JPS637812B2 - - Google Patents
Info
- Publication number
- JPS637812B2 JPS637812B2 JP53094814A JP9481478A JPS637812B2 JP S637812 B2 JPS637812 B2 JP S637812B2 JP 53094814 A JP53094814 A JP 53094814A JP 9481478 A JP9481478 A JP 9481478A JP S637812 B2 JPS637812 B2 JP S637812B2
- Authority
- JP
- Japan
- Prior art keywords
- circulation tank
- cooling tower
- absorption
- exhaust gas
- absorption tower
- 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
Links
- 238000010521 absorption reaction Methods 0.000 claims description 61
- 239000007788 liquid Substances 0.000 claims description 55
- 238000001816 cooling Methods 0.000 claims description 48
- 230000002745 absorbent Effects 0.000 claims description 46
- 239000002250 absorbent Substances 0.000 claims description 46
- 239000002002 slurry Substances 0.000 claims description 44
- 239000007789 gas Substances 0.000 claims description 42
- 238000006477 desulfuration reaction Methods 0.000 claims description 26
- 230000023556 desulfurization Effects 0.000 claims description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 26
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 12
- 239000003546 flue gas Substances 0.000 claims description 12
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 claims description 10
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 239000012809 cooling fluid Substances 0.000 claims 1
- 239000000498 cooling water Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000004044 response Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 238000004566 IR spectroscopy Methods 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 230000002457 bidirectional effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、湿式排煙脱硫装置に関し、特に排ガ
ス中のイオウ酸化物（主に二酸化イオウSO2）を
石灰石スラリー等の吸収液を用いて吸収除去する
排煙脱硫装置における運転制御の改良に関するも
のである。[Detailed Description of the Invention] [Industrial Application Field] The present invention relates to a wet flue gas desulfurization system, and in particular to a wet flue gas desulfurization system that removes sulfur oxides (mainly sulfur dioxide SO 2 ) from flue gas using an absorbing liquid such as limestone slurry. This invention relates to improvement of operation control in flue gas desulfurization equipment that absorbs and removes sulfur.
吸収剤として石灰石を用いた従来の排煙脱硫装
置の系統図を第１図に示す。この装置は、排ガス
を冷却する冷却塔１と、該冷却塔１に冷却水を循
環させる冷却塔循環タンク２と、冷却塔１で冷却
された排ガスからイオウ酸化物（二酸化イオウ
SO2で代表される）を吸収除去する吸収塔３と、
該吸収塔３へ吸収液を循環させる吸収塔循環タン
ク４とから主としてなる。排ガスは、ライン５か
ら冷却塔１に導入され、ここで冷却水スプレーノ
ズル６から噴霧される冷却水で冷却され、一部の
SO2が除去され、次いでライン７から吸収塔３に
送られる。一方、冷却水はライン８を通つて冷却
塔循環タンク２に回収され、ここから循環ポンプ
９およびライン１０を通つてスプレーノズル６に
送られる。冷却塔循環タンク２には液面制御器が
取付けられており、前記循環タンク２の液面レベ
ルが設定値になるように、補給水制御弁１２の開
度が調節され、ライン１３を介して補給水を前記
タンク２へ供給することによつて液面が一定レベ
ルに保たれる。
A system diagram of a conventional flue gas desulfurization equipment using limestone as an absorbent is shown in Fig. 1. This device includes a cooling tower 1 that cools exhaust gas, a cooling tower circulation tank 2 that circulates cooling water in the cooling tower 1, and a cooling tower 1 that converts sulfur oxide (sulfur dioxide) from the exhaust gas cooled in the cooling tower 1.
an absorption tower 3 that absorbs and removes (represented by SO 2 );
It mainly consists of an absorption tower circulation tank 4 that circulates the absorption liquid to the absorption tower 3. The exhaust gas is introduced into the cooling tower 1 from the line 5, where it is cooled by cooling water sprayed from the cooling water spray nozzle 6, and some of the exhaust gas is
SO 2 is removed and then sent to absorption column 3 via line 7. On the other hand, the cooling water is collected through line 8 to cooling tower circulation tank 2, from where it is sent to spray nozzle 6 through circulation pump 9 and line 10. A liquid level controller is attached to the cooling tower circulation tank 2, and the opening degree of the make-up water control valve 12 is adjusted so that the liquid level in the circulation tank 2 reaches a set value. By supplying makeup water to the tank 2, the liquid level is maintained at a constant level.
一方、ライン７を通つて吸収塔３に導入された
排ガスは、スプレーノズル１４から供給される吸
収剤スラリーと接触して排ガス中のSO2が反応除
去され、清浄化された処理ガスはライン１５から
系外に排出される。また吸収液は吸収塔３の下部
からライン１６を通つて吸収塔循環タンク４に送
入され、ライン１７から新たに補給される吸収剤
スラリーと混合され、再び循環ポンプ１８により
ライン１９を通つて吸収塔３内のスプレーノズル
１４に供給される。循環ライン１９には、流量計
２３および流量制御弁２６が設けられ、排ガス流
量当りの吸収液の循環流量（Ｌ／Ｇ）が一定にな
るように制御される。すなわち、流量計２３の流
量測定値信号は流量制御装置２５から入力され、
ここで排ガス流量から求められた上記Ｌ／Ｇが一
定になる流量設定値信号と比較され、その差に応
じて流量制御弁２６の開度が調節される。 On the other hand, the exhaust gas introduced into the absorption tower 3 through the line 7 comes into contact with the absorbent slurry supplied from the spray nozzle 14, so that SO 2 in the exhaust gas is removed by reaction, and the purified treated gas is transferred to the line 15. is discharged from the system. In addition, the absorption liquid is sent from the lower part of the absorption tower 3 to the absorption tower circulation tank 4 through a line 16, mixed with absorbent slurry newly supplied from a line 17, and then passed through a line 19 again by a circulation pump 18. It is supplied to the spray nozzle 14 in the absorption tower 3. The circulation line 19 is provided with a flow meter 23 and a flow control valve 26, and is controlled so that the circulation flow rate (L/G) of the absorption liquid per exhaust gas flow rate is constant. That is, the flow rate measurement value signal of the flow meter 23 is inputted from the flow rate control device 25,
Here, the L/G determined from the exhaust gas flow rate is compared with a constant flow rate set value signal, and the opening degree of the flow rate control valve 26 is adjusted according to the difference.
また上記吸収剤スラリーの供給ライン１７には
吸収剤流量制御弁２７が設けられ、吸収塔循環タ
ンク４内に設けられたPH計28およびPH制御装置２
９によりPHが所定値になるようにその開度が調節
される。また吸収塔循環タンク４には、液面（レ
ベル）制御器２１および液面制御弁２２が設けら
れ、該循環タンク４が所定の液面レベルを保持す
るように前記ライン２０の液面制御弁２２が調節
される。循環される吸収液の一部は、吸収塔循環
タンク４の液面レベル弁２２により、分岐ライン
２０を通つて冷却塔循環タンク２に供給されるよ
うになつており、この吸収液は冷却塔循環タンク
２内で冷却水と混合され、冷却塔における冷却兼
吸収液として利用される。 Further, an absorbent flow rate control valve 27 is provided in the absorbent slurry supply line 17, and a PH meter 28 and a PH control device 2 provided in the absorption tower circulation tank 4 are provided.
9, the opening degree is adjusted so that the PH becomes a predetermined value. Further, the absorption tower circulation tank 4 is provided with a liquid level controller 21 and a liquid level control valve 22, and the liquid level control valve of the line 20 is arranged so that the circulation tank 4 maintains a predetermined liquid level. 22 is adjusted. A part of the circulating absorption liquid is supplied to the cooling tower circulation tank 2 through a branch line 20 by a liquid level valve 22 of the absorption tower circulation tank 4, and this absorption liquid is supplied to the cooling tower circulation tank 2 through a branch line 20. It is mixed with cooling water in the circulation tank 2 and used as a cooling and absorption liquid in the cooling tower.
脱硫によつて各循環タンク２，４内に生成する
生成物（CaSO4等）は、冷却塔循環タンク２内の
吸収剤スラリーの一部をライン１０の分岐ライン
５６より取り出されて後処理装置へ送られ、最終
処理される。その取り出しは、関数発生器５７、
流量計５８、制御器５９及び流量制御弁６０によ
つて制御されて連続的に行なわれる。すなわち、
排ガスのSO2量に対応して信号を出力する流量制
御装置３７からの信号を受けて関数発生器５７に
より吸収剤スラリーの取り出し量を設定する信号
が制御器５９に出力される。また、分岐ライン５
６中の流量計５８から流量信号が制御器５９に出
力され、該制御器５９から流量制御弁６０の制御
信号が出力され、吸収剤スラリーの一部が連続的
に取り出されて前記生成物（CaSO4等）が連続的
に処理される。 Products (such as CaSO 4 ) generated in each circulation tank 2 and 4 due to desulfurization are removed from a part of the absorbent slurry in the cooling tower circulation tank 2 through a branch line 56 of the line 10 and sent to a post-treatment device. and sent for final processing. The extraction is performed by a function generator 57,
The flow rate is continuously controlled by a flow meter 58, a controller 59, and a flow control valve 60. That is,
In response to a signal from the flow control device 37 which outputs a signal corresponding to the amount of SO 2 in the exhaust gas, the function generator 57 outputs a signal to the controller 59 to set the amount of absorbent slurry to be taken out. Also, branch line 5
A flow rate signal is outputted from the flow meter 58 in 6 to the controller 59, and a control signal for the flow rate control valve 60 is outputted from the controller 59, and a part of the absorbent slurry is continuously taken out and the product ( CaSO 4 etc.) are treated continuously.
吸収剤スラリーの取り出しにより両タンク２，
４内の液面レベルが低下すると、その低下が検知
されて補給水制御弁１２が開となり補給水が補給
される。 By taking out the absorbent slurry, both tanks 2,
When the liquid level in the tank 4 decreases, the drop is detected and the make-up water control valve 12 is opened to replenish the make-up water.
上記従来装置においては、先ず吸収剤スラリー
循環系に用いる流量計２３、流量制御弁２６に炭
酸カルシウムのような吸収剤その他の固形分が付
着してスケーリングを生じ、また固形分による摩
耗が激しく、長時間連続使用することができず、
極端な場合には、例えば３ケ月毎に分解点検補修
を要するという問題がある。
In the above-mentioned conventional apparatus, first, absorbent such as calcium carbonate and other solid contents adhere to the flow meter 23 and flow control valve 26 used in the absorbent slurry circulation system, causing scaling, and the solid contents cause severe wear. It cannot be used continuously for a long time,
In extreme cases, there is a problem that disassembly, inspection and repair are required every three months, for example.
第二に、吸収剤供給流量制御系においては、吸
収剤スラリーのPHを測定するPH計28の電極にスラ
リー中の固形分が付着し、例えば１週間以内、場
合によつては３日に１度程度の清浄を必要とす
る。またPHによる制御では、処理排ガス流量の変
化に対して系内に循環している吸収剤スラリーの
量が多量であるため、排ガス流量の変化に対し、
PHの変化が非常に遅れて発生する。このため、吸
収塔３に供給される吸収液スラリーのPHの偏差が
大きくなり、脱硫効率（出口硫黄酸化物量／入口
硫黄酸化物量で定義される）が大巾に変動すると
いう問題がある。 Second, in the absorbent supply flow rate control system, the solid content in the slurry adheres to the electrode of the PH meter 28 that measures the pH of the absorbent slurry, for example within one week, and in some cases once every three days. Requires moderate cleaning. In addition, with PH control, the amount of absorbent slurry circulating in the system is large in response to changes in the flow rate of the treated exhaust gas.
Changes in PH occur very late. For this reason, there is a problem in that the deviation in the pH of the absorption liquid slurry supplied to the absorption tower 3 becomes large, and the desulfurization efficiency (defined as the amount of sulfur oxides at the outlet/the amount of sulfur oxides at the inlet) fluctuates widely.
第三に、上記のように冷却塔１および吸収塔３
の二段階でイオウ酸化物の吸収を図る脱硫装置に
おいては、高温の排ガスは冷却塔１で吸収剤スラ
リーと接触することにより、スラリー中の水分を
蒸発させて冷却されるとともに前述のようにイオ
ウ酸化物が一部除去されて、吸収塔３へ送られ、
さらに吸収塔３でイオウ酸化物が除去された後、
系外へ送り出される。補給水流量としては、前述
の蒸発水分に相当する補給水を供給するととも
に、供給吸収剤スラリー濃度と、系内スラリー濃
度が異なる場合には、濃度調節用の補給水が供給
される。ここで、上記蒸発水分量の測定は実際上
困難であるため、その代りに循環タンク２の液面
レベルを測定して補給水を供給する方法がとられ
ている。しかし、この方法では該補給水の他に吸
収塔３の循環スラリーの一部が制御弁２２を通つ
て冷却塔循環タンク２へ流入するので、冷却塔循
環タンク２内の液面レベルが既に設定値にあると
きには、この流入により該冷却塔循環タンク２内
の液面レベルが異常に増加することになる。従つ
て、常に安定した制御を行なうことは困難であ
る。また、冷却塔１から吸収塔３の排ガスととも
に、吸収剤スラリーがミストとして飛散するとい
う問題があつた。 Third, as mentioned above, cooling tower 1 and absorption tower 3
In the desulfurization equipment that attempts to absorb sulfur oxides in two stages, the high-temperature exhaust gas is cooled by contacting the absorbent slurry in the cooling tower 1 to evaporate the moisture in the slurry and remove sulfur as described above. Some of the oxides are removed and sent to the absorption tower 3,
Furthermore, after sulfur oxides are removed in absorption tower 3,
Sent out of the system. As for the flow rate of make-up water, make-up water corresponding to the above-mentioned evaporated water is supplied, and if the supplied absorbent slurry concentration differs from the slurry concentration in the system, make-up water for concentration adjustment is supplied. Here, since it is practically difficult to measure the amount of evaporated water, an alternative method is to measure the liquid level in the circulation tank 2 and supply makeup water. However, in this method, in addition to the make-up water, part of the circulating slurry in the absorption tower 3 flows into the cooling tower circulation tank 2 through the control valve 22, so the liquid level in the cooling tower circulation tank 2 has already been set. When the cooling tower circulation tank 2 is at this value, the liquid level in the cooling tower circulation tank 2 will abnormally increase due to this inflow. Therefore, it is difficult to always perform stable control. Further, there was a problem in that the absorbent slurry was scattered as mist from the cooling tower 1 together with the exhaust gas from the absorption tower 3.
本発明の目的は、上記従来技術の欠点を除き、
簡単で応答が早く、排ガス量または排ガス中のイ
オウ酸化物濃度が変動した場合においても安定し
た運転制御を行なうことができる湿式排煙脱硫装
置を提供することにある。 The purpose of the present invention is to eliminate the drawbacks of the above-mentioned prior art,
It is an object of the present invention to provide a wet flue gas desulfurization device that is simple, has a quick response, and can perform stable operation control even when the amount of exhaust gas or the concentration of sulfur oxides in the exhaust gas fluctuates.
本発明は、吸収塔循環タンクから吸収塔へ循環
させる吸収液の循環流量を一定とし、冷却塔循環
タンクと吸収塔循環タンクとを連絡配管で連通さ
せ、冷却塔および吸収塔の各循環タンクの液面レ
ベルの変動を検出して当該各循環タンクの液量が
一定になるように補給水を供給する制御系統と、
冷却塔に供給される排ガスの物理量を検出して該
排ガス中のイオウ酸化物の反応当量以上の吸収剤
が供給されるように前記吸収剤スラリーの供給量
を調節する制御系統とを設けることにより、冷却
塔循環タンクへの蒸発減少を補なう補給水の供給
を安定制御することができると共に、連絡配管に
よつて冷却塔循環タンクと吸収塔循環タンクとの
液面レベルを共通にして、一方の液面レベルが異
常に増加するおそれをなくし、排ガスの流量変動
等に対し安定した脱硫性能を発揮し得るようにし
たものである。
In the present invention, the circulation flow rate of the absorption liquid circulated from the absorption tower circulation tank to the absorption tower is constant, the cooling tower circulation tank and the absorption tower circulation tank are communicated with each other by connecting piping, and each circulation tank of the cooling tower and absorption tower is a control system that detects fluctuations in the liquid level and supplies make-up water so that the liquid volume in each circulation tank is constant;
By providing a control system that detects the physical amount of exhaust gas supplied to the cooling tower and adjusts the supply amount of the absorbent slurry so that an amount of absorbent that is equal to or more than the reaction equivalent of sulfur oxide in the exhaust gas is supplied. , it is possible to stably control the supply of make-up water to the cooling tower circulation tank to compensate for the decrease in evaporation, and to make the liquid level common between the cooling tower circulation tank and the absorption tower circulation tank through the connecting piping. This eliminates the risk of an abnormal increase in the liquid level on one side, and allows stable desulfurization performance to be exhibited against fluctuations in the flow rate of exhaust gas.
第２図は、本発明の一実施例を示す脱硫装置の
系統図である。第１図の従来装置と異なる第１の
特徴は、吸収塔循環タンク４の流量計２３および
流量制御弁２６を省き、ポンプ揚程、配管、スプ
レーノズルを適当に選定して、常に一定の吸収液
スラリー循環を得るようにし、排ガス流量が変化
しても吸収剤スラリーの循環流量はほぼ一定のま
ま保たれるように構成したことである。
FIG. 2 is a system diagram of a desulfurization apparatus showing an embodiment of the present invention. The first feature that differs from the conventional device shown in FIG. The slurry is circulated, and even if the exhaust gas flow rate changes, the absorbent slurry circulation flow rate remains almost constant.
上記装置の第２の特徴は、吸収塔循環タンクの
吸収剤供給系において、従来装置のPH計28および
PH制御装置２９の代りに、処理する排ガスの物理
量である排ガス流量信号と排ガスのイオウ酸化物
濃度信号から計算器３２により排ガス中のイオウ
酸化物総量を求め、次に制御器３７により、前記
イオウ酸化物総量信号３３と吸収剤スラリー流量
計３６からの濃度信号３４とから必要な吸収剤ス
ラリーの供給流量を得るように、吸収剤流量制御
弁３５の開度を調節するようにしたことである。 The second feature of the above device is that in the absorbent supply system of the absorption tower circulation tank, the PH meter 28 of the conventional device and
Instead of the PH controller 29, the calculator 32 calculates the total amount of sulfur oxides in the exhaust gas from the exhaust gas flow rate signal, which is a physical quantity of the exhaust gas to be processed, and the sulfur oxide concentration signal of the exhaust gas, and then the controller 37 determines the sulfur oxide concentration signal. The opening degree of the absorbent flow rate control valve 35 is adjusted so that the required supply flow rate of absorbent slurry is obtained from the total oxide amount signal 33 and the concentration signal 34 from the absorbent slurry flowmeter 36. .
さらに第３の特徴は、冷却塔循環タンク２の液
面レベルおよび吸収塔循環タンク４の液面レベル
を測定し、両者の値から系内に保存される吸収剤
スラリーの総量を計算し、この値が一定になるよ
うに補給水流量を制御するようにしたことであ
る。すなわち、冷却塔循環タンク２と吸収塔循環
タンク４を、連絡配管３８で連通させ、さらに各
循環タンク２，４にそれぞれ、液面レベル伝送器
３９および４０、演算器４１および４２を設け、
各液面レベルと各タンクの断面積から各タンクの
液量を算出し、次いで加算器４３でこれらの演算
値を加算して、これを液面レベル制御器４４に入
力し、両タンクの液面レベルが一定値になるよう
に補給水制御弁１２の開度を調節する補給水供給
制御系を設けたことである。 Furthermore, the third feature is that the liquid level in the cooling tower circulation tank 2 and the liquid level in the absorption tower circulation tank 4 are measured, and the total amount of absorbent slurry stored in the system is calculated from both values. The make-up water flow rate was controlled so that the value remained constant. That is, the cooling tower circulation tank 2 and the absorption tower circulation tank 4 are connected through a connecting pipe 38, and each circulation tank 2, 4 is provided with liquid level transmitters 39 and 40, and computing units 41 and 42, respectively.
The liquid volume of each tank is calculated from each liquid level and the cross-sectional area of each tank, and then the adder 43 adds these calculated values, and this is input to the liquid level controller 44 to calculate the liquid level of both tanks. A make-up water supply control system is provided that adjusts the opening degree of the make-up water control valve 12 so that the surface level becomes a constant value.
前記吸収塔循環タンク４の制御系において、排
ガス流量の測定は、差圧発生機構であるオリフイ
ス、ベンチユリーまたはタービンメータ等の既知
の方法で行なわれ、信頼性ある測定値を得ること
ができる。排ガス中のイオウ酸化物濃度の測定
は、既知の分析計、例えば、赤外線分光法、化学
発光法等により、長期間の連続分析が可能であ
り、同様に安定した測定値を得ることができる。
これら両者の信号の積は、排ガス中のイオウ酸化
物の総量を示すことになり、この値に対し反応当
量以上のモル比の吸収剤を注入するように制御系
が構成される。 In the control system of the absorption tower circulation tank 4, the flow rate of the exhaust gas is measured by a known method such as an orifice, a ventilee, or a turbine meter, which are differential pressure generating mechanisms, and reliable measured values can be obtained. The sulfur oxide concentration in the exhaust gas can be continuously analyzed over a long period of time using a known analyzer, such as infrared spectroscopy or chemiluminescence, and stable measurement values can also be obtained.
The product of these two signals indicates the total amount of sulfur oxides in the exhaust gas, and the control system is configured to inject the absorbent at a molar ratio greater than the reaction equivalent to this value.
前記の吸収剤供給制御系統においては、吸収剤
スラリーの流量測定は、スラリー中の鉄分が多い
場合は浮子式流量計、鉄分が含まれていない場合
は電磁流量計が好適に用いられる。いずれの場合
も吸収剤スラリー供給配管の口径は比較的大きく
てもよく、安価に構成することができる。上記構
成により、排ガスの流量が変化しても直ちに吸収
剤供給スラリー流量が変化するので、系内で循環
している吸収剤スラリーのPH変化は小さく、脱硫
効率はほとんど変化しない。 In the above-mentioned absorbent supply control system, for measuring the flow rate of the absorbent slurry, a float type flowmeter is suitably used when the slurry contains a large amount of iron, and an electromagnetic flowmeter is suitably used when the slurry does not contain iron. In either case, the diameter of the absorbent slurry supply piping may be relatively large and can be constructed at low cost. With the above configuration, even if the flow rate of exhaust gas changes, the flow rate of the absorbent supply slurry changes immediately, so the pH change of the absorbent slurry circulating in the system is small, and the desulfurization efficiency hardly changes.
前記の補給水流量制御系においては、各々の循
環タンク２，４の液面レベルを測定した信号は、
それぞれタンク２，４の断面積に相当する係数を
乗じて補正された後、加算される。加算された値
は、両循環タンク２，４に保有されている吸収剤
スラリーの総和となるので、この値が一定となる
ように補給水流量が制御される。各循環タンク
２，４の液面レベル制御は、前記のように連絡配
管３８を設けたので、両方向形の液面制御系と同
価となり、吸収液スラリーは液面レベルの高い方
から低い方へ流れることになる。このようにし
て、補給水が両タンク２，４の保有スラリーの合
計が常に一定になるように供給され、制御系が単
純化されるとともに、片側のタンクの液面レベル
が異常に増減することを防止し、常に安定した運
転制御が可能となる。 In the makeup water flow rate control system described above, the signals obtained by measuring the liquid level in each of the circulation tanks 2 and 4 are as follows:
After being corrected by multiplying each by a coefficient corresponding to the cross-sectional area of the tanks 2 and 4, they are added. Since the added value is the total sum of the absorbent slurry held in both circulation tanks 2 and 4, the makeup water flow rate is controlled so that this value remains constant. Since the liquid level control of each circulation tank 2, 4 is provided with the connecting pipe 38 as described above, it is equivalent to a bidirectional type liquid level control system, and the absorption liquid slurry is distributed from the higher liquid level to the lower liquid level. It will flow to In this way, make-up water is supplied so that the total slurry held in both tanks 2 and 4 is always constant, the control system is simplified, and the liquid level in one tank is prevented from increasing or decreasing abnormally. This enables stable operation control at all times.
脱硫による生成物（CaSO4等）の取り出しは、
第１図の従来例と同様なので説明は省略する。
尚、関数発生器５７は第１図の流量制御装置２５
に対応する制御器３７から信号を受けるように形
成されている。すなわち、吸収剤の供給量を制御
する信号により吸収剤スラリーの前記取り出し量
を設定するようになつている。 The removal of products (CaSO 4 etc.) from desulfurization is
Since it is similar to the conventional example shown in FIG. 1, the explanation will be omitted.
Note that the function generator 57 is the same as the flow rate control device 25 in FIG.
The controller 37 is configured to receive a signal from a controller 37 corresponding to the controller 37 . That is, the amount of absorbent slurry taken out is set by a signal that controls the amount of absorbent supplied.
第３図は、第１図の従来装置および第２図の本
発明装置を用いて排ガスの脱硫実験を行つた結果
を示す。図中、５０（破線）は本発明装置、５１
（実線）は従来装置を用いた場合のそれぞれの排
ガス流量に対する脱硫効率を示したものである。
排ガス流量は基準値の百分率で示した。図から明
らかなように、本発明装置は、排ガス流量によら
ずに安定した高い脱硫効率（約90％以上）を得る
ことができる。 FIG. 3 shows the results of an exhaust gas desulfurization experiment using the conventional apparatus shown in FIG. 1 and the apparatus of the present invention shown in FIG. 2. In the figure, 50 (broken line) is the device of the present invention, 51
(Solid line) shows the desulfurization efficiency for each exhaust gas flow rate when using the conventional device.
The exhaust gas flow rate was expressed as a percentage of the standard value. As is clear from the figure, the apparatus of the present invention can obtain stable and high desulfurization efficiency (approximately 90% or more) regardless of the exhaust gas flow rate.
次に第４図は、同様に第１図の従来装置および
第２図の本発明装置を用いて脱硫実験を行つた場
合の特性値の経時変化を示すものである。図中、
実線は本発明装置の場合、破線は従来装置の場合
で、５２は脱硫効率、５３は排ガス流量、５４は
吸収液のPH測定値、５５は吸収剤スラリー流量の
それぞれの経時変化（基準値に対する増減値）を
示す。 Next, FIG. 4 similarly shows changes over time in characteristic values when desulfurization experiments were conducted using the conventional apparatus shown in FIG. 1 and the apparatus of the present invention shown in FIG. 2. In the figure,
The solid line is for the device of the present invention, the broken line is for the conventional device, 52 is the desulfurization efficiency, 53 is the exhaust gas flow rate, 54 is the measured pH value of the absorbent, and 55 is the change over time in the absorbent slurry flow rate (relative to the reference value). increase/decrease value).
第４図から明らかなように、本発明装置では、
排ガス流量の変動によつて脱硫効率、吸収液のPH
はほとんど変化せず、長時間にわたつて安定した
運転制御を行なうことができる。 As is clear from FIG. 4, in the device of the present invention,
Desulfurization efficiency and absorption liquid PH vary depending on flue gas flow rate fluctuations.
There is almost no change in the current, and stable operation control can be performed over a long period of time.
具体的数値により脱硫処理の一例を説明する。
ライン５から冷却塔１へ導入される排ガスの流量
が2000×103Nm3／時、SO2濃度が500ppmのと
き、吸収剤である石灰石スラリーは濃度20重量％
のもので、供給量18ton／時で吸収塔循環タンク
４に送られる。冷却塔１への冷却液の循環量は
4000ton／時、吸収塔３への吸収液の循環量は
15000ton／時である。この状態での分岐ライン５
６からの吸収剤スラリーの抜き出し量は70ton／
時である。この抜き出し量に応じて補給水が冷却
塔循環タンク２内に補給される。 An example of desulfurization treatment will be explained using specific numerical values.
When the flow rate of exhaust gas introduced from line 5 to cooling tower 1 is 2000×10 3 Nm 3 /hour and the SO 2 concentration is 500 ppm, the concentration of limestone slurry as an absorbent is 20% by weight.
It is sent to the absorption tower circulation tank 4 at a feed rate of 18 tons/hour. The amount of circulation of cooling liquid to cooling tower 1 is
4000ton/hour, the circulation amount of absorption liquid to absorption tower 3 is
15000ton/hour. Branch line 5 in this state
The amount of absorbent slurry extracted from 6 is 70 tons/
It's time. Makeup water is replenished into the cooling tower circulation tank 2 in accordance with the amount of this withdrawal.
本発明によれば、吸収塔循環タンクから吸収塔
へ循環させる吸収液の循環流量を一定とし、冷却
塔循環タンクと吸収塔循環タンクとを連絡配管で
連通させ、冷却塔および吸収塔の各循環タンクの
液面レベルの変動を検出して当該各循環タンクの
液量が一定になるように補給水を供給する制御系
統と、冷却塔に供給される排ガスの物理量を検出
して該排ガス中のイオウ酸化物の反応当量以上の
吸収剤が供給されるように前記吸収剤スラリーの
供給量を調節する制御系統とを設けたので以下の
効果を有する。
According to the present invention, the circulation flow rate of the absorption liquid circulated from the absorption tower circulation tank to the absorption tower is kept constant, the cooling tower circulation tank and the absorption tower circulation tank are communicated with each other through a connecting pipe, and each circulation of the cooling tower and absorption tower is A control system that detects changes in the liquid level in tanks and supplies make-up water so that the liquid level in each circulation tank becomes constant, and a control system that detects the physical amount of exhaust gas supplied to the cooling tower and controls the amount of water in the exhaust gas. Since a control system is provided to adjust the supply amount of the absorbent slurry so that an amount of absorbent equal to or more than the reaction equivalent of sulfur oxide is supplied, the following effects can be obtained.
(1) 冷却塔循環タンク内の水分蒸発に伴なう液量
減少分の補給を、冷却塔循環タンク及び吸収塔
循環タンク内の両液量を直接的に検出して補給
する構成であるため、前記蒸発減少の補給を確
実かつ安定して行なうことができる。(1) The system is configured to directly detect the amount of liquid in both the cooling tower circulation tank and the absorption tower circulation tank to replenish the amount of liquid that has decreased due to water evaporation in the cooling tower circulation tank. , it is possible to reliably and stably replenish the evaporation loss.
(2) 吸収塔循環タンクへの吸収剤の捕給を排ガス
の物理量（排ガス流量、イオウ酸化物濃度）を
検出して行なう構成であるため、排ガスの流量
変動、濃度変化等に対して応答性が優れ、安定
した脱硫性能を有する排煙脱硫装置を得ること
ができる。(2) The structure captures the absorbent into the absorption tower circulation tank by detecting the physical quantities of the exhaust gas (exhaust gas flow rate, sulfur oxide concentration), so it is responsive to fluctuations in the exhaust gas flow rate, concentration changes, etc. It is possible to obtain a flue gas desulfurization device having excellent and stable desulfurization performance.
(3) 冷却塔循環タンクと吸収塔循環タンクの両液
面レベルは連絡配管により共通となるため、補
給水が両タンクの保有スラリーの合計が常に一
定になるように供給され、制御系が単純化され
るとともに、片側のタンクの液面レベルが異常
に増減することを防止し、常に安定した運転制
御が可能となる。(3) Since the liquid level in both the cooling tower circulation tank and the absorption tower circulation tank is shared by the connecting piping, make-up water is supplied so that the total slurry held in both tanks is always constant, simplifying the control system. This also prevents the liquid level in one tank from increasing or decreasing abnormally, making stable operation control possible at all times.
第１図は、従来の湿式排煙脱硫装置の系統図、
第２図は、本発明の実施例を示す排煙脱硫装置の
系統図、第３図および第４図は、それぞれ本発明
装置の脱硫性能および経時的安定性の一例を示す
特性図である。
１……冷却塔、２……冷却塔循環タンク、３…
…吸収塔、４……吸収塔循環タンク、３２……計
算器、３５……吸収剤スラリー流量制御弁、３６
……吸収剤スラリー流量計、３７……制御器、３
８……連絡配管、３９，４０……液面レベル伝送
器、４３……加算器、４４……液面レベル制御
器。
Figure 1 is a system diagram of a conventional wet flue gas desulfurization equipment.
FIG. 2 is a system diagram of a flue gas desulfurization device showing an embodiment of the present invention, and FIGS. 3 and 4 are characteristic diagrams showing an example of the desulfurization performance and stability over time of the device of the present invention, respectively. 1...Cooling tower, 2...Cooling tower circulation tank, 3...
... Absorption tower, 4 ... Absorption tower circulation tank, 32 ... Calculator, 35 ... Absorbent slurry flow rate control valve, 36
...Absorbent slurry flowmeter, 37 ...Controller, 3
8... Connection piping, 39, 40... Liquid level transmitter, 43... Adder, 44... Liquid level controller.
Claims (1)
一部のイオウ酸化物を吸収除去する冷却塔と、前
記冷却塔に冷却液を循環させるラインを備えた冷
却塔循環タンクと、該冷却塔循環タンクに補給水
を供給するラインと、前記冷却塔を出た前記排ガ
スをイオウ酸化物の吸収液と接触反応させて該イ
オウ酸化物を除去する吸収塔と、吸収剤スラリー
の供給ラインおよび前記吸収塔へ吸収液を循環さ
せるラインを有する吸収塔循環タンクとを備えた
排煙脱硫装置において、前記吸収塔循環タンクか
ら吸収塔へ循環させる吸収液の循環流量を一定と
し、冷却塔循環タンクと吸収塔循環タンクとを連
絡配管で連通させ、前記冷却塔および吸収塔の各
循環タンクの液面レベルの変動を検出して当該各
循環タンクの液量が一定になるように補給水を供
給する制御系統と、冷却塔に供給される排ガスの
物理量を検出して該排ガス中のイオウ酸化物の反
応当量以上の吸収剤が供給されるように前記吸収
剤スラリーの供給量を調節する制御系統とを設け
たことを特徴とする湿式排煙脱硫装置。1. A cooling tower that cools sulfur oxide-containing exhaust gas and absorbs and removes some of the sulfur oxides, a cooling tower circulation tank equipped with a line that circulates cooling fluid in the cooling tower, and replenishing the cooling tower circulation tank. a line for supplying water; an absorption tower for removing the sulfur oxides by contacting the exhaust gas exiting the cooling tower with a sulfur oxide absorption liquid; a supply line for absorbent slurry and absorption into the absorption tower; In a flue gas desulfurization apparatus equipped with an absorption tower circulation tank having a line for circulating liquid, the circulating flow rate of the absorption liquid circulated from the absorption tower circulation tank to the absorption tower is constant, and the cooling tower circulation tank and the absorption tower circulation tank are provided with a cooling tower circulation tank and an absorption tower circulation tank. a control system that communicates with the cooling tower and the absorption tower through a connecting pipe, detects fluctuations in the liquid level of each circulation tank of the cooling tower and the absorption tower, and supplies make-up water so that the liquid amount in each circulation tank is constant; and a control system that detects the physical amount of exhaust gas supplied to the cooling tower and adjusts the supply amount of the absorbent slurry so that an amount of absorbent equal to or more than the reaction equivalent of sulfur oxide in the exhaust gas is supplied. A wet flue gas desulfurization equipment featuring:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9481478A JPS5520681A (en) | 1978-08-02 | 1978-08-02 | Wet type exhaust gas desulfurization apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9481478A JPS5520681A (en) | 1978-08-02 | 1978-08-02 | Wet type exhaust gas desulfurization apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5520681A JPS5520681A (en) | 1980-02-14 |
| JPS637812B2 true JPS637812B2 (en) | 1988-02-18 |
Family
ID=14120514
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP9481478A Granted JPS5520681A (en) | 1978-08-02 | 1978-08-02 | Wet type exhaust gas desulfurization apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5520681A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59160518U (en) * | 1983-04-13 | 1984-10-27 | モリト株式会社 | gloves |
| JP2002361040A (en) * | 2001-06-12 | 2002-12-17 | Takuma Co Ltd | Control method of waste gas treatment and its control mechanism |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5161040A (en) * | 1974-11-25 | 1976-05-27 | Hitachi Ltd | BOIRAHAIENDATSURYUSEIGYOSOCHI |
| JPS5230783A (en) * | 1975-09-05 | 1977-03-08 | Mitsubishi Heavy Ind Ltd | Wet desulfurization process of exhaust gas |
-
1978
- 1978-08-02 JP JP9481478A patent/JPS5520681A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5161040A (en) * | 1974-11-25 | 1976-05-27 | Hitachi Ltd | BOIRAHAIENDATSURYUSEIGYOSOCHI |
| JPS5230783A (en) * | 1975-09-05 | 1977-03-08 | Mitsubishi Heavy Ind Ltd | Wet desulfurization process of exhaust gas |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5520681A (en) | 1980-02-14 |
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