JPH0691940B2 - Oxidizing air control method for wet flue gas desulfurization equipment - Google Patents
Oxidizing air control method for wet flue gas desulfurization equipmentInfo
- Publication number
- JPH0691940B2 JPH0691940B2 JP61047026A JP4702686A JPH0691940B2 JP H0691940 B2 JPH0691940 B2 JP H0691940B2 JP 61047026 A JP61047026 A JP 61047026A JP 4702686 A JP4702686 A JP 4702686A JP H0691940 B2 JPH0691940 B2 JP H0691940B2
- Authority
- JP
- Japan
- Prior art keywords
- amount
- oxidizing air
- air
- flue gas
- slurry
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 230000001590 oxidative effect Effects 0.000 title claims description 35
- 238000006477 desulfuration reaction Methods 0.000 title claims description 30
- 230000023556 desulfurization Effects 0.000 title claims description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 11
- 239000003546 flue gas Substances 0.000 title claims description 11
- 238000000034 method Methods 0.000 title claims description 8
- 239000002002 slurry Substances 0.000 claims description 27
- 239000007789 gas Substances 0.000 claims description 22
- 239000011575 calcium Substances 0.000 claims description 10
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 9
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 claims description 7
- 235000010261 calcium sulphite Nutrition 0.000 claims description 7
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 6
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 5
- 229910052791 calcium Inorganic materials 0.000 claims description 5
- 150000001875 compounds Chemical class 0.000 claims description 4
- 229940043430 calcium compound Drugs 0.000 claims 1
- 150000001674 calcium compounds Chemical class 0.000 claims 1
- 230000002745 absorbent Effects 0.000 description 11
- 239000002250 absorbent Substances 0.000 description 11
- 238000010586 diagram Methods 0.000 description 7
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 6
- 239000010440 gypsum Substances 0.000 description 5
- 229910052602 gypsum Inorganic materials 0.000 description 5
- 239000007788 liquid Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 238000007664 blowing Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 230000000087 stabilizing effect 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
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (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の酸化空気制御方法に係り、
特に循環タンクスラリ液組成安定化をはかることによ
り、脱硫性能を確保するに好適な湿式排煙脱硫装置の酸
化空気制御方法に関するものである。TECHNICAL FIELD The present invention relates to an oxidizing air control method for a wet flue gas desulfurization apparatus,
In particular, the present invention relates to a method for controlling oxidized air in a wet flue gas desulfurization apparatus, which is suitable for ensuring desulfurization performance by stabilizing the composition of a circulation tank slurry liquid.
（従来の技術） 従来、塔内で排ガスをカルシウム系化合物スラリと接触
させるとともに、底部の循環タンク内に空気を吹込んで
硫黄酸化物の吸収によって生じた亜硫酸カルシウムの酸
化を行なう一塔式の湿式排煙脱硫装置が知られている。
その概略系統を第８図に示す。この装置では、ボイラ等
の排ガス１は、煙道14により吸収塔２に導入され循環ポ
ンプ４により供給される吸収剤スラリとの気液接触によ
り排ガス中のダストが除去される。同時に排ガス中のSO
xが吸収、除去され、除去された後、デミスタ５で同伴
ミストが除去され、清浄ガス６が煙道15より排出され
る。ここで、循環タンク３内の吸収剤スラリにはSOxを
吸収し生成した亜硫酸カルシウム等を酸化し、石膏を生
成するためにコンプレッサ13より供給される酸化用空気
10をブロアしている。酸化用空気10は、循環タンク３内
のスラリの沈降防止を目的として設置された攪拌機９の
翼近傍に供給することにより微細気泡化され酸化に使わ
れる。亜硫酸カルシウムを酸化して得られた石膏は石膏
スラリ抜出管12より抜出され回収される。(Prior Art) Conventionally, a one-column wet process in which exhaust gas is brought into contact with a calcium-based compound slurry in a tower and air is blown into a circulation tank at the bottom to oxidize calcium sulfite generated by absorption of sulfur oxides. Flue gas desulfurization devices are known.
The schematic system is shown in FIG. In this apparatus, the exhaust gas 1 from the boiler or the like is removed from the dust in the exhaust gas by gas-liquid contact with the absorbent slurry introduced into the absorption tower 2 by the flue 14 and supplied by the circulation pump 4. At the same time SO in the exhaust gas
After x is absorbed, removed, and removed, entrained mist is removed by the demister 5, and the clean gas 6 is discharged from the flue 15. Here, the absorbent slurry in the circulation tank 3 absorbs SOx to oxidize the generated calcium sulfite and the like, and the oxidizing air supplied from the compressor 13 to generate gypsum.
Blower 10 The oxidizing air 10 is supplied to the vicinity of the blades of the stirrer 9 installed for the purpose of preventing the slurry in the circulation tank 3 from settling, whereby it is made into fine bubbles and used for oxidation. The gypsum obtained by oxidizing calcium sulfite is extracted from the gypsum slurry extraction pipe 12 and collected.
（発明が解決しようとする問題点） 上記従来装置においては、上記攪拌翼９近傍に供給され
る酸化用空気10は常に一定量ブロアされているため、低
負荷時には、必要以上の空気10をブロアすることにな
り、コンプレッサ13動力を必要以上消費するという欠点
を生ずる。(Problems to be Solved by the Invention) In the above-mentioned conventional apparatus, since the oxidizing air 10 supplied near the stirring blade 9 is always blown by a constant amount, when the load is low, more air 10 than necessary is blown. Therefore, there is a drawback that the power of the compressor 13 is consumed more than necessary.
一方、循環タンク３内吸収剤スラリの亜硫酸イオン濃度
は、脱硫性能に大きく影響し、例えば負荷変動時に、吸
収剤スラリ中の亜硫酸イオン濃度が変動すれば、所望の
脱硫率が得られなくなることも起こる。従って、循環タ
ンク３内の吸収剤スラリ液組成（特にカルシウム濃度）
の安定化をはかり、亜硫酸カルシウム濃度を一定に保ち
つつ、コンプレッサ13の動力コストを低減できる制御方
式が要望される。On the other hand, the sulfite ion concentration of the absorbent slurry in the circulation tank 3 has a great influence on the desulfurization performance. For example, if the sulfite ion concentration in the absorbent slurry changes when the load changes, a desired desulfurization rate may not be obtained. Occur. Therefore, the composition of the absorbent slurry liquid in the circulation tank 3 (especially calcium concentration)
There is a demand for a control method capable of reducing the power cost of the compressor 13 while stabilizing the concentration of calcium sulfite and keeping the concentration of calcium sulfite constant.
本発明の目的は、上記した欠点をなくし、負荷変動にも
安定した吸収剤スラリ液組成を確保し、動力コストを低
減できる湿式排煙脱硫装置の酸化空気制御方法を提供す
ることにある。An object of the present invention is to provide an oxidizing air control method for a wet flue gas desulfurization apparatus, which eliminates the above-mentioned drawbacks, secures a stable absorbent slurry composition against load fluctuations, and can reduce power cost.
（問題点を解決するための手段） 要するに本発明は、循環タンク内吸収剤スラリの亜硫酸
イオン濃度を総SOx量または負荷によらず一定とすべ
く、該SOx量または負荷に応じて循環タンク内酸化用空
気流量の制御を行なうようにしたものである。すなわ
ち、本発明は、脱硫塔底部に設置した循環タンク内に貯
えられたカルシウム系化合物スラリを塔内にスプレして
排ガスと接触させ、含有される硫黄酸化物を除去し、一
方、該循環タンク内のカルシウム系化合物スラリ中に空
気を吹込み、硫黄酸化物の吸収によって生ずる亜硫酸カ
ルシウムを酸化する湿式排煙脱硫装置において、前記循
環タンク内のスラリ中に吹込む酸化用空気の量が前記排
ガス中に含まれる総硫黄酸化物量または負荷に対応する
量になるように、前記酸化用空気量を制御することを特
徴とする。(Means for Solving the Problems) In short, the present invention is designed to make the sulfite ion concentration of the absorbent slurry in the circulation tank constant regardless of the total SOx amount or load, and The flow rate of oxidizing air is controlled. That is, the present invention is to spray the calcium-based compound slurry stored in the circulation tank installed at the bottom of the desulfurization tower into the exhaust gas to contact the exhaust gas to remove the contained sulfur oxides, while the circulation tank In a wet flue gas desulfurization device in which air is blown into the calcium-based compound slurry inside and the calcium sulfite generated by absorption of sulfur oxides is oxidized, the amount of oxidizing air blown into the slurry in the circulation tank is the exhaust gas. It is characterized in that the oxidizing air amount is controlled such that the total amount of sulfur oxides contained therein or the amount corresponding to the load is controlled.
以下、本発明が適用される湿式脱硫装置内での反応およ
びそれに関連して本発明の酸化用空気制御の原理につい
て説明する。Hereinafter, the principle of the reaction in the wet desulfurization apparatus to which the present invention is applied and the related control of the oxidizing air of the present invention will be described.
第１図または第８図において、吸収塔２内に導入された
排ガス１は、循環ポンプ４により供給される吸収剤であ
る石灰石スラリとの気液接触により（１）、（２）式の
反応が行われる。In FIG. 1 or FIG. 8, the exhaust gas 1 introduced into the absorption tower 2 reacts with the formulas (1) and (2) by gas-liquid contact with the limestone slurry which is the absorbent supplied by the circulation pump 4. Is done.
SO2＋H2O＝H2SO3 …（１） CaCO3＋2H2SO3＝ Ca(HSO3)2＋CO2＋H2O …（２） 次に、SO2を吸収した吸収剤スラリは、循環タンク３内
において、酸化用空気10と反応し、（３）、（４）式の
反応が行われる。SO 2 + H 2 O = H 2 SO 3 (1) CaCO 3 + 2H 2 SO 3 = Ca (HSO 3 ) 2 + CO 2 + H 2 O (2) Next, the absorbent slurry that absorbed SO 2 is circulated. In the tank 3, it reacts with the oxidizing air 10 to carry out the reactions of the formulas (3) and (4).
Ca(HSO3)2＋O2＝ CaSO4＋H2SO4 …（３） 2CaSO3＋O2＝2CaSO4 …（４） この時、（３）式、（４）式の左辺の酸素O2がそれぞれ
十分であると、それぞれCa(HSO3)2および2CaSO3が全量
反応し、石膏CaSO4を得ることができる。しかしなが
ら、実際には全量反応しないため、循環タンクスラリ中
には、Ca(HSO3)2、2CaSO3が残存することになる。これ
らは、スラリ溶液中では、亜硫酸イオンSO3 2-の形で存
在し、このSO3 2-イオン濃度の高低が脱硫性能に大きく
影響することになる。そこで第１図に示す脱硫装置のパ
イロットプラント（排ガス処理容量600Nm2/H）では、循
環タンクスラリ内の総亜硫酸イオンＴ（Totalの略）SO3
濃度と脱硫率の関係は、例えば第４図のようになる。す
なわち、ある要求される脱硫率を確保するには、Ｔ−SO
3濃度を必要値以下にする必要がある。Ca (HSO 3 ) 2 + O 2 = CaSO 4 + H 2 SO 4 (3) 2CaSO 3 + O 2 = 2CaSO 4 (4) At this time, oxygen O 2 on the left side of the equations (3) and (4) respectively When it is sufficient, Ca (HSO 3 ) 2 and 2CaSO 3 react in the total amount, and gypsum CaSO 4 can be obtained. However, since the total amount does not actually react, Ca (HSO 3 ) 2 and 2CaSO 3 remain in the circulation tank slurry. These exist in the form of sulfite ion SO 3 2− in the slurry solution, and the high or low concentration of this SO 3 2− ion greatly affects the desulfurization performance. Therefore, in the desulfurization equipment pilot plant (exhaust gas treatment capacity 600 Nm 2 / H) shown in Fig. 1, total sulfite ion T (abbreviation of Total) SO 3 in the circulation tank slurry was used.
The relationship between the concentration and the desulfurization rate is, for example, as shown in FIG. That is, in order to secure a certain required desulfurization rate, T-SO
3 It is necessary to keep the concentration below the required value.
また、パイロットプラント試験において、脱硫率、Ｔ−
SO3濃度と酸化空気10供給量の関係を求めると、第５図
のようになる。この結果によると、一定以上の酸化空気
10をブロアすれば、Ｔ−SO3濃度を抑えることができ、
脱硫率も確保できることが分かる。しかしながら、必要
以上に酸化空気をブロアすれば、前述のようにコンプレ
ッサ動力コストを必要以上に消費することになる。In a pilot plant test, the desulfurization rate, T-
The relationship between the SO 3 concentration and the supply amount of oxidizing air 10 is obtained as shown in FIG. According to this result, more than a certain amount of oxidizing air
Blower 10 can reduce the concentration of T-SO 3 ,
It can be seen that the desulfurization rate can be secured. However, if the oxidizing air is blown more than necessary, the compressor power cost will be consumed more than necessary as described above.
一方、（３）式、（４）式の左辺のCa(HSO3)2、2CaSO3の
量は、排ガス中に含まれる総SO2量に依存することか
ら、第６図に示すように総SO2量に対応した量だけの酸
化用空気をブロアすれば、要求する脱硫率を確保できる
ことになる。On the other hand, the amounts of Ca (HSO 3 ) 2 and 2CaSO 3 on the left side of equations (3) and (4) depend on the total amount of SO 2 contained in the exhaust gas. The required desulfurization rate can be secured by blowing the oxidizing air in an amount corresponding to the SO 2 amount.
以下、本発明を実施例によりさらに具体的に説明する。Hereinafter, the present invention will be described more specifically by way of examples.
（実施例） 第１図は、本発明の一実施例を示す湿式排煙脱硫装置の
概略系統図を示す。第２図と異なる点は循環タンク３に
空気をブロアする系統に空気調整弁11を設置した点であ
る。以下、この空気制御方法について説明する。(Example) FIG. 1 is a schematic system diagram of a wet flue gas desulfurization apparatus showing an embodiment of the present invention. The difference from FIG. 2 is that the air regulating valve 11 is installed in the system for blowing air into the circulation tank 3. Hereinafter, this air control method will be described.
第２図は、第１図の装置における酸化用空気制御系を示
したものである。入口SO2濃度計31により入口SO2濃度信
号34、排ガス流量計32により排ガス流量信号35、酸化空
気流量計33により酸化空気流量信号36を計測し、本制御
系の入力とされる。37は掛算器、39は関数発生器、41は
調節計、42は電気／空気変換器である。FIG. 2 shows an oxidizing air control system in the apparatus of FIG. The inlet SO 2 concentration meter 31 measures the inlet SO 2 concentration signal 34, the exhaust gas flow meter 32 measures the exhaust gas flow rate signal 35, and the oxidizing air flow meter 33 measures the oxidizing air flow rate signal 36, which are input to this control system. 37 is a multiplier, 39 is a function generator, 41 is a controller, and 42 is an electric / pneumatic converter.
上記構成において、入口SO2濃度計31により入口SO2濃度
信号34、排ガス流量計32により排ガス流量信号35を計測
し、掛算器37において排ガス中に含まれる総SO2量信号3
8が求められる。一方、循環タンク内亜硫酸イオンSO3 2-
を酸化するのに必要な酸化空気量信号40が関数発生器39
において求められる。関数発生器39には、第６図に示す
関数をデータとしてもっている。そこで、必要酸化空気
量信号40と、酸化空気流量計33より計測される実際の酸
化、空気流量信号36を調節計41において比較、調整し、
電気／空気変換器42を介して空気調整弁11により、酸化
空気流量を制御する。本実施例によれば、総SO2量小す
なわち低負荷時には、少ない酸化空気量で、要求脱硫率
を確保することができ、酸化空気供給のためのコンプレ
ッサ動力を低減することができる。さらに、循環タンク
内スラリのＴ−SO3 2-濃度を一定に制御することにより
負荷変動時に脱硫率制御の安定化に寄与することができ
る。In the above configuration, the inlet SO 2 concentration meter 31 measures the inlet SO 2 concentration signal 34 and the exhaust gas flowmeter 32 measures the exhaust gas flow rate signal 35, and the multiplier 37 measures the total SO 2 amount signal 3 contained in the exhaust gas.
8 is required. On the other hand, sulfite ion SO 3 2- in the circulation tank
Oxidation air quantity signal 40 required to oxidize
Required in. The function generator 39 has the function shown in FIG. 6 as data. Therefore, the required oxidizing air amount signal 40, the actual oxidation measured by the oxidizing air flow meter 33, the air flow rate signal 36 is compared and adjusted in the controller 41,
The flow rate of oxidizing air is controlled by the air regulating valve 11 via the electric / air converter 42. According to this embodiment, when the total SO 2 amount is small, that is, when the load is low, the required desulfurization rate can be secured with a small amount of oxidizing air, and the compressor power for supplying oxidizing air can be reduced. Further, by controlling the T-SO 3 2− concentration of the slurry in the circulation tank to be constant, it is possible to contribute to stabilization of the desulfurization rate control during load fluctuation.
第３図は、第２図の実施例のうち、総SO2量を入口SO2濃
度34および排ガス流量35より求める代わり、ボイラ負荷
発信器43でボイラ負荷を計測し、その信号44を関数発生
器45において第６図の関係で得られる空気量により、酸
化空気流量36を制御するものである。この実施例によれ
ば、計測点および制御系を簡略化することができる。In FIG. 3, instead of obtaining the total SO 2 amount from the inlet SO 2 concentration 34 and the exhaust gas flow rate 35 in the embodiment of FIG. 2 , the boiler load transmitter 43 measures the boiler load and the signal 44 is generated as a function. The oxidizing air flow rate 36 is controlled by the air quantity obtained in the container 45 according to the relationship shown in FIG. According to this embodiment, the measuring point and the control system can be simplified.
以上の実施例では、酸化用空気量を調整弁により制御し
たが、これと同等の手段、例えばコンプレッサ電動機の
回転数によって制御することもできる。In the above embodiments, the amount of oxidizing air was controlled by the adjusting valve, but it is also possible to control it by means equivalent to this, for example, by the rotation speed of the compressor motor.
（発明の効果） 本発明によれば、酸化用空気量を排ガス中の総SO2量ま
たはボイラ負荷をもとに制御するため、第７図破線Ｂに
示す一定量の酸化用空気量に比べ、曲線Ａの酸化用空気
量で済み、ハッチング部Ｃに示す動力を低減することが
できる。また、従来の酸化用空気量一定では、負荷変動
時循環タンク内スラリ中のＴ−SO3 2-濃度も変動するこ
とになり、要求脱硫率を確保できなくなるおそれがある
が、本発明によれば、Ｔ−SO3 2-濃度を一定に制御する
ことができ、要求脱硫率も確保可能となる。(Effect of the Invention) According to the present invention, since the oxidizing air amount is controlled based on the total SO 2 amount in the exhaust gas or the boiler load, compared with the constant amount of oxidizing air shown by the broken line B in FIG. Therefore, the amount of oxidizing air in the curve A is sufficient, and the power shown in the hatched portion C can be reduced. Further, when the conventional amount of oxidizing air is constant, the T-SO 3 2− concentration in the slurry in the circulation tank also fluctuates when the load fluctuates, which may make it impossible to secure the required desulfurization rate. For example, the T-SO 3 2- concentration can be controlled to be constant, and the required desulfurization rate can be secured.
第１図は、本発明に用いる湿式排煙脱硫装置の系統図、
第２図、第３図は、それぞれ本発明による制御系統図、
第４図は、総SO3 2-イオン濃度Ｔ−SO3 2-と脱硫率の関係
を示す図、第５図は、酸化空気供給量と脱硫率およびＴ
−SO3 2-濃度の関係を示す図、第６図は、総SO2量または
負荷と必要酸化空気量の関係を示す図、第７図は、総SO
2量または負荷とコンプレッサ動力の関係を示す図、第
８図は、従来の一塔式の湿式排煙脱硫装置の系統図であ
る。 １…排ガス、２…吸収塔、３…循環タンク、４…循環ポ
ンプ、５…デミスタ、６…清浄ガス、７…吸収剤スラリ
タンク、８…吸収剤スラリ、９…攪拌機、10…空気、11
…空気調整弁、12…石膏スラリ抜出管、13…コンプレッ
サ、14、15…煙道。FIG. 1 is a system diagram of a wet flue gas desulfurization apparatus used in the present invention,
2 and 3 are respectively a control system diagram according to the present invention,
FIG. 4 is a diagram showing the relationship between the total SO 3 2− ion concentration T−SO 3 2− and the desulfurization rate, and FIG. 5 is the oxidizing air supply amount and the desulfurization rate and T.
-SO 3 2- Concentration diagram, Fig. 6 shows the relation between total SO 2 amount or load and required oxidizing air amount, Fig. 7 shows total SO 2 amount
FIG. 8 is a diagram showing a relationship between two amounts or loads and compressor power, and FIG. 8 is a system diagram of a conventional one-column type wet flue gas desulfurization apparatus. 1 ... Exhaust gas, 2 ... Absorption tower, 3 ... Circulation tank, 4 ... Circulation pump, 5 ... Demister, 6 ... Clean gas, 7 ... Absorbent slurry tank, 8 ... Absorbent slurry, 9 ... Stirrer, 10 ... Air, 11
… Air control valve, 12… Gypsum slurry extraction pipe, 13… Compressor, 14, 15… Flue.
Claims (1)
られたカルシウム系化合物スラリを塔内にスプレして排
ガスと接触させ、含有される硫黄酸化物を除去し、一
方、該循環タンク内のカルシウム系化合物スラリ中に空
気を吹込み、硫黄酸化物の吸収によって生ずる亜硫酸カ
ルシウムを酸化する湿式排煙脱硫装置において、前記循
環タンク内のスラリ中に吹込む酸化用空気の量が前記排
ガス中に含まれる総硫黄酸化物量または負荷に対応する
量になるように、前記酸化用空気量を制御することを特
徴とする湿式排煙脱硫装置の酸化空気制御方法。1. A calcium compound slurry stored in a circulation tank installed at the bottom of a desulfurization tower is sprayed into the tower and brought into contact with exhaust gas to remove sulfur oxides contained therein, while the inside of the circulation tank is being sprayed. In the wet flue gas desulfurization device in which air is blown into the calcium-based compound slurry to oxidize calcium sulfite generated by absorption of sulfur oxides, the amount of oxidizing air blown into the slurry in the circulation tank is in the exhaust gas. A method for controlling oxidative air in a wet flue gas desulfurization apparatus, wherein the amount of oxidizing air is controlled so that the total amount of sulfur oxides contained in or the amount corresponding to the load is controlled.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61047026A JPH0691940B2 (en) | 1986-03-04 | 1986-03-04 | Oxidizing air control method for wet flue gas desulfurization equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61047026A JPH0691940B2 (en) | 1986-03-04 | 1986-03-04 | Oxidizing air control method for wet flue gas desulfurization equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62204828A JPS62204828A (en) | 1987-09-09 |
| JPH0691940B2 true JPH0691940B2 (en) | 1994-11-16 |
Family
ID=12763662
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61047026A Expired - Fee Related JPH0691940B2 (en) | 1986-03-04 | 1986-03-04 | Oxidizing air control method for wet flue gas desulfurization equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0691940B2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3326708A4 (en) * | 2015-07-23 | 2018-07-04 | Mitsubishi Hitachi Power Systems, Ltd. | Wet type flue gas desulfurization device and method for operating wet type flue gas desulfurization device |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH084710B2 (en) * | 1986-05-07 | 1996-01-24 | バブコツク日立株式会社 | Operation method of wet flue gas desulfurization equipment |
| JP5081000B2 (en) * | 2008-01-26 | 2012-11-21 | 中国電力株式会社 | Method for controlling the amount of air supplied for oxidation in wet flue gas desulfurization equipment |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5118269A (en) * | 1974-08-06 | 1976-02-13 | Mitsubishi Heavy Ind Ltd | HAIENDATSURYUHOHO |
| JPS5895216U (en) * | 1981-12-18 | 1983-06-28 | 石川島播磨重工業株式会社 | Gas blowing device to absorption tower |
| JPS5913624A (en) * | 1982-07-14 | 1984-01-24 | ゼネラル・エレクトリツク・カンパニイ | By-production of gypsum simultaneously in single smoke exhaust desulfurization apparatus |
| JPS59230620A (en) * | 1983-06-14 | 1984-12-25 | Mitsubishi Heavy Ind Ltd | Slurry concentration control method of wet waste gas desulfurization apparatus |
| JPS6012119A (en) * | 1983-07-01 | 1985-01-22 | Mitsubishi Heavy Ind Ltd | Method for controlling flow amount of compressed air of oxidizing tower in wet type waste gas desulfurizing apparatus |
| JPS6058229A (en) * | 1983-09-09 | 1985-04-04 | Mitsubishi Heavy Ind Ltd | Control of flow amount of compressed air in oxidizing tower |
| JPS60172335A (en) * | 1984-02-20 | 1985-09-05 | Babcock Hitachi Kk | Wet type stack gas desulfurization apparatus |
-
1986
- 1986-03-04 JP JP61047026A patent/JPH0691940B2/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP3326708A4 (en) * | 2015-07-23 | 2018-07-04 | Mitsubishi Hitachi Power Systems, Ltd. | Wet type flue gas desulfurization device and method for operating wet type flue gas desulfurization device |
| US10646820B2 (en) | 2015-07-23 | 2020-05-12 | Mitsubishi Hitachi Power Systems, Ltd. | Wet flue gas desulfurization apparatus and operation method for wet flue gas desulfurization apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62204828A (en) | 1987-09-09 |
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