JPH0355171B2 - - Google Patents
Info
- Publication number
- JPH0355171B2 JPH0355171B2 JP58041416A JP4141683A JPH0355171B2 JP H0355171 B2 JPH0355171 B2 JP H0355171B2 JP 58041416 A JP58041416 A JP 58041416A JP 4141683 A JP4141683 A JP 4141683A JP H0355171 B2 JPH0355171 B2 JP H0355171B2
- Authority
- JP
- Japan
- Prior art keywords
- air
- amount
- oxidation tower
- calcium sulfite
- 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 - Lifetime
Links
- 230000003647 oxidation Effects 0.000 claims description 63
- 238000007254 oxidation reaction Methods 0.000 claims description 63
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 claims description 40
- 235000010261 calcium sulphite Nutrition 0.000 claims description 40
- 238000010521 absorption reaction Methods 0.000 claims description 28
- 239000002002 slurry Substances 0.000 claims description 25
- 238000006477 desulfuration reaction Methods 0.000 claims description 18
- 230000023556 desulfurization Effects 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 17
- 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
- 239000007789 gas Substances 0.000 claims description 16
- 239000010440 gypsum Substances 0.000 claims description 10
- 229910052602 gypsum Inorganic materials 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 9
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 4
- 235000019738 Limestone Nutrition 0.000 claims description 4
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 4
- 239000004571 lime Substances 0.000 claims description 4
- 239000006028 limestone Substances 0.000 claims description 4
- 238000000605 extraction Methods 0.000 claims description 3
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 2
- 230000001590 oxidative effect Effects 0.000 description 12
- 230000002745 absorbent Effects 0.000 description 10
- 239000002250 absorbent Substances 0.000 description 10
- 238000010586 diagram Methods 0.000 description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000011505 plaster Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 230000003584 silencer Effects 0.000 description 1
Description
【発明の詳細な説明】
本発明は湿式排煙脱硫装置の制御方法に係り、
特に酸化用空気圧縮機の動力費を低減するに好適
な酸化塔の制御方法に関するものである。[Detailed Description of the Invention] The present invention relates to a method for controlling a wet flue gas desulfurization equipment,
In particular, the present invention relates to an oxidation tower control method suitable for reducing the power cost of an oxidation air compressor.
現在、ボイラ等の排ガスの処理に使用されてい
る排煙脱硫装置の中では、石灰石、石灰等を吸収
剤（以後、石灰石、石灰等を吸収剤、また、吸収
塔に供給する吸収剤を含むスラリを吸収液スラリ
と称する）として用い、ボイラ等の排ガス中の硫
黄酸化物（SOx）を吸収して生成した亜硫酸カル
シウムを酸化して、硫酸カルシウム、すなわち石
膏として回収する湿式排煙脱硫装置が一般的に用
いられている。 Currently, flue gas desulfurization equipment used to treat flue gas from boilers, etc. uses limestone, lime, etc. as an absorbent (hereinafter referred to as "limestone, lime, etc. as an absorbent", and also includes an absorbent supplied to an absorption tower). A wet flue gas desulfurization device that uses a slurry (absorbing liquid slurry) to oxidize calcium sulfite produced by absorbing sulfur oxides ( SO is commonly used.
従来の湿式排煙脱硫装置の系統図を第１図に示
す。ボイラ等の排ガスは煙道１を通つて除じん塔
２に導入され、ここで除じん塔循環タンク５から
循環ポンプ４により供給される循環液との気液接
触により、飽和温度まで冷却されると同時に、排
ガス中に含有しているダストが除去された後、吸
収塔７に送られる。吸収塔７で循環ポンプ１０に
より配管４０を通つて供給される吸収液スラリと
の気液接触により排ガス中のSOxが吸収、除去さ
れた後、デミスタ８で同伴ミストが除去され、煙
道９から排出される。 Figure 1 shows a system diagram of a conventional wet flue gas desulfurization system. Exhaust gas from a boiler or the like is introduced into a dust removal tower 2 through a flue 1, where it is cooled to a saturation temperature by gas-liquid contact with circulating liquid supplied from a dust removal tower circulation tank 5 by a circulation pump 4. At the same time, the dust contained in the exhaust gas is removed and then sent to the absorption tower 7. After SOx in the exhaust gas is absorbed and removed by gas-liquid contact with the absorption liquid slurry supplied through the pipe 40 by the circulation pump 10 in the absorption tower 7, the entrained mist is removed in the demister 8, and the flue 9 is discharged from.
