JPS58163421A - Treatment of exhaust gas of fluidized combustion boiler - Google Patents
Treatment of exhaust gas of fluidized combustion boilerInfo
- Publication number
- JPS58163421A JPS58163421A JP57046553A JP4655382A JPS58163421A JP S58163421 A JPS58163421 A JP S58163421A JP 57046553 A JP57046553 A JP 57046553A JP 4655382 A JP4655382 A JP 4655382A JP S58163421 A JPS58163421 A JP S58163421A
- Authority
- JP
- Japan
- Prior art keywords
- desulfurization
- coal
- combustion
- exhaust gas
- fluidized
- 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.)
- Granted
Links
Landscapes
- Treating Waste Gases (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Chimneys And Flues (AREA)
Abstract
Description
【発明の詳細な説明】
石油の資源枯渇及び高騰に伴って、代替エネルギー源と
して石炭が見直されている。従来、石炭焚−イラでは微
粉炭バーナーが広く使用されているが、微粉炭／々−ナ
ーを用いる燃焼方式は適用できる炭種に制約があるため
、現在では流動（床）燃焼方式が注目を集めている。こ
の燃焼方式は、（イ）石炭の燃焼性や灰の溶融性に起因
する制約が少ないので、広範囲に亘る炭機が使用できる
、（→石炭粒と共に成る檜の脱硫剤を流動化させる仁と
ｋよシ、炉内脱硫を行なうことができる、といつ九利点
があるほか、低温燃焼を行なわせれば、ＮＯｘの発生を
抑制できる点でも好都合である。尚、石炭火力の問題点
の一つは、石油火力に比べて煤塵、８０ｘ、ＮＯｘの排
出量が多いことであるが、近い将来の排ガス規制での許
容濃度は、それぞれ１ｏｗｇ／Ｎ−以下、５０ ｐｐｍ
以下及び６０ ｐｐｍ以下とされている。DETAILED DESCRIPTION OF THE INVENTION Coal is being reconsidered as an alternative energy source as petroleum resources become depleted and prices soar. Conventionally, pulverized coal burners have been widely used in coal-fired furnaces, but combustion methods using pulverized coal/charners have restrictions on the types of coal that can be applied, so fluidized (bed) combustion methods are currently attracting attention. are collecting. This combustion method has (a) fewer restrictions due to the combustibility of coal and the meltability of ash, so a wide range of coal machines can be used; In addition to being able to perform in-furnace desulfurization, it is also advantageous in that low-temperature combustion can suppress the generation of NOx.One of the problems with coal-fired power is that The emissions of soot, dust, 80x, and NOx are higher than that of oil-fired power plants, but the permissible concentrations under future exhaust gas regulations are 1 owg/N- or less and 50 ppm, respectively.
and 60 ppm or less.
ところで上述した炉内脱硫は、ＯａＯ，Ｂａｄ、 Ｍｇ
Ｏなどのアルカリ土類金属酸化物やそれらの炭酸塩等を
脱硫剤に使用してヒれを石炭粒と共ＫｔＩＬ動化させ、
例えば次式に示すような反応によって、石炭の燃焼で生
ずる８０ｘを脱硫剤に固定させるものである。By the way, the above-mentioned in-furnace desulfurization is performed using OaO, Bad, Mg
Using alkaline earth metal oxides such as O and their carbonates as desulfurization agents, the fins are activated with KtIL together with coal grains,
For example, 80x produced in the combustion of coal is fixed to the desulfurization agent by the reaction shown in the following formula.
ＯａＯ＋ Ｂｏｗ ＋ ／２０ｍ−→０ａ８０４ＢａＯ
＋ Ｓｏｗ ＋ ／２０ｍ−→Ｂａ８０４ＭｔＯ＋ Ｂ
ｏｗ ＋ ／２０ｓ→Ｍｇ８０４しかしながら、この反
応は脱硫剤内部への８０゜及びＯ諺の拡散が律速になる
ため、炉内脱硫によって高い脱硫率を得るには、墳論化
学ｉ量の数倍以上もの多量の脱硫剤を流動化させなけれ
ばならない。しかも多量の脱硫剤を流動化させることは
必然的に大量の未使用脱硫剤や廃脱硫剤が石炭アッシユ
と共に流動床から排出される結果を招くので、２次公害
を防止する意味でこれらの処理も問題となる。OaO+ Bow + /20m-→0a804BaO
+ Sow + /20m-→Ba804MtO+ B
ow + /20s→Mg804 However, this reaction is rate-limited by the diffusion of 80° and O proverbs into the desulfurizing agent, so in order to obtain a high desulfurization rate by in-furnace desulfurization, the amount of Mg804 must be several times or more A large amount of desulfurization agent must be fluidized. Moreover, fluidizing a large amount of desulfurization agent inevitably results in a large amount of unused desulfurization agent and waste desulfurization agent being discharged from the fluidized bed along with the coal ash, so these treatments are necessary to prevent secondary pollution. is also a problem.
