JPH0533087B2 - - Google Patents
Info
- Publication number
- JPH0533087B2 JPH0533087B2 JP60179232A JP17923285A JPH0533087B2 JP H0533087 B2 JPH0533087 B2 JP H0533087B2 JP 60179232 A JP60179232 A JP 60179232A JP 17923285 A JP17923285 A JP 17923285A JP H0533087 B2 JPH0533087 B2 JP H0533087B2
- Authority
- JP
- Japan
- Prior art keywords
- stirring member
- stirring
- tubular lance
- gas treatment
- propeller
- 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
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2332—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements the stirrer rotating about a horizontal axis; Stirrers therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2335—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the direction of introduction of the gas relative to the stirrer
- B01F23/23354—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the direction of introduction of the gas relative to the stirrer the gas being driven away from the rotating stirrer
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/20—Mixing gases with liquids
- B01F23/23—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids
- B01F23/233—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements
- B01F23/2336—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the location of the place of introduction of the gas relative to the stirrer
- B01F23/23366—Mixing gases with liquids by introducing gases into liquid media, e.g. for producing aerated liquids using driven stirrers with completely immersed stirring elements characterised by the location of the place of introduction of the gas relative to the stirrer the gas being introduced in front of the stirrer
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/05—Stirrers
- B01F27/11—Stirrers characterised by the configuration of the stirrers
- B01F27/113—Propeller-shaped stirrers for producing an axial flow, e.g. shaped like a ship or aircraft propeller
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Description
【発明の詳細な説明】
発明の目的
（産業上の利用分野）
この発明はガス処理装置、より詳細には煙道ガ
スがアブソーバタンク内に導入され、二酸化硫黄
に水を加えることにより同二酸化硫黄が石灰に結
合され、更に空気を加えることにより酸化されて
石膏が形成され、この石膏がアブソーバタンク内
に設けた撹拌部材にて懸濁されるガス処理装置に
関する。[Detailed Description of the Invention] Purpose of the Invention (Field of Industrial Application) The present invention relates to a gas treatment device, more specifically, a gas treatment device, in which flue gas is introduced into an absorber tank, and sulfur dioxide is converted into sulfur dioxide by adding water to the same. It relates to a gas processing device in which gypsum is formed by being combined with lime and further oxidized by adding air, and this gypsum is suspended in a stirring member provided in an absorber tank.
（従来の技術）
第１図及び第２図に従つて従来例について述べ
る。第１図は煙道ガスを湿式に脱硫するために使
用されるアブソーバタンク１０の下部を示すもの
である。(Prior Art) A conventional example will be described with reference to FIGS. 1 and 2. FIG. 1 shows the lower part of an absorber tank 10 used for wet desulfurization of flue gas.
この脱硫工程において煙ガスはアブソーバタン
ク１０内に導入され、二酸化硫黄は水が加えられ
て石灰、生石灰または水酸化カルシウムに結合す
る。そして、このあと結合した二酸化硫黄には空
気が加えられ、アブソーバタンク１０の下方にお
いて、亜硫酸塩を経て硫酸カルシウムが形成され
る。 In this desulfurization process, smoke gases are introduced into the absorber tank 10 and the sulfur dioxide is combined with lime, quicklime or calcium hydroxide with the addition of water. Then, air is added to the combined sulfur dioxide, and calcium sulfate is formed below the absorber tank 10 via sulfite.
この過程では、アブソーバタンク１０の下部に
水と石膏の粒子からなる懸濁液１２が形成され
る。なお、同懸濁液１２中における固形成分の占
める割合は16重量％である。懸濁液１２は常に懸
濁される必要があり、このためにアブソーバタン
ク１０内に撹拌部材１６が設けられている。この
撹拌部材１６はアブソーバタンク１０の側方に設
けられ、石膏の粒子を懸濁して沈降を防止するも
のである。 In this process, a suspension 12 of water and gypsum particles is formed in the lower part of the absorber tank 10. The proportion of solid components in the suspension 12 was 16% by weight. The suspension 12 must be constantly suspended, and for this purpose a stirring member 16 is provided in the absorber tank 10. This stirring member 16 is provided on the side of the absorber tank 10 and serves to suspend the gypsum particles and prevent them from settling.
