EP0291937B1 - Verfahren und Vorrichtung zur Bindung von Salzbildnern an Feststoffen bei der Verbrennung von fossilen Brennstoffen, Müll o. dgl. - Google Patents

Verfahren und Vorrichtung zur Bindung von Salzbildnern an Feststoffen bei der Verbrennung von fossilen Brennstoffen, Müll o. dgl. Download PDF

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Publication number
EP0291937B1
EP0291937B1 EP88107907A EP88107907A EP0291937B1 EP 0291937 B1 EP0291937 B1 EP 0291937B1 EP 88107907 A EP88107907 A EP 88107907A EP 88107907 A EP88107907 A EP 88107907A EP 0291937 B1 EP0291937 B1 EP 0291937B1
Authority
EP
European Patent Office
Prior art keywords
process according
reaction chamber
fire bed
basic substances
combustion
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
EP88107907A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0291937A2 (de
EP0291937A3 (en
Inventor
Horst Welzel
Otto Faatz
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.)
Eee European Engineering & Environment Sah
Original Assignee
Teset 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
Priority claimed from DE3717191A external-priority patent/DE3717191C1/de
Application filed by Teset AG filed Critical Teset AG
Priority to AT88107907T priority Critical patent/ATE71979T1/de
Publication of EP0291937A2 publication Critical patent/EP0291937A2/de
Publication of EP0291937A3 publication Critical patent/EP0291937A3/de
Application granted granted Critical
Publication of EP0291937B1 publication Critical patent/EP0291937B1/de
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
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K1/00—Preparation of lump or pulverulent fuel in readiness for delivery to combustion apparatus
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/10—Treating solid fuels to improve their combustion by using additives
    • 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
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/70—Blending
    • F23G2201/701—Blending with additives
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2201/00—Pretreatment of solid fuel
    • F23K2201/50—Blending
    • F23K2201/505—Blending with additives

