WO2005028595A1 - Appareil et procede pour la production de gaz combustibles a partir d'une matiere organique - Google Patents

Appareil et procede pour la production de gaz combustibles a partir d'une matiere organique Download PDF

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Publication number
WO2005028595A1
WO2005028595A1 PCT/DK2004/000569 DK2004000569W WO2005028595A1 WO 2005028595 A1 WO2005028595 A1 WO 2005028595A1 DK 2004000569 W DK2004000569 W DK 2004000569W WO 2005028595 A1 WO2005028595 A1 WO 2005028595A1
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WO
WIPO (PCT)
Prior art keywords
gasses
reaction bed
section
organic material
air
Prior art date
Application number
PCT/DK2004/000569
Other languages
English (en)
Inventor
Thomas Koch
Original Assignee
Tk Energi A/S
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 Tk Energi A/S filed Critical Tk Energi A/S
Priority to EP04762790A priority Critical patent/EP1727879A1/fr
Publication of WO2005028595A1 publication Critical patent/WO2005028595A1/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
    • C10J3/58—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
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/0956—Air or oxygen enriched air

Definitions

  • the invention relates to an apparatus and a method for producing combustible gasses from an organic material and to a control unit for regulating said apparatus.
  • the invention relates to an apparatus, for producing combustible gasses from an organic material, comprising a pyrolysis section into which the organic material is fed and moved along while being exposed to heat in such a way that the organic material is decomposed at least into coke and gasses, a gas combustion section wherein the generated gasses are mixed with air and at least partially burnt in order to generate the heat necessary to thermally crack the remaining gasses, and a hot reaction bed section wherein the coke from the pyrolysis section is gasified.
  • organic refuse A major problem faced by today's society is how to get rid of organic refuse.
  • Some examples of typical organic refuse are e.g. plastic and rubber waste, straw from the agriculture industry, and wood chips from the forest industry.
  • Such types of organic refuse are typically mainly composed of fixed carbon and volatiles. This means that the refuse can be converted to combustible gasses and in this way be converted to useful energy.
  • the DE patent No. 672 921 discloses a vertically arranged apparatus for generating combustible gasses .
  • the apparatus consists of an outer combustion chamber and an inner reduction chamber, the inner reduction chamber being arranged inside the combustion chamber.
  • the inner and outer chambers are connected together at a lower area.
  • the outer and inner chambers are filled from above.
  • the outer chamber is filled with a bituminous fuel and the inner chamber is filled with a reducing fuel such as e.g. charcoal.
  • a reducing fuel such as e.g. charcoal.
  • the reducing fuel is heated by burning the bituminous fuel, whereby combustible gasses, which are discharged via a pipe at the top of the inner chamber, are generated.
  • This apparatus is not suitable for generating combustible gasses directly from the types of organic refuse mentioned earlier since there is no way of decomposing the refuse into the reducing fuel.
  • a simple apparatus for generating combustible gasses from organic refuses is known from the US patent No. 4,142,867.
  • This apparatus is shaped as a shaft, which during operation is filled with the organic waste materials from above.
  • the material is subjected to low-temperature carbonisation at temperatures between 300°C and 600°C in the absence of air.
  • the carbonisation residues and gasses are continuously drawn through a hot reaction bed at temperatures between 1000°C and 1200°C and converted to combustible gasses in reaction with preheated air supplied to the bed.
  • the useful yield of this apparatus is, however relatively low.
  • the organic material is, in this case, carbonised in a first stage via pyrolysis, by indirectly heating the organic material in the absence of air inside a rotating drum at a temperature between 300°C and 600°C.
  • the drum is heated by means of the exhaust gasses from a gas motor driven by the combustible gasses produced by the apparatus.
  • the hot gasses produced in the first stage are, in a second stage, mixed with preheated air and thermally cracked at temperatures between 850°C and 1200°C.
  • the gasses are then passed through a reaction zone comprised of the low carbonisation coke obtained during the first stage.
  • the gas mixture which initially has a temperature between 850°C and 1200°C, is sucked through said reaction zone of the low carbonisation coke, whereby the temperature is reduced due to the endothermic reaction in this zone.
  • the hot generated gasses together with the gasses from the second stage exchange heat, in a heat exchanger, with the air necessary for performing the processes of the apparatus .
  • the rotateable drum which provides for the pyrolysis of the organic material, is a relatively expensive part of the entire apparatus. Moreover it introduces a number of problems during the operation of the apparatus .
  • Another problem is that the sliding connection between the rotating drum and the surrounding jacket is rather difficult to keep airtight. This means that the poisonous exhaust gasses from the gas motor tend to leak out into the environment with the risk of injuring e.g. the operators of the apparatus.
