JPH026964B2 - - Google Patents
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- Publication number
- JPH026964B2 JPH026964B2 JP57046553A JP4655382A JPH026964B2 JP H026964 B2 JPH026964 B2 JP H026964B2 JP 57046553 A JP57046553 A JP 57046553A JP 4655382 A JP4655382 A JP 4655382A JP H026964 B2 JPH026964 B2 JP H026964B2
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- JP
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- Prior art keywords
- boiler
- desulfurization
- coal
- combustion
- 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.)
- Expired - Lifetime
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- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Chimneys And Flues (AREA)
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】
石油の資源枯渇及び高騰に伴つて、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
焚ボイラでは微粉炭バーナーが広く使用されてい
るが、微粉炭バー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、広範囲に亘る炭種が使用できる。(ロ)石
炭粒と共に或る種の脱硫剤を流動化させることに
より、炉内脱硫を行なうことができる、といつた
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、SOx、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10mg／Ｎm3以下、50ppm以下及び60ppm以下
とされている。DETAILED DESCRIPTION OF THE INVENTION As petroleum resources become depleted and prices soar, coal is being reconsidered as an alternative energy source. Conventionally, pulverized coal burners have been widely used in coal-fired boilers, but combustion methods using pulverized coal burners have restrictions on the types of coal that can be applied, so currently fluidized (bed)
The combustion method is attracting attention. This combustion method is
(a) Since there are fewer restrictions due to the combustibility of coal and the meltability of ash, a wide range of coal types can be used. (b) In addition to the advantage that in-furnace desulfurization can be carried out by fluidizing a certain type of desulfurization agent together with the coal grains, low-temperature combustion also
It is also advantageous in that it can suppress the generation of NOx.
One of the problems with coal-fired power generation is that it emits more soot, SOx, and NOx than oil-fired power generation, but the permissible concentrations under near-future exhaust gas regulations are 10 mg/Nm 3 or less, respectively. It is set to be 50ppm or less and 60ppm or less.
ところで上述した炉内脱硫は、CaO、BaO、
MgO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これを石炭粒と共に
流動化させ、例えば次式に示すような反応によつ
て、石炭の燃焼で生ずるSOx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 on CaO, BaO,
By using alkaline earth metal oxides such as MgO and their carbonates as desulfurization agents and fluidizing them together with coal grains, for example, through the reaction shown in the following equation, SOx generated during coal combustion can be removed. It is fixed to the desulfurizing agent.
CaO＋SO2＋1/2O2→CaSO4
BaO＋SO2＋1/2O2→BaSO4
MgO＋SO2＋1/2O2→MgSO4
しかしながら、この反応は脱硫剤内部へのSO4
及びO2の拡散が律速になるため、炉内脱硫によ
つて高い脱硫率を得るには、理論化学当量の数倍
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
ツ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。 CaO+SO 2 +1/2O 2 →CaSO 4 BaO+SO 2 +1/2O 2 →BaSO 4 MgO+SO 2 +1/2O 2 →MgSO 4However , this reaction causes SO 4 to enter the desulfurization agent.
Since diffusion of O 2 and O 2 becomes rate-limiting, in order to obtain a high desulfurization rate by in-furnace desulfurization, a large amount of desulfurization agent, several times the theoretical chemical equivalent, 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まま排出される脱硫
剤を適当な手段で回収し、これを流動床に改めて
循環したり、あるいは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。しかし、こ
うした態様を採用したところで、炉内脱硫によつ
て95％以上の脱硫率を得るためには、石炭の燃焼
によつて生ずるSOxを固定するのに必要な理論化
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。 Of course, if the desulfurization agent discharged unused from the fluidized bed is recovered by appropriate means and recycled to the fluidized bed again, or if the waste desulfurization agent is regenerated and recycled, The above disadvantages can be alleviated to some extent. However, even if such an embodiment is adopted, in order to obtain a desulfurization rate of 95% or more through in-furnace desulfurization, at least five times the theoretical chemical equivalent required to fix SOx produced by coal combustion must be used. The desulfurization agent must be allowed to flow.
さらに付け加えれば、流動燃焼方式の利点の一
つは、900℃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所謂サーマルNOxの発
生を抑止できることであるが、フユーエルNOx
の発生までは防止できない。従つて、このNOx
の除去を目的として、２段燃焼法を採用し、フユ
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。ところが、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、こ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
を相殺するためには炉内で流動させる脱硫剤をさ
らに増量させなければならない。 Furthermore, one of the advantages of the fluidized combustion method is that it is possible to burn at a low temperature of around 900℃.
