EP2231829A1 - Gazéificateur et procédés de gazéification l'utilisant - Google Patents

Gazéificateur et procédés de gazéification l'utilisant

Info

Publication number
EP2231829A1
EP2231829A1 EP08702378A EP08702378A EP2231829A1 EP 2231829 A1 EP2231829 A1 EP 2231829A1 EP 08702378 A EP08702378 A EP 08702378A EP 08702378 A EP08702378 A EP 08702378A EP 2231829 A1 EP2231829 A1 EP 2231829A1
Authority
EP
European Patent Office
Prior art keywords
zone
ash
gasifier
air
syngas
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.)
Withdrawn
Application number
EP08702378A
Other languages
German (de)
English (en)
Inventor
Omer Salman
Coskun Mancuhan
N. Selen Tanner
Akin Yildiz
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Gep Yesil Enerji Uretim Teknolojileri Ltd Sti
Original Assignee
Gep Yesil Enerji Uretim Teknolojileri Ltd Sti
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 Gep Yesil Enerji Uretim Teknolojileri Ltd Sti filed Critical Gep Yesil Enerji Uretim Teknolojileri Ltd Sti
Publication of EP2231829A1 publication Critical patent/EP2231829A1/fr
Withdrawn legal-status Critical Current

Links

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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • 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
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • This invention is related to a gasifier which is used to recover gas from waste by thermally processing the waste and is also related to gasification methods using this gasifier. Specifically, this invention is related to gasification methods realized using this gasifier in which switching between downdraft and updraft modes can be realized without any interruptions according to the feedstock material introduced and the gas recovered , for which the gasification realized under vacuum conditions with high efficiency.
  • WO2007/081296 which belongs to the owner of the present application, it is disclosed that ash and tar production is high in circulating bed up/downdraft gasifies compared to fix bed up/downdraft gasifiers. During the suction of the gas, partially unprocessed feedstock will come out along with and the pyrolytic operation will not be proper. In addition to that, since the unprocessed feedstock will leak from the gasifier, full process may not be realized.
  • One of the objects of this invention is to provide modular solutions instead of huge plants at geographical areas where the access is difficult by processing in an environmentally sound manner the refuse -derived -fuel (RDF) obtained from waste including hazardous, industrial and municipal waste.
  • RDF refuse -derived -fuel
  • Another object of this invention is to let the smooth transfer between modes without interrupting the process. Therefore energy, labor and time saving is realized via the invented gasifier and the gasification method.
  • Another object of this invention is to obtain a gasifier and a gasification method which decreases pollution in the output gas and increases the hydrogen content.
  • Another object of this invention is to obtain a gasifier and a gasification method which prevent the solidification of feedstock and clinker formation within the reactor and provides continuous gas production.
  • Incineration It is the combusting process of municipal solid waste at a temperature of 1200-1600 0 C within full oxygen environment. Some of the differences between gasification and incineration are:
  • the incineration process mainly forms carbon monoxide and vapor. These are waste gases and are let into the atmosphere. However, the syngas formed in gasification process is mainly formed of hydrogen and carbon monoxide gases. The syngas is not a waste gas. This can be used in burners, in gas turbines or in internal combustion engines for electrical energy production.
  • Incineration forms complex molecules containing poisonous materials such as dioxins and furans. Whereas gasification transforms complex molecules into gases with simpler molecule formation and prevents the formation of poisonous compounds such as dioxins and furans.
  • Pyrolysis It is the thermal degradation of solid waste at 500-600 0 C and in no oxygen containing environment.
  • the syngas formed mainly contains hydrogen, carbon monoxide, carbon dioxide, methane and tar including complex hydrocarbons. This gas mixture can be used in burners for burning purposes, in gas turbines and internal combustion engines for electrical energy generation or coal and active carbon production.
  • Figure 1 is the general outlook of the plant in which the gasifier and gasification method according to this invention are used
  • Figure 2 shows the schematic cross section of the gasifier working in updraft mode.
  • Figure 3 shows the schematic cross section of the gasifier working in downdraft mode.
  • Figure 4 shows the schematic cross section of the ash pool of this invention.
  • the present gasifier (1) comprises a scale (9.2)
  • a bottleneck zone (2) that comprises a double sliding valve (9) and a rotating valve
