JP2002153727A - Double chamber type wet flue gas desulfurization device - Google Patents
Double chamber type wet flue gas desulfurization deviceInfo
- Publication number
- JP2002153727A JP2002153727A JP2000353965A JP2000353965A JP2002153727A JP 2002153727 A JP2002153727 A JP 2002153727A JP 2000353965 A JP2000353965 A JP 2000353965A JP 2000353965 A JP2000353965 A JP 2000353965A JP 2002153727 A JP2002153727 A JP 2002153727A
- Authority
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- Japan
- Prior art keywords
- circulation tank
- slurry
- exhaust gas
- flow
- partition plate
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、ボイラなどの燃焼
装置から排出される排ガス中の二酸化硫黄（ＳＯ ２）を
除去する湿式排煙脱硫装置に係わり、特に、吸収塔内部
への仕切板の設置によって、排ガスが上向きに流れる上
昇流領域と下向きに流れる下降流領域の二つの気液接触
部に分けられた二室型の脱硫装置において、循環タンク
内での石膏堆積防止と、亜硫酸カルシウムの酸化性能を
向上できる機能を備えた二室型湿式排煙脱硫装置に関す
るものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to the combustion of a boiler or the like.
Sulfur dioxide (SO 2)
In connection with the wet flue gas desulfurization equipment to be removed, especially inside the absorption tower
Exhaust gas flows upward by installing a partition plate
Two gas-liquid contacts in the ascending region and the downward flowing region
The circulation tank in the two-chamber desulfurization unit divided into
Prevention of gypsum accumulation in the inside and oxidation performance of calcium sulfite
A two-chamber wet flue gas desulfurization system with improved functions
Things.
【０００２】[0002]
【従来の技術】火力発電所等において、化石燃料の燃焼
に伴って発生する排ガス中の硫黄酸化物、中でも特にＳ
Ｏ２は、大気汚染・酸性雨等の環境問題における主原因
の一つである。排ガス中の硫黄酸化物を取り除く脱硫シ
ステムは石灰石−石膏法による湿式法が主流を占めてお
り、中でも最も実績が多く信頼性の高いスプレ方式が世
界的にも多く採用されている。2. Description of the Related Art In a thermal power plant or the like, sulfur oxides in exhaust gas generated by the combustion of fossil fuels,
O 2 is one of the main causes in environmental problems such as air pollution and acid rain. As a desulfurization system for removing sulfur oxides from exhaust gas, a wet method based on a limestone-gypsum method is predominant, and among them, a spray method having the highest performance and a high reliability is widely used worldwide.
【０００３】スプレ方式を採用し、低コスト化を図った
二室型の湿式排煙脱硫装置の従来技術を図６に示す。湿
式排煙脱硫装置は、主に吸収塔本体１、入口ダクト２、
出口ダクト３、仕切板４、吸収液循環ポンプ５、循環タ
ンク７、攪拌機８、空気吹込み管９、ミストエリミネー
タ１０、吸収液抜出し管１１、排ガス上昇流領域１２、
排ガス下降流領域１３、循環配管１４、スプレヘッダー
１５、スプレノズル１６〜１７等から構成される。FIG. 6 shows a conventional technique of a two-chamber wet flue gas desulfurization apparatus which adopts a spray method and reduces cost. Wet flue gas desulfurization equipment mainly consists of absorption tower main body 1, inlet duct 2,
Outlet duct 3, partition plate 4, absorption liquid circulation pump 5, circulation tank 7, stirrer 8, air injection pipe 9, mist eliminator 10, absorption liquid discharge pipe 11, exhaust gas ascending flow area 12,
It comprises an exhaust gas descending region 13, a circulation pipe 14, a spray header 15, spray nozzles 16 to 17, and the like.
【０００４】スプレノズル１６及び１７は、ガス流れに
対して直交する断面内に複数個設置されており、更にガ
ス流れ方向に複数段設置されている。また、攪拌機８及
び空気吹込み管９は、吸収液スラリ６（以下、単にスラ
リということがある）が滞留する循環タンク７に設置さ
れ、ミストエリミネータ１０は出口ダクト３内に設置さ
れる。A plurality of spray nozzles 16 and 17 are provided in a cross section orthogonal to the gas flow, and a plurality of spray nozzles are provided in the gas flow direction. In addition, the stirrer 8 and the air blowing pipe 9 are installed in a circulation tank 7 in which the absorbing liquid slurry 6 (hereinafter, sometimes simply referred to as slurry) stays, and the mist eliminator 10 is installed in the outlet duct 3.
【０００５】ボイラから排出される排ガスは、脱硫ファ
ンにより入口ダクト２から吸収塔本体１にほぼ水平方向
に導入され、出口ダクト３から排出される。スプレ方式
による吸収塔の多くは、排ガスと吸収液６を向流接触さ
せるために、吸収塔下部から導入した排ガスを塔頂部か
ら排出させるが、図６に示す従来技術は吸収塔本体１内
に仕切板４を設置し、出口ダクト３を入口ダクト２とほ
ぼ同じ高さに設けているため、入口ダクト２から導入さ
れた排ガスは、仕切板４に遮られ、上昇流領域１２を上
昇し、塔頂部で反転した後、下降流領域１３を下降す
る。The exhaust gas discharged from the boiler is introduced into the absorption tower main body 1 from the inlet duct 2 by the desulfurization fan in a substantially horizontal direction, and is discharged from the outlet duct 3. Most of the spray-type absorption towers discharge exhaust gas introduced from the lower part of the absorption tower from the top of the tower in order to bring the exhaust gas and the absorbing liquid 6 into countercurrent contact. However, the prior art shown in FIG. Since the partition plate 4 is installed and the outlet duct 3 is provided at substantially the same height as the inlet duct 2, the exhaust gas introduced from the inlet duct 2 is blocked by the partition plate 4 and rises in the upflow area 12, After reversing at the top of the tower, it descends downflow region 13.