  • a third problem is that heat content of the exhaust gasses from the gas motor does not always match the heat necessary for performing the pyrolysis in the rotating drum.
  • a fourth problem is that the apparatus is difficult to control .
  • an apparatus of the type mentioned in the opening paragraph is provided which has a simple and reliable construction.
  • an apparatus of the type mentioned in the opening paragraph which during operation produces a higher useful yield than known hitherto .
  • an apparatus of the type mentioned in the opening paragraph which is arranged in such a way that the organic material does not tend to agglomerate during the pyrolysis process .
  • an apparatus of the type mentioned in the opening paragraph which is able to operate without the risk of injuring e.g. the operators of the apparatus due to exhaust gasses from a gas motor.
  • an apparatus of the type mentioned in the opening paragraph is provided, which can be operated in such a way that the generated combustible gasses can optionally be used for any purpose.
  • an apparatus of the type mentioned in the opening paragraph is provided which is arranged for precisely generating the necessary heat for performing the pyrolysis process.
  • an apparatus of the type mentioned in the opening paragraph which is arranged such that all or nearly all of the coke is gasified in an independent endothermic process.
  • an apparatus of the type mentioned in the opening paragraph which is easy to control .
  • the new and unique way in which the current invention fulfills the above mentioned aspects is by presenting an apparatus for producing combustible gasses from an organic material, in which a pyrolysis section is arranged such that the heat necessary to decompose the organic material at least into coke and gasses is generated by partially burning the organic material while it is in motion upwards in said pyrolysis section.
  • the pyrolysis section itself generates the heat necessary for pyrolysis, the system becomes simpler and more reliable since fewer system components are required. Furthermore, due to the simplicity of the system and the reduced number of interacting components, the efficiency of the system is higher and a greater yield will be generated when compared to existing systems.
  • the apparatus can further comprise a feeder for forcing the organic material into the pyrolysis section via a material inlet arranged at a lower area of this section, and a first air inlet, for introducing the air necessary for the partial combustion of the organic material in the pyrolysis section, placed at a distance from the material inlet such that the temperature at the material inlet does not exceed the temperature which the feeder can withstand.
  • the partial combustion of the organic material in the pyrolysis section, and therefore the heat generated in the pyrolysis section, can be easily controlled, just by controlling the amount of air injected into the pyrolysis section.
  • the air, necessary for the partial combustion of the organic material can advantageously be introduced into the pyrolysis section at a distance from the material inlet and in such a quantity that the reaction along a first length of said pyrolysis section is exothermic and along a succeeding length endothermic.
  • the partial combustion of the organic material can be accurately controlled and kept to a limited area so that just enough heat is generated by the partial combustion so that the decomposition of the organic material into coke and gasses can proceed optimally in the remaining area of the pyrolysis section.
  • the apparatus can further comprise a second air inlet for introducing the air for partial combustion of the gasses in the gas combustion section.
  • the partial combustion of the gasses in the combustion chamber raises the temperature of the coke in order to provide the energy necessary for the highly endothermic reactions in the reaction bed. Injecting air is therefore a very accurate and simple method of controlling the temperature in the gas combustion section.
  • the apparatus can have a gas outlet for the gasses generated by the apparatus.
  • the gas can therefore easily be removed and used for any purpose.
  • the apparatus can further comprise a heat exchanger for transferring heat from the gasses output at the gas outlet to cold air input to the heat exchanger and supplying the warmed air to at least one of the air inlets of the apparatus. In this way, the heat in the produced gas can be reused and fed back into the apparatus. This increases the efficiency of the apparatus.
  • the apparatus can comprise a residue outlet placed at the bottom of the reaction bed section in order to allow residues like ashes and unburned constituents to be removed from the reaction bed, and a discharger for removing said residues from the residue outlet.
  • the top of the reaction bed can be placed at a distance from the residue outlet such that the residue layer, which forms at the base of the reaction bed, is able to isolate the discharger against harm due to the high heat present at the top of the hot reaction bed.
  • the apparatus can advantageously comprise a control unit for adjusting the level of the hot reaction bed by regulating a combination of the feeding, discharging, and air injection operations in response to signals received from a number of temperature sensors placed in successive levels in the walls at least around the combustion chamber and the hot reaction bed. Since the chemical reactions taking place in the reaction bed are endothermic, the temperature in the reaction bed drops rapidly from a maximum value located at the top of the reaction bed. Therefore by measuring the temperatures at different levels at the walls of the reaction bed and the gas combustion section, the location of the top of the reaction bed can be determined.
