WO2014012651A1 - Gazéification à contre-courant/co-courant de substances riches en carbone - Google Patents

Gazéification à contre-courant/co-courant de substances riches en carbone Download PDF

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Publication number
WO2014012651A1
WO2014012651A1 PCT/EP2013/002094 EP2013002094W WO2014012651A1 WO 2014012651 A1 WO2014012651 A1 WO 2014012651A1 EP 2013002094 W EP2013002094 W EP 2013002094W WO 2014012651 A1 WO2014012651 A1 WO 2014012651A1
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WO
WIPO (PCT)
Prior art keywords
bulk material
gas
process chamber
vertical process
column
Prior art date
Application number
PCT/EP2013/002094
Other languages
German (de)
English (en)
Inventor
Leonhard Baumann
Roland Möller
Original Assignee
Ecoloop Gmbh
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 Ecoloop Gmbh filed Critical Ecoloop Gmbh
Priority to EP13752581.2A priority Critical patent/EP2875102A1/fr
Publication of WO2014012651A1 publication Critical patent/WO2014012651A1/fr

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Classifications

    • 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
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • 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
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Definitions

  • the present invention relates to a process for the production of synthesis gas by gasification of carbon-rich substances using bulk material as the reaction surface.
  • a method of the aforementioned type is known from AT 387 786 B, which describes the use of a self-oxidized, circulated bulk material.
  • CONFIRMATION COPY From DE 40 30 644 Al a method for producing combustible gases is known, in which a gas conversion is provided in a moving coke bed.
  • a moving coke bed For the after-treatment of synthesis gases, which are produced in accordance with DE 10 2007 062 414 A1, a moving coke bed has proved unsuitable.
  • Countercurrent gasifiers with a bulk reaction moving bed exhibit excellent mass transfer between the individual phases of the reactants, so that in particular also reactions between the solid phase and the gas phase allow energetically highly efficient embodiments of such gasification processes.
  • the main disadvantage of countercurrent gasifiers is that the achievable maximum gas temperature at the upper gas outlet is limited by the preheating of the above introduced solids. This usually only temperatures of 400 ° C can be realized. This usually leads to the fact that the quality of the gaseous reaction products is diminished by not fully gasified oil and tar shares and also undesirable condensation of such by-products in the upper gas space and in the gas exhaust pipes occur.
  • the countercurrent gasifiers are usually followed by a second gasification stage, which ensures the thermal decomposition of the oil and tar components at significantly higher temperatures, which are in some cases above 1000.degree.
  • a second gasification stage which ensures the thermal decomposition of the oil and tar components at significantly higher temperatures, which are in some cases above 1000.degree.
  • two-stage gasification processes are extremely expensive and usually have unsatisfactory thermal efficiencies.
  • the object of the present invention is therefore to improve processes of the type described above so that the gaseous reaction products can be obtained in an energy-efficient manner as high-quality synthesis gas in high gas yield and free of oil and tar fractions.
  • This object is achieved in a method of the type mentioned by the fact that the gasification in a first stage in a first vertical process space in a first from top to bottom moving column of bulk, which are added to the carbon-rich substances before entering the first vertical process space with oxygen-containing gas is carried out by Partialo idation in countercurrent and passed the resulting gaseous products in a second vertical process space, and in a second stage cocurrent with oxygen-containing gas in a second moving from top to bottom bulk column after increasing the temperature, and in the lower Part of the vertical process space, are deducted, being used as bulk material in the second column of bulk wholly or partially inert substances.
  • the bulk material acts as a reaction surface on which such oil and tar-like substances form a condensation and evaporation equilibrium, whereby an extension of the average residence time of such substances in the post-gasification zone is achieved.
  • the physical properties of the inert material components are retained over the entire bulk material column.
  • the bulk material Because of its inert substance content, it also acts as an energy buffer and ensures an almost ideal energy distribution. This ensures a very efficient thermal decomposition of the oils and tars.
  • the moving bulk material column acts as the first dust separation stage in the gasification, wherein the dust separated from the gas phase can be very easily discharged from the post-gasification together with the bulk material by the migrating bulk material column.
  • the first bulk material column and / or the second bulk material column are formed from bulk material having a particle size of up to 30 cm.
  • This coarse-grained bulk material ensures ideal gas permeability, energy distribution and very good mass transfer in both process chambers.
  • the bulk material in the first column of bulk material and / or the second bulk material column consists wholly or partly of alkaline substances, for example of lumpy calcium oxide, and / or this alkaline substances, such as lumpy calcium oxide and particularly preferably powdered calcium oxide and / or calcium hydroxide are admixed.
  • the use of calcium oxide has proved to be advantageous, since this substance has catalytic properties which promotes the thermal decomposition of oil and tar-like cracking products and at the same time acts as a pollutant binder.
  • chlorine and sulfur compounds for example, chemically bound to the calcium, while heavy metals bind physically to the active upper calcium oxide ⁇ surface of the.
  • an oxidation zone is formed in which the pyrolysis coke produced in the upper process zone zones is oxidized, thereby supplying the necessary energy to the process.
  • this is equipped with a support firing, which is operated by burner lances with fuel and with oxidizing gas.
  • the gasification takes place in the first vertical process chamber by adding air and / or technical oxygen as the oxidizing gas, the air or oxygen quantity being adjusted such that a total lambda of less than 1 is preferred over all stages of the gasification in the process space less than 0.7, and more preferably less than 0.5.
