JP2994887B2 - Furnace desulfurization and denitration method for pressurized fluidized bed boiler - Google Patents
Furnace desulfurization and denitration method for pressurized fluidized bed boilerInfo
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- JP2994887B2 JP2994887B2 JP4313310A JP31331092A JP2994887B2 JP 2994887 B2 JP2994887 B2 JP 2994887B2 JP 4313310 A JP4313310 A JP 4313310A JP 31331092 A JP31331092 A JP 31331092A JP 2994887 B2 JP2994887 B2 JP 2994887B2
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- Japan
- Prior art keywords
- fluidized bed
- limestone
- fluidized
- bed
- furnace
- 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.)
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、加圧流動床ボイラの炉
内脱硫方法に関し、また、石炭等の固体燃料やＣＷＭ、
重油等の液体燃料の燃焼から発生する亜酸化窒素（Ｎ2
Ｏ）を低減する加圧流動床ボイラの炉内脱硫脱硝方法に
関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for desulfurization of a pressurized fluidized-bed boiler in a furnace.
Nitrous oxide (N 2) generated from the combustion of liquid fuels such as heavy oil
The present invention relates to a method for desulfurization and denitration in a furnace of a pressurized fluidized-bed boiler for reducing O).
【０００２】[0002]
【従来の技術】二度のオイルショック以来、世界各国に
おいて石油代替エネルギ開発の一環として石炭の再利用
が高まり、石炭エネルギ転換技術として石炭焚流動床燃
焼炉及び加圧型石炭焚流動床燃焼炉（以下加圧流動床ボ
イラと略する）、加圧型流動床、噴流床石炭ガス化炉等
の実用化研究が盛んに行われている。2. Description of the Related Art Since the two oil shocks, the recycling of coal has increased in various countries around the world as part of the development of alternative energy to petroleum, and coal-fired fluidized bed combustion furnaces and pressurized coal-fired fluidized bed combustion furnaces ( A pressurized fluidized bed boiler (hereinafter abbreviated as boiler), a pressurized fluidized bed, a spouted bed coal gasifier and the like have been actively studied for practical use.
【０００３】この中で、加圧流動床ボイラは、設備が小
さく建設費が安くなること、炉内脱硫が可能なこと、ガ
スタービンとの組合せによる発電効率の向上が見込まれ
ることの特徴から、開発至近距離のものとして注目され
ている。[0003] Among them, pressurized fluidized bed boilers are characterized by small facilities, low construction costs, in-furnace desulfurization, and improvement in power generation efficiency by combination with a gas turbine. It is attracting attention as a close-range product.
【０００４】加圧流動床ボイラでは、高圧下（１５気圧
程度）で脱硫剤として用いられる石灰石又はドロマイト
に含んだＣａＯを炉内に投入する燃料（石炭）中の燃焼
性Ｓ量に対して１〜２倍になるように調整して、空気で
流動床を形成する。そして、流動床中に燃料（石炭等）
を供給し、８００〜９００℃の最適な脱硫温度にて燃焼
させることにより、燃焼とともに発生するＳ化合物をＣ
ａに固定させる炉内脱硫と低温燃焼及びオーバファイア
エア（Ｏ・Ｆ・Ａ）燃焼によるＮ化合物の炉内脱硝を行
うことを目的とする。[0004] In a pressurized fluidized-bed boiler, the amount of combustible S in a fuel (coal) in which CaO contained in limestone or dolomite used as a desulfurizing agent under high pressure (about 15 atm) is introduced into a furnace is considered. Adjust to ~ 2x to form a fluidized bed with air. And the fuel (coal etc.) in the fluidized bed
And combust at an optimum desulfurization temperature of 800 to 900 ° C. to reduce the S compound generated with combustion to C
The purpose of the present invention is to perform in-furnace denitrification of N compounds by in-furnace desulfurization, low-temperature combustion, and overfire air (OFA) combustion fixed to a.
