JP3305363B2 - Wet flue gas desulfurization equipment - Google Patents
Wet flue gas desulfurization equipmentInfo
- Publication number
- JP3305363B2 JP3305363B2 JP19954092A JP19954092A JP3305363B2 JP 3305363 B2 JP3305363 B2 JP 3305363B2 JP 19954092 A JP19954092 A JP 19954092A JP 19954092 A JP19954092 A JP 19954092A JP 3305363 B2 JP3305363 B2 JP 3305363B2
- Authority
- JP
- Japan
- Prior art keywords
- tank
- absorption tower
- limestone
- absorption
- liquid
- 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 - Fee Related
Links
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- Treating Waste Gases (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は湿式排煙脱硫装置に関
し、特に高さを低くした吸収塔構造を持つ湿式排煙脱硫
装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a wet flue gas desulfurization apparatus and, more particularly, to a wet flue gas desulfurization apparatus having a reduced absorption tower structure.
【０００２】[0002]
【従来の技術】世界的問題となっている大気汚染の中で
特に酸性雨については、火力発電所において化石燃料が
ボイラにて燃焼される際に排出される燃焼排ガス中の硫
黄酸化物および窒素酸化物が大きな要因となっている。
この中で硫黄酸化物、主に二酸化硫黄の除去方法とし
て、湿式石灰石−石膏脱硫方法が広く実用化されてい
る。ここで従来の湿式石灰石−石膏法排煙脱硫装置を図
３に示す。2. Description of the Related Art Regarding air pollution, which is a global problem, especially for acid rain, sulfur oxides and nitrogen in flue gas discharged when fossil fuel is burned in a boiler in a thermal power plant Oxides are a major factor.
Among them, wet limestone-gypsum desulfurization method is widely used as a method for removing sulfur oxides, mainly sulfur dioxide. FIG. 3 shows a conventional wet limestone-gypsum method flue gas desulfurization apparatus.
【０００３】二酸化硫黄を含むボイラからの排ガスは吸
収塔２の側面に設けられた吸収塔入口ダクト３より吸収
塔２内へ導かれ、吸収塔２の上方へ流れる。一方、吸収
塔２の吸収液タンク部４には石灰石を含むスラリ吸収液
が一定量保有されており、循環ポンプ５より吸収塔２の
上部に位置するスプレノズル６へ送られ、吸収塔２内に
導かれた排ガスと向流接触するように石灰石を含むスラ
リ吸収液がスプレノズル６から噴霧される。排ガス中に
含まれていた二酸化硫黄は前記スラリ吸収液に吸収さ
れ、スラリ吸収液中に含まれていた石灰石と反応して亜
硫酸カルシウムとなる。二酸化硫黄を吸収したスラリ吸
収液は吸収塔２の下部のタンク部４に落下するが、タン
ク部４内の吸収液スラリ中に供給されている空気７によ
り、スラリ吸収液中の亜硫酸カルシウムは直ちに酸化さ
れて硫酸カルシウム、すなわち、工業的に利用価値の高
い石膏となる。[0003] Exhaust gas from a boiler containing sulfur dioxide is guided into the absorption tower 2 from an absorption tower inlet duct 3 provided on the side of the absorption tower 2 and flows upward of the absorption tower 2. On the other hand, a certain amount of slurry absorption liquid containing limestone is held in the absorption liquid tank section 4 of the absorption tower 2, sent to the spray nozzle 6 located above the absorption tower 2 by the circulation pump 5, and A slurry absorbing liquid containing limestone is sprayed from the spray nozzle 6 so as to be brought into countercurrent contact with the introduced exhaust gas. The sulfur dioxide contained in the exhaust gas is absorbed by the slurry absorbing solution, and reacts with the limestone contained in the slurry absorbing solution to form calcium sulfite. The slurry absorbing liquid that has absorbed the sulfur dioxide falls into the tank 4 at the lower part of the absorption tower 2, but the calcium sulfite in the slurry absorbing liquid is immediately converted by the air 7 supplied to the slurry in the absorbing liquid in the tank 4. It is oxidized to calcium sulfate, that is, gypsum of high industrial value.