  • the gasification in the vertical process space takes place in the presence of steam and calcium oxide and / or calcium carbonate and / or calcium hydroxide.
  • This is a calcium-catalyzed reforming of substantial proportions of the resulting oil and / or tar-containing cleavage products having a chain length greater than C4, to carbon monoxide, carbon dioxide and hydrogen at temperatures above 400 ° C is performed.
  • a temperature increase which is conducive to the post-gasification in the vertical process space is achieved via burner lances in the upper gas space and / or further down in the bulk material column, the burner lances being operated with oxygen or oxygen-containing gas.
  • the temperature increase can also take place in such a way that the temperature is already reached in the vertical process chamber via Nerlanzen done in the upper gas space and / or in the transition to the upper gas space of the process space, which burner lances are operated with oxygen or oxygen-containing gas.
  • the withdrawn gaseous reaction products can be cooled after filtration at least partially via a heat exchanger, and the resulting condensates are separated at temperatures below 100 ° C.
  • the withdrawal of the gaseous reaction products is preferably carried out by means of a gas delivery device, which is preferably connected downstream of the heat exchanger.
  • the countercurrent carburetor or the vertical process chamber is equipped at the lower end with a cooling zone, in which cooling gas is introduced from below.
  • Oxygen-containing gas for example air
  • syngas can also be used after cooling has taken place.
  • water can additionally be used as cooling and / or gasifying agent in the cooling zone of the vertical process chamber.
  • the bulk material from at least one of the two bulk solids columns is withdrawn batchwise or continuously by means of metering devices from the respective vertical process chamber.
  • Preferably turntable discharge systems can be used here, which allow a uniform and continuous withdrawal of the bulk material from the process spaces.
  • the withdrawn bulk material from the first and / or the second bulk material column are discharged via vertical Pitot tubes, in which by means of level controls a minimum damming height is maintained, being ensured by the pressure loss, a gas seal against the outside atmosphere.
  • the bulk material from the bulk material column, after exiting the pitot tube, can be separated by physical separation methods, preferably by sieving and / or screening, into different particle fractions, and preferably the fine fraction containing bound contaminants, at least partially removed from the process.
  • the resulting coarse fraction can be used at least partially as bulk material in at least one of the two vertical process spaces.
  • a very efficient cycle process can be formed, whereby the additional demand for supplied fresh bulk material can be reduced to a minimum.
  • the bulk material from the secondary gasification or from the second bulk material column can be cooled countercurrently by introducing synthesis gas purified by dust separation and cooling into the lower part of the vertical process chamber.
  • this cooling of the second column of bulk material can also take place by indirect cooling before exiting the pitot tube by means of cooling water and / or by means of an indirectly cooled conveying section operated with cooling water after leaving the pitot tube.
  • the bulk material from the second bulk material column can be separated by physical separation methods, preferably by screening and / or screening in different grain fractions, and preferably the fine fraction containing bound pollutants from the process, at least partially discharged.
  • the resulting coarse fraction can be at least partially reused as bulk material in at least one of the two vertical process spaces
  • the bulk material from the second bulk material column can be used at least partially directly and using the sensible heat as additional bulk material via a separate metering in the first vertical process space.
  • FIG. 1 shows a preferred embodiment of the method according to the invention for the gasification of carbon-rich substances.
  • a mixture of carbon-rich substances (A) is in coarse-shaped form and a grain size of less than 30 cm a first vertical process chamber (1), which is designed as a countercurrent carburetor, fed from above via a vertical Schurre (2).
  • These carbon-rich substances before entering the countercurrent carburetor (1) coarse bulk material (3), for example, lumpy calcium oxide, admixed.
  • alkaline substances (4) preferably fine-grained calcium oxide are added to the bulk material bed before entering the vertical process space (1).
  • the mixture (5) of carbon-rich substances, lumpy calcium oxide and alkaline substances flows through the vertical process space (1) by gravity from top to bottom.
  • the flow rate of the bulk material is controlled by means of a metering device (6), which is at the lower end of the first vertical process chamber (1) and can be formed, for example, as a turntable discharge system.
  • This metering device conveys the bulk material into a pitot tube (7) at the lower outlet of the process chamber (1), in which the accumulated material ensures its own pressure loss for a gas seal to the atmosphere.
  • the countercurrent carburettor has burner lances (8) in the central region, which provide for base load firing in the vertical process space and for the stationary formation of an oxidation zone (9). These burner lances can be operated with fossil fuels (10) and oxygen-containing gas (11). As an alternative to fossil fuels, synthesis gas from the process can also be used.
  • oxygen-containing gas for example air
  • This gas is used initially for cooling the bulk material before leaving the vertical process space (1) in a cooling zone (14), wherein the oxygen-containing gas is simultaneously heated to above 800 ° C, and used in the oxidation zone (9) as a gasification agent.
  • introduced amount of oxygen-containing gas is adjusted so that sets a total lambda of preferably less than 0.5 in the vertical process space.
  • the oxygen continues to decrease, so that finally only can take place smoldering to CO, to even all the oxygen is used up earlier and finally a reduction zone (15) is developed with a completely reductive conditions.