【０００６】この間、上昇流領域１２及び下降流領域１
３では、吸収液循環ポンプ５から送られる炭酸カルシウ
ムを含んだ吸収液６が、それぞれの領域に設けられたス
プレノズル１６及び１７から微粒化されて噴射され、吸
収液６と排ガスの気液接触が行われる。このとき、吸収
液６は排ガス中のＳＯ２を選択的に吸収し、亜硫酸カル
シウムを生成する。亜硫酸カルシウムを生成した吸収液
６のうち、液滴径の小さいものは排ガスに同伴され、出
口ダクト３に設けられたミストエリミネータ１０によっ
て捕集される。それ以外の液滴径の大きなものは、一旦
循環タンク７に溜まり、酸化用の攪拌機８によって攪拌
されながら、空気吹込み管９から供給される気泡１９中
の酸素により硫酸カルシウム（石膏）を生成する。ま
た、循環タンク７内のスラリ６の上層部には泡沫層１８
が形成される。炭酸カルシウム及び石膏が共存する循環
タンク７内の吸収液６の一部は、吸収液循環ポンプ５に
よって再びスプレノズル１６及び１７に送られ、一部は
吸収液抜き出し管１１より図示していない廃液処理・石
膏回収系へと送られる。During this time, the upflow region 12 and the downflow region 1
In 3, the absorption liquid 6 containing calcium carbonate sent from the absorption liquid circulation pump 5 is atomized and sprayed from the spray nozzles 16 and 17 provided in the respective regions, and the gas-liquid contact between the absorption liquid 6 and the exhaust gas is established. Done. At this time, the absorbing liquid 6 selectively absorbs SO 2 in the exhaust gas and generates calcium sulfite. Among the absorbing liquids 6 that have generated calcium sulfite, those having a small droplet diameter are entrained by the exhaust gas and collected by the mist eliminator 10 provided in the outlet duct 3. Other large droplets temporarily accumulate in the circulation tank 7 and generate calcium sulfate (gypsum) by oxygen in bubbles 19 supplied from the air blowing pipe 9 while being stirred by the oxidizing stirrer 8. I do. Further, a foam layer 18 is formed on the upper layer of the slurry 6 in the circulation tank 7.
Is formed. A part of the absorbent 6 in the circulation tank 7 in which calcium carbonate and gypsum coexist is sent again to the spray nozzles 16 and 17 by the absorbent circulation pump 5, and a part of the waste liquid treatment (not shown) is drawn from the absorbent extraction pipe 11.・ Sent to the gypsum collection system.
【０００７】酸化用の攪拌機８の主なる目的は亜硫酸カ
ルシウムを酸化することであるが、循環タンク７内にお
いて石膏の堆積を防ぐ役割も果たす。しかしながら、攪
拌機８の台数は亜硫酸カルシウムの酸化に必要な酸素量
によって決定され、前記台数は必ずしも石膏が循環タン
ク７の底部に堆積しないように吸収液６を攪拌するのに
十分な動力が得られる数ではない。The main purpose of the oxidizing stirrer 8 is to oxidize calcium sulfite, but also serves to prevent the accumulation of gypsum in the circulation tank 7. However, the number of the stirrers 8 is determined by the amount of oxygen required for the oxidation of calcium sulfite, and the number can provide sufficient power to stir the absorbent 6 so that the gypsum does not necessarily accumulate on the bottom of the circulation tank 7. Not a number.
【０００８】また、吸収塔本体１で吸収されるＳＯ２の
うち、そのほとんどは上昇流領域１２で吸収されるた
め、上昇流領域１２から循環タンク７に落下する吸収液
６中の亜硫酸カルシウム濃度は下降流領域１３から落下
する吸収液６中のそれに比べて３〜１０倍程度高い。上
昇流領域１２側の亜硫酸カルシウムを高濃度で含む吸収
液６は循環ポンプ５に吸い込まれるまでの滞留時間の間
に酸化されるが、実際には上昇流領域１２側の吸収液６
のうちでも仕切板４付近に落下した吸収液６は入口ダク
ト２付近に落下した吸収液６と比較して吸収液循環ポン
プ５の吸収口に近く、高亜硫酸カルシウム濃度の吸収液
６が短時間で循環ポンプ５に吸い込まれ、亜硫酸カルシ
ウムを完全に酸化する滞留時間を得ることが難しい。Further, since most of the SO 2 absorbed by the absorption tower main body 1 is absorbed in the upflow region 12, the concentration of calcium sulfite in the absorbent 6 falling from the upflow region 12 to the circulation tank 7 is reduced. Is about 3 to 10 times higher than that in the absorbent 6 falling from the downflow region 13. The absorbing solution 6 containing calcium sulfite at a high concentration in the upflow region 12 is oxidized during the residence time before being sucked into the circulating pump 5.
