EP0484993B1 - Procédé pour la régulation de la mise en marche d'une gasification en lit fluidisé d'un combustible solide - Google Patents

Procédé pour la régulation de la mise en marche d'une gasification en lit fluidisé d'un combustible solide Download PDF

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Publication number
EP0484993B1
EP0484993B1 EP91202539A EP91202539A EP0484993B1 EP 0484993 B1 EP0484993 B1 EP 0484993B1 EP 91202539 A EP91202539 A EP 91202539A EP 91202539 A EP91202539 A EP 91202539A EP 0484993 B1 EP0484993 B1 EP 0484993B1
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EP
European Patent Office
Prior art keywords
temperature
reactor
oxygen
gasification
phase
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
EP91202539A
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German (de)
English (en)
Other versions
EP0484993A1 (fr
Inventor
Gerhard Schmitt
Horst Mielke
Peter Dr. Herbert
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
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Publication date
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Publication of EP0484993A1 publication Critical patent/EP0484993A1/fr
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Anticipated expiration legal-status Critical
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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
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C10J3/487—Swirling or cyclonic gasifiers
    • 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
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners
    • 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
    • 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
    • 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
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S48/00—Gas: heating and illuminating
    • Y10S48/04—Powdered fuel injection

Definitions

  • the invention relates to a method for regulating the start-up of gasification of solid, fine-grained fuels with oxygen-containing gas and water vapor in the fluidized state in a gasification reactor, which has an outlet duct for product gas at the upper end and an ash outlet in the lower region.
  • the gasification works at a pressure of 1 to 100 bar.
  • the invention has for its object to start the gasification reactor easily controllable, wherein the reactor can be structurally simple. According to the invention, this is achieved in the process mentioned at the outset by burning an ash and fine-grained fuel-containing solid mixture in the reactor in the heating-up phase with the supply of oxygen-containing gas in the vortex state while supplying oxygen-containing gas and thereby the temperature in the reactor up to about the target temperature of the gasification increased that at the end of the heating phase in a subsequent inerting phase, the supply of oxygen-containing gas is reduced, an inert gas is passed into the reactor, the free oxygen content in the product gas is practically reduced to zero and the temperature is kept practically constant, and that after the Inerting phase passes into the gasification, with oxygen or oxygen-containing gas and possibly water vapor conducts into the reactor, increases the fuel supply and keeps the target gasification temperature in the range from 600 to 1500 ° C, measured in the upper region of the reactor or in the discharge duct, practically constant after a set time and, if the temperature is too low, reduces the
  • the temperature is gradually increased. In the case of a reactor with brick lining, temperature increases of approximately 40 to 120 ° C. per hour are recommended. If the temperature is too high, the supply of solid fuel is reduced and if the temperature is too low, the supply of solid fuel is increased, because there is an excess of stoichiometric oxygen in the gasification reactor. For economic reasons in particular, it is advantageous to pass air into the reactor as an oxygen-containing gas in the heating phase. For example, when the heating-up phase has ended and the target temperature of the gasification has been reached, the supply of oxygen-containing gas is reduced and, in an inerting phase, an increasing amount of inert gas is introduced into the reactor. The total amount of gas supplied remains mostly constant. This inert gas is usually recycled product gas, nitrogen or carbon dioxide.
  • the gasification can begin.
  • a gasifying agent mixture is passed into the reactor, which mainly consists of oxygen (for example also air) and more or less water vapor.
  • inert gas eg N2 or CO2
  • the reactor is given more fuel and reduces the proportion of ashes fed to zero. If the fuel, eg lignite, itself contains a lot of water, the proportion of water vapor in the gasifying agent mixture can be reduced and possibly omitted entirely.
  • the temperature is kept constant with a fluctuation range of ⁇ 40 ° C, which is done by regulating the fuel supply.
  • the supply of water vapor can be varied, which is possible both in the heating phase and during inerting and gasification.
  • solid fuels are gasified in the vortex state, which are fed in by a conveyor (2).
  • Coal, lignite or peat can be used as solid fuels.
  • the fuels or inert material are fed from a storage bunker (3) via a metering device (4), for example a rotary valve.
