EP0607210B1 - Verfahren zur verbrennung von feststoffen - Google Patents

Verfahren zur verbrennung von feststoffen Download PDF

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Publication number
EP0607210B1
EP0607210B1 EP92920686A EP92920686A EP0607210B1 EP 0607210 B1 EP0607210 B1 EP 0607210B1 EP 92920686 A EP92920686 A EP 92920686A EP 92920686 A EP92920686 A EP 92920686A EP 0607210 B1 EP0607210 B1 EP 0607210B1
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EP
European Patent Office
Prior art keywords
flue gas
process according
combustion
air
water vapour
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
EP92920686A
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German (de)
English (en)
French (fr)
Other versions
EP0607210A1 (de
Inventor
Jörg Krüger
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.)
MUELLKRAFTWERK SCHWANDORF BETRIEBSGESELLSCHAFT MBH
Original Assignee
MUELLKRAFTWERK SCHWANDORF BETRIEBSGESELLSCHAFT MBH
MUELLKRAFTWERK SCHWANDORF BETR
Muellkraftwerk Schwandorf Betriebsgesellschaft Mbh
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Publication of EP0607210A1 publication Critical patent/EP0607210A1/de
Application granted granted Critical
Publication of EP0607210B1 publication Critical patent/EP0607210B1/de
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L2900/00—Special arrangements for supplying or treating air or oxidant for combustion; Injecting inert gas, water or steam into the combustion chamber
    • F23L2900/07009—Injection of steam into the combustion chamber