また、アブソーバタンク１０の底部には複数個
の管材を互いに連結して形成したガス処理用クロ
ス管（Begasungskreuz）１４が設けられてい
る。これら管材には孔が形成され、クロス管１４
内に供給された空気が管材の孔を通して懸濁液１
２内に進入し、石灰に結合した二酸化硫黄を酸化
して石膏を形成する。なお、この石膏は適切な方
法（図示せず）にてアブソーバタンク１０から取
り出される。 Further, at the bottom of the absorber tank 10, a gas processing cross pipe (Begasungskreuz) 14 formed by connecting a plurality of pipe materials to each other is provided. Holes are formed in these pipe materials, and the cross pipe 14
The air supplied into the suspension 1 passes through the holes in the tube material.
2 and oxidizes sulfur dioxide bound to lime to form gypsum. Note that this gypsum is removed from the absorber tank 10 by an appropriate method (not shown).
第２図は一例として３つの撹拌部材１６を、懸
濁液１２内で互いに120゜離間させて配置した状態
を示すものであり、これら撹拌部材１６はアブソ
ーバタンク１０の内側壁に接近した位置に設けら
れている。第１図に示すよう、各撹拌部材１６の
軸は鋭角的に下方へと傾斜し、さらに第２図に示
すよう、円周方向にも鋭角的に配置されている。 FIG. 2 shows, as an example, three stirring members 16 arranged at a distance of 120° from each other in the suspension 12, and these stirring members 16 are located close to the inner wall of the absorber tank 10. It is provided. As shown in FIG. 1, the axis of each stirring member 16 is inclined downward at an acute angle, and furthermore, as shown in FIG. 2, it is arranged at an acute angle in the circumferential direction.
前記懸濁液１２が撹拌部材１６にて充分に撹拌
される一方、ガス処理用クロス管１４から出る気
泡１８によつて酸化が行われる。なお、アブソー
バタンク１０の直径は10〜20ｍに設定され、また
アブソーバタンク１０は５ｍの高さまで充填可能
である。なお、ガス処理用クロス管１４内には図
示しない送風機にて空気が吹き込まれている。 While the suspension 12 is sufficiently stirred by the stirring member 16, oxidation is carried out by the bubbles 18 coming out from the gas treatment cross pipe 14. The diameter of the absorber tank 10 is set to 10 to 20 m, and the absorber tank 10 can be filled up to a height of 5 m. Note that air is blown into the gas processing cross pipe 14 by a blower (not shown).
上記したガス処理装置では撹拌部材１６が単に
懸濁を行うことのみに作用するので、撹拌部材１
６自体が有する撹拌出力は低い。これを補うた
め、送風機の出力を大きくして、ガス処理用クロ
ス管１４に多量の空気を吹き込む必要がある。従
つて、稼働コストが高いものとなる。 In the above-mentioned gas treatment device, the stirring member 16 acts only to perform suspension, so the stirring member 16
6 itself has a low stirring power. To compensate for this, it is necessary to increase the output of the blower and blow a large amount of air into the gas processing cross pipe 14. Therefore, the operating cost becomes high.
また、ガス処理用クロス管１４は腐食防止の見
地から高品質な鋼にて形成されており、非常に高
価なものとなる。さらには、多量の空気を送り込
むための送風機が必要となり、これらの原因によ
り投資コストが高くなる。 Further, the gas processing cross pipe 14 is made of high quality steel from the viewpoint of corrosion prevention, and is very expensive. Furthermore, a blower is required to blow in a large amount of air, which increases the investment cost.