By performing this low-temperature combustion, it is possible to suppress the generation of so-called thermal NOx, but fuel NOx
cannot be prevented until it occurs. Therefore, this NOx
For the purpose of removing NOx, a method has been proposed that uses a two-stage combustion method to decompose fuel NOx 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, and this is a condition that conflicts with in-furnace desulfurization, which depends on the oxygen concentration in the furnace. In order to offset this, it is necessary to further increase the amount of desulfurization agent fluidized in the furnace.
つまり、石炭だき流動燃焼ボイラに於て、炉内
脱硫だけで高い脱硫率を達成せんとする場合に
は、大過剰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、第１図は炉内
脱硫剤としてCaOを使用した場合の炉内のCaO／
SOxモル比と脱硫率との関係を示すグラフであ
る。第１図から明らかな通り、モル比がほゞ１に
達するまでは、モル比の増大に伴つて脱硫率は直
線的に上昇するものの、その後は次第に上昇率が
低下し、モル比約７付近で頭打ちとなる。従つ
て、炉内脱硫率が60〜70％でよい場合はCaO／
SOxのモル比は1.0〜2.0の範囲に維持すれば充分
であるけれども、95％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CaO＋SO2＋1/2O2→CaSO4なる反応は
SO2濃度の一次反応であり、当切多孔質であつた
CaOの表面がCaSO4で被われ、SO2のCaO内部へ
の拡散が阻害されるため、ある程度まで反応は急
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 other words, in a coal-fired fluidized combustion boiler, if a high desulfurization rate is to be achieved through in-furnace desulfurization alone, the disadvantage is that a large excess of desulfurization agent must be fluidized. By the way, Figure 1 shows the CaO/in the furnace when CaO is used as the in-furnace desulfurization agent.
It is a graph showing the relationship between SOx molar ratio and desulfurization rate. As is clear from Figure 1, the desulfurization rate increases linearly as the molar ratio increases until the molar ratio reaches approximately 1, but after that the rate of increase gradually decreases until the molar ratio reaches approximately 7. It reaches a plateau. Therefore, if the in-furnace desulfurization rate is 60 to 70%, CaO/
Although it is sufficient to maintain the molar ratio of SOx in the range of 1.0 to 2.0, if a desulfurization rate of 95% or more is desired, the molar ratio must be maintained at 5 or more. The reason for this is that the reaction CaO + SO 2 + 1/2O 2 → CaSO 4 is
It was a first-order reaction of SO 2 concentration, and it was porous.
This is thought to be because the surface of CaO is covered with CaSO 4 and the diffusion of SO 2 into CaO is inhibited, so the reaction proceeds rapidly to a certain extent, but as the SO 2 concentration decreases, the reaction rate decreases. .
本発明は炉内脱硫のみで流動燃焼ボイラの排ガ
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つて、その特徴と
するところは石炭の流動燃焼ボイラ内で石炭粒と
共に比較的少量の脱硫剤を流動化させることによ
り石炭の燃焼によつて生ずるSOxの一部を脱硫剤
で固定し、ボ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SO2ガスを流動燃焼ボイラにリサ
イクルすることにある。この方法によれば流動燃
焼ボ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、ボ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
SO2ガスは、流動燃焼ボ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
酸製造装置や単体イオウ製造装置を省略すること
ができる。 The present invention proposes a new flue gas treatment method that eliminates the disadvantages of treating flue gas from a fluidized combustion boiler using only in-furnace desulfurization. At the same time, by fluidizing a relatively small amount of desulfurization agent, a part of the SOx generated by coal combustion is fixed with the desulfurization agent, and the exhaust gas from the boiler is supplied to a renewable desulfurization equipment for treatment. The purpose is to recycle the concentrated SO 2 gas recovered during equipment regeneration to the fluidized combustion boiler. According to this method, the burden of in-furnace desulfurization in a fluidized combustion boiler can be reduced, and therefore the amount of desulfurization agent to be fluidized together with coal grains in the boiler can be reduced. In addition, the concentrate recovered during regeneration of the renewable desulfurization unit
Since the SO 2 gas can be recycled to the fluidized combustion boiler, it is possible to omit the sulfuric acid production equipment and elemental sulfur production equipment that are normally attached to the desulfurization equipment.
本発明に於て、ボイラ内で流動化せしめられる
脱硫剤の量は、石炭の燃焼によつて生ずるSOx及
びボイラにリサイクルされるSO2を固定するのに
必要な理論化学当量の1.0〜2.0倍を可とし、これ
によつ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 boiler is 1.0 to 2.0 times the theoretical chemical equivalent required to fix SOx generated by coal combustion and SO 2 recycled to the boiler. This allows the desulfurization rate of in-furnace desulfurization to be maintained at 60 to 70%.
