[go: up one dir, main page]
More Web Proxy on the site http://driver.im/

EP0979262B1 - Procede et dispositif servant a traiter des dechets par gazeification - Google Patents

Procede et dispositif servant a traiter des dechets par gazeification Download PDF

Info

Publication number
EP0979262B1
EP0979262B1 EP97909579A EP97909579A EP0979262B1 EP 0979262 B1 EP0979262 B1 EP 0979262B1 EP 97909579 A EP97909579 A EP 97909579A EP 97909579 A EP97909579 A EP 97909579A EP 0979262 B1 EP0979262 B1 EP 0979262B1
Authority
EP
European Patent Office
Prior art keywords
gas
fluidized
wastes
temperature
bed reactor
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.)
Expired - Lifetime
Application number
EP97909579A
Other languages
German (de)
English (en)
Other versions
EP0979262A1 (fr
Inventor
Hiroyuki Fujimura
Yoshio Hirayama
Shosaku Fujinami
Kazuo Takano
Masaaki Irie
Tetsuhisa Hirose
Shuichi Nagato
Takahiro Oshita
Toshio Fukuda
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.)
Ebara Corp
Ube Corp
Original Assignee
Ebara Corp
Ube Industries Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from JP11743497A external-priority patent/JP4222645B2/ja
Application filed by Ebara Corp, Ube Industries Ltd filed Critical Ebara Corp
Publication of EP0979262A1 publication Critical patent/EP0979262A1/fr
Application granted granted Critical
Publication of EP0979262B1 publication Critical patent/EP0979262B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

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
    • C10J3/72—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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • 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
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1693—Integration of gasification processes with another plant or parts within the plant with storage facilities for intermediate, feed and/or product
    • 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
    • C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas
    • 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
    • C10J2300/1861—Heat exchange between at least two process streams
    • 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
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas

Definitions

  • this prior art does not disclose that steam is generated by contacting the synthesis gas with water directly and the generated steam is supplied together with the quenched synthesis gas to the CO conversion reaction. Further, this prior art does not disclose that the synthesis gas is supplied to the CO conversion reaction without separating CO 2 , and the product gas obtained by the CO conversion reaction is separated into H 2 and residual gas, and the residual gas is returned to the first fluidized-bed furnace as a fluidizing gas.
  • the fluidized-bed temperature of the fluidized-bed reactor is preferably in the range of 450 to 950°C.
  • the wastes preferably has an average lower calorific value of 3500 kcal/kg or more. If the average lower calorific value of the wastes is 3500Kcal/kg or less, a supplementary fuel may be added to the wastes to allow the average lower calorific value to be 3500kcal/kg or more.
  • a supplementary fuel fossil fuel, which is generally used, such as coal or petroleum coke, may be used.
  • the present invention is also applicable to organic materials including oil shale, garbage, carcasses of beasts, waste clothing, waste paper, and any other material.
  • gas whose mole ratio of H 2 to N 2 is 3:1 is produced, and the produced gas is used for synthesis of ammonia. That is, as a gasifying agent supplied to the fluidized-bed reactor, in order to avoid agglomeration or clinker, it is necessary to reduce oxygen gas content to the range of 20 to 30 %. If a mixture of oxygen gas and steam is used as a gasifying agent, a large amount of steam is required. However, in case of producing ammonia as a final product, it is possible to use air. This is because if nitrogen gas remains in the produced gas and the mole ratio of H 2 to N 2 is 3:1, the produced gas can be used for synthesis of ammonia as it is.
  • the substances discharged from the bottom of fluidized-bed reactor after being depressurized by a rock hopper 14 which is normally used for high-temperature fine particles, are separated into the incombustibles "c" and the fluidized medium "d" by the screen 15.
  • the high-temperature combustor is not composed of a single vertically cylindrical chamber, but is composed of a combination of a vertical chamber 10 and a lateral chamber 11.
  • molten slag can stay in the combustor for a longer time, which makes it possible to reduce unburned carbon and to accelerate evaporation of metals having a low-melting point such as zinc and lead.
  • the wastes "a” crushed to a desired size is supplied above the fluidized-bed of hard silica sand in the fluidized-bed reactor 110.
  • the internal pressure of the fluidized-bed reactor 110 is about 40 atm.