  • the pyrolysis section forms an acute angle with the other sections, said other sections extending in a mainly vertical direction in continuation of each other. In this way, the material is forced upwards against gravity through the pyrolysis section and then falls down through the other sections with the help of gravity.
  • Fig. 1 is a process flow diagram of the apparatus, showing the individual steps of the process.
  • Fig. 2 shows a schematic section view of the apparatus seen from the side.
  • Fig. 1 shows a process flow diagram of the individual sub processes which occur in an example embodiment of the apparatus according to the current invention.
  • the overall process can be broken down into three distinct sub processes.
  • organic material 1 at room temperature, is fed into the pyrolysis section 2 via a feeder 3.
  • heat is applied to the organic material 1 in order to reduce it to coke and gasses 4.
  • Some unusable components might also be generated due to impurities in the refuse material being decomposed.
  • the heat is generated by injecting hot air 5 into the pyrolysis section.
  • the hot air 5 causes a partial combustion of the organic material 1 to take place, which generates the heat necessary for pyrolysis.
  • the temperature reaches up to 1000°C or more.
  • the coke and gasses 4 progress up the pyrolysis section they cool down and are at a temperature of around 600°C when they exit the pyrolysis section 2.
  • the gasses 4 which exit the pyrolysis section 2 are at least partially combusted in the gas combustion section 9.
  • the gasses are partially combusted by adding heated air 10 to the gas combustion section 9.
  • the amount of air added into the combustion chamber is controlled in such a way that there will not be enough air for full combustion of the gasses. Therefore, a large percentage of the gasses passes through the gas combustion section 9 without combusting.
  • the temperature in the gas combustion section 9 is at around
  • the high temperature is necessary to thermally crack (refine) the complex carbon molecules in the gasses. Due to the high temperature the complex carbon molecules break down into smaller molecules. In addition, the high temperature heats up the coke in order to supply the energy for the highly endothermic reactions which occur in the reaction bed.
  • the coke which falls through the gas combustion section 9 is deposited in a reaction bed 12.
  • the reaction bed 12 is a heap of hot coke.
  • the gasses exiting the gas combustion section 9 are sucked through the reaction bed causing the gasification of the coke to take place, which generates combustible gasses 13.
  • the Q in the chemical equations above is energy.
  • the reactions are highly endothermic reactions, which is why the coke and gasses 11 need to be heated to such high temperatures in the gas combustion section 9.
  • the combustible gasses 13, generated in the reaction bed, are sucked through a heat exchanger 16 by a blower 17. Air 18 at ambient room temperature is blown through the heat exchanger 16 by a second fan 19. The heated air 20 is supplied to control valves 21 and 23, which inject the heated air 20 into the pyrolysis section 2 and the gas combustion section 9 respectively.
  • a controller 24 controls the process based on temperature sensors 25 mounted at the gas combustion section 9 and reaction bed 12.
  • the controller 24 controls the feeder 3, the discharger 15, the first fan 17, the second fan 19, and the control valves 21, 23 via control signals 26.
  • Fig. 2 shows a physical example embodiment of the apparatus according to the invention. The figure shows a schematic side view in section. The apparatus is built with steel walls 27 which sandwich a layer of insulation 28. This construction ensures that the apparatus is strong and insulated so that excess heat is not lost to the surrounding atmosphere.
  • the organic material 1 is inserted into the feeder 3.
  • the feeder 3 comprises a hopper 29, an electric motor 30, and a feed screw mechanism 31.
  • the feed screw mechanism 31 forces the organic material 1 into the pyrolysis section 2 at the material inlet 32.
  • the air injected into the pyrolysis section via the first air inlet causes a partial combustion of the organic material 1 to take place this raises the temperature around the first air inlet to around 1000°C.
  • Insulation 33a around the first air inlet 5 protects the apparatus from the high temperatures.
  • first air inlet 5 is placed at a distance from the material inlet 32, causes a "buffer" 34 of non burning material to exist between the material inlet 32 and the first air inlet 5. This protects the feeder 3 from damage due to the high temperatures .
  • the material As more material is forced into the material opening 32, the material is slowly forced upwards along the pyrolysis section 2. Since only a small amount of air is injected into the pyrolysis section 2, only a partial combustion of the material takes place. As the material moves away from the first air inlet, it stops combusting. However, due to the high heat still present in the pyrolysis section 2, the material decomposes into coke, gasses, and tar. The heat and gasses from the combustion occurring around the first air inlet 5, and the gasses produced from the decomposition of the material, bubble through the material on their way up the pyrolysis section and ensure that the material does not agglomerate. As the material passes up the pyrolysis section 2, the temperature falls from 1000°C to around 600°C. Once the material reaches the top of the pyrolysis section 2, the coke falls down through the gas combustion section 9 and lands on the reaction bed 12.
