JPH0425444B2 - - Google Patents
Info
- Publication number
- JPH0425444B2 JPH0425444B2 JP60163992A JP16399285A JPH0425444B2 JP H0425444 B2 JPH0425444 B2 JP H0425444B2 JP 60163992 A JP60163992 A JP 60163992A JP 16399285 A JP16399285 A JP 16399285A JP H0425444 B2 JPH0425444 B2 JP H0425444B2
- Authority
- JP
- Japan
- Prior art keywords
- fluidized bed
- air
- water vapor
- fluidized
- amount
- 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
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 238000002485 combustion reaction Methods 0.000 claims description 26
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims description 18
- 239000007789 gas Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 8
- 230000001603 reducing effect Effects 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 4
- 239000002918 waste heat Substances 0.000 description 9
- 239000002699 waste material Substances 0.000 description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000009841 combustion method Methods 0.000 description 2
- -1 during startup Chemical compound 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229920001807 Urea-formaldehyde Polymers 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000010985 leather Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
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
- F23L7/002—Supplying water
- F23L7/005—Evaporated water; Steam
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、ボイラ付き流動床燃焼設備において
発生する燃焼排ガス中の窒素酸化物濃度を低減す
る方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for reducing the concentration of nitrogen oxides in combustion exhaust gas generated in a fluidized bed combustion facility with a boiler.
一般に、流動床ボイラや、廃熱ボイラ付き廃棄
物流動床焼却炉等の流動床燃焼設備において、燃
料、各種廃棄物等の燃焼排ガス中には窒素酸化物
（以下「NOx」という）が含まれている。
In general, in fluidized bed combustion equipment such as fluidized bed boilers and waste fluidized bed incinerators with waste heat boilers, nitrogen oxides (hereinafter referred to as "NOx") are contained in the combustion exhaust gas of fuels, various wastes, etc. ing.
近年、国の内外を問わず公害に関する意識が定
着し、NOxに関しても規制が厳しくなつてきて
おり、このために、流動床ボイラや廃棄物流動床
焼却炉等においても、それに対応することなしで
は新設することができなくなつてきている。 In recent years, awareness of pollution has become established both domestically and internationally, and regulations regarding NOx have become stricter. For this reason, fluidized bed boilers, waste fluidized bed incinerators, etc. have to comply with these regulations. It is becoming impossible to build new ones.
従来、流動床燃焼設備における燃焼排ガス中の
NOxを低減するためには、二段燃焼法として、
流動化空気の空気過剰率を１前後に絞り、フユー
エルNOxを還元、又はNOxの発生を抑えたの
ち、残つたCOや未燃物をフリーボード部より添
加した空気で再熱焼させる方式をとつている場合
が多く、また、流動床部やフリーボード部に直接
水を注入してNOxを低下させることも一部に行
われていた。 Conventionally, in the flue gas of fluidized bed combustion equipment,
In order to reduce NOx, as a two-stage combustion method,
After reducing the excess air ratio of the fluidized air to around 1 and reducing the fuel NOx or suppressing the generation of NOx, the remaining CO and unburned materials are reheated and burned using air added from the freeboard section. In some cases, water was directly injected into the fluidized bed or freeboard section to reduce NOx.
しかしながら、流動床燃焼設備における前記従
来の二段燃焼方式によるNOx発生の抑制でも、
例えば都市ごみを消却する場合の排ガス中の
NOxを通常120ppm（O212％換算値、以下同じ）
前後以下に抑えるのは難しかつた。
However, even when suppressing NOx generation using the conventional two-stage combustion method in fluidized bed combustion equipment,
For example, in exhaust gas when municipal waste is destroyed,
Normally NOx is 120ppm (O 2 12% conversion value, same below)
It was difficult to keep it below around 100%.
また、流動床に直接水を注入する方法は、水の
潜熱を奪うために流動床温度を下げることにな
り、低位発熱量が高く、流動床を冷却しなければ
ならないものを除き好ましくはなく、さらにこの
注水方式ではあまり燃焼空気と混合し難いために
効果が部分にとどまり、十分ではなかつた。 In addition, the method of directly injecting water into the fluidized bed lowers the temperature of the fluidized bed to remove latent heat from the water, and is not preferred unless the lower heating value is high and the fluidized bed must be cooled. Furthermore, with this water injection method, it was difficult to mix with the combustion air, so the effect was limited to a limited area and was not sufficient.