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)
  • Gasification And Melting Of Waste (AREA)

Claims (13)

  1. Procédé de traitement de déchets par gazéification, comprenant les étapes consistant à :
    gazéifier en brûlant partiellement au moins un déchet sélectionné dans le groupe composé des déchets urbains, des déchets plastiques comprenant des matières plastiques renforcées par fibres, des déchets de la biomasse, du carburant dérivés des ordures et des déchets de l'industrie automobile dans un réacteur à lit fluidisé fonctionnant à une température comprise entre 450°C et 950°C pour produire un matériau gazeux contenant des cendres et des résidus de carbonisation ;
    introduire ledit matériau gazeux dans un foyer à haute température possédant une chambre de gazéification à haute température et une chambre de refroidissement ;
    gazéifier en brûlant partiellement ledit matériau gazeux dans ladite chambre de gazéification à haute température à une température supérieure à un point de fusion des cendres pour produire un gaz de synthèse et une scorie en fusion ;
    éteindre ledit gaz de synthèse et ladite scorie en les mettant directement en contact avec de l'eau contenue dans ladite chambre de refroidissement pour former un gaz de synthèse éteint et une scorie granulée et pour générer de la vapeur ;
    évacuer ladite scorie granulée de ladite chambre de refroidissement ;
    épurer ledit gaz de synthèse éteint et ladite vapeur générée provenant de ladite chambre de refroidissement pour extraire du chlorure d'hydrogène et des poussières ;
    introduire ledit gaz de synthèse épuré et ladite vapeur épurée dans un réacteur de conversion de CO et mettre en oeuvre une réaction de conversion de CO pour convertir CO et H20 en H2 et en CO2 ;
    séparer le gaz obtenu par ladite réaction de conversion de CO en H2 et en gaz résiduel ; et
    fournir ledit gaz résiduel audit réacteur à lit fluidisé comme gaz de fluidisation.
  2. Procédé selon la revendication 1, dans lequel ledit réacteur à lit fluidisé comprend un réacteur à lit fluidisé à circulation rotative.
  3. Procédé selon la revendication 1, dans lequel les produits non combustibles et un milieu fluidisé sont évacués du fond dudit réacteur à lit fluidisé, et lesdits produits non combustibles sont extraits dudit milieu fluidisé et ledit milieu fluidisé est ramené dans ledit réacteur à lit fluidisé.
  4. Procédé selon la revendication 1, dans lequel ledit foyer à haute température comprend un foyer à haute température à écoulement tourbillonnaire.
  5. Procédé selon la revendication 1, dans lequel ladite gazéification dans ledit réacteur à lit fluidisé et ladite gazéification dans ledit foyer à haute température sont effectuées sous une pression comprise entre 5 et 90 atm.
  6. Procédé selon la revendication 1, dans lequel ladite température dans ledit foyer à haute température est supérieure ou égale à 1200°C.
  7. Procédé selon la revendication 1, dans lequel lesdits déchets ont une valeur calorifique moyenne inférieure qui est supérieure ou égale à 3500 Kcal/kg.
  8. Procédé selon la revendication 1, dans lequel lorsque lesdits déchets ont une valeur calorifique moyenne inférieure qui est inférieure ou égale à 3500 Kcal/kg, on ajoute aux dits déchets un carburant supplémentaire pour que ladite valeur calorifique moyenne inférieure soit supérieure ou égale à 3500 Kcal/kg.