尤も、流動床から未使用のｔｉ排出される脱硫剤を適尚
な手段で回収し、これを流動床に改めて循環したり、あ
るいけまた廃脱硫剤を再生して循環使用する態様を採用
すれば、上記した不利益をある程度は軽減させることが
できる。Of course, it is necessary to recover the unused desulfurization agent discharged from the fluidized bed by appropriate means and recirculate it to the fluidized bed, or alternatively, adopt a mode in which the waste desulfurization agent is regenerated and reused. For example, the above disadvantages can be alleviated to some extent.
しかし、こうした態様を採用したところで、炉内脱硫に
よって９５１以上の脱硫率を得るためには、石炭の燃焼
によって生ずる８０ｘを固定するＯＫ必要な理論化学当
量の少なくとも５倍もの脱硫剤を流動させなければなら
ない。However, even if such an embodiment is adopted, in order to obtain a desulfurization rate of 951 or higher by in-furnace desulfurization, it is necessary to flow a desulfurizing agent with an amount at least five times the theoretical chemical equivalent required to fix 80x produced by combustion of coal. Must be.
さらに付は加えれば、流動燃焼方式の利点の一つは、９
００℃前後の低温度での燃焼が可能であり、この低温燃
焼を行なえば新開サーマルＮＯｘの発生を抑止できるこ
とであるが、フューエルＮＯｘの発生までは防止できな
い。従って、このＮＯｘの除去を目的として、２段燃焼
法を採用し、フューエルＮＯｘを還元性雰囲気で分解す
る方法が提案されている。とζろが、この方法は還元性
雰囲気を維持するために、全体の空気過剰率を低く抑え
る必要があり、仁のことは炉内の酸素濃度に依存する炉
内脱硫と相反する条件となるの′で、□これを相殺する
九めＫは炉内で流動させる脱硫剤をさらに増量しなけれ
ばならない。In addition, one of the advantages of the fluidized combustion method is 9
Combustion is possible at a low temperature of around 00° C., and if this low temperature combustion is performed, the generation of new thermal NOx can be suppressed, but the generation of fuel NOx cannot be prevented. Therefore, for the purpose of removing this NOx, a method has been proposed in which a two-stage combustion method is adopted and fuel NOx is decomposed in a reducing atmosphere. However, in this method, in order to maintain a reducing atmosphere, it is necessary to keep the overall excess air ratio low, which is a condition that conflicts with in-furnace desulfurization, which depends on the oxygen concentration in the furnace. To offset this, the amount of desulfurizing agent fluidized in the furnace must be further increased.
