EP1846694B1 - Verfahren zur reduzierung von stickoxidemissionen eines kessels mit blasenbildendem wirbelbett - Google Patents

Verfahren zur reduzierung von stickoxidemissionen eines kessels mit blasenbildendem wirbelbett Download PDF

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EP1846694B1
EP1846694B1 EP06708960.7A EP06708960A EP1846694B1 EP 1846694 B1 EP1846694 B1 EP 1846694B1 EP 06708960 A EP06708960 A EP 06708960A EP 1846694 B1 EP1846694 B1 EP 1846694B1
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air
fluidized bed
fuel
furnace
volatile matter
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French (fr)
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EP1846694A4 (de
EP1846694A1 (de
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Pauli Dernjatin
Marko Fabritius
Jukka RÖPPÄNEN
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Valmet Technologies Oy
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Valmet Technologies Oy
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • 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
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/10—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of field or garden waste or biomasses
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2201/00—Staged combustion
    • F23C2201/10—Furnace staging
    • F23C2201/101—Furnace staging in vertical direction, e.g. alternating lean and rich zones

Definitions

  • the invention relates to a method for reducing nitrogen oxide emissions of a bubbling fluidized bed boiler burning biofuel according to the preamble of the appended claim 1.
  • biofuel refers to solid fuels, wherein the portion of volatile matter in ash-free dry solids is over 60%.
  • This type of fuels are, for example, peat, bark, wood chips, sawdust, waste construction timber, sludge created in process industry, and municipal solid waste.
  • Bubbling fluidized bed boilers are generally used in energy production, wherein the fuels include biofuels, such as, for example, peat and wood chips.
  • the fuels include biofuels, such as, for example, peat and wood chips.
  • a fluidized bed which is composed of a fine, incombustible material, typically sand, which fluidizes over a grate forming the bottom of the boiler.
  • the fluidizing of the material is created by feeding fluidizing gas through the grate to the fluidized bed.
  • the fluidizing gas can be composed solely of air, so-called primary air, or it may be a gas mixture formed by primary air and inert gas, for example, flue gas.
  • a bubbling fluidized bed boiler the flow rate of the fluidizing gas supplied through the grate is set into such that the particles forming the fluidized bed do not escape with air to the upper part of the boiler, but they remain in the lower part of the furnace forming a fluidized bed that is continuously moving and efficiently mixes the fluidized bed material and the fuel supplied to it.
  • the combustion air needed for burning fuel is generally supplied stagewise and in several portions to the furnace of the boiler in such a manner that a part of combustion air, i.e. fluidizing air, is formed by the primary air blown through the grate with the fluidizing gas a part is formed by secondary air supplied above the fluidized bed, and the rest of the combustion air is supplied to the upper part of the furnace of the boiler as so-called tertiary air.
  • the boiler can also be divided into different air zones according to the air supplied to the boiler: the area between the fluidized bed and the secondary air supply is called the primary air zone, and the area between the secondary air supply and the tertiary air supply is called the secondary
  • Fuel is fed by means of so-called carrier air to the bubbling fluidized bed boiler on the fluidized bed.
  • the drying of fuel particles i.e. pyrolysis
  • the combustion of the remaining carbon residue i.e. pyrolysis
  • Drying and pyrolysis are very fast compared to the total combustion time of fuel particles.
  • the volatile matter released in pyrolysis are mainly methane, CH 4 and carbon monoxide CO, as well as nitrogen oxide emissions causing ammonia NH 3 and hydrogen cyanide HCN.
  • the volatile matter rises upwards and burns when reaching an oxygenous area.
  • a boiler equipped with staged air the combustion of volatile matter primarily is done by secondary air and partly tertiary air, and the combustion of the carbon residue of fuel particle is done by fluidizing, secondary and tertiary air.
  • staged air supply By means of the staged air supply it is possible to reduce the formation of nitrogen oxides. That is, when there is oxygen, NH 3 and HCN react into nitrogen monoxide NO.
  • staging the air supply reducing, substoichiometric areas are formed in the furnace of the bubbling fluidized bed boiler. In these areas the NH 3 and HCN formed of fuel are reduced to molecular nitrogen in accordance with the following reaction equations 1 and 2: and
  • reaction equation 3 nitrogen oxides are reduced by means of an internal reburning reaction, wherein the hydrocarbon radicals formed in pyrolysis take part in reducing nitrogen oxides.
  • reaction equation 3 An example of this kind of reaction is shown in reaction equation 3, wherein the hydrocarbon radical is -CHi.
  • the reducing areas are formed by adjusting the amount of fluidizing and secondary air.
  • the furnace is maintained substoichiometric in relation to oxygen until the tertiary air supply, in which case the delay time needed for reactions (1) and (2) is maximized and the amount of NH 3 and HCN is minimized before the tertiary air level.