Definitions

  • the present invention relates to a method for the combustion of solids, in particular for waste incineration, in a combustion boiler which comprises at least one combustion chamber and an afterburning chamber, water vapor being introduced into the combustion boiler.
  • a sufficient burnout of the flue gases with the oxygen in the air is only guaranteed if there is an excess of air and corresponding turbulence in or directly above the combustion chamber.
  • part of the combustion air is usually blown in as secondary air at low pressure and moderate speeds.
  • the aim is to reduce the formation of carbon monoxide and nitrogen oxides.
  • the amount of secondary air blown in must be selected to be correspondingly high.
  • this excess air significantly increases the amount of exhaust gas and thus the loss of usable energy.
  • the adiabatic combustion temperatures decrease considerably with increasing air excess. If there is a large excess of air, additional CO formation can be caused by supercooling the fuel gases by adding the secondary air. However, high temperature peaks can occur in the edge region of the secondary air flow, which in conjunction with the locally high oxygen concentrations contribute to the formation of NO x .
  • the oxygen concentration in the moist flue gas after the incineration boiler is usually around 10% by volume.
  • the excess air in this case is about 150%, corresponding to an air ratio of 2.5.
  • Between 20 and 40% of the combustion air is usually blown in as secondary air. A reduction in the secondary air leads to poorer combustion of the fuel gases, a reduction in the primary air leads to poorer combustion of the slag.
  • Another task of the secondary air is to achieve a certain flame control. This is intended to break the thermals in the 1st draft of the combustion boiler (afterburning chamber) and thus create a narrow range of dwell times in the 1st draft. This goal has so far been achieved incompletely.
  • the use of tertiary air to break the thermal is only of limited use due to the additional air volume, since cooling results in additional CO formation and additional flue gas volumes.
  • a major disadvantage of the previous methods is the high amount of secondary or tertiary air required to burn out the exhaust gases safely and to break the thermals. These high air volumes can only be added if the primary air volume is reduced at the same time, although the burnout result on the grate is endangered. Increasing the amount of flue gas also leads to a shorter average residence time in the first train. Optimal pollutant degradation is therefore not guaranteed. Furthermore, the adiabatic combustion temperature is reduced by the increased amount of air. The temperature reduction in the area of the steam generator is accordingly flat. This significantly reduces the use of heat.
  • the object of the present invention is to develop a method for the combustion of solids with which it is possible to reduce the amounts of pollutants in the flue gas. Either the amount of flue gas should be significantly reduced while maintaining the same heat output, or vice versa the fuel throughput should be increased significantly. The process should be able to operate with as little excess air as possible. At the same time, the disadvantages of the known methods are to be largely avoided. The method is said to be particularly suitable for use in waste power plants.
  • the solids such as. B. garbage or coal
  • the primary combustion air is blown through the grate from below.
  • Flow through the hot flue gases generated in the combustion chamber First, an afterburner chamber (1st draft of the boiler) and then fed to the convective part of the boiler via further radiation.
  • the flue gas is then freed of dust and pollutants in a flue gas cleaning system and released into the atmosphere via a chimney.
  • no further combustion air such as e.g. Secondary or tertiary air
  • a gas and / or superheated, vaporous medium is injected into the combustion boiler 1 as a fluid medium above the combustion chamber 2 and in the lower region of the afterburning chamber 4.
  • the injection of water vapor does not promote the formation of carbon monoxide and nitrogen oxide in the flue gas.
  • the mixing energy required to generate the turbulence necessary for optimal combustion conditions of the fuel gases is applied via the water vapor. In this way, the total amount of air and the oxygen content of the flue gas can be significantly reduced.
  • the main advantages of this method of operation are a reduction in the amount of flue gas with the same net heat output and lower fuel consumption, or an increase in heat output by increasing the fuel throughput with the same amount of flue gas.
  • Determining the mixing energy which according to the invention is introduced into the combustion boiler via water vapor the set pressure and the volume flow of the water vapor.