（発明が解決しようとする問題点）
この発明は上述したように、稼働コスト及び投
資コストが高くなるという問題点を解決しようと
するものである。(Problems to be Solved by the Invention) As described above, the present invention attempts to solve the problem that operating costs and investment costs are high.
発明の目的
（問題点を解決するための手段）
この発明は上述した問題点を解決するために、
第３図に示すように、撹拌部材２２の領域内に空
気を導入して、撹拌するための少なくとも１つの
管状ランス２６を設けたものである。Purpose of the invention (means for solving the problems) In order to solve the problems mentioned above, this invention
As shown in FIG. 3, at least one tubular lance 26 is provided for introducing air into the region of the stirring member 22 for stirring.
また、前記攪拌部材２２はその軸方向に攪拌作
用を行う。前記管状ランス２６の開口２８は前記
攪拌部材２２の圧力側に配置されている。前記管
状ランス２６の開口２８と攪拌部材２２の中心軸
３０との間隔ｅ及び攪拌部材２２のプロペラ２４
の直径d2によつて定められる比率ｅ／d2は0.08か
ら0.18の範囲内にある。前記管状ランス２６の中
心軸３０と攪拌部材２２のプロペラ２４の中心面
との間隔ｈ及び攪拌部材２２のプロペラ２４の直
径d2によつて定められる比率ｈ／d2は0.4から0.5
の範囲内にある
（作用）
この発明は上記した手段を採用したことによ
り、管状ランス２６を通過して吹き込まれた空気
が撹拌部材２２作用領域中で生ずる剪断力によつ
て小さな気泡３８となりまた撹拌部材２２によつ
て懸濁液３６は充分に撹拌され、かつ形成された
石膏粒子は懸濁状態に維持される。 Further, the stirring member 22 performs a stirring action in its axial direction. The opening 28 of the tubular lance 26 is arranged on the pressure side of the stirring member 22. The distance e between the opening 28 of the tubular lance 26 and the central axis 30 of the stirring member 22 and the propeller 24 of the stirring member 22
The ratio e/d 2 determined by the diameter d 2 is in the range from 0.08 to 0.18. The ratio h/d 2 determined by the distance h between the central axis 30 of the tubular lance 26 and the central plane of the propeller 24 of the stirring member 22 and the diameter d 2 of the propeller 24 of the stirring member 22 is from 0.4 to 0.5.
(Function) By employing the above-mentioned means, the present invention can cause the air blown through the tubular lance 26 to become small bubbles 38 due to the shearing force generated in the action area of the stirring member 22. The suspension 36 is sufficiently stirred by the stirring member 22 and the formed gypsum particles are maintained in suspension.
また、上記した所定の位置関係及び各比率に従
つて撹拌部材及びプロペラを配置したので、空気
が懸濁液中に極めて効率的に導入され、導入され
た空気の拡散が促進されて、均一に懸濁液と混合
される。 In addition, since the stirring members and propellers are arranged according to the above-mentioned predetermined positional relationships and respective ratios, air is introduced into the suspension extremely efficiently, the diffusion of the introduced air is promoted, and the air is evenly distributed. mixed with suspension.
（実施例）
以下、この発明の一実施例を第３図に従つて詳
述する。(Example) Hereinafter, an example of the present invention will be described in detail with reference to FIG.
アブソーバタンク２０内に設けた撹拌部材２２
は、第２図に示した従来例と同様な配置状態とな
つている。なお、第３図では撹拌プロペラ２４を
有する撹拌部材２２が１つのみ示されているが、
この実施例では従来と同様に３つ設けたものとす
る。 Stirring member 22 provided inside the absorber tank 20
The arrangement is similar to that of the conventional example shown in FIG. Although only one stirring member 22 having a stirring propeller 24 is shown in FIG.
In this embodiment, three are provided as in the conventional case.