【０００５】[0005]
【発明が解決しようとする課題】前記の加圧流動床ボイ
ラにおいて、平均径０．８mmの石灰石と平均径１．０mm
の石炭を用いてＣa ／Ｓのモル比を２に設定し、圧力１
５気圧、流動床温度８５０℃の条件で運転した結果６５
〜７５％の脱硫率しか得られず、充分な脱硫率を得るこ
とは困難であった。In the pressurized fluidized bed boiler described above, limestone having an average diameter of 0.8 mm and limestone having an average diameter of 1.0 mm are used.
, The molar ratio of Ca / S was set to 2 and the pressure was 1
As a result of operating under the conditions of 5 atm and fluidized bed temperature of 850 ° C, 65
Only a desulfurization rate of ~ 75% was obtained, and it was difficult to obtain a sufficient desulfurization rate.
【０００６】一方、成層圏のオゾン層破壊の原因物質の
一つである亜酸化窒素（Ｎ2 Ｏ）は一般に高温度（１３
００℃以上）での燃焼方式（微粉炭燃焼、ガス燃焼、油
燃焼等）では殆ど生じないが、加圧流動床ボイラでは炉
内脱硫温度の関係上、低温度（７００〜９００℃）で燃
焼させるため、数百ppm の濃度のＮ2 Ｏが発生し、炉内
の空気比を小さくしてもＮ2 Ｏの発生量は低下しなかっ
た。On the other hand, nitrous oxide (N 2 O), which is one of the substances causing the depletion of the ozone layer in the stratosphere, generally has a high temperature (13 ° C.).
Although it hardly occurs in the combustion method (pulverized coal combustion, gas combustion, oil combustion, etc.) with the temperature of 00 ° C or more, combustion at a low temperature (700 to 900 ° C) occurs in the pressurized fluidized bed boiler due to the desulfurization temperature in the furnace. For this reason, N 2 O was generated at a concentration of several hundred ppm, and the amount of generated N 2 O did not decrease even if the air ratio in the furnace was reduced.
【０００７】本発明は、このような従来技術の課題を解
決するためになされたもので加圧流動床ボイラにおい
て、効率良い炉内脱硫及び亜酸化窒素（Ｎ2 Ｏ）の発生
を低減することを目的とする。SUMMARY OF THE INVENTION The present invention has been made to solve the problems of the prior art, and it is an object of the present invention to provide a pressurized fluidized-bed boiler with efficient furnace desulfurization and reduction of nitrous oxide (N 2 O) generation. With the goal.
【０００８】[0008]
（１） 本発明の加圧流動床ボイラの炉内脱硫方法は、
加圧流動床ボイラの流動床を形成している粗粒の石炭と
粗粒の石灰石中に流動床重量の３％以下の超微粒の石灰
石を供給して炉内脱硫を行わせることを特徴とする。 （２） また、本発明の加圧流動床ボイラの炉内脱硫脱
硝方法は、前記（１）の加圧流動床ボイラの炉内脱硫方
法において、加圧流動床ボイラの流動床表面と気泡の破
裂個所に空気又は酸素を噴霧して流動床から排出される
微粉の未燃炭素を燃焼させ、流動床表面温度を９００℃
〜１０００℃に制御して亜酸化窒素を熱分解して除去す
ることを特徴とする。(1) The in-furnace desulfurization method of the pressurized fluidized-bed boiler of the present invention comprises:
Ultra-fine limestone of 3% or less of the weight of the fluidized bed is supplied into coarse coal and coarse limestone forming the fluidized bed of the pressurized fluidized-bed boiler to perform in-furnace desulfurization. I do. (2) The method for desulfurization and denitration in a furnace of a pressurized fluidized-bed boiler according to the present invention is the method for desulfurization in a furnace of a pressurized fluidized-bed boiler according to the above (1), wherein Air or oxygen is sprayed at the rupture location to burn fine unburned carbon discharged from the fluidized bed, and the fluidized bed surface temperature becomes 900 ° C.