Among them, the absorbent 6 that has fallen near the partition plate 4 is closer to the absorption port of the absorbent circulating pump 5 than the absorbent 6 that has fallen near the inlet duct 2, and the absorbent 6 having a high calcium sulfite concentration is short-lived. Therefore, it is difficult to obtain a residence time for completely oxidizing calcium sulfite after being sucked into the circulation pump 5.
【０００９】[0009]
【発明が解決しようとする課題】上記従来技術では、循
環タンク７内における石膏の堆積防止に対して十分な攪
拌力が得られず、吸収液６の攪拌が十分に行われない循
環タンク７の中央部において石膏が堆積する。また、堆
積して固化した石膏が循環ポンプ５に吸い込まれると、
スプレノズル１６、１７の詰まりや循環ポンプ５の破損
を引き起こす。In the above-mentioned prior art, a sufficient stirring force for preventing the accumulation of gypsum in the circulation tank 7 is not obtained, and the circulation tank 7 in which the absorption liquid 6 is not sufficiently stirred is not obtained. Gypsum accumulates in the center. Further, when the gypsum that has been deposited and solidified is sucked into the circulation pump 5,
This causes clogging of the spray nozzles 16 and 17 and breakage of the circulation pump 5.
【００１０】また、従来技術では、循環タンク７内の吸
収液６中における亜硫酸カルシウムの酸化に関して十分
に考慮されていない。循環ポンプ５から吸収塔本体１へ
スプレされる吸収液６中に亜硫酸カルシウムが残存する
と、吸収塔での脱硫性能低下及びスプレノズル１６、１
７や塔壁などへのスケーリングの発生を引き起こす問題
がある。In the prior art, the oxidation of calcium sulfite in the absorbing solution 6 in the circulation tank 7 is not sufficiently considered. If calcium sulfite remains in the absorption liquid 6 sprayed from the circulation pump 5 to the absorption tower main body 1, the desulfurization performance in the absorption tower decreases and the spray nozzles 16 and 1
There is a problem that scaling occurs on the wall 7 and the tower wall.
【００１１】本発明の課題は、循環タンク底部における
石膏の堆積を防ぐこと、また、吸収塔内での排ガスの上
昇流領域側における吸収液スラリ６中の高濃度亜硫酸カ
ルシウムを循環タンク内で完全に酸化することにより、
スプレノズルの詰まりや循環ポンプの破損、脱硫性能の
低下及びスケーリングの発生を防止し、信頼性が高く、
安定した運転が可能な湿式排煙脱硫装置を得ることにあ
る。An object of the present invention is to prevent the accumulation of gypsum at the bottom of the circulation tank, and to completely remove the high-concentration calcium sulfite in the absorbent slurry 6 in the upflow region of the exhaust gas in the absorption tower in the circulation tank. By oxidizing to
Prevents clogging of spray nozzles, breakage of circulation pump, reduction of desulfurization performance and occurrence of scaling, high reliability,
An object of the present invention is to provide a wet flue gas desulfurization device capable of stable operation.
【００１２】[0012]
【課題を解決するための手段】本発明の上記課題は、循
環タンクの上側にボイラなどの燃焼装置から排出される
排ガスをほぼ水平方向に導入する入口ダクトと、浄化し
た排ガスをほぼ水平方向に排出する出口ダストとを設
け、前記入口ダクトと出口ダクトの間に排ガス流路を設
け、その排ガス流路を入口ダクト側と出口ダクト側の二
室に分割するための天井部側に開口部を有する仕切板を
設けることで入口ダクトから導入される排ガスが上向き
に流れる上昇流領域と天井側の開口部で反転した後に出
口ダクトに向けて下向きに排ガスが流れる下降流領域を
形成し、それぞれの領域にスプレノズルを設置し、該ス
プレノズルから噴出する吸収液スラリと排ガスを上昇流
領域では向流接触、下降流領域では並流接触させるよう
に配置した、排ガス中の硫黄酸化物を処理する吸収塔
と、前記吸収塔の下方にスプレノズルから噴出する吸収
液スラリを貯留する循環タンクとを備えた二室型湿式排
煙脱硫装置において、前記仕切板の下端部を循環タンク
内の吸収液内に浸漬させ、該仕切板により、循環タンク
内の吸収液スラリの液深の半分の位置よりも下側であっ
て、かつ仕切板の下端部と循環タンクの底部との間に吸
収液スラリ流通部を設けたことを特徴とする二室型湿式
排煙脱硫装置により解決される。SUMMARY OF THE INVENTION The object of the present invention is to provide an inlet duct for introducing exhaust gas discharged from a combustion device such as a boiler in a substantially horizontal direction above a circulation tank; An outlet dust to be discharged is provided, an exhaust gas flow path is provided between the inlet duct and the outlet duct, and an opening is formed on a ceiling side for dividing the exhaust gas flow path into two chambers on the inlet duct side and the outlet duct side. By providing a partition plate having an upward flow region in which exhaust gas introduced from the inlet duct flows upward and a downward flow region in which exhaust gas flows downward toward the outlet duct after being reversed at the opening on the ceiling side, A spray nozzle is installed in the region, and the absorbent slurry ejected from the spray nozzle and the exhaust gas are arranged to be in countercurrent contact in the upward flow region and to be in parallel flow contact in the downward flow region. In a two-chamber wet-type flue gas desulfurization device equipped with an absorption tower for treating sulfur oxides of the type and a circulation tank for storing the absorption slurry discharged from the spray nozzle below the absorption tower, the lower end of the partition plate is removed. Immersed in the absorbent in the circulation tank, and the partition plate is located below the half of the liquid depth of the absorbent slurry in the circulation tank, and the lower end of the partition plate and the bottom of the circulation tank. A two-chamber wet-type flue gas desulfurization apparatus characterized in that an absorption liquid slurry flow section is provided between the two.