管状ランス（Rehrlanze）２６はアブソーバタ
ンク２０内に上方から導入され、開口２８が撹拌
部材２２の撹拌作用領域に達している。撹拌部材
２２の撹拌プロペラ２４は矢印Ｐ方向に撹拌作用
を行い、管状ランス２６は撹拌プロペラ２４の作
動時における圧力側に配置されるのが望ましい。 A tubular lance 26 is introduced into the absorber tank 20 from above, with an opening 28 reaching the stirring area of the stirring element 22 . It is desirable that the stirring propeller 24 of the stirring member 22 performs a stirring action in the direction of arrow P, and that the tubular lance 26 is disposed on the pressure side when the stirring propeller 24 is in operation.
管状ランス２６は撹拌部材２２の撹拌プロペラ
２４の吸引側にも配置可能であるが、この場合に
は開口２８からアブソーバタンク２０内に送出さ
れる気泡３８によつて撹拌プロペラ２４が包囲さ
れた状態となることがある。従つて、撹拌部材２
２の撹拌プロペラ２４は気泡３８内で作動して、
撹拌プロペラ２４の作動効率が損なわれる虞れが
ある。このため、管状ランス２６を撹拌部材２２
の撹拌プロペラ２４の圧力側に配置することが望
ましい。 The tubular lance 26 can also be placed on the suction side of the stirring propeller 24 of the stirring member 22, but in this case, the stirring propeller 24 is surrounded by air bubbles 38 that are sent into the absorber tank 20 from the opening 28. It may become. Therefore, the stirring member 2
The stirring propeller 24 of No. 2 operates within the bubble 38,
There is a possibility that the operating efficiency of the stirring propeller 24 may be impaired. For this reason, the tubular lance 26 is connected to the stirring member 22.
It is desirable to arrange it on the pressure side of the stirring propeller 24.
撹拌部材２２の撹拌プロペラ２４の中央面から
管状ランス２６の中央軸３２までの間隔はｈにて
示され、また撹拌プロペラ２４の直径はd2にて示
されている。そして、ｈ：d2の比は0.4〜0.5の範
囲、特に0.46が望ましい。 The distance from the central plane of the stirring propeller 24 of the stirring member 22 to the central axis 32 of the tubular lance 26 is designated h, and the diameter of the stirring propeller 24 is designated d 2 . The h: d2 ratio is preferably in the range of 0.4 to 0.5, particularly 0.46.
管状ランス２６の開口２８は、撹拌部材２２の
中心軸３０の若干上方に配置されている。撹拌部
材２２の中心軸３０と管状ランス２６の開口２８
との間隔はｅにて示されている。第３図において
は、開口２８が管状ランス２６の長手方向の中心
軸３２に対して斜状をなすため、ｅは撹拌部材２
２の中心軸３０から管状ランス２６の開口２８の
中心までの間隔となる。なお、ｅ：d2の比は0.08
〜0.18の範囲内の値、特に0.13が望ましい。 The opening 28 of the tubular lance 26 is located slightly above the central axis 30 of the stirring member 22. Central axis 30 of stirring member 22 and opening 28 of tubular lance 26
The distance between the two is indicated by e. In FIG. 3, since the opening 28 is oblique with respect to the longitudinal central axis 32 of the tubular lance 26, e represents the stirring member 2.
2 to the center of the opening 28 of the tubular lance 26. Note that the ratio of e:d 2 is 0.08
Values in the range ~0.18, especially 0.13, are preferred.
前記管状ランス２６を通過して懸濁液３６中に
吹き込まれた空気はプロペラジエツトに発生する
剪断力により、撹拌部材２２の撹拌プロペラ２４
にて分散されて運搬され気泡３８を形成する。こ
のシステムは非凝縮的であり、形成された気泡３
８は小さいまま安定して保持され、大きな気泡３
８は形成されない。従つて、撹拌部材２２が気泡
３８で包囲されることが防止される。 The air passed through the tubular lance 26 and blown into the suspension 36 is moved by the stirring propeller 24 of the stirring member 22 due to the shear force generated in the propeller jet.