Definitions

  • the invention relates to a method and an apparatus for binding salt formers to solids in the combustion of fossil fuels, garbage or the like.
  • basic substances in particular CaCO3 or MgCO3, are added to the garbage before combustion.
  • DE-A-32 43 969 discloses a process for flue gas desulfurization in the combustion of sulfur-containing solid fuels, in which a fine-grained absorbent is mixed with the solid fuel before the combustion.
  • the solid fuel and the fine-grained absorbent are burned together, with a suitable air duct ensuring that the temperatures in the reaction zone do not exceed 900 ° C.
  • An incorporation reaction for the sulfur is clearly aimed at during the combustion process.
  • the invention is based on the object of designing a method of the type mentioned at the outset such that practically no more acid gases are formed during the combustion from the salt formers, so that subsequent flue gas cleaning is unnecessary.
  • the method according to the invention aims to obtain a practically one hundred percent conversion of the salt formers into harmless compounds which have a high thermal strength, that is to say a high thermal dissociation temperature, even before the fire bed. This makes it possible to retain the new compounds virtually completely in the slag if the combustion temperature is set so that the fire bed temperature is below this dissociation temperature.
  • the use of calcium carbonate or magnesium carbonate means that the thermal dissociation temperature is 850 ° C. or higher, so that, without prior examination of the waste, preferably a fire bed temperature below 850 ° C., preferably below 810 ° C is set.
  • the effective temperature in the combustion chamber for waste incineration is u. U. much higher, so that an effective waste incineration is achieved even when setting the fire bed temperature below 850 ° C.
  • the stoichiometric ratio between the basic substances and the salt formers is preferably below 4.2: 1, in particular approximately 2: 1.
  • the stoichiometric ratio depends on the type of addition of the basic substances, that is on the fine distribution of the basic substances achieved Within the fossil fuels, the garbage or the like. A very fine distribution, i.e. intimate mixing of basic substances with the fossil fuels, the garbage or the like, is achieved if the basic substances are sprayed on, for example.
  • the specified moisture content of the fossil fuels does not refer to crystalline or chemically bound water, and by adjusting a water vapor saturation state during the dwell time it is achieved that the basic substances can react almost completely with the halogens in the fossil fuels or in the waste. Since the reactions are exothermic, considerable heating occurs. This leads to a strong evaporation, which leads to the drying of the fossil fuels, the garbage or the like. So that this can be burned well on the fire bed.
  • the residence time in the closed container between the addition of the solids and the fire bed is preferably at least 10, preferably at least 20 minutes.
  • the dwell time can advantageously result from the transport of the fossil fuels, the garbage or the like from the feed station for the basic substances to the fire bed.
  • water vapor saturation should occur at at least 40 ° C to create good reaction conditions.
  • the compounds formed with the addition of calcium carbonate or magnesium carbonate with the salt formers are, for example, CaCl2, CaSO4, Ca (NO3) 2 or MgCl2, MgSO4 and Mg (NO3) 2. These substances have the high thermal dissociation temperatures, which are not reached if the fire bed temperature is below 850 ° C, so that these substances remain in the slag and this slag is safe as a building material, e.g. B. can be used for road construction.
  • the basic substances can preferably be added as a suspension or solution of basic solids.
  • the moisture content of the fossil fuels, waste or the like is preferably set to 25% by volume.
  • an advantageous temperature can be set for the conversion of the salt formers into harmful solids with high dissociation temperatures desired before the combustion on the fire bed, without additional heating having to be carried out for this purpose.
  • the temperature set in the addition station is 180 ° to 300 ° C., preferably 300 ° C.
  • Good regulation of the low fire bed temperature can be achieved by creating a vacuum above the fire bed by gas extraction.
  • the vacuum can preferably be 0.3 mbar, the flow velocity in the combustion chamber should be ⁇ 3 m / s.
  • the hydrocarbons can also be rendered harmless in a common device, in which a post-reaction chamber which receives the combustion gas and whose walls are designed in such a way that only heat losses occur is arranged above the fire bed.
  • the walls are made of an infrared radiation material, preferably ceramic, whereby SiC connections offer particular advantages.
  • the combustion gases automatically cause a temperature of over 900 ° C, in particular a temperature between 1050 ° C - 1250 ° C occurs in the post-reaction chamber.
  • the radiation intensity of the infrared radiation for the combustion gases in the post-reaction chamber can be intensified so that under the action of the infrared radiation the hydrocarbon molecules dissociate to CO2 and HO2 or CO2 and NO2 if the exposure time of the infrared radiation is more than 0.1 s.