つｔ、ｂ、石炭だき流動燃焼−イラに於て、炉内脱硫だ
けで高い脱硫率を達成せんとする場合には、大過鯛の脱
硫剤を流動化させねばならない不利を免れないのである
。ちなみに、＃！１図は炉内脱硫剤としてＯａＯを使用
した場合の炉内のＯａＯ／８０ｘモル比と脱硫率との関
係を示すグラフである。Ｎ１図から明らかな通夛、モル
比がはソＩＫ遍するまでは、モル比の増大に伴って脱硫
率は直線的に上昇するものの、その後は次ｊｌＫ上昇率
が低下し、モル比約１付近で−打ちとなる。従って、炉
内脱硫率が６０〜１０＠でよい場合はＯａＯ／８０ｘの
モル比は１．０〜２． ＯＯ範囲に維持すれば充分であ
るけれども、ｅｌＩ慢以上の脱硫率を望む場合は前記の
モル比を５以上に保持する必要がある。この理由はＯａ
Ｏ４−８０ｍ＋ ”／２０＊→０ａ８０４なる反応は８
偽濃度の一次反応であり、尚切条孔質であったＯａＯの
表面が０ａ８０４で破われ、ＳＯｌのＯｍＯ内部への拡
散が阻害されるため、ある程！ｆまで反応は急速に進む
が、ＳＯ２濃度が低下するに従い、反応速度が低下する
ためと考えられる。In coal-fired fluidized combustion combustion, if a high desulfurization rate is to be achieved through in-furnace desulfurization alone, the disadvantage of having to fluidize the desulfurization agent from large sea bream cannot be avoided. . By the way,#! FIG. 1 is a graph showing the relationship between the OaO/80x molar ratio in the furnace and the desulfurization rate when OaO is used as the in-furnace desulfurization agent. It is clear from the N1 diagram that the desulfurization rate increases linearly as the molar ratio increases until the molar ratio reaches IK, but after that the rate of increase in JlK decreases and the molar ratio reaches approximately 1. It will be a negative hit in the vicinity. Therefore, if the in-furnace desulfurization rate is 60-10@, the OaO/80x molar ratio is 1.0-2. Although it is sufficient to maintain the desulfurization rate within the OO range, if a desulfurization rate higher than elI is desired, it is necessary to maintain the above molar ratio at 5 or more. The reason for this is Oa
The reaction O4-80m+ ”/20*→0a804 is 8
This is a first-order reaction with a false concentration, and the surface of OaO, which was keratinized, is broken by 0a804, and the diffusion of SOI into OmO is inhibited, so to a certain extent! This is thought to be because the reaction proceeds rapidly up to f, but as the SO2 concentration decreases, the reaction rate decreases.
本発明は炉内脱硫のみで流動燃焼Ｉイツの排ガスを処理
する場合の不利を解消させた新しい排ガス処理方法を提
案するものであって、その特徴とするとζろは石炭の流
動燃焼−イラ内で石炭粒と共に比較的少量の脱硫剤を流
動化させることＫよシ石炭の燃焼によって生ずる８０ｘ
の一部を脱硫剤で固定し、ゼイラから出る排ガスを再生
可能な脱硫装置に供給して処理し、該脱硫装置の再生時
に回収される濃縮Ｓ０８ガスを流動態１１ｉ、Ｊ？イラ
にリサイクルすることＫある。この方法によれば流動燃
焼Ｉイラでの炉内脱硫の負担を軽減させることができる
ため、−イラ内で石炭粒と共に流動化させる脱硫剤の量
を減少させることができる。加えて再生可能な脱硫装置
の再生時に回収される濃縮８０Ｉガスは、流動態１＠ｄ
イラにリサイクルすることができるので、該脱硫装置に
通常付設される硫酸製造装置や巣体イオク製造装復を省
略することができる。The present invention proposes a new exhaust gas treatment method that eliminates the disadvantages of treating flue gas from fluidized combustion by in-furnace desulfurization alone. Fluidizing a relatively small amount of desulfurization agent along with the coal particles at 80x
A part of the S08 gas is fixed with a desulfurizing agent, and the exhaust gas emitted from Zeira is supplied to a regenerable desulfurization device for treatment, and the concentrated S08 gas recovered during regeneration of the desulfurization device is converted into a fluidized state 11i, J? There is something wrong with recycling. According to this method, the burden of in-furnace desulfurization in the fluidized combustion I-ira can be reduced, and therefore the amount of desulfurization agent to be fluidized together with the coal grains in the I-ira can be reduced. In addition, the concentrated 80I gas recovered during regeneration of the renewable desulfurization equipment has a flow rate of 1@d
Since the desulfurization equipment can be recycled, it is possible to omit the sulfuric acid production equipment and nest ion production equipment that are normally attached to the desulfurization equipment.
本発明に於て、Ｉイラ内で流動化せしめられる脱硫剤の
量は、石炭の燃焼によって生ずる８０ｘ及びｉイラにリ
サイクルされる８０歳を固定するのに必要な理論化学当
量の１．０〜２．０倍を町とし、これによって炉内脱硫
の脱硫率を６０〜７０−に維持することができる。In the present invention, the amount of desulfurization agent fluidized in the I-ira is 1.0 to 1.0 to the theoretical chemical equivalent necessary to fix the 80x produced by combustion of coal and the 80-year-old recycled to the I-ira. By setting the ratio to 2.0 times, the desulfurization rate of in-furnace desulfurization can be maintained at 60 to 70.