The gas is dispersed and transported to form bubbles 38. This system is non-condensable and the bubbles formed 3
8 remains small and stable, and large bubble 3
8 is not formed. Therefore, the stirring member 22 is prevented from being surrounded by air bubbles 38.
上記の理由により、管状ランス２６を通過して
吹き込まれた空気は各々の撹拌部材２２の剪断領
域中で生ずる剪断力によつて小さな気泡３８とな
るばかりでなく、撹拌装置２２によつて懸濁液３
６は充分に撹拌され、かつ形成された石膏粒子は
懸濁状態に維持される。 For the above reasons, the air blown through the tubular lance 26 is not only formed into small bubbles 38 by the shear forces generated in the shear region of each stirring member 22, but also suspended by the stirring device 22. liquid 3
6 is thoroughly agitated and the gypsum particles formed are kept in suspension.
さて、ここで従来技術と本発明との比較を以下
に述べる。 Now, a comparison between the prior art and the present invention will be described below.
この比較は実験に基づくものであり、両者の実
験とも物質移転フアクターKLａが同じ70h-1とい
う条件下で行われた。 This comparison is based on experiments, and both experiments were carried out under the same mass transfer factor K L a of 70 h -1 .
また、両者の装置の各部の寸法は下記のように
統一された。 Additionally, the dimensions of each part of both devices were unified as shown below.
アブソーバタンクの直径 Ｄ＝13.6ｍ
充填高さ Ｈ＝6.5ｍ
プロペラ直径 d2＝１ｍ
さらに、両者にはそれぞれ３個の撹拌部材が使
用された。 Absorber tank diameter D = 13.6 m Filling height H = 6.5 m Propeller diameter d 2 = 1 m Furthermore, three stirring members were used for each of both.
従来のガス処理用クロス管１４を使用したガス
処理装置の実験では、
撹拌部材１６の電力消費量は、
３×8.5Kw＝25.5Kw
ガス処理用クロス管１４の空気吹き込み量は、
8200m3／時間
送風機の出力は、
193Kw
であつた。従つて、この実験では撹拌部材１６と
送風機との総出力は218.5Kwであつた。従来のガ
ス処理装置では撹拌部材１６は単に懸濁を行うこ
とのみに作用するので固有の撹拌出力は低いこと
が立証された。 In an experiment of a gas processing device using a conventional cross pipe 14 for gas processing, the power consumption of the stirring member 16 was 3 x 8.5 Kw = 25.5 Kw The amount of air blown into the cross pipe 14 for gas processing was 8200 m 3 /hour. The output of the blower was 193Kw. Therefore, in this experiment, the total output of the stirring member 16 and the blower was 218.5Kw. It has been demonstrated that in conventional gas treatment devices, the stirring member 16 serves only to effect suspension and therefore has a low inherent stirring power.
また、本発明における管状ランス２６を使用し
たガス処理装置の実験では
撹拌部材２２の電力消費量は３×18.7＝
56.1Kwであつた。本発明において、撹拌部材２
２は懸濁化及びガス処理の両者を行うために使用
される。すなわち、懸濁化を行うことのほか、管
状ランス２６を経て吹き出される空気を撹拌部材
２２にて分散させる。従つて、従来品と比較して
撹拌部材２２の電力消費量は大きなものとなつ
た。 In addition, in an experiment of a gas treatment device using the tubular lance 26 according to the present invention, the power consumption of the stirring member 22 was 3×18.7=
It was 56.1Kw. In the present invention, the stirring member 2
2 is used to perform both suspension and gas treatment. That is, in addition to performing suspension, the air blown out through the tubular lance 26 is dispersed by the stirring member 22. Therefore, the power consumption of the stirring member 22 is greater than that of the conventional product.