本発明の方法は石炭の流動燃焼ボイラすべてに
適用可能であるが、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
能なボ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
使用可能であつて、典型的にはCaO、MgO、
BaOなどのアルカリ土類金属酸化物やそれらの
炭酸塩等が使用される。再生可能な脱硫装置とし
ては、活性炭を吸着剤とし、SO2を吸着した廃吸
着剤を加熱再生して濃縮SO2ガスを回収する乾式
装置と、KOH、NaOHなどのアルカリ液を吸収
剤とし、SO2を吸収した廃吸収剤を再生してSO2
を回収する湿式装置が知られている。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、これに導入
されるボ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。 The method of the present invention is applicable to all fluidized coal combustion boilers, but in order to suppress the generation of NOx and reduce the amount of unburned coal, a boiler that can employ a two-stage combustion method is preferable. As desulfurization agents, all those conventionally used for in-furnace desulfurization can be used, typically CaO, MgO,
Alkaline earth metal oxides such as BaO and their carbonates are used. Renewable desulfurization equipment includes a dry type equipment that uses activated carbon as an adsorbent and recovers concentrated SO 2 gas by heating and regenerating the waste adsorbent that has adsorbed SO 2 , and a dry equipment that uses an alkaline liquid such as KOH or NaOH as an absorbent. The waste absorbent that absorbed SO 2 is regenerated to produce SO 2
Wet-type equipment for collecting Although both of these can be used in the present invention, the former activated carbon adsorption desulfurization equipment in particular has the following effects:
This is preferable as the desulfurization apparatus of the present invention because it enables denitration at the same time as desulfurization.
進んで第２図にそつて本発明の方法を説明す
る。１は石炭だき流動燃焼ボイラであつて、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、その燃焼によつて生ずる
SOxの一部はボイラ内で脱硫剤に固定される。ボ
イラ内で流動化せしめられる脱硫剤の使用量は、
石炭の燃焼によつて生ずるSOx及びボイラ１にリ
サイクルされるSO2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。ボイラ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。 The method of the present invention will now be explained with reference to FIG. 1 is a coal-fired fluidized combustion boiler, in which coal grains and a desulfurizing agent are supplied, and the coal grains are fluidized and combusted, and the
Some of the SOx is fixed in the desulfurization agent in the boiler. The amount of desulfurization agent fluidized in the boiler is:
This is 1.0 to 2.0 times the theoretical chemical equivalent required to fix SOx produced by combustion of coal and SO 2 recycled to the boiler 1. In boiler 1, a two-stage combustion method is adopted in order to suppress the generation of NOx and reduce unburned coal, and it is preferable to set the primary air ratio to around 1.0 and the total air ratio to around 1.2.
ボイラ１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はここで
捕集されてボイラ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置５
に供給される。脱硫装置５には既述の通り、アル
カリ液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使用し、これに供
給される排ガスに所定量のアンモニアを注入する
ことによつて目的を達成させることができる。脱
硫装置で処理された排ガスは煙突６から大気中に
放出される。脱硫装置５の再生時に回収される濃
縮SO2ガスは、図示の通り、ボイラの燃焼用空気
に混合してボイラ１へリサイクルされる。 Combustion exhaust gas from the boiler 1 is sent to a cyclone 2, where unburned coal and the like entrained in the exhaust gas are collected and returned to the boiler 1. After the exhaust gas exiting the cyclone 2 undergoes heat exchange with an air heater 3, it is removed with a dust collector 4, and then passed through a renewable desulfurization device 5.
is supplied to As mentioned above, a wet desulfurization device that uses alkaline liquid 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, use an activated carbon adsorption desulfurization device and supply the This can be achieved by injecting a predetermined amount of ammonia into the exhaust gas. The exhaust gas treated by the desulfurization device is released into the atmosphere from the chimney 6. The concentrated SO 2 gas recovered during regeneration of the desulfurization device 5 is mixed with combustion air of the boiler and recycled to the boiler 1, as shown in the figure.