【００１３】[0013]
【作用】本発明の二室型湿式排煙脱硫装置により、仕切
板の下端部と循環タンクの底部との間であって、循環タ
ンク内の吸収液スラリの液深の半分の位置よりも下側に
スラリ流通部を設けることにより、石膏粒子がスラリの
流れに同伴して、該スラリ流通部を流れるので石膏が循
環タンク底部に堆積することを防止できる。According to the two-chamber wet flue gas desulfurization apparatus of the present invention, a portion between the lower end of the partition plate and the bottom of the circulation tank, which is lower than a half of the liquid depth of the absorbent slurry in the circulation tank. By providing the slurry flow portion on the side, gypsum particles flow along the slurry flow portion accompanying the flow of the slurry, so that gypsum can be prevented from accumulating on the bottom of the circulation tank.
【００１４】また、前記循環タンク内の吸収液スラリ流
通部における吸収液スラリの平均流速が０．５〜４ｍ／
秒となるように該スラリ流通部の大きさを設定するの
で、スケーリングの発生を防止することができる。The average flow rate of the absorbent slurry in the absorbent slurry flow section in the circulation tank is 0.5 to 4 m / m.
Since the size of the slurry flow section is set to be seconds, the occurrence of scaling can be prevented.
【００１５】また、排ガスが下向きに流れる吸収塔内部
の下降流領域のガス流れ方向の断面積より、仕切板で仕
切られた前記下降流領域下方に位置する循環タンク内の
スラリの貯留部のガス流れ方向の断面積を小さくするこ
とで、吸収塔内部の上昇流領域側の循環タンク内の体積
を大きくして高濃度で亜硫酸カルシウムを含む吸収液ス
ラリ側の降下速度を減少させ、十分な滞留時間を得るこ
とができ、高濃度の亜硫酸カルシウムを循環タンク内で
完全に酸化することが可能となる。Further, the gas in the storage portion of the slurry in the circulation tank located below the descending flow region divided by the partition plate is determined from the sectional area of the descending flow region inside the absorption tower in which the exhaust gas flows downward. By reducing the cross-sectional area in the flow direction, the volume in the circulation tank on the side of the ascending flow area inside the absorption tower is increased, and the descent speed on the side of the absorbent slurry containing calcium sulfite in high concentration is reduced, and sufficient retention Time can be obtained, and high-concentration calcium sulfite can be completely oxidized in the circulation tank.
【００１６】また、吸収塔内の排ガスが上向きに流れる
上昇流領域の下方に位置する循環タンク内のスラリ中に
留まる酸化用空気の量によって気泡が多く発生する場合
に、循環タンク内に浸漬した仕切板部分に酸化用空気流
通孔を設けておけば、該流通孔から吸収塔内の下降流領
域１３の下方に位置する循環タンク内のスラリ中に酸化
用空気を流通させることができ、前記上昇流領域側の下
方の循環タンク内のスラリ中の酸化用空気の量を調整す
ることができる。In the case where many bubbles are generated due to the amount of oxidizing air remaining in the slurry in the circulation tank located below the upward flow region in which the exhaust gas in the absorption tower flows upward, the gas is immersed in the circulation tank. By providing the oxidizing air circulation holes in the partition plate portion, it is possible to circulate the oxidizing air from the circulation holes into the slurry in the circulation tank located below the downflow region 13 in the absorption tower, The amount of oxidizing air in the slurry in the circulation tank below the upflow region can be adjusted.
【００１７】[0017]
【発明の実施の形態】以下、本発明の実施の形態につい
て図面を用いて説明する。図１は本発明による実施の形
態であり、図６で説明した同一機能を有する部材には同
一番号を付している。図１は、循環タンク７内の仕切板
４の下端以下におけるスラリ流通部が循環タンク７の底
部に接し、その高さが液深の１／５となるよう設けるこ
とにより、スラリ流通部を通過する平均スラリ流速を
０．５ｍ／秒にした吸収塔の側面図を示したものであ
る。図２は、タンク７の底部に堆積する石膏量とスラリ
流通部を通過するスラリ６の平均流速の関係を表した図
である。図３は、排ガスが下向きに流れる吸収塔本体の
下降流領域の断面積の１／５倍となるよう、該下降流領
域下部の循環タンク７内のスラリ貯留部の断面積を減少
させた例である。Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 shows an embodiment according to the present invention, in which members having the same functions described in FIG. 6 are denoted by the same reference numerals. FIG. 1 shows that the slurry flow portion below the lower end of the partition plate 4 in the circulation tank 7 is in contact with the bottom of the circulation tank 7 and the height thereof is 1/5 of the liquid depth so that the slurry flow portion passes through the slurry flow portion. FIG. 3 is a side view of the absorption tower in which the average slurry flow rate is set to 0.5 m / sec. FIG. 2 is a diagram showing the relationship between the amount of gypsum deposited on the bottom of the tank 7 and the average flow velocity of the slurry 6 passing through the slurry flow section. FIG. 3 shows an example in which the cross-sectional area of the slurry storage section in the circulation tank 7 below the downflow region is reduced so that the cross-sectional area of the downflow region of the absorption tower main body in which the exhaust gas flows downward is 1/5 times. It is.