  • a container (6) for the fuels to be gasified Above the storage bunker (3) there is a container (6) for the fuels to be gasified and a container (7) for inert material, especially ash or sand.
  • the following explanations speak of the fact that the fuel to be gasified is coal and the inert material is ash.
  • the reactor (1) has a distribution chamber (9) for gases and / or water vapor which flow in through the line (10). These fluids enter the reactor (1) through a grate (11).
  • a branch line (12) with a valve (13) enables the metered supply of these fluids simultaneously into an area above the grate (11).
  • a circulating fluidized bed forms in the reactor (1), a mixture of product gas and solids passing through the exhaust duct (15) into a cyclone (16) and being separated there.
  • the product gas flows through line (17) to a waste heat boiler (18) and is available in line (19) for further use. Since the product gas is rich in the components H2 and CO, it can e.g. be processed into synthesis gas.
  • a water vapor line (26), an oxygen line (27), an air line (28) and an inert gas line (29) are connected to the collecting line (10).
  • Each of these lines (26) to (29) has a control valve (30) and a measuring device (31) for determining the amount flowing through.
  • the control valves (30) are actuated by a control unit (35) via signal lines (32); the quantity flowing through the respective line is communicated to the control unit (35) by a signal line (33) from the measuring device (31).
  • a temperature measuring device (34) detects the temperature in the exhaust duct (15) and this information passes through the signal line (36) into the control unit (35). From here, the temperature is regulated by semi-automatic or fully automatic control in a manner to be described.
  • the supply of coal to the reactor (1) is regulated via the control line (37). Details of the possibilities of how this regulation takes place are explained with the aid of FIGS. 2a and 2b.
  • Fig. 2a the vertical axis (T) indicates the temperature (e.g. in ° C), the horizontal axis (t) is the same for Figs. 2a and 2b the time axis (values e.g. in hours).
  • the vertical axis (M) of Fig. 2b relates to quantities (e.g. in kg / h) of substances which are fed to the reactor (1) as a function of time.
  • the solid line (a) represents the course of the air supply through line (28), line (b) belongs to the inert gas supplied through line (29), the dash-dotted line (c) belongs to the coal feed and the dotted line (d ) belongs to the water vapor that flows through line (26).
  • ash is placed in the reactor (1), swirled with hot air and later a start-up burner (40) is started.
  • Gaseous or liquid fuel for example natural gas or heating oil, is fed to this burner (40) through line (41) and air is fed in through line (42).
  • the temperature measured in the measuring device (34) gradually increases until, at time (A), coal is fed from the bunker (3) in a metered amount via the cellular wheel sluice (4) to the reactor (1).
  • the coal swirled by the air supply burns with excess oxygen in the reactor, as a result of which the temperature is further increased.
  • the start-up burner (40) can be switched off and the proportion of ash supplied is almost zero.
  • the setpoint temperature can be specified in the control unit (35) by manual control or by automatic calculation.
  • the temperature rise in the heating phase continues until the setpoint of the gasification temperature is reached or slightly exceeded.
  • the inerting phase now begins to make the oxygen content in the product gas disappear.
  • the supply of air through line (28) to the reactor (1) is reduced at constant temperature and at the same time the amount of inert gas is increased. It is ensured that the total amount of air and inert gas remains approximately constant.
  • the time (C) denotes the point at which the oxygen content in the product gas has decreased to 0 and the inerting phase has ended.
  • An analyzer determines the oxygen content in the product gas of the channel (15).
  • the reactor (1) is ideally provided with constant amounts of coal, water vapor and oxygen (for example in the form of air) supplied, for example, 1 kg of water vapor is used per Nm3 of oxygen. If lignite or peat is gasified, which is very watery, the supply of water vapor can be reduced or possibly completely eliminated.
  • the temperature is regulated by regulating the coal supply via the cellular wheel sluice (4), the reactor (1) being given more coal if the temperature is too high and less coal if the temperature is too low. It is advisable to keep the temperature constant during the gasification with a fluctuation range of ⁇ 40 ° C and preferably ⁇ 30 ° C.
  • the reactor (1) has a diameter of 2.5 m and a height above the grate (11) of 15 m.
  • the coal to be gasified is a coal mixture with a lower calorific value of 5579 kcal / kg, a water content of 24% by weight and an ash content of 8.3% by weight.
  • the coal has the following elementary analysis (water and ash free):
  • the combustion and gasification takes place without technically pure oxygen only with air, nitrogen and water vapor.
  • the supply of secondary air through line (12) is dispensed with.
  • the gas composition in channel (15) at different times is:

