JPS6244733Y2 - - Google Patents
Info
- Publication number
- JPS6244733Y2 JPS6244733Y2 JP5281082U JP5281082U JPS6244733Y2 JP S6244733 Y2 JPS6244733 Y2 JP S6244733Y2 JP 5281082 U JP5281082 U JP 5281082U JP 5281082 U JP5281082 U JP 5281082U JP S6244733 Y2 JPS6244733 Y2 JP S6244733Y2
- Authority
- JP
- Japan
- Prior art keywords
- desulfurization
- tower
- liquid level
- liquid
- oxidation 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
- 239000007788 liquid Substances 0.000 claims description 157
- 238000006477 desulfuration reaction Methods 0.000 claims description 124
- 230000023556 desulfurization Effects 0.000 claims description 124
- 230000003647 oxidation Effects 0.000 claims description 60
- 238000007254 oxidation reaction Methods 0.000 claims description 60
- 238000011282 treatment Methods 0.000 claims description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 16
- 239000003546 flue gas Substances 0.000 claims description 16
- 238000012545 processing Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 23
- 229910052602 gypsum Inorganic materials 0.000 description 15
- 239000010440 gypsum Substances 0.000 description 15
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 9
- 235000011941 Tilia x europaea Nutrition 0.000 description 9
- 239000004571 lime Substances 0.000 description 9
- 230000007423 decrease Effects 0.000 description 8
- 238000000034 method Methods 0.000 description 8
- 230000007246 mechanism Effects 0.000 description 7
- 239000003595 mist Substances 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 230000001590 oxidative effect Effects 0.000 description 5
- 238000005192 partition Methods 0.000 description 5
- 239000002002 slurry Substances 0.000 description 5
- 239000011575 calcium Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 3
- 230000003009 desulfurizing effect Effects 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 238000012805 post-processing Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- LVGQIQHJMRUCRM-UHFFFAOYSA-L calcium bisulfite Chemical compound [Ca+2].OS([O-])=O.OS([O-])=O LVGQIQHJMRUCRM-UHFFFAOYSA-L 0.000 description 1
- 235000010260 calcium hydrogen sulphite 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
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Description
【考案の詳細な説明】
本考案は湿式石灰法による排煙脱硫装置に関
し、特にその脱硫塔および酸化塔における液面制
御システムの改良に係る。[Detailed Description of the Invention] The present invention relates to a flue gas desulfurization device using a wet lime method, and particularly relates to an improvement of a liquid level control system in a desulfurization tower and an oxidation tower.
湿式石灰法による排煙脱硫法は、排ガスを石灰
スラリーと接触させることにより排ガス中に含ま
れる亜硫酸ガス（以下SO2ガスという）を主に亜
硫酸カルシウム（CaSO2・１／２H2O）として、また
一部は亜硫酸水素カルシウム（Ca（HSO3）2とし
て固定し、除去するものである。そして、生成し
たCaSO3・１／２H2OおよびCa（HSO3）2は安定な硫酸
塩（CaSO4）に酸化され、有用な副生物である石
膏として、回収されている。従つて、湿式石灰法
による排煙脱硫装置には上記SO2ガスの固定を行
なう脱硫塔と、CaSO3・１／２H2O等を酸化するため
の酸化塔と、石膏を分離回収するための後処理装
置が含まれている。 The flue gas desulfurization method using the wet lime method converts the sulfur dioxide gas (hereinafter referred to as SO 2 gas) contained in the flue gas into mainly calcium sulfite (CaSO 2 1/2H 2 O) by bringing the flue gas into contact with lime slurry. A part of it is fixed as calcium bisulfite (Ca(HSO 3 ) 2 ) and removed.The generated CaSO 3 1/2H 2 O and Ca(HSO 3 ) 2 are converted into stable sulfate (CaSO 3 ) 2 . 4 ) and is recovered as gypsum, which is a useful by-product.Therefore, the flue gas desulfurization equipment using the wet lime method includes a desulfurization tower that fixes the above-mentioned SO 2 gas, and CaSO 3.1 / It includes an oxidation tower for oxidizing 2H 2 O, etc., and a post-treatment device for separating and recovering gypsum.
第１図は、従来の湿式石灰法による排煙脱硫装
置を示すフローチヤートである。同図において、
１は脱硫塔、２は酸化塔、３は後処理装置であ
る。脱硫塔１の底部には排ガス中のSO2ガスを吸
収固定する脱硫液が貯溜される脱硫液溜４が形成
されている。該脱硫液溜４に貯溜された脱硫液は
ポンプ５により抜き出され、ライン６および図示
しないその分岐ラインを通つて脱硫塔１の頂部か
ら脱硫塔内部にスプレーされる。スプレーされた
脱硫液は入口ダクト７から脱硫塔１に導入した排
ガスと向流接触し、排ガス中に含まれるSO2ガス
を吸収固定して脱硫液溜４に帰還する。従つて、
脱硫液溜４に貯溜されている脱硫液には石灰
（CaCO3）の他にCaSO3・１／２H2OおよびCa
（HSO3）2が含まれている。 FIG. 1 is a flowchart showing a conventional wet lime method flue gas desulfurization device. In the same figure,
1 is a desulfurization tower, 2 is an oxidation tower, and 3 is a post-treatment device. A desulfurization liquid reservoir 4 is formed at the bottom of the desulfurization tower 1 in which a desulfurization liquid for absorbing and fixing SO 2 gas in the exhaust gas is stored. The desulfurization liquid stored in the desulfurization liquid reservoir 4 is extracted by a pump 5 and sprayed from the top of the desulfurization tower 1 into the inside of the desulfurization tower through a line 6 and its branch line (not shown). The sprayed desulfurization liquid comes into countercurrent contact with the exhaust gas introduced into the desulfurization tower 1 from the inlet duct 7, absorbs and fixes SO 2 gas contained in the exhaust gas, and returns to the desulfurization liquid reservoir 4. Therefore,
The desulfurization liquid stored in the desulfurization liquid reservoir 4 contains CaSO 3 1/2H 2 O and Ca (HSO 3 ) 2 in addition to lime (CaCO 3 ).
他方、SO2ガスを除去された排ガスは出口ダク
トに設けられたミストセパレータ８でミストを分
離された後、系外に放出される。そして、ミスト
セパレータ８で分離されたミストはミストドレン
管９を通つて脱硫液溜４に帰還する。また、脱硫
液溜４に貯溜されている脱硫液を撹拌して脱硫液
からスラリーが分離沈降するのを防止するために
撹拌機１０が設けられている。この撹拌機１０の
設置部分は通常密閉されず、脱硫塔１はこの部分
を通して開方系になつている。このため、、排ガ
スがこの部分から系外に放出されるのを防止する
ために仕切板１１によるガスシール構造が採用さ
れている。即ち、仕切板１１は脱硫塔１内部の上
部空間を撹拌器１０設置側と排ガス入口側として
分割するように設置され、しかもその下端部が脱
硫液中に浸漬されるように設置されている。従つ
て、導入された排ガスは仕切板１１および脱硫液
にシールされ、撹拌器１０側の液室１２への漏れ
が防止される。脱硫塔１には石灰液供給ライン１
３から新しい石灰液が供給される一方、SO2ガス
の吸収で生成されたCaSO3・１／２H2Oを含む脱硫液
はポンプ５により抜き取られ、ライン７および流
量調節弁１４を経て酸化塔２の頂部へ導入され
る。これとは別に酸化塔２には硫酸（H2SO4）が
供給されると共に空気の吹込みが行なわれ、導入
された脱硫液中に含まれるCaSO3・１／２H2O，Ca
（HSO3）2および未反応のCaCO3はH2SO4および酸
素の作用によりCaSO4に酸化される。こうして生
成したCaSO4を含むスラリー（以下石膏液とい
う）は酸化塔２の底部からライン１５により抜き
取られ、流量調節弁１６を経て後処理装置３に導
入される。後処理装置３では石膏液からの石膏の
分離回収が行なわれる。なお、酸化塔２から抜き
取られた石膏液の一部はライン１７により分岐さ
れ、脱硫塔１内でスケールが生成するのを防止す
るための種晶として脱硫塔１に再循環される。こ
の再循環量はライン１７に設けられた流量調節弁
１８およびその開度を調節する流量調節計１９に
よつて制御されている。 On the other hand, the exhaust gas from which the SO 2 gas has been removed is discharged to the outside of the system after the mist is separated by a mist separator 8 provided in the outlet duct. The mist separated by the mist separator 8 returns to the desulfurization reservoir 4 through the mist drain pipe 9. Further, a stirrer 10 is provided to stir the desulfurization liquid stored in the desulfurization liquid reservoir 4 and to prevent the slurry from separating and settling from the desulfurization liquid. The part where the stirrer 10 is installed is usually not sealed, and the desulfurization tower 1 is an open system through this part. For this reason, a gas seal structure using the partition plate 11 is adopted to prevent the exhaust gas from being released from this part to the outside of the system. That is, the partition plate 11 is installed so as to divide the upper space inside the desulfurization tower 1 into the agitator 10 installation side and the exhaust gas inlet side, and is installed so that its lower end is immersed in the desulfurization liquid. Therefore, the introduced exhaust gas is sealed by the partition plate 11 and the desulfurization liquid, and leakage to the liquid chamber 12 on the stirrer 10 side is prevented. The desulfurization tower 1 has a lime liquid supply line 1
Fresh lime liquid is supplied from 3, while the desulfurization liquid containing CaSO 3 1/2 H 2 O generated by absorption of SO 2 gas is extracted by pump 5 and sent to the oxidation tower via line 7 and flow control valve 14. Introduced to the top of 2. Separately, sulfuric acid (H 2 SO 4 ) is supplied to the oxidation tower 2, and air is blown into the oxidation tower 2. CaSO 3 1/2H 2 O, Ca (HSO 3 ) 2 and unreacted CaCO 3 are oxidized to CaSO 4 by the action of H 2 SO 4 and oxygen. The slurry containing CaSO 4 thus generated (hereinafter referred to as gypsum liquid) is extracted from the bottom of the oxidation tower 2 through a line 15 and introduced into the aftertreatment device 3 via a flow rate control valve 16 . In the post-processing device 3, gypsum is separated and recovered from the gypsum solution. A portion of the gypsum liquid extracted from the oxidation tower 2 is branched off through a line 17 and recycled to the desulfurization tower 1 as seed crystals to prevent scale from forming within the desulfurization tower 1. The amount of recirculation is controlled by a flow rate control valve 18 provided in the line 17 and a flow rate control meter 19 that adjusts its opening degree.
ところで、上記のような排煙脱硫装置では脱硫
装置１、酸化塔２および後処理装置３での反応お
よび処理が所定の良好な状態で行なわれるように
前記脱硫液および石膏液の抜取り量を制御しなけ
ればならず、この制御は脱硫塔１における脱硫液
の液面高さおよび酸化塔２における石膏液の液面
高さに基づき、両者の液面が所定のレベルに維持
されるように行なわれている。そして、脱硫塔１
における脱硫液溜４の容積は一般に酸化塔２の容
積よりも大容量で液面レベルの変動がゆるやかで
あることから、この制御には脱硫塔１の液面レベ
ル制御を主体とした制御システムが従来採用され
ている。これを第１図の例について説明すれば次
の通りである。まず、脱硫塔１の液面レベル制御
は液室１２の側壁に設けられた液面検出計２０
と、該液面検出計２０からの信号に従つて液室１
２内の液レベルが所定の高さになるように流量調
節弁１４の開度を制御する脱硫塔液レベル調節計
２１によつて制御されている。また、酸化塔２の
液レベルは酸化塔、側壁に設けられた液面検出計
２２と、該液面検出計２２からの信号に従つて酸
化塔２の液レベルが所定の高さになるように流量
調節弁１６の開度を制御する酸化塔液レベル調節
計２３によつて制御されている。即ち、両者とも
夫々独立した自己制御ループでの制御が行なわれ
ており、上流側にある脱硫塔１の液面レベル変動
が小さければこの制御システムで安定な運転が可
能である。 By the way, in the flue gas desulfurization apparatus as described above, the amount of the desulfurization liquid and the gypsum liquid to be extracted is controlled so that the reactions and treatments in the desulfurization apparatus 1, oxidation tower 2, and post-treatment apparatus 3 are carried out in a predetermined good condition. This control is based on the liquid level of the desulfurizing liquid in the desulfurizing tower 1 and the liquid level of the gypsum liquid in the oxidizing tower 2, and is performed so that both liquid levels are maintained at a predetermined level. It is. And desulfurization tower 1
Since the volume of the desulfurization liquid reservoir 4 is generally larger than the volume of the oxidation tower 2 and the liquid level fluctuates more slowly, this control requires a control system that mainly controls the liquid level of the desulfurization tower 1. Traditionally used. This will be explained with reference to the example shown in FIG. 1 as follows. First, the liquid level of the desulfurization tower 1 is controlled by a liquid level detector 20 installed on the side wall of the liquid chamber 12.
and the liquid chamber 1 according to the signal from the liquid level detector 20.
It is controlled by a desulfurization tower liquid level controller 21 that controls the opening degree of the flow rate control valve 14 so that the liquid level in the desulfurization tower 2 reaches a predetermined height. The liquid level in the oxidation tower 2 is determined by a liquid level detector 22 installed on the side wall of the oxidation tower and a signal from the liquid level detector 22 so that the liquid level in the oxidation tower 2 reaches a predetermined level. It is controlled by an oxidation tower liquid level controller 23 which controls the opening degree of the flow rate control valve 16. That is, both of them are controlled by independent self-control loops, and if fluctuations in the liquid level of the upstream desulfurization tower 1 are small, stable operation is possible with this control system.
ところが、実際には脱硫塔１における前述のガ
スシール構造により液室１２の液面レベルは排ガ
ス流量に従つて頻繁に変動する。即ち、排ガス流
量が変化すると脱硫塔１内のガスシールされた空
間および液室１２内の空間の間に内圧差が生じ、
従つて仕切板１１の両側でのこの内圧差に相当す
る液面レベル差が生じるから、液室１２内の液面
レベルは入口ダクト７から導入される排ガスの圧
力に追従して変動することになる。そして、排ガ
ス圧力が低下して液室１２内の液レベルが低下し
た場合、脱硫塔液レベル調節計２１は流量調節弁
１４の開度を絞つて酸化塔２へ送給される脱硫液
の量を減少させる。これに対して、酸化塔２でも
前記の液面レベル制御機構２２，２３，１６によ
る制御が働きはするが、この制御とは無関係にラ
イン１７からは常に一定量の石膏スラリーが種晶
として脱硫塔１へ再循環される。従つて、このと
き酸化塔２の液面レベルは低下する。しかも酸化
塔２の容積が脱硫塔液溜４の容量に比較して極め
て小さいから一時的には酸化塔２の液面レベルが
大幅に低下する異常現象が生じ、酸化機能が低下
するといつた問題を生じる。 However, in reality, due to the aforementioned gas seal structure in the desulfurization tower 1, the liquid level in the liquid chamber 12 frequently fluctuates in accordance with the flow rate of the exhaust gas. That is, when the exhaust gas flow rate changes, an internal pressure difference occurs between the gas-sealed space in the desulfurization tower 1 and the space in the liquid chamber 12,
Therefore, since a liquid level difference corresponding to this internal pressure difference occurs on both sides of the partition plate 11, the liquid level in the liquid chamber 12 fluctuates in accordance with the pressure of the exhaust gas introduced from the inlet duct 7. Become. When the exhaust gas pressure decreases and the liquid level in the liquid chamber 12 decreases, the desulfurization tower liquid level controller 21 reduces the opening degree of the flow rate control valve 14 to reduce the amount of desulfurization liquid sent to the oxidation tower 2. decrease. On the other hand, control by the liquid level control mechanisms 22, 23, and 16 works in the oxidation tower 2 as well, but regardless of this control, a certain amount of gypsum slurry is always supplied from the line 17 as a seed crystal for desulfurization. Recirculated to column 1. Therefore, at this time, the liquid level in the oxidation tower 2 decreases. Moreover, since the volume of the oxidizing tower 2 is extremely small compared to the capacity of the desulfurizing tower liquid reservoir 4, an abnormal phenomenon occurs in which the liquid level of the oxidizing tower 2 temporarily drops significantly, resulting in a decrease in the oxidizing function. occurs.
これと反対に入口ダクト７から導入される排ガ
スの圧力が増大して液室１２の液面レベルが上昇
した場合には、脱硫塔の液面レベル制御機構２
０，２１，１４により酸化塔２へ送給される脱硫
液の量が増大する。このとき制御機構２２，２
３，１６は後処理装置２３への石膏液の送給量を
急増させるから、酸化塔２では導入された脱硫液
の帯溜時間が短かくなつて酸化が不充分になると
いつた問題が生じる。また、後処理装置３では負
荷が急増して石膏分離能力等に問題が生じること
になる。 On the contrary, when the pressure of the exhaust gas introduced from the inlet duct 7 increases and the liquid level in the liquid chamber 12 rises, the liquid level control mechanism 2 of the desulfurization tower
0, 21, and 14, the amount of desulfurization liquid fed to the oxidation tower 2 increases. At this time, the control mechanism 22, 2
3 and 16 rapidly increase the amount of gypsum liquid fed to the post-processing device 23, which shortens the residence time of the desulfurization liquid introduced in the oxidation tower 2, causing problems such as insufficient oxidation. . Moreover, the load on the post-processing device 3 increases rapidly, causing problems in the gypsum separation ability and the like.
本考案は上記事情に鑑みてなされたもので、酸
化塔に導入される脱硫液および酸化塔から抜き取
られて後処理装置へ導入される石膏液の流量を安
定して制御でき、もつて酸化塔の高効率化および
後処理装置の裕度向上を達成し得る制御システム
を備えた排煙脱硫装置を提供するものである。 The present invention was developed in view of the above circumstances, and it is possible to stably control the flow rate of the desulfurization liquid introduced into the oxidation tower and the gypsum liquid extracted from the oxidation tower and introduced into the post-treatment equipment, and thereby The present invention provides a flue gas desulfurization device equipped with a control system that can achieve high efficiency and improved tolerance of the after-treatment device.
即ち、本考案は、液面検出計を備えた脱硫塔
と、該脱硫塔に脱硫液供給ラインを介して接続さ
れた酸化塔と、該脱硫液供給ラインに取付けられ
た脱硫液流量調節弁と、前記酸化塔に取付けられ
た酸化塔液面検出計と、前記酸化塔に脱硫処理液
供給ラインを介して接続された後処理装置と、該
脱硫処理液供給ラインに取付けられた処理液流量
調節弁と、前記酸化塔液面検出計の出力を受けて
所定の弁開度信号を前記脱硫液流量調節弁に供給
する酸化塔液レベル調節計と、前記液面検出計の
出力を受けて所定の弁開度信号を前記処理液流量
調節弁に供給する脱硫塔液レベル調節計とを具備
する排煙脱硫装置である。 That is, the present invention includes a desulfurization tower equipped with a liquid level detector, an oxidation tower connected to the desulfurization tower via a desulfurization liquid supply line, and a desulfurization liquid flow rate control valve attached to the desulfurization liquid supply line. , an oxidation tower liquid level detector attached to the oxidation tower, a post-treatment device connected to the oxidation tower via a desulfurization treatment liquid supply line, and a treatment liquid flow rate adjustment installed on the desulfurization treatment liquid supply line. an oxidation tower liquid level controller that receives the output of the oxidation tower liquid level detector and supplies a predetermined valve opening degree signal to the desulfurization liquid flow rate control valve; and a desulfurization tower liquid level controller that supplies a valve opening degree signal to the treated liquid flow rate control valve.
以下第２図〜第５図を参照して本考案の実施列
を説明する。 Embodiments of the present invention will be described below with reference to FIGS. 2 to 5.
第２図は本考案の一実施例になる排煙脱硫装置
を示すフローチヤートである。同図において、第
１図と同じ部分には、同一の参照番号を付してあ
る。第２図から明らかなように、この実施例の排
煙脱硫装置の構成はそのフロー制御システムを除
いて総て第１図のものと同じである。即ち、この
実施例では脱硫塔１の液面検出計２０に接続され
た脱硫塔液レベル調節計２１が後処理装置３へ導
入される石膏スラリーの供給量を調節する流量調
節弁１６に接続されてその開度を制御している点
で第１図の場合と相違している。また、酸化塔２
の液面検出計２２に接続された酸化塔液レベル調
節計２３は酸化塔に導入される脱硫液の量を調節
するための流量調節弁１４に接続されてその開度
を制御しており、この点でも第１図の場合と相違
している。この結果、酸化塔２においては液面レ
ベル制御機構２２，２３，１４によつて液面の自
己制御ループが形成されているが、脱硫塔１にお
ける液面レベル制御機構２０，２１，２３は自己
制御ループを形成していない。つまり、脱硫塔１
の液面レベルは、まず流量調節弁１６の開度調節
により酸化塔２からの石膏液の抜き取り量を制御
し、この影響により酸化塔２の液面レベル制御機
構２２，２３，１４を動作させて脱硫塔１から酸
化塔２へ供給される脱硫液流量を制御するといつ
た制御ループ、即ち酸化塔２の自己制御ループを
介在した連鎖制御ループで行なわれる。 FIG. 2 is a flowchart showing a flue gas desulfurization device according to an embodiment of the present invention. In this figure, the same parts as in FIG. 1 are given the same reference numbers. As is clear from FIG. 2, the structure of the flue gas desulfurization apparatus of this embodiment is the same as that of FIG. 1 except for its flow control system. That is, in this embodiment, a desulfurization tower liquid level controller 21 connected to a liquid level detector 20 of the desulfurization tower 1 is connected to a flow rate control valve 16 that adjusts the supply amount of gypsum slurry introduced into the aftertreatment device 3. This is different from the case shown in FIG. 1 in that the opening degree is controlled by the lever. In addition, oxidation tower 2
The oxidation tower liquid level controller 23 connected to the liquid level detector 22 is connected to a flow rate adjustment valve 14 for adjusting the amount of desulfurization liquid introduced into the oxidation tower, and controls its opening degree. This point also differs from the case shown in FIG. As a result, in the oxidation tower 2, a self-control loop for the liquid level is formed by the liquid level control mechanisms 22, 23, and 14, but the liquid level control mechanisms 20, 21, and 23 in the desulfurization tower 1 are self-controlled. No control loop is formed. In other words, desulfurization tower 1
The liquid level is determined by first controlling the amount of gypsum liquid extracted from the oxidation tower 2 by adjusting the opening of the flow rate control valve 16, and by this influence, the liquid level control mechanisms 22, 23, and 14 of the oxidation tower 2 are operated. The flow rate of desulfurization liquid supplied from the desulfurization tower 1 to the oxidation tower 2 is controlled by a control loop, that is, a chain control loop with a self-control loop of the oxidation tower 2 interposed therebetween.
上記第２図の実施例において、脱硫塔１に導入
される排ガスの圧力（即ち、排ガス量）が減少し
て液室１２の液面レベルが低下したとすると、ま
ず脱硫塔１の液面レベル制御機構２０，２１が流
量調節弁１６の開度を制御し、酸化塔２の抜出し
液流量を調節する。つまり、脱硫塔液レベル調節
計２１は、積分動作機能を有する調節計を設け、
脱硫塔液室１２の液レベルが急激に変化した場合
も、流量調節弁１６を徐々に開閉することによ
り、酸化塔２の抜き出流量と供給量の急変と大巾
な変動を制御する。その結果、酸化塔２の供給量
を安定にして酸化効率の向上と安定化を図り、酸
化塔２を小形にして必要空気量を減少してコスト
ダウンを達成できる。 In the embodiment shown in FIG. 2 above, if the pressure of the exhaust gas introduced into the desulfurization tower 1 (that is, the amount of exhaust gas) decreases and the liquid level in the liquid chamber 12 decreases, first the liquid level in the desulfurization tower 1 decreases. Control mechanisms 20 and 21 control the opening degree of the flow rate control valve 16 to adjust the flow rate of liquid extracted from the oxidation tower 2. In other words, the desulfurization tower liquid level controller 21 is provided with a controller having an integral operation function,
Even when the liquid level in the desulfurization tower liquid chamber 12 changes suddenly, sudden changes and large fluctuations in the extraction flow rate and supply amount of the oxidation tower 2 can be controlled by gradually opening and closing the flow rate control valve 16. As a result, the supply amount of the oxidation tower 2 can be stabilized to improve and stabilize the oxidation efficiency, and the oxidation tower 2 can be made smaller to reduce the amount of air required, thereby achieving cost reduction.
第３図は、本考案の他の実施例の概略構成を示
す説明図である。なお、第２図に示す排煙脱硫装
置と同じ部分には、同一の参照番号を付してあ
る。この排煙脱硫装置は、第３図から明らかなよ
うに、脱硫塔１，１′を２台設けたことに起因し
て、フロー制御システムに偏差変換器３１と演算
器２１及び選択器３０を設けた点を除いて、総て
第２図に示すものと同様の構成を有している。即
ち、この実施例のフロー制御システムは、２台の
脱硫塔１，１′の液面検出計２０，２０′の出力信
号を受けて所定の弁開度信号を脱硫塔液レベル調
節計２１に供給する選択器３０を有している。ま
た、このフロー制御システムは、これらの液面検
出計２０，２０′からの出力信号によつて液面レ
ベル差を検出する偏差変換器３１と、この偏差変
換器３１及び酸化塔液レベル調節計２３の出力信
号を受けて、所定の弁開度信号を流量調節弁１
４，１４′に供給する演算器３２とを有してい
る。 FIG. 3 is an explanatory diagram showing a schematic configuration of another embodiment of the present invention. Note that the same parts as in the flue gas desulfurization apparatus shown in FIG. 2 are given the same reference numbers. As is clear from FIG. 3, this flue gas desulfurization equipment is equipped with a deviation converter 31, a calculator 21, and a selector 30 in the flow control system due to the provision of two desulfurizers 1 and 1'. All of them have the same structure as that shown in FIG. 2 except for the points provided. That is, the flow control system of this embodiment receives output signals from the liquid level detectors 20 and 20' of the two desulfurization towers 1 and 1', and sends a predetermined valve opening signal to the desulfurization tower liquid level controller 21. It has a selector 30 for supplying. This flow control system also includes a deviation converter 31 that detects a liquid level difference based on output signals from these liquid level detectors 20 and 20', and this deviation converter 31 and an oxidation tower liquid level controller. 23, a predetermined valve opening signal is sent to the flow control valve 1.
4 and 14'.
而して、脱硫塔１，１′の液面レベル偏差を検
出する偏差変換器３１は、例えば第４図に示す偏
差信号ΔＬを演算器３２に供給する。 The deviation converter 31 that detects the liquid level deviation in the desulfurization towers 1 and 1' supplies, for example, a deviation signal ΔL shown in FIG. 4 to the calculator 32.
ここで、偏差信号ΔＬは、〔（第１脱硫塔１から
の液面レベル信号）−（第２脱硫塔１′からの液面
レベル信号）〕の偏差を意味し、偏差信号ΔＬに
対応する任意の液レベル偏差出力X1は、液レベ
ル偏差が零時にX1＝50％を出力し、第２脱硫塔
１′の液面レベルが低い場合には液レベル偏差出
力X1は大きくなり、第１脱硫塔１の液面レベル
が低い場合は、液レベル偏差出力X1が小さくな
ることを意味する。また、演算器３２は酸化塔液
面制御信号を主入力とし、偏差信号ΔＬを分配信
号として入力、演算するものであり、第５図に示
す特性演算と、演算値Y1，Y1′のそれぞれに酸化
塔液面制御信号を乗算して脱硫液抜出し量信号を
出力する演算機能を有する。第５図実線（太線）
は第１脱硫塔１の演算値Y1、破線は第２脱硫塔
１′の演算値Y1′の演算出力特性線を示す。 Here, the deviation signal ΔL means the deviation of [(liquid level signal from the first desulfurization tower 1)−(liquid level signal from the second desulfurization tower 1')], and corresponds to the deviation signal ΔL. The arbitrary liquid level deviation output X 1 outputs X 1 =50% when the liquid level deviation is zero, and when the liquid level of the second desulfurization tower 1' is low, the liquid level deviation output X 1 becomes large. When the liquid level of the first desulfurization tower 1 is low, it means that the liquid level deviation output X 1 becomes small. Further, the calculator 32 receives the oxidation tower liquid level control signal as the main input and inputs the deviation signal ΔL as the distribution signal to perform calculations, and performs the characteristic calculations shown in FIG. 5 and the calculated values Y 1 and Y 1 '. It has an arithmetic function that multiplies each by an oxidation tower liquid level control signal and outputs a desulfurization liquid withdrawal amount signal. Figure 5 Solid line (thick line)
indicates the calculated value Y 1 of the first desulfurization tower 1, and the broken line represents the calculated output characteristic line of the calculated value Y 1 ' of the second desulfurization tower 1'.
なお分配演算器と乗算演算器を個別に設置した
場合も同等の機能を有する。 It should be noted that the same function can be obtained even when the distribution arithmetic unit and the multiplication arithmetic unit are installed separately.
従つて、第２脱硫塔１′の液レベルが第１脱硫
塔１側より高い液レベル偏差出力X1′の場合、第
１脱硫塔１側は所定の演算値Y1′を出力し乗算す
るので脱硫液抜出量信号はこの演算値Y1′の比率
だけ酸化塔２２の液面制御信号を抑制して調節弁
１４に供給され、開度調節を行う。一方レベルの
高い第２脱硫塔１′は演算値Y1′＝100％を出力し
乗算するので制御信号がそのまま流量調節弁１
４′に供給され、開度調節を行う。又第１脱硫塔
１側の液レベルが高い液レベル偏差出力X1″の場
合、脱硫液の抜出量信号は、演算値Y1″＝100％
により制御信号と同一となり、調節弁１４は酸化
塔液レベル調節計２３で直接制御するのと同等の
動作をする。又第２脱硫塔１′は演算値X1″の偏
差信号ΔＬより演算値Y1″を演算出力し、制御信
号を乗算することにより、制御信号をこの演算値
Y1″比率相当抑制して流量調節弁１４′を調節す
る。 Therefore, when the liquid level of the second desulfurization tower 1' is higher than that of the first desulfurization tower 1 side, the first desulfurization tower 1 side outputs a predetermined calculated value Y1 ' and multiplies it. Therefore, the desulfurization liquid withdrawal amount signal suppresses the liquid level control signal of the oxidation tower 22 by the ratio of this calculated value Y 1 ', and is supplied to the control valve 14 to adjust the opening degree. On the other hand, the second desulfurization tower 1', which has a high level, outputs the calculated value Y1 '=100% and multiplies it, so the control signal is sent directly to the flow rate control valve 1.
4' and adjusts the opening. In addition, when the liquid level on the first desulfurization tower 1 side is high and the liquid level deviation output is X 1 ″, the desulfurization liquid withdrawal amount signal is calculated value Y 1 ″ = 100%.
This becomes the same as the control signal, and the control valve 14 operates in the same way as if it were directly controlled by the oxidation tower liquid level controller 23. In addition, the second desulfurization tower 1' calculates and outputs the calculated value Y 1 '' from the deviation signal ΔL of the calculated value X 1 '', and multiplies it by the control signal to convert the control signal to this calculated value.
The flow control valve 14' is adjusted by suppressing the Y 1 '' ratio.
すなわち、常に脱硫塔液レベルが高い方の流量
調節弁１４，１４′を100％調節し低い方は偏差比
率に比例して調節弁開度を抑制制御する作用を持
つ。抑制比率は、第５図の偏差信号ΔＬと液レベ
ル偏差出力X1の変換勾配により定まり第１脱硫
塔１と第２脱硫塔１′の液レベル差は、偏差信号
ΔＬの範囲内に自動制御される。 That is, the flow control valve 14, 14' whose desulfurization tower liquid level is higher is always 100% controlled, and the flow control valve 14, 14' whose desulfurization tower liquid level is lower has the effect of suppressing and controlling the opening degree of the control valve in proportion to the deviation ratio. The suppression ratio is determined by the conversion gradient of the deviation signal ΔL and liquid level deviation output be done.
一方、脱硫塔液レベル調節計２１は、選択器３
０により常に第１脱硫塔１又は第２脱硫塔１′の
いずれか高い方のレベル信号を受信して酸化塔２
の抜出流量調節弁１６を制御し、酸化塔２の抜出
量及び脱硫塔１，１′の脱硫液抜出量を制御する
もので、第１脱硫塔１、第２脱硫塔１′の液レベ
ル差を解消しつつ脱硫液を後処理工程に送る。 On the other hand, the desulfurization tower liquid level controller 21
0, the oxidation tower 2 always receives the level signal from either the first desulfurization tower 1 or the second desulfurization tower 1', whichever is higher.
The control valve 16 controls the amount of extraction from the oxidation tower 2 and the amount of desulfurization liquid from the desulfurization towers 1 and 1'. The desulfurization liquid is sent to the post-treatment process while eliminating the liquid level difference.
また、本システムによると後処理工程への抜出
し量の最大値を流量調節弁１６の弁口径寸法で規
制して、脱硫塔液溜４，４′を脱硫液のクツシヨ
ンタンクとして使用し酸化塔供給量及び抜出し流
量を抑制することが出来酸化塔２及び後処理工程
の処理効率の向上、コストダウンに寄与するもの
である。 In addition, according to this system, the maximum amount of extraction to the post-treatment process is regulated by the valve diameter of the flow rate control valve 16, and the desulfurization tower reservoirs 4 and 4' are used as a cushion tank for the desulfurization liquid. The supply amount and the withdrawal flow rate can be suppressed, which contributes to improving the processing efficiency of the oxidation tower 2 and the post-treatment process and reducing costs.
以上説明した如く、本考案に係る排煙脱硫装置
によれば、酸化塔に導入される脱硫液および酸化
塔から抜き取られて後処理装置へ導入される石膏
液の液量の制御を安定して行い、もつて酸化塔の
高効率化および後処理装置への裕度向上を達成で
きる等顕著な効果を奏するものである。 As explained above, according to the flue gas desulfurization device according to the present invention, the amount of the desulfurization liquid introduced into the oxidation tower and the gypsum liquid extracted from the oxidation tower and introduced into the post-treatment device can be stably controlled. When carried out, remarkable effects can be achieved, such as increasing the efficiency of the oxidation tower and improving the margin for the after-treatment equipment.
第１図は、従来の排煙脱硫装置の概略構成を示
す説明図、第２図は、本考案の一実施例の概略構
成を示す説明図、第３図は、本考案の他の実施例
の概略構成を示す説明図、第４図は、液レベル偏
差出力と脱硫塔液レベル偏差の関係を示す特性
図、第５図は、演算出力と液レベル偏差出力の関
係を示す特性図である。
１……脱硫塔、２……酸化塔、３……後処理装
置、４……脱硫液溜、５……ポンプ、６……ライ
ン、７……入口ダクト、８……ミストセパレー
タ、９……ミストドレイン管、１０……撹拌機、
１１……仕切板、１２……液室、１３……石灰液
供給ライン、１４……流量調節弁、１５……ライ
ン、１６……流量調節弁、１７……ライン、１８
……流量調節弁、１９……流量調節計、２０……
液面検出計、２１……脱硫塔液レベル調節計、２
２……液面検出計、２３……酸化塔液レベル調節
計、３０……選択器、３１……偏差変換器、３２
……演算器。
FIG. 1 is an explanatory diagram showing a schematic configuration of a conventional flue gas desulfurization device, FIG. 2 is an explanatory diagram showing a schematic configuration of an embodiment of the present invention, and FIG. 3 is an explanatory diagram showing a schematic configuration of an embodiment of the present invention. 4 is a characteristic diagram showing the relationship between the liquid level deviation output and the desulfurization tower liquid level deviation, and FIG. 5 is a characteristic diagram showing the relationship between the calculation output and the liquid level deviation output. . DESCRIPTION OF SYMBOLS 1... Desulfurization tower, 2... Oxidation tower, 3... After-treatment device, 4... Desulfurization liquid reservoir, 5... Pump, 6... Line, 7... Inlet duct, 8... Mist separator, 9... ...Mist drain pipe, 10...Agitator,
11... Partition plate, 12... Liquid chamber, 13... Lime liquid supply line, 14... Flow rate control valve, 15... Line, 16... Flow rate control valve, 17... Line, 18
...Flow rate control valve, 19...Flow rate controller, 20...
Liquid level detector, 21... Desulfurization tower liquid level controller, 2
2... Liquid level detector, 23... Oxidation tower liquid level controller, 30... Selector, 31... Deviation converter, 32
...Arithmetic unit.
Claims (1)
硫液供給ラインを介して接続された酸化塔と、
該脱硫液供給ラインに取付けられた脱硫液流量
調節弁と、前記酸化塔に取付けられた酸化塔液
面検出計と、前記酸化塔に脱硫処理液供給ライ
ンを介して接続された後処理装置と、該脱硫処
理液供給ラインに取付けられた処理液流量調節
弁と、前記酸化塔液面検出計の出力を受けて所
定の弁開度信号を前記脱硫液流量調節弁に供給
する酸化塔液レベル調節計と、前記液面検出計
の出力を受けて所定の弁開度信号を前記処理液
流量調節弁に供給する脱硫塔液レベル調節計と
を具備することを特徴とする排煙脱硫装置。 (2) 脱硫塔が複数個あり、各々の該脱硫塔に取付
けられた液面検出計の出力信号の偏差を算出し
て所定の出力信号を脱硫塔液レベル調節計に供
給する選択器が設けられている実用新案登録請
求の範囲第１項記載の排煙脱硫装置。[Claims for Utility Model Registration] (1) A desulfurization tower equipped with a liquid level detector, an oxidation tower connected to the desulfurization tower via a desulfurization liquid supply line,
A desulfurization liquid flow rate control valve attached to the desulfurization liquid supply line, an oxidation tower liquid level detector attached to the oxidation tower, and a post-treatment device connected to the oxidation tower via a desulfurization treatment liquid supply line. , a processing liquid flow control valve attached to the desulfurization processing liquid supply line, and an oxidation tower liquid level that receives the output of the oxidation tower liquid level detector and supplies a predetermined valve opening signal to the desulfurization liquid flow control valve. A flue gas desulfurization apparatus comprising: a controller; and a desulfurization tower liquid level controller that receives the output of the liquid level detector and supplies a predetermined valve opening degree signal to the treated liquid flow rate control valve. (2) There are multiple desulfurization towers, and there is a selector that calculates the deviation of the output signal of the liquid level detector attached to each desulfurization tower and supplies a predetermined output signal to the desulfurization tower liquid level controller. The flue gas desulfurization device according to claim 1 of the registered utility model.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5281082U JPS58156524U (en) | 1982-04-12 | 1982-04-12 | Flue gas desulfurization equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5281082U JPS58156524U (en) | 1982-04-12 | 1982-04-12 | Flue gas desulfurization equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58156524U JPS58156524U (en) | 1983-10-19 |
| JPS6244733Y2 true JPS6244733Y2 (en) | 1987-11-27 |
Family
ID=30063507
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5281082U Granted JPS58156524U (en) | 1982-04-12 | 1982-04-12 | Flue gas desulfurization equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58156524U (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7242378B2 (en) * | 2019-03-28 | 2023-03-20 | 三菱重工業株式会社 | Separation and recovery system and separation and recovery method |
-
1982
- 1982-04-12 JP JP5281082U patent/JPS58156524U/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58156524U (en) | 1983-10-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1088389C (en) | Method for separating SO2 from waste gas | |
| US6041272A (en) | Desulfurization process for flue gases | |
| JPH06182148A (en) | Controlling apparatus for wet flue gas desulfurization apparatus | |
| JPS6244733Y2 (en) | ||
| JPH1085549A (en) | Wet exhaust gas desulfurization device and exhaust gas desulfutization | |
| JPS59169523A (en) | Control of wet waste gas desulfurization apparatus | |
| US4618482A (en) | Method for controlling a concentration of slurry in wet flue gas desulfurization apparatus | |
| JPH11197450A (en) | Wet desulfurization equipment and its operation method | |
| JPH10128053A (en) | Stack gas treating device and treatment of stack gas | |
| JPH0919623A (en) | Wet type waste gas desulfurizing method and device therefor | |
| JPS585846B2 (en) | Wet lime plaster method flue gas desulfurization method | |
| JP2933664B2 (en) | Absorbent PH control unit for wet flue gas desulfurization unit | |
| JPS5932924A (en) | Controlling method of desulfurizing ratio in waste gas desulfurizing apparatus applied with wet lime method | |
| JP2004243169A (en) | Desulfurization method for waste gas by double decomposition method | |
| JP3532028B2 (en) | Exhaust gas desulfurization method | |
| JP2798973B2 (en) | Exhaust gas desulfurization equipment | |
| JPS6018449B2 (en) | Method for removing sulfur oxides from exhaust gas | |
| JPH11244648A (en) | Control of absorbent slurry flow rate of wet stack gas desulfurizer and device therefor | |
| JPS59160519A (en) | Wet type waste gas desulfurizer | |
| JPS6121720A (en) | Control apparatus of wet waste gas desulfurization apparatus | |
| JPH0147215B2 (en) | ||
| JPS631090B2 (en) | ||
| JPS5852685B2 (en) | Desulfurization method for flue gas with large fluctuations in SO↓2 concentration | |
| JPH09271631A (en) | Desulfurization of exhaust gas | |
| JP2000015051A (en) | Control method for absorption tower bleed liquid flow rate in flue gas desulfurization apparatus |