  • a drying zone (3.1) located under the bottleneck zone (2) with a diameter bigger than the bottleneck zone comprising a higher syngas outlet zone (3.2), a safety valve (11), a level indicator (12), an inspection glass (12.1), a sliding cover (12.2), a thermocouple (13.2), a pressure forwarder (14), a pressure meter in syngas outlet zone, a proportional valve (19) and a hydraulic piston (21);
  • a pyrolysis zone (4) located under the drying zone (3) comprising a preheated air and oxygen inlet (4.1), air nozzles (4.4), a vibrator (10), a thermocouple (13.1), liquid hazardous waste injection nozzles (20), a proportional valve for hazardous liquid waste (20.1);
  • a cambered oxidation zone (5) comprising top air nozzles (4.2), bottom air nozzles
  • a reduction zone (6) interior surface of which is covered with refractory material to prevent heat dissolvement comprising upper air nozzles (4.5), lower air nozzles (4.6), an air chamber (4.8), lower preheated air or oxygen inlet (6.2), proportional valve (6.4) for air or oxygen inlet, an ash grate (7.1) at the gas outlet zone for creating centrifugal effect, vapour nozzles (7.2) for increasing the carbon monoxide and hydrogen amount to enrich syngas, an igniter (8.1), igniting system (10.1) for the arc formation, a thermocouple (13.3), a vapour proportional valve (15) for regulating the vapour percentage;
  • an ash section (7) comprising ash discharger (7.3), an ash pool (22), a first threaded carrier (22.1) to convey big particles from ash discharger into the ash pool, a second threaded carrier (22.2), an ash carrying palette (22.3);
  • a precooler and scrubber system placed between the gasifier reactor and fan and comprising a cyclone, syngas vapor exchanger, a gas cleaning scrubber and an electro static precipitator at least one fan (24); and valves (17,18).
  • the gasifier permits the switching between downdraft and updraft modes without any interruption during the gasification process according to the feedstock material and the gas produced.
  • the gasifier (1) contains the an ash section (7) and at least one ash discharger in order to create centrifugal effect, at least one ash pool (22), at least one first threaded carrier (22.1) which conveys big particles coming from ash discharger into ash pool, at least one second threaded carrier (22.2), at least one ash carriage palette (22.3), at least one dry ash pool (22.4).
  • the second carrier (22.2) axially rotates and carries small particles of ash accumulated at the bottom and popped to the surface through the ash carrying palette (22.3) into the dry ash pool (22.4).
  • the double sliding valve (9) located at the bottleneck zone prevents the leakage and moves horizontally back and forth reciprocally. It is formed of two valves located as one on top of the other one and which is driven by a hydraulic piston. .
  • the RDF level in the gasifier (1) needs to be supervised by the operator and this can be done thru ultrasonic voiced level indicator (12).
  • ultrasonic voiced level indicator (12) In order to control the RDF, there is an optional high heat and vacuum resistant window (12.1).
  • the sliding cover (12.2) used for protecting the inspection window is formed in a single sliding cover system and prevents the pollution of the inspection window by tar gases and explosions of gas in the gasifier (1).
  • the sliding cover (12.2) is opened when there is high vacuum in gasifier (1) and thus it helps to extract the tar gases in the drying zone (3).
  • the inspection window (12.1) is located at the same place with the level indicator.
  • the security valve (11) is used to prevent damage in the system for when there is a sudden pressure increase in the system and when there is gas accumulation at the drying zone at the pyrolysis (4) and drying zones of the gasifier (1) and when the gas can not find a path to outflow from the system.
  • the thermocouple (13.2) located in the drying zone is used to transmit the heat information in this zone to the supervision room.
  • the pressure meter (14, 14.1, 14.2) in the drying zone is used to check the vacuum power applied by the fan (24).
  • the pressure meter (14.1) used during downdraft mode indicates the pressure of the syngas outlet.
  • the other pressure meter (14.2) is used for the same purpose in the updraft mode.
  • FIG. 1 The important portion of the gas is formed in the pyrolysis zone (4) .
  • the syngas is brought to its desired condition, cleaned and reducted for its further processing.
  • this zone ()4 is the oxygen free combustion zone. At the lack of oxygen the partial combustion reactions are realized here.
  • the vibrator (10) located in the pyrolysis zone vibrates when the RDF flow is not proper.
  • thermocouple (13.1) is used to transmit the heat information in the pyrolysis zone (4) to the supervision room.
  • the hazardous waste spraying nozzles (20) are used to feed the hazardous waste into the gasifier (1). Sprayed liquid hazardous waste is completely mixed with the reactions and increase the syngas efficiency within the pyrolysis zone (4).
  • the proportional valve (20.1) is used to feed the liquid hazardous waste into the gasifier in defined quantities.
  • the next zone within the gasifier where the gas is processed is the oxidation zone (5).