  • a value of at least 1 bar should be selected as the minimum overpressure for the water vapor. Below this value, the volume flow of the water vapor must be set very high to ensure sufficient mixing energy. The amount of flue gas can then be reduced slightly at most. In addition, undesirably high water contents in the flue gas can result. In principle, the highest possible excess pressure of the water vapor should therefore be provided. The upper limit is only determined by the justifiable expenditure on equipment.
  • the volume flow of the water vapor to be set depends on the overpressure, with a higher volume requiring a lower volume flow and vice versa.
  • the volume flow is preferably selected so that a mixing energy in the range between 0.1 and 30 kW per m3 of turbulence space is introduced.
  • the area in the combustion boiler that is directly detected by the blown-in water vapor is referred to as the turbulence space.
  • d hydr. hydrof / U F corresponds to the cross-section through which the combustion gases flow (e.g. smallest cross-section after exiting the combustion chamber) and U denotes its circumference.
  • the mixing energy to be introduced can also be related to the exhaust gas volume.
  • mixing energies in the range between 0.03 and 3 W per Nm3 / h exhaust gas should preferably be set.
  • the temperature when entering the afterburning chamber should preferably be in the range between 1273 and 1673 K in order to ensure adequate combustion of the pollutants. Above 1673 K there is a risk of increased NO x formation even with lower oxygen levels in the flue gas.
  • the mean residence time of the flue gases in the afterburning chamber at temperatures ⁇ 1123 K can be increased to such an extent that the degradation of pollutants is considerably promoted.
  • FIG. 1 A conventional incinerator for solids according to the prior art is shown schematically in FIG. 1.
  • the grate 3 is arranged, on which the solids, such as garbage or coal, are burned with the addition of primary air 9.
  • the combustion chamber 2 Immediately above the grate 3 is the combustion chamber 2, which merges upwards into the afterburning chamber 4, corresponding to the 1st draft of the boiler.
  • the hot flue gases generated during combustion in the combustion chamber 2 first flow through the afterburning chamber 4. They are then conducted via the second train 5 of the boiler 1 to the evaporators and superheaters 6 and the ECO 7. Dust and pollutants are then removed in a flue gas cleaning system 8.
  • the supply takes place via secondary air nozzles 10, which are arranged in the combustion chamber 2 in the region of the transition to the afterburning chamber 4.
  • additional tertiary air can be blown in via tertiary air nozzles 11, which are installed in the afterburning chamber 4.
  • the amount of fuel and the amount of primary air can be reduced with the same steam output when the secondary or tertiary air is fully replaced.
  • the primary air volume and the fuel volume can be reduced by 10%, for example.
  • the amount of primary air is preferably reduced to such an extent that the excess air is between the value of 150% customary for such combustion plants and a lower limit value of 20%. With an air excess of 20%, the oxygen content in the flue gas is approx. 2%. If this value is undershot, the pollutants in the flue gases have a very aggressive effect on the boiler wall.
  • the steam is blown in via nozzles designed for supersonic operation, since this enables a particularly good conversion of pressure energy into kinetic energy.
  • the nozzles are installed in the area where the combustion gases exit from the combustion chamber 2 and / or directly in the area of the afterburning chamber 4. They are preferably arranged in one or more nozzle levels.
  • Existing systems can be converted to the method according to the invention in a simple manner by directly installing the nozzles for the water vapor instead of already existing secondary and / or tertiary air nozzles.
  • the combustion and mixing conditions in the combustion chamber 2 and in the inlet to the afterburning chamber 4 are optimized in particular. If, in addition or as an alternative, the water vapor is blown directly into the afterburning chamber 4, z. B. of smoke streaks favors the formation of a uniform piston flow. In this way, it is possible to generate a uniformly narrow residence time spectrum in the afterburning chamber 4 and to significantly increase the pollutant burnup.
  • the dust content of the exhaust gas can be separated with exceptionally high efficiency in the electrical flue gas cleaning.
  • the dust concentration in the exhaust gas after the electrostatic precipitator can be reduced to about 10 mg / Nm3.
  • gases or gas mixtures could also be used instead of water vapor, which are also composed in such a way that they do not promote the formation of CO and NO x in the flue gas, such as, for. B. recycled flue gas or nitrogen and other inert gases or mixtures thereof.