It is characterized in that nitrous oxide is thermally decomposed and removed by controlling the temperature to ~ 1000 ° C.
【０００９】[0009]
【作用】前記本発明（１）では、流動床内に超微粒の石
灰石が滞留するために、石灰石の反応表面積が従来の粗
粒の石灰石を使用した場合に比して数十倍に増加し、石
灰石のＳＯ2 ガスとの反応割合が増加して脱硫率が向上
する。According to the present invention (1), since the ultrafine limestone stays in the fluidized bed, the reaction surface area of the limestone is increased by several tens of times as compared with the case where the conventional coarse limestone is used. In addition, the reaction rate of limestone with SO 2 gas increases, and the desulfurization rate improves.
【００１０】流動床内における超微粒の石灰石の濃度が
流動床重量の３％を超えると、それ以上超微粒の石灰石
を流動床内に保持させることが困難となり、未反応の超
微粒の石灰石が反応しないまま系外に排出されてしまう
ことになる。従って、本発明（１）においては、超微粒
の石灰石の量を流動床重量の３％以下とした。When the concentration of ultrafine limestone in the fluidized bed exceeds 3% of the weight of the fluidized bed, it becomes difficult to keep the ultrafine limestone in the fluidized bed further, and unreacted ultrafine limestone becomes unreacted. It will be discharged out of the system without reacting. Therefore, in the present invention (1), the amount of ultrafine limestone is set to 3% or less of the fluidized bed weight.
【００１１】また、石灰石は３〜５μm の大きさの石灰
石結晶粒子の集まりから形成されており、超微粒の石灰
石はその大きさを小さくする程表面積が増大して脱硫反
応速度を増加することができるが、石灰石の粉砕技術と
経済性を考慮すると、本発明（１）においては、超微粒
の石灰石の大きさは０．１〜２０μm 程度の範囲とする
のが適当であり、特に約２０μm 前後とするのが最適で
ある。Further, limestone is formed from a collection of limestone crystal particles having a size of 3 to 5 μm, and ultra-fine limestone has a surface area which increases as the size decreases, and the desulfurization reaction rate increases. However, in consideration of the limestone crushing technique and economy, in the present invention (1), the size of the ultrafine limestone is suitably in the range of about 0.1 to 20 μm, and particularly about 20 μm. It is most suitable.
【００１２】本発明（２）においては、前記本発明
（１）において、加圧流動床ボイラの流動床表面と気泡
の破裂個所に空気又は酸素を噴霧して流動床から排出さ
れる微粉の未燃分を燃焼させる。前記本発明（１）にお
いては、前記したように、炉内脱硫を行うために通常低
温度（７００〜９００℃）での燃焼が行われるが、本発
明（２）においては、流動床表面と気泡の破裂個所に空
気又は酸素を噴霧して微粉の未燃炭素を燃焼させて流動
床表面温度を９００〜１０００℃に維持する。これによ
って、Ｎ2 Ｏを熱分解してＮ2 Ｏが効果的に低減され
る。[0012] In the present invention (2), in the present invention (1), air or oxygen is sprayed on the fluidized bed surface of the pressurized fluidized bed boiler and the rupture point of bubbles to remove fine powder discharged from the fluidized bed. Burn the fuel. In the present invention (1), as described above, combustion at a low temperature (700 to 900 ° C.) is usually performed in order to perform in-furnace desulfurization. Air or oxygen is sprayed at the rupture points of the bubbles to burn fine unburned carbon, and the fluidized bed surface temperature is maintained at 900 to 1000 ° C. Thereby, N 2 O is thermally decomposed to effectively reduce N 2 O.
【００１３】[0013]
【実施例】図１は、本発明の一実施例に用いられる加圧
流動床ボイラの縦断面図である。FIG. 1 is a longitudinal sectional view of a pressurized fluidized-bed boiler used in one embodiment of the present invention.