  • Air nozzles (4.2), lower air nozzles (4.3) for the downdraft working mode are located in the gasifier (1), and first air nozzles (4.3, 4.2) for downdraft mode and second air nozzles (4.5,4.6) for updraft mode are activated.
  • the upper air nozzles (4.5) are located in an angular manner to lower air nozzles (16).
  • the distance between the two air nozzles are defined according to the RDF properties and the ash quantity.
  • the gap between the two air nozzles (4.2 and 4.3) forms the first oxidation zone (5). In this zone the heat and the carbon monoxide formation is high.
  • the air nozzles (4.2 and 4.3) are made of high heat resistant high alloy stainless steel located separately from each other and parallel to the gasifier bed (1) so that they do not get clogged. Not all air nozzles can be activated at the same time.
  • the air chamber (4.7) is active whereas for updraft mode, the air chamber (4.8) is active.
  • Air entering from either (4.1) or from left or right air valves (6.2) can circulate through all of the nozzles (4.2, 4.3).
  • the air nozzle (4.4) located at the upper side of the pyrolysis zone(4) for the downdraft mode is designed and located there to fix the level at the oxidation zone (5) and the pyrolysis zone (4).
  • the Bouduard reactions are realized in the reduction zone (6) of the gasifier during the downdraft working mode. Active carbon content high materials such as ash and tar are found.
  • the reduction reactions are completed in this zone (6) for the syngas sucked from pyrolysis zone (4), tar gas and the carbondioxide.
  • the syngas, the gas mixture formed in pyrolysis zone (4) are directed to the reduction zone (6) and reducted when it is passing thru the tar and ash mixture.
  • the ash needs to be discharged during the catalytic cracking reactions when the tar quantity is lowered and the ash content is high. Ash discharge timing is directly related to the retention time of the RDF in the reduction zone (6). There is the thermocouple (13.3) to transmit the heat information from this zone to the supervision room.
  • the gasifier is positioned on a 50-70° angle to the ground so that oxidized RDF in tar and ash form can easily flow downward to the reduction zone.
  • the parts active at the reaction zone (6) are upper air nozzles (4.5), lower air nozzles (4.6), air chamber (4.8), lower preheated air or oxygen inlet (6.2), proportional valve (6.4) for air or oxygen inlet, ash grate (7.1) at the gas outlet zone for creating centrifugal effect, vapour nozzles (7.2) for increasing the carbon monoxide and hydrogen quantity to enrich syngas, igniter (8.1), igniting system (10.1) for the arc formation, thermocouple (13.3), vapour proportional valve (15) to regulate vapour rate, refractory material inside the zone (7.4) to prevent heat dissolvement.
  • the air flow into the air chamber (4.8) is regulated via the proportional valve (6.4) for air or oxygen inlet into the gasifier (1) during the updraft working mode and the valve (17) is opened to create vacuum.
  • the ash formed in the reduction zone (6) follows the ash path (7.3) and is discharged to ash system (22) thru the ash carrier.
  • the first threaded carrier (22.1) carries the big particulate ash from the water trap into the dry ash pool (22.4).
  • the second threaded carrier is used to carry accumulated and suspended ash to the dry ash pool (22.4).
  • the ash pallet (22.3) carries the bottom accumulating ash to the second threaded carrier (22.2). In order to decrease the ash content in the ash pool (22), dry ash pool that contains dehydrated ash.
  • the ash discharge system is trapped into the pool with water in order to prevent the air leakage into the reduction zone (6) since there is vacuum effect in the gasifier (1).
  • the inner holes of the ash grate (7.1) located in the ash part of the reduction zone are made out of high alloy stainless steel and the syngas formed in and moving from the pyrolysis zone (4) passes thru it.
  • This grate (7.1) has catalytic effect on reduction process to provide more effective and simpler reactions.
  • the active carbon rich tar kept by the grate (7.1) provides smooth flow of the syngas and carbon dioxide mixture. During this flow the catalysis effect of the grate takes place and both the carbon dioxide and methanization reactions are completed.
  • the particles carried by the syngas formed in and carried from the pyrolysis zone (4) are dissolved on the grate (7.1) due to the catalytic effect and the syngas is conveyed to have the catalytic cracking by passing through these grates (7.1) by a centrifugal effect.
  • RDF form to the system and lets the water to evaporate in the drying zone (3) and sucked into the reduction zone (6) by the vacuum effect and creates water gas effects and this is considered as the vapour resource.
  • the third one is through the controlled suction of vapor from the ash pool at the ash discharge system thru the vacuum by causing the water vapour phase balance impaired.
  • the vapour resulting from these three sources especially the one resulting from the vapour nozzles (7.2) complete the hydro cracking reactions since it is sucked by the char in the carbonated ash after the pyrolytic process.