本発明は、上記の問題点を解決し、簡単な操作
によつてフユーエルNOxの還元とNOxの生成抑
制を行おうとするものである。 The present invention aims to solve the above problems and reduce fuel NOx and suppress the production of NOx through simple operations.
本発明は、含水率の高いスラツジ等の流動床焼
却炉においては、スラツジ中の窒素分が可燃分中
の10％前後と高いにもかかわらず、NOxの発生
が常時約50ppm以下と低いのに着目し、幾多の実
験を重ねて完成したものであつて、ボイラ付きの
流動床燃焼設備であつて、流動床の複数個所に単
位面積当たりの流動化空気の量に差をつけて供給
するものにおいて、流動化空気の空搭速度の高い
領域に前記ボイラで発生した水蒸気を混入するこ
とを特徴とする燃焼排ガス中の窒素酸化物濃度を
低減する方法である。
In a fluidized bed incinerator for sludge with a high moisture content, the present invention is capable of generating low NOx, at about 50 ppm or less, even though the nitrogen content in the sludge is high at around 10% of the combustible content. This is a fluidized bed combustion equipment equipped with a boiler, which was developed after many experiments and which supplies different amounts of fluidized air per unit area to multiple locations in the fluidized bed. A method for reducing the concentration of nitrogen oxides in combustion exhaust gas is characterized in that water vapor generated in the boiler is mixed into a region of high empty loading velocity of fluidized air.
本発明によれば、流動床燃焼設備の発生熱を利
用したボイラで得られた水蒸気の一部を、流動床
燃焼設備の流動化空気に混入するものであるか
ら、酸素分圧を水蒸気で希釈し、同時に水蒸気を
流動床中の炭素等と流動床の熱で反応させて水性
ガスCOとＨラジカルH2を生成し、それが強力な
還元作用を行うことになる。ここで、水性ガス化
反応に流動砂が触媒として、特に反応熱供給体と
しての役割を果たしながら関与することで、脱硝
効果を生ずるのである。
According to the present invention, a part of the water vapor obtained by the boiler that utilizes the heat generated by the fluidized bed combustion equipment is mixed into the fluidized air of the fluidized bed combustion equipment, so the oxygen partial pressure is diluted with water vapor. At the same time, water vapor reacts with carbon, etc. in the fluidized bed using the heat of the fluidized bed to generate water gas CO and H radical H 2 , which performs a strong reducing action. Here, the fluidized sand participates in the water gasification reaction as a catalyst, particularly as a reaction heat supplier, thereby producing a denitrification effect.
この場合、低位発熱量の高い焼却対象物ほど一
般に同伴水が少ないために、添加する水蒸気量を
多くしなければならないが、同時に一般に燃焼用
空気を必要とするため、流動化空気量も増加させ
る傾向になる。逆に、低位発熱量の低い焼却対象
物ほど一般に同伴水が多いため、添加水蒸気量か
少なくてよく、また流動床部の出熱を抑えて少し
でも流動床部の温度を高く保持するためにも添加
水蒸気量を節減するのが好ましく、一般には燃焼
用空気量も少なくてすむ傾向にある。 In this case, the amount of water vapor added must be increased because the incineration target with a higher lower calorific value generally has less entrained water, but at the same time, the amount of fluidized air must also be increased because air for combustion is generally required. become a trend. On the other hand, the lower the lower calorific value of the incineration target, the more entrained water there is in general, so the amount of added steam can be reduced. It is also preferable to reduce the amount of added steam, and generally the amount of combustion air tends to be small.
通常、流動床部への流動化空気は、幾つかの区
画に区分されて供給されている。この場合、相対
的に焼却対象物が投入される部分より離れ、焼却
対象物に同伴された水分の蒸発が終了し激しい焼
却が行われる部分に対しては、より多量に流動化
空気が供給される。したがつて、該部分（流動化
空気の空塔速度の高にい領域）に水蒸気を混入す
る。 Usually, fluidizing air is supplied to the fluidized bed section in several sections. In this case, a larger amount of fluidizing air is supplied to the part that is relatively far away from the part where the material to be incinerated is thrown in, where the water entrained in the material to be incinerated has finished evaporating and intense incineration occurs. Ru. Therefore, water vapor is mixed into this portion (the region where the superficial velocity of the fluidizing air is high).