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  • 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)
  • Solid-Fuel Combustion (AREA)

Claims (6)

  1. Procédé de régulation de la mise en marche d'une gazéification de combustible solide en grains fins par du gaz contenant de l'oxygène et de la vapeur d'eau à l'état fluidisé dans un réacteur de gazéification qui comporte, à l'extrémité supérieure, un canal d'évacuation du gaz produit et, dans la partie inférieure, une évacuation de cendres, caractérisé en ce qu'il consiste à brûler, à l'état fluidisé dans le réacteur, avec une hyperstoechiométrie d'oxygène, pendant la phase de chauffage avant la gazéification, un mélange de matières solides contenant une cendre et du combustible à grains fins avec apport de gaz contenant de l'oxygène et à porter ainsi la température dans le réacteur à peu près à la température de consigne de la gazéification, à diminuer à la fin de la phase de chauffage, dans une phase ultérieure d'inactivation, l'apport de gaz contenant de l'oxygène, à envoyer un gaz inerte dans le réacteur, à réduire pratiquement à zéro la teneur en oxygène libre du gaz produit et à maintenir ainsi pratiquement constante la température et à passer, après la phase d'inactivation à la gazéification en envoyant de l'oxygène ou du gaz en contenant et éventuellement de la vapeur d'eau dans le réacteur, en augmentant l'apport de combustible et en maintenant pratiquement constante, après une durée de réglage, la température de consigne de la gazéification de l'ordre de 600 à 1550°C mesurée dans la partie supérieure du réacteur ou dans le canal d'évacuation et, si la température est trop basse, à diminuer l'apport de combustible solide et si elle est trop haute, à augmenter l'apport de combustible.
  2. Procédé suivant la revendication 1, caractérisé en ce qu'il consiste à élever peu à peu la température dans la phase de chauffage, à diminuer l'apport de combustible solide si la température est trop haute et à augmenter l'apport de combustible solide si la température est trop basse.
  3. Procédé suivant la revendication 1, caractérisé en ce qu'il consiste à maintenir constante pendant la gazéification, après la durée de réglage, la température avec une plage de fluctuation de ± 40°C.
  4. Procédé suivant la revendication 1, caractérisé en ce qu'il consiste à envoyer au réacteur dans la phase de chauffage, de l'air en tant que gaz contenant de l'oxygène.
  5. Procédé suivant la revendication 1, caractérisé en ce qu'il consiste à utiliser comme gaz inerte pendant la phase d'inactivation de l'azote, du dioxyde de carbone ou du gaz produit.
  6. Procédé suivant la revendication 1 ou l'une des suivantes, caractérisé en ce qu'il consiste à maintenir pratiquement constante pendant la phase d'inactivation la quantité totale de gaz contenant de l'oxygène et du gaz inerte.
EP91202539A 1990-11-07 1991-10-01 Procédé pour la régulation de la mise en marche d'une gasification en lit fluidisé d'un combustible solide Expired - Lifetime EP0484993B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE4035293 1990-11-07
DE4035293A DE4035293C1 (fr) 1990-11-07 1990-11-07

Publications (2)

Publication Number Publication Date
EP0484993A1 EP0484993A1 (fr) 1992-05-13
EP0484993B1 true EP0484993B1 (fr) 1994-01-05

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Country Status (5)

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US (1) US5145491A (fr)
EP (1) EP0484993B1 (fr)
AU (1) AU641055B2 (fr)
DE (2) DE4035293C1 (fr)
ZA (1) ZA918838B (fr)

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JP5804888B2 (ja) 2011-10-19 2015-11-04 三菱日立パワーシステムズ株式会社 ガスタービン発電プラントの制御方法、ガスタービン発電プラント、炭素含有燃料ガス化炉の制御方法及び炭素含有燃料ガス化炉
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Also Published As

Publication number Publication date
DE59100812D1 (de) 1994-02-17
DE4035293C1 (fr) 1992-01-02
AU8699491A (en) 1992-05-14
US5145491A (en) 1992-09-08
ZA918838B (en) 1993-05-07
EP0484993A1 (fr) 1992-05-13
AU641055B2 (en) 1993-09-09

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