【００１４】図１において、流動床１は、図示しない加
圧容器の内側に設けた水冷壁２に囲まれ、分散板３上に
形成されている。流動床１とは分散板３の下方から供給
されるガスによって粒子が浮遊し、ガスにより混合攪拌
されている状態であり、その上方には粒子の存在割合が
流動床１よりも１桁以上小さくなったフリーボード４が
存在する。粗粒の石炭５は供給ノズル７から、また、粗
粒の石灰石６と超微粉石灰石６ａは、供給ノズル８か
ら、それぞれ流動床１へ供給され、空気９は空気供給ノ
ズル１０から風箱１１を経て、分散板３の多数の小孔３
ａから流動床１へ供給される。In FIG. 1, a fluidized bed 1 is surrounded by a water cooling wall 2 provided inside a pressurized container (not shown) and formed on a dispersion plate 3. The fluidized bed 1 is a state in which particles are suspended by a gas supplied from below the dispersion plate 3 and are mixed and stirred by the gas. Above that, the existing ratio of the particles is at least one digit smaller than that of the fluidized bed 1. There is a free board 4. The coarse coal 5 is supplied from the supply nozzle 7, and the coarse limestone 6 and the ultrafine limestone 6 a are supplied from the supply nozzle 8 to the fluidized bed 1, and the air 9 is supplied from the air supply nozzle 10 to the wind box 11. Through a number of small holes 3 in the dispersion plate 3
a to the fluidized bed 1.
【００１５】また、水冷壁２と流動床１内に設置された
冷却管１２とは、流動床１内の反応熱を除去するため、
それぞれ、冷却水１３、１４が供給されている。流動床
１内の粗大粒子は、流動床１の下部から下方へ延びる排
出管１５から排出される。燃焼ガスは、フリーボード４
で燃焼ガスに随伴された未燃粒子および脱硫剤粒子を重
力分級により分離した後、フリーボード４の上部に開口
する排出口１６からダストを含んだ燃焼排ガス１７とし
て排出される。The water cooling wall 2 and the cooling pipe 12 installed in the fluidized bed 1 are used to remove reaction heat in the fluidized bed 1.
Cooling waters 13 and 14 are supplied, respectively. The coarse particles in the fluidized bed 1 are discharged from a discharge pipe 15 extending downward from the lower part of the fluidized bed 1. Combustion gas is free board 4
After the unburned particles and desulfurizing agent particles entrained in the combustion gas are separated by gravity classification, they are discharged as a combustion exhaust gas 17 containing dust from a discharge port 16 opened at an upper portion of the free board 4.
【００１６】さらに、流動床１の上部には、複数の燃焼
用空気ノズル１８が流動床１の表面に向って設置され、
流動床表面及び気泡の破裂箇所に空気（又は酸素）１９
が供給されるようになっている。Further, a plurality of combustion air nozzles 18 are provided above the fluidized bed 1 toward the surface of the fluidized bed 1.
Air (or oxygen) 19 at the fluidized bed surface and at the point where bubbles burst
Is supplied.
【００１７】次に、以上に説明した加圧流動床ボイラの
運転方法の一具体例について述べる。Next, a specific example of an operation method of the pressurized fluidized bed boiler described above will be described.