また、適切な燃焼用空気量となるよう燃焼排ガ
ス中の酸素濃度等によつて加減している流動化空
気量を計測し、それに対して一定の比率となるよ
うに添加水蒸気量を制御することが好ましい。 In addition, the amount of fluidized air, which is adjusted depending on the oxygen concentration in the combustion exhaust gas, etc., is measured to ensure an appropriate amount of combustion air, and the amount of added water vapor is controlled to be a constant ratio. is preferred.
なお、立上げ時など、添加水蒸気中に水滴が混
入する場合も考えられるが、これは水蒸気量を正
確に把握できなかつたり、流動化空気を押込む均
圧室等での発錆やスケール付着などの原因となる
ために好ましくはないが、特に脱硝反応の意味で
は問題ない。 Note that there may be cases where water droplets get mixed into the added water vapor, such as during startup, but this may be due to the inability to accurately determine the amount of water vapor, or rusting or scale buildup in the pressure equalization chamber where fluidized air is forced. However, it is not a problem, especially in terms of denitrification reactions.
流動床燃焼設備における燃焼対象物としては、
窒素分を多く含み、同伴水の少ないものほどその
効果は顕著であり、例えば、石炭、高質乃至基準
質の都市ごみ、皮類、尿素樹脂等の窒素分を含む
プラスチツクなどが挙げられる。 The objects to be combusted in fluidized bed combustion equipment are:
The effect is more pronounced as it contains more nitrogen and less entrained water; examples include coal, high-quality or standard-quality municipal waste, leather, plastics containing nitrogen such as urea resin, and the like.
さらに、本発明の実施例を図面に参照しながら
説明すると、流動床焼却炉１のフリーボード部２
には廃熱ボイラ３が連結され、廃熱ボイラ３では
流動床焼却炉１の廃熱を回収して水蒸気４を発生
させている。廃熱ボイラ３で発生した水蒸気４は
蒸気ヘツダ５に導かれ、その一部を、流動床焼却
炉１の流動化空気として押込送風機６から供給さ
れる押込空気を予熱するための予熱器７で利用す
る。
Furthermore, to explain an embodiment of the present invention with reference to the drawings, the freeboard portion 2 of the fluidized bed incinerator 1
A waste heat boiler 3 is connected to the waste heat boiler 3, and the waste heat boiler 3 recovers waste heat from the fluidized bed incinerator 1 to generate steam 4. Steam 4 generated in the waste heat boiler 3 is led to a steam header 5, and a part of it is used as fluidized air for the fluidized bed incinerator 1 in a preheater 7 for preheating forced air supplied from a forced air blower 6. Make use of it.
流動床焼却炉１は、流動床９の中央部に供給機
１０によつて焼却対象物を投入し、流動化空気の
床単位面積当たりの押込風量を、中央の均圧室１
１の部分では相対的に両端の均圧室１２，１２に
対して抑え、かつ両側壁を内部にせり出させたデ
イフレクタ１３と呼ぶ形状にすることで、流動床
９の部分での矢印の如き旋回流を流動砂に与える
ことにより、中央部では水分蒸発と蒸し焼き、両
端部では激しい燃焼を行わせているため、両端の
均圧室１２，１２に水蒸気を混入し、中央の均圧
室１１には水蒸気を混入しない。 In the fluidized bed incinerator 1, materials to be incinerated are fed into the center of a fluidized bed 9 by a feeder 10, and the amount of forced air per unit area of the bed is controlled by a pressure equalizing chamber 1 in the center.
In the part 1, by forming a shape called a deflector 13, which is relatively suppressed against the pressure equalizing chambers 12, 12 at both ends and having both side walls protruding inside, the part 1 is shaped like an arrow in the part of the fluidized bed 9. By applying a swirling flow to the fluidized sand, water vapor evaporates and steams in the center, and intense combustion occurs at both ends, so water vapor is mixed into the pressure equalizing chambers 12 at both ends, and the pressure equalizing chamber 11 in the center is mixed. Do not mix water vapor.