【００１８】図１に示す実施の形態は、循環タンク７内
に浸漬した仕切板４の下端部と循環タンク７の底部の間
のスラリ流通部の高さは該タンク７の底部から液深の約
１／５となるように設けて、スラリ６流通部を通過する
吸収液スラリ６の平均流速を０．５ｍ／秒にしている点
で従来技術と異なる。上昇流領域側１２に落下する吸収
液６は循環タンク７を下降し、仕切板４下端部にあるス
ラリ流通部を通り抜け、吸収液循環ポンプ５に吸い込ま
れる。In the embodiment shown in FIG. 1, the height of the slurry flow section between the lower end of the partition plate 4 immersed in the circulation tank 7 and the bottom of the circulation tank 7 is set at a liquid depth from the bottom of the tank 7. It differs from the prior art in that it is provided so as to be about 1/5 and the average flow velocity of the absorbent slurry 6 passing through the slurry 6 flow section is 0.5 m / sec. The absorbent 6 falling to the upflow area side 12 descends through the circulation tank 7, passes through a slurry circulation section at the lower end of the partition plate 4, and is sucked into the absorbent circulation pump 5.
【００１９】このとき、石膏粒子がスラリ６の流れに同
伴して流れるよう、スラリ流通部を通過する平均スラリ
流速を考慮して該スラリ流通部の断面積を設定すること
で石膏の堆積を防止できる。二室型湿式排煙脱硫装置に
おいて、スラリ流通部を通過するスラリ６の平均流速
は、およそ０．１ｍ／秒以下である。At this time, the gypsum particles are prevented from being deposited by setting the cross-sectional area of the slurry flow section in consideration of the average slurry flow velocity passing through the slurry flow section so that the gypsum particles flow along with the flow of the slurry 6. it can. In the two-chamber wet-type flue gas desulfurization device, the average flow velocity of the slurry 6 passing through the slurry flow section is about 0.1 m / sec or less.
【００２０】図２は、スラリ流通部を通過するスラリ６
の平均流速とタンク７底部に堆積した石膏量の関係を表
したものである。堆積した石膏量は、流速が０．１ｍ／
秒以上の時を基準にして相対量で表してある。図２よ
り、スラリ流通部を通過するスラリ６の平均流速が速い
場合、石膏の堆積量が減少することが分かる。望ましく
は、平均スラリ流速を０．５ｍ／秒以上とした場合、石
膏の堆積が防止できる。また、スラリ流通部を通過する
平均スラリ流速を上昇させると、それらを再び吸収塔へ
と循環させるポンプ５の動力の負荷が高くなり、循環量
が減少し、脱硫性能が低下してしまう。これらを考慮し
て、循環タンク７内の仕切板４の流通部における平均ス
ラリ流速を０．５〜４ｍ／秒にすることが望ましい。FIG. 2 shows the slurry 6 passing through the slurry flow section.
And the relationship between the average flow velocity of gypsum and the amount of gypsum deposited on the bottom of the tank 7. The amount of deposited gypsum is 0.1 m /
It is expressed as a relative amount based on time of seconds or more. From FIG. 2, it can be seen that when the average flow velocity of the slurry 6 passing through the slurry flow section is high, the amount of gypsum deposited decreases. Desirably, when the average slurry flow rate is 0.5 m / sec or more, accumulation of gypsum can be prevented. Further, when the average slurry flow rate passing through the slurry flow section is increased, the load of the power of the pump 5 for circulating them to the absorption tower again increases, the circulation amount decreases, and the desulfurization performance decreases. In consideration of these, it is desirable to set the average slurry flow velocity in the circulation section of the partition plate 4 in the circulation tank 7 to 0.5 to 4 m / sec.
【００２１】図３に示す実施の形態は、排ガスが下向き
に流れる吸収塔本体の下降流領域１３の断面積の１／５
倍となるよう、該下降流領域１３下方の循環タンク７内
のガス流れ方向の断面積を減少させた点で従来技術と異
なる。循環タンク７内の上昇流領域１２側のガス流れ方
向の断面積を大きくすれば、スラリ６の降下速度が減少
することにより、上昇流領域１２側の循環タンク７内で
の滞留時間が長くなり、亜硫酸カルシウムをより完全に
酸化することができるが、下降流領域１３側の循環タン
ク７内のガス流れ方向の断面積は小さくなり、該下降流
領域１３でのスラリ６の下降速度が増加し、滞留時間が
短くなる。下降流領域１３側のスラリ６中にも無視でき
ない程度の亜硫酸カルシウムがあり、その酸化に見合う
滞留時間が必要であること、さらに、スラリ６の下降速
度の増加に伴い、循環タンク７内のスラリ６中の酸化空
気が循環ポンプ５に吸収される割合が多くなり、ポンプ
５のキャビテーションやスラリ６の循環量低下が発生す
ることから、上昇流領域１２側の循環タンク７内のガス
流れ方向の断面積の上限が制限される。これらを考慮し
て、排ガスが下向きに流れる吸収塔本体１の下降流領域
１３のガス流れ方向の断面積より、該下降流領域１３の
下部に位置する仕切板４で仕切られる循環タンク７内の
ガス流れ方向の断面積を１〜１／１０倍とすることが望
ましい。FIG. 3 shows an embodiment in which the cross-sectional area of the downflow region 13 of the absorption tower body in which the exhaust gas flows downward is 1/5.
