EP0676465B1 - Procédé pour la gazéification de déchets dans un lit fluide circulant - Google Patents

Procédé pour la gazéification de déchets dans un lit fluide circulant Download PDF

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Publication number
EP0676465B1
EP0676465B1 EP95104128A EP95104128A EP0676465B1 EP 0676465 B1 EP0676465 B1 EP 0676465B1 EP 95104128 A EP95104128 A EP 95104128A EP 95104128 A EP95104128 A EP 95104128A EP 0676465 B1 EP0676465 B1 EP 0676465B1
Authority
EP
European Patent Office
Prior art keywords
gas
reactor
gasification
separator
cracking 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
EP95104128A
Other languages
German (de)
English (en)
Other versions
EP0676465A1 (fr
Inventor
Johannes Dr. Albrecht
Johannes Dr. Löffler
Rainer Dr. Reimert
Martin Dr. Hirsch
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.)
GEA Group AG
Original Assignee
Metallgesellschaft AG
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
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Publication of EP0676465A1 publication Critical patent/EP0676465A1/fr
Application granted granted Critical
Publication of EP0676465B1 publication Critical patent/EP0676465B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • C10J3/46—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
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • 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
    • 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
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
    • 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
    • C10K3/001—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 thermal treatment
    • 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
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1628—Ash post-treatment
    • C10J2300/1631—Ash recycling
    • 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 invention relates to a method for gasifying waste materials containing combustible components in the circulating fluidized bed, taking out the waste materials in a gasification reactor with the addition of Gasified gas in the swirl state, from upper area of the gasification reactor Gas-solid mixture feeds a separator from which Separator removes dusty gas and separates it separated solids and the solids at least partially in the gasification reactor leads back.
  • the invention has for its object to ensure in waste gasification that the formation of highly toxic substances, such as especially dioxins and furans, is avoided as far as possible. At the same time, the amount of exhaust gas formed should be kept low. According to the invention, this is achieved in the process mentioned at the outset by carrying out the gasification in the gasification reactor at temperatures in the range from 800 to 1100 ° C.
  • gaseous gasification agent which consists of 20 to 90% by volume of oxygen by leaving the separator draws off a dust-containing gas, the content of free O 2 of which is at most 0.5% by volume, that the gas drawn off from the separator is partially burned in a cracking reactor which is at the same time from 70 to 100% by volume of oxygen-rich O 2 existing gas is supplied, that temperatures in the range of 1200 to 1600 ° C are maintained in the cracking reactor and liquid slag is generated which is discharged from the cracking reactor, and that the cracking gas formed in the cracking reactor is cooled in at least one cooler with a cooling rate of at least 100 Cools down to a maximum temperature of 300 ° C per second.
  • a gaseous gasification agent is understood to mean all gases supplied to the gasification reactor, but with the exception of H 2 O in liquid form or in vapor form.
  • the O 2 content of the total amount of gaseous gasifying agent is preferably at least 50% by volume.
  • the oxygen necessary for the partial oxidation in the gasification reactor is supplied by the gaseous gasification agent preferably in the form of air enriched with oxygen or technically pure oxygen.
  • the amount of inert gas which leaves the gasification reactor in the gas-solid mixture is kept low and the dust-containing gas drawn off from the separator has a calorific value of approximately 4000 to 8000 kJ / Nm 3 . If the calorific value of this gas is high enough, there is no need to add additional fuel in the cracking reactor.
  • the waste materials to be gasified which can be, for example, municipal or industrial waste, are fed in line (1) to a gasification reactor (2), where they come into contact with hot gases and particles in the state of the circulating fluidized bed.
  • Oxygen-containing fluidizing gas is introduced in line (3) and passed through a distribution chamber (4) with a grate (5) into the fluidized bed of the reactor (2).
  • additional oxygen-rich gas is added to the fluidized bed above the grate (5), the O 2 content of this gas being higher than in the gas in line (3).
  • the O 2 content in the gas is 50 to 90% by volume (calculated as anhydrous).
  • the gasification in the reactor (2) takes place at temperatures of 800 to 1100 ° C and mostly at temperatures in the range from 850 to 1000 ° C.
  • Ash is removed through the line (6) withdrawn and a separating device (60), e.g. one Sieve. Rough ash parts are drawn in the Line (61) and the fine ash parts are passed through the line (62) to a grinding (63), in order to then if desired, on the transport route (12a) To be able to give up the gap reactor (13).
  • a gas-solid mixture leaves the reactor through the channel (8) and flows into a cyclone separator (9), from which dust-containing gas with a free O 2 content of at most 0.5 Vol .-% is withdrawn through line (10).
  • a cyclone separator (9) from which dust-containing gas with a free O 2 content of at most 0.5 Vol .-% is withdrawn through line (10).
  • Separated solids are returned from the lower area of the separator (9) through line (11) to the reactor (2).
  • the line (11) can also have a side draw (12) for removing an excess of solids. This excess of solids can also be passed into the gap reactor (13) on the transport path (12a).
  • the dust-containing gas drawn off in the line (10) from the separator (9) is fed to the cracking reactor (13), where partial combustion takes place at temperatures in the range from 1200 to 1600 ° C. and preferably 1250 to 1500 ° C.
  • oxygen-rich gas containing 70 to 100% by volume of O 2 is introduced, which can also be technically pure oxygen.
  • a line (15) for additional fuel, for example natural gas, is also provided. Partial combustion in the cracking reactor (13) produces liquid slag that flows downwards. Hot cracked gas leaves the reactor (13) together with liquid slag through the channel (17).
  • the cracking reactor (13) can be, for example, a combustion chamber, a melting cyclone or a hearth furnace.
  • many pollutants introduced in line (10) are destroyed at the high temperatures reached there, and in particular also higher hydrocarbons are split, so that the cracked gas in channel (17) is practically free of hydrocarbons with more than 4 carbon atoms per Molecule is.
  • the cooled gas from line (20) is now still further cleaned by washing water, taking it down through a jet washer (28) up through the channel (29) in an aerosol washer (30) through line (31) a venturi washer (32), down there to the channel (33) and then flows up through the spray tower (34).
  • the Spray tower (34) is led through line (35) Fresh water to which you also add sodium hydroxide solution can, in particular, chlorine in the gas to be treated tie. It is useful to have one in the spray tower (34) Pack (36) for intensifying the Provide gas-liquid contact.
  • the gas that the Leaves spray tower (34) through line (37) is through an activated carbon filter (38) passed to mercury remove before it is in line (39) further, per se known cleaning stages or a combustion, e.g. in a power plant.
  • Another Possibility is to gas the line (37) first of all to a known desulfurization undergo before passing it through the filter (38), however this possibility was not shown in the drawing considered.
  • Fig. 1 are water supply lines with the Reference number (40) and cooler with reference number (41) Mistake. Used water in the pipes (42) and (43) runs, gets into the settling container (44). Out partially clarified water is fed to this container Reuse in the jet washer (28) and Aerosol washer (30) pulls wastewater through the Line (45) and removes sludge through the Line (46). Mud and sewage are not in shown further processed separately.
  • a wastewater-free process for cooling the hot Cracked gas that is generated in the reactor (13) is with the help the schematic representation of FIG. 2 explained.
  • the amount of water is so on Temperature and the amount of gas matched that the all of the water along with the chilled gas in the form of Water vapor is drawn off through line (52).
  • Solids that dry out at the bottom of the spray tower (50) collect, are removed through line (48).
  • the Gas of the line containing water vapor and dust (52) is passed through a filter device (53) in which e.g. around a bag filter or an electrostatic filter can act; you can also have several here Combine filter types. Dust-free gas flows in the Line (54) and is the other, known per se Gas cleaning supplied, which is not shown here.
  • a heavy cake containing heavy metals is obtained in an amount of 50 kg / h.
  • the gas in line (20) which is produced in an amount of 10800 kg / h, has a calorific value of 5.7 MJ / Nm 3 .
  • the slag drawn off in the line (24) is glazed by the pretreatment and can therefore be deposited without any problems.