吸収塔７にはボイラ等の排ガス中から吸収、除
去すべきSOx量に応じて、吸収剤スラリが吸収剤
スラリタンク２５からポンプ２６により、供給さ
れる。一方、SOxを吸収し、生成した亜硫酸カル
シウムを含有するスラリが吸収塔抜き出しポンプ
１１により、SOxの吸収量に見合つて抜き出さ
れ、酸化塔供給タンク１３に供給される。酸化塔
供給タンク１３に入つたスラリは硫酸２８との反
応により、未反応の吸収剤が石膏になると共に、
PH調整された後、ポンプ１４により、酸化塔１５
に送られ、スラリ中の亜流酸カルシウムは酸化用
空気圧縮機２１から供給される空気により酸化さ
れ、石膏となり石膏シツクナ１６を経て、石膏ス
ラリタンク１７に貯蔵され、さらにポンプ１８に
より脱水機１９に送られ、脱水された後、石膏２
０として回収される。また、酸化塔に供給された
空気は塔頂から抜き出された吸収塔７に送られ
る。なお、図中、３は排水ポンプ、６はミストエ
リミネータ、１２は補給水、２３は濾過水タン
ク、２４は濾過水ポンプ、２７は吸収剤を示す。 Absorbent slurry is supplied to the absorption tower 7 from an absorbent slurry tank 25 by a pump 26 according to the amount of SO x to be absorbed and removed from exhaust gas from a boiler or the like. On the other hand, a slurry containing calcium sulfite produced by absorbing SO x is extracted by an absorption tower extraction pump 11 in proportion to the amount of SO x absorbed, and is supplied to an oxidation tower supply tank 13 . The slurry that entered the oxidation tower supply tank 13 reacts with sulfuric acid 28, and the unreacted absorbent becomes gypsum, and
After the pH is adjusted, the oxidation tower 15 is pumped by the pump 14.
The calcium sulfite in the slurry is oxidized by the air supplied from the oxidizing air compressor 21 and becomes gypsum, which is stored in the gypsum slurry tank 17 via the gypsum tanker 16, and further transferred to the dehydrator 19 by the pump 18. After being sent and dehydrated, plaster 2
It is recovered as 0. Moreover, the air supplied to the oxidation tower is sent to the absorption tower 7, which is extracted from the top of the tower. In addition, in the figure, 3 is a drainage pump, 6 is a mist eliminator, 12 is make-up water, 23 is a filtered water tank, 24 is a filtered water pump, and 27 is an absorbent.
次に脱硫装置内での主な反応を述べる。 Next, we will discuss the main reactions inside the desulfurization equipment.
吸収塔７内においては、吸収されたSO2は(1)式
に示すように吸収剤と反応し、亜硫酸カルシウム
となり、更にその一部は排ガス中に含有するO2
により、(2)式に示すように酸化されて石膏とな
る。 In the absorption tower 7, the absorbed SO 2 reacts with the absorbent as shown in equation (1) to become calcium sulfite, and a part of it is converted into O 2 contained in the exhaust gas.
As a result, it is oxidized and becomes gypsum as shown in equation (2).
CaSO3＋SO2＋１／２H2O→CaSO3・１／２H2O＋CO2
……(1)
CaSO3・１／２H2O＋１／２O2＋３／２H2O→CaSO4・
2H2O ……(2)
従つて吸収塔７から抜き出されるスラリの組成
は、上記の亜硫酸カルシウム、石膏および未反応
の吸収剤からなる。このスラリは酸化塔供給タン
ク１３に送られ、タンク内で硫酸と反応し石膏と
なる。次に酸化塔１５で上記(2)式の反応におり酸
化され、亜硫酸カルシウムはほとんどすべて石膏
となる。CaSO 3 +SO 2 +1/2H 2 O→CaSO 3・1/2H 2 O+CO 2 …(1) CaSO 3・1/2H 2 O+1/2O 2 +3/2H 2 O→CaSO 4・2H 2 O …( 2) Therefore, the composition of the slurry extracted from the absorption tower 7 consists of the above-mentioned calcium sulfite, gypsum, and unreacted absorbent. This slurry is sent to the oxidation tower supply tank 13, where it reacts with sulfuric acid and becomes gypsum. Next, in the oxidation tower 15, the calcium sulfite is oxidized in the reaction of formula (2) above, and almost all of the calcium sulfite is converted to gypsum.
上記のような装置系統において、従来の酸化塔
１５への空気の供給は、酸化塔１５に流入するス
ラリ量および組成にかかわらず、圧力、供給量共
一定で行つていた。 In the device system as described above, conventional air supply to the oxidation tower 15 was carried out at a constant pressure and supply amount regardless of the amount and composition of the slurry flowing into the oxidation tower 15.
しかし、ボイラの負荷変動や燃料中のＳ分の変
動に伴ない、脱硫装置に流入するSO2量は変動す
るため、吸収塔から抜き出される亜硫酸カルシウ
ムの量も変動する。例えば低負荷時または燃料中
のＳ分が減少すれば、生成する亜硫酸カルシウム
の量も減少する。また入口ガス中のO2濃度によ
り、上記(2)式の酸化速度が変化し、O2濃度が高
い程、吸収系の酸化速度が大きくなり、抜き出さ
れる亜硫酸カルシウムの量は減少する。 However, the amount of SO 2 flowing into the desulfurization equipment fluctuates as the boiler load fluctuates and the S content in the fuel fluctuates, so the amount of calcium sulfite extracted from the absorption tower also fluctuates. For example, when the load is low or the S content in the fuel decreases, the amount of calcium sulfite produced also decreases. Furthermore, the oxidation rate in equation (2) above changes depending on the O 2 concentration in the inlet gas, and the higher the O 2 concentration, the greater the oxidation rate in the absorption system, and the smaller the amount of calcium sulfite extracted.
このように、ボイラの運転状態の変動により、
酸化塔１５に流入する亜硫酸カルシウム量が変動
するにもかかわらず、常に一定の酸化用空気を空
気圧縮機２１から供給することは、低負荷時にお
いて、空気圧縮機の動力を不必要に消費すること
になり、極めて不経済である。 In this way, due to fluctuations in boiler operating conditions,
Even though the amount of calcium sulfite flowing into the oxidation tower 15 fluctuates, constantly supplying a constant amount of oxidizing air from the air compressor 21 consumes the power of the air compressor unnecessarily at low load times. This is extremely uneconomical.
本発明の目的は、上記従来技術の欠点をなく
し、酸化塔に供給される亜硫酸カルシウムの酸化
用の空気量を低減し、これにより空気圧縮機等の
動力費を低減することができる排煙脱硫装置の制
御方法を提供することにある。 The purpose of the present invention is to provide flue gas desulfurization which eliminates the drawbacks of the above-mentioned prior art, reduces the amount of air for oxidizing calcium sulfite supplied to the oxidation tower, and thereby reduces power costs for air compressors, etc. The object of the present invention is to provide a method for controlling a device.
本発明は、排ガス中のSOxを石灰石または石灰
等を含むスラリよりなる吸収液スラリを用いて吸
収し、生成した亜硫酸カルシウムを酸化塔で空気
により酸化させ石膏として回収する湿式排煙脱硫
装置において、酸化塔に供給される亜硫酸カルシ
ウムの量に見合つて、酸化塔に供給する空気量ま
たは／および空気圧力を制御することを特徴とす
るものである。 The present invention provides a wet flue gas desulfurization device that absorbs SO x in flue gas using an absorption liquid slurry made of limestone or slurry containing lime, etc., and oxidizes the generated calcium sulfite with air in an oxidation tower and recovers it as gypsum. The method is characterized in that the amount of air and/or air pressure supplied to the oxidation tower is controlled in accordance with the amount of calcium sulfite supplied to the oxidation tower.
本発明において、酸化塔供給空気の流量または
圧力を調節する方法としては、供給空気源の空気
圧縮機出口に空気槽を設け、該空気槽の圧力設定
値により、空気圧縮機をロード、アンロードの繰
返し運転させたり、空気圧縮機を複数台設置し、
運転台数を選択して運転する方法が好ましい。 In the present invention, as a method of adjusting the flow rate or pressure of the oxidation tower supply air, an air tank is provided at the outlet of the air compressor of the supply air source, and the air compressor is loaded and unloaded according to the pressure setting value of the air tank. by repeatedly operating air compressors, installing multiple air compressors,
A method in which the number of vehicles to be operated is selected and operated is preferable.
また酸化塔に供給される亜硫酸カルシウムの量
を求めるには、吸収塔に流入する排ガス量、SOx
濃度、O2濃度および吸収塔からの抜出しスラリ
量から算出するか、また酸化塔出口空気のO2濃
度により算出する方法があげられる。 In addition, to determine the amount of calcium sulfite supplied to the oxidation tower, the amount of exhaust gas flowing into the absorption tower, SO x
Examples of methods include calculating from the concentration, O 2 concentration, and amount of slurry extracted from the absorption tower, or calculating from the O 2 concentration of the air at the outlet of the oxidation tower.