本発明の方法は石炭の流動燃焼ｄイラすべてに適用可能
でめるが、ＮＯｘの発生を抑制し、未燃石炭を少なくす
るために、２段燃焼方式が採用可能なゼイラであること
が好ましい、脱硫剤としては、炉内脱硫で従来使用され
て来たものがすべて使用０Ｔ能であって、典型的にはＯ
ａＯ。The method of the present invention can be applied to all types of fluidized coal combustion zeilers, but in order to suppress the generation of NOx and reduce the amount of unburned coal, it is preferable to use zeilers that can adopt a two-stage combustion method. As for the desulfurization agent, all the desulfurization agents conventionally used for in-furnace desulfurization have 0T capacity, and typically O
aO.
ＭｇＯ，ＢａＯなとのアルカリ土類金＊酸化物やそれら
の炭酸塩等が使用される。再生可能な脱硫着し九廃吸着
剤を加熱再生して濃縮８０重ガスを回収する乾式装置と
、ＫＯＬ（、ＮａＯＨなどのアルカリ液を吸収剤とし、
Ｓ偽を吸収した廃吸収剤を再生して８偽を回収する湿式
装置が知られている１本発明ではこの両者がいずれも使
用可能であるけれども、特に前者の活性炭吸着法式脱硫
装置は、辷れに導入されるゼイラ排ガスにアンモニアを
注入すると、脱硫と同時に脱硝も可能になるので、本発
明の脱硫装置として好ましい。Alkaline earth gold* oxides such as MgO and BaO, their carbonates, etc. are used. A dry device that recovers concentrated 80 heavy gas by heating and regenerating the reproducible desulfurization and nine-waste adsorbent, and a dry device that recovers concentrated 80 heavy gas by desulfurizing and regenerating nine waste adsorbents,
There is a known wet type device that regenerates the waste absorbent that has absorbed the S-sulfur and recovers the S-sulfur. Although both of these can be used in the present invention, the former activated carbon adsorption desulfurization equipment is particularly difficult to use. If ammonia is injected into the Zeila exhaust gas introduced into the system, it is possible to perform denitrification at the same time as desulfurization, which is preferable as the desulfurization apparatus of the present invention.
進んで第２図にそって本発明の方法を釈明する。１け石
炭だき流動燃焼２イラであって、ここには石炭粒と脱硫
剤が供給され、石炭粒は流動燃焼せしめられると共に、
その燃焼によって生ずる８０ｘの一部Ｆｉセイラ内で脱
硫剤に固定される。ｄイラ内で流動化せしめられる脱硫
剤の使用量は、石炭の燃焼によって生ずる８０ｘ及びＩ
イブｌｌＩＣリサイクルされる８偽を固定するのに必要
な理論化学当量の１．０〜２．０倍である。The method of the present invention will now be explained with reference to FIG. This is a 1-layer coal-fired fluidized combustion 2-layer, in which coal grains and desulfurization agent are supplied, and the coal grains are fluidized and combusted.
A portion of the 80x produced by its combustion is fixed to the desulphurizer in the sailor. The amount of desulfurization agent fluidized in the
IllC is 1.0 to 2.0 times the theoretical chemical equivalent needed to immobilize the recycled 8 pseudo.
−イラ１ではＮＯｘの発生を抑制し、未燃石炭を少なく
するために２段燃焼方式を採用し、１次空気比を１．０
前後、全空気比を１．２前後とすることが好ましい。-Ira 1 adopts a two-stage combustion method to suppress the generation of NOx and reduce unburned coal, and the primary air ratio is set to 1.0.
It is preferable that the front and rear total air ratios be around 1.2.