【０００４】なお、タンク部４に供給される空気７はタ
ンク部４の側壁に設けられた酸化用撹拌機８の高速回転
しいるプロペラの剪断力により微細化され、酸化能力を
高めている。また、タンク部４の底部に固形物が沈降す
るのを防止するための撹拌機９がタンク部４の側壁に設
けられている。[0004] The air 7 supplied to the tank 4 is miniaturized by the shearing force of a high-speed propeller of an oxidizing stirrer 8 provided on the side wall of the tank 4 to increase the oxidizing ability. Further, a stirrer 9 is provided on the side wall of the tank 4 to prevent the solids from settling at the bottom of the tank 4.
【０００５】吸収塔２内で生成した石膏を回収するた
め、スラリ吸収液の一部が吸収塔２内より抜き出され、
石膏回収システム１１より脱水されて石膏１２が回収さ
れる。また、二酸化硫黄と反応する石灰石を補うためラ
イン１０より石灰石が供給されている。吸収塔２内で二
酸化硫黄が除去された排ガスは吸収塔２内で二酸化硫黄
が除去された排ガスは吸収塔２の上部に設置されたミス
トエリミネータ１３にて、排ガス流に同伴する微細なス
ラリを除去された後、吸収塔出口ダクト１４を経て系外
へ排出される。[0005] In order to recover the gypsum produced in the absorption tower 2, a part of the slurry absorption liquid is withdrawn from the absorption tower 2,
The gypsum 12 is recovered by being dehydrated by the gypsum recovery system 11. Limestone is supplied from the line 10 to supplement limestone that reacts with sulfur dioxide. The exhaust gas from which the sulfur dioxide has been removed in the absorption tower 2 is subjected to fine slurry accompanying the exhaust gas flow by the mist eliminator 13 installed in the upper part of the absorption tower 2. After being removed, it is discharged out of the system through the absorption tower outlet duct 14.
【０００６】[0006]
【発明が解決しようとする課題】上記図３に示す従来の
吸収塔２においては、吸収塔タンク部４のスラリ吸収液
が吸収塔入口ダクト３に入るのを防ぐために、通常吸収
塔入口ダクト３と吸収塔タンク部４のスラリ液面の間を
２〜３ｍあけておく必要があり、この無駄なスペースの
ため、吸収塔２の高さが増し、設備費が高くなる問題が
あった。In the conventional absorption tower 2 shown in FIG. 3, in order to prevent the slurry absorbing liquid in the absorption tower tank section 4 from entering the absorption tower entrance duct 3, the conventional absorption tower entrance duct 3 is used. It is necessary to keep a gap of 2 to 3 m between the slurry level of the absorption tower tank section 4 and this, and there is a problem that the height of the absorption tower 2 increases and the equipment cost increases due to this wasted space.
【０００７】また、酸化用撹拌機８で微細化された酸化
用空気７が循環ポンプ５に吸い込まれるとキャビテーシ
ョンの原因となるため、酸化用撹拌機８は循環ポンプ５
の吸込口より上方に設備する必要がある。さらに、タン
ク部４内での亜硫酸カルシウムの酸化効率を高めるため
には、酸化用撹拌機８から液面まで一定の距離を保つ必
要がある。これらのことから、吸収塔２のタンク部４の
液レベルを一定の高さに保つ必要があり、タンク部４は
吸収塔２全体の高さの約３０％の高さを占めていた。When the oxidizing air 7 finely divided by the oxidizing agitator 8 is sucked into the circulating pump 5, it causes cavitation.
It is necessary to install the equipment above the suction port. Further, in order to increase the efficiency of oxidizing calcium sulfite in the tank section 4, it is necessary to keep a certain distance from the oxidizing agitator 8 to the liquid surface. For these reasons, it is necessary to keep the liquid level in the tank 4 of the absorption tower 2 at a constant level, and the tank 4 occupies about 30% of the height of the entire absorption tower 2.
【０００８】一方、吸収塔２のタンク部４にライン１０
より供給された石灰石はタンク部４のスラリにより希釈
され、石灰石濃度の低いスラリが循環スプレされ、脱硫
性能を低下させる問題もあった。そこで、本発明の目的
は、吸収塔高を低減できる吸収塔構造とし、かつ供給し
た石灰石の希釈を最小限にして石灰石濃度の高い循環用
スラリ吸収液とする湿式排煙脱硫装置を提供することに
ある。On the other hand, a line 10 is connected to the tank section 4 of the absorption tower 2.