このように、流動床燃焼炉１の均圧室１２，１
２への流動化空気に、その廃熱ボイラ３からの水
蒸気４の一部を混入することによつて、酸素分圧
を水蒸気で希釈し、水性ガス化反応に伴う還元作
用により燃焼排ガス中のNOxを低減させること
ができ、例えば、都市ごみを焼却した場合、流動
化空気への体積で２割程度の水蒸気混入で、燃焼
排ガス中のNOx濃度を80ppm以下に抑えること
ができた。 In this way, the pressure equalization chambers 12, 1 of the fluidized bed combustion furnace 1
By mixing a part of the water vapor 4 from the waste heat boiler 3 into the fluidized air 2, the oxygen partial pressure is diluted with water vapor, and the reduction effect accompanying the water gasification reaction reduces the amount of water in the combustion exhaust gas. NOx can be reduced. For example, when municipal waste is incinerated, the NOx concentration in the combustion exhaust gas can be suppressed to 80 ppm or less by mixing about 20% of the volume of water vapor into the fluidized air.
図中、１４は二次送風機であつて、流動床９で
の未燃物や残留COを再燃焼させるために、流動
床燃焼炉１のフリーボード部２に送気するための
ものである。 In the figure, reference numeral 14 is a secondary blower, which is used to supply air to the freeboard section 2 of the fluidized bed combustion furnace 1 in order to re-burn unburned materials and residual CO in the fluidized bed 9.
なお、水蒸気混入後に流動床焼却炉１の空気吹
込用の均圧室壁面などで結露することは、錆の発
生や空気中に含まれる粉じん等の付着を生じるた
め、長期的には好ましくないので、壁温を水蒸気
混入後の空気の露点以上に保持する必要がある。
そのために、予熱器７にて押込送風機６からの押
込空気を露点（80℃前後）以上の温度にまで予熱
しておくことが好ましい。この場合、図示例のよ
うに、予熱された押込空気の温度に応じて指示調
節温度計TICを利用して、予熱用の水蒸気量を調
節するとよい。 It should be noted that condensation on the walls of the pressure equalization chamber for air blowing in the fluidized bed incinerator 1 after water vapor is mixed in is undesirable in the long term because it causes rust and adhesion of dust contained in the air. , it is necessary to maintain the wall temperature above the dew point of the air after mixing with water vapor.
For this purpose, it is preferable to preheat the forced air from the forced air blower 6 to a temperature equal to or higher than the dew point (approximately 80° C.) using the preheater 7. In this case, as shown in the illustrated example, it is preferable to adjust the amount of water vapor for preheating using the indicating adjustment thermometer TIC according to the temperature of the preheated forced air.
また、水蒸気混入に際しては、流動床焼却炉１
での焼却対象物の低位発熱量に関連して増減され
る押込空気量に対して一定の比率となるように制
御することが好ましく、図示例のように、押込送
風機６で押込まれる空気量を指示流量計FIにて
計測する一方、水蒸気量を指示調節流量計FICに
て計測し、水蒸気量が流動化空気量に対して一定
の比率とるように流動調節弁８を作動させて制御
するとよい。この場合、通常の都市ごみでは還元
ガス生成反応を伴うために、添加水蒸気量は流動
化空気量の１〜３割程度で十分な効果を発揮させ
ることができ、廃熱ボイラ３の発生蒸気の１割前
後をふりむけるだけでよい。 In addition, when water vapor is mixed in, the fluidized bed incinerator 1
It is preferable to control the amount of forced air to be a constant ratio to the amount of forced air that is increased or decreased in relation to the lower calorific value of the object to be incinerated. is measured by the indicating flow meter FI, while the amount of water vapor is measured by the indicating regulating flow meter FIC, and the flow control valve 8 is operated and controlled so that the amount of water vapor has a constant ratio to the amount of fluidized air. good. In this case, since ordinary municipal waste involves a reducing gas production reaction, the amount of added steam can be sufficiently effective with about 10 to 30% of the amount of fluidized air, and the amount of steam generated by the waste heat boiler 3 can be All you have to do is focus on around 10%.
〔発明の効果〕
以上述べたように、本発明によれば、ボイラ付
き流動床燃焼設備において、高価な触媒方式など
を採用することなしに、ボイラで発生した水蒸気
の一部を流動化空気の空搭速度の高い領域に混入
するのみの簡単な方法よつて、従来の技術の限界
とされていた燃焼排ガス中中のNOx濃度120ppm
の壁を取ることができ、そのための装置も技術的
問題はなく単純なものとし、さらに混入する水蒸
気も系外か入手する必要なく、特に今後の都市ご
み焼却炉或いは今後の一般化する傾向にる石炭流
動床ボイラ等におけるNOx対策として、カルシ
ウムの炉内投入による脱硫と相俟つて、設備の大
小にかかわらず適用容易である。[Effects of the Invention] As described above, according to the present invention, in a fluidized bed combustion equipment with a boiler, a part of the water vapor generated in the boiler can be converted into fluidized air without adopting an expensive catalyst system. By using a simple method that only mixes NOx into areas with high empty loading speed, it is possible to reduce the concentration of NOx in combustion exhaust gas to 120ppm, which was considered to be the limit of conventional technology.