Ｉイラ］からの燃焼排ガスはサイクロン２に送られ、排
ガスに同伴される未燃石炭などけとこで捕集されてｌイ
ラ１に戻される。サイクロン２を出た排ガスはエアヒー
タ３で熱交換された後、集塵器４で除塵され、次いで再
生可能な脱硫装Ｏｆ５に供給される。脱硫装置５には既
述の通り、アルカＩＪ ｉを吸収剤とする湿式脱硫装置
も使用できるが、排ガスの脱硝を脱硫と同時に希望する
場合には、活性炭吸着法式脱硫装置を１！！！用し、こ
れに供給される排ガスに所定量のアンモニアｔａ人する
ことＫよって目的を４成させることかできる。脱硫装置
で処理された排ガスは煙突６妙・ら大気中に放出される
。脱Ｗｔ装厘５の再生時に回収されるｌｌ！ｌＩ縮８０
．ガスは、図ポの通り、ｌイラの燃焼用空気ｒ（混合し
てＩイラ１ヘリサイクルされる。The combustion exhaust gas from the exhaust gas is sent to the cyclone 2, where unburned coal accompanying the exhaust gas is collected and returned to the exhaust gas. The exhaust gas exiting the cyclone 2 undergoes heat exchange with an air heater 3, is removed with a dust collector 4, and is then supplied to a regenerable desulfurizer Of5. As mentioned above, a wet desulfurization device using Alka IJ i as an absorbent can be used as the desulfurization device 5, but if you wish to denitrate the exhaust gas at the same time as desulfurization, an activated carbon adsorption desulfurization device can be used. ! ! By adding a predetermined amount of ammonia to the exhaust gas supplied thereto, four purposes can be achieved. The exhaust gas treated by the desulfurization equipment is released into the atmosphere through a chimney. ll collected when regenerating the de-Wt outfit 5! lI contraction 80
．． As shown in the figure, the gas is mixed with combustion air (R) and recycled to IRA 1.
以上の通り、本発明は石炭だ！！流流動燃焼ゼブラ再生
可能な脱硫装置を組合わせ、燃焼排ガスの脱硫を一イラ
と脱硫装置に分担させているので、炉内脱硫に要する脱
硫剤の使用量を従来の４〜４に低減させても全体として
は為い脱硫率を確保することができる。また脱硫装置に
ついて言えば、本発明ではＩイラでの炉内脱硫によっで
ある程１ｉ：８０ｘ量が減少せしめられた排ガスを処理
すれば足りるので、吸着剤乃至吸収剤の補給量を少なく
することができ、さらに該脱流装置の再生時に回収され
る＠＠ＳＯ，ガスも一イラにリサイクルすることができ
るので、硫＃製造装置中単体イオウ製造装置の設置を省
略できる利点もある。As mentioned above, the present invention is coal! ! By combining the fluid-fluid combustion Zebra regenerable desulfurization equipment, the desulfurization of the flue gas is shared between the desulfurization equipment and the desulfurization equipment, reducing the amount of desulfurization agent required for in-furnace desulfurization to 4 to 4 compared to conventional methods. However, overall a high desulfurization rate can be ensured. Regarding the desulfurization equipment, in the present invention, it is sufficient to treat exhaust gas whose amount has been reduced to a certain extent by 1i:80x due to in-furnace desulfurization in the I-ira, so the amount of adsorbent or absorbent replenishment can be reduced. Furthermore, since the @@SO and gas recovered during regeneration of the deflowing device can also be recycled, there is an advantage that the installation of an elemental sulfur production device in the sulfur # production device can be omitted.
実施例
燃焼量１００に４７時の流動燃焼−イラと、活性炭吸着
法式脱硫装置を組合わせて次のような結果を得た。EXAMPLE The following results were obtained by combining a fluidized combustion furnace with a combustion amount of 100 at 47 hours and an activated carbon adsorption desulfurization device.
流動態ｆｉ／イラでは燃焼性イオク分１ｒｓ窒嵩分！、
４優の歴實炭を８５０Ｃで２段燃焼させ（１次空気比！
１．０ 、全空気比ｆｉ １．２ ）、炉内脱硫剤に
は平均粒径０．２園の石灰石を使用し、前記歴實炭の燃
焼によって生ずる８０ｘ及び脱硫装置からリサイクルさ
れる８偽を固定するのに必要な化学量論量の１．４倍に
和尚する石灰石を歴青炭と共に流動化させた。−イラか
もの排ガスをサイクロンに通して固形分を分離し、これ
を全量−イラに戻した。サイクロンから出たガスを１４
０℃に冷却し、さらに除塵後！６０ｐｐｍのアン４！ア
を注入して脱硫装置で処理し、骸脱硫装置の再生時に回
収される鎖線８０．ガスを一イラにリサイクルした。In fluid dynamics fi/ira, the combustible ion content is 1rs nitrogen volume! ,
4-grade Rekiji coal is burned in two stages at 850C (primary air ratio!