  • these gases are usually present under normal pressure or only a slight excess pressure, so that an extraordinarily high outlay on equipment would be necessary to set the high pressures required for the process according to the invention.
  • the amount to be supplied is so high that the advantages of the process according to the invention cannot be achieved.
  • the hot flue gas can e.g. B. can be returned via one or more connecting channels from the 2nd train to the 1st train of the boiler.
  • the water vapor nozzles are preferably arranged concentrically in the connecting channels for the recirculated flue gas. Due to the injector effect of the steam injected under high pressure, some of the hot flue gases are sucked out of the 2nd draft of the boiler and injected into the combustion boiler together with the water vapor without complex measures. Since the pressure conditions to be overcome for this flue gas recirculation are very low, only a correspondingly small amount of steam is required for this.
  • the proportion of recirculated flue gas is set to values between 5 and 50%, preferably around 30%, of the total flue gas quantity.
  • the maximum temperatures, the temperature reduction and the dwell times in the 1st and 2nd draft of the boiler can thus be easily adjusted to optimal values.
  • nitrogen or other inert gases or their mixtures can be injected into the combustion boiler together with the high-pressure water vapor by the process according to the invention.
  • the oxygen content of the flue gas dropped to approximately 6% by volume (moist). With comparable fuel, the air ratio dropped from 2.5 to 1.8. The amount of flue gas decreased from 100,000 Nm3 / h to 72,500 Nm3 / h and was thus reduced by a total of approx. 27%. The NO x content of the flue gas was reduced by approx. 25%. At the same time, the CO content of the flue gas dropped from 20 mg / Nm3 to values below 10 mg / Nm3.
  • the exhaust gas temperature after the steam generators was reduced from approx. 500 K to approx. 470 K. This increased the chloride separation in the flue gas cleaning system and reduced the HCl emission concentration from 50 to 80 mg / Nm3 to values below 30 mg / Nm3.
  • the dust carried in the flue gas and the hydrated lime used for dry flue gas cleaning, as well as the corresponding reaction products, can be separated out excellently in the electrical flue gas cleaning due to the higher water vapor partial pressure. This behavior is favored by the lower flue gas temperatures. Dust emissions are also positively influenced by the significantly lower gas speeds in the electrical flue gas cleaning system.
  • the dust content in the flue gas after the electrostatic precipitator was reduced from 40 to 60 mg / Nm3 to approx. 10 mg / Nm3.
  • the combustion temperature in the entrance to the afterburner was increased by approx. 200 K.
  • the flue gas temperature at the end of the afterburner rose only slightly by 30 to 50 K.
  • hot flue gas with a temperature of approx. 900 K was returned to the 1st train of the boiler together with part of the water vapor.
  • Some of the nozzles for the steam were installed concentrically in the individual flue gas return channels. Due to the suction effect of the water vapor injected under a pressure of approx. 6 bar, part of the flue gases was withdrawn from the second draft (convective part) and injected into the 1st draft of the boiler. The proportion of the returned flue gas was 30% of the total flue gas amount.
  • the pressure conditions to be overcome were very low with a maximum of 1 to 5 mbar, so that only a little steam was required to return the flue gases.
  • the temperature in the hot zone could e.g. from approximately 1473 K (without flue gas recirculation) to approximately 1308 K.
  • the temperature in the transition to the 1st train could be reduced while maintaining a minimal amount of combustion air.
  • the temperature reduction in the 1st and 2nd draft was somewhat flatter in this case, while the temperature and heat reduction in the convective part of the boiler practically matched the corresponding values without flue gas recirculation. Even under these conditions, a minimum dwell time of 2 s at temperatures above 1123 K could easily be maintained.
  • the other advantages as described when using water vapor without flue gas recirculation are retained.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Incineration Of Waste (AREA)
  • Chimneys And Flues (AREA)
  • Air Supply (AREA)
  • Solid-Fuel Combustion (AREA)
  • Gasification And Melting Of Waste (AREA)
EP92920686A 1991-10-08 1992-10-02 Verfahren zur verbrennung von feststoffen Expired - Lifetime EP0607210B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE4133239 1991-10-08
DE4133239 1991-10-08
PCT/EP1992/002280 WO1993007422A1 (de) 1991-10-08 1992-10-02 Verfahren zur verbrennung von feststoffen