【００１８】まず初めに、流動床１、フリーボード４に
空気供給ノズル１０から空気９を通気し、１６ata に加
圧する。例えば、２．０mm以下に粉砕・分級した粗粒の
石炭５と粒径が１．４１〜０．５mmの粗粒の石灰石６を
それぞれ石炭、石灰石ノズル７、８より供給し、約１メ
ートルの高さの流動床１を形成する。流動床１の空塔速
度を０．８〜１．０ｍ／sec 、Ｃa ／Ｓのモル比を２．
０前後に調整する。また、流動床１の温度は石炭供給量
と冷却管１２に通水する冷却水１４の水量とにより調整
し、流動床１内を最適な脱硫温度８００〜８７０℃の範
囲内である８５０℃にコントロールを行う。First, air 9 is passed through the fluidized bed 1 and the free board 4 from the air supply nozzle 10 and pressurized to 16 ata. For example, coarse coal 5 pulverized and classified to 2.0 mm or less and coarse limestone 6 having a particle size of 1.41 to 0.5 mm are supplied from coal and limestone nozzles 7 and 8, respectively, and are supplied by approximately 1 meter. A fluidized bed 1 of height is formed. The superficial velocity of the fluidized bed 1 is 0.8 to 1.0 m / sec, and the molar ratio of Ca / S is 2.
Adjust to around 0. The temperature of the fluidized bed 1 is adjusted by the amount of coal supplied and the amount of the cooling water 14 flowing through the cooling pipe 12, and the inside of the fluidized bed 1 is set to 850 ° C., which is within the optimum desulfurization temperature of 800 to 870 ° C. Take control.
【００１９】この結果、燃焼排ガス１７中の亜硫酸ガス
（ＳＯ2 ）、酸化窒素（ＮＯ）、亜酸化窒素（Ｎ
2 Ｏ）、濃度は、それぞれ、ＳＯ2 ＝６４ppm （Ｏ2 −
６％換算）脱硫率７０％、ＮＯ＝３９ppm （Ｏ2 −６％
換算）、Ｎ2 Ｏ＝１２３ppm （Ｏ2−６％換算）であっ
た。As a result, sulfur dioxide (SO 2 ), nitric oxide (NO), and nitrous oxide (N
2 O) and the concentration were SO 2 = 64 ppm (O 2 −
Desulfurization rate 70%, NO = 39ppm (O 2 -6%)
Equivalent), it was N 2 O = 123ppm (O 2 -6% conversion).
【００２０】前記のＳＯx は連続ＳＯx 計（非分散型赤
外法）またＮＯは連続ＮＯx 計、さらにＮ2 Ｏはガスク
ロマトグラフィを用いて行った。The above SO x was measured using a continuous SO x meter (non-dispersive infrared method), NO was measured using a continuous NO x meter, and N 2 O was measured using gas chromatography.
【００２１】本発明の実施例では、前記の運転条件を基
に、約２０μm の超微粒石灰石６ａを１．４１〜０．５
mmの粗粒石灰石６中に重量比で２．５％になるように調
整し石灰石供給ノズル８から流動床１に供給する。この
場合、流動床重量割合は、チャー０．２〜１％、灰分１
０〜５０％、石灰石５０〜９０％となり、超微粒石灰石
６ａは流動床総重量の３％となる。In the embodiment of the present invention, the ultrafine limestone 6a having a thickness of about 20 .mu.
The weight is adjusted to 2.5% by weight in the coarse-grained limestone 6 mm and supplied to the fluidized bed 1 from the limestone supply nozzle 8. In this case, the weight ratio of the fluidized bed is char 0.2-1%, ash content 1
0 to 50% and limestone 50 to 90%, and the ultrafine limestone 6a accounts for 3% of the total weight of the fluidized bed.
【００２２】この超微粒石灰石６ａの反応表面積は著し
く大きく、ＳＯ2 ガスとの反応が充分に行われる。この
結果、排ガス１７中のＳＯ2 ＝６４ppm （Ｏ2 −６％換
算）から３８ppm （Ｏ2 −６％換算）に低減することが
できた（脱硫率８３％）。The reaction surface area of the ultrafine limestone 6a is extremely large, and the reaction with SO 2 gas is sufficiently performed. As a result, SO 2 in the exhaust gas 17 was reduced from 64 ppm (O 2 -6% conversion) to 38 ppm (O 2 -6% conversion) (desulfurization rate 83%).
【００２３】一方ＮＯ及びＮ2 Ｏ値は変化しなかった。On the other hand, NO and N 2 O values did not change.