1.0, total air ratio fi 1.2), limestone with an average particle size of 0.2 was used as the desulfurization agent in the furnace, and 80x produced by combustion of the above-mentioned coal and 8x recycled from the desulfurization equipment were used. Limestone containing 1.4 times the stoichiometric amount required to fix the coal was fluidized with bituminous coal. - The exhaust gas from the Ira was passed through a cyclone to separate the solid content, and the entire amount was returned to the Ira. The gas released from the cyclone is 14
After cooling to 0℃ and removing dust! 60ppm Anne 4! The chain line 80. The gas was completely recycled.
仁の場合、−イラ出ロガスの８０１浪度は３５０１）Ｉ
）Ｗｂ Ｎｏｗ＠＆は１４０ ｐｐｍとなシ、歴青炭の
燃焼による理論発生ＳｏｔｍＫＫ対する炉内脱硫率は５
７．１ｖＩ、 リサイクル８０．を加味し九場合のそれ
は５ｔＯ−となった、を九脱硫装置の脱硫率は８＆ｌチ
、脱硝率は５１ＬＯ哄であった。ヒれらを総合すると、
全体としての脱硫率は９ｓ−となシ、脱硫装置から煙突
に送られるガスのＮｏｚ濃度は！Ｉ Ｉ ｐｐｍとなっ
た。In the case of jin, -801 rondo of ira de logas is 3501) I
) Wb Now@& is 140 ppm, and the in-furnace desulfurization rate for SotmKK theoretically generated by combustion of bituminous coal is 5.
7.1vI, Recycling 80. The desulfurization rate of the 9th case was 5tO-, and the desulfurization rate of the 9th desulfurization device was 8.1ch, and the denitrification rate was 51LO. Putting all the fins together,
The overall desulfurization rate is 9s-, and the Noz concentration of the gas sent from the desulfurization equipment to the chimney is! I I ppm.
比較例
上記実施例に於ける脱硫装置を取除き、流動燃焼−イラ
の華独運転により次の結果を得た。Comparative Example The desulfurization equipment in the above example was removed, and the following results were obtained by operating the fluidized combustion furnace in China.
ぜイラでの１次空気比をＯ，Ｓとし、歴青炭と共に流動
化せしめる石灰石の量を理論化学当量の５．０倍とした
以外は実施例と同じ条件で歴青炭を流動燃焼させたとζ
ろ、ぜイラ出ロガスの８０に濃度は４１ ｐｐｍ％ＮＯ
ｘ濃度は１００ ｐｐｍとな妙、理論発生ＳＯ１濃度に
対する脱硫率は９５鴫と六つた。The bituminous coal was fluidized and combusted under the same conditions as in the example except that the primary air ratio in the zeira was O, S, and the amount of limestone fluidized together with the bituminous coal was 5.0 times the theoretical chemical equivalent. and ζ
The concentration of 80% of the gas emitted from the gas is 41 ppm%NO.
The x concentration was 100 ppm, and the desulfurization rate was 95% compared to the theoretically generated SO1 concentration.
第１図は炉内脱硫に於ける脱硫剤（Ｏａｔ’）の使用量
と脱硫率との関係を示すグラフであり、第２図は本発明
方法のフローシートである２、１：流動燃焼ゼイラ
２；サイクロン３；ヱアヒータ ４；集塵器
５；脱硫装肯 ６；煙 突Figure 1 is a graph showing the relationship between the amount of desulfurization agent (Oat') used and the desulfurization rate in in-furnace desulfurization, and Figure 2 is a flow sheet of the method of the present invention.