  • the provisions in the re- production zone first a drying of the possibly moist feed materials up to a temperature of 100 ° C instead. Thereafter, the actual temperature of the materials continues to increase, so that the gasification process of the plastics contained in the carbon-rich substances, for example, also begins and at an autogenous temperature of up to 500 ° C, the formation of methane, hydrogen and CO begins.
  • the intrinsic temperature of the materials continues to increase due to the hot gases rising from the oxidation zone (9), so that the carbon-rich materials are finally completely degassed and consist only of residual coke, the so-called pyrolysis coke, and ash components.
  • the pyrolysis coke is transported further with the bulk material in the vertical process space (1) down to where it at temperatures above 800 ° C in the lower part of the reduction zone (15) with the C0 2 shares from the oxidation zone (9) by Boudouard conversion at least partially converted to CO. Part of the pyrolysis coke also reacts in this zone according to the water gas reaction with water vapor, which is also contained in the hot gases, to form CO and hydrogen.
  • Residues of pyrolysis coke are finally oxidized in the oxidation zone (9) with the oxygen-containing gas at temperatures below 1800 ° C and used thermally.
  • the bulk material moving bed together with the remaining ash portions, reaches the cooling zone (14).
  • cooling zone (14) and water (16) via water lances (17) can be metered as another cooling and gasifying agent.
  • the synthesis gas formed in the vertical process space is aspirated (18) at the upper end, so that a slight negative pressure is preferably established in the upper gas space (19) of the vertical process space (1).
  • the extracted synthesis gas contains dust, which consists essentially of the solid salts of halogens, fine-grained alkaline substances, other pollutants and inert particles. Furthermore, the synthesis gas still contains incompletely gasified oil and tar-like organic cracking products. To completely gas these, the dust, oil and tar-containing synthesis gas in the gas space (19) of the vertical process chamber (1) or after leaving the vertical process space at
  • the treatment of the synthesis gas in the presence of steam and fine-grained calcium oxide at temperatures of above 400 ° C in a downstream second vertical process chamber (20) is provided, in which the synthesis gas in DC through a moving from top to bottom
  • the bulk material column (21) is guided.
  • the bulk material column (21) can also be formed by coarse bulk material (22), for example lumpy calcium oxide.
  • coarse bulk material (22) for example lumpy calcium oxide.
  • alkaline substances (23) preferably fine-grained niges calcium oxide or calcium hydroxide of the bulk material column (21) are admixed.
  • the bulk material column (21) flows through the vertical process chamber (20) by its own gravity from top to bottom.
  • the flow rate of the bulk material is controlled by means of a metering device (24), which is installed at the lower end of the vertical process space (20) and can be designed, for example, as a turntable delivery system.
  • This metering device conveys the bulk material into a pitot tube (25) at the lower outlet of the process chamber (20), in which the accumulated material ensures its own pressure loss for a gas seal to the atmosphere.
  • the treatment of the synthesis gas may preferably be carried out by using direct firing into the synthesis gas via burner lances (26) operated with oxygen-containing gas (27).
  • burner lances can be installed, for example, in the gas space (19) of the process space (1) or else in the feed line (18) to the process space (20).
  • the use of such burner lances is particularly advantageous when they are installed in the gas space (28) or also further down in the area of the bulk material column (21) of the process space (20).
  • the dust-containing synthesis gas (29) is then at Tem ⁇ temperatures above 300 ° C via a hot gas filtration (30) freed from dust.
  • the halogen-containing filter dust (31) is discharged from the process.
  • the resulting synthesis gas (32) is virtually halogen-free and is cooled by means of a gas cooler (33) and freed from condensates.
  • the resulting condensate (34) can be at least partially used again as a cooling and gasifying agent over the water lances (17) in the vertical reaction space.
  • the synthesis gas cooled in the gas cooler (33) is drawn off from the second process chamber (20) at (29) via gas filter (30) and gas cooler (33) by means of gas compressor (35) and then conveyed to further thermal or material utilization (12) ,
  • the bulk material mixture emerging at the lower end of the first vertical reaction space (1) via the pitot tube (7) contains essentially coarse-grained bulk material, residues of ash and fine-grained calcium oxide.
  • the fine sieve fraction (40) contains residues of ash, bound pollutants and fine-grained calcium oxide.
  • the remaining fine fraction is discharged from the process.
  • An embodiment of the method is that industrial oxygen as oxygen-containing gas at (11) inserted ⁇ is set. As a result, a particularly high-calorie synthesis gas can be generated.
  • the burner lances (8) are operated so that the amount of oxygen-containing gas (11) is used more than stoichiometrically based on the fuel (10). At the same time, in this case, cold synthesis gas (41) is used as the cooling gas in the cooling zone (14).
  • the synthesis gas flowing into the oxidation zone (9) from the cooling zone (14) is at least partially incinerated, forming further carbon dioxide and water vapor.
  • the heat of reaction liberates the energy required for the gasification process.
  • the amount of synthesis gas is adjusted in such a way that on the one hand the bulk material moving bed in the cooling zone (14) is completely cooled down and residual embers are extinguished, and on the one hand a high proportion of the necessary process energy is covered by the synthesis gas.
  • the bulk material mixture emerging at the lower end of the vertical reaction space (20) via the pitot tube (25) contains essentially coarse-grained bulk material, residues of ash and fine-grained calcium oxide.
  • This bulk material can be used without cooling by using its sensible heat directly at (42) as additional bulk material in the vertical process chamber (1).
  • the bulk material can also be cooled by means of indirect cooling with cooling water or air.
  • the fine sieve fraction (46) contains residues of ash, bound pollutants and fine-grained calcium oxide.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)