  • the gasses Due to the flow of the gasses in the apparatus, the gasses are drawn down through the gas combustion section 9. Heated air 20 injected into the gas combustion section 9 via the second air inlet 10 and the control valve ⁇ 23 cause a portion of the gasses to combust and generate high heat. The temperature of the gasses and the coke passing through the gas combustion section 9 rises to around 1200°C. Due to the high temperatures, an insulating liner 33b is placed around the gas combustion section. The insulating liner 33b extends also into the reaction bed 12.
  • the reaction bed 12 is a stack of hot coke.
  • the top of the reaction bed has a temperature of around 1200°C since it is heated by the gas combustion section 9.
  • the gasses in the apparatus are then passed through the reaction bed and sucked out of the reaction bed via the ring channel 35a and the gas outlet tube 35b.
  • the coke is gasified, it disappears leaving only a small amount of residues comprising mainly ash and some unburned components. These residues form a layer 36 at the bottom of the reaction bed 12 with a temperature of around 200°C.
  • a discharger 15, comprising an electric motor 37 and a screw mechanism 38 removes the bottom of the residues layer via the residue opening 39 at the bottom of the reaction bed.
  • the gasses output at the gas outlet tube 35b, are sucked through a heat exchanger 16 via a first fan 17.
  • a second fan 18 pumps ambient air, at around 20°C, into the heat exchanger 16.
  • the ambient air is heated up and used to supply the rest of the apparatus with heated air 20 of around 500°C.
  • a small amount of ash 40 is removed from the output gasses in the heat exchanger 16.
  • a cyclone (not shown) can be used together with the heat exchanger 16 if the gas is not very clean.
  • An example of an apparatus according to the invention had a pyrolysis section with a diameter of 400mm and a length of 2500mm.
  • the gas combustion section had a minimum diameter of around 1000mm.
  • the distance from the top of the gas combustion section to the bottom of the reaction bed was around 2000mm.
  • the reaction bed had a diameter of around 1500mm.
  • the reaction bed was regulated so that it was around 700mm high.
  • Wood chips were used as the organic material .
  • the wood chips used had an approximate chemical composition by weight of 45% carbon, 47% oxygen, 7% hydrogen, and 1% ash.
  • the gas produced had a combustion value of 4.8 MJ/kg at standard temperature and pressure.
  • the gas had an approximate chemical composition by weight of 22% CO, 9% C0 2 , 17% H 2 , 1% CH 4 , and 51% N 2 .
  • about 1kg of ash and 1kg of unburned components were produced.
  • the gas produced by an apparatus according to the current invention can be used for many purposes.
  • One example is as a fuel for a heating furnace (not shown) .
  • a heating furnace could be found in, e.g. a house, an manufacturing plant, or as a part of an industrial process.
  • Another example of how the gas could be used is as a fuel source for an internal combustion engine (not shown) .
  • the feeder 3 and the discharger 15 are shown as feed screws. It is also possible to use many other types of feeding and discharging devices.
  • One such example is a reciprocating piston mechanism (not shown) .
  • the apparatus is well suited as one component of a larger plant (not shown) .
  • wood chips are stored in a storage bin.
  • a feed screw transports the wood chips into a drier which removes excess water content from the wood chips. After being dried, the wood chips are deposited into the feeder 3 of the apparatus.
  • the final produced gas 13, once it leaves the heat exchanger 16, is still quite warm, typically around 400°C. It can therefore be cooled down in a further water/gas heat exchanger and then the cool gas can be passed through a bag filter, which removes the last of the ash and other impurities.
  • a blower pushes the cooled and cleaned gas to the desired gas consumer.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention a trait à un appareil et un procédé pour la production de gaz combustibles à partir d'une matière organique (1). L'appareil comporte d'abord une section de pyrolyse (2) dans laquelle la matière organique (1) est alimentée et déplacée tout en étant exposée à la chaleur de sorte que la matière organique (1) soit décomposée au moins en coke et en gaz. Le coke et les gaz sont ensuite alimentés dans une section de combustion de gaz (9) dans laquelle les gaz générés sont mélangés avec l'air et au moins partiellement brûlés en vue de générer la chaleur nécessaire pour le craquage thermique des gaz restants. Enfin, le coke est déposé sur une section de lit de réaction chaud (12) dans laquelle les cokes en provenance de la section de pyrolyse (2) sont gazéifiés. L'appareil est agencé de sorte que la chaleur requise pour la décomposition de la matière organique (1) est générée par la combustion partielle de la matière organique (1) alors qu'elle se déplace vers le haut dans ladite section de pyrolyse (2). Ainsi, on obtient un appareil simple et fiable présentant un rendement utile élevé et facile à contrôler.
PCT/DK2004/000569 2003-08-28 2004-08-27 Appareil et procede pour la production de gaz combustibles a partir d'une matiere organique WO2005028595A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP04762790A EP1727879A1 (fr) 2003-08-28 2004-08-27 Appareil et procede pour la production de gaz combustibles a partir d'une matiere organique

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DKPA200301230 2003-08-28
DKPA200301230 2003-08-28

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Publication Number Publication Date
WO2005028595A1 true WO2005028595A1 (fr) 2005-03-31

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011006789A3 (fr) * 2009-07-14 2011-06-23 Erwin Schiefer Réacteur et procédé de gazéification de biomasse
WO2015054710A1 (fr) 2013-10-17 2015-04-23 Hinterecker, Claus Dispositif et procédé de gazéification d'une matière première
DE102015000357A1 (de) * 2015-01-20 2016-07-21 Michael Artmann Vorrichtung und Verfahren zur Erzeugung von Produktgas aus kohlenwasserstoffhaltigem Vergasungsmaterial
WO2018007205A1 (fr) * 2016-07-06 2018-01-11 Basf Se Procédé de production parallèle de gaz de synthèse, de carbone, et de charbon résiduel à faible teneur en polluants à partir de lignite
CN111500302A (zh) * 2020-05-09 2020-08-07 济南大学 秸秆热解碳化设备

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DE29912277U1 (de) * 1999-07-14 1999-10-07 Hochreiter, Johann, 83530 Schnaitsee Vorrichtung zum Entgasen von organischen Substanzen
EP1207191A2 (fr) * 1994-12-01 2002-05-22 Mitsubishi Jukogyo Kabushiki Kaisha Gazéificateur à lit fixe et méthode de gazéification de déchets organiques
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Publication number Priority date Publication date Assignee Title
US4126519A (en) * 1977-09-12 1978-11-21 Edward Koppelman Apparatus and method for thermal treatment of organic carbonaceous material
DD135211A1 (de) * 1977-11-07 1979-04-18 Manfred Duerlich Verfahren und vorrichtung zur festbettvergasung von kohle
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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011006789A3 (fr) * 2009-07-14 2011-06-23 Erwin Schiefer Réacteur et procédé de gazéification de biomasse
WO2015054710A1 (fr) 2013-10-17 2015-04-23 Hinterecker, Claus Dispositif et procédé de gazéification d'une matière première
DE102015000357A1 (de) * 2015-01-20 2016-07-21 Michael Artmann Vorrichtung und Verfahren zur Erzeugung von Produktgas aus kohlenwasserstoffhaltigem Vergasungsmaterial
DE102015000357B4 (de) * 2015-01-20 2021-01-07 Michael Artmann Vorrichtung und Verfahren zur Erzeugung von Produktgas aus kohlenwasserstoffhaltigem Vergasungsmaterial
WO2018007205A1 (fr) * 2016-07-06 2018-01-11 Basf Se Procédé de production parallèle de gaz de synthèse, de carbone, et de charbon résiduel à faible teneur en polluants à partir de lignite
CN111500302A (zh) * 2020-05-09 2020-08-07 济南大学 秸秆热解碳化设备

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