  • the hydrogen and carbon monoxide increases by promoting the gas combination.
  • the gasifier is placed on a flexible wire (10.1) as a support in order to prevent loose joints and deformations on the gasifier (1) when it is working at high heat and vibration is applied. Thus, when the vibration is applied, the complete reactor shakes and joints do not loosen.
  • RDF is weighed and passed thru the bottleneck (2).
  • the RDF meets for the first time the heat in oxygen free environment in the bottleneck zone (2).
  • the heat is appropriate for dehydrating the RDF that increases hydrogen with gasification.
  • the vacuum inside the gasifier provides safe working conditions and the suction power of the fan (24) is just sufficient to provide gasification process continuity.
  • Syngas pre-cooling and scrubbing unit (23) is also the same for both modes.
  • the outlet syngas from the gasifier is precooled and cleaned.
  • use of the vapor exchanger creates the difference from conventional systems.
  • the organic gases containing energy (CO-CH4-C2H4-C3H8) face sudden temperature decrease in scrubber and they are let in water with tar, so the energy in the gas is highly lost.
  • Without the vapor exchanger integration it is not possible to protect the syngas and to obtain an efficient gas after the scrubber.
  • the heat is decreased in vapor exchanger without destroying the energy content in the organic gas.
  • the particles are taken away without destroying the energy content in the organic gases.
  • the gas combination proceeds after scrubber once its tar and solid particles are removed.
  • the particles and tar formed in the pyrolysis zone are not filtrated and not reducted and that is how they are sucked because in updraft form, the syngas is not passing thru the ash and the feeding is realized in shorter period. Therefore less clean syngas is sucked from the system compared to the downdraft mode.
  • the syngas zone (3.1) is activated during the updraft form.
  • the valve (17) is opened for the updraft mode.
  • the proportional valve (6.4) is opened and proportioned according to the fed material in order to create vacuum in the gasifier.
  • the gas continues upwards to the outlet (3.2) under vacuum. However, since the tar gas formed in the pyrolysis zone (4) is also sucked and the syngas moves without being reducted.
  • the zone which is 10 cm. away from the oxidation zone lower air nozzles (4.5,4.6) is the pyrolysis zone.
  • the valves (18 and 6.3) are fully closed.
  • igniters (8.1) are ignited and they are turned off after the ignition.
  • the igniters (8.1) are located at each air chamber (4.7 and 4.8).
  • igniters are located symmetrically to each other in air chamber (4.8). It is important to ignite them mutually at the oxidation zone during the start up.
  • the syngas desired to be recovered under vacuum condition defines the amount of the RDF to be fed and expected ash amount will vary according to the elements in RDF.
  • the proportional valve (6.4) is proportionally opened for creating vacuum. It is the first chamber where the air is introduced into the gasifier (1). The air inlet is regulated through the proportional valve (6.4). The air flows into the air chamber (4.8) under vacuum and from there it proceeds to the oxidation zone (5) to continue with the oxidation reactions.
  • the stainless steel slope is designed for preventing the excess heat up in the air chamber by meeting the cold air.
  • the hot syngas passes thru either oxygen or air inlet zone (6.2), the air coming in warms up and the syngas cools down.
  • vapor is introduced to the reduction zone (6 ) thru the vapor nozzles (7.2) via proportional valves (15). These valves (15) are fully closed during the updraft mode and no vapor is introduced. There is no interruption during the switching between the downdraft and updraft modes.
  • the air chamber (4.7) is the part where air meets and the valve is open (19) in the downdraft mode.
  • air or oxygen is fed into the nozzles (4.4) in a controlled manner for the process to be properly continued.
  • the proportional valve ise opened (6.3) for vacuum creation.
  • the required amount of air is introduced by valve (6.3).
  • the air comes into the air chamber (4.7) under vacuum and goes down to the oxidation zone (5) to continue reactions.
  • the heat balance is created by cooling down the stainless steel slope by the cold air entering into the air chamber.
  • the hot syngas passes thru the oxygen inlet (4.1) so the inlet air is heated up and outlet syngas is cooled down.
  • valve (18) is fully open and the proportional valve (6.3) is proportionally open to create vacuum.
  • the valves (17 and 6.4) are fully closed.
  • the igniters (8) are activated and they are turned off after ignition.
  • the igniters (8) are located in each air chamber (4.7 and 4.8). Once the process starts, they are deactivated.
  • the igniters are positioned symmetrically in the air chamber (4.7).
  • the igniters are fed thru the LPG system.
  • the end point of igniters are located in between the air nozzles (4.2 and 4.3). It is important to ignite the igniters mutually on the oxidation zone simultaneously. There is no continuous LPG feeding.

