JPH05111615A - Ph control device for wet flue gas desulfurization plant - Google Patents
Ph control device for wet flue gas desulfurization plantInfo
- Publication number
- JPH05111615A JPH05111615A JP3273871A JP27387191A JPH05111615A JP H05111615 A JPH05111615 A JP H05111615A JP 3273871 A JP3273871 A JP 3273871A JP 27387191 A JP27387191 A JP 27387191A JP H05111615 A JPH05111615 A JP H05111615A
- Authority
- JP
- Japan
- Prior art keywords
- desulfurization plant
- control device
- detector
- absorbent
- 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.)
- Pending
Links
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 15
- 230000023556 desulfurization Effects 0.000 title claims abstract description 15
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 7
- 239000003546 flue gas Substances 0.000 title claims abstract description 7
- 239000007789 gas Substances 0.000 claims abstract description 16
- 239000002250 absorbent Substances 0.000 claims abstract description 15
- 230000002745 absorbent Effects 0.000 claims abstract description 15
- 238000010521 absorption reaction Methods 0.000 claims description 25
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 7
- 239000007788 liquid Substances 0.000 abstract description 19
- 239000006096 absorbing agent Substances 0.000 abstract 4
- 239000003463 adsorbent Substances 0.000 abstract 1
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 description 4
- 229910001437 manganese ion Inorganic materials 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- WAEMQWOKJMHJLA-UHFFFAOYSA-N Manganese(2+) Chemical compound [Mn+2] WAEMQWOKJMHJLA-UHFFFAOYSA-N 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 230000035945 sensitivity Effects 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- PPNAOCWZXJOHFK-UHFFFAOYSA-N manganese(2+);oxygen(2-) Chemical compound [O-2].[Mn+2] PPNAOCWZXJOHFK-UHFFFAOYSA-N 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は処理ガス中の亜硫酸ガス
（ＳＯ2 ）を除去する湿式排煙脱硫プラントにおける吸
収液のｐＨ制御装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a pH control device for absorbing liquid in a wet flue gas desulfurization plant for removing sulfurous acid gas (SO 2 ) in a processing gas.
【０００２】[0002]
【従来の技術】脱硫プラント、例えば炭酸カルシウムを
吸収剤とする湿式石灰石こう法廃煙脱硫プラントの概略
構成を図３に示す系統図を参照して説明する。2. Description of the Related Art A schematic structure of a desulfurization plant, for example, a wet lime-gypsum waste smoke desulfurization plant using calcium carbonate as an absorbent will be described with reference to a system diagram shown in FIG.
【０００３】図３において、吸収塔１には処理ガス導入
ダクト２を介して亜硫酸ガスを含有する処理ガス３が上
方から導入される。この吸収塔１下方に設けられたタン
ク４内には吸収液５が収容され、この吸収液５は循環ポ
ンプ６及び循環配管７により吸収塔１内を循環されてい
る。前記処理ガス３は循環塔１内で吸収液５と接触し、
処理ガス３中に含まれる亜硫酸ガスが除去される。すな
わち、処理ガス３中のＳＯ2 と次式（Ｉ）で示す反応に
よりＨ2 ＳＯ3 を生成して流下する。このＨ2 ＳＯ3 の
一部は処理ガス３中の酸素（Ｏ2 ）により酸化され、次
式（II) で示すようにＨ2 ＳＯ4 となる。また、吸収塔
１内で酸化されなかったＨ2 ＳＯ3 はタンク４内で配管
２０より供給される空気と接触し（II) 式の反応で全量
Ｈ2 ＳＯ 4 となる。 ＳＯ2 ＋Ｈ2 Ｏ → Ｈ2 ＳＯ3 ・・・・・（Ｉ） Ｈ2 ＳＯ3 ＋ 1/2Ｏ2 → Ｈ2 ＳＯ4 ・・・・・（II) そして、吸収塔１を通過し、亜硫酸ガスが除去された処
理ガスは排気ダクト８を介して処理済ガスとして大気中
に放出される。In FIG. 3, the processing gas is introduced into the absorption tower 1.
Processing gas 3 containing sulfurous acid gas through duct 2
It is introduced by the people. The tank installed below the absorption tower 1
The absorbent 4 is contained in the chamber 4, and the absorbent 5 is circulated.
Is circulated in the absorption tower 1 by the pump 6 and the circulation pipe 7.