  • the optimum total air coefficient before the tertiary air supply in relation to NO x emissions is slightly below 1 depending on the combustion temperature.
  • the air required for the burning out of volatile matter and carbon residue is supplied to the furnace as tertiary air.
  • the residue NH 3 and HCN in the flue gases are oxidized after the tertiary air zone into nitrogen oxides.
  • the nitrogen oxide emissions can be reduced approximately 30% in comparison to a non-staged air supply. Still problematic are the fine and light fuels, because most of the fuel particles do not end up in the fluidized bed, but they are pulled with the fluidizing gas and secondary air to the upper parts of the furnace. Thus, it is almost impossible for the fuels to create fuel combustion conditions in the furnace that are controlled and favourable to reducing nitrogen oxides.
  • Publication WO 02/090829 also discloses a nitrogen oxide reduction method based on the staging of combustion air.
  • recirculation gas composed of flue gases is supplied between the supply points of secondary and tertiary airs, in the elevation of the bubbling fluidized bed boiler.
  • the nitrogen oxides contained by the recirculation gas take part in the final stage of the above-presented reduction reactions (1) and (2) and intensify the reaction of nitrogen compounds formed of the fuel into molecular nitrogen.
  • the problem with this solution is that it causes the amount of flue gases in the boiler to increase, in which case the size of the furnace must be increased, which in turn raises the price of the boiler.
  • the method is suitable mainly for dry fuels. With wet fuels the amount of heat needed for drying reduces the combustion temperature in the secondary stage too much, thus preventing the creation of conditions favourable for reducing the nitrogen oxides.
  • publication US 6230664 B1 also discloses also discloses a nitrogen oxide reduction method based on the staging of combustion air.
  • the purpose of the present invention is to provide a method for reducing nitrogen oxide emissions of a bubbling fluidized bed boiler burning biofuel, by means of which the above-mentioned drawbacks can be avoided.
  • the method according to the invention is primarily characterized in what will be presented in the characterizing part of the independent claim 1.
  • the invention is based on the idea that the nitrogen oxide emissions of a bubbling fluidized bed boiler are reduced by using a staged air supply in such a manner that a part of primary air is supplied in connection with fuel supply, i.e. with the fuel or within the immediate vicinity of the fuel supply point in the same direction as the fuel itself.
  • This part of primary air is in this application referred to as the combustion air of volatile matter.
  • the pyrolysis following the drying and the combustion of the volatile matter released from the fuel in the pyrolysis also takes place almost immediately after the fuel has mixed with the fluidized bed, because the fuel and the oxygen in the air supplied in connection with it are mixed quickly. Due to the quick mixing of the fuel and the oxygen, most of the volatile matter released from the fuel can be burnt in the upper part of the fluidized bed and on the fluidized bed, before the supply of secondary air.
  • the combustion of volatile matter creates a high temperature, which maximizes the creation of hydrocarbon radicals formed of the fuel and promotes the reduction of the released nitrogen oxides.
  • the amount of combustion air of volatile matter supplied in connection with the fuel supply is adjusted into such that the combustion of volatile matter released in pyrolysis from the fuel being burnt takes place in substoichiometric conditions in relation to the volatile matter.
  • the air coefficient SR v in relation to the volatile matter is thus as high as possible, however, below 1, advantageously between 0.75 to 0.97 and preferably between 0.90 to 0.95.
  • the total air coefficient SR tot on the same level of the furnace varies between 0.50 to 0.80, advantageously being 0.65.
  • Secondary air is supplied form the secondary air nozzles and tertiary air is supplied from the tertiary air nozzles placed above the secondary air nozzles.
  • the task of the fluidizing gas supplied to the furnace through its bottom is to maintain the fluidized bed bubbling and its temperature suitable.
  • the combustion air amounts supplied in different stages of the staged combustion are thus adjusted, i.e. the total air coefficient SR tot needed for combustion and further the air coefficient in relation to the volatile matter SR v .
  • Feeding the fuel with air to the fluidized bed in such a manner that substantially all the fuel particles are forced there enables controlling the combustion substantially better than at present. Further, the amount of unburnt fuel can be minimized, because the delay time of fuel in the furnace is longer than in the solutions according to prior art.
  • the method it is not the amount of air supplied to the furnace nor the total air coefficient that is affected, but how the air distribution is performed in order to have the air coefficient in relation to the volatile matter of the fuel as high as possible as low in the furnace as possible and yet as long as possible before the secondary air nozzles.
  • Fig. 1 shows a side view of a furnace of a bubbling fluidized bed boiler 1.
  • a fluidized bed 2 composed of bed material on the bottom of the furnace.
