EP0437698B1 - Verfahren zum Betrieb einer Anlage für die Vergasung fester Brennstoffe - Google Patents

Verfahren zum Betrieb einer Anlage für die Vergasung fester Brennstoffe Download PDF

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Publication number
EP0437698B1
EP0437698B1 EP90121843A EP90121843A EP0437698B1 EP 0437698 B1 EP0437698 B1 EP 0437698B1 EP 90121843 A EP90121843 A EP 90121843A EP 90121843 A EP90121843 A EP 90121843A EP 0437698 B1 EP0437698 B1 EP 0437698B1
Authority
EP
European Patent Office
Prior art keywords
oxygen
flue dust
gasification
primary
dust
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
EP90121843A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0437698A1 (de
Inventor
Hans-Richard Baumann
Lothar Semrau
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.)
Krupp Koppers GmbH
Original Assignee
Krupp Koppers GmbH
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 DE3941816A external-priority patent/DE3941816A1/de
Application filed by Krupp Koppers GmbH filed Critical Krupp Koppers GmbH
Publication of EP0437698A1 publication Critical patent/EP0437698A1/de
Application granted granted Critical
Publication of EP0437698B1 publication Critical patent/EP0437698B1/de
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
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow 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
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners

Definitions

  • EP-A1-0 370 201 which does not belong to the prior art, relates to a method for operating a plant for the gasification of fine-grained to dust-like solid fuels, with Gasification reactor equipped with gasification burners, Device for the separation of dust from the raw gas, Dust collection container and device for returning dust to the gasification reactor, wherein the gasification burners burn into the gasification reactor with a fuel / reactant jet that is rotationally symmetrical at the gasification burner outlet and a primary reaction zone of high temperature is formed by the fuel / reactant jets in the gasification reactor.
  • the method of operation according to EP-A1-0 370 201 is based on the task of guiding the process in such a way that the fly dust separated dry from the raw gas is fully integrated in the slag without any special treatment and without interfering with the gasification process, the at the same time residual carbon contained in the dust is to be burned completely.
  • the dust with its raw gas content and its residual carbon are introduced into the axis of at least one fuel / reactant jet by a conveying gas stream, are introduced by the fuel / reactant jet into the primary reaction zone and are melted therein.
  • gasification burners can be used which have a feed channel for primary oxygen coaxial with the burner axis, a surrounding ring channel for the fuel feed and a ring channel surrounding this for the feed of secondary oxygen.
  • the fly dust should be fed through a special feed channel (lance) which is arranged in the axis of the feed channel for the primary oxygen.
  • the invention is therefore based on the object of optimizing the method variant described above with regard to its operating conditions.
  • the invention proposes that a mass ratio of primary oxygen to secondary oxygen of 1: 1 to 1: 4, preferably 1: 1 to 1: 3, be used.
  • the primary oxygen primarily ensures that the fuel metered in the ring channel with high flow rate density but low speed is sufficiently accelerated and swirled.
  • This swirling of the fuel stream provides the fuel particles with the required amount of oxygen for reaction, which takes place directly at the burner mouth as combustion to CO2.
  • the fly dust which is also dosed in the center of the gasification burner with a high flow rate density and low speed, therefore reaches a high temperature zone at the burner mouth, which favors the reaction of the residual carbon contained in the fly dust.
  • the secondary oxygen is said to loosen up and accelerate the fuel flow from the outside.
  • the raw synthesis gas already generated is recirculated from the reaction space of the gasification reactor to the burner mouth by the secondary oxygen emerging from the gasification burner at high speed and by the other material flows.
  • the mass ratio of primary oxygen to secondary oxygen according to the invention, the supply of secondary oxygen to the raw synthesis gas is limited.
  • the raw synthesis gas which consists of 90% CO + H2
  • a further combustion reaction to CO2 + H2O can therefore only take place to a very limited extent.
  • the mass ratio of primary oxygen to secondary oxygen is observed, the CO2 content in the synthesis gas generated by the gasification can be kept in the range between 1 and 3% for most fuels.
  • water vapor which serves as a temperature moderator in the reaction zone
  • the mass ratio of oxygen (total) to water vapor in the range from 1: 0.1 to 1: 0.6 should lie.
  • the water vapor should preferably be added to the secondary oxygen.
  • CO2 can also be used as a temperature moderator instead of water vapor if this does not result in the desired composition of the partial oxidation crude gas generated is adversely affected.
  • impure oxygen with e.g. 15% N2 + Ar or strongly preheated air can be used as an oxygen carrier, with the numerical values given above always referring to pure oxygen.
  • the flow density of the fly dust must be reduced by adding a carrier gas.
  • a carrier gas For example, N2 and / or CO2 or part of the synthesis gas generated can be used for this.
  • the particle size of the flying dust particles must not exceed 1 mm. Oversized grain must therefore before the introduction of the Airborne dust in the gasification burner can be removed by suitable measures.
  • the head of a gasification burner suitable for carrying out this process variant is shown in the figure as an axial section.
  • the burner jacket 1 is provided with a circumferential cooling channel 2 and an annular channel 3 for the introduction of protective gas.
  • the ring channel 4 serves to supply the secondary oxygen and the ring channel 5 serves to supply the fuel.
  • the outlet openings of the ring channels 3 to 5 are inclined towards the burner axis.
  • the dust is supplied here through the ring channel 6, which is arranged in the area of the central supply of the primary oxygen, so that it is introduced through the central supply channel 7 and the ring channel 8.
  • the swirl bodies 9 can be arranged in the feed channel 7 and in the ring channel 8, by means of which the swirling of the primary oxygen with the flying dust and the fuel is improved. This effect is also supported by the fact that the outlet openings of the ring channels 3 to 5 are inclined towards the burner axis. The supply of protective gas via the ring channel 3 reduces the oxygen concentration on the cooled burner mouth 10.
  • the central supply of primary oxygen via the supply channel 7 also has the advantage that the light guide 11 of a flame detector installed outside the gasification burner can be arranged in the center of the gasification burner.
  • the gasification burner described above can also be used as a pilot burner if by the Ring channel 6, a gaseous ignition medium, such as natural gas or propane, is introduced instead of flying dust.
  • a gaseous ignition medium such as natural gas or propane