  • sulfur oxide and nitrogen oxide gases are also prepared in such a way that they can be conducted as sulfuric acid gases and hydrochloric acid gases in a condenser, where they are extracted from the exhaust air as acid condensate, as described, for example, in DE Patent 33 29 823.
  • the aforementioned extraction of the combustion gases is advantageous if a fresh air supply, possibly throttled, is arranged below the fire bed. This ensures that there is no temperature drop above the fire bed in the combustion gases area by secondary air, as was the case with previous secondary air supplies above the fire bed to increase the fire bed temperature. The secondary reaction is therefore not disturbed by the secondary air supply.
  • the combustion bed temperature can be kept at the desired low value by the adjustable extraction of the combustion gases. In addition, it can be prevented that too much combustion air is sucked through the fire bed, which is not required for the combustion and could therefore lower the temperature above the fire bed.
  • a measure of the correct combustion is the maintenance of a free oxygen content in the post-reaction chamber of 3 vol.% Or lower. It is therefore expedient to check the free oxygen content in the post-reaction chamber to measure and regulate the suction accordingly.
  • a device according to the invention for performing the method is shown schematically in the drawing.
  • a feed belt 2 that moves back and forth in the horizontal direction, as indicated by the double arrow A.
  • the feed belt 2 has driver wedges 3 on its upper side, which rise obliquely in the transport direction and then drop steeply in a sawtooth shape and thereby form a steep edge 4.
  • the steep edge 4 pushes during the advancement of the conveyor belt 2 over the slanted fuel in the transport direction, so that in this way a transport takes place to the right in the drawing, although the conveyor belt 2 only moves back and forth.
  • the fossil fuels are fed in from the top of the housing 1 via a dosing device 5, for example a dosing screw or a rotary valve.
  • a dosing device 5 for example a dosing screw or a rotary valve.
  • the fossil fuels fall via a stage 6 to a lower level on which a fire grate 7 is located.
  • a slide 8 is coupled, which pushes the fossil fuels on the fire grate 7 to the right in the drawing, where they form the fire bed.
  • a throttle valve 11 In the fresh air supply there is a throttle valve 11 with which the fresh air flow can be regulated.
  • an addition station 12 for a solution or a suspension of basic solids in the top of the housing 1.
  • the addition station 12 has a drip nozzle 13 with which the addition of the basic substances can be metered.
  • the after-reaction chamber 14 receives the combustion gases.
  • the after-reaction chamber 14 has ceramic side walls 15 and a ceramic one Partition 16 on, which is arranged so that a vertical riser 17 and a vertical counterflow line 18 is formed, which in an outlet 19 of the post-reaction chamber 14.
  • a separate (not shown) conventional heat exchanger At the outlet 19 is a separate (not shown) conventional heat exchanger.
  • the ceramic outer wall 15 'pointing to the feed station 12' has a large heat radiation surface.
  • the heat radiated by it is absorbed by a heat-conducting sheet 20 that extends obliquely upwards from below the conveyor belt 2 away from the fire grate 7 and is arranged directly next to the loading station 12.
  • the heat-conducting sheet is heated by the heat radiation emitted by the ceramic outer wall 15 'to a temperature which ensures a sufficient reaction temperature in the area of the feed station 12.
  • a temperature of about 300 ° C. is preferably set here, which favors the conversion of the halogens with the basic substances added to harmless reaction products with high dissociation temperatures.
  • the slightly below the drip nozzle 13 upper edge of the sheet 20 is continued with a piece of sheet metal 21 inclined to the outer wall 15 '.
  • the sheet metal piece 21 has openings for condensate liquid through which the cooled in the upper region of the housing 1 condensate liquid between sheet 20 and outer wall 15 'of the post-reaction chamber 14 and through an opening in a ceramic bottom 22 between sheet 20 and outer wall 15' on the fire grate 7 can drip so that a cycle is formed.
  • the illustrated design of the after-reaction chamber 14 ensures that the combustion gases remain in a high temperature range for a sufficient time by maintaining a low flow rate for the combustion gases by suitably adjusting the extraction system. As a result, the combustion gases are converted in the desired manner.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Incineration Of Waste (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Treating Waste Gases (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)
  • Solid-Fuel Combustion (AREA)
  • Glanulating (AREA)
  • Pyridine Compounds (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
EP88107907A 1987-05-22 1988-05-18 Verfahren und Vorrichtung zur Bindung von Salzbildnern an Feststoffen bei der Verbrennung von fossilen Brennstoffen, Müll o. dgl. Expired - Lifetime EP0291937B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT88107907T ATE71979T1 (de) 1987-05-22 1988-05-18 Verfahren und vorrichtung zur bindung von salzbildnern an feststoffen bei der verbrennung von fossilen brennstoffen, muell o. dgl.

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE3717191A DE3717191C1 (en) 1987-05-22 1987-05-22 Process for immobilising halogens on solids during the combustion of fossil fuels, refuse or the like
DE3717191 1987-05-22
DE3808485 1988-03-15
DE3808485A DE3808485A1 (de) 1987-05-22 1988-03-15 Verfahren und vorrichtung zur bindung von halogenen an feststoffen bei der verbrennung von fossilen brennstoffen oder muell

Publications (3)

Publication Number Publication Date
EP0291937A2 EP0291937A2 (de) 1988-11-23
EP0291937A3 EP0291937A3 (en) 1989-03-22
EP0291937B1 true EP0291937B1 (de) 1992-01-22

Family

ID=25855891

Family Applications (1)

Application Number Title Priority Date Filing Date
EP88107907A Expired - Lifetime EP0291937B1 (de) 1987-05-22 1988-05-18 Verfahren und Vorrichtung zur Bindung von Salzbildnern an Feststoffen bei der Verbrennung von fossilen Brennstoffen, Müll o. dgl.

Country Status (14)

Country Link
US (1) US4869182A (cs)
EP (1) EP0291937B1 (cs)
JP (1) JPH01163511A (cs)
CN (1) CN1013925B (cs)
AT (1) ATE71979T1 (cs)
CA (1) CA1295128C (cs)
CZ (1) CZ278279B6 (cs)
DE (2) DE3808485A1 (cs)
ES (1) ES2028173T3 (cs)
GR (1) GR3004163T3 (cs)
IL (1) IL86465A (cs)
LV (1) LV5547A3 (cs)
RU (1) RU2023948C1 (cs)
TR (1) TR24493A (cs)

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2249766C2 (ru) * 2002-05-08 2005-04-10 Общество с ограниченной ответственностью "Сибирские строительные материалы и Экология" ООО "СибстромЭко" Способ сжигания твердых бытовых и прочих органических отходов и устройство для его осуществления
KR100599251B1 (ko) 2003-09-20 2006-07-13 에스케이 주식회사 디메틸에테르 합성용 촉매와 촉매의 제조방법

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1526062A1 (de) * 1966-01-27 1970-03-26 Ver Kesselwerke Ag Verfahren und Einrichtung zur Verbrennung von Muell
JPS5230780A (en) * 1975-09-04 1977-03-08 Hitachi Zosen Corp Treating method of waste products containing nitrogenous organic subst ances
JPS5246682A (en) * 1975-10-11 1977-04-13 Honshu Paper Co Ltd Process for drying and incinerating a pulp waste liquor
JPS56119415A (en) * 1980-02-25 1981-09-19 Mitsubishi Heavy Ind Ltd Waste incinerating furnace
JPS574279A (en) * 1980-06-09 1982-01-09 Ebara Infilco Co Ltd Incineration treatment of waste
JPS5835315A (ja) * 1981-08-25 1983-03-02 Agency Of Ind Science & Technol 燃焼炉内での塩化水素とイオウ般化物の同時除去方法
US4465000A (en) * 1982-02-08 1984-08-14 Conoco Inc. Method of increasing the efficiency of cyclone-fired boilers using high sodium lignite fuel
DE3243969A1 (de) * 1982-11-27 1984-05-30 Viessmann Werke Kg, 3559 Allendorf Verfahren zur rauchgasentschwefelung und heizungskessel zu seiner durchfuehrung
US4487137A (en) * 1983-01-21 1984-12-11 Horvat George T Auxiliary exhaust system
DE3324627C2 (de) * 1983-07-08 1987-04-09 Müllverbrennungsanlage Wuppertal GmbH, 5600 Wuppertal Verfahren zum Verbrennen von Müll
DE3325570A1 (de) * 1983-07-15 1985-01-24 Wolf-Rüdiger 4130 Moers Naß Verfahren und vorrichtung zum entschwefeln von feststoffe enthaltenden substanzen
DE3329823C2 (de) * 1983-08-18 1987-01-29 ERA GmbH, 3300 Braunschweig Verfahren zum Entzug von SO↓x↓, NO↓x↓, Chlorverbindungen, Schwer- und Edelmetallen aus heißen Rauchgasen
US4546711A (en) * 1983-10-24 1985-10-15 Marblehead Lime Company Apparatus and method for incinerating waste material with a converted preheater-type lime kiln
JPS61197910A (ja) * 1985-02-28 1986-09-02 Sasakura Eng Co Ltd 塩化水素除去廃棄物燃焼方法および装置
US4624192A (en) * 1986-03-20 1986-11-25 Mansfield Carbon Products Fluidized bed combuster process

Also Published As

Publication number Publication date
US4869182A (en) 1989-09-26
RU2023948C1 (ru) 1994-11-30
IL86465A0 (en) 1988-11-15
DE3867905D1 (de) 1992-03-05
CZ325188A3 (en) 1993-07-14
LV5547A3 (lv) 1994-03-10
EP0291937A2 (de) 1988-11-23
CA1295128C (en) 1992-02-04
DE3808485A1 (de) 1989-09-28
TR24493A (tr) 1991-11-11
CZ278279B6 (en) 1993-11-17
CN1013925B (zh) 1991-09-18
EP0291937A3 (en) 1989-03-22
JPH01163511A (ja) 1989-06-27
GR3004163T3 (cs) 1993-03-31
CN88103007A (zh) 1988-12-21
ES2028173T3 (es) 1992-07-01
ATE71979T1 (de) 1992-02-15
IL86465A (en) 1991-11-21

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