  9. Procédé selon la revendication 1, dans lequel de l'oxygène gazeux ou un mélange d'oxygène gazeux et de vapeur est fourni audit réacteur à lit fluidisé comme agent de gazéification, et où l'oxygène gazeux ou un mélange d'oxygène gazeux et de vapeur est fourni audit foyer à haute température comme agent de gazéification.
  10. Procédé selon la revendication 1, dans lequel un mélange d'oxygène gazeux et d'air ou un mélange d'oxygène, d'air et de vapeur est fourni audit réacteur à lit fluidisé comme agent de gazéification, et où un mélange d'oxygène gazeux, d'air et de vapeur est fourni au dit brûleur à deux étages à haute température comme agent de gazéification, de façon à ce que ledit gaz de synthèse produit dans ledit brûleur à deux étages à haute température contienne CO, H2, et N2 et que le rapport molaire entre la somme de CO et de H2 et N2 soit approximativement égal à 3.
  11. Appareil de traitement de déchets par gazéification comprenant :
    un réacteur à lit fluidisé destiné à gazéifier par combustion partielle au moins un déchet sélectionné dans le groupe composé des déchets urbains, des déchets plastiques comprenant des matières plastiques renforcées par fibres, des déchets de la biomasse, un carburant dérivé des ordures et des déchets de l'industrie automobile à une basse température pour produire un matériau gazeux contenant des cendres et des résidus de carbonisation ;
    une chambre de gazéification à haute température dans un foyer à haute température pour gazéifier par combustion partielle ledit matériau gazeux à haute température afin de produire un gaz de synthèse et une scorie en fusion ;
    une chambre de refroidissement dans ledit foyer à haute température qui est destinée à éteindre ledit gaz de synthèse et ladite scorie en fusion en les mettant directement en contact avec de l'eau pour former un gaz de synthèse éteint et une scorie granulée et pour générer de la vapeur ;
    un épurateur à eau destiné à extraire le chlorure d'hydrogène et les poussières du gaz provenant de la chambre de refroidissement ;
    un réacteur de conversion de CO destiné à mettre en oeuvre une réaction de conversion de CO pour convertir CO et H20 qui sont contenus dans le gaz provenant dudit épurateur à eau en H2 et en CO2 ;
    un équipement de séparation destiné à séparer le gaz obtenu par ladite réaction de conversion de CO en H2 et en gaz résiduel ; et
    une conduite d'alimentation destinée à fournir ledit gaz résiduel audit réacteur à lit fluidisé comme gaz de fluidisation.
  12. Appareil selon la revendication 11, dans lequel ledit réacteur à lit fluidisé comprend un réacteur à lit fluidisé à circulation rotative.
  13. Appareil selon la revendication 11, dans lequel ledit brûleur à deux étages à haute température comprend un foyer à haute température à écoulement tourbillonnaire.
EP97909579A 1997-04-22 1997-10-22 Procede et dispositif servant a traiter des dechets par gazeification Expired - Lifetime EP0979262B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP11743497 1997-04-22
JP11743497A JP4222645B2 (ja) 1996-04-23 1997-04-22 有機性廃棄物の資源化方法及び資源化装置
PCT/JP1997/003814 WO1998047985A1 (fr) 1997-04-22 1997-10-22 Procede et dispositif servant a traiter des dechets par gazeification

