EP1131150B1 - Procede d'exploitation d'une installation de combustion - Google Patents

Procede d'exploitation d'une installation de combustion Download PDF

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Publication number
EP1131150B1
EP1131150B1 EP99972122A EP99972122A EP1131150B1 EP 1131150 B1 EP1131150 B1 EP 1131150B1 EP 99972122 A EP99972122 A EP 99972122A EP 99972122 A EP99972122 A EP 99972122A EP 1131150 B1 EP1131150 B1 EP 1131150B1
Authority
EP
European Patent Office
Prior art keywords
reducing agent
nitrogen
sub
air
stoichiometric
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
EP99972122A
Other languages
German (de)
English (en)
Other versions
EP1131150A1 (fr
Inventor
Hermann BRÜGGENDICK
Andreas Hospital
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.)
Steag Energy Services GmbH
Original Assignee
Steag Encotec 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
Application filed by Steag Encotec GmbH filed Critical Steag Encotec GmbH
Publication of EP1131150A1 publication Critical patent/EP1131150A1/fr
Application granted granted Critical
Publication of EP1131150B1 publication Critical patent/EP1131150B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J7/00—Arrangement of devices for supplying chemicals to fire

Definitions

  • the invention relates to a method according to the preamble of claim 1.
  • SCR Selective Catalytic Reduction
  • the burnt flue gas will be behind the burnout zone with the addition of a reducing agent by a catalytic Reactor passed in which at temperatures of 300-400 ° C splitting the nitrogen oxides to form of molecular nitrogen.
  • the catalytic The investment required for the reactor is considerable. Also there are high operating costs because the catalytic converters are cleaned and need to be renewed.
  • SNCR Selective Non-Catalytic Reduction
  • the reducing agent is introduced directly into the overstoichiometric, high-temperature burnt flue gas after the burnout zone.
  • the same reactions take place as in the catalytic reactor, but due to a lack of catalyst at a higher temperature level and with less pressure loss.
  • a temperature window must be maintained, which is approximately between 950 and 1050 ° C. Above this temperature window there is a risk that the reducing agent will oxidize to nitrogen oxides in the presence of the excess of oxygen.
  • the desired reactions occur to an insufficient extent below the temperature window.
  • the result is a slippage of reducing agent, ie the reducing agent is carried away by the flue gas as an ineffective ballast.
  • the effectiveness of the SNCR process presupposes that the reducing agent is mixed with the burnt-out flue gas very intensively and uniformly, for example via lances and the like, using a propellant. Accordingly, the large-scale use of this process is prohibited. Its application is limited to smaller incinerators, e.g. B. on thermal power stations and waste incineration plants. A large-scale use would presuppose that a mixing over a cross-section of 100-500 m 2 is carried out in a uniform manner, which is obviously excluded.
  • the reducing agent intense and Mixing evenly into the flue gas stream also adheres the high-temperature process under development on.
  • the reducing agent is in a reduction zone entered between the burner zone and the burnout zone located. Burner zone and reduction zone operated substoichiometrically. This may be necessary be working with fuel grading, d. i.e., a remainder of fuel in the reduction zone.
  • To the Introducing the reducing agent requires a carrier medium. Air is out of the question because the reduction zone is substoichiometric must stay. In turn, nitrogen is too expensive. So there remains water vapor and vaporizable liquids, whereby in both cases the efficiency of the Process sinks. The same applies to the introduction of ammonia water, whose water content to be evaporated is approx. 75% lies. In the burnout zone following the reduction zone the air ratio is increased to over 1 by Addition of additional combustion air.
  • a method of the type mentioned is known from WO 91/10864 known.
  • the reducing agent is considered fine divided, particulate material introduced into the primary zone.
  • Reducing agents are calcium sulfide, calcium oxide, iron sulfide and iron oxide and mixtures thereof. The The reducing effect of these materials is at least limited.
  • the invention has for its object a method of the type mentioned at the beginning, which can be achieved with little Investment and operating expenses in effective and reliable way for large-scale use.
  • the substoichiometric flame core has a comparatively small cross section so that there is none Difficulties arise, the reducing agent evenly to distribute over this cross section. Also play here Load changes don't matter.
  • Ammonia can be used as a reducing agent, furthermore ammonia water, urea and similar nitrogen compounds, as well as hydrocarbons, especially natural gas (CH 4 ).
  • hydrocarbons especially natural gas (CH 4 ).
  • CH 4 natural gas
  • the reducing agent causes the concentration of the radicals NHi, CHi, HCN to increase. These radicals react with the resulting nitrogen monoxide, reduce it and thereby generate molecular nitrogen.
  • the method according to the invention is free from Temperature restrictions to which the SNCR process is subject. Rather, it turned out to be particularly advantageous in the sub-stoichiometric flame zone Set temperature of over 1,100 ° C.
  • the temperature of the process should preferably be carried out in such a way that during subsequent burn-out, ie when air is supplied later, the nitrogen molecules formed (and also the N 2 molecules of the combustion air) do not thermally decompose again and form nitrogen oxides.
  • the temperature must therefore not exceed 1400 ° C.
  • substoichiometric flame core with a veil of secondary air, preferably with another Veil of tertiary air is enveloped.
  • substoichiometric Flame core finds the decomposition and Reduction of the NO instead.
  • the flue gas therefore occurs with the surrounding ones Walls not in substoichiometric condition Contact. This will prevent the occurrence of high temperature corrosion effectively prevented, in which an essential further Advantage of the invention can be seen.
  • the nitrogen oxide reducing agent can be by side or central lances in the substoichiometric flame core be introduced. Preferably, however, it becomes common with the fuel in the substoichiometric flame core brought in. It can also be advantageous that Nitric oxide reducing agent together with the primary air in the substoichiometric flame core. Possibly. the fuel is already with the primary air or a Mix part of the primary air. The mixture consists of these circumstances from fuel, primary air and reducing agent.
  • the invention preferably develops its advantages everywhere where the fuel has a high proportion of nitrogen contains. This is the case for example with hard coal, Tar oil, heavy oil, residual oil, process gas and the like.
  • Solid fuels are ground before combustion.
  • the Reductant can be in solid form (also ground) are present or also liquid or gaseous. The procedure is suitable for all power levels and works without additional pressure loss.
  • the main field of application of the invention is power plant technology.
  • the burners are arranged in several levels one above the other in the side of the boiler wall, the cross-section of the boiler being 100-500 m 2 .
  • Upper air is blown in above the top burner level.
  • Each burner represents its own, substoichiometric NO reduction system and delivers superstoichiometric flue gases into the boiler. Obviously, it is not difficult to switch individual burner levels on or off.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Regulation And Control Of Combustion (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Cylinder Crankcases Of Internal Combustion Engines (AREA)
  • Gas Separation By Absorption (AREA)
  • Control Of Steam Boilers And Waste-Gas Boilers (AREA)

