewith the working area is separated from ambient atmosphere. The working room, inclusive of the reaction zone, is stepwise heated with the heating elements 4. Starting with temperature 100 °C, rubber contained in tires begins to decompose. With the help of the fan 5, flow of a part of released gases is inducted by means of the slats 6 to the vicinity of heating elements, where heating of these gases to maximum temperature 600 0 C occurs. Flow of heated gases is directed through the slats 6 towards tires.
  • Gases drawn off from the reaction zone are subsequently cooled down in two phases, namely in the first phase to temperature in the range of 80 up to 100 0 C, namely at formation of the first part of liquid fraction and in the second phase to temperature about 20 0 C at formation of the second part of liquid fraction.
  • Not liquefied residue is sucked off, in the course of pyrolysis, from the second outlet 22 of second cooler 29 for not liquefied residue by means of the suction pump 31.
  • Capacity of the suction pump H is controlled on the basis of pressures, picked up with the first sensor 191 and the third sensor 193. whereas slight overpressure against ambient pressure is maintained in the working chamber.
  • Power input of the heating elements 4 is controlled on the basis of temperature picked up with the second sensor 192 for temperature monitoring.
  • Procedure of pyrolysis is monitored on the basis of chemical composition of pyrolytic gases with the first sensor 191 for monitoring of temperature and composition of pyrolytic gases.
  • the first part of liquid fraction obtained in the first cooler 79 is collected in the settler 82, which is maintained at the temperature above 80 0 C to prevent unwanted solidification of the first part of liquid fraction.
  • the second part of liquid fraction, obtained in the second cooler 29 ⁇ is collected in the sedimentation tank 52 and at its topping it overflows into the reservoir 62. Not liquefied residue is sucked off from the second outlet 22 of second cooler 29 for not liquefied residue by means of the suction pump 31 and is inducted into the cogeneration unit 4J . for further processing.
  • the heating elements 4 are turned off, and the interior of the working chamber 1, inclusive of the reaction zone 1 containing not gasified tire residues, is cooled down through air delivery from ambient atmosphere into the cooling zone 7, which is located between the reaction zone 2 and the thermal-insulating layer 2J_. Cooling air is not mixed with gases located inside of the working chamber 1. Interior of the working chamber 1 is further cooled down through not liquefied gases delivered with the second fan 161 from the second outlet 22 of second cooler 29 for not gasified residue through the auxiliary cooler 42 with desludger into the gas inlet 16 to the working chamber 1. So extraction of further heat from the reaction zone occurs. After sufficient cooling down of interior and complete condensation of substances, which are released from the charge, the chamber I is opened and not gasifiable residues are removed. The device is herewith ready for further usage.
  • the device according to the example 2 is intended for thermal decomposition of piece rubber and piece plastic. Plastics, which melt by heat effect can be used.
  • This device differs from the device described in the example 1 in that there are not, located in interior of the working chamber I x any supports 91 for pacing tires, on which the used tires could be placed, but the tanks 8 with piece charge 9 are located in the reaction zone 3.
  • the tanks 8 have a form of from above opened bathes, which are located above each other so that hot gases could be delivered to the vicinity of the charge 9, which is located in them.
  • the device according to the example 2 further differs from the device described in the example 1 in that the cover 121 is thermal- insulating and contains between its walls the cooling zone H of cover 121.
  • the cover ⁇ is provided with the cooling medium inlet 1.31 to the cover 121 and the cooling medium outlet 141 from cover 121, which runs into the cooling zone Zl of over 121.
  • the charge of plastic materials further contains matters facilitating depolymerization of plastic materials.
  • the invention can be utilized for thermal decomposition both, solid and meltable matters, namely also in case that such thermal decomposition is to be enabled or be conditioned with presence of catalytic agents or if it is to be induced through chemical reactions with other substances added to the charge.

