JP3029928B2 - Wet flue gas treatment method - Google Patents

Wet flue gas treatment method

Info

Publication number
JP3029928B2
JP3029928B2 JP4284280A JP28428092A JP3029928B2 JP 3029928 B2 JP3029928 B2 JP 3029928B2 JP 4284280 A JP4284280 A JP 4284280A JP 28428092 A JP28428092 A JP 28428092A JP 3029928 B2 JP3029928 B2 JP 3029928B2
Authority
JP
Japan
Prior art keywords
temperature
refrigerant
exhaust gas
absorbent
pipe
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
Application number
JP4284280A
Other languages
Japanese (ja)
Other versions
JPH06134255A (en
Inventor
雅和 鬼塚
清水  拓
光範 加藤
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mitsubishi Heavy Industries Ltd
Original Assignee
Mitsubishi Heavy Industries Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Mitsubishi Heavy Industries Ltd filed Critical Mitsubishi Heavy Industries Ltd
Priority to JP4284280A priority Critical patent/JP3029928B2/en
Publication of JPH06134255A publication Critical patent/JPH06134255A/en
Application granted granted Critical
Publication of JP3029928B2 publication Critical patent/JP3029928B2/en
Anticipated expiration legal-status Critical
Expired - Fee Related legal-status Critical Current

Links

Description

【発明の詳細な説明】DETAILED DESCRIPTION OF THE INVENTION

【0001】[0001]

【産業上の利用分野】本発明は湿式排煙処理方法に関
し、さらに詳しくは該方法における用水回収に適用され
る冷却器の適正運転制御を行なう同方法に関する。
BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a wet flue gas treatment method and, more particularly, to a method for appropriately controlling the operation of a cooler applied to water recovery in the method.

【0002】[0002]

【従来の技術】従来例を、図2に示す一実施態様例に基
づき説明する。図2において、充填物102を備えた吸
収塔101では吸収液循環ポンプ106で攪拌機105
を備えた液溜め104内の吸収液が配管107を介して
揚液され、吸収液スプレーパイプ108を経て吸収液ス
プレーノズル109から吸収塔101内に散布されてお
り、該散布吸収液で吸収塔101の塔頂から導入される
未処理排ガスAAは洗浄処理されるとともに増湿冷却さ
れ水分飽和排ガスとなる。冷却及び洗浄された該水分飽
和排ガスは前記吸収液溜め104の貯留吸収液の液面1
03上を通過し冷却器110で間接冷却され処理排ガス
BBとして排出される。前記冷却器110へは流量検出
器126で流量を検出し、調節計129によって調節弁
122で一定流量に制御された冷媒が配管DDから供給
されており、該冷媒は排ガスから間接的に熱を吸収した
後配管EEから抜き出されている。この排ガスから冷媒
への熱交換によって排ガス中の水分の一部は凝縮し温水
となり配管111を介して回収水タンク112に至り一
時貯留される。回収水タンク112に貯留された回収水
はポンプ113で配管114を介し前記吸収塔液溜め1
04に、また配管115を介して吸収剤調整タンク11
6へとそれぞれの補給水として使用される。なお、図2
中、117は吸収剤供給ポンプ、118は吸収剤供給配
管、CCは吸収剤、FFは吸収液抜出し配管を示す。
2. Description of the Related Art A conventional example will be described with reference to an embodiment shown in FIG. In FIG. 2, in an absorption tower 101 provided with a packing 102, a stirrer 105 is
The liquid in the liquid reservoir 104 provided with the liquid is pumped through the pipe 107 and is sprayed through the liquid spray pipe 108 from the liquid spray nozzle 109 into the absorption tower 101. The untreated exhaust gas AA introduced from the top of 101 is subjected to a washing treatment and is humidified and cooled to become a moisture-saturated exhaust gas. The cooled and washed water-saturated exhaust gas is applied to the liquid level 1 of the stored absorbent in the absorbent reservoir 104.
03, and is indirectly cooled by the cooler 110 and discharged as the processing exhaust gas BB. A flow rate is detected by a flow rate detector 126 to the cooler 110, and a refrigerant controlled to a constant flow rate by a control valve 122 by a controller 129 is supplied from a pipe DD. The refrigerant indirectly generates heat from exhaust gas. After being absorbed, it is extracted from the pipe EE. Due to the heat exchange from the exhaust gas to the refrigerant, a part of the moisture in the exhaust gas is condensed to become hot water, which is temporarily stored in the recovered water tank 112 via the pipe 111. The recovered water stored in the recovered water tank 112 is pumped by a pump 113 via a pipe 114 to the absorption tower liquid reservoir 1.
04, and the absorbent adjustment tank 11 via a pipe 115.
6 is used as make-up water for each. Note that FIG.
In the figure, 117 is an absorbent supply pump, 118 is an absorbent supply pipe, CC is an absorbent, and FF is an absorbent extraction pipe.

【0003】[0003]

【発明が解決しようとする課題】以上従来例を説明した
ように、従来例では冷却器には一定流量の冷媒が供給さ
れており、排煙処理装置への処理ガス流量負荷が運転環
境の変化に対応して変動しても冷却水の流量は一定であ
った。この場合、処理ガスの量が半減しても回収水の量
は半減されず過剰に水を回収することがあった。そのた
め負荷が低い時の回収水の量が消費量を越さないような
冷媒の流量に設定し、回収水量が消費水量を下回るよう
にしていた。そのため、負荷が高い時には用水の回収不
足となり、その不足分は工業用水などで賄っていた。
As described above, in the conventional example, a constant flow of refrigerant is supplied to the cooler in the conventional example, and the load of the processing gas flow to the flue gas treatment apparatus is changed by the change in the operating environment. The flow rate of the cooling water was constant even if it varied in response to In this case, even if the amount of the processing gas is reduced by half, the amount of the recovered water is not reduced by half, and the water may be recovered excessively. For this reason, the flow rate of the refrigerant is set so that the amount of recovered water when the load is low does not exceed the amount of consumption, so that the amount of recovered water is lower than the amount of consumed water. For this reason, when the load is high, the recovery of water is insufficient, and the shortage is covered by industrial water.

【0004】本発明は上記技術水準に鑑み、従来法にお
ける上述の問題点を解消し、必要な量の回収水を常に回
収することができる湿式排煙処理方法を提供しようとす
るものである。
The present invention has been made in view of the above-mentioned state of the art, and aims to solve the above-mentioned problems in the conventional method and to provide a wet-type flue gas treatment method capable of always collecting a required amount of recovered water.

【0005】[0005]

【課題を解決するための手段】本発明は (1)増湿冷却された水分飽和燃焼排ガスを間接冷却
し、該排ガスから水を回収し有効利用するに当って、排
ガス冷却器の出口排ガス温度を検出して該冷却器への冷
媒の供給流量を制御すると共に前記排ガス冷却によって
得られる回収水の消費速度に応じて前記冷却器出口排ガ
スの冷却温度設定を制御することを特徴とする湿式排煙
処理方法。 (2)上記(1)における排ガス冷却器に供給される冷
媒として海水を用いるに際して、該冷媒の入口と出口の
温度を検出して低温側冷媒を高温側冷媒に混合して高温
側と低温側の冷媒の温度差が設定温度以上にならないよ
うに制御することを特徴とする湿式排煙処理方法。 である。
SUMMARY OF THE INVENTION The present invention relates to (1) indirect cooling of a moisture-saturated flue gas which has been subjected to humidification and cooling, and recovering and effectively utilizing water from the flue gas; And controlling the supply flow rate of the refrigerant to the cooler and controlling the cooling temperature setting of the exhaust gas at the cooler outlet according to the consumption rate of the recovered water obtained by the exhaust gas cooling. Smoke treatment method. (2) When seawater is used as the refrigerant to be supplied to the exhaust gas cooler in the above (1), the temperatures at the inlet and the outlet of the refrigerant are detected, the low-temperature refrigerant is mixed with the high-temperature refrigerant, and the high-temperature refrigerant and the low-temperature refrigerant are mixed. Controlling the difference in temperature between the refrigerants so as not to exceed a set temperature. It is.

【0006】[0006]

【作用】本発明によれば、未処理排ガスの増湿冷却への
消費量および排ガス洗浄に使用された吸収剤の消費量に
応じて変化する回収水の消費量が回収水タンクでの液位
変化として検出できるため、その液位の変化状況に応じ
て冷却処理排ガスの温度を変化させれば必要な時に必要
量の回収水が確保できる。また、海水を冷媒として用い
る場合、排出海水の温度を一定値内に制御できるので、
排出海水が放流される海域の温度上昇を所定値内に制御
することができる。
According to the present invention, the consumption of recovered water, which varies according to the consumption of untreated exhaust gas for humidifying cooling and the consumption of absorbent used for exhaust gas cleaning, is increased in the level of the recovered water tank. Since it can be detected as a change, if the temperature of the cooling treatment exhaust gas is changed according to the change state of the liquid level, a required amount of recovered water can be secured when necessary. Also, when using seawater as a refrigerant, the temperature of the discharged seawater can be controlled within a certain value,
The temperature rise in the sea area where the discharged seawater is discharged can be controlled within a predetermined value.

【0007】[0007]

【実施例】本発明を図1に示す一実施態様例を用いて具
体的に説明する。図1において、充填物2を備えた吸収
塔1に約110℃の未処理排ガスAを毎時15,000
3 N乃至7,000m3 Nを導入し、該吸収塔1内に
吸収液循環ポンプ6で攪拌機5を備えた液溜め4内のC
a化合物を含んだ吸収液を配管7を介して毎時180m
3 で揚液し、吸収液スプレーパイプ8を介して吸収スプ
レーノズル9から吸収塔1内に散布し、該散布吸収液で
前記未処理排ガスAを脱硫処理するとともに約50℃に
増湿冷却し、前記吸収液溜め4内の貯留吸収液の液面3
上を通過させた後冷却器10で間接冷却し処理排ガスB
として排出した。前記冷却器10へは冷媒供給配管Dか
ら約18℃の海水を供給した。
DESCRIPTION OF THE PREFERRED EMBODIMENTS The present invention is implemented by using an embodiment shown in FIG.
Explain physically. In FIG. 1, the absorption with the filling 2
The untreated exhaust gas A at about 110 ° C.
m ThreeN to 7,000mThreeN is introduced into the absorption tower 1
C in the reservoir 4 provided with the stirrer 5 by the absorption liquid circulation pump 6
180 m / h through pipe 7
ThreeAnd absorb it through the absorbent spray pipe 8
Sprayed from the laser nozzle 9 into the absorption tower 1, and
The untreated exhaust gas A is desulfurized and brought to about 50 ° C.
The humidified and cooled surface of the absorbing liquid stored in the absorbing liquid reservoir 4
After passing through the upper part, the exhaust gas B is indirectly cooled by the cooler 10 and treated.
As discharged. Is the refrigerant supply pipe D to the cooler 10?
Seawater at about 18 ° C.

【0008】該海水の供給流量の調節は前記処理排ガス
Bの温度を温度検出器20で検出し、該信号を温度調節
器21に入力し、該温度調節器21での設定温度との偏
差に応じて調節弁22を駆動させ冷媒流量を調節し前記
処理排ガスBの温度調節を行った。冷却器10では冷媒
による処理排ガスBからの熱の吸収によって排ガスBの
温度低下が起こり、該排ガスBの水分の一部が凝縮し温
水と化し、回収水配管11を介して回収水タンク12に
流下して回収水として集められ、ポンプ13で前記吸収
液溜め4及び吸収剤調整タンク16へとそれぞれ配管1
4及び配管15を介して補給した。これらの補給水量は
それぞれ吸収塔1での排ガスAの増湿冷却用として消費
された水量および吸収塔1での脱硫中和に消費された吸
収剤供給配管18から吸収剤調整ポンプ17によって供
給される吸収剤の供給流量に対応した量である。これら
の補給及び回収水配管11からの回収水の流入による回
収水タンク12の液位の変化を液位検出器23で検出し
て液位指示計24で液位を指示させ、その液位信号をも
とに演算器25で演算し、該演算信号で前記温度調節器
21の設定温度を可変させるようにした。
In order to adjust the supply flow rate of the seawater, the temperature of the treated exhaust gas B is detected by a temperature detector 20 and the signal is input to a temperature controller 21 to calculate the deviation from the set temperature at the temperature controller 21. Accordingly, the control valve 22 was driven to adjust the flow rate of the refrigerant, and the temperature of the treated exhaust gas B was adjusted. In the cooler 10, the temperature of the exhaust gas B decreases due to the absorption of heat from the processing exhaust gas B by the refrigerant, and a part of the moisture of the exhaust gas B is condensed into hot water. It is collected as recovered water by flowing down, and the pipe 13 is connected to the absorbent reservoir 4 and the absorbent adjusting tank 16 by a pump 13.
4 and the supply via the pipe 15. These replenishing water amounts are respectively supplied by an absorbent adjusting pump 17 from an absorbent supply pipe 18 consumed for the humidifying cooling of the exhaust gas A in the absorption tower 1 and an absorbent supply pipe 18 consumed for desulfurization neutralization in the absorption tower 1. The amount corresponds to the supply flow rate of the absorbent. A change in the liquid level in the recovered water tank 12 due to the inflow of the recovered water from the replenishment and recovered water pipe 11 is detected by a liquid level detector 23, and the liquid level is indicated by a liquid level indicator 24. Is calculated by the calculator 25 based on the above equation, and the set temperature of the temperature controller 21 is varied by the calculation signal.

【0009】ところで、上記において配管Dから供給さ
れる冷媒として海水を使用したが、該海水は使用後は配
管Eを介して放水した。放水するに当って、該海水の温
度を温度検出器27で検出し温度指示計28で監視する
と共に配管Dを介して冷却器10に供給されている海水
の温度も温度検出器26で検出し同様に温度指示計29
で監視し、さらに温度検出器26及び27での検出温度
信号を温度差調節計30に入力し、該温度差調節計30
でこれらの温度差が設定温度差6℃を上回らないよう調
節弁31を制御し、配管Dより流入する海水の一部を分
岐し配管Eに合流する配管を介して供給し、配管Eを介
して放流される海水の温度上昇を所定値以下にした。な
お、図1中、Fは吸収液抜出し配管を示す。
In the above description, seawater was used as the refrigerant supplied from the pipe D. The seawater was discharged through the pipe E after use. In discharging the water, the temperature of the seawater is detected by the temperature detector 27 and monitored by the temperature indicator 28, and the temperature of the seawater supplied to the cooler 10 via the pipe D is also detected by the temperature detector 26. Similarly, the temperature indicator 29
, And the temperature signals detected by the temperature detectors 26 and 27 are input to the temperature difference controller 30.
Then, the control valve 31 is controlled so that these temperature differences do not exceed the set temperature difference of 6 ° C., a part of the seawater flowing from the pipe D is supplied through a pipe which branches and joins the pipe E, and is supplied through the pipe E. The temperature rise of the discharged seawater was kept below a predetermined value. In addition, in FIG. 1, F shows an absorption liquid extraction pipe.

【0010】なお、この実施例で使用した吸収塔1は断
面が1m角で高さ10mであり、充填物としては格子状
のものを3m充填した。冷却器の伝熱面積は70m2
ものを用いた。また、供試未処理排ガス中のSO2 濃度
は平均して600ppm程度であった。
The absorption tower 1 used in this example had a cross section of 1 m square and a height of 10 m, and was filled with a lattice-like packing of 3 m. The heat transfer area of the cooler was 70 m 2 . The SO 2 concentration in the untreated exhaust gas was about 600 ppm on average.

【0011】以上、本発明を図1の実施態様例を用いて
具体的に説明したが、この実施例では上記したように未
処理排ガスAの流量を毎時15,000〜7,000m
3 Nの範囲で変化させたが回収タンクでの保持回収水量
はほぼ一定していた。その間液溜め4及び吸収剤の供給
流量は処理ガス流量の変動に応じて変動しており、この
実施例による制御が好調に動作したことが間接的に確認
された。また、放流海水の温度は供給海水に対して約4
〜6℃の上昇であった。
The present invention has been described in detail with reference to the embodiment shown in FIG. 1. In this embodiment, as described above, the flow rate of untreated exhaust gas A is 15,000 to 7,000 m / h.
Although the amount was changed within the range of 3N, the amount of collected water retained in the collection tank was almost constant. During that time, the supply flow rates of the liquid reservoir 4 and the absorbent fluctuated according to the fluctuation of the processing gas flow rate, and it was indirectly confirmed that the control according to this embodiment operated favorably. The temperature of the discharged seawater is about 4
66 ° C. increase.

【0012】[0012]

【発明の効果】本発明によれば、冷却する処理排ガス流
量が変動し用水の消費量が変動しても用水の消費量に応
じて必要な量の用水を排ガスから回収できるものであ
る。また、冷媒として海水を使用しても放流海水温度を
放流海域に影響を及ぼさない温度にすることができる。
According to the present invention, a required amount of water can be recovered from the exhaust gas in accordance with the consumption of the water even if the flow rate of the treated exhaust gas to be cooled fluctuates and the consumption of the water fluctuates. In addition, even if seawater is used as the refrigerant, the temperature of the discharged seawater can be set to a temperature that does not affect the discharged sea area.

【図面の簡単な説明】[Brief description of the drawings]

【図1】本発明の一実施態様の説明図。FIG. 1 is an explanatory diagram of one embodiment of the present invention.

【図2】従来の湿式排煙処理方法の一実施態様の説明
図。
FIG. 2 is an explanatory view of one embodiment of a conventional wet smoke exhaust treatment method.

【符号の説明】[Explanation of symbols]

1.吸収塔 2.充填物 3.吸収液液面 4.吸収液溜め 5.攪拌機 6.吸収液循環ポンプ 7.配管 8.吸収液スプレーパイプ 9.吸収液スプレーノズル 10.冷却器 11.回収水配管 12.回収水タンク 13.回収水ポンプ 14.回収水補給配管 15.回収水補給配管 16.吸収剤調整タンク 17.吸収剤調整ポンプ 18.吸収剤供給配管 20.温度検出器 21.温度調節計 22.調節弁 23.液位検出器 24.液位指示計 25.演算器 26.温度検出器 27.温度検出器 28.温度指示計 29.温度指示計 30.温度差調節計管 31.調節弁 A.未処理排ガス B.処理排ガス C.吸収剤 D.冷却水供給配管 E.冷却水抜出し配管 F.吸収液抜出し配管 1. Absorption tower 2. Filling 3. Absorbent liquid level 4. Absorbent reservoir 5. Stirrer 6. Absorbent circulation pump 7. Piping 8. 8. Absorbent spray pipe Absorbent spray nozzle 10 Cooler 11. Collected water piping 12. Collected water tank 13. 13. Collected water pump 14. Collected water supply pipe Collected water supply piping 16. Absorbent adjustment tank 17. Absorbent adjustment pump 18. Absorbent supply piping 20. Temperature detector 21. Temperature controller 22. Control valve 23. Liquid level detector 24. Liquid level indicator 25. Arithmetic unit 26. Temperature detector 27. Temperature detector 28. Temperature indicator 29. Temperature indicator 30. Temperature difference controller tube 31. Control valve A. Untreated exhaust gas B. Processed exhaust gas C. Absorbent D. Cooling water supply piping E. Coolant drain pipe Absorbent drain pipe

───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 昭50−119362(JP,A) (58)調査した分野(Int.Cl.7,DB名) B01D 53/34 B01D 53/50 B01D 53/77 ──────────────────────────────────────────────────続 き Continuation of the front page (56) References JP-A-50-119362 (JP, A) (58) Fields investigated (Int. Cl. 7 , DB name) B01D 53/34 B01D 53/50 B01D 53 / 77

Claims (2)

(57)【特許請求の範囲】(57) [Claims] 【請求項1】 増湿冷却された水分飽和燃焼排ガスを間
接冷却し、該排ガスから水を回収し有効利用するに当っ
て、排ガス冷却器の出口排ガス温度を検出して該冷却器
への冷媒の供給流量を制御すると共に前記排ガス冷却に
よって得られる回収水の消費速度に応じて前記冷却器出
口排ガスの冷却温度設定を制御することを特徴とする湿
式排煙処理方法。
1. A method for indirectly cooling a moisture-saturated flue gas that has been subjected to humidification and cooling, and for recovering and effectively utilizing water from the flue gas, detects an exhaust gas temperature at an outlet of a flue gas cooler and sends the refrigerant to the cooler. And controlling a cooling temperature setting of the exhaust gas at the cooler outlet according to a consumption rate of the recovered water obtained by the cooling of the exhaust gas.
【請求項2】 請求項1における排ガス冷却器に供給さ
れる冷媒として海水を用いるに際して、該冷媒の入口と
出口の温度を検出して低温側冷媒を高温側冷媒に混合し
て高温側と低温側の冷媒の温度差が設定温度以下になら
ないように制御することを特徴とする湿式排煙処理方
法。
2. When seawater is used as the refrigerant to be supplied to the exhaust gas cooler according to claim 1, the temperature of the inlet and the outlet of the refrigerant is detected, the low-temperature refrigerant is mixed with the high-temperature refrigerant, and the high-temperature refrigerant and the low-temperature refrigerant are mixed. Controlling the temperature difference between the refrigerants on the side to be lower than a set temperature.
JP4284280A 1992-10-22 1992-10-22 Wet flue gas treatment method Expired - Fee Related JP3029928B2 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
JP4284280A JP3029928B2 (en) 1992-10-22 1992-10-22 Wet flue gas treatment method

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JP4284280A JP3029928B2 (en) 1992-10-22 1992-10-22 Wet flue gas treatment method

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JPH06134255A JPH06134255A (en) 1994-05-17
JP3029928B2 true JP3029928B2 (en) 2000-04-10

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Publication number Priority date Publication date Assignee Title
CN101879379B (en) * 2010-07-12 2012-05-23 西安交通大学 Gas exhausting and water containing system and method for lithium bromide recycling desulfurization system
JP2013039527A (en) * 2011-08-16 2013-02-28 Babcock Hitachi Kk Wet-type flue gas desulfurization apparatus, and thermal power generation plant provided with the same

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