しかし、この発明では管状ランス２６から吹き
出される空気の量は単に3100m3／時間となり、送
風機の出力は74Kwと低くなつた。従つて、この
発明のガス処理装置において必要とされる総出力
は130.1Kwであり、従来品における総出力
218.5Kwに対して大幅に低い値となつている。こ
のため、ガス処理装置の稼働コストを低く抑える
ことができる。 However, in this invention, the amount of air blown out from the tubular lance 26 was only 3100 m 3 /hour, and the output of the blower was as low as 74 Kw. Therefore, the total output required for the gas treatment equipment of this invention is 130.1Kw, which is the total output of the conventional product.
This is a significantly lower value compared to 218.5Kw. Therefore, the operating cost of the gas treatment device can be kept low.
また、従来品に使用した高価なガス処理用クロ
ス管１４に代えて、簡単な構成の管状ランス２６
を使用し、さらには消費電力の少ない送風機を使
用したため、投資コストも低く抑えることができ
る。 In addition, instead of the expensive gas processing cross pipe 14 used in conventional products, a tubular lance 26 with a simple configuration is used.
In addition, investment costs can be kept low because a blower with low power consumption is used.
なお、この発明は上記した実施例に拘束された
ものではなく、例えば管状ランス２６の開口２８
に対して多くの孔を透設したカバーを取り付け
て、気泡３８の大きさのばらつきをなくす等、こ
の発明の趣旨から逸脱しない限りにおいて任意の
変更は無論可能である。 Note that the present invention is not limited to the above-described embodiments; for example, the opening 28 of the tubular lance 26
It goes without saying that arbitrary changes can be made without departing from the spirit of the invention, such as attaching a cover with many holes transparent thereto to eliminate variations in the size of the bubbles 38.
発明の効果
以上詳述したように、この発明は撹拌部材の領
域内に空気を導入して撹拌するための少なくとも
１つの管状ランスを設けたことにより、投資コス
ト及び駆動コストを低く抑えることができるとい
う優れた効果を奏する。Effects of the Invention As detailed above, the present invention can keep investment costs and driving costs low by providing at least one tubular lance for introducing air into the region of the stirring member for stirring. It has this excellent effect.
また、上記した所定の位置関係及び各比率に従
つて撹拌部材及びプロペラを配置したので、空気
が懸濁液中に極めて効率的に導入され、導入され
た空気の拡散が促進されて、懸濁液と均一に混合
することができる。 In addition, since the stirring members and propellers are arranged according to the above-mentioned predetermined positional relationships and respective ratios, air is introduced into the suspension very efficiently, the diffusion of the introduced air is promoted, and the suspension is suspended. Can be mixed uniformly with liquid.
第１図及び第２図は従来例を示すものであり、
うち第１図はガス処理用クロス管を有するアブソ
ーバタンクの側面図、第２図は同アブソーバタン
クの平面図、また第３図は本発明に係るガス処理
装置の断面図である。
撹拌部材２２、管状ランス２６。
Figures 1 and 2 show conventional examples,
1 is a side view of an absorber tank having a cross pipe for gas treatment, FIG. 2 is a plan view of the same absorber tank, and FIG. 3 is a sectional view of a gas treatment apparatus according to the present invention. Stirring member 22, tubular lance 26.