  • Fluidizing gas is supplied to the furnace 1 through nozzles 4 arranged on its bottom 3, which gas fluidizes the bed material.
  • the fluidizing gas can be solely air, or it may be a mixture of air and recirculating gas.
  • the fuel is supplied to the fluidized bed 2 from fuel supply means 5 arranged above the surface of the fluidized bed and placed substantially on a mutually same level. In the figure there are three fuel feeding means, but their number may vary depending on the size of the furnace or other parameters of the boiler.
  • Fuel feeding means can also be arranged on the opposite side wall (not shown) of the furnace substantially on the same level with the fuel feeding means arranged on the side wall, as shown in the figure. They can also be placed on the front and/or back walls of the furnace.
  • the fuel is fed to the fluidized bed by means of air.
  • the amount of air used in connection with fuel feeding is so large, that it prevents fuel particles from escaping to the upper parts of the furnace by directing the fuel substantially on the surface of the fluidized bed.
  • the additional air, combustion air of the volatile matter supplied in connection with air supply is a part of primary air.
  • Secondary air is supplied from secondary air nozzles 6 located above the fuel feeding means to above the fluidized bed 2. Tertiary air is supplied to the furnace above the secondary air nozzles 6 via tertiary air nozzles 7 arranged in the upper part of the furnace.
  • the amount of air supplied to the furnace does not therefore increase in comparison to a conventional solution, but it is distributed in a different manner.
  • the amount of primary air supplied as fluidizing gas or as a part of it and the amount of tertiary air remain substantially equal to conventional staged combustion.
  • separate combustion air of volatile matter is supplied to the furnace, which air correspondingly decreases the amount of secondary air.
  • Fig. 2 shows a front view of a furnace 1 of a bubbling fluidized bed boiler.
  • Fuel is fed from a fuel supply means 5 to the fluidized bed 2.
  • Fuel feeding takes place by means of carrier air and the combustion air of volatile matter, in which case the fuel-air-mixture 8 is forced all the way to the surface 2a of the fluidized bed 2.
  • Finely divided fuel supplied to the fluidized bed dries immediately when coming into contact with hot bed material and pyrolizes substantially entirely.
  • the volatile matter released from the fuel burn on the surface 2a of the fluidized bed 2 and above the surface 2a of the fluidized bed by means of primary air forming a first, reducing primary air zone 9, which extends from the upper part of the fluidized bed to the secondary air nozzles 6.
  • the combustion of volatile matter takes place in the primary air zone 9 in substoichiometric conditions in relation to the air coefficient SR v of volatile matter.
  • the total air coefficient SR tot is naturally below 1.
  • the air coefficient SR v in relation to volatile matter is as large as possible, but still a little below 1, the volatile matter burns quickly and forms a high local temperature, and it forms a maximum amount of hydrocarbon radicals, which are needed in order to reduce nitrogen oxides formed from the fuel.
  • the reducing secondary air zone 10 extends from the secondary air nozzles all the way to the tertiary air nozzles arranged over them.
  • Reducing the nitrogen oxides formed from fuel into molecular nitrogen is thus performed in two stages.
  • the first reducing stage i.e. in the primary air zone 9
  • most of the volatile matter released from the fuel and a part of the carbon residue is burnt. This takes place in relation to both the total air coefficient SR tot and the air coefficient SR v of the volatile matter of the fuel in substoichiometric conditions, which results in a large amount of hydrocarbon radicals.
  • the primary air required in this stage is brought to the furnace in connection with fuel supply and at least as a part of the fluidizing gas. 75 to 95%, preferably 90% of the air needed for combustion of pyrolysis gases is supplied as primary air.
  • the second reducing stage i.e.
  • combustion air is supplied to the furnace from secondary air nozzles 6 arranged within a distance from the surface of the fluidized bed in such a manner that the substoichiometric conditions remain, i.e. the total air coefficient SR tot is still below 1.
  • the air coefficient SR v of volatile matter of the fuel rises in this zone above 1. Feeding of primary air in the manner described above in two stages, as fluidizing air and as combustion air of volatile matter has the effect that the temperatures in the lower parts of the furnace are higher than in known boilers equipped with staged air distribution. By means of the method, the fuel is inflamed quickly and most of the volatile matter can be burnt before the actual secondary air level.
  • FIG 2 there are three secondary and tertiary air nozzles 6 and 7 side by side on the front wall of the furnace. Their number and placement may vary depending on the size of the boiler. The air nozzles can also be placed on the side walls of the boiler.
  • the following tables 1 and 2 show two examples of applying the method in a bubbling fluidized bed boiler, whose firing rate is 300 MW.
  • the examples show stagewise both the air distribution in a bubbling fluidized bed boiler according to prior art and the air distribution in the same boiler in accordance with the method when the fuel and boiler load remain the same.
  • the air amount (kg/s) supplied to the boiler in each stage, the total air coefficient SR tot of the stage in question and the air coefficient in relation to the volatile matter SR v are shown.
  • the fuel is peat and in the example of table 2 the fuel is wood.
  • Air distribution according to prior art Air distribution according to the invention Air (kg/s) SR tot SR v Air (kg/s) SR tot SR v Fluidizing air 41 0,39 0,66 41 0,39 0,66 Carrier air 6 0,44 0,76 6 0,44 0,76 Combustion air of volatile matter 0 0,44 0,76 12 0,56 0,95 Start-up burner cooling 3,5 0,48 0,81 3,5 0,59 1,00 Secondary air 44 0,89 1,52 32 0,89 1,52 Load carrying burner cooling 4 0,93 1,58 4 0,93 1,58 Tertiary air 23 1,14 1,95 23 1,14 1,95 Total 121,5 1,145 1,952 121,5 1,145 1,952 121,5 1,145 1,952
  • the percentage of the volatile matter of the dry fuel flow is approximately 70 mass-%, coke approximately 24.5 mass-% and ash approximately 5.5 mass-%.
  • the moisture content of the fuel is 46 mass-%.
  • Table 2. Fuel wood, full power of the boiler. Air distribution according to prior art Air distribution according to the invention Air (kg/s) SR tot SR v Air (kg/s) SR tot SR v Fluidizing air 38 0,36 0,48 38 0,36 0,48 Carrier air 6 0,42 0,55 6 0,42 0,55 Combustion air of volatile matter 0 0,42 0,55 31,5 0,72 0,95 Start-up burner cooling 3,5 0,45 0,60 3,5 0,75 0,99 Secondary air 46,5 0,89 1,18 15 0,89 1,18 Load carrying burner cooling 4 0,93 1,23 4 0,93 1,23 Tertiary air 23 1,15 1,52 23 1,15 1,52 Total 121 1,147 1,520 121 1,147 1,520 121 1,147 1,520
  • the percentage of the volatile matter of the dry fuel flow is approximately 85 mass-%, coke approximately 13 mass-% and ash approximately 2 mass-%.
  • the moisture content of the fuel is 46 mass-%.
  • the new air distribution according to the method has an effect on the amounts of additional air and secondary air supplied in connection with fuel supply.
  • the other, fluidizing air and tertiary air supplied together with the fluidizing gas, as well as the small air amounts used in cooling start-up burners and load carrying burners remain the same as in air distribution according to prior art.
  • the amount of air supplied together with the fuel is significantly larger than the amount of carrier air used for fuel supply in prior art.
  • the amount of air supplied with the fuel varies depending on the fuel, because different fuels contain different amounts of volatile matter and the purpose is to burn them in substoichiometric conditions before the supply of secondary air.
  • the additional air fed in connection with fuel supply i.e. the combustion air of volatile matter, which is a part of primary air
  • fuel supply i.e. the combustion air of volatile matter, which is a part of primary air
  • Figure 3a shows a fuel supply means 5, i.e. a fuel feeding opening 5a seen from the inside of the furnace, wherein the fuel and the combustion air supplied with it are mixed right before they are fed to the furnace together.
  • the feeding opening 5a is rectangular, which is the most advantageous form for a feeding opening, but otherwise shaped feeding openings may also be applied.
  • the fuel and combustion air are fed parallel to the furnace.
  • the fuel is fed to the furnace by means of carrier air from the fuel feeding opening 5a, which is on three sides surrounded by a uniform air channel 11 for supplying combustion air of volatile matter.
  • the air channel 11 is a uniform channel and it surrounds the fuel feeding opening from its three sides in such a manner that there is no air supply from below the feeding opening 5a.
  • the air channels 11a, 11 b and 11c are separate air channels in relation to the fuel feeding opening 5a, which channels are placed within a small distance from the fuel feeding opening 5a, on its three sides.
  • the air channels 11 a to 11c are also placed in such a manner that there is no air channel under the fuel feeding opening 5a.
  • the design of the air channel and the placement of the air channels 11 a to 11c in relation to the fuel feeding opening help in directing the fuel particles to be directed to the fluidized bed.
  • Figure 4 shows the portion of pyrolysis gas in a furnace above the surface of the bed, wherein the portion of pyrolysis gases formed as a result of air distribution according to prior art is illustrated by dashed lines and the portion of pyrolysis gases reached by means of the method is illustrated with a solid line.
  • the graphs show that by means of the method the releasing and combustion of pyrolysis gas mostly take place before the secondary air supply.
  • the releasing of pyrolysis gas significantly takes place before the secondary air level, but because of lack of oxygen hardly any combustion takes place. Because of the escaping fuel particles, the releasing of pyrolysis gases takes place even on secondary and tertiary air levels.
  • Figure 5 shows the temperature distribution above the bed of a furnace.
  • the temperature distribution according to prior art is shown by dashed lines and the temperature distributions reached by means of the method are shown by a solid line. It can be seen from the graphs that by means of the method the temperature of the furnace is higher in the primary air zone than in a bubbling fluidized bed boiler equipped with air distribution according to prior art. The temperature remains higher almost to the tertiary level, after which it decreases to lower than in prior art, because there is no more combustible matter left.

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  • General Engineering & Computer Science (AREA)
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Claims (10)

  1. Verfahren zur Verringerung der Stickoxidemissionen eines sprudelnden Wirbelschichtkessels, der mit Biobrennstoff befeuert wird, wobei das Verfahren Folgendes umfasst:
    - Zuführen mindestens primärer Luft in eine Wirbelschicht (2), die in einem unteren Bereich einer Feuerungsanlage (1) des Wirbelschichtkessels angeordnet ist, welcher für das Wirbelschichtmaterial bestimmt ist, das die Wirbelschicht (2) in der Feuerungsanlage bildet,
    - Einspeisen von Brennstoff, der flüchtige Stoffe umfasst, in die Wirbelschicht (2), wobei dieser trocknet, wenn er mit dem heißen Schichtmaterial in Kontakt kommt, und eine Pyrolyse zu einem Pyrolysegas erfährt, das flüchtige Stoffe des Brennstoffs umfasst, wobei das Pyrolysegas nach oben in die Feuerungsanlage aufsteigt und dort verbrennt,
    - Verbrennen mindestens eines Teils des Kohlenstoffrückstands aus der Pyrolyse in der Wirbelschicht (2) mit der primären Luft,
    - Zuführen von sekundärer Luft oberhalb der Wirbelschicht, ausgehend von Sekundärluftdüsen, und
    - Zuführen von tertiärer Luft oberhalb der Sekundärluftdüsen, ausgehend von Tertiärluftdüsen,
    gekennzeichnet durch:
    - Zuführen von Luft zum Verbrennen flüchtiger Stoffe in die Feuerungsanlage (1), um mindestens einen Teil des Pyrolysegases zu derart zu verbrennen, dass der Brennstoff zwangsläufig im Wesentlichen an die Oberfläche der Wirbelschicht (2) gelangt und der Brennstoff, welcher flüchtige Stoffe umfasst, im Wesentlichen vollständig zu Pyrolysegas pyrolysiert wird, wobei die Luft zum Verbrennen flüchtiger Stoffe zusammen mit dem Brennstoff oder parallel zu dem Brennstoff der Feuerungsanlage (1) zugeführt wird,
    - Verbrennen mindestens eines Teils des Pyrolysegases in einem Primärluftbereich (9), der sich zwischen einem oberen Abschnitt der Wirbelschicht und den Sekundärluftdüsen (6) befindet, wobei die Luftzahl im Verhältnis zu den flüchtigen Stoffen im Pyrolysegas im unterstöchiometrischen Bereich liegt, wobei die Luftzahl im Verhältnis zu den flüchtigen Stoffen 0,75 bis 0,97 beträgt und die Luftzahl im Primärluftbereich insgesamt 0,5 bis 0,8 beträgt, und
    - Verbrennen des Pyrolysegases in einem unterstöchiometrischen Sekundärluftbereich (10), der sich zwischen den Sekundärluftdüsen und den Tertiärluftdüsen (7) befindet, wobei die Luftzahl im Verhältnis zu den flüchtigen Stoffen mehr als 1 beträgt und die Gesamtluftzahl 0,7 bis 0,95 beträgt.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Luft zum Verbrennen flüchtiger Stoffe der Feuerungsanlage (1) derart zugeführt wird, dass mindestens ein Teil des Pyrolysegases verbrannt wird, bevor der Feuerungsanlage Sekundärluft zugeführt wird.
  3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass der Teil des Pyrolysegases mittels der Primärluft verbrannt wird, welchr der Feuerungsanlage zugeführt wird.
  4. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass der Brennstoff durch den Impuls der zugeführten Luft zum Verbrennen flüchtiger Stoffe zwangsläufig an die Oberfläche der Wirbelschicht gelangt.
  5. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass der Primärluftbereich (9) viele Kohlenwasserstoffradikale umfasst, die Stickoxide reduzieren.
  6. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Luft zum Verbrennen flüchtiger Stoffe der Feuerungsanlage (1) derart zugeführt wird, dass die Luftzahl (SRv) im Verhältnis zu den flüchtigen Stoffen 0,90 bis 0,95 beträgt.
  7. Verfahren nach Anspruch 6, dadurch gekennzeichnet, dass die Gesamtluftzahl (SRtot) 0,65 beträgt.
  8. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass der Sekundärluftbereich auf Stickoxide reduzierend wirkt, wobei die Gesamtluftzahl (SRtot) im Sekundärluftbereich 0,85 bis 0,9 beträgt.
  9. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Luft zum Verbrennen flüchtiger Stoffe der Feuerungsanlage (1) rundum eine Brennstoff-Einspeiseöffnung (5a) zugeführt wird,.
  10. Verfahren nach Anspruch 1, gekennzeichnet durch das Zuführen von zurückgeführtem Gas in die Wirbelschicht (2), um das Schichtmaterial, welches die Wirbelschicht (2) in der Feuerungsanlage (1) bildet, in einen fließfähigen Zustand zu versetzen.
EP06708960.7A 2005-02-11 2006-02-09 Verfahren zur reduzierung von stickoxidemissionen eines kessels mit blasenbildendem wirbelbett Active EP1846694B1 (de)

