EP3219777A1 - Procede et installation pour la transformation de matériaux combustibles dans des gaz purifiés sans goudrons - Google Patents

Procede et installation pour la transformation de matériaux combustibles dans des gaz purifiés sans goudrons Download PDF

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Publication number
EP3219777A1
EP3219777A1 EP16202784.1A EP16202784A EP3219777A1 EP 3219777 A1 EP3219777 A1 EP 3219777A1 EP 16202784 A EP16202784 A EP 16202784A EP 3219777 A1 EP3219777 A1 EP 3219777A1
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EP
European Patent Office
Prior art keywords
chamber
combustion
reactor
pirolysis
anoxic
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Application number
EP16202784.1A
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German (de)
English (en)
Inventor
Ivan Bordonzotti
Giuseppe Antonioli
Francesco Berti
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Individual
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Individual
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Publication date
Priority claimed from CH01796/15A external-priority patent/CH711859A2/it
Priority claimed from ITUB2015A006873A external-priority patent/ITUB20156873A1/it
Application filed by Individual filed Critical Individual
Publication of EP3219777A1 publication Critical patent/EP3219777A1/fr
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/30—Fuel charging devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • 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
    • F23G5/20—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having rotating or oscillating drums
    • 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

Definitions

  • the present invention concerns the field of the transformation of combustible materials.
  • the present invention concerns a plant for the transformation of combustible materials in tar-free clean gas.
  • the present invention further concerns a proceeding for transforming of combustible materials in tar-free clean gas.
  • the present invention concerns the field of proceedings and of the plants used for transforming combustible materials based on molecules containing at least carbon and hydrogen (such as for example biomasses, municipal waste, plastics, tires, car fluff, ..) in clean combustible gas and inert residual.
  • molecules containing at least carbon and hydrogen such as for example biomasses, municipal waste, plastics, tires, car fluff, ..
  • the clean combustible gas can be obtained thanks to known processes of pyrolysis, gasification or pyrogasification also if, however, the quality of products, in particular regarding the produced gas, is usually so unsatisfactory that it requires before its use complex treatment systems.
  • the best proceeding carried out according to the known technique consists in a first phase of pyrolysis followed by a phase of gasification and/or of combustion.
  • the punctually required heat in the process is generated through combustion (oxidation) of a part of the combustible (material) to be treated or of a part of products generated by it.
  • the plant aforementioned does not allow to obtain a process of creation of gas without the production of tars.
  • the incombustible part of gasified material due to the high temperatures that exist into the zone (1800°C and more), blend and collect on the bottom of the chamber of gasification where they are then extracted, always in the liquid state, through a siphon that has the scope of keeping insulated the inner from the environment.
  • the inert liquids that exit from the siphon are then vitrified through water hardening.
  • the material to be treated is directed through an inlet 4 provided with means suitable for ensuring its watertight integrity respective to the surrounding environment.
  • a supply equipment 5 that conveys the material (arrow B) toward the inner of a pirolysis reactor, constituted by a sheathed rotating drum 2, walls thereof are touched by fumes of combustion that go through the space comprised between said rotating drum 2 and a chamber 3 thermally insulated that contains it, exiting (arrow C) through an exhaust conduit 13.
  • These fumes release much of their heat to the pirolysis reactor 2, within which the material to be treated, reaching temperatures around 400-500°C, undergoes a process of pyrolysis transforming itself into into gas and char.
  • oxides in the final residual is dangerous because some metals if oxidized transform into toxic réelles; for example the chrome, that if oxidized, can transform in hexavalent chrome.
  • One of thes problems is the fusion of the ashes, due to the high temperatures reached by the process of oxidation and that causes damages, premature wear or malfunctions of the involved equipments.
  • the presence of oxygen promotes the fusion of the ashes also thanks to its participation to the formation of low-melting substances such as glass starting from sodium, potassium and silica.