上記酸化塔に供給される亜硫酸カルシウムの量
は、酸化塔出口スラリのPHにより補正されること
が望ましい。 It is desirable that the amount of calcium sulfite supplied to the oxidation tower is corrected based on the pH of the slurry at the outlet of the oxidation tower.
以下、本発明を図面により、さらに詳細に説明
する。第２図は本発明の制御方法を示す酸化塔回
りの装置系統図、第３図および第３Ａ図は、本発
明における酸化用空気の供給量の制御系統図であ
る。 Hereinafter, the present invention will be explained in more detail with reference to the drawings. FIG. 2 is a system diagram of equipment around an oxidizing tower showing the control method of the present invention, and FIGS. 3 and 3A are system diagrams of controlling the supply amount of oxidizing air in the present invention.
この実施例は、入口排ガス量１００とSO2濃度
１０１の積算により求めた吸収SO2量から生成す
る亜硫酸カルシウム量を算出し、これに対し、入
口排ガス中のO2濃度から決まる吸収系で酸化さ
れる亜硫酸カルシウムの量を補正し、更に吸収塔
内での保有液量と吸収塔からの抜出し量から決ま
る時間遅れ要素を加味することにより、吸収塔か
ら抜き出される亜硫酸カルシウムの量を求め、こ
の亜硫酸カルシウム量を先行信号とし、必要に応
じて酸化塔出口スラリのPH１０８を補正信号とし
て、酸化塔への空気量を調節弁１１１で制御する
ものである。 In this example, the amount of calcium sulfite produced is calculated from the absorbed SO 2 amount obtained by integrating the inlet exhaust gas amount 100 and the SO 2 concentration 101, and the amount of calcium sulfite is oxidized in the absorption system determined from the O 2 concentration in the inlet exhaust gas. The amount of calcium sulfite extracted from the absorption tower is determined by correcting the amount of calcium sulfite extracted from the absorption tower, and further taking into account the time delay factor determined from the amount of liquid retained in the absorption tower and the amount extracted from the absorption tower. This amount of calcium sulfite is used as a leading signal, and the PH108 of the slurry at the outlet of the oxidation tower is used as a correction signal as needed to control the amount of air to the oxidation tower by the control valve 111.
先ず第２図において、酸化塔１５に供給される
空気は、吸込弁１１３から空気圧縮機２１に吸入
され、空気槽２２で一旦貯留された後、酸化塔入
口空気圧力調節計１０７および空気圧力調節弁１
１０により一定圧力に制御され、酸化塔１５に供
給される。なお、１０５は空気流量計、１０６は
圧力スイツチ、１０８はPH計、１１１は空気流量
調節弁、１１２は放風弁、１１４は放風サイレン
サである。この場合の空気量の制御方法は、第３
図に示すように、入口排ガス流量計１００とSO2
濃度計１０１の信号を掛算器１２１で処理して吸
収SO2量を求め、これを定数を掛けて生成する亜
硫酸カルシウム量を算出し、一方、O2濃度計１
０２で検出した排ガス中の酸素濃度から関数発生
器１２５および掛算器１２１で吸収塔内で酸化さ
れる亜硫酸カルシウムの量を求め、加算器１２２
で前記排ガス中のSO2濃度から求めた亜硫酸カル
シウム量から差し引いて補正する。この補正した
生成亜硫酸カルシウム量qo（mol／ｈ）に対し、
吸収塔から抜き出される亜硫酸カルシウム量ｑ
（mol／ｈ）はタンクの保有液量Ｖ（）、吸収塔
からの抜出しスラリ量Ｑ（／ｈ）から決まるタ
ンクの１時遅れの時定数Ｑ／Ｖを用いて
ｑ＝Ｑ／Ｖ∫（qo−ｑ）dt
として求められる。これは本図に示す通り加算器
１３０、積分器１３１、掛算器１３２を用いて算
出することができる。上述の通り求めた亜硫酸カ
ルシウム量を先行信号とし、関数発生器１２６で
酸化塔１５に入る必要空気量信号を設定する。こ
のとき、酸化塔出口スラリのPH値をPH計１０８で
検出し、反応完結の目安として予め設定された調
節計１２０の設定値と比較し、その偏差を関数発
生器１２４で空気量信号に変換し、前記先行空気
量信号を補正する。この空気量信号を加算器１２
２で加算したものを設定値とし、酸化塔空気流量
計１０５で検出された空気量が設定値に近ずくよ
うに調節計１２７を介して空気流量調節弁１１１
を制御する。 First, in FIG. 2, air supplied to the oxidation tower 15 is sucked into the air compressor 21 from the suction valve 113, and after being temporarily stored in the air tank 22, the air is sent to the oxidation tower inlet air pressure controller 107 and the air pressure controller. Valve 1
The pressure is controlled to be constant by the oxidation tower 10 and supplied to the oxidation tower 15. In addition, 105 is an air flow meter, 106 is a pressure switch, 108 is a PH meter, 111 is an air flow control valve, 112 is a blow-off valve, and 114 is a blow-off silencer. In this case, the air amount control method is as follows.
As shown in the figure, the inlet exhaust gas flow meter 100 and the SO 2
The signal from the densitometer 101 is processed by a multiplier 121 to obtain the amount of SO 2 absorbed, and this is multiplied by a constant to calculate the amount of calcium sulfite produced.
The amount of calcium sulfite oxidized in the absorption tower is calculated from the oxygen concentration in the exhaust gas detected in step 02 using a function generator 125 and a multiplier 121.
Then, the amount of calcium sulfite determined from the SO 2 concentration in the exhaust gas is subtracted and corrected. For this corrected amount of calcium sulfite produced qo (mol/h),
Amount of calcium sulfite extracted from the absorption tower q
(mol/h) is determined by the amount of liquid held in the tank V() and the amount of slurry extracted from the absorption tower Q(/h), using the time constant Q/V of the tank with a one-hour lag. q=Q/V∫( qo−q)dt. This can be calculated using an adder 130, an integrator 131, and a multiplier 132 as shown in the figure. The amount of calcium sulfite determined as described above is used as a preceding signal, and the function generator 126 sets a signal for the amount of air required to enter the oxidation tower 15. At this time, the PH value of the slurry at the outlet of the oxidation tower is detected by the PH meter 108, compared with the preset value of the controller 120 as a guide for completion of the reaction, and the deviation is converted into an air amount signal by the function generator 124. and corrects the preceding air amount signal. This air amount signal is added to the adder 12.
2 is set as the set value, and the air flow rate control valve 111 is adjusted via the controller 127 so that the air amount detected by the oxidation tower air flow meter 105 approaches the set value.
control.
ここで酸化塔入口空気圧力は、第２図および第
３Ａ図に示すように調節計１０７および１２８を
介して調節弁１１０により一定に制御されるが、
更に酸化用空気圧縮機出口には空気槽２２が設け
られ、空気槽２２の圧力スイツチ１０６により、
空気圧縮機２１がロードまたはアンロード運転さ
れ、アンロード運転のときは空気圧縮機２１の吸
込弁１１３および放風弁１１２が全閉される。 Here, the oxidation tower inlet air pressure is controlled to be constant by the control valve 110 via the controllers 107 and 128, as shown in FIGS. 2 and 3A.
Furthermore, an air tank 22 is provided at the outlet of the oxidizing air compressor, and a pressure switch 106 of the air tank 22 allows
The air compressor 21 is operated in a loading or unloading operation, and during the unloading operation, the suction valve 113 and the blowoff valve 112 of the air compressor 21 are fully closed.
以上のような制御方式を行なうことにより、低
負荷時において、酸化用空気の必要量が減少した
場合、アンロード時間を長くすることにより、空
気圧縮機の電力量を低減することができる。例え
ば、下記の条件において本発明を実施した場合、
空気圧縮機の動力を１日3240KWH、年間で
972000KWH低減することができる。 By performing the above-described control method, when the required amount of oxidizing air is reduced during low load, the amount of electric power of the air compressor can be reduced by lengthening the unloading time. For example, if the present invention is implemented under the following conditions,
The power of the air compressor is 3240KWH per day, per year.
Can be reduced by 972000KWH.
実施条件
(1) 脱硫装置の条件
入口ガス量 1628000Nm3／ｈ
入口SO2濃度 550ppm
脱硫率 90％
O2濃度 2.7％
(2) 運転条件
１日の運転負荷パターン
100％負荷 12時間
20％負荷 12時間
次に第４図は、本発明の他の実施例を示す酸化
塔の制御系統図である。これは、負荷変動に応じ
て酸化塔の圧力を調整するもので、上記実施例と
同様な方法で算出した吸収塔から抜出される亜硫
酸カルシウムの量を先行信号とし、酸化塔１５出
口スラリのPHを補正信号とし、さらに圧力調節計
１０４，１０７の空気圧力の設定値を変えること
により、酸化塔圧力調整弁１０９および／または
酸化塔入口空気圧力調整弁１１０を制御し、この
圧力設定値に応じて空気圧縮機出口の空気槽２２
の圧力設定値を複数個設けた圧力スイツチ１０６
の切換えにより、空気圧縮機２１をロード、アン
ロード運転させるものである。この実施例によつ
ても低負荷時には圧縮機のアンドロード時間を長
くすることができるため、電力消費量を低減する
ことができる。Implementation conditions (1) Desulfurization equipment conditions Inlet gas volume 1628000Nm 3 /h Inlet SO 2 concentration 550ppm Desulfurization rate 90% O 2 concentration 2.7% (2) Operating conditions Daily operating load pattern 100% load 12 hours 20% load 12 Time Next, FIG. 4 is a control system diagram of an oxidation tower showing another embodiment of the present invention. This is to adjust the pressure of the oxidation tower according to load fluctuations, and uses the amount of calcium sulfite extracted from the absorption tower calculated in the same manner as in the above example as a leading signal, and the pH of the slurry at the outlet of the oxidation tower 15. is used as a correction signal, and by changing the air pressure settings of the pressure regulators 104 and 107, the oxidation tower pressure adjustment valve 109 and/or the oxidation tower inlet air pressure adjustment valve 110 are controlled, and the oxidation tower inlet air pressure adjustment valve 110 is controlled according to this pressure setting value. Air tank 22 at the air compressor outlet
Pressure switch 106 with multiple pressure setting values
By switching, the air compressor 21 is operated to load or unload. Also in this embodiment, the unload time of the compressor can be lengthened when the load is low, so power consumption can be reduced.
上記実施例においては、空気量を制御する信号
として、酸化塔１５入口の亜硫酸カルシウムの量
を、脱硫装置入口ガス量およびガス中のSO2濃
度、O2濃度および吸収塔保有液量と抜出量（滞
留時間）から求めたが、これに代り、酸化塔出口
空気配管にO2濃度計を設置し、該酸化塔出口空
気中のO2濃度を上記制御信号として使用するこ
とができる。これは、酸化塔で酸化される亜硫酸
カルシウムの量は消費されるO2量と比例するた
め、酸化塔出口のO2濃度を設定値に保つ方法に
よつても上記実施例と同様の効果を得ることがで
きるからである。 In the above embodiment, the amount of calcium sulfite at the inlet of the oxidation tower 15 is used as a signal to control the amount of air, and the amount of calcium sulfite at the inlet of the oxidation tower 15 is expressed as However, instead of this, it is possible to install an O 2 concentration meter in the oxidation tower outlet air piping and use the O 2 concentration in the oxidation tower outlet air as the control signal. This is because the amount of calcium sulfite oxidized in the oxidation tower is proportional to the amount of O 2 consumed, so the same effect as in the above example can be obtained by keeping the O 2 concentration at the outlet of the oxidation tower at the set value. Because you can get it.
また、酸化用空気圧縮機を複数台設置し、酸化
塔に供給される亜硫酸カルシウムの量により、運
転台数を制御することによつても酸化用空気圧縮
機の動力の大幅な低減が可能になる。 Additionally, by installing multiple oxidizing air compressors and controlling the number of units in operation depending on the amount of calcium sulfite supplied to the oxidizing tower, it is possible to significantly reduce the power required for the oxidizing air compressors. .
以上、本発明によれば、酸化塔に流入する生成
亜硫酸カルシウムの量に応じて、酸化用空気の圧
力および／または流量を変化させることにより、
低負荷時の空気圧縮機の動力を低減することがで
きる。 As described above, according to the present invention, by changing the pressure and/or flow rate of the oxidizing air according to the amount of produced calcium sulfite flowing into the oxidizing tower,
The power of the air compressor during low load can be reduced.
第１図は、本発明が適用される排煙脱硫装置の
系統図、第２図は、本発明の実施例を示す酸化塔
回りの系統図、第３図、第３Ａ図は、酸化塔の空
気供給量の制御系統図、第４図は、本発明の他の
実施例を示す酸化塔の空気供給量の制御系統図で
ある。
７……吸収塔、１３……酸化塔供給タンク、１
５……酸化塔、２１……酸化用空気圧縮機、２５
……吸収剤スラリタンク、１００……排ガス流量
計、１０１……SOx濃度計、１０２……O2濃度
計、１０３……吸収塔抜出流量計、１０４……酸
化塔圧力調節計、１０５……酸化塔空気流量計、
１０８……PH計、１１１……酸化塔空気。
Fig. 1 is a system diagram of a flue gas desulfurization equipment to which the present invention is applied, Fig. 2 is a system diagram of an oxidation tower showing an embodiment of the present invention, and Figs. 3 and 3A are diagrams of an oxidation tower. FIG. 4 is a diagram showing a control system for controlling the amount of air supplied to an oxidation tower showing another embodiment of the present invention. 7... Absorption tower, 13... Oxidation tower supply tank, 1
5...Oxidation tower, 21...Oxidation air compressor, 25
... Absorbent slurry tank, 100 ... Exhaust gas flow meter, 101 ... SO x concentration meter, 102 ... O 2 concentration meter, 103 ... Absorption tower extraction flow meter, 104 ... Oxidation tower pressure regulator, 105 ... Oxidation tower air flow meter,
108...PH meter, 111...Oxidation tower air.
Claims (1)
を石灰石または石灰等を含むスラリよりなる吸収
液スラリを用いて吸収し、生成した亜硫酸カルシ
ウムを酸化塔で空気により酸化させ石膏として回
収する湿式排煙脱硫装置の制御方法において、酸
化塔に供給される亜硫酸カルシウムの量に見合つ
て、酸化塔に供給する空気量または／および空気
圧力を制御することを特徴とする湿式排煙脱硫装
置の制御方法。 ２ 特許請求の範囲第１項において、前記の酸化
塔供給空気の流量または圧力を調節する手段とし
て、供給空気源の空気圧縮機出口に空気槽を設
け、該空気槽の圧力設定値により、空気圧縮機を
ロード、アンロードの繰返し運転させることを特
徴とする湿式排煙脱硫装置の制御方法。 ３ 特許請求の範囲第１項において、酸化塔供給
空気の流量を調節する手段として、空気圧縮機を
複数台設置し、運転台数によつて流量を制御する
ことを特徴とする湿式排煙脱硫装置の制御方法。 ４ 特許請求の範囲第１項ないし第３項のいずれ
かにおいて、酸化塔に供給される亜硫酸カルシウ
ムの量は、吸収塔に流入する排ガス量、SOx濃
度、O2濃度および吸収塔からの抜出しスラリ量
から算出されることを特徴とする湿式排煙脱硫装
置の制御方法。 ５ 特許請求の範囲第１項ないし第３項のいずれ
かにおいて、酸化塔に供給される亜硫酸カルシウ
ムの量は、酸化塔出口空気のO2濃度により算出
されることを特徴とする湿式排煙脱硫装置の制御
方法。 ６ 特許請求の範囲第４項または第５項におい
て、酸化塔に供給される亜硫酸カルシウムの量
は、酸化塔出口スラリのPHにより補正されること
を特徴とする湿式排煙脱硫装置の制御方法。[Claims] 1. Sulfur oxides in exhaust gas (hereinafter referred to as SO x )
In a control method for a wet flue gas desulfurization equipment, in which calcium sulfite is absorbed using an absorption liquid slurry made of limestone or slurry containing lime, etc., and the generated calcium sulfite is oxidized with air in an oxidation tower and recovered as gypsum, the calcium sulfite that is supplied to the oxidation tower is 1. A method for controlling a wet flue gas desulfurization equipment, which comprises controlling the amount and/or air pressure of air supplied to an oxidation tower in accordance with the amount of calcium sulfite. 2. In claim 1, as a means for adjusting the flow rate or pressure of the air supplied to the oxidation tower, an air tank is provided at the outlet of the air compressor of the supply air source, and the air is adjusted according to the pressure setting value of the air tank. A method for controlling a wet flue gas desulfurization equipment, characterized by repeatedly loading and unloading a compressor. 3. A wet flue gas desulfurization device according to claim 1, characterized in that a plurality of air compressors are installed as means for adjusting the flow rate of the air supplied to the oxidation tower, and the flow rate is controlled depending on the number of operating units. control method. 4. In any one of claims 1 to 3, the amount of calcium sulfite supplied to the oxidation tower depends on the amount of exhaust gas flowing into the absorption tower, the SO x concentration, the O 2 concentration, and the extraction from the absorption tower. A method for controlling a wet flue gas desulfurization device, characterized in that calculation is performed from an amount of slurry. 5. The wet flue gas desulfurization method according to any one of claims 1 to 3, characterized in that the amount of calcium sulfite supplied to the oxidation tower is calculated based on the O 2 concentration of the air at the outlet of the oxidation tower. How to control the device. 6. A method for controlling a wet flue gas desulfurization apparatus according to claim 4 or 5, wherein the amount of calcium sulfite supplied to the oxidation tower is corrected based on the pH of the slurry at the outlet of the oxidation tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58041416A JPS59169523A (en) | 1983-03-15 | 1983-03-15 | Control of wet waste gas desulfurization apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58041416A JPS59169523A (en) | 1983-03-15 | 1983-03-15 | Control of wet waste gas desulfurization apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59169523A JPS59169523A (en) | 1984-09-25 |
| JPH0355171B2 true JPH0355171B2 (en) | 1991-08-22 |
Family
ID=12607747
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58041416A Granted JPS59169523A (en) | 1983-03-15 | 1983-03-15 | Control of wet waste gas desulfurization apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59169523A (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61150032U (en) * | 1985-03-11 | 1986-09-17 | ||
| JPS6233531A (en) * | 1985-08-05 | 1987-02-13 | Mitsubishi Metal Corp | Stack gas desulfurization device |
| JPH0829217B2 (en) * | 1987-01-14 | 1996-03-27 | バブコツク日立株式会社 | Oxidation tower air flow rate control method in wet desulfurization equipment |
| JP5268320B2 (en) * | 2007-10-15 | 2013-08-21 | 中国電力株式会社 | Method for suppressing unreacted surplus slurry in exhaust gas desulfurization unit |
| CN102020305B (en) * | 2010-12-27 | 2012-12-05 | 马鞍山钢铁股份有限公司 | Method for preparing gypsum by using semi-dry method to sinter flue gas desulfurization byproduct |
| CN102512917B (en) * | 2011-12-14 | 2014-03-26 | 攀钢集团有限公司 | Control system for renewable flue gas desulfurization system and control method |
| CN106039947A (en) * | 2016-07-29 | 2016-10-26 | 无锡研奥电子科技有限公司 | Limestone flue gas desulfurization control system |
-
1983
- 1983-03-15 JP JP58041416A patent/JPS59169523A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS59169523A (en) | 1984-09-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109092045B (en) | Limestone-gypsum method flue gas desulfurization slurry oxidation control method | |
| JPH06182148A (en) | Controlling apparatus for wet flue gas desulfurization apparatus | |
| JPH0355171B2 (en) | ||
| JPH0352097Y2 (en) | ||
| JPH1085549A (en) | Wet exhaust gas desulfurization device and exhaust gas desulfutization | |
| JPH0919623A (en) | Wet type waste gas desulfurizing method and device therefor | |
| JP3651918B2 (en) | Control method of wet flue gas desulfurization equipment | |
| JP2933664B2 (en) | Absorbent PH control unit for wet flue gas desulfurization unit | |
| JP2883365B2 (en) | Control device for wet flue gas desulfurization unit | |
| JPS58112025A (en) | Controlling method of waste gas desulfurizing apparatus | |
| JPS63294928A (en) | Device for controlling wet exhaust gas desulfurizer | |
| JPH0573452B2 (en) | ||
| JPH0417691B2 (en) | ||
| JP3519582B2 (en) | Flue gas desulfurization device and flue gas desulfurization method | |
| JPH11244648A (en) | Control of absorbent slurry flow rate of wet stack gas desulfurizer and device therefor | |
| JP2798973B2 (en) | Exhaust gas desulfurization equipment | |
| JP3991132B2 (en) | Sludge acceptance control method and apparatus for flue gas desulfurization equipment absorption tower | |
| JPS59102425A (en) | Supply method of adsorbent for wet type stack gas desulfurizer | |
| JPS6244733Y2 (en) | ||
| JPH10202050A (en) | Suppressing method of oxidation of selenium in flue gas desulfurization apparatus and device therefor | |
| JP2510583B2 (en) | Exhaust gas treatment device | |
| JPH0691940B2 (en) | Oxidizing air control method for wet flue gas desulfurization equipment | |
| JPH1199316A (en) | Method of controlling sludge in waste water for wet flue gas desulfurizer | |
| JPH10296047A (en) | Method and apparatus for flue gas desulfurization | |
| JP2003126650A (en) | Control method and apparatus for wet flue gas desulfurization plant |