【００２４】さらに、燃料用空気ノズル１８から空気１
９を流動床１の表面及び気泡の破裂箇所に噴霧する。こ
れによって、流動床１の表面及びフリーボード４の下部
の温度は８４５℃から９４３℃に上昇し、排ガス１７中
のＮ2 Ｏは２４ppm 、ＮＯは３５ppm 、ＳＯ2 は３６pp
m に低減することが判明した。Further, the air 1 from the fuel air nozzle 18
9 is sprayed on the surface of the fluidized bed 1 and the rupture point of bubbles. As a result, the temperature of the surface of the fluidized bed 1 and the lower part of the free board 4 rises from 845 ° C. to 943 ° C., N 2 O in the exhaust gas 17 is 24 ppm, NO is 35 ppm, and SO 2 is 36 pp.
m.
【００２５】本実施例において、以上の通り、超微粉石
灰石を流動床内に供給することは、石灰石の反応表面積
は大幅に増大し、ＳＯ2 低減手段として有効である。一
方、流動床表面及び気泡の破裂部に燃料用空気又は酸素
を噴霧して微粉の未燃炭素を燃焼させることによって、
流動床表面の温度を９００℃以上に維持することがで
き、Ｎ2 Ｏを大幅に低減させることができる。In the present embodiment, as described above, supplying ultrafine limestone into the fluidized bed greatly increases the reaction surface area of limestone and is effective as a means for reducing SO 2 . On the other hand, by spraying air or oxygen for fuel on the fluidized bed surface and the rupture portion of bubbles to burn fine unburned carbon,
The temperature of the fluidized bed surface can be maintained at 900 ° C. or higher, and N 2 O can be significantly reduced.
【００２６】[0026]
【発明の効果】以上述べたように、本発明によれば、加
圧流動床ボイラの流動床内に粗粒の石炭等の燃料、粗粒
の石灰石及び超微粒石灰石を共存させることで最適な流
動床を形成し、ＳＯ2 と反応する石灰石の反応表面積を
最大限に有効活用することが可能となり、ＳＯ2 の発生
を大幅に低減することができる。As described above, according to the present invention, an optimum fuel such as coarse coal, coarse limestone and ultrafine limestone coexist in the fluidized bed of a pressurized fluidized bed boiler. A fluidized bed can be formed, and the reaction surface area of limestone reacting with SO 2 can be effectively used to the maximum, and generation of SO 2 can be significantly reduced.
【００２７】また、さらに、流動床表面と気泡の破裂箇
所に燃焼用空気又は酸素を噴霧して流動床から排出され
る未燃炭素を燃焼させ、流動床表面に温度を９００〜１
０００℃に維持するという簡単な方法で、地球温室効果
および成層圏オゾン層破壊の原因物質である亜酸化窒素
（Ｎ2 Ｏ）を容易に効果的に低減することができる。Further, combustion air or oxygen is sprayed on the surface of the fluidized bed and the rupture point of bubbles to burn unburned carbon discharged from the fluidized bed, and the temperature of the fluidized bed surface is increased to 900-1.
With a simple method of maintaining the temperature at 000 ° C., nitrous oxide (N 2 O), which is a causative substance of the global greenhouse effect and stratospheric ozone depletion, can be easily and effectively reduced.
【図１】本発明の一実施例に用いられる加圧流動床ボイ
ラの縦断面図である。FIG. 1 is a vertical sectional view of a pressurized fluidized-bed boiler used in one embodiment of the present invention.