Publications (2)

Publication Number Publication Date
EP0979262A1 EP0979262A1 (fr) 2000-02-16
EP0979262B1 true EP0979262B1 (fr) 2004-09-22

Family

ID=14711559

Family Applications (1)

Application Number Title Priority Date Filing Date
EP97909579A Expired - Lifetime EP0979262B1 (fr) 1997-04-22 1997-10-22 Procede et dispositif servant a traiter des dechets par gazeification

Country Status (5)

Country Link
EP (1) EP0979262B1 (fr)
CN (1) CN1137249C (fr)
DE (1) DE69730870T2 (fr)
ES (1) ES2229339T3 (fr)
WO (1) WO1998047985A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102585912A (zh) * 2012-02-04 2012-07-18 王俊 一种多仓微波加热连续工业制取煤气方法

Families Citing this family (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101312905B (zh) 2005-10-21 2015-07-22 泰勒生物质能有限责任公司 原位脱除焦油的气化方法和系统
CA2734630C (fr) * 2008-05-15 2014-03-18 Enersol Power Llc Systeme de gazeification d'un materiau organique ameliore par un courant de chaleur rayonnante
DE102008032957A1 (de) * 2008-07-12 2010-01-14 Dinano Ecotechnology Llc Verfahren zur Gewinnung von synthetischem Diesel
US8192647B2 (en) * 2008-12-19 2012-06-05 Enerkem Inc. Production of synthesis gas through controlled oxidation of biomass
US8821598B2 (en) * 2009-07-27 2014-09-02 General Electric Company Control system and method to operate a quench scrubber system under high entrainment
US8535518B2 (en) * 2011-01-19 2013-09-17 Saudi Arabian Oil Company Petroleum upgrading and desulfurizing process
SG11201408516UA (en) * 2012-07-09 2015-03-30 Southern Co Gasification of high ash, high ash fusion temperature bituminous coals
CN105561743B (zh) * 2014-10-14 2018-04-03 中国石油化工股份有限公司 一种用于合成气膜法脱碳的增湿缓冲系统
CN105694984A (zh) * 2016-04-06 2016-06-22 杭州燃油锅炉有限公司 一种生物质气化装置
EP3512804A1 (fr) * 2016-10-25 2019-07-24 Nextchem S.r.l. Procédé et appareil associé pour fabriquer de l'hydrogène pur à partir d'un gaz de synthèse provenant d'une gazéification de déchets
CN108929722B (zh) * 2018-07-26 2020-05-12 新奥科技发展有限公司 一种煤气化方法以及煤气化系统
IT201900013239A1 (it) * 2019-07-29 2021-01-29 Milano Politecnico Impianto per la produzione di syngas a partire da polimeri plastici di recupero pretrattati
CN111457404B (zh) * 2020-05-18 2024-08-13 江苏金门能源装备有限公司 一种安全型有机废气蓄热催化氧化装置
CN114074919A (zh) * 2020-08-13 2022-02-22 国家能源投资集团有限责任公司 城市垃圾转化生产氢气的方法

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3153091B2 (ja) * 1994-03-10 2001-04-03 株式会社荏原製作所 廃棄物の処理方法及びガス化及び熔融燃焼装置
US4583993A (en) * 1978-06-26 1986-04-22 Mobil Oil Corporation Process for the production of carbon monoxide and hydrogen from carbonaceous material
DE2836175A1 (de) * 1978-08-18 1980-02-28 Metallgesellschaft Ag Verfahren zum vergasen fester, feinkoerniger brennstoffe
ZA842807B (en) * 1983-05-31 1984-11-28 Westinghouse Electric Corp Gasification process for ammonia production
FR2559776B1 (fr) * 1984-02-16 1987-07-17 Creusot Loire Procede de production de gaz de synthese
GB8519821D0 (en) * 1985-08-07 1985-09-11 Ici Plc Hydrogen streams
DE4026272A1 (de) * 1990-08-20 1992-02-27 Kurt Kugler Verfahren und einrichtung zur thermischen behandlung von stoffen nach dem wirbelschichtverfahren
DE4412004A1 (de) * 1994-04-07 1995-10-12 Metallgesellschaft Ag Verfahren zum Vergasen von Abfallstoffen in der zirkulierenden Wirbelschicht
DE4435349C1 (de) * 1994-09-21 1996-05-02 Noell En Und Entsorgungstechni Verfahren und Vorrichtung zur Verwertung von brennbaren Rest- und Abfallstoffen

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102585912A (zh) * 2012-02-04 2012-07-18 王俊 一种多仓微波加热连续工业制取煤气方法