This is different from the prior art in that the cross-sectional area in the gas flow direction in the circulation tank 7 below the downflow region 13 is reduced so as to be doubled. If the cross-sectional area in the gas flow direction on the side of the upflow region 12 in the circulation tank 7 is increased, the descent speed of the slurry 6 decreases, and the residence time in the circulation tank 7 on the side of the upflow region 12 increases. , The calcium sulfite can be more completely oxidized, but the cross-sectional area in the gas flow direction in the circulation tank 7 on the side of the downflow region 13 becomes smaller, and the descent speed of the slurry 6 in the downflow region 13 increases. And the residence time is reduced. There is a considerable amount of calcium sulfite in the slurry 6 on the side of the downflow area 13, and a residence time commensurate with its oxidation is required. Further, as the descent speed of the slurry 6 increases, the slurry in the circulation tank 7 6 is absorbed by the circulation pump 5, the cavitation of the pump 5 and the reduction of the circulation amount of the slurry 6 occur, so that the gas flow direction in the circulation tank 7 on the upflow region 12 side is reduced. The upper limit of the cross-sectional area is limited. In consideration of these, the cross-sectional area in the gas flow direction of the downflow region 13 of the absorption tower main body 1 in which the exhaust gas flows downward, the circulation tank 7 in the circulation tank 7 partitioned by the partition plate 4 located below the downflow region 13. It is desirable that the cross-sectional area in the gas flow direction be 1 to 1/10 times.
【００２２】図４に示す実施の形態は、図１に示す実施
の形態において循環ポンプ５の吸入口の上方の循環タン
ク７の壁面に空気吹込み管２１を伴う攪拌機２０を設置
した点で図１に示す実施の形態とは異なる。仕切板４の
下端部と循環タンク７の底部との間のスラリ流通部を通
過する平均スラリ流速を上昇させるため、該スラリ流通
部の面積を小さくし、攪拌機８のスラリ攪拌動力を下げ
ることにより、攪拌機８から供給される酸化用空気を循
環タンク７の上昇流領域１２側に留める。さらに、下降
流領域１３側のスラリ６中の亜硫酸カルシウムは低濃度
であるため、長い酸化時間は必要なく、循環ポンプ５へ
吸い込まれず、気泡２２の吸い込みによるポンプ５のキ
ャビテーション、スラリ６の循環量の低下及び変動を防
止できる。The embodiment shown in FIG. 4 differs from the embodiment shown in FIG. 1 in that a stirrer 20 with an air blowing pipe 21 is installed on the wall surface of the circulation tank 7 above the suction port of the circulation pump 5. 1 is different from the embodiment shown in FIG. To increase the average slurry flow rate passing through the slurry flow section between the lower end of the partition plate 4 and the bottom of the circulation tank 7, the area of the slurry flow section is reduced, and the slurry stirring power of the stirrer 8 is reduced. Then, the oxidizing air supplied from the stirrer 8 is kept on the upflow area 12 side of the circulation tank 7. Furthermore, since the calcium sulfite in the slurry 6 on the downflow region 13 side has a low concentration, a long oxidation time is not required, the calcium sulfite is not sucked into the circulation pump 5, the cavitation of the pump 5 due to the suction of the bubbles 22, and the circulation amount of the slurry 6 Can be prevented from decreasing and fluctuating.
【００２３】図５に示した実施の形態は、図１に示す実
施の形態において循環タンク７内に浸漬した仕切板４部
分に酸化用空気流通孔２３を設けた点で図１、図４に示
す実施の形態とは異なる。仕切板４で仕切られた上昇流
領域１２側の循環タンク７内のスラリ６中に留まる酸化
用空気の量により、泡沫層１８が多く発生する場合、流
通孔２３から仕切板４で仕切られた下降流領域１３側の
循環タンク７内のスラリ６中に酸化用空気を流通させる
ことにより、循環タンク７の上昇流領域１２側の循環タ
ンク７内のスラリ６中に留まる酸化用空気の量を調整す
ることができる。The embodiment shown in FIG. 5 differs from the embodiment shown in FIG. 1 in that an oxidizing air flow hole 23 is provided in a part of the partition plate 4 immersed in the circulation tank 7 as shown in FIGS. This is different from the embodiment shown. When a large amount of the foam layer 18 is generated due to the amount of the oxidizing air remaining in the slurry 6 in the circulation tank 7 on the side of the upflow area 12 divided by the partition plate 4, the partition plate 4 separates the foam layer 18 from the circulation holes 23. By circulating the oxidizing air through the slurry 6 in the circulating tank 7 on the downflow region 13, the amount of oxidizing air remaining in the slurry 6 in the circulating tank 7 on the upflow region 12 of the circulating tank 7 is reduced. Can be adjusted.