  • the document WO 2015/049659 shows a device with rotating chamber of gasification wherein in the process there are two additions of oxidizing agents: a mix of gasifying agents in the gasifier and air of combustion in the burner. It is therefore a plant with indirect pyrolysis. It is excluded the direct contact between the fumes of combustion and the char to be gasified. This causes a less clean production of combustible gases, and affects therefore the overall efficiency of the plant.
  • the document WO 2015/084193 shows that the solid fraction of material is gasified with air.
  • US 4,881,947 shows a plant of gasification with conical rotating reactor heated through radiant tubes, wherein pyrolysis and gasification take place at the same time in the reactor itself.
  • Said waste material still has significant carbon rates and does not have the possibility to further react with the gas, reducing therefore the overall efficiency of conversion of combustible materials into tar-free gas.
  • the residual product is still a char, and not an ash.
  • the scope of the present invention is to describe a plant and a process that permit to solve the aforementioned drawbacks.
  • the scope of the present invention is realized by means of a plant and a process that are totally without oxidative processes both of solid material at the inlet of the plant, and of any other flow of material solid created during the process of working in the plant.
  • the plant of the present invention can advantageously operate also on poor coals, at low heating value, operating a complete gasification of the carbon in carbon dioxide and a partial oxidation of the carbon in carbon monoxide.
  • a plant for transforming combustible materials into clean tar-free gas comprising:
  • said plant comprises furthermore a supplying hopper positioned exiting from said pirolysis reactor and wherein said first inlet means comprise a supplying auger of char, positioned to a height lower than said supplying hopper.
  • said second inlet means of said chamber of anoxic decarburization are positioned to a height lower than said first inlet means of said chamber of anoxic decarburization.
  • At least said first inlet means are configured for insulating an inlet of said chamber of anoxic decarburization.
  • said flow generation chamber has the particularity of geometrically being an extension of the first chamber sharing with it the external walls and being separated from it through a septum partition.
  • said plant comprises furthermore a dust eliminating filter installed in correspondence of a terminal portion of an outlet conduit that is positioned on the top of the hopper.
  • said first chamber comprises an exhaust of fumes, and wherein said exhaust comprises furthermore thermal exchanger.
  • said thermal exchanger preheat and/or dry said combustible material upstream of the inlet within said pirolysis reactor.
  • said gas of combustion within said first chamber have a content of oxygen always higher than zero and typically comprised between the 3% and the 15%.
  • said first zone is a zone interposed between said nozzles and said burner.
  • said method comprises a step of positioning of second inlet means in said chamber of anoxic decarburization to a height lower than said first inlet means.
  • said method comprises a step of filtering of pyrolysis gases produced from said pirolysis reactor upstream of their said burning within said flow generation chamber.
  • burning said pyrolysis gases, within said first chamber are produced combustion gases within said first chamber, and said combustion gases have a content of oxygen always higher than zero and typically comprised between 3% and 15%.
  • said pyrolysis gases are burnt generating two separate flows of combustion, wherein a first flow of combustion contains oxygen and is directed towards said first chamber and a second flow of combustion, that is absolutely oxygen-free and is directed toward said second inlet means to the anoxic decarburization unit.
  • said second flow is obtained from a mixing step of said gas of combustion produced in said first chamber with a fraction or part of said pyrolysis gases.
  • said pyrolysis gases are introduced in said chamber for a quantity at least sufficient for consuming, through its combustion, the oxygen contained in said gases of combustion used in the mixing.
  • the pyrolysis unit receives the combustible material that is subjected to the proceeding of pyrolysis.
  • the material to be treated is heated, in absence of oxygen, up to temperatures comprised about between 400 and 800°C, maintaining it in those conditions for a time enough to cause the complete transformation into gas, vapors of condensable substances (called tars) and char.
  • the char is composed by a combustible and energetic fraction, essentially carbon, and by a non-combustible part the composition thereof depends by the material supplied to the plant.
  • the incombustible part of the char is composed by minerals and other material while treating unsorted waste into the composition of the incombustible part there are also metal and glass.
  • the char generated in the unit of pyrolysis is then transferred to an anoxic decarburization unit to the end of energetically enhancing the carbon contained in said char and at the same time obtaining a residual of lower mass possible and totally non combustible.
  • anoxic decarburization is intended therefore a process of removal of the carbon in absence of oxygen.