Claims (6)

  1. Procédé de combustion d'un combustible contenant de l'azote en évitant l'émission d'oxydes d'azote, où une zone primaire sous-stoéchiométrique est produite et est alimentée en un moyen de réduction d'oxydes d'azote,
       caractérisé en ce que la zone primaire sous-stoéchiométrique est réalisée sous forme de dard de flamme, et que sont utilisés comme moyen de réduction des oxydes d'azote des composés azotés ou des hydrocarbures.
  2. Procédé selon la revendication 1, caractérisé en ce qu'on règle dans le dard de flamme sous-stoéchiométrique une température supérieure à 1.100°C.
  3. Procédé selon la revendication 1 ou 2, caractérisé en ce que le dard de flamme sous-stoéchiométrique est entouré d'un rideau d'air secondaire, de préférence d'un autre rideau d'air tertiaire.
  4. Procédé selon l'une des revendications 1 à 3, caractérisé en ce que le moyen de réduction des oxydes d'azote est introduit ensemble avec le combustible dans le dard de flamme sous-stoéchiométrique.
  5. Procédé selon l'une des revendications 1 à 4, caractérisé en ce que le moyen de réduction des oxydes d'azote est introduit ensemble avec l'air primaire dans le dard de flamme sous-stoéchiométrique.
  6. Procédé selon la revendication 5, caractérisé en ce que l'air de dard est soufflé dans la flamme, et en ce que le moyen de réduction des oxydes d'azote est introduit ensemble avec l'air de dard dans le dard de flamme sous-stoéchiométrique.
EP99972122A 1998-11-18 1999-10-22 Procede d'exploitation d'une installation de combustion Expired - Lifetime EP1131150B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19853162 1998-11-18
DE19853162A DE19853162C2 (de) 1998-11-18 1998-11-18 Verfahren zum Verbrennen eines stickstoffhaltigen Brennstoffs
PCT/EP1999/008040 WO2000029094A1 (fr) 1998-11-18 1999-10-22 Procede d'exploitation d'une installation de combustion

Publications (2)

Publication Number Publication Date
EP1131150A1 EP1131150A1 (fr) 2001-09-12
EP1131150B1 true EP1131150B1 (fr) 2003-02-05

Family

ID=7888204

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99972122A Expired - Lifetime EP1131150B1 (fr) 1998-11-18 1999-10-22 Procede d'exploitation d'une installation de combustion

Country Status (8)

Country Link
EP (1) EP1131150B1 (fr)
AT (1) ATE232133T1 (fr)
CA (1) CA2351663A1 (fr)
DE (2) DE19853162C2 (fr)
DK (1) DK1131150T3 (fr)
ES (1) ES2192417T3 (fr)
PL (1) PL194273B1 (fr)
WO (1) WO2000029094A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10142804A1 (de) * 2000-10-17 2002-08-08 Bosch Gmbh Robert Abgasreinigungsanlage und Verfahren zur Abgasreinigung

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4023921A (en) * 1975-11-24 1977-05-17 Electric Power Research Institute Oil burner for NOx emission control
DE3021875C2 (de) * 1980-06-11 1985-04-25 L. & C. Steinmüller GmbH, 5270 Gummersbach Verfahren zur Anwendung der selektiven Reduktion von Stickoxiden aus einer Flammenverbrennung mit Hilfe von Ammoniak
DE3331989A1 (de) * 1983-09-05 1985-04-04 L. & C. Steinmüller GmbH, 5270 Gummersbach Verfahren zur verminderung der no(pfeil abwaerts)x(pfeil abwaerts)-emission bei der verbrennung von stickstoffhaltigen brennstoffen
NL8902963A (nl) * 1989-12-01 1991-07-01 Int Flame Research Foundation Werkwijze voor het verbranden van brandstof met een laag nox-gehalte in de verbrandingsgassen door middel van getrapte brandstoftoevoer en brander te gebruiken daarbij.
US5085156A (en) * 1990-01-08 1992-02-04 Transalta Resources Investment Corporation Combustion process

Also Published As

Publication number Publication date
DK1131150T3 (da) 2003-06-02
WO2000029094A1 (fr) 2000-05-25
PL348340A1 (en) 2002-05-20
DE19853162C2 (de) 2003-04-30
ATE232133T1 (de) 2003-02-15
ES2192417T3 (es) 2003-10-01
DE59904247D1 (de) 2003-03-13
CA2351663A1 (fr) 2000-05-25
DE19853162A1 (de) 2000-05-31
PL194273B1 (pl) 2007-05-31
EP1131150A1 (fr) 2001-09-12

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