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Processing Of Solid Wastes (AREA)
  • Air Supply (AREA)
  • Carbon And Carbon Compounds (AREA)
EP90121843A 1989-12-19 1990-11-15 Verfahren zum Betrieb einer Anlage für die Vergasung fester Brennstoffe Expired - Lifetime EP0437698B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3941816 1989-12-19
DE3941816A DE3941816A1 (de) 1988-11-05 1989-12-19 Verfahren zum betrieb einer anlage fuer die vergasung fester brennstoffe

Publications (2)

Publication Number Publication Date
EP0437698A1 EP0437698A1 (de) 1991-07-24
EP0437698B1 true EP0437698B1 (de) 1993-02-03

Family

ID=6395735

Family Applications (1)

Application Number Title Priority Date Filing Date
EP90121843A Expired - Lifetime EP0437698B1 (de) 1989-12-19 1990-11-15 Verfahren zum Betrieb einer Anlage für die Vergasung fester Brennstoffe

Country Status (7)

Country Link
EP (1) EP0437698B1 (pl)
CN (1) CN1025868C (pl)
DE (1) DE59000845D1 (pl)
DK (1) DK0437698T3 (pl)
ES (1) ES2038862T3 (pl)
PL (1) PL164928B3 (pl)
ZA (1) ZA909213B (pl)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT402440B (de) * 1995-06-01 1997-05-26 Voest Alpine Ind Anlagen Brenner
JP3492099B2 (ja) * 1995-10-03 2004-02-03 三菱重工業株式会社 バーナ
US7416404B2 (en) 2005-04-18 2008-08-26 General Electric Company Feed injector for gasification and related method
CN101363624B (zh) 2007-08-06 2011-05-25 国际壳牌研究有限公司 燃烧器
CN101363626B (zh) 2007-08-06 2015-05-20 国际壳牌研究有限公司 制造燃烧器前脸的方法
AU2009209689B2 (en) 2008-01-28 2011-10-27 Air Products And Chemicals, Inc. Process to start-up a coal gasification reactor
US8434700B2 (en) * 2008-04-30 2013-05-07 General Electric Company Methods and systems for mixing reactor feed
DE102008063505A1 (de) 2008-12-17 2010-07-01 Uhde Gmbh Verfahren zur Vergleichmäßigung der Förderung von Brennstoffen in einen Vergaser zur Erzeugung von Synthesegas

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE968970C (de) * 1952-12-11 1958-04-17 Basf Ag Verfahren zur Vergasung staubfoermiger bis koerniger Brennstoffe
US4480559A (en) * 1983-01-07 1984-11-06 Combustion Engineering, Inc. Coal and char burner
US4443230A (en) * 1983-05-31 1984-04-17 Texaco Inc. Partial oxidation process for slurries of solid fuel
GB8317251D0 (en) * 1983-06-24 1983-07-27 Shell Int Research Burner for gasification of solid fuel
DE3837586A1 (de) * 1988-11-05 1990-05-10 Krupp Koppers Gmbh Vergasungsbrenner fuer eine anlage fuer die vergasung von festen brennstoffen

Also Published As

Publication number Publication date
PL164928B3 (pl) 1994-10-31
ZA909213B (en) 1991-09-25
CN1025868C (zh) 1994-09-07
DK0437698T3 (da) 1993-06-01
CN1052889A (zh) 1991-07-10
EP0437698A1 (de) 1991-07-24
ES2038862T3 (es) 1993-08-01
PL288309A3 (en) 1991-12-02
DE59000845D1 (de) 1993-03-18

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