  • the fusion of the ashes is avoided thanks to the absence of oxygen and thanks ot the fact that this is a endothermic process (that absorbs heat).
  • the maximum temperature reached in the process is the one of the decarburizing flow, better explained hereinafter, generated and controlled with precision into the flow generation chamber. For this reason in the unit of decarburization cannot formed, not even locally, zones with excessive temperatures and such to cause the fusion of the ashes.
  • This combustible gas is the main product of the proceeding and has, as better further described, the particularity of being absolutely free from condensable substances (tars) making it suitable for being used, after filtration and cooling, in motors or gas turbines or basic substance for chemical syntheses.
  • the flow generation chamber is an essentialteil of the system, making the proceeding possible in its entirety as well as giving innovative character to the system considered as a whole.
  • the plant 10 object of the present invention there are mainly three elements, physically united between them and inseparable: the unit of pyrolysis, the flow generation chamber and the anoxic decarburization unit.
  • the combustible material to be treated is directed toward the plant 10 (arrow A) through an inlet 40 provided with means (rotary feeders, double guillotines, double clapper, etc.) suitable for ensuring water tightness respective to the surrounding environment.
  • the plant Downstream to said inlet 40 the plant comprises a supplying equipment 50 or power supply, that conveys the material (arrow B), by means of an auger, pusher pistons or equivalent technical means system, toward the inner of a pirolysis reactor.
  • the pirolysis reactor comprises a rotating drum 20 sheathed and partially lying in a chamber 30 thermally insulated (first chamber); the wall of the rotating drum 20 is touched by fumes of combustion that go through the space comprised between said rotating drum 20 and a first chamber 30 thermally insulated that contains it, exiting (arrow C) through an exhaust conduit 130.
  • the rotating drum is defined partially lying within the first chamber 30 thermally insulated, even if some ending portions of said drum are on the outside.
  • the plant 10 object of the present invention comprises also an outlet conduit 60 for the exiting (arrow E) of pyrolysis gases or pyrogas.
  • the char for effect of the rotation of the rotating drum 20 (that optionally but preferably can be combined with an opportune inclination of its longitudinal axis, even if in the present invention it is possible also a horizontal configuration as schematically shown in figure 2 ), moves (arrow D) towards a hopper 90 wherein it lies (arrow F) and from which it is extracted through an extraction means 70 (rotary feeders, double guillotines, double clapper, etc.) suitable for ensuring a perfect division of the atmosphere existing upstream and downstream of itself and that in detail can bring to the decarburisation into the chamber that will be subsequently described also as vacuum.
  • the extraction means 70 is followed (arrow G) by a transport auger 80 that supplies directly a chamber 100 of anoxic decarburization of fixed type.
  • the plant 10 object of the present invention comprises also a dust removal filter 180 installed in correspondence of a terminal portion of the outlet conduit 60 that is positioned on the top of the hopper 90; downstream of said dust removal filter, the plant 10 object of the present invention comprises also a fan 160.
  • the pyrolysis gases exiting from said outlet conduit 60 is dedusted in the dust removal filter 180 (for example of inertial type, with metallic or ceramic braid), aspirated by means of the fan 160 and, through conducts 170, directed (arrow J) to the flow generation chamber 140, that is fixed.
  • the dust removal filter 180 for example of inertial type, with metallic or ceramic braid
  • the dust retained by the dust removal filter 180 mainly composed by fine particles of char moved by the pyrolysis gases, is extracted with known means (not indicated in the annexed figures).
  • the flow generation chamber 140 has the particularity of geometrically being an extension of the first chamber 30 sharing with it the external walls and being separated from it only by the divisor septum 190, this last provided with openings in number, size and position such as to subdivide the gas flow that moves here (arrow K) in a suitable way and ensure the sufficient heating of the pirolysis reactor 20 and the correct distribution of the heat on the its surface.
  • Another particular aspect is the fact that the flow generation chamber 140 itself is then directly connected also to the chamber of anoxic decarburization 100 fixed , thus creating, with the first chamber 30, a sole complete assembly, designed to reduce at the minimum the path of heated flows (at temperatures comprised between about 1200 and 1800°C and anyway preferably over 1000°C to the end of obtaining a correct heating of the pirolysis reactor and an efficient anoxic decarburization) generated into the flow generation chamber 140 and sent to the other two chambers thus limiting the thermal losses and avoiding the use of conducts that, as it is known by the experts in the art are of complex realization.