以上の通り、本発明は石炭だき流動燃焼ボイラ
に再生可能な脱硫装置を組合わせ、燃焼排ガスの
脱硫を炉ボ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1/
５〜2/5に低減させても全体としては高い脱硫率を
確保することができる。また脱硫装置について言
えば、本発明ではボイラでの炉内脱硫によつてあ
る程度SOx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、さらに該脱硫装置の再生時
に回収される濃縮SO2ガスもボイラにリサイクル
することができるので、硫酸製造装置や単体イオ
ウ製造装置の設置を省略できる利点もある。 As described above, the present invention combines a coal-fired fluidized combustion boiler with a renewable desulfurization device, and the desulfurization of flue gas is shared between the furnace boiler and the desulfurization device, thereby reducing the amount of desulfurization agent required for in-furnace desulfurization. Conventional 1/
Even if it is reduced to 5 to 2/5, a high desulfurization rate can be ensured as a whole. Regarding the desulfurization equipment, in the present invention, it is sufficient to treat the exhaust gas whose SOx amount has been reduced to some extent by in-furnace desulfurization in the boiler, so the amount of adsorbent or absorbent replenishment can be reduced. Furthermore, since the concentrated SO 2 gas recovered during regeneration of the desulfurization device can also be recycled to the boiler, there is an advantage that installation of a sulfuric acid production device or an elemental sulfur production device can be omitted.
実施例
燃焼量100Kg／時の流動燃焼ボイラと、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 boiler with a combustion rate of 100 kg/hour and an activated carbon adsorption desulfurization device.
流動燃焼ボイラでは燃焼性イオウ分１％、窒素
分1.4％の歴青炭を850℃で２段燃焼させ（１次空
気比＝1.0、全空気比＝1.2）、炉内脱硫剤には平
均粒径0.2mmの石灰石を使用し、前記歴青炭の燃
焼によつて生ずるSOx及び脱硫装置からリサイク
ルされるSO2を固定するのに必要な化学量論量の
1.4倍に相当する石灰石を歴青炭と共に流動化さ
せた。ボイラからの排ガスをサイクロンに通して
固形分を分離し、これを全量ボイラに戻した。リ
サイクルから出たガスを140℃に冷却し、さらに
除塵後260ppmのアンモニアを注入して脱硫装置
で処理し、該脱硫装置の再生時に回収される濃縮
SO2ガスをボイラにリサイクルした。 In the fluidized combustion boiler, bituminous coal with a combustible sulfur content of 1% and a nitrogen content of 1.4% is burned in two stages at 850℃ (primary air ratio = 1.0, total air ratio = 1.2), and the desulfurization agent in the furnace is an average grain Using limestone with a diameter of 0.2 mm, the stoichiometric amount necessary to fix SOx produced by the combustion of the bituminous coal and SO 2 recycled from the desulfurization equipment is used.
Limestone equivalent to 1.4 times was fluidized together with bituminous coal. The exhaust gas from the boiler was passed through a cyclone to separate the solid content, and the entire amount was returned to the boiler. The gas emitted from recycling is cooled to 140℃, and after dust removal, 260 ppm ammonia is injected and processed in a desulfurization equipment, and the concentrated gas is recovered when the desulfurization equipment is regenerated.
SO 2 gas was recycled to the boiler.
この場合、ボイラ出口ガスのSO2濃度は
350ppm、NOx濃度は140ppmとなり、歴青炭の
燃焼による理論発生SO2濃度に対する炉内脱硫率
は57.3％、リサイクルSO2を加味した場合のそれ
は69.0％となつた。また脱硫装置の脱硫率は88.3
％、脱硝率は58.0％であつた。これらを総合する
と、全体としての脱硫率は95％となり、脱硫装置
から煙突に送られるガスのSOx濃度は59ppmとな
つた。 In this case, the SO 2 concentration of the boiler outlet gas is
350ppm, the NOx concentration was 140ppm, and the in-furnace desulfurization rate was 57.3% with respect to the theoretical SO 2 concentration generated by bituminous coal combustion, and when recycled SO 2 was taken into account, it was 69.0%. In addition, the desulfurization rate of the desulfurization equipment is 88.3
%, and the denitrification rate was 58.0%. Putting these together, the overall desulfurization rate was 95%, and the SOx concentration in the gas sent from the desulfurization equipment to the chimney was 59ppm.
比較例
上記実施例に於ける脱硫装置を取除き、流動燃
焼ボイラの単独運転により次の結果を得た。Comparative Example The desulfurization device in the above example was removed and the fluidized combustion boiler was operated independently to obtain the following results.
ボイラでの１次空気比を0.9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
流動燃焼させたところ、ボイラ出口ガスのSOx濃
度は41ppm、NOx濃度は100ppmとなり、理論発
生SO2濃度に対する脱硫率は95％となつた。 The primary air ratio in the boiler is set to 0.9, and the amount of limestone to be fluidized together with bituminous coal is calculated based on the theoretical chemical equivalent.