Claims (1)
し、二酸化硫黄に水を加えて石灰に結合させ、さ
らに空気を加えることにより酸化させて石膏を形
成し、この石膏を前記アブソーバタンク１０内の
攪拌部材２２にて懸濁し、少なくとも一つの攪拌
部材の領域において懸濁液に空気を導入可能な少
なくとも一つの管状ランス２６を備えた煙道ガス
の湿式脱硫用アブソーバタンクを備えたガス処理
装置において、 前記攪拌部材２２はその軸方向に攪拌作用を行
い、 前記少なくとも一つの管状ランス２６の開口２
８は前記攪拌部材２２の圧力側に配置され、 前記管状ランス２６の開口２８と攪拌部材２２
の中心軸３０との間隔ｅ及び攪拌部材２２のプロ
ペラ２４の直径d2によつて定められる比率ｅ／d2
は0.08から0.18の範囲内にあり、前記管状ランス
２６の中心軸３０と攪拌部材２２のプロペラ２４
の中心面との間隔ｈ及び攪拌部材２２のプロペラ
２４の直径d2によつて定めらる比率ｈ／d2は0.4
から0.5の範囲内にある ことを特徴とするガス処理装置。 ２ 少なくとも一つの管状ランス２６が各攪拌部
材２２と関連づけられていることを特徴とする特
許請求の範囲第１項に記載のガス処理装置。 ３ 前記管状ランス２６の開口２８は攪拌部材２
２の中心軸３０の上方に配置されていることを特
徴とする特許請求の範囲第１項及び第２項のいず
れか一項に記載のガス処理装置。 ４ 前記管状ランス２６は攪拌部材２２の中心軸
３０を通過する面、特に垂直面に配置されている
ことを特徴とする特許請求の範囲第１項乃至第３
項のいずれか一項に記載のガス処理装置。[Claims] 1. Flue gas is introduced into the absorber tank 10 and sulfur dioxide is oxidized by adding water to bind to lime and further adding air to form gypsum, which gypsum is an absorber tank for wet desulfurization of flue gas suspended in a stirring element 22 in the absorber tank 10 and equipped with at least one tubular lance 26 through which air can be introduced into the suspension in the region of at least one stirring element; In the gas treatment apparatus, the stirring member 22 performs a stirring action in its axial direction, and the opening 2 of the at least one tubular lance 26
8 is arranged on the pressure side of the stirring member 22, and the opening 28 of the tubular lance 26 and the stirring member 22
The ratio e/d 2 determined by the distance e from the central axis 30 of the stirring member 22 and the diameter d 2 of the propeller 24 of the stirring member 22
is within the range of 0.08 to 0.18, and the central axis 30 of the tubular lance 26 and the propeller 24 of the stirring member 22
The ratio h/d 2 determined by the distance h from the center plane of the stirring member 22 and the diameter d 2 of the propeller 24 of the stirring member 22 is 0.4.
A gas processing device characterized in that the gas is within a range of 0.5 to 0.5. 2. Gas treatment device according to claim 1, characterized in that at least one tubular lance 26 is associated with each stirring member 22. 3 The opening 28 of the tubular lance 26 is connected to the stirring member 2
2. The gas treatment device according to claim 1, wherein the gas treatment device is disposed above the central axis 30 of the gas treatment device. 4. Claims 1 to 3, characterized in that the tubular lance 26 is disposed in a plane passing through the central axis 30 of the stirring member 22, particularly in a vertical plane.
The gas treatment device according to any one of paragraphs.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3434114A DE3434114C2 (en) | 1984-09-17 | 1984-09-17 | Fumigation device for absorber tanks in wet flue gas desulfurization |
| DE3434114.5 | 1984-09-17 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6174630A JPS6174630A (en) | 1986-04-16 |
| JPH0533087B2 true JPH0533087B2 (en) | 1993-05-18 |
Family
ID=6245614
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60179232A Granted JPS6174630A (en) | 1984-09-17 | 1985-08-14 | Gas treatment apparatus |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JPS6174630A (en) |
| DE (1) | DE3434114C2 (en) |
| GB (1) | GB2164576A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019010075A1 (en) * | 2017-07-03 | 2019-01-10 | Marsulex Environmental Technologies Corporation | Wet flue gas desulfurization process and apparatus |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0615012B2 (en) * | 1985-10-04 | 1994-03-02 | バブコツク日立株式会社 | Wet Flue Gas Desulfurization Method |