【００２４】なお、上記の実施の形態で示した発明は、
丸型、角型循環タンクによらず効果を得ることができ
る。The invention described in the above embodiment is
The effect can be obtained regardless of the round or square circulation tank.
【００２５】[0025]
【発明の効果】本発明によれば、循環タンク底部におけ
る石膏の堆積を防ぐことができるため、堆積し、固化し
た石膏が循環ポンプに吸い込まれてスプレーの目詰まり
及びポンプ破損を起こすことを防止することができる。According to the present invention, since the accumulation of gypsum at the bottom of the circulation tank can be prevented, it is possible to prevent the accumulated and solidified gypsum from being sucked into the circulation pump to cause clogging of the spray and damage to the pump. can do.
【００２６】また、上昇流領域から落下してくる亜硫酸
カルシウム濃度が高いスラリを循環タンク内で完全に酸
化することができるため、吸収塔での脱硫性能の低下及
びスケーリングの発生防止が可能となり、信頼性が高
く、安定した運転が可能な湿式排煙脱硫装置となる。Further, since the slurry having a high concentration of calcium sulfite falling from the upflow region can be completely oxidized in the circulation tank, it is possible to prevent the desulfurization performance in the absorption tower from lowering and prevent the occurrence of scaling. It is a highly reliable wet flue gas desulfurization unit that can be operated stably.
【図面の簡単な説明】[Brief description of the drawings]
【図１】 本発明による実施例であり、循環タンク内の
仕切板におけるスラリ流通部の平均スラリ流速を０．５
ｍ／秒にするよう流通部を設けた吸収塔の側面図を示し
たものである。FIG. 1 is an embodiment according to the present invention, in which an average slurry flow rate in a slurry flow section of a partition plate in a circulation tank is set to 0.5.
FIG. 3 is a side view of an absorption tower provided with a flow section so as to have a flow rate of m / sec.
【図２】 タンク底部に堆積する石膏量と仕切板の流通
部を通過するスラリの平均流速の関係を表した図であ
る。FIG. 2 is a diagram showing a relationship between an amount of gypsum deposited on a tank bottom and an average flow velocity of a slurry passing through a distribution part of a partition plate.
【図３】 排ガスが下向きに流れる吸収塔本体の下降流
領域の断面積の１／５倍となるよう、該部分下部の循環
タンク内の断面積を減少させた吸収塔の実施例である。FIG. 3 shows an embodiment of an absorption tower in which the cross-sectional area in the circulation tank below the portion is reduced so that the cross-sectional area becomes 1/5 times the cross-sectional area of the downflow region of the absorption tower body in which exhaust gas flows downward.
【図４】 図１の実施例において循環ポンプの吸入口の
上に空気吹込み管を伴う攪拌機を設置した実施例であ
る。FIG. 4 is an embodiment in which a stirrer with an air blowing pipe is installed above the suction port of the circulation pump in the embodiment of FIG.
【図５】 図１に示す実施例において循環タンク内に浸
漬した仕切板部分に酸化空気流通孔を設けた実施例であ
る。FIG. 5 is an embodiment in which oxidizing air circulation holes are provided in a part of the partition plate immersed in the circulation tank in the embodiment shown in FIG.
【図６】 従来技術の二室型湿式排煙脱硫装置における
吸収塔の側面図である。FIG. 6 is a side view of an absorption tower in a conventional two-chamber wet flue gas desulfurization apparatus.
１ 吸収塔本体 ２ 入口ダクト ３ 出口ダクト ４ 仕切板 ５ 吸収液循環ポンプ ６ 吸収液（スラ
リ） ７ 循環タンク ８、２０ 攪拌機 ９、２１ 空気吹込み管 １０ ミストエリ
ミネータ １１ 吸収液抜出し管 １２ 排ガス上昇
流領域 １３ 排ガス下降流領域 １４ 循環配管 １５ スプレヘッダー １６、１７ スプ
レノズル １８ 泡沫層 １９、２２ 気泡 ２３ 酸化用空気流通孔DESCRIPTION OF SYMBOLS 1 Absorption tower main body 2 Inlet duct 3 Outlet duct 4 Partition plate 5 Absorbent liquid circulation pump 6 Absorbent liquid (slurry) 7 Circulation tank 8, 20 Stirrer 9, 21 Air injection pipe 10 Mist eliminator 11 Absorbent liquid extraction pipe 12 Exhaust gas rising flow Area 13 Exhaust gas descending flow area 14 Circulation pipe 15 Spray header 16, 17 Spray nozzle 18 Foam layer 19, 22 Bubbles 23 Oxidation air flow hole
───────────────────────────────────────────────────── フロントページの続き (72)発明者 吉川 博文 広島県呉市宝町３番36号 バブコック日立 株式会社呉研究所内 (72)発明者 尾田 直己 広島県呉市宝町６番９号 バブコック日立 株式会社呉事業所内 Ｆターム(参考） 4D002 AA02 AC01 BA02 BA16 CA01 CA20 DA05 DA16 EA12 FA03 GB05 ──────────────────────────────────────────────────続 き Continuing on the front page (72) Hirofumi Yoshikawa 3-36 Takara-cho, Kure-shi, Hiroshima Babcock-Hitachi Inside Kure Research Laboratory (72) Naoki Oda 6-9 Takara-cho, Kure-shi, Hiroshima Babcock-Hitachi, Ltd. F-term in Kure Plant (reference) 4D002 AA02 AC01 BA02 BA16 CA01 CA20 DA05 DA16 EA12 FA03 GB05
Claims (4)
ガスをほぼ水平方向に導入する入口ダクトと、浄化した
排ガスをほぼ水平方向に排出する出口ダクトとを設け、
前記入口ダクトと出口ダクトの間に排ガス流路を設け、
その排ガス流路を入口ダクト側と出口ダクト側の二室に
分割するための天井部側に開口部を有する鉛直方向に立
てた仕切板を設けることで入口ダクトから導入される排
ガスが上向きに流れる上昇流領域と天井側の開口部で反
転した後に出口ダクトに向けて下向きに排ガスが流れる
下降流領域を形成し、それぞれの領域にスプレノズルを
設置し、該スプレノズルから噴出する吸収液スラリと排