Claims (7)

  1. Procédé de gazéification de déchets contenant des constituants combustibles en lit fluidisé circulant qui consistent à gazéifier à l'état fluidisé les déchets dans un réacteur de gazéification avec addition de gaz contenant de l'oxygène, à envoyer par la partie supérieure du réacteur de gazéification, un mélange de gaz et de matière solide à un séparateur, à soutirer du gaz contenant de la poussière du séparateur, et indépendamment de cela, à en décharger des matières solides séparées, et à retourner les matières solides au moins en partie au réacteur de gazéification, caractérisé en ce qu'il consiste à effectuer la gazéification dans un réacteur de gazéification, à des températures de l'ordre de 800 à 1100°C avec apport d'agent de gazéification gazeux constitué pour 20 à 90 % en volume d'oxygène, à soutirer du séparateur un gaz contenant de la poussière et dont la teneur en O2 libre est au plus de 0,5 % en volume, à brûler partiellement le gaz soutiré du séparateur dans un réacteur de craquage auquel on envoie simultanément un gaz riche en oxygène constitué pour 70 à 100 % en volume de O2, à maintenir dans le réacteur de craquage des températures de l'ordre de 1200 à 1600°C et à y produire de la scorie liquide que l'on soutire du réacteur de craquage et à refroidir le gaz de craquage formé dans le réacteur de craquage dans au moins un dispositif de refroidissement, à une vitesse de refroidissement d'au moins 100 °C à la seconde pour l'amener à une température de 300°C au plus.
  2. Procédé suivant la revendication 1, caractérisé en ce qu'il consiste à refroidir le gaz de craquage formé dans le réacteur de craquage dans au moins un dispositif de refroidissement par contact direct avec de l'eau projetée en excès et à soutirer des dispositifs de refroidissement de l'eau résiduaire.
  3. Procédé suivant la revendication 1, caractérisé en ce qu'il consiste à refroidir le gaz de craquage formé dans le réacteur de craquage dans au moins un dispositif de refroidissement par de l'eau de refroidissement projetée et à soutirer du dispositif de refroidissement du gaz de craquage refroidi contenant l'eau de refroidissement sous forme de vapeur d'eau et ayant une température de 300°C au plus.
  4. Procédé suivant l'une des revendications 1 à 3, caractérisé en ce qu'il consiste à refroidir le gaz de refroidissement dans un dispositif de refroidissement ayant une température d'entrée d'au moins 800°C et une température de sortie de 300°C au plus, à une vitesse de refroidissement d'au moins 100°C à la seconde.
  5. Procédé suivant l'une des revendications 1 à 4, caractérisé en ce que le gaz contenant de la poussière est soutiré du séparateur à une valeur calorifique de 3000 à 8000 kJ/m3 normal environ.
  6. Procédé selon l'une des revendications 1 à 5, caractérisé en ce qu'il consiste à envoyer du combustible au réacteur de craquage.
  7. Procédé selon l'une des revendications 1 à 6, caractérisé en ce qu'il consiste à envoyer des matières solides déchargées du réacteur de gazéification au réacteur de craquage.
EP95104128A 1994-04-07 1995-03-21 Procédé pour la gazéification de déchets dans un lit fluide circulant Expired - Lifetime EP0676465B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4412004A DE4412004A1 (de) 1994-04-07 1994-04-07 Verfahren zum Vergasen von Abfallstoffen in der zirkulierenden Wirbelschicht
DE4412004 1994-04-07

Publications (2)

Publication Number Publication Date
EP0676465A1 EP0676465A1 (fr) 1995-10-11
EP0676465B1 true EP0676465B1 (fr) 1998-08-05

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EP95104128A Expired - Lifetime EP0676465B1 (fr) 1994-04-07 1995-03-21 Procédé pour la gazéification de déchets dans un lit fluide circulant

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DE (2) DE4412004A1 (fr)

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5922090A (en) 1994-03-10 1999-07-13 Ebara Corporation Method and apparatus for treating wastes by gasification
DE19544200A1 (de) * 1995-11-28 1997-06-05 Metallgesellschaft Ag Verfahren zum Behandeln von Abgas aus der Vergasung von kohlenstoffhaltigem Material
DE69624073T2 (de) * 1995-11-28 2003-08-14 Ebara Corp Verfahren und Vorrichtung zur Behandlung von Abfällen mittels Vergasung
EP0801218B1 (fr) * 1996-04-09 2001-07-11 ANSALDO RICERCHE S.r.l. Méthode et système pour produire et utiliser des gaz combistibles, en particulier des gaz obtenus à partir de biomasses et déchet
US5900224A (en) * 1996-04-23 1999-05-04 Ebara Corporation Method for treating wastes by gasification
US5980858A (en) * 1996-04-23 1999-11-09 Ebara Corporation Method for treating wastes by gasification
US6902711B1 (en) 1996-04-23 2005-06-07 Ebara Corporation Apparatus for treating wastes by gasification
JP4454045B2 (ja) * 1996-09-04 2010-04-21 株式会社荏原製作所 旋回溶融炉及び二段ガス化装置
DE19652770A1 (de) * 1996-12-18 1998-06-25 Metallgesellschaft Ag Verfahren zum Vergasen fester Brennstoffe in der zirkulierenden Wirbelschicht
ES2229339T3 (es) * 1997-04-22 2005-04-16 Ebara Corporation Procedimiento y dispositivo que sirve para tratar desechos por gasificacion.
DE102004049364A1 (de) * 2004-10-08 2006-04-20 Kerr-Mcgee Pigments Gmbh Wirbelschichtreaktor und Verfahren zur Durchführung von Wilbelschichtreaktionen
DE102008029927B4 (de) 2008-06-26 2013-06-20 Projektentwicklung Energie Und Umwelt Leipzig Gmbh Flash-Pyrolyse von organischen Stoffen mit ionischer Flüssigkeit als Wärmeträger zur Herstellung von öligen bzw. gasförmigen Zwischenprodukten
AU2020256686A1 (en) * 2019-04-12 2021-12-02 Enerkem Inc. Production of synthesis gas from gasifying and reforming carbonaceous material

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3130031A1 (de) * 1981-07-30 1982-04-08 Davy McKee AG, 6000 Frankfurt Verfahren zur vergasung von kohle
FR2559776B1 (fr) * 1984-02-16 1987-07-17 Creusot Loire Procede de production de gaz de synthese
DE4125522C1 (en) * 1991-08-01 1992-10-29 Energiewerke Schwarze Pumpe Ag, O-7610 Schwarze Pumpe, De Simultaneous disposal of solid and liq. waste material, avoiding environmental pollution - by combustion in solid bed pressure gasification plant, quenching hot effluent gases then mixing with oxygen@-contg. gases and combusting further
ATE134698T1 (de) * 1991-11-29 1996-03-15 Noell En Und Entsorgungstechni Verfahren zur thermischen verwertung von abfallstoffen

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Publication number Publication date
EP0676465A1 (fr) 1995-10-11
DE4412004A1 (de) 1995-10-12
DE59503039D1 (de) 1998-09-10

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