The supplied limestone is diluted by the slurry in the tank section 4, and the slurry having a low limestone concentration is circulated and sprayed, and there is a problem that the desulfurization performance is reduced. Therefore, an object of the present invention is to provide a wet flue gas desulfurization apparatus having an absorption tower structure capable of reducing the height of the absorption tower, and minimizing dilution of the supplied limestone and using the slurry as a circulating slurry absorbent having a high limestone concentration. It is in.
【０００９】[0009]
【課題を解決するための手段】本発明の上記目的は次の
構成によって達成される。すなわち、吸収塔下部に設け
られた吸収液を保有する吸収塔タンク部から循環供給さ
れる吸収液をスプレノズルから噴霧して排ガス流入ダク
トから流入する排ガスと気液接触させ、排ガス中の硫黄
酸化物を吸収させる吸収塔を備えた湿式排煙脱硫装置に
おいて、吸収塔タンク部を、石灰石供給部を設けた石灰
石供給タンク部と酸化用吸気導入部を設けた酸化用タン
ク部に仕切板により分離し、吸収液が酸化用タンク部か
ら仕切板をオーバーフローして石灰石供給タンク部に流
入可能な構成とし、かつ石灰石供給タンク部からスプレ
ノズルに吸収液を循環供給する吸収液循環配管を設け、
該スプレノズルからスプレされた吸収液を吸収塔タンク
部の酸化用タンク部に落下させる構造とし、排ガス流入
ダクトからの排ガスを石灰石供給タンク部に向けて導入
し、次いで、Ｕターンして、上昇させて吸収液と接触さ
せる排ガス流路を持つ吸収塔を備えた湿式排煙脱硫装置
である。また、本発明の湿式排煙脱硫装置は、石灰石供
給タンク部からスプレノズルに吸収液を循環供給する吸
収液循環配管に吸収液抜出配管を分岐させて設けた構成
とすることができる。The above object of the present invention is achieved by the following constitution. That is, the absorbing liquid circulated and supplied from the absorbing tower tank section holding the absorbing liquid provided at the lower part of the absorbing tower is sprayed from the spray nozzle and brought into gas-liquid contact with the exhaust gas flowing from the exhaust gas inflow duct, and sulfur oxides in the exhaust gas are in the wet flue gas desulfurization apparatus comprising an absorption tower for absorbing, absorbing tower tank, Tan oxidation having a suction inlet section for oxidation and lime <br/> stone supply tank section provided with a limestone feed portion
Separated by a partition plate.
From the limestone supply tank.
And a spray from the limestone supply tank.
Provide an absorption liquid circulation pipe for circulating the absorption liquid to the nozzle,
The absorption liquid sprayed from the spray nozzle is stored in an absorption tower tank.
A structure for dropping the oxidation tank section parts, the exhaust gas from the exhaust gas inlet duct is introduced toward the limestone feed tank, then a U-turn, with the exhaust gas passage to contact with the absorption liquid is raised It is a wet flue gas desulfurization unit equipped with an absorption tower. Further, the wet flue gas desulfurization device of the present invention is a limestone supply device.
Circulates absorption liquid from the supply tank to the spray nozzle
Configuration in which the absorption liquid extraction pipe is branched from the liquid collection circulation pipe
It can be .
【００１０】ここで、前記湿式排煙脱硫装置において、
吸収液が酸化用タンク部から仕切板をオーバーフローし
て石灰石供給タンク部に流入可能な構成として、石灰石
供給タンク部からスプレノズルに吸収液を循環供給し、
酸化用タンク部には酸化用空気を供給し、かつ吸収塔上
部でスプレされた吸収液が酸化用タンク部に落下し、石
灰石供給タンク部には前記スプレされた吸収液が落下し
ない構造とすることができる。Here, in the wet type flue gas desulfurization apparatus,
As a configuration in which the absorbing liquid can overflow the partition plate from the oxidizing tank section and flow into the limestone supply tank section, circulate and supply the absorbing liquid from the limestone supply tank section to the spray nozzle,
The oxidizing tank is supplied with oxidizing air, and the absorbent sprayed at the top of the absorption tower falls into the oxidizing tank, and the sprayed absorbent does not fall into the limestone supply tank. be able to.