  • the size of the flow generation chamber 140 are anyway such that to ensure sufficient residing times for the material such that to have a completion of the chemical reactions that then take place.
  • the pyrolysis gas is distributed into the chamber of generation flows 140 in two different zones, controlling the subdivision of the flow through the adjustment valves 200.
  • a part of the gas is burned in conditions of air excess in the burner 210 previously mentioned.
  • Said burner 210 is in detail positioned at the top of the flow generation chamber 140, preferably laying on a side of itself in correspondence of a divisor septum 190 that separates said flow generation chamber 140 by the overlaying first chamber 30.
  • a resting part of gas is directly injected in flow generation chamber 140 through the nozzles 220 located between the burner 210 and the connection to the chamber of anoxic decarburization 100.
  • Part of fumes generated in the burner 210 heat the rotating drum 20 through the openings with which it is provided with the divisor septum 190 (arrow K).
  • THE fumes necessary to the heating of the pirolysis reactor must have a well defined temperature to the end of ensuring the desired heat exchange and remaining at the same time under the limits of temperature of use of materials of the rotating drum 20.
  • the adjustment of the temperature of fumes takes place, as the technicians of the sector know, by acting on the air excess set to the burner 210.
  • the fumes of combustion obtained will therefore have a tenor of oxygen always higher than zero (typically between the 3 and the 10%) and the function of the desired temperature.
  • the fraction of fumes not used for the heating of the rotating drum 20 passes through the flow generation chamber 140 (arrow M) reacting then with the gas flow injected through the nozzles 220 (arrow L).
  • the oxygen contained in the flow of fumes deriving from the burner 210 is consumed due to the combustion of the pyrolysis gases injected through the nozzles 220 into the flow generation chamber 140 underlying the first chamber 30 thermally insulated.
  • the resulting flow, free from oxygen and with a very high temperature (1200-1800°C) is then conveyed (arrow H) to the chamber of anoxic decarburization 100.
  • the distribution of the gas between the burner 210 and the nozzles 220 is such as that the flow resulting from the interaction of two is absolutely free from oxygen. Practically, the flow of gas injected through the nozzles 220 must be, as defined by the experts in the art, stoichiometric (quantity of gas exact for consuming all the available oxygen) or slightly over-stoichiometric (quantity of gas excessive respective to the available oxygen).
  • THE tars normally present in said pyrolysis gases are completely removed during the process of combustion.
  • the flow generation chamber 140 In other terms, into the flow generation chamber 140 generate two flows of fumes of combustion, both composed by nitrogen, carbon dioxide and water (under the form of vapor), but with the particularity that one of them contains also oxygen while the second one is free from it.
  • an equipment of distribution 80 that in the preferred shape of embodiment described and here shown is an auger conveyer and represents the first inlet means for the chamber of anoxic decarburization.
  • a chamber of anoxic decarburization fixed advantageously permits a better chemical reaction between the gas flows deriving from the flow generation chamber 140 and the material present into the chamber 100 of anoxic decarburization. This is in detail true even if the supply of said chamber 100 of anoxic decarburization takes place from bottom.
  • the gas flows produced by the flow generation chamber 140 pass through therefore the material posed into the chamber 100 of anoxic decarburization from bottom up (arrows Z) in a substantial stasis condition of the material.
  • the char present into the chamber of anoxic decarburization and that already is undergoing the process of gasification with the flows deriving from the flow generation chamber 140 is progressively covered by new char transported by the transport auger 80 and gradually that the process of anoxic decarburization takes place, falls into the direction substantially detected by the force of gravity, toward the bottom of the chamber itself, from which it is progressively extracted.
  • said char deposits on the bottom of the chamber of anoxic decarburization 100, of thermo-insulated type, where, reacting with the gas flow generated and deriving (arrow H) from the chamber of generation of gas 140 consumes losing the carbon contained transforming so itself in an incombustible residual then removed (arrow I) by the chamber of anoxic decarburization 100 by means of an equipment of extraction 120 of a known type, for example of the auger type as shown in figure 2 , combined with a system of watertight exhaust 150 (rotary feeders, double guillotines, double clappers, etc.) that separates the inner atmosphere of the chamber 100 of anoxic decarburization from the external environment.