Abstract

La charge contenant du caoutchouc et/ou du plastique est soumise à une température de 100 à 600 °C dans l’environnement séparé de l’atmosphère ambiante, alors qu’une partie de gaz dégagés est chauffée et est entraînée plusieurs fois à proximité de la charge. L’excès de gaz dégagés est retiré de la zone de réaction et est refroidi jusqu’à liquéfaction d’au moins une partie de fraction liquéfiable. Les résidus non liquéfiés sont traités dans l’unité de cogénération ou sont collectés dans le réservoir. Pour un achèvement plus rapide des actions de pyrolyse, il est avantageux, lors de la phase de refroidissement, d’entraîner les résidus non liquéfiés de gaz pyrolytiques dans la zone de réaction. Le dispositif contient la chambre de travail (1), dont les parois sont pourvues de l’isolation thermique. A l’intérieur de la chambre de travail (1) se trouve la zone de réaction (3) destinée à la mise en place de la charge (9), qui est partiellement entourée d’éléments de chauffage (4) et de becs destinés à l’orientation de l’écoulement gazeux. Au-dessus de la zone de réaction (3) se trouve en outre le ventilateur (5) destiné à assurer la circulation de gaz à l’intérieur de la chambre de travail (1). Une partie de la chambre de travail (1) est également la zone de refroidissement (7), séparée de la zone de réaction (3). La chambre de travail (1) est en outre pourvue de l’entrée (16) de gaz et de la sortie (11, 15) de gaz pyrolytiques, qui est reliée à l’entrée (73) d’au moins un premier refroidisseur (79). Le premier refroidisseur (79) est pourvu de la sortie (72) du premier refroidisseur (79) pour la première partie de fraction liquide et de la sortie de fraction gazeuse (77). La sortie de fraction gazeuse (77) est reliée à l’entrée (24) d’au moins un second refroidisseur (29), qui est pourvu de la première sortie (23) du second refroidisseur (29) pour la seconde partie de fraction liquide et d’au moins une seconde sortie (22) du second refroidisseur (29) pour résidus non liquéfiés. La seconde sortie (22) du second refroidisseur (29) pour résidus non liquéfiés peut être reliée par l’intermédiaire du refroidisseur auxiliaire (42) et/ou du nettoyeur à l’entrée (16) de gaz reliée à la chambre de nettoyage (1) et à l’entrée (311) de la pompe d’aspiration (31), dont la sortie (312) est reliée à l’unité de cogénération (41) et/ou au réservoir de résidus non liquéfiés. La première sortie (23) du second refroidisseur (29) pour la seconde partie de fraction liquide peut être entraînée sous le niveau de la seconde partie de fraction liquide, qui se situe dans la cuve de sédimentation (52), qui est avantageusement reliée par l’intermédiaire du déversoir (53) au réservoir (62) et la sortie (72) du premier refroidisseur (79) pour la première partie de fraction liquide peut être entraînée sous le niveau de la première partie de fraction liquide, qui se situe dans le décanteur (82). Il est également avantageux que l’entrée d’agent de refroidissement (13) de la zone de refroidissement (7) soit reliée à la sortie de l’unité de refroidissement (100), à savoir par l’intermédiaire avantageux du troisième ventilateur (132).
PCT/CZ2010/000079 2009-07-22 2010-07-19 Procédé et dispositif destinés à la décomposition thermique de caoutchouc et/ou plastique WO2011009419A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP20100766215 EP2456813A1 (fr) 2009-07-22 2010-07-19 Procédé et dispositif destinés à la décomposition thermique de caoutchouc et/ou plastique

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CZ20090473A CZ2009473A3 (cs) 2009-07-22 2009-07-22 Zpusob tepelného rozkladu pryže a/nebo plastu a zarízení k jeho provádení
CZPV2009-473 2009-07-22
CZ20090472A CZ2009472A3 (cs) 2009-07-22 2009-07-22 Zpusob získávání kapalné frakce z pyrolýzního plynu a zarízení k jeho provádení
CZPV2009-472 2009-07-22

Publications (1)

Publication Number Publication Date
WO2011009419A1 true WO2011009419A1 (fr) 2011-01-27

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Country Link
EP (1) EP2456813A1 (fr)
CA (1) CA2710657A1 (fr)
CZ (1) CZ2012116A3 (fr)
WO (1) WO2011009419A1 (fr)

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CN113827999A (zh) * 2021-10-09 2021-12-24 济南恒誉环保科技股份有限公司 一种裂解油气多级冷却净化装置

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CZ306376B6 (cs) * 2014-07-15 2016-12-28 Alpajar Group S.R.O. Způsob kontinuální výroby kapalných a plynných paliv z podílu organických látek v odpadech

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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
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EP1664240A1 (fr) 2004-02-18 2006-06-07 Technologie Ekologiczne Procede et dispositif pour la conversion continue de dechets organiques
WO2005100509A1 (fr) * 2004-04-09 2005-10-27 Maekawa Seisakujo Co., Ltd. Traitement de carbonisation intermittent et dispositif de fabrication de l'huile produite
EP1785248A1 (fr) 2004-04-26 2007-05-16 Krivoruchko, Evgeny Petrovich Procede de retraitement thermique de pneus uses et dispositif correspondant
WO2008069741A1 (fr) * 2006-12-05 2008-06-12 Bengt-Sture Ershag Réacteur pour pyrolyse et procédé pour charger et vider ledit réacteur
WO2008075105A1 (fr) * 2006-12-19 2008-06-26 Used Tyre Distillation Research Limited Système et procédé pour recycler des matériaux contenant du carbone
CA2584557A1 (fr) 2007-04-04 2008-10-04 Afab Financial Ltd. Systeme de pyrolyse ameliore pour dechets de caoutchouc
CZ17601U1 (cs) 2007-04-27 2007-06-11 Ochvát@Juraj Zarízení pro separaci pyrolýzního oleje pri zpracování odpadové pryze

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