Abstract

L'invention concerne un procédé permettant de produire du gaz de synthèse par gazéification de substances riches en carbone en utilisant des matières en vrac comme surface de réaction. Ladite gazéification est réalisée, selon une premier étape, dans une première chambre verticale de réaction (1) au sein d'une première colonne de matières en vrac (5) pouvant se déplacer d'en haut vers le bas, les substances riches en carbone (A) y étant ajoutées avant qu'elles n'atteignent la première chambre verticale de réaction (1), par oxydation partielle à contre-courant en mettant en œuvre un gaz contenant de l'oxygène. Afin de pouvoir récupérer les produits gazeux de la réaction d'une manière économe en énergie, avec un rendement élevé en gaz, et sous forme d'un gaz de synthèse de haute qualité lequel est exempt de constituants huileux et bitumineux, les produits gazeux obtenus selon l'invention sont introduits, au sein de la zone supérieure, dans une deuxième chambre verticale de réaction (20) pour réaliser, selon une deuxième étape, dans une colonne de matières en vrac (21) pouvant se déplacer d'en haut vers le bas, une gazéification ultérieure à co-courant en mettant en œuvre un gaz contenant de l'oxygène et en augmentant la température, puis pour soutirer lesdits produits d'une zone (29) située plus en bas de la chambre verticale de réaction (20).
PCT/EP2013/002094 2012-07-18 2013-07-15 Gazéification à contre-courant/co-courant de substances riches en carbone WO2014012651A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP13752581.2A EP2875102A1 (fr) 2012-07-18 2013-07-15 Gazéification à contre-courant/co-courant de substances riches en carbone