  • a system of watertight exhaust 150 rotary feeders, double guillotines, double clappers, etc.
  • the chamber of anoxic decarburization 100 has first inlet means represented by the equipment of distribution 80 and second inlet means that are represented by the conduct present between the flow generation chamber 140 and the portion lower than of the chamber of anoxic decarburization itself.
  • the chamber of anoxic decarburization operates therefore in a controlled atmosphere, along the chain of distribution of the char and extraction of the residual through the means 120, in a controlled atmosphere.
  • said chamber of anoxic decarburization 100 has said second inlet means to a height lower than respective to said first inlet means. This advantageously allows for optimizing the flow of the pyrolysis gases reburned, exiting from the flow generation chamber, respective to the char that falls into the chamber of decarburization deriving from the equipment of distribution 80, ensuring a more complete and efficient decarburization.
  • the equipment of extraction 120 is activated and adjusted to the end of keeping constant the level of the bed of char into the chamber 140; level controlled with known equipments (such as propeller or ultra-sonic level-switches, etc.) not indicated in the figures.
  • the combustible fraction of the char is essentially composed by carbon that is consumed into the chamber of anoxic decarburization 100 by the carbon dioxide and by the water (under the form of vapor) contained in the heated gas flow (arrow H) deriving from the flow generation chamber 140 transforming itself in combustible gases that comprise at least carbon monoxide and hydrogen thanks to endothermic chemical reactions.
  • the final composition of the combustible gas produced by the plant will be a mix composed mainly by nitrogen, carbon dioxide, carbon monoxide, hydrogen and water (at the state of vapor) with concentrations of single compounds depending both by the composition of the beginning combustible solid material and by times and temperatures applied in the proceeding.
  • heated gas flow deriving from the chamber of generation of gas 140 is in quantity sufficient to complete the reactions of decarburisation; the residual is therefore free from unburned materials, since free from carbon.
  • the combustible gas obtained free from condensable substances (tars) since they are absent both in the char and in the gas flow at the inlet of the chamber of anoxic decarburization 100, exits passing countercurrent through the bed of char (arrow N) and the upper free part of the chamber itself where, for effect of the reduction of speed, looses for decantation a good part of the displaced dusts.
  • the gas is then extracted from the plant (arrow O) through a conduit 110, arranged in correspondence of the top of the said chamber of anoxic decarburization 100.
  • the advantages of the plant object of the present invention are clear on the light of the description that precedes.
  • said plant allows for producing residual solid free from combustible substances (called unburned materials) that, further than signifying an energetic loss, increase their mass and the cost of the eventual disposal.
  • This producing clean combustible gas, that can be used without further steps of treatment in applications such as motors or turbines, wherein it is burned for generating traction and/or mechanic couple or electricity.
  • the plant object of the present invention can therefore advantageously be defined a direct pyrolysis plant, wherein there is a direct contact between the fumes and the char to be gasified.
  • said plant allows for having finally residuals without oxidized metals, since they are produced by anoxic proceedings; this allows for avoiding the plurality of residuals - such as for example the hexavalent chromium- that can be strongly toxic. Therefore, the plant object of the present invention is also characterized by an environmental friendliness greater respective to the past.
  • the efficiency deriving from the absence of oxidized metals derives in that the construction of the plant 10 permits to have a total absence of oxidative processes into the decarburating part of the process. Furthermore, this process allows for avoiding the creation of fused ashes.
  • the carbonization does not take place downstream of the gasification, and in detail does not take place in presence of overheated vapor and this permits a true and proper decarburization in absence of oxidants, and preferably, under vacuum.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Processing Of Solid Wastes (AREA)
EP16202784.1A 2015-12-09 2016-12-07 Procede et installation pour la transformation de matériaux combustibles dans des gaz purifiés sans goudrons Withdrawn EP3219777A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH01796/15A CH711859A2 (it) 2015-12-09 2015-12-09 Procedimento ed impianto per la trasformazione di materiali combustibili in gas pulito esente da catrami.
ITUB2015A006873A ITUB20156873A1 (it) 2015-12-09 2015-12-09 Procedimento ed impianto per la trasformazione di materiali combustibili in gas pulito esente da catrami.