１ 流動床 ２ 水冷壁 ３ 分散板 ３ａ 小孔 ４ フリーボード ５ 石炭 ６ 粗粒石灰石 ６ａ 超微粒石灰石 ７ 石炭の供給ノズル ８ 石灰石の供給ノズル ９ 空気 １０ 空気供給ノズル １１ 風箱 １２ 冷却管 １３ 冷却水 １４ 冷却水 １５ 排出管 １６ 排出口 １７ 燃焼排ガス １８ 燃焼用空気ノズル １９ 空気（又は酸素） DESCRIPTION OF SYMBOLS 1 Fluidized bed 2 Water cooling wall 3 Dispersion plate 3a Small hole 4 Free board 5 Coal 6 Coarse limestone 6a Ultrafine limestone 7 Coal supply nozzle 8 Limestone supply nozzle 9 Air 10 Air supply nozzle 11 Wind box 12 Cooling pipe 13 Cooling water 14 cooling water 15 discharge pipe 16 discharge port 17 combustion exhaust gas 18 combustion air nozzle 19 air (or oxygen)
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平４−222304（ＪＰ，Ａ) 特開 昭55−77605（ＪＰ，Ａ) 特開 昭63−83507（ＪＰ，Ａ) 実開 平２−28909（ＪＰ，Ｕ) 国際公開87／7528（ＷＯ，Ａ１) (58)調査した分野(Int.Cl.6，ＤＢ名) F23C 11/02 301 F23C 11/02 304 F23C 11/02 310 ──────────────────────────────────────────────────続 き Continuation of the front page (56) References JP-A-4-222304 (JP, A) JP-A-55-77605 (JP, A) JP-A-63-83507 (JP, A) 28909 (JP, U) WO 87/7528 (WO, A1) (58) Fields investigated (Int. Cl. 6 , DB name) F23C 11/02 301 F23C 11/02 304 F23C 11/02 310
Claims (2)
る粗粒の石炭と粗粒の石灰石中に流動床重量の３％以下
の超微粒の石灰石を供給して炉内脱硫を行わせることを
特徴とする加圧流動床ボイラの炉内脱硫方法。An in-furnace desulfurization is performed by supplying ultra-fine limestone of 3% or less of the weight of a fluidized bed into coarse coal and coarse limestone forming a fluidized bed of a pressurized fluidized bed boiler. A desulfurization method in a furnace of a pressurized fluidized-bed boiler, characterized in that:
内脱硫方法において、加圧流動床ボイラの流動床表面と
気泡の破裂個所に空気又は酸素を噴霧して流動床から排
出される微粉の未燃炭素を燃焼させ、流動床表面温度を
９００℃〜１０００℃に制御して亜酸化窒素を熱分解し
て除去することを特徴とする加圧流動床ボイラの炉内脱
硫脱硝方法。2. The method for desulfurizing a pressurized fluidized-bed boiler in a furnace according to claim 1, wherein air or oxygen is sprayed onto the fluidized-bed surface of the pressurized fluidized-bed boiler and a rupture point of bubbles to be discharged from the fluidized bed. Denitrification in a furnace of a pressurized fluidized-bed boiler, comprising burning unburned carbon of fine powder, controlling the fluidized bed surface temperature to 900 ° C. to 1000 ° C., and thermally decomposing and removing nitrous oxide. .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4313310A JP2994887B2 (en) | 1992-11-24 | 1992-11-24 | Furnace desulfurization and denitration method for pressurized fluidized bed boiler |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4313310A JP2994887B2 (en) | 1992-11-24 | 1992-11-24 | Furnace desulfurization and denitration method for pressurized fluidized bed boiler |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06159614A JPH06159614A (en) | 1994-06-07 |
| JP2994887B2 true JP2994887B2 (en) | 1999-12-27 |
Family
ID=18039685
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4313310A Expired - Fee Related JP2994887B2 (en) | 1992-11-24 | 1992-11-24 | Furnace desulfurization and denitration method for pressurized fluidized bed boiler |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2994887B2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115178195B (en) * | 2022-07-12 | 2023-07-07 | 中国石油大学(华东) | Pressurized bubbling fluidized bed cold die experimental device |
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1992
- 1992-11-24 JP JP4313310A patent/JP2994887B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH06159614A (en) | 1994-06-07 |
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