It The processing gas 3 comes into contact with the absorbing liquid 5 in the circulation tower 1,
Sulfurous acid gas contained in the processing gas 3 is removed. sand
That is, SO in the processing gas 32And the reaction represented by the following formula (I)
More H2SO3Generate and flow down. This H2SO3of
A part of the oxygen (O2) Is oxidized by
As shown in formula (II), H2SOFourBecomes Also the absorption tower
H not oxidized in 12SO3Is piped in tank 4
Contact with the air supplied from 20
H2SO FourBecomes SO2+ H2O → H2SO3 (I) H2SO3+ 1 / 2O2 → H2SOFour (II) Then, after passing through the absorption tower 1, the sulfurous acid gas was removed.
The processing gas is in the atmosphere as processed gas through the exhaust duct 8.
Is released to.
【０００４】以上のように吸収塔１内で処理ガス３との
接触を続けると、前記吸収液５中には上記（Ｉ）及び
（II) で示した吸収反応及び酸化反応により生成したＨ
2 ＳＯ 4 が多量に含まれるため、何らかの措置をとらな
ければＳＯ2 を吸収することが困難となる。そこで、タ
ンク４内の吸収液５に流量調節弁１０を介装した吸収剤
供給配管１１を介して吸収剤、例えば炭酸カルシウム
（ＣａＣＯ3 ）を供給し、次式（III)に示すように吸収
液５を中和して亜硫酸ガスを容易に吸収し得るように再
生している。 Ｈ2 ＳＯ4 ＋ＣａＣＯ3 →ＣａＳＯ4 ＋Ｈ2 Ｏ＋ＣＯ2 ↑ ・・・（III) 上記（III)式により生成したＣａＳＯ4 を含む吸収液５
の一部は移送配管１２を介して図示しない別の工程へ移
送される。As described above, in the absorption tower 1
If the contact is continued, the above-mentioned (I) and
H produced by the absorption and oxidation reactions shown in (II)
2SO FourIs included in a large amount, so do not take any measures.
If SO2Becomes difficult to absorb. Therefore,
Absorbent in which the flow control valve 10 is interposed in the absorbent 5 in the tank 4.
Absorbent via supply line 11, eg calcium carbonate
(CaCO3) Is supplied and absorbed as shown in the following formula (III):
Liquid 5 should be neutralized so that it can be easily absorbed by sulfur dioxide.
Alive H2SOFour+ CaCO3→ CaSOFour+ H2O + CO2↑ (III) CaSO generated by the above formula (III)FourAbsorption liquid containing 5
A part of it is transferred to another process (not shown) through the transfer pipe 12.
Will be sent.
【０００５】以上の説明から示唆されるように、吸収液
５のＳＯ2 吸収能力が脱硫プラントの性能に多大な影響
を及ぼす。この吸収液５のＳＯ2吸収能力の指標となる
のは、吸収液５のｐＨである。すなわち、吸収液５中の
ＣａＣＯ3 濃度が高く、ｐＨが高いほどＳＯ2 吸収反応
が促進される。単純には吸収液のｐＨを高く維持するた
めに多量の吸収剤を供給することが考えられるが、これ
はコストの面から好ましいことではない。As suggested by the above description, the SO 2 absorption capacity of the absorbing liquid 5 has a great influence on the performance of the desulfurization plant. The pH of the absorption liquid 5 is an index of the SO 2 absorption capacity of the absorption liquid 5. That is, as the CaCO 3 concentration in the absorption liquid 5 is higher and the pH is higher, the SO 2 absorption reaction is promoted. It is possible to simply supply a large amount of the absorbent in order to keep the pH of the absorbing solution high, but this is not preferable in terms of cost.
【０００６】こうしたことから所望の性能を維持できる
程度のｐＨで脱硫プラントの運転を行なうことが要望さ
れている。[0006] Therefore, it is required to operate the desulfurization plant at a pH at which the desired performance can be maintained.
【０００７】図３で図示の従来の脱硫プラントにおいて
は、循環液５のｐＨ制御装置は以下のようなものであ
る。すなわち、前記循環配管７にはｐＨ検出器１３が取
付けられており、このｐＨ検出器１３からの出力信号Ｓ
13はｐＨ調節器１４に入力される。このｐＨ調節器１４
では、予め設定されたｐＨ設定値とｐＨ検出器１３から
の出力信号とを比較し、ＰＩ又はＰＩＤ（Ｐ：比例、
Ｉ：積分、Ｄ：微分）のフィードバック制御を行なう。
このＰH 調節器１４の出力信号で、吸収剤供給配管１１
に設置された流量調整弁１０の開度を調整する。このよ
うにして、吸収液５のｐＨが所定値となるように制御し
ている。In the conventional desulfurization plant shown in FIG. 3, the pH control device for the circulating liquid 5 is as follows. That is, a pH detector 13 is attached to the circulation pipe 7, and an output signal S from the pH detector 13 is attached.