2; Cyclone 3; Heater 4; Dust collector 5; Desulfurization equipment 6; Chimney
Claims (1)
を流動化させることにょ）石炭の燃焼によって生ずる８
０ｘの一部を脱硫剤で固定し、該２イラから出る排ガス
を再生可能な脱減装ｆ１１１ンこ供給して処理し、該脱
硫装置の再生時に回収される濃縮ＳＯ，ガスを該−イラ
にリサイク声・することを特徴とする流動燃焼ゼイラの
排ガス処理方法。 ２、メイラ内で流動せしめられる脱硫剤の量を、石炭の
燃焼によって生ずる８０ｘ及びリサイクルされる８偽を
固定するのに必要な理論化学当量の１．０〜２．０倍と
して流動態ｍメイラでの炉内脱硫率を６０−以上とする
特許請求の範囲第１項記載の方法。 ３、石炭だき流動燃焼メイラ内で石炭粒と共に脱硫剤を
流動化させる仁とにょう石炭の燃焼によって生ずる８０
ｘの一部を脱硫剤で固定し、該−イラかも排出される排
ガス中にアンモニアを付加混入して炭素質吸着−剤吸着
法式脱硫装ｆＫ供給して脱硫および脱硝処理し、該脱硫
装置の再生時Ｋ［Ｉ鶴される濃縮８０．ガスを該ゼイラ
にリサイクルすることを特徴とする石炭だ自流動燃焼Ｉ
イラの排ガス処理方法。[Claims] 1. Fluidized desulfurization agent together with coal grains in a coal-fired fluidized combustion mailer) produced by combustion of coal.
A part of the 0x is fixed with a desulfurization agent, and the exhaust gas emitted from the two furnaces is supplied to a recyclable de-reducing unit for treatment, and the concentrated SO and gas recovered during regeneration of the desulfurization equipment are transferred to the furnace. A method for treating exhaust gas from a fluidized combustion zeira, which is characterized by recycling. 2. The amount of desulfurization agent fluidized in the mailer is set to 1.0 to 2.0 times the theoretical chemical equivalent required to fix 80x produced by coal combustion and 8x recycled. The method according to claim 1, wherein the in-furnace desulfurization rate is 60 or more. 3. 80 produced by the combustion of kerosene coal that fluidizes the desulfurization agent along with coal grains in a coal-fired fluidized combustion mailer.
A part of Concentration 80. Coal self-flowing combustion I characterized by recycling gas into the zeira
Ira's exhaust gas treatment method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57046553A JPS58163421A (en) | 1982-03-24 | 1982-03-24 | Treatment of exhaust gas of fluidized combustion boiler |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57046553A JPS58163421A (en) | 1982-03-24 | 1982-03-24 | Treatment of exhaust gas of fluidized combustion boiler |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58163421A true JPS58163421A (en) | 1983-09-28 |
| JPH026964B2 JPH026964B2 (en) | 1990-02-14 |
Family
ID=12750506
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57046553A Granted JPS58163421A (en) | 1982-03-24 | 1982-03-24 | Treatment of exhaust gas of fluidized combustion boiler |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58163421A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6280411A (en) * | 1985-10-04 | 1987-04-13 | Electric Power Dev Co Ltd | Operation process for fluidized bed type combustion device with low volume of discharging of sox, and nox and high efficiency of combustion |
| JPS6275312U (en) * | 1985-10-29 | 1987-05-14 | ||
| KR100880576B1 (en) * | 2002-08-29 | 2009-01-30 | 재단법인 포항산업과학연구원 | Recycling system for reducing the nox contained in the combustion gas |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008072787A2 (en) | 2006-12-14 | 2008-06-19 | Cta Technology (Proprietary) Limited | Manufacturing method for a multi-channel copper tube, and manufacturing apparatus for the tube |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5584403U (en) * | 1978-12-08 | 1980-06-11 | ||
| JPS5833368U (en) * | 1981-08-31 | 1983-03-04 | 日産デイ−ゼル工業株式会社 | Handle shaft position adjustment device |
-
1982
- 1982-03-24 JP JP57046553A patent/JPS58163421A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5584403U (en) * | 1978-12-08 | 1980-06-11 | ||
| JPS5833368U (en) * | 1981-08-31 | 1983-03-04 | 日産デイ−ゼル工業株式会社 | Handle shaft position adjustment device |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6280411A (en) * | 1985-10-04 | 1987-04-13 | Electric Power Dev Co Ltd | Operation process for fluidized bed type combustion device with low volume of discharging of sox, and nox and high efficiency of combustion |
| JPS6275312U (en) * | 1985-10-29 | 1987-05-14 | ||
| KR100880576B1 (en) * | 2002-08-29 | 2009-01-30 | 재단법인 포항산업과학연구원 | Recycling system for reducing the nox contained in the combustion gas |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH026964B2 (en) | 1990-02-14 |
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