EP0484993A1 - 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
EP0484993A1
EP0484993A1 EP91202539A EP91202539A EP0484993A1 EP 0484993 A1 EP0484993 A1 EP 0484993A1 EP 91202539 A EP91202539 A EP 91202539A EP 91202539 A EP91202539 A EP 91202539A EP 0484993 A1 EP0484993 A1 EP 0484993A1
Authority
EP
European Patent Office
Prior art keywords
temperature
gasification
reactor
oxygen
supply
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.)
Granted
Application number
EP91202539A
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German (de)
English (en)
Other versions
EP0484993B1 (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
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 Metallgesellschaft AG filed Critical Metallgesellschaft AG
Publication of EP0484993A1 publication Critical patent/EP0484993A1/fr
Application granted granted Critical
Publication of EP0484993B1 publication Critical patent/EP0484993B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/54Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/48Apparatus; Plants
    • C10J3/485Entrained flow gasifiers
    • C10J3/487Swirling or cyclonic gasifiers
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72Other features
    • C10J3/723Controlling or regulating the gasification process
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10KPURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00Purifying combustible gases containing carbon monoxide
    • C10K1/02Dust removal
    • C10K1/026Dust removal by centrifugal forces
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00Details of gasification apparatus
    • C10J2200/15Details of feeding means
    • C10J2200/158Screws
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0959Oxygen
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/09Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953Gasifying agents
    • C10J2300/0973Water
    • C10J2300/0976Water as steam
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/12Heating the gasifier
    • C10J2300/1223Heating the gasifier by burners
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807Recycle loops, e.g. gas, solids, heating medium, water
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00Details of gasification processes
    • C10J2300/18Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861Heat exchange between at least two process streams
    • C10J2300/1884Heat exchange between at least two process streams with one stream being synthesis gas
    • YGENERAL 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
    • Y10TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10STECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S48/00Gas: heating and illuminating
    • Y10S48/04Powdered 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, the reactor can be structurally simple. According to the invention, this is achieved in the process mentioned at the outset by burning an ashes and fine-grained fuel-containing solid mixture in the reactor in the heating-up phase before the gasification with the supply of oxygen-containing gas in the swirling state with excess stoichiometric oxygen supply, and thereby the temperature in the reactor up to approximately the setpoint 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 Inertization phase passes into the gasification, whereby oxygen or gas containing oxygen 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 exhaust duct, practically constant after a set time and,
  • the temperature is gradually increased in the heating phase.
  • 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.
  • the gasification can begin.
  • a gasifying agent mixture is passed into the reactor, which mainly consists of oxygen (eg also air) and more or less water vapor.
  • oxygen eg also air
  • 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 and a container (7) for inert material, in particular 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 is formed in the reactor (1), a mixture of product gas and solids passing through the discharge channel (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 the measuring device (31) by means of a signal line (33).
  • a temperature measuring device (34) determines 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).
  • ashes are 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 when there is an excess of 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 reactor (1) is ideally provided with constant amounts of coal, water vapor and oxygen (for example in the form of air) supplied, for example using 1 kg of water vapor per Nm3 of oxygen. If gasified lignite or peat that contains a lot of water is gasified, 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 at too high a temperature and less coal at too low a temperature. 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. For the first heating up to about 350 ° C, hot air of 420 ° C is fed into the reactor, which contains up to 1000 kg of ash in increasing quantities.
  • the gas composition in the channel (15) is at different times: time A B C. CO2 (vol .-%) 1.9 6.69 6.69 H2O (vol .-%) 1.9 2.74 2.74 O2 (vol .-%) 17.9 13.13 0 N2 (vol .-%) 78.3 77.44 90.57

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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)
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
DE4035293A DE4035293C1 (fr) 1990-11-07 1990-11-07
DE4035293 1990-11-07

Publications (2)

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

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ID=6417759

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EP91202539A Expired - Lifetime EP0484993B1 (fr) 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

Country Status (5)

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

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DE4340459C1 (de) * 1993-11-27 1995-05-18 Rheinische Braunkohlenw Ag Verfahren zum Betreiben eines Wirbelschichtreaktors zum Vergasen von kohlenstoffhaltigen Einsatzstoffen
US5455011A (en) * 1994-02-28 1995-10-03 The Babcock & Wilcox Company System and method for heating and gasification of residual waste liquor
US5516345A (en) * 1994-06-30 1996-05-14 Iowa State University Research Foundation, Inc. Latent heat-ballasted gasifier method
KR100391121B1 (ko) * 2000-12-11 2003-07-16 김현영 고분자 유기물의 가스화 방법 및 장치
US7276096B2 (en) * 2003-06-27 2007-10-02 Ultracell Corporation Fuel processor dewar and methods
US20060156627A1 (en) * 2003-06-27 2006-07-20 Ultracell Corporation Fuel processor for use with portable fuel cells
US8821832B2 (en) 2003-06-27 2014-09-02 UltraCell, L.L.C. Fuel processor for use with portable fuel cells
KR100637340B1 (ko) * 2004-04-09 2006-10-23 김현영 고온 개질기
KR101424614B1 (ko) 2006-04-11 2014-08-01 서모 테크놀로지스 엘엘씨 고체 탄소물질의 합성가스 발생 방법 및 장치
DE202006020601U1 (de) * 2006-06-28 2009-03-05 Siemens Aktiengesellschaft Vorrichtung für Flugstrom-Vergasungsreaktoren hoher Leistung mit Kombinationsbrenner und Mehrbrenneranordnung
US20110179762A1 (en) * 2006-09-11 2011-07-28 Hyun Yong Kim Gasification reactor and gas turbine cycle in igcc system
KR101010520B1 (ko) 2007-11-21 2011-01-24 두산중공업 주식회사 가스화기 운전 제어시스템 및 그의 제어방법
NL2002330C2 (nl) * 2008-12-15 2010-06-16 Essent En Produktie B V Vergassen van vaste brandstoffen in een circulerend wervelbed.
WO2012122622A1 (fr) * 2011-03-17 2012-09-20 Nexterra Systems Corp. Système et procédé à chauffe direct
US20120255301A1 (en) 2011-04-06 2012-10-11 Bell Peter S System for generating power from a syngas fermentation process
US8945507B2 (en) 2011-04-21 2015-02-03 Kellogg Brown & Root Llc Systems and methods for operating a gasifier
US8673181B2 (en) 2011-08-11 2014-03-18 Kellogg Brown & Root Llc Systems and methods for starting up a gasifier
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
US9388980B2 (en) 2011-12-15 2016-07-12 Kellogg Brown + Root LLC Systems and methods for gasifying a hydrocarbon feedstock
US9574770B2 (en) 2012-04-17 2017-02-21 Alter Nrg Corp. Start-up torch
CN103773506B (zh) * 2014-01-28 2015-01-07 广州贝龙火地生物质能源设备科技有限责任公司 生物质双裂解一体炉

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EP0303851A2 (fr) * 1987-08-14 1989-02-22 Rheinbraun Aktiengesellschaft Procédé pour mettre en route un gazogène

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Also Published As

Publication number Publication date
DE4035293C1 (fr) 1992-01-02
DE59100812D1 (de) 1994-02-17
ZA918838B (en) 1993-05-07
AU641055B2 (en) 1993-09-09
AU8699491A (en) 1992-05-14
EP0484993B1 (fr) 1994-01-05
US5145491A (en) 1992-09-08

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