13 is input to the pH controller 14. This pH controller 14
Then, the preset pH set value is compared with the output signal from the pH detector 13, and PI or PID (P: proportional,
Feedback control (I: integral, D: derivative) is performed.
The output signal of the P H adjuster 14, absorbent feed pipe 11
The opening degree of the flow rate adjusting valve 10 installed in the above is adjusted. In this way, the pH of the absorbing liquid 5 is controlled to be the predetermined value.
【０００８】[0008]
【発明が解決しようとする課題】従来の装置では循環配
管のｐＨすなわちタンク内のｐＨをｐＨ計によって測定
している。タンク内には、ＳＯ2 を吸収して生成された
Ｈ2 ＳＯ3 を酸化させるために空気を吹きこんでいる。
この空気によって吸収剤である天然の石灰石に含まれる
微量成分のマンガンイオンが酸化され、酸化マンガンと
なって、ｐＨ計の電極表面に付着し、ｐＨ計の測定感度
が低下するという問題が生じている。この酸化マンガン
は、Ｈ2 ＳＯ3 が大量に存在する吸収塔内では、このＨ
2 ＳＯ3 によって還元されてマンガンイオンになる。マ
ンガンイオンの状態においてはｐＨ計の電極表面に付着
することはなく、ｐＨ計は正常に作動する。すなわち、
Ｈ2 ＳＯ3 が存在するところで、ｐＨを測定すれば、こ
のような問題は生じることはない。In the conventional apparatus, the pH of the circulation pipe, that is, the pH in the tank is measured by a pH meter. Air is blown into the tank to oxidize H 2 SO 3 produced by absorbing SO 2 .
This air oxidizes the trace amount of manganese ions contained in the natural limestone that is the absorbent, turns into manganese oxide, and adheres to the electrode surface of the pH meter, causing a problem that the measurement sensitivity of the pH meter decreases. There is. This manganese oxide is the H 2 SO 3 in the absorption tower in which a large amount is present.
It is reduced by 2 SO 3 into manganese ions. In the state of manganese ion, it does not adhere to the electrode surface of the pH meter, and the pH meter operates normally. That is,
If the pH is measured in the presence of H 2 SO 3 , such a problem does not occur.
【０００９】本発明は上記知見に基づいて、従来技術に
おけるようなｐＨ計の電極面に酸化マンガンが付着せ
ず、湿式排煙脱硫プラント内の吸収液のｐＨを正確に制
御することができるｐＨ制御装置を提供しようとするも
のである。On the basis of the above findings, the present invention is such that manganese oxide does not adhere to the electrode surface of the pH meter as in the prior art, and the pH of the absorbing liquid in the wet flue gas desulfurization plant can be accurately controlled. It is intended to provide a control device.
【００１０】[0010]
【課題を解決するための手段】本発明は吸収塔内での落
下液のｐＨを検出するｐＨ検出器と、前記ｐＨ検出器の
出力信号を制御量とするｐＨ調節計と、前記吸収塔に供
給する吸収剤供給配管に設置され、前記ｐＨ調節計の出
力信号で操作する調節弁とを具備してなることを特徴と
する湿式排煙脱硫装置のｐＨ制御装置である。According to the present invention, there is provided a pH detector for detecting the pH of a falling liquid in an absorption tower, a pH controller having an output signal of the pH detector as a control amount, and the absorption tower. A pH control apparatus for a wet flue gas desulfurization apparatus, which is installed in an absorbent supply pipe for supply and is provided with a control valve operated by an output signal of the pH controller.
【００１１】[0011]
【作用】本発明ではｐＨ計が正常に作動するＨ2 ＳＯ3
が存在する場所すなわち吸収塔内の落下液のｐＨを測定
し、このｐＨを所定値に制御する。In the present invention, the pH meter operates normally with H 2 SO 3
The pH of the falling liquid in the absorption tower, that is, in the presence of is measured, and this pH is controlled to a predetermined value.