| JPH0655011U (en) * | 1992-10-02 | 1994-07-26 | スタンレー電気株式会社 | Burner nozzle |
| TW402520B (en) | 1997-11-05 | 2000-08-21 | Mitsubishi Heavy Ind Ltd | Wet flue gas desulfurizer and oxygen-containing gas blowing device for use therein |
| NZ504254A (en) * | 1999-05-17 | 2001-12-21 | United States Gypsum Co | Method for making smooth surface gypsum fiberboard panels with dilute and calcined slurry deposited on pond, sprayed and pressed |
| US6416695B1 (en) * | 1999-05-17 | 2002-07-09 | United States Gypsum Company | Method for making smooth surfaced gypsum fiberboard panel |
| US7377497B2 (en) | 2005-09-16 | 2008-05-27 | Philadelphia Gear Corporation | Aeration system and method |
| SG141244A1 (en) * | 2006-09-08 | 2008-04-28 | Ultra Flo Pte Ltd | Filter renewal system and a method thereof |
| DE102013202492A1 (en) * | 2013-02-15 | 2014-08-21 | Leonhard Fuchs | Wastewater treatment apparatus and method for wastewater treatment |
| DE102013225615B4 (en) | 2013-12-11 | 2022-01-20 | KSB SE & Co. KGaA | Device and method for flue gas desulfurization |
| CN108940099A (en) * | 2018-07-23 | 2018-12-07 | 王芳 | A kind of comprehensive water meter housing that air-flow is combined with grid manufacture mixing apparatus |
| CN111514705A (en) * | 2020-05-08 | 2020-08-11 | 董保成 | Environment-friendly exhaust treatment device |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3643403A (en) * | 1970-04-29 | 1972-02-22 | Richard E Speece | Downflow bubble contact aeration apparatus and method |
| JPS51130677A (en) * | 1975-05-08 | 1976-11-13 | Nippon Kokan Kk <Nkk> | A vapor-liquid contact apparatus |
| GB1584103A (en) * | 1977-06-01 | 1981-02-04 | Ranks Hovis Mcdougall Ltd | Method and apparatus for promoting fermentation |
| US4290885A (en) * | 1977-12-22 | 1981-09-22 | Dochan Kwak | Aeration device |
| SE412011B (en) * | 1978-03-31 | 1980-02-18 | Sala International Ab | DEVICE FOR MIXTURES AND EMISSIONS OF GASES IN WASTE MATERIALS WHICH ARE REQUIRED BY AN AXIAL PUMP WHEEL BY A VERTICAL RISK |
| CA1135883A (en) * | 1978-08-17 | 1982-11-16 | Aeration Industries, Inc. | Method of treating water |
| DE2844398C2 (en) * | 1978-10-12 | 1985-11-28 | Heinrich Frings Gmbh & Co Kg, 5300 Bonn | Method and device for dispersing a gas in a liquid |
| DE3008718C2 (en) * | 1980-03-07 | 1987-01-22 | Hölter, Heinz, Dipl.-Ing., 4390 Gladbeck | Gas scrubbing device for chemisorption plants |
| JPS60132830U (en) * | 1984-02-17 | 1985-09-05 | バブコツク日立株式会社 | Wet exhaust gas desulfurization equipment |
-
1984
- 1984-09-17 DE DE3434114A patent/DE3434114C2/en not_active Expired - Lifetime
-
1985
- 1985-07-23 GB GB08518560A patent/GB2164576A/en not_active Withdrawn
- 1985-08-14 JP JP60179232A patent/JPS6174630A/en active Granted
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2019010075A1 (en) * | 2017-07-03 | 2019-01-10 | Marsulex Environmental Technologies Corporation | Wet flue gas desulfurization process and apparatus |
| US10603624B2 (en) * | 2017-07-03 | 2020-03-31 | Marsulex Environmental Technologies Corporation | Wet flue gas desulfurization process and apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6174630A (en) | 1986-04-16 |
| GB2164576A (en) | 1986-03-26 |
| DE3434114C2 (en) | 1994-12-01 |
| DE3434114A1 (en) | 1986-03-20 |
| GB8518560D0 (en) | 1985-08-29 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |