JPS63294928A - Device for controlling wet exhaust gas desulfurizer - Google Patents
Device for controlling wet exhaust gas desulfurizerInfo
- Publication number
- JPS63294928A JPS63294928A JP62127018A JP12701887A JPS63294928A JP S63294928 A JPS63294928 A JP S63294928A JP 62127018 A JP62127018 A JP 62127018A JP 12701887 A JP12701887 A JP 12701887A JP S63294928 A JPS63294928 A JP S63294928A
- Authority
- JP
- Japan
- Prior art keywords
- liq
- absorbent
- absorption
- slurry
- absorption liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000010521 absorption reaction Methods 0.000 claims abstract description 103
- 239000002002 slurry Substances 0.000 claims abstract description 92
- 239000000428 dust Substances 0.000 claims abstract description 51
- 230000002745 absorbent Effects 0.000 claims abstract description 35
- 239000002250 absorbent Substances 0.000 claims abstract description 35
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 21
- 230000023556 desulfurization Effects 0.000 claims abstract description 21
- 239000007788 liquid Substances 0.000 claims description 69
- 239000007789 gas Substances 0.000 claims description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 239000003546 flue gas Substances 0.000 claims description 7
- 239000000779 smoke Substances 0.000 claims 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims 1
- 229910052815 sulfur oxide Inorganic materials 0.000 claims 1
- 230000003647 oxidation Effects 0.000 abstract description 16
- 238000007254 oxidation reaction Methods 0.000 abstract description 16
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 6
- 235000019738 Limestone Nutrition 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000006028 limestone Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000007423 decrease Effects 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 239000010440 gypsum Substances 0.000 description 2
- 229910052602 gypsum Inorganic materials 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 239000011575 calcium Substances 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 235000010216 calcium carbonate Nutrition 0.000 description 1
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 1
- 235000010261 calcium sulphite Nutrition 0.000 description 1
- 230000008094 contradictory effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
Description
【発明の詳細な説明】
（１）産業上の利用分野
本発明は湿式排煙脱硫装置に係り、特に負荷変動に対応
して吸収液スラリを供給することができる湿式排煙脱硫
装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION (1) Industrial Application Field The present invention relates to a wet flue gas desulfurization system, and particularly relates to a wet flue gas desulfurization system that can supply absorbent slurry in response to load fluctuations. be.
（２）従来の技術
従来の湿式排煙脱硫装置の吸収液スラリの供給は第５図
において吸収液スラリタンク１４から吸収液スラリポン
プ１５、吸収液スラリ供給配管１６により吸収部循環タ
ンク１９へ吸収液スラリを供給し、一方吸収部循環タン
ク１９内のスラリの一部を吸収部循環ポンプ１７で抜出
し、吸収部５に供給し、排ガスと気液接触させながら吸
収部（塔）５内を落下し、コレクタ４で捕集し下降管４
９を通って吸収部循環タンク１９に戻し循環させること
によって行われる。また吸収液スラリの一部は吸収部循
環タンク１９への吸収液スラリ供給量に見合って導管１
８に依り、除塵部循環タンク９に抜出される。また除塵
部循環タンク９には空気供給配管１０を設置し、空気を
吸い込むことに依り、亜硫酸塩を酸化し石膏１３とする
。(2) Prior Art Absorbent slurry in a conventional wet flue gas desulfurization system is supplied from an absorbent slurry tank 14 to an absorbent circulation tank 19 through an absorbent slurry pump 15 and an absorbent slurry supply pipe 16 in FIG. A liquid slurry is supplied, and on the other hand, a part of the slurry in the absorption section circulation tank 19 is extracted by the absorption section circulation pump 17, supplied to the absorption section 5, and dropped inside the absorption section (tower) 5 while bringing it into gas-liquid contact with the exhaust gas. is collected by the collector 4 and sent to the downcomer pipe 4.
9 and returns to the absorption section circulation tank 19 for circulation. In addition, a portion of the absorption liquid slurry is transferred to the conduit 1 according to the amount of absorption liquid slurry supplied to the absorption section circulation tank 19.
8, it is extracted to the dust removal section circulation tank 9. Further, an air supply pipe 10 is installed in the dust removal section circulation tank 9, and sulfite is oxidized to gypsum 13 by sucking in air.
しかし除塵部循環タンク９に空気を吸い込み酸化させる
工程において高い酸化率を得るためには、除塵部循環タ
ンク９内のスラリ液をある所定のＰＨに維持する必要が
あるが、第５図の従来のものにおいては吸収液スラリの
供給は、吸収部循環タンク１９、導管１８、除塵部循環
タンク９へと供給されるために時間遅れがあり、吸収部
５で既にＳｏｘと反応しているためにＰＨが下がり、反
応性に乏しくボイラ負荷変化特等脱硫装置入口のＳＯに
濃度が変化した際、除塵部循環タンク９内のスラリ液Ｏ
ＰＨ値が変動し、酸化率も不安定なものとなる。すなわ
ち、安定した高い酸化率を得る運転方法については配慮
されていなかった。However, in order to obtain a high oxidation rate in the step of sucking air into the dust removal section circulation tank 9 and oxidizing it, it is necessary to maintain the slurry liquid in the dust removal section circulation tank 9 at a certain pH. In this case, there is a time delay in supplying the absorption liquid slurry to the absorption section circulation tank 19, the conduit 18, and the dust removing section circulation tank 9, and because it has already reacted with Sox in the absorption section 5. When the pH decreases and the concentration of SO at the inlet of the desulfurization equipment changes due to poor reactivity and boiler load changes, the slurry liquid O in the dust removal section circulation tank 9 changes.
The pH value fluctuates and the oxidation rate becomes unstable. That is, no consideration was given to an operating method for obtaining a stable and high oxidation rate.
尚、１は脱硫ファン、２は煙道、３は除塵部、１１は遠
心分離機、１２はシラフナである。In addition, 1 is a desulfurization fan, 2 is a flue, 3 is a dust removal part, 11 is a centrifugal separator, and 12 is Shirafuna.
（３）発明が解決しようとする問題点
上記従来技術はボイラ負荷変動時の脱硫装置人口Ｓ Ｏ
ｘ濃度変化による酸化率への影響が配慮されておらず、
安定した高い酸化性能が得られないという問題があった
。(3) Problems to be solved by the invention The above-mentioned conventional technology is designed to solve the problem of desulfurization equipment population S O during boiler load fluctuations.
The effect of changes in x concentration on the oxidation rate is not taken into account,
There was a problem that stable and high oxidation performance could not be obtained.
本発明の目的は吸収部循環タンク及び除塵部循環タンク
ヘフレツシュな吸収液スラリを供給し、ボイラ側の負荷
が変動しても高い酸化率と脱硫率を得ることの出来る制
御装置を提供することにある。An object of the present invention is to provide a control device that supplies fresh absorption liquid slurry to an absorption section circulation tank and a dust removal section circulation tank, and can obtain a high oxidation rate and desulfurization rate even if the load on the boiler side changes. There is a particular thing.
（４）問題点を解決するための手段
上記目的は、除塵部循環タンク９ヘフレッシュな吸収液
スラリを供給する吸収液スラリ副供給管２０、及びこの
吸収液スラリの供給量を制御するための除塵部吸収液ス
ラリ流量調節弁３３、除塵部吸収液スラリ流量検出器３
０と、吸収部循環タンク１９へ吸収液スラリを供給する
ための吸収部吸収液スラリ流量調節弁４８、吸収部吸収
液スラリ流量検出器４５を設けることにより、達成され
る。(4) Means for solving the problem The above purpose is to provide an absorption liquid slurry sub-supply pipe 20 for supplying fresh absorption liquid slurry to the dust removal section circulation tank 9, and a system for controlling the supply amount of this absorption liquid slurry. Dust removing section absorption liquid slurry flow rate control valve 33, dust removal section absorption liquid slurry flow rate detector 3
This is achieved by providing an absorbent absorbent slurry flow rate control valve 48 for supplying the absorbent slurry to the absorbent circulation tank 19 and an absorbent absorbent slurry flow rate detector 45.
（５）作用
吸収液スラリ副供給管２０及び除塵部吸収液スラリ流量
検出器３０、除塵部吸収液スラリ流量調節弁３３により
吸収液スラリタンク１４からのフレッシュな吸収液を除
塵部循環タンク９に供給する。それによって除塵部循環
タンク９内の吸収液のＰＨは安定し酸化率が低下するこ
とは無い。また除塵部循環タンク９とは別に吸収部循環
タンク１９への吸収液スラリは吸収部吸収液スラリ流量
調節弁４８、吸収部吸収液スラリ流量検出器４５によっ
て供給量が制御されるので所定の脱硫率を維持すること
が出来る。(5) Effect Fresh absorption liquid from the absorption liquid slurry tank 14 is transferred to the dust removal part circulation tank 9 by the absorption liquid slurry sub-supply pipe 20, the dust removal part absorption liquid slurry flow rate detector 30, and the dust removal part absorption liquid slurry flow rate adjustment valve 33. supply As a result, the pH of the absorption liquid in the dust removal section circulation tank 9 is stabilized, and the oxidation rate does not decrease. In addition to the dust removal section circulation tank 9, the supply amount of the absorption liquid slurry to the absorption section circulation tank 19 is controlled by an absorption section absorption liquid slurry flow rate control valve 48 and an absorption section absorption liquid slurry flow rate detector 45, so that the predetermined desulfurization is carried out. rate can be maintained.
（６）発明の実施例
第１図において、排ガスは脱硫ファン１１煙道２から除
塵部３へ導かれ、除塵、冷却及び一部脱硫された後、コ
レクタ４の間を通り吸収部５へ導かれる。ここで排ガス
中の亜硫酸ガスは吸収液スラリと気液接触し、ＳＯＸが
吸収除去され、更にデミスタ６により同伴ミストが除去
された後、脱硫塔（吸収部）５の出ロアから排出される
。(6) Embodiment of the invention In FIG. 1, exhaust gas is guided from the desulfurization fan 11 flue 2 to the dust removing section 3, where it is removed, cooled and partially desulfurized, and then passed between the collectors 4 and guided to the absorption section 5. It will be destroyed. Here, the sulfur dioxide gas in the exhaust gas comes into gas-liquid contact with the absorption liquid slurry, SOX is absorbed and removed, and entrained mist is further removed by the demister 6, after which it is discharged from the output lower of the desulfurization tower (absorption section) 5.
一方、吸収剤である吸収液スラリは吸収液スラリタンク
１４から吸収液スラリポンプ１５、吸収液スラリ供給配
管１６、吸収液スラリ副供給配管２０により吸収部循環
タンクＩ９、及び除塵部循環タンク９に独自に供給され
る。On the other hand, the absorption liquid slurry, which is an absorbent, is transferred from the absorption liquid slurry tank 14 to the absorption part circulation tank I9 and the dust removal part circulation tank 9 via the absorption liquid slurry pump 15, the absorption liquid slurry supply pipe 16, and the absorption liquid slurry sub-supply pipe 20. Uniquely supplied.
吸収部循環タンク１９内の吸収液スラリは、吸収部循環
ポンプ１７により吸収部５に供給され、排ガスと気液接
触しながら塔（吸収部）５内を落下し、コレクタ４で捕
集され、下降管４９を通って吸収部循環タンク１９に戻
され循環して使用する。また吸収液スラリの一部は吸収
部循環タンク１９への吸収液スラリ供給量に見合って導
管１８により、除塵部循環タンク９に抜出される。一方
除塵部循環タンク９には吸収液スラリ副供給配管２０に
よりフレッシュな吸収剤スラリか供給され、且つこの吸
収剤スラリが除塵部循環ポンプ８により除塵部３でスプ
レーされ排ガスと気液接触して、排ガスの冷却、除塵及
び一部脱硫が行われる。また除塵部循環タンク９には空
気配管１０を設置し、空気を吸い込むことにより、亜硫
酸塩を酸化し石膏１３とする。The absorption liquid slurry in the absorption section circulation tank 19 is supplied to the absorption section 5 by the absorption section circulation pump 17, falls through the tower (absorption section) 5 while in gas-liquid contact with the exhaust gas, and is collected by the collector 4. It is returned to the absorption section circulation tank 19 through the downcomer pipe 49 and is used for circulation. Further, a portion of the absorption liquid slurry is drawn out to the dust removal section circulation tank 9 through the conduit 18 in proportion to the amount of absorption liquid slurry supplied to the absorption section circulation tank 19. On the other hand, fresh absorbent slurry is supplied to the dust removal section circulation tank 9 by the absorption liquid slurry sub-supply pipe 20, and this absorbent slurry is sprayed in the dust removal section 3 by the dust removal section circulation pump 8 and comes into gas-liquid contact with the exhaust gas. , exhaust gas is cooled, dust removed, and partially desulfurized. Further, an air pipe 10 is installed in the dust removal section circulation tank 9, and by sucking air, sulfite is oxidized to gypsum 13.
尚、除塵部３における脱硫率とＰＨ，酸化率とＰＨの関
係を第３図、第４図を用いて説明する。The relationship between the desulfurization rate and PH and the oxidation rate and PH in the dust removal section 3 will be explained using FIGS. 3 and 4.
第３図、第４図に示す様に、除塵部循環タンク９内のＰ
Ｈと脱硫率、酸化率とＰＨの関係は相反するものである
ために、高い脱硫率、酸化率で運転するためには除塵部
３のＰＨを５．０〜５．５付近で運転することが必要に
なってくる。しかし除塵部循環タンク９内で空気供給配
管１０からの酸化用空気によって強制的に酸化を行うた
め除塵部循環タンク９内のスラリ中に亜硫酸カルシウム
は殆ど共存せず、ＰＨは不安定となる。また石灰石粒子
の表面を覆うブラインデインク現象が無いため石灰石の
反応性は向上し、スラリ中のＣａ ＣＯｓは殆ど亜硫酸
ガスに吸収される。その結果除塵部循環タンク９内のス
ラリ中にはＣａＣＯ３は殆ど無くなり、ＰＨは低下する
ことになる。しかし本発明では吸収部５とは別に冷却部
３ヘフレッシュな吸収液スラリを吸収液スラリ副供給管
２０から供給するため、ＰＨを５．０〜５．５付近に安
定させ高い酸化率を得ることが出来る。また吸収部循環
タンク１９へも吸収液スラリタンク１４からの吸収液ス
ラリを吸収部吸収液スラリ流量調節弁４日、吸収部吸収
液スラリ流量検出器４５で煙道２から入ってくる排ガス
中の総ＳＯ，ｌＮに見合った供給量に制御するため吸収
部５での所定の脱硫率を得ることが出来る。As shown in FIGS. 3 and 4, P inside the dust removal section circulation tank 9 is
Since the relationships between H, desulfurization rate, and oxidation rate and PH are contradictory, in order to operate at a high desulfurization rate and oxidation rate, the pH of the dust removal section 3 should be operated at around 5.0 to 5.5. becomes necessary. However, since oxidation is forcibly carried out in the dust removal section circulation tank 9 by the oxidizing air from the air supply pipe 10, almost no calcium sulfite coexists in the slurry in the dust removal section circulation tank 9, and the pH becomes unstable. Furthermore, since there is no blinding phenomenon covering the surface of limestone particles, the reactivity of limestone is improved, and most of the Ca COs in the slurry is absorbed by sulfur dioxide gas. As a result, there is almost no CaCO3 in the slurry in the dust removal section circulation tank 9, and the pH decreases. However, in the present invention, fresh absorption liquid slurry is supplied to the cooling unit 3 from the absorption liquid slurry sub-supply pipe 20 separately from the absorption unit 5, so that the pH is stabilized at around 5.0 to 5.5 and a high oxidation rate is obtained. I can do it. Also, the absorption liquid slurry from the absorption liquid slurry tank 14 is transferred to the absorption part circulation tank 19 by the absorption part absorption liquid slurry flow rate control valve 4, and the absorption part absorption liquid slurry flow rate detector 45 detects the absorption liquid slurry in the flue gas coming in from the flue 2. Since the supply amount is controlled to match the total SO and IN, a predetermined desulfurization rate in the absorption section 5 can be obtained.
次に本発明の制御系統を第２図について説明する。排ガ
ス流量検出器２１と入口Ｓ Ｏを濃度検出器２２からの
排ガス流量信号２３とＳＯ２濃度信号２４を乗算器２５
により乗算して、総ＳＯ，量信号２６を求め、この総Ｓ
Ｏ，量信号２６を関数発生器２７により総Ｓ Ｏを量信
号２６に対する除塵部吸収液スラリ流！調節計２８のＰ
Ｈ設定信号２９とし、除塵部吸収液スラリ流量検出器３
０からの吸収液スラリ流量検出信号３１と比較し、比例
積分動作させた後、電空変換器３２により空気信号に変
換し、吸収液スラリ副供給配管２０の除塵部吸収液スラ
リ流量調節弁３３を操作する０以上の回路により各負荷
で安定したＰＨが得られる様吸収液スラリか供給される
が、負荷変動等の外乱が入った場合、一時的にＰＨが変
動することを防ぐため除塵部循環タンクＰＨ検出器３４
からの実測信号を除塵部循環タンクｐＨｌｆｌ計３５で
の設定信号と比較し、比例積分動作させた後この信号を
補正信号３６として加算器３７で加算し、除塵部吸収液
スラリ供給流量の設定信号２９を修正する。つまり負荷
一定時等はＰＨの変動は殆ど無く安定しているため、加
算器３７への補正信号３６はゼロとなり、関数発生器２
７からの出力信号がそのままＰＨ設定信号２９となるが
、負荷変動時等には除塵部循環タンク９のＰＨが変動す
るため、加算器３７へ補正信号３６が入力され、ＰＨ設
定信号２９が修正される。Next, the control system of the present invention will be explained with reference to FIG. The exhaust gas flow rate detector 21 and the inlet SO are multiplied by the exhaust gas flow rate signal 23 from the concentration detector 22 and the SO2 concentration signal 24 in a multiplier 25.
The total SO, amount signal 26 is obtained by multiplying by
O, the amount signal 26 is converted to the total SO by the function generator 27, and the dust removal section absorption liquid slurry flow for the amount signal 26! Controller 28 P
The H setting signal is 29, and the dust removal section absorption liquid slurry flow rate detector 3
The absorption liquid slurry flow rate detection signal 31 is compared with the absorption liquid slurry flow rate detection signal 31 from 0, and after performing proportional integral operation, it is converted into an air signal by the electro-pneumatic converter 32, and the absorption liquid slurry flow rate adjustment valve 33 of the dust removal section of the absorption liquid slurry sub-supply piping 20 is Absorbing liquid slurry is supplied so that a stable pH can be obtained at each load by a circuit of 0 or more that operates the Circulation tank PH detector 34
The actual measurement signal from the dust removal section is compared with the setting signal of the pHlfl meter 35 in the circulation tank of the dust removal section, and after a proportional-integral operation is performed, this signal is added as a correction signal 36 in the adder 37, and the setting signal of the flow rate of the absorption liquid slurry supply to the dust removal section is obtained. Modify 29. In other words, when the load is constant, the PH is stable with almost no fluctuation, so the correction signal 36 to the adder 37 becomes zero, and the function generator 2
The output signal from 7 becomes the PH setting signal 29 as it is, but since the PH of the dust removal section circulation tank 9 fluctuates when the load fluctuates, the correction signal 36 is input to the adder 37, and the PH setting signal 29 is corrected. be done.
次に吸収部循環タンク１９への吸収液スラリ供給方法に
ついて説明する。先に述べた総ＳＯ１信号２６に対し関
数発生器３８で吸収部循環タンク１９のＰＨを設定し、
この設定信号と吸収部循環タンクＰＨ検出器４０の出力
信号との偏差を減算器４１で求め、関数発生器３９で設
定した総ＳＯ□信号に対する石灰石過剰率の設定過剰率
の設定値に対し先に求めた偏差を無くするための補正信
号とを加算器４３で加算することにより石灰石過剰率補
正信号とする。この補正信号と総Ｓｏｗ信号とを乗算器
４４で乗算することにより吸収部吸収液スラリ要求流量
を求め吸収部吸収液スラリ流量検出器４５での出力信号
と比較し、吸収部吸収液スラリ流量調節計４６で比例積
分動作させた後、電空変換器４７により空気信号に変換
し、吸収液スラリ供給配管１６の吸収部吸収液スラリ流
ＭＥＮ節弁４８を操作する。Next, a method of supplying the absorption liquid slurry to the absorption section circulation tank 19 will be explained. Set the pH of the absorption section circulation tank 19 with the function generator 38 for the total SO1 signal 26 mentioned above,
The deviation between this set signal and the output signal of the absorption section circulation tank PH detector 40 is obtained by the subtractor 41, and the limestone excess rate is calculated based on the set value of the excess rate of limestone with respect to the total SO□ signal set by the function generator 39. An adder 43 adds the correction signal for eliminating the deviation found in the above to obtain a limestone excess rate correction signal. By multiplying this correction signal and the total Sow signal by the multiplier 44, the required flow rate of the absorption liquid slurry in the absorption part is obtained and compared with the output signal from the absorption part absorption liquid slurry flow rate detector 45, and the flow rate of the absorption liquid slurry in the absorption part is adjusted. After the proportional integral operation is carried out in the total 46, the signal is converted into an air signal by the electro-pneumatic converter 47, and the absorption part absorption liquid slurry flow MEN control valve 48 of the absorption liquid slurry supply piping 16 is operated.
（８）発明の効果
本発明によれば吸収液スラリタンクから除塵部循環タン
クへ吸収液スラリを供給する吸収液スラリ副供給管を設
けたのでボイラが負荷変動を行っても除塵部のＰＨを安
定させることが出来、高い酸化率を得られる効果がある
。また吸収液スラリタンクから吸収部循環タンクへ供給
する吸収液スラリ供給量を制御できるのでボイラが負荷
変動を行っても所定の脱硫率を得られる効果がある。(8) Effects of the Invention According to the present invention, since an absorption liquid slurry sub-supply pipe is provided that supplies the absorption liquid slurry from the absorption liquid slurry tank to the dust removal section circulation tank, the pH of the dust removal section can be maintained even when the boiler load fluctuates. It can be stabilized and has the effect of obtaining a high oxidation rate. Furthermore, since the amount of absorption liquid slurry supplied from the absorption liquid slurry tank to the absorption section circulation tank can be controlled, there is an effect that a predetermined desulfurization rate can be obtained even if the load of the boiler changes.
第１図は本発明の実施例に係る湿式排煙脱硫装置の概略
系統図、第２図は第１図の制御系統図、第３図及び第４
図は除塵部における脱硫率とＰＨ１酸化率とＰＨの関係
を示す特性図、第５図は従来の湿式排煙脱硫装置の概略
系統図である。
第１図
第２図
第３図
ＰＨ（−）
第４図
−ＰＨ（−）
第５図FIG. 1 is a schematic system diagram of a wet flue gas desulfurization apparatus according to an embodiment of the present invention, FIG. 2 is a control system diagram of FIG. 1, and FIGS.
The figure is a characteristic diagram showing the relationship between the desulfurization rate, PH1 oxidation rate, and PH in the dust removal section, and FIG. 5 is a schematic system diagram of a conventional wet flue gas desulfurization apparatus. Figure 1 Figure 2 Figure 3 PH (-) Figure 4 - PH (-) Figure 5
Claims (1)
収液スラリを貯蔵する除塵部循環タンクと、排ガス中の
硫黄酸化物を吸収液スラリで吸収する吸収部と、この吸
収液スラリを貯蔵する吸収部循環タンクとを備え、吸収
液スラリタンクから吸収部循環タンクへ吸収液スラリを
供給する湿式排煙脱硫装置において、前記吸収液スラリ
タンクから除塵部循環タンクへ吸収液スラリを供給する
吸収液スラリ副供給配管を設け、この吸収液スラリ副供
給配管から除塵部循環タンクへ及び吸収液スラリタンク
から吸収部循環タンクへそれぞれ吸収液スラリを供給で
きる手段を設けたことを特徴とする湿式排煙脱硫装置の
制御装置。A dust removal section that cools and removes dust from exhaust gas using an absorbent slurry, a dust removal section circulation tank that stores this absorption liquid slurry, an absorption section that absorbs sulfur oxides in the exhaust gas with an absorption liquid slurry, and stores this absorption liquid slurry. In the wet flue gas desulfurization equipment which is equipped with an absorption part circulation tank and supplies the absorption liquid slurry from the absorption liquid slurry tank to the absorption part circulation tank, the absorption liquid which supplies the absorption liquid slurry from the absorption liquid slurry tank to the dust removal part circulation tank. A wet smoke exhaust system, characterized in that a slurry sub-supply pipe is provided, and a means is provided for supplying the absorbent slurry from the absorbent slurry sub-supply pipe to the dust removing section circulation tank and from the absorbent slurry tank to the absorption section circulation tank, respectively. Control device for desulfurization equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62127018A JPS63294928A (en) | 1987-05-26 | 1987-05-26 | Device for controlling wet exhaust gas desulfurizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62127018A JPS63294928A (en) | 1987-05-26 | 1987-05-26 | Device for controlling wet exhaust gas desulfurizer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63294928A true JPS63294928A (en) | 1988-12-01 |
Family
ID=14949650
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62127018A Pending JPS63294928A (en) | 1987-05-26 | 1987-05-26 | Device for controlling wet exhaust gas desulfurizer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63294928A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2018517561A (en) * | 2015-04-22 | 2018-07-05 | バルチラ モス アクティーゼルスカブＷａｒｔｓｉｌａ Ｍｏｓｓ ＡＳ | Inline scrubber with dual water system |
-
1987
- 1987-05-26 JP JP62127018A patent/JPS63294928A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2018517561A (en) * | 2015-04-22 | 2018-07-05 | バルチラ モス アクティーゼルスカブＷａｒｔｓｉｌａ Ｍｏｓｓ ＡＳ | Inline scrubber with dual water system |
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