【００１２】[0012]
【実施例】以下、本発明の一実施例を図１を参照して説
明する。なお、図３に示す従来の装置と同一の機器等に
は同一の番号を付して説明を省略する。本発明に係るｐ
Ｈ制御装置において新たに設けられた機器は、吸収塔１
内の吸収液の落下液のｐＨを測定するｐＨ検出器１７の
みである。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described below with reference to FIG. It should be noted that the same components as those of the conventional device shown in FIG. P according to the present invention
The equipment newly installed in the H control device is the absorption tower 1
Only the pH detector 17 for measuring the pH of the falling liquid of the absorbing liquid therein.
【００１３】落下液のｐＨを測定する詳細な実施例とし
て、図２のように落下液捕集器具１５と捕集落下液をｐ
Ｈ検出器１７に導き、ｐＨ検出後再度吸収塔１に戻す配
管１６が考えられる。勿論、ｐＨ検出器１７を図１に示
すように、直接吸収塔１内に差しこむことでもよい。As a detailed example for measuring the pH of the falling liquid, as shown in FIG.
A pipe 16 that leads to the H detector 17 and returns to the absorption tower 1 after pH detection can be considered. Of course, the pH detector 17 may be directly inserted into the absorption tower 1 as shown in FIG.
【００１４】[0014]
【発明の効果】本発明によれば、落下液のｐＨを測定す
るｐＨ検出器とｐＨ調節器と調節弁とにより落下液のｐ
Ｈを所定の値に保つことができる。しかも吸収塔ではＨ
2 ＳＯ 3 が大量に存在するため、酸化マンガンは還元さ
れ、マンガンイオンとなるため、従来装置の欠点であっ
た酸化マンガンによるｐＨ計の測定感度が悪くなること
もない。According to the present invention, the pH of falling liquid can be measured.
The pH of the falling liquid is adjusted by the pH detector, pH controller and control valve
H can be maintained at a predetermined value. Moreover, H in the absorption tower
2SO 3Manganese oxide is reduced due to the large amount of
Is a manganese ion, which is a drawback of the conventional device.
The measurement sensitivity of the pH meter due to manganese oxide deteriorates
Nor.
【図１】本発明の一実施例の説明図FIG. 1 is an explanatory diagram of an embodiment of the present invention.
【図２】本発明の他の実施例の説明図FIG. 2 is an explanatory diagram of another embodiment of the present invention.
【図３】従来の湿式排煙脱硫装置のｐＨ制御装置の説明
図FIG. 3 is an explanatory view of a pH control device of a conventional wet flue gas desulfurization device.
Claims (1)
内に導入し、吸収剤を含有し吸収塔内を循環する吸収液
と接触させて脱硫する脱硫プラントにおいて、吸収塔内
での落下液のｐＨを検出するｐＨ検出器と、前記ｐＨ検
出器の出力信号を制御量とするｐＨ調節計と、前記吸収
塔に供給する吸収剤供給配管に設置され前記ｐＨ調節計
の出力信号で操作する調節弁とを具備してなることを特
徴とする湿式排煙脱硫プラントのｐＨ制御装置。1. A desulfurization plant in which a treatment gas containing sulfurous acid gas is introduced into an absorption tower and is desulfurized by contacting with an absorbent containing an absorbent and circulating in the absorption tower. PH detector for detecting the pH of the pH detector, a pH controller that uses the output signal of the pH detector as a control amount, and an absorbent supply pipe that is supplied to the absorption tower and is operated by the output signal of the pH controller. A pH control device for a wet flue gas desulfurization plant, comprising a control valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3273871A JPH05111615A (en) | 1991-10-22 | 1991-10-22 | Ph control device for wet flue gas desulfurization plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3273871A JPH05111615A (en) | 1991-10-22 | 1991-10-22 | Ph control device for wet flue gas desulfurization plant |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH05111615A true JPH05111615A (en) | 1993-05-07 |
Family
ID=17533729
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3273871A Pending JPH05111615A (en) | 1991-10-22 | 1991-10-22 | Ph control device for wet flue gas desulfurization plant |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH05111615A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109200763A (en) * | 2018-09-30 | 2019-01-15 | 北京国电龙源环保工程有限公司 | A kind of flue gas desulphurization system loop slurry detection system |
-
1991
- 1991-10-22 JP JP3273871A patent/JPH05111615A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109200763A (en) * | 2018-09-30 | 2019-01-15 | 北京国电龙源环保工程有限公司 | A kind of flue gas desulphurization system loop slurry detection system |
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|---|---|---|---|
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