ガスを上昇流領域では向流接触、下降流領域では並流接
触させるように配置した、排ガス中の硫黄酸化物を処理
する吸収塔と、 前記吸収塔の下方にスプレノズルから噴出する吸収液ス
ラリを貯留する循環タンクと、を備えた二室型湿式排煙
脱硫装置において、 前記仕切板の下端部を循環タンク内の吸収液内に浸漬さ
せ、該仕切板により、循環タンク内の吸収液スラリの液
深の半分の位置よりも下側であって、かつ仕切板の下端
部と循環タンクの底部との間に吸収液スラリ流通部を設
けたことを特徴とする二室型湿式排煙脱硫装置。1. An inlet duct for introducing exhaust gas discharged from a combustion device such as a boiler in a substantially horizontal direction, and an outlet duct for discharging purified exhaust gas in a substantially horizontal direction are provided.
An exhaust gas channel is provided between the inlet duct and the outlet duct,
Exhaust gas introduced from the inlet duct flows upward by providing a vertical partition plate with an opening on the ceiling side to divide the exhaust gas channel into two chambers on the inlet duct side and outlet duct side Forming a downward flow region in which exhaust gas flows downward toward the outlet duct after being inverted at the upward flow region and the opening on the ceiling side, installing a spray nozzle in each region, and removing the absorbent slurry and exhaust gas ejected from the spray nozzle. An absorption tower for treating sulfur oxides in exhaust gas, which is arranged to be in countercurrent contact in the upflow region and cocurrent contact in the downflow region, and stores an absorbent slurry ejected from a spray nozzle below the absorption tower. A circulation tank, comprising: a lower end portion of the partition plate is immersed in an absorbent in the circulation tank; A two-chamber wet type, wherein an absorption liquid slurry flow section is provided below a position at half the liquid depth of the absorption liquid slurry and between the lower end of the partition plate and the bottom of the circulation tank. Flue gas desulfurization equipment.
ける吸収液スラリの平均流速が０．５〜４ｍ／秒となる
ように該吸収液スラリ流通部の大きさを設定することを
特徴とする請求項１記載の二室型湿式排煙脱硫装置。2. The size of the absorption liquid slurry flow section is set such that the average flow rate of the absorption liquid slurry in the absorption liquid slurry flow section in the circulation tank is 0.5 to 4 m / sec. The two-chamber wet flue gas desulfurization apparatus according to claim 1.
降流領域のガス流れ方向の断面積より、仕切板で仕切ら
れた前記下降流領域下部に位置する循環タンク内のスラ
リ貯留部ガス流れ方向の断面積を小さくすることを特徴
とする請求項１記載の二室型湿式排煙脱硫装置。3. A gas flow direction of a slurry storage portion in a circulation tank located below the descending flow region divided by a partition plate, based on a cross-sectional area of the descending flow region inside the absorption tower in which exhaust gas flows downward. 2. The two-chamber wet-type flue gas desulfurization apparatus according to claim 1, wherein the cross-sectional area of the desulfurization apparatus is reduced.
化用空気流通孔を設けることを特徴とする請求項１記載
の二室型湿式排煙脱硫装置。4. The two-chamber wet flue gas desulfurization apparatus according to claim 1, wherein an oxidizing air circulation hole is provided in a partition plate portion immersed in the circulation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000353965A JP4014073B2 (en) | 2000-11-21 | 2000-11-21 | Two-chamber wet flue gas desulfurization system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000353965A JP4014073B2 (en) | 2000-11-21 | 2000-11-21 | Two-chamber wet flue gas desulfurization system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2002153727A true JP2002153727A (en) | 2002-05-28 |
| JP4014073B2 JP4014073B2 (en) | 2007-11-28 |
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|---|---|---|---|
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| CN105396451B (en) * | 2015-12-03 | 2017-07-07 | 华北电力大学 | Caustic dip efficient removal SO in a kind of spray desulfurizing tower3Technique |
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2000
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113457398A (en) * | 2021-06-28 | 2021-10-01 | 徐四保 | Multistage recyclable chemical flue gas desulfurization and denitrification equipment |
| CN114288830A (en) * | 2021-12-08 | 2022-04-08 | 常州大学 | Waste gas desulfurization treatment device |
| CN114471125A (en) * | 2022-03-17 | 2022-05-13 | 龙游县金怡热电有限公司 | Solid waste burns burning boiler gas cleaning device |
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| JP4014073B2 (en) | 2007-11-28 |
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