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FI20055063A FI20055063A (fi) 2005-02-11 2005-02-11 Menetelmä kerrosleijukattilan typenoksidipäästöjen vähentämiseksi ja kerrosleijukattilan ilmanjakojärjestelmä
PCT/FI2006/050056 WO2006084954A1 (en) 2005-02-11 2006-02-09 A method for reducing nitrogen oxide emissions of a bubbling fluidized bed boiler and an air distribution system of a bubbling fluidized bed boiler

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EP1846694A1 EP1846694A1 (de) 2007-10-24
EP1846694A4 EP1846694A4 (de) 2012-01-04
EP1846694B1 true EP1846694B1 (de) 2017-05-10

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US (1) US20080149012A1 (de)
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WO (1) WO2006084954A1 (de)

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CA2615344A1 (en) * 2006-12-22 2008-06-22 Covanta Energy Corporation Tertiary air addition to solid waste-fired furnaces for nox control
US20080149010A1 (en) 2006-12-22 2008-06-26 Covanta Energy Corporation Tertiary air addition to solid waste-fired furnaces for nox control
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CA2597159C (en) 2013-10-22
CA2597159A1 (en) 2006-08-17
EP1846694A4 (de) 2012-01-04
US20080149012A1 (en) 2008-06-26
FI20055063A (fi) 2006-08-12
WO2006084954A1 (en) 2006-08-17
FI20055063A0 (fi) 2005-02-11
EP1846694A1 (de) 2007-10-24

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