【００１１】[0011]
【作用】本発明により、吸収塔入口排ガスを吸収塔タン
ク部の液面のすぐ上から吸収塔内に導くことになり、従
来技術の欠点であった吸収塔排ガス入口部とタンク部液
面との間の無駄なスペースを無くすことが可能となる。
また、吸収塔タンク部を吸収塔排ガス入口部下部に位置
する石灰石供給タンク部と酸化用タンク部に分割し、石
灰石供給タンク部からスプレノズルに吸収液を循環供給
する吸収液循環配管を設け、酸化用タンク部には酸化用
空気を導入する酸化用空気導入部を設ける。このことに
より、酸化用タンク部では吸収液循環ポンプの吸込口が
無いため、酸化用撹拌機をタンク最下部に設置すること
ができ、酸化用空気を有効に利用でき、かつ吸収塔の液
レベルを下げることが可能となった。According to the present invention, the exhaust gas at the inlet of the absorption tower is introduced into the absorption tower from just above the liquid level in the tank section of the absorption tower. Can be eliminated.
Further, by dividing the absorption tower tank oxidation tank section and the limestone supply tank portion located to the absorber exhaust gas inlet part lower, stone
Circulating supply of absorbent from limestone supply tank to spray nozzle
Provide an absorbent circulation pipe to oxidize
An oxidation air inlet for introducing air is provided. As a result, since there is no suction port for the absorption liquid circulation pump in the oxidation tank, the oxidation stirrer can be installed at the bottom of the tank, the oxidation air can be used effectively, and the liquid level of the absorption tower can be improved. Can be lowered.
【００１２】また、酸化用タンク部からスラリ吸収液が
仕切板をオーバーフローして石灰石供給タンク部に流入
する際に、吸収液内に含まれる気泡が分離するので、循
環ポンプに気泡が吸い込まれる恐れがなくなる。また、
石灰石供給タンク部の上方に吸収塔排ガス入口部が位置
するため、ここに未酸化のスラリが落下することもなく
酸化空気を供給する必要がない。さらに、石灰石供給タ
ンク部に石灰石を供給することで、循環スラリ中の石灰
石濃度を３〜５倍に高めることができ脱硫性能の向上を
達成できる。Further, when the slurry absorbing liquid overflows the partition plate from the oxidizing tank and flows into the limestone supply tank, bubbles contained in the absorbing liquid are separated, so that bubbles may be sucked into the circulation pump. Disappears. Also,
Since the absorption tower exhaust gas inlet is located above the limestone supply tank, there is no need to supply oxidized air without causing unoxidized slurry to fall there. Further, by supplying limestone to the limestone supply tank section, the limestone concentration in the circulating slurry can be increased 3 to 5 times, and the desulfurization performance can be improved.
【００１３】[0013]
【実施例】本発明の一実施例を図面と共に説明する。図
１に本実施例の湿式排煙脱硫装置の吸収塔部分の構造図
を示す。吸収塔２のタンク部４はスプレノズル６から噴
霧されたスラリが落下してくる酸化用タンク部１５と石
灰石供給タンク部１６に仕切板１７で２つに分割されて
おり、石灰石供給タンク部１６にはライン１０により石
灰石が供給され循環ポンプ５にて吸収塔２上部に循環さ
れ、スプレノズル６からスプレされ、排ガスと気液接触
する。また、仕切板１７で仕切られた酸化用タンク部１
５から溢れたスラリが石灰石供給タンク部１６に流れ込
むようになっている。仕切板１７は酸化用タンク部１５
の側壁の一部の構成要素となっている。さらに、吸収塔
入口ダクト３は石灰石供給タンク部１６の上方に位置
し、石灰石供給タンク部１６の吸収液液面に向けて開口
し、かつ酸化用タンク部１５の吸収液液面上方の吸収塔
２の側壁に設けられた開口部に接続している。従って、
入口排ガスは石灰石供給タンク部１６の液面に向けられ
て導入され、吸収塔２内ではＵターンしてスプレノズル
６からスプレされる石灰石を含むスラリと向流接触して
排ガス中の二酸化硫黄が吸収除去される。An embodiment of the present invention will be described with reference to the drawings. FIG. 1 shows a structural diagram of an absorption tower portion of a wet flue gas desulfurization apparatus of the present embodiment. The tank part 4 of the absorption tower 2 is divided into two parts by a partition plate 17 into an oxidation tank part 15 and a limestone supply tank part 16 from which the slurry sprayed from the spray nozzle 6 falls. Limestone is supplied by the line 10 and circulated to the upper part of the absorption tower 2 by the circulation pump 5, sprayed from the spray nozzle 6 and brought into gas-liquid contact with exhaust gas. Further, the oxidation tank portion 1 partitioned by the partition plate 17
The slurry overflowing from 5 flows into the limestone supply tank section 16. The partition plate 17 is a tank 15 for oxidation
Is a part of the side wall. Further, the absorption tower inlet duct 3 is located above the limestone supply tank section 16, opens toward the absorbent liquid level of the limestone supply tank section 16, and is located above the absorbent liquid level of the oxidation tank section 15. 2 is connected to an opening provided on the side wall. Therefore,
The inlet exhaust gas is directed toward the liquid surface of the limestone supply tank section 16 and is made into a U-turn in the absorption tower 2 and comes into countercurrent contact with the slurry containing limestone sprayed from the spray nozzle 6 to absorb sulfur dioxide in the exhaust gas. Removed.
【００１４】二酸化硫黄を吸収除去したスラリは酸化用
タンク部１５に落下、酸化用タンク部１５の側面の下部
に設置された酸化用撹拌機８により微細化された酸化用
空気７で直ちに酸化されて石膏を生成する。酸化用タン
ク部１５にはスプレされたスラリ吸収液が絶え間なく落
下し、直ちに酸化された後に石灰石供給タンク部１６へ
溢れ出し、石灰石供給タンク部１６で石灰石を供給され
た後に再び循環スプレされる。ここで図１では固形物の
沈降防止用の撹拌機９を酸化用撹拌機８と共用するよう
に図示しているが、それぞれを別々に設置しても良い。
なお、吸収塔２内で生成した石膏を回収するため、スラ
リ吸収液の一部を石膏回収システム１１に送り石膏１２
を回収する。The slurry from which sulfur dioxide has been absorbed and removed falls into the oxidizing tank 15 and is immediately oxidized by the oxidizing air 7 which has been miniaturized by the oxidizing stirrer 8 installed at the lower part of the side surface of the oxidizing tank 15. To produce gypsum. The sprayed slurry absorbing liquid constantly falls into the oxidizing tank portion 15, immediately oxidizes, overflows into the limestone supply tank portion 16, is supplied with limestone in the limestone supply tank portion 16, and is circulated and sprayed again. . Here, FIG. 1 shows that the stirrer 9 for preventing sedimentation of solids is shared with the stirrer 8 for oxidation, but they may be separately installed.
In order to collect the gypsum generated in the absorption tower 2, a part of the slurry absorption liquid is sent to the gypsum recovery system 11 and the gypsum 12
Collect.
【００１５】上記構成からなる本実施例では、排ガスは
酸化用タンク部１５のスラリ吸収液の液面のすぐ上に導
入されることになり、吸収塔入口ダクト３と酸化用タン
ク部１５との間に無駄なスペースは無くなる。また、吸
収塔タンク部４を吸収塔入口ダクト３の下部に位置する
石灰石供給タンク部１６と酸化用タンク部１５に分割す
ることにより、酸化用空気が循環ポンプ５に吸い込まれ
てキャビテーションを発生させることがなくなる。ま
た、酸化用タンク部１５には循環ポンプ５の吸込口が無
くなるので、酸化用撹拌機８をタンク最下部に設置する
ことができ、酸化用空気を有効に利用でき、かつ吸収塔
２の液レベルを下げることも可能となる。In this embodiment having the above structure, the exhaust gas is introduced just above the level of the slurry absorbing liquid in the oxidizing tank 15, and the exhaust gas is introduced between the absorption tower inlet duct 3 and the oxidizing tank 15. There is no wasted space in between. Further, by dividing the absorption tower tank section 4 into a limestone supply tank section 16 and an oxidation tank section 15 located below the absorption tower entrance duct 3, the oxidation air is sucked into the circulation pump 5 to generate cavitation. Disappears. Also, since the suction port of the circulation pump 5 is eliminated in the oxidation tank section 15, the oxidation stirrer 8 can be installed at the bottom of the tank, the oxidation air can be effectively used, and the liquid in the absorption tower 2 can be used. It is also possible to lower the level.
【００１６】さらに、酸化用タンク部１５から仕切板１
７を越えて石灰石供給タンク部１６にオーバーフローす
る際に、スラリ吸収液中の気泡が分離するので、循環ポ
ンプ５に気泡が吸い込まれる恐れがなくなる。また、石
灰石供給タンク部１６の上方には吸収塔入口ダクト３が
位置するだけで、吸収塔２内の未酸化の循環スラリ吸収
液が流下しないので、ここに酸化空気を供給する必要が
ない。また、仕切板１７で酸化用タンク部１５から分離
された石灰石供給タンク部１６に石灰石を供給すること
で、循環スラリ吸収液中の石灰石濃度を３〜５倍に高め
ることができ脱硫性能の向上を達成できる。Further, the partition plate 1 is removed from the oxidation tank 15.