The wall can be removed, the equipment for that purpose is simple and there are no technical problems, and there is no need to obtain water vapor from outside the system, especially in future municipal waste incinerators or in the future, which will become more common. As a NOx countermeasure in coal fluidized bed boilers, etc., it is easy to apply, in combination with desulfurization by introducing calcium into the furnace, regardless of the size of the equipment.
図面は本発明の一実施例を示す系統説明図であ
る。
１……流動床焼却炉、２……フリーボード部、
３……廃熱ボイラ、４……水蒸気、５……蒸気ヘ
ツダ、６……押込送風機、７……予熱器、８……
流量調節弁、９……流動床、１０……供給機、１
１，１２……均圧室、１３……デイフレクタ、１
４……二次送風機。
The drawing is a system explanatory diagram showing an embodiment of the present invention. 1...Fluidized bed incinerator, 2...Freeboard section,
3... Waste heat boiler, 4... Steam, 5... Steam header, 6... Forced blower, 7... Preheater, 8...
Flow rate control valve, 9... Fluidized bed, 10... Supply machine, 1
1, 12... pressure equalization chamber, 13... deflector, 1
4... Secondary blower.
Claims (1)
床の複数個所に単位面積当たりの流動化空気の量
に差をつけて供給するものにおいて、流動化空気
の空搭速度の高い領域に前記ボイラで発生した水
蒸気を混入することを特徴とする燃焼排ガス中の
窒素酸化物濃度を低減する方法。 ２ 前記水蒸気の混入量を、流動化空気量に対し
て一定の比率となるように制御するものである特
許請求の範囲第１項記載の燃焼排ガス中の窒素酸
化物濃度を低減する方法。[Claims] 1. In a fluidized bed combustion equipment equipped with a boiler, in which fluidized air is supplied to multiple locations in the fluidized bed with different amounts of fluidized air per unit area, the empty loading speed of the fluidized air is A method for reducing the concentration of nitrogen oxides in combustion exhaust gas, the method comprising: mixing water vapor generated in the boiler into a region where the nitrogen oxide concentration is high. 2. The method for reducing the concentration of nitrogen oxides in combustion exhaust gas according to claim 1, wherein the amount of water vapor mixed in is controlled to be a constant ratio to the amount of fluidized air.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60163992A JPS6226404A (en) | 1985-07-26 | 1985-07-26 | Reducing method for nitrogen oxides concentration in burnt exhaust gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60163992A JPS6226404A (en) | 1985-07-26 | 1985-07-26 | Reducing method for nitrogen oxides concentration in burnt exhaust gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6226404A JPS6226404A (en) | 1987-02-04 |
| JPH0425444B2 true JPH0425444B2 (en) | 1992-04-30 |
Family
ID=15784701
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60163992A Granted JPS6226404A (en) | 1985-07-26 | 1985-07-26 | Reducing method for nitrogen oxides concentration in burnt exhaust gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6226404A (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH03158614A (en) * | 1989-11-16 | 1991-07-08 | Nkk Corp | Method of igniting in fluidized bed type incinerator |
| FR2682459B1 (en) * | 1991-10-09 | 1997-11-21 | Stein Industrie | METHOD AND DEVICES FOR REDUCING THE NITROGEN PROTOXIDE CONTENT OF THE GASES OF AN OXIDIZING COMBUSTION OF A FLUIDIZED BED REACTOR. |
| JP2001296008A (en) * | 2000-04-12 | 2001-10-26 | P C Center:Kk | Incinerator |
| JP2001296002A (en) * | 2000-04-12 | 2001-10-26 | P C Center:Kk | Combustion method utilizing water |
| BG105259A (en) * | 2001-02-16 | 2002-08-30 | Бойко БОЖИЛОВ | Method for the recuperation of waste water steam in firing of solid, liquid and gaseous fuels |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61128513U (en) * | 1985-01-23 | 1986-08-12 |
-
1985
- 1985-07-26 JP JP60163992A patent/JPS6226404A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6226404A (en) | 1987-02-04 |
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