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102012014161.0A DE102012014161A1 (de) 2012-07-18 2012-07-18 Gegenstrom-/Gleichstrom-Vergasung von kohlenstoffreichen Substanzen
DE102012014161.0 2012-07-18

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Publication Number Publication Date
WO2014012651A1 true WO2014012651A1 (fr) 2014-01-23

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PCT/EP2013/002094 WO2014012651A1 (fr) 2012-07-18 2013-07-15 Gazéification à contre-courant/co-courant de substances riches en carbone

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EP (1) EP2875102A1 (fr)
DE (1) DE102012014161A1 (fr)
WO (1) WO2014012651A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016030001A1 (fr) * 2014-08-26 2016-03-03 Ecoloop Gmbh Procédé de craquage de substances contenant du carbone et de l'hydrogène

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102017102789A1 (de) 2017-02-13 2018-08-16 Ecoloop Gmbh Herstellung von Synthesegas aus kohlenstoffreichen Substanzen mittels eines Gleichstrom-Gegenstrom-Verfahrens

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT387786B (de) 1984-03-22 1989-03-10 Waagner Biro Ag Verfahren zur vergasung von kohlenstoffhaeltigen materialien
DE4030644A1 (de) 1990-09-25 1992-03-26 Sanhog Technik Dr Ing Horst Ga Verfahren zur erzeugung brennbarer gase mit anschliessender gasumwandlung in einem bewegten koksbett
WO2002046332A2 (fr) * 2000-12-08 2002-06-13 Luterek, Janusz, Franciszek Procede et generateur de gaz destines a la production de gaz de combustion
EP1371713A1 (fr) * 2001-01-18 2003-12-17 Japan Science and Technology Corporation Appareil de gazeification d'un combustible solide
WO2007102032A2 (fr) * 2006-03-07 2007-09-13 Lampros Elefsiniotis Unité de gazéification combinée à deux étages à cocourant/contre-courant
WO2008107727A2 (fr) * 2007-03-06 2008-09-12 Lampros Elefsiniotis Gazogène à trois phases et lit fixe, qui comprend une zone tampon du courant gazeux entre la zone de pyrolyse et la zone de combustion
DE102007062414A1 (de) 2007-12-20 2009-07-02 Conera Process Solutions Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
WO2009080297A1 (fr) * 2007-12-20 2009-07-02 Ecoloop Gmbh Procédé et dispositif pour le retraitement de gaz d'échappement contenant du co2

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT387786B (de) 1984-03-22 1989-03-10 Waagner Biro Ag Verfahren zur vergasung von kohlenstoffhaeltigen materialien
DE4030644A1 (de) 1990-09-25 1992-03-26 Sanhog Technik Dr Ing Horst Ga Verfahren zur erzeugung brennbarer gase mit anschliessender gasumwandlung in einem bewegten koksbett
WO2002046332A2 (fr) * 2000-12-08 2002-06-13 Luterek, Janusz, Franciszek Procede et generateur de gaz destines a la production de gaz de combustion
EP1371713A1 (fr) * 2001-01-18 2003-12-17 Japan Science and Technology Corporation Appareil de gazeification d'un combustible solide
WO2007102032A2 (fr) * 2006-03-07 2007-09-13 Lampros Elefsiniotis Unité de gazéification combinée à deux étages à cocourant/contre-courant
WO2008107727A2 (fr) * 2007-03-06 2008-09-12 Lampros Elefsiniotis Gazogène à trois phases et lit fixe, qui comprend une zone tampon du courant gazeux entre la zone de pyrolyse et la zone de combustion
DE102007062414A1 (de) 2007-12-20 2009-07-02 Conera Process Solutions Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
WO2009080297A1 (fr) * 2007-12-20 2009-07-02 Ecoloop Gmbh Procédé et dispositif pour le retraitement de gaz d'échappement contenant du co2

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016030001A1 (fr) * 2014-08-26 2016-03-03 Ecoloop Gmbh Procédé de craquage de substances contenant du carbone et de l'hydrogène

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DE102012014161A1 (de) 2014-02-20
EP2875102A1 (fr) 2015-05-27

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