Publications (1)

Publication Number Publication Date
EP3219777A1 true EP3219777A1 (fr) 2017-09-20

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EP16202784.1A Withdrawn EP3219777A1 (fr) 2015-12-09 2016-12-07 Procede et installation pour la transformation de matériaux combustibles dans des gaz purifiés sans goudrons

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020074943A1 (fr) * 2018-10-11 2020-04-16 Business Growth S.A. Installation de traitement des déchets multi-composants
US11220644B2 (en) 2017-10-12 2022-01-11 Danmarks Tekniske Universitet Method for reducing the tar content in pyrolysis gas

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4881947A (en) 1988-06-28 1989-11-21 Parker Thomas H High efficiency gasifier with recycle system
WO1995021903A1 (fr) 1994-02-15 1995-08-17 Crg Kohlenstoffrecycling Ges.Mbh Procede de generation de gaz combustible
EP0976806A1 (fr) 1998-07-30 2000-02-02 Thermoselect Aktiengesellschaft Appareil pour la mise en oeuvre du recyclage à haute température de déchets hétérogènes et procédé de chargement
EP1122296A2 (fr) * 2000-02-03 2001-08-08 Chugoku Maintenance Co., Ltd. Procédé et dispositif pour la récupération de ressources à partir de substances organiques
US20070163176A1 (en) 2005-07-28 2007-07-19 Choren Industries Gmbh Process and apparatus for the endothermic gasification of carbon
CH697942B1 (it) 2005-10-07 2009-03-31 Solenia S A Procedimento e impianto per la trasformazione di materiali organici in gas e carbone.
WO2015049659A1 (fr) 2013-10-03 2015-04-09 Eni S.P.A. Incinérateur de déchets boueux par pyrolyse et gazéification et procédé associé
WO2015084193A1 (fr) 2013-12-04 2015-06-11 Get Energy Prime Italy Srl Réacteur de traitement de déchets polyvalent

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4881947A (en) 1988-06-28 1989-11-21 Parker Thomas H High efficiency gasifier with recycle system
WO1995021903A1 (fr) 1994-02-15 1995-08-17 Crg Kohlenstoffrecycling Ges.Mbh Procede de generation de gaz combustible
EP0976806A1 (fr) 1998-07-30 2000-02-02 Thermoselect Aktiengesellschaft Appareil pour la mise en oeuvre du recyclage à haute température de déchets hétérogènes et procédé de chargement
EP1122296A2 (fr) * 2000-02-03 2001-08-08 Chugoku Maintenance Co., Ltd. Procédé et dispositif pour la récupération de ressources à partir de substances organiques
US20070163176A1 (en) 2005-07-28 2007-07-19 Choren Industries Gmbh Process and apparatus for the endothermic gasification of carbon
CH697942B1 (it) 2005-10-07 2009-03-31 Solenia S A Procedimento e impianto per la trasformazione di materiali organici in gas e carbone.
WO2015049659A1 (fr) 2013-10-03 2015-04-09 Eni S.P.A. Incinérateur de déchets boueux par pyrolyse et gazéification et procédé associé
WO2015084193A1 (fr) 2013-12-04 2015-06-11 Get Energy Prime Italy Srl Réacteur de traitement de déchets polyvalent

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11220644B2 (en) 2017-10-12 2022-01-11 Danmarks Tekniske Universitet Method for reducing the tar content in pyrolysis gas
WO2020074943A1 (fr) * 2018-10-11 2020-04-16 Business Growth S.A. Installation de traitement des déchets multi-composants

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