Landscapes

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

Abstract

Cette invention concerne un gazéificateur et des procédés de gazéification mis en œuvre dans ledit gazéificateur pour apporter des solutions modulaires dans des zones géographiques dont l'accès est difficile, en traitant le combustible dérivé de déchets (CDD) obtenu à partir de déchets, notamment des déchets industriels et municipaux dangereux, de manière sûre pour l'environnement. La commutation entre les modes de gazéification ascendant et descendant dans ledit gazéificateur est possible sans interruption du système. Des économies d'énergie, de travail et de temps sont ainsi réalisées grâce au gazéificateur et au procédé de gazéification de l'invention.
EP08702378A 2007-11-19 2008-01-03 Gazéificateur et procédés de gazéification l'utilisant Withdrawn EP2231829A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
TR200707958 2007-11-19
PCT/IB2008/050007 WO2009066187A1 (fr) 2007-11-19 2008-01-03 Gazéificateur et procédés de gazéification l'utilisant

Publications (1)

Publication Number Publication Date
EP2231829A1 true EP2231829A1 (fr) 2010-09-29

Family

ID=40084363

Family Applications (1)

Application Number Title Priority Date Filing Date
EP08702378A Withdrawn EP2231829A1 (fr) 2007-11-19 2008-01-03 Gazéificateur et procédés de gazéification l'utilisant

Country Status (4)

Country Link
US (1) US20110005135A1 (fr)
EP (1) EP2231829A1 (fr)
EA (1) EA017588B1 (fr)
WO (1) WO2009066187A1 (fr)

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Publication number Priority date Publication date Assignee Title
US9416006B2 (en) * 2013-09-17 2016-08-16 Ineos Bio Sa Thermal decomposition process for reducing agglomerate formation

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Publication number Priority date Publication date Assignee Title
US5028241A (en) * 1989-07-13 1991-07-02 Set Technology B.V. Down-draft fixed bed gasifier system
US6112677A (en) * 1996-03-07 2000-09-05 Sevar Entsorgungsanlagen Gmbh Down-draft fixed bed gasifier system and use thereof
WO2001051591A1 (fr) * 2000-01-10 2001-07-19 Fuerst Adrian Dispositif et procede pour produire des gaz combustibles
GB0325668D0 (en) * 2003-11-04 2003-12-10 Dogru Murat Intensified and minaturized gasifier with multiple air injection and catalytic bed
DE102004010407B4 (de) * 2004-03-01 2013-02-21 Kbi International Ltd. Reaktor zur thermischen Abfallbehandlung
DE102004016993B4 (de) * 2004-04-02 2014-11-06 Kbi International Ltd. Reaktor zur thermischen Abfallbehandlung mit einem Zuführkanal und Verfahren zur thermischen Abfallbehandlung
AT505188B1 (de) * 2004-08-27 2009-06-15 Schiefer Erwin Reaktor zur vergasung von biomasse
WO2007081296A1 (fr) 2006-01-16 2007-07-19 Gep Yesil Enerji Uretim Teknolojileri Ltd. Sti. Gazogene a ecoulement descendant/ascendant pour production de gaz de synthese a partir de dechets solides
US20070169411A1 (en) 2006-01-25 2007-07-26 Thiessen Randall J Rotating bed gasifier
US7736402B2 (en) * 2006-07-11 2010-06-15 Crorey Jr William G Biomass gasifier
TR200705430A2 (tr) * 2007-08-03 2008-12-22 Detes Maden Enerji̇ Ve Çevre Teknoloji̇si̇ Si̇stemleri̇ Li̇mi̇ted Şi̇rketi̇ Katı yakıt gazlaştırma ve gaz temizleme sistemi.

Non-Patent Citations (1)

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Title
See references of WO2009066187A1 *

Also Published As

Publication number Publication date
EA017588B1 (ru) 2013-01-30
WO2009066187A1 (fr) 2009-05-28
US20110005135A1 (en) 2011-01-13
EA201000835A1 (ru) 2011-06-30

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