When bituminous coal was subjected to fluidized combustion under the same conditions as in the example except that it was increased by 5.0 times, the SOx concentration of the boiler outlet gas was 41 ppm, the NOx concentration was 100 ppm, and the desulfurization rate was 95% with respect to the theoretically generated SO 2 concentration. Ta.
第１図は炉内脱硫に於ける脱硫剤（CaO）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。
１；流動燃焼ボイラ、２；サイクロン、３；エ
アヒータ、４；集塵器、５；脱硫装置、６；煙
突。
Figure 1 is a graph showing the relationship between the amount of desulfurization agent (CaO) used and the desulfurization rate in in-furnace desulfurization.
The figure is a flow sheet of the method of the present invention. 1: Fluidized combustion boiler, 2: Cyclone, 3: Air heater, 4: Dust collector, 5: Desulfurization equipment, 6: Chimney.
Claims (1)
硫剤を流動化させることにより石炭の燃焼によつ
て生ずるSOxの一部を脱硫剤で固定し、該ボイラ
から出る排ガスを再生可能な炭素質吸着法式脱硫
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SOzガスを該ボイラにリサイクルす
ることを特徴とする流動燃焼ボイラの排ガス処理
方法。 ２ ボイラ内で流動せしめられる脱硫剤の量を、
石炭の燃焼によつて生ずるSOx及びリサイクルさ
れるSOzを固定するに必要な理論化学量の1.0〜
2.0倍として流動燃焼ボイラで炉内脱硫率を60％
以上とする特許請求の範囲第１項記載の方法。 ３ 石炭だき流動燃焼ボイラ内で石炭粒と共に脱
硫剤を流動化させることにより石炭の燃焼によつ
て生ずるSOxの一部を脱硫剤で固定し、該ボイラ
から排出される排ガス中にアンモニアを付加混入
して炭素質吸着法式脱硫装置に供給して脱硫およ
び脱硝処理し、該脱硫装置の再生時に回収される
濃縮SOzガスを該ボイラにリサイクルすることを
特徴とする石炭だき流動燃焼ボイラの排ガス処理
方法。[Claims] 1. A desulfurizing agent is fluidized together with coal grains in a coal-fired fluidized combustion boiler to fix a part of SOx generated by combustion of coal with the desulfurizing agent, and to regenerate the exhaust gas emitted from the boiler. A method for treating flue gas from a fluidized combustion boiler, characterized in that the SOz gas is supplied to a carbonaceous adsorption desulfurization device for treatment, and the concentrated SOz gas recovered during regeneration of the desulfurization device is recycled to the boiler. 2 The amount of desulfurizing agent fluidized in the boiler,
The theoretical stoichiometric amount required to fix SOx generated by coal combustion and recycled SOz is 1.0~
2.0 times the in-furnace desulfurization rate in a fluidized combustion boiler to 60%
The method according to claim 1, which is defined above. 3. By fluidizing the desulfurizing agent together with the coal grains in a coal-fired fluidized combustion boiler, a part of the SOx produced by the combustion of coal is fixed with the desulfurizing agent, and ammonia is additionally mixed into the exhaust gas discharged from the boiler. A method for treating exhaust gas from a coal-fired fluidized combustion boiler, characterized in that the SOz gas is supplied to a carbonaceous adsorption desulfurization device for desulfurization and denitration treatment, and the concentrated SOz gas recovered during regeneration of the desulfurization device is recycled to the boiler. .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57046553A JPS58163421A (en) | 1982-03-24 | 1982-03-24 | Fluidized combustion boiler exhaust gas treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57046553A JPS58163421A (en) | 1982-03-24 | 1982-03-24 | Fluidized combustion boiler exhaust gas treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58163421A JPS58163421A (en) | 1983-09-28 |
| JPH026964B2 true 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 | Fluidized combustion boiler exhaust gas treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58163421A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8869874B2 (en) | 2006-12-14 | 2014-10-28 | Cta Technology (Proprietary) Limited | Manufacturing method for a multi-channel copper tube, and manufacturing apparatus for the tube |
Families Citing this family (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 | Recirculation System of Combustion Flue Gas for NOx Reduction |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5833368Y2 (en) * | 1978-12-08 | 1983-07-26 | 三菱重工業株式会社 | Fluidized bed combustion equipment |
| 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
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8869874B2 (en) | 2006-12-14 | 2014-10-28 | Cta Technology (Proprietary) Limited | Manufacturing method for a multi-channel copper tube, and manufacturing apparatus for the tube |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58163421A (en) | 1983-09-28 |
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