Also Published As

Publication number Publication date
EP0979262A1 (fr) 2000-02-16
CN1137249C (zh) 2004-02-04
WO1998047985A1 (fr) 1998-10-29
DE69730870D1 (de) 2004-10-28
CN1253577A (zh) 2000-05-17
ES2229339T3 (es) 2005-04-16
DE69730870T2 (de) 2005-09-29

Similar Documents

Publication Publication Date Title
US5980858A (en) Method for treating wastes by gasification
EP0803562B1 (fr) Procédé et appareil pour le traitement de déchets par gazéification
EP0776962B1 (fr) Procédé et appareil pour le traitement de déchets par gazéification
US6676716B2 (en) Method and apparatus for treating wastes by gasification
US6161490A (en) Swirling-type melting furnace and method for gasifying wastes by the swirling-type melting furnace
US4597771A (en) Fluidized bed reactor system for integrated gasification
CA2673274C (fr) Procede et installation de production d'energie electrique dans une centrale a cycle combine
EP0979262B1 (fr) Procede et dispositif servant a traiter des dechets par gazeification
JP3415748B2 (ja) 有機性廃棄物の二段ガス化方法及び装置
JPH10156314A (ja) 廃棄物からのエネルギ回収方法
US6902711B1 (en) Apparatus for treating wastes by gasification
JPH10310783A (ja) 廃棄物の高温ガス化方法及び装置
JP4222645B2 (ja) 有機性廃棄物の資源化方法及び資源化装置
JP3079051B2 (ja) 廃棄物のガス化処理方法
US5163374A (en) Combustion process
JP4155507B2 (ja) バイオマスのガス化方法およびガス化装置
JPH1081885A (ja) 有機性廃棄物の資源化方法及び資源化装置
CN110016366B (zh) 生活垃圾气化甲烷化发电系统
JPH10130662A (ja) 廃棄物の資源化方法
JPH10132234A (ja) ガスタービン複合発電方法
WO1979000687A1 (fr) Moyens et procede de gazeification de carburants solides

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 19991015

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): DE ES FR GB IT

17Q First examination report despatched

Effective date: 20020708

GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: UBE INDUSTRIES, LTD.

Owner name: EBARA CORPORATION

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

RIN1 Information on inventor provided before grant (corrected)

Inventor name: FUKUDA, TOSHIO

Inventor name: OSHITA, TAKAHIRO

Inventor name: NAGATO, SHUICHI

Inventor name: HIROSE, TETSUHISA

Inventor name: IRIE, MASAAKI

Inventor name: TAKANO, KAZUO

Inventor name: FUJINAMI, SHOSAKU

Inventor name: HIRAYAMA, YOSHIO

Inventor name: FUJIMURA, HIROYUKI

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): DE ES FR GB IT

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

REF Corresponds to:

Ref document number: 69730870

Country of ref document: DE

Date of ref document: 20041028

Kind code of ref document: P

REG Reference to a national code

Ref country code: ES

Ref legal event code: FG2A

Ref document number: 2229339

Country of ref document: ES

Kind code of ref document: T3

ET Fr: translation filed
PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed

Effective date: 20050623

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IT

Payment date: 20101023

Year of fee payment: 14

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20121022

REG Reference to a national code

Ref country code: FR

Ref legal event code: PLFP

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 20160919

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: ES

Payment date: 20160913

Year of fee payment: 20

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20161018

Year of fee payment: 20

Ref country code: GB

Payment date: 20161019

Year of fee payment: 20

REG Reference to a national code

Ref country code: DE

Ref legal event code: R071

Ref document number: 69730870

Country of ref document: DE

REG Reference to a national code

Ref country code: GB

Ref legal event code: PE20

Expiry date: 20171021

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20171021

REG Reference to a national code

Ref country code: ES

Ref legal event code: FD2A

Effective date: 20180508

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION

Effective date: 20171023