When overflowing into the limestone supply tank section 16 beyond 7, the bubbles in the slurry absorbing liquid are separated, so that there is no possibility that the bubbles will be sucked into the circulation pump 5. Further, since the absorption tower inlet duct 3 is merely located above the limestone supply tank section 16 and the unoxidized circulating slurry absorption liquid in the absorption tower 2 does not flow down, there is no need to supply oxidized air to this. Further, by supplying limestone to the limestone supply tank section 16 separated from the oxidation tank section 15 by the partition plate 17, the limestone concentration in the circulating slurry absorption liquid can be increased 3 to 5 times, and the desulfurization performance is improved. Can be achieved.
【００１７】（実験例）本実施例の効果を確認するた
め、２５０Ｎｍ3／ｈのパイロットプラントにより実験
を行った。試験条件は下記で行った。 試験条件： 処理ガス量…２５０Ｎｍ3／ｈ 入口ＳＯ2濃度…７００ｐｐｍ 石灰石過剰率…０．５〜４％ 液−ガス比…１２リットル／Ｎｍ3 図２は石灰石過剰率と脱硫率の関係について従来技術と
本発明のこの実験例を比較したものである。同一の石灰
石過剰率では明らかに本実験例の方が脱硫率が高くなっ
ている。なお、循環スプレしたスラリ吸収液中の分析結
果を下表に示すが、本実験例によるとスラリ吸収液中の
石灰石濃度を増加させることができたため、脱硫性能を
向上させることが可能となることが判明した。(Experimental Example) In order to confirm the effect of the present embodiment, an experiment was conducted using a pilot plant of 250 Nm 3 / h. The test conditions were as follows. Test conditions: Processing gas amount: 250 Nm 3 / h Inlet SO 2 concentration: 700 ppm Limestone excess ratio: 0.5 to 4% Liquid-gas ratio: 12 liters / Nm 3 FIG. 2 shows the relationship between the limestone excess ratio and the desulfurization ratio. This is a comparison between the technology and this experimental example of the present invention. At the same limestone excess rate, the desulfurization rate is clearly higher in this experimental example. The analysis results in the circulated sprayed slurry absorbing solution are shown in the table below. According to this experimental example, the limestone concentration in the slurry absorbing solution could be increased, so that the desulfurization performance could be improved. There was found.
【００１８】[0018]
【表１】 [Table 1]
【００１９】[0019]
【発明の効果】本発明によれば、従来技術の問題点であ
った吸収塔排ガス入口部の無駄なスペース、循環ポンプ
吸込口への酸化用空気の巻込、および供給石灰石のタン
ク部スラリ吸収液による希釈を解決できるので、吸収塔
のコンパクト化および高性能化が図れる。According to the present invention, there are problems in the prior art, such as wasted space at the exhaust gas inlet portion of the absorption tower, entrainment of oxidizing air into the inlet of the circulation pump, and absorption of slurry in the limestone tank. Since the dilution with the liquid can be solved, the absorption tower can be made compact and high-performance.
【図１】 本発明の一実施例の湿式排煙脱硫装置のプロ
セスフローを示す図である。FIG. 1 is a view showing a process flow of a wet flue gas desulfurization apparatus according to one embodiment of the present invention.
【図２】 本発明の一実施例の湿式排煙脱硫装置のパイ
ロットプラントにより実験を行った結果を従来技術の結
果と共に示したグラフの図である。FIG. 2 is a graph showing the results of an experiment conducted by a pilot plant of a wet flue gas desulfurization apparatus according to one embodiment of the present invention, together with the results of a conventional technique.
【図３】 従来の湿式排煙脱硫装置のプロセスフローを
示す図である。FIG. 3 is a view showing a process flow of a conventional wet flue gas desulfurization apparatus.