Publications (2)

Publication Number Publication Date
EP0607210A1 EP0607210A1 (de) 1994-07-27
EP0607210B1 true EP0607210B1 (de) 1996-01-31

Family

ID=6442216

Family Applications (1)

Application Number Title Priority Date Filing Date
EP92920686A Expired - Lifetime EP0607210B1 (de) 1991-10-08 1992-10-02 Verfahren zur verbrennung von feststoffen

Country Status (8)

Country Link
US (1) US5553556A (cs)
EP (1) EP0607210B1 (cs)
AT (1) ATE133772T1 (cs)
CZ (1) CZ284076B6 (cs)
DE (1) DE59205258D1 (cs)
DK (1) DK0607210T3 (cs)
SK (1) SK281396B6 (cs)
WO (1) WO1993007422A1 (cs)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012000262A1 (de) 2012-01-10 2013-07-11 Jörg Krüger Verfahren und Vorrichtung zur Verbesserung des Ausbrandes von Schlacken auf Verbrennungsrosten

Families Citing this family (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19511609C2 (de) * 1995-03-30 1998-11-12 Muellkraftwerk Schwandorf Betr Verfahren und Vorrichtung zur Verbrennung von Feststoffen
DE59509469D1 (de) * 1995-05-05 2001-09-06 Bbp Environment Gmbh Verfahren und Feuerung zum Verbrennen von Abfällen
US5906806A (en) * 1996-10-16 1999-05-25 Clark; Steve L. Reduced emission combustion process with resource conservation and recovery options "ZEROS" zero-emission energy recycling oxidation system
DE19723298A1 (de) * 1997-06-04 1998-12-10 Abb Patent Gmbh Verfahren zur Steuerung der Mischungsgüte bei der Müllverbrennung
US5937772A (en) * 1997-07-30 1999-08-17 Institute Of Gas Technology Reburn process
DE19938269A1 (de) * 1999-08-12 2001-02-15 Asea Brown Boveri Verfahren zur thermischen Behandlung von Feststoffen
US6647903B2 (en) * 2000-09-14 2003-11-18 Charles W. Aguadas Ellis Method and apparatus for generating and utilizing combustible gas
DE10051733B4 (de) * 2000-10-18 2005-08-04 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verfahren zur gestuften Verbrennung von Brennstoffen
DE10339133B4 (de) * 2003-08-22 2005-05-12 Fisia Babcock Environment Gmbh Verfahren zur NOx-Minderung in Feuerräumen und Vorrichtung zur Durchführung des Verfahrens
US7140309B2 (en) * 2003-09-22 2006-11-28 New Energy Corporation Method of clean burning and system for same
AU2006263659B2 (en) * 2005-06-28 2010-09-30 Community Power Corporation Method and apparatus for automated, modular, biomass power generation
US8038744B2 (en) * 2006-10-02 2011-10-18 Clark Steve L Reduced-emission gasification and oxidation of hydrocarbon materials for hydrogen and oxygen extraction
US7833296B2 (en) * 2006-10-02 2010-11-16 Clark Steve L Reduced-emission gasification and oxidation of hydrocarbon materials for power generation
WO2008137815A1 (en) * 2007-05-04 2008-11-13 Clark Steve L Reduced-emission gasification and oxidation of hydrocarbon materials for liquid fuel production
US10641173B2 (en) * 2016-03-15 2020-05-05 Bechtel Power Corporation Gas turbine combined cycle optimized for post-combustion CO2 capture
CN114383137B (zh) * 2021-12-31 2024-08-20 中环国投生态科技股份有限公司 一种垃圾热解气化处理设备

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CH428063A (de) * 1965-03-31 1967-01-15 Von Roll Ag Verfahren zur Verbrennung von Abfallbrennstoffen, insbesondere Müll, sowie Verbrennungsofen zur Durchführung dieses Verfahrens
US3473331A (en) * 1968-04-04 1969-10-21 Combustion Eng Incinerator-gas turbine cycle
CH583881A5 (cs) * 1975-07-04 1977-01-14 Von Roll Ag
US4028551A (en) * 1975-10-17 1977-06-07 Champion International Corporation Apparatus and method for corona discharge priming a dielectric web
US4285282A (en) * 1977-12-22 1981-08-25 Russell E. Stadt Rubbish and refuse incinerator
DE3125429A1 (de) * 1981-06-27 1983-02-03 Erk Eckrohrkessel Gmbh, 1000 Berlin "einrichtung zur durchmischung von gasstraehnen"
DE3915992A1 (de) * 1988-05-19 1989-11-23 Theodor Koch Verfahren zur reduktion von stickstoffoxiden
EP0487052B1 (en) * 1990-11-22 1997-02-12 Hitachi Zosen Corporation Refuse incinerator

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102012000262A1 (de) 2012-01-10 2013-07-11 Jörg Krüger Verfahren und Vorrichtung zur Verbesserung des Ausbrandes von Schlacken auf Verbrennungsrosten
WO2013104407A2 (de) 2012-01-10 2013-07-18 Krüger, Jörg Verfahren und vorrichtung zur verbesserung des ausbrandes von schlacken auf verbrennungsrosten
DE102012000262B4 (de) * 2012-01-10 2015-12-17 Jörg Krüger Verfahren und Vorrichtung zur Verbesserung des Ausbrandes von Schlacken auf Verbrennungsrosten

Also Published As

Publication number Publication date
SK40594A3 (en) 1994-08-10
WO1993007422A1 (de) 1993-04-15
SK281396B6 (sk) 2001-03-12
DE59205258D1 (de) 1996-03-14
ATE133772T1 (de) 1996-02-15
CZ80294A3 (en) 1994-08-17
DK0607210T3 (da) 1996-03-18
EP0607210A1 (de) 1994-07-27
US5553556A (en) 1996-09-10
CZ284076B6 (cs) 1998-08-12

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