２…吸収塔、３…吸収塔入口ダクト、４…吸収塔タンク
部、５…循環ポンプ、６…スプレノズル、７…酸化用空
気、８…酸化用撹拌機、９…沈殿防止用撹拌機、１０…
石灰石供給ライン、１１…石膏回収システム、１２…石
膏、１３…ミストエリミネータ、１４…吸収塔出口ダク
ト、１５…酸化用タンク部、１６…石灰石供給タンク
部、１７…仕切板2 ... absorption tower, 3 ... absorption tower inlet duct, 4 ... absorption tower tank, 5 ... circulation pump, 6 ... spray nozzle, 7 ... oxidizing air, 8 ... oxidizing stirrer, 9 ... precipitation preventing stirrer, 10 …
Limestone supply line, 11: gypsum recovery system, 12: gypsum, 13: mist eliminator, 14: absorption tower outlet duct, 15: tank for oxidation, 16: limestone supply tank, 17: partition plate
───────────────────────────────────────────────────── フロントページの続き (58)調査した分野(Int.Cl.7，ＤＢ名) B01D 53/34 ──────────────────────────────────────────────────続 き Continued on the front page (58) Field surveyed (Int.Cl. 7 , DB name) B01D 53/34
Claims (2)
る吸収塔タンク部から循環供給される吸収液をスプレノ
ズルから噴霧して排ガス流入ダクトから流入する排ガス
と気液接触させ、排ガス中の硫黄酸化物を吸収させる吸
収塔を備えた湿式排煙脱硫装置において、 吸収塔タンク部を、石灰石供給部を設けた石灰石供給タ
ンク部と酸化用吸気導入部を設けた酸化用タンク部に仕
切板により分離し、吸収液が酸化用タンク部から仕切板
をオーバーフローして石灰石供給タンク部に流入可能な
構成とし、かつ石灰石供給タンク部からスプレノズルに
吸収液を循環供給する吸収液循環配管を設け、該スプレ
ノズルからスプレされた吸収液を吸収塔タンク部の酸化
用タンク部に落下させる構造とし、排ガス流入ダクトか
らの排ガスを石灰石供給タンク部に向けて導入し、次い
で、Ｕターンして、上昇させて吸収液と接触させる排ガ
ス流路を持つ吸収塔を備えたことを特徴とする湿式排煙
脱硫装置。An absorption liquid circulated and supplied from an absorption tower tank section having an absorption liquid provided at a lower part of the absorption tower is sprayed from a spray nozzle and brought into gas-liquid contact with an exhaust gas flowing from an exhaust gas inflow duct. In a wet flue gas desulfurization apparatus having an absorption tower for absorbing sulfur oxides, the absorption tower tank section is connected to a limestone supply tank provided with a limestone supply section .
Specifications oxidation tank section provided with oxidation air inlet portion and the ink portion
Separated by the cutting plate, the absorbing liquid is separated from the oxidation tank
Can overflow into the limestone supply tank
And the limestone supply tank to the spray nozzle
Provision of an absorption liquid circulation pipe for circulating the absorption liquid
Oxidation of absorption liquid sprayed from nozzle into absorption tank
A structure for dropping the use tank, the exhaust gas from the exhaust gas inlet duct is introduced toward the limestone feed tank, in then <br/>, a U-turn, the exhaust gas stream is contacted with the absorption liquid is raised A wet flue gas desulfurization unit comprising an absorption tower having a passage.
吸収液を循環供給する吸収液循環配管に吸収液抜出配管
を分岐させて設けたことを特徴とする請求項１記載の湿
式排煙脱硫装置。2. From the limestone supply tank to the spray nozzle
Absorbent extraction pipe in absorbent circulation pipe
2. The wet flue gas desulfurization apparatus according to claim 1, wherein the apparatus is branched .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19954092A JP3305363B2 (en) | 1992-07-27 | 1992-07-27 | Wet flue gas desulfurization equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP19954092A JP3305363B2 (en) | 1992-07-27 | 1992-07-27 | Wet flue gas desulfurization equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0639239A JPH0639239A (en) | 1994-02-15 |
| JP3305363B2 true JP3305363B2 (en) | 2002-07-22 |
Family
ID=16409532
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP19954092A Expired - Fee Related JP3305363B2 (en) | 1992-07-27 | 1992-07-27 | Wet flue gas desulfurization equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3305363B2 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5665317A (en) * | 1995-12-29 | 1997-09-09 | General Electric Company | Flue gas scrubbing apparatus |
-
1992
- 1992-07-27 JP JP19954092A patent/JP3305363B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0639239A (en) | 1994-02-15 |
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