JPS59160519A - Wet type waste gas desulfurizer - Google Patents
Wet type waste gas desulfurizerInfo
- Publication number
- JPS59160519A JPS59160519A JP58034617A JP3461783A JPS59160519A JP S59160519 A JPS59160519 A JP S59160519A JP 58034617 A JP58034617 A JP 58034617A JP 3461783 A JP3461783 A JP 3461783A JP S59160519 A JPS59160519 A JP S59160519A
- Authority
- JP
- Japan
- Prior art keywords
- absorbent
- slurry
- load
- concn
- 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.)
- Granted
Links
- 239000002912 waste gas Substances 0.000 title abstract 2
- 239000002250 absorbent Substances 0.000 claims abstract description 95
- 230000002745 absorbent Effects 0.000 claims abstract description 94
- 239000002002 slurry Substances 0.000 claims abstract description 75
- 238000010521 absorption reaction Methods 0.000 claims abstract description 33
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 23
- 230000023556 desulfurization Effects 0.000 claims abstract description 23
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 13
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 11
- 239000003546 flue gas Substances 0.000 claims description 11
- 229910052815 sulfur oxide Inorganic materials 0.000 claims description 4
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 2
- 230000007423 decrease Effects 0.000 abstract description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 10
- 238000010586 diagram Methods 0.000 description 9
- 239000010440 gypsum Substances 0.000 description 6
- 229910052602 gypsum Inorganic materials 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 239000000428 dust Substances 0.000 description 4
- 239000003595 mist Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 2
- 235000010261 calcium sulphite Nutrition 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 239000006028 limestone Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 241001062872 Cleyera japonica Species 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 239000003657 drainage water Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- -1 that is Inorganic materials 0.000 description 1
Landscapes
- Treating Waste Gases (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は湿式排煙脱硫装置に係シ、特に吸収剤および硫
酸の消費量を低減するに好適な湿式排煙脱硫装置に関す
るものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a wet flue gas desulfurization system, and more particularly to a wet flue gas desulfurization system suitable for reducing the consumption of absorbent and sulfuric acid.
現在、火力発電所等に設置されている排煙脱硫装置は、
石灰石、石灰等を吸収剤としたスラリからなる吸収液ス
ラリを用い、ボイラ等の排ガス中の硫黄酸化物（８０，
）を吸収し、得られ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方法が最も
一般的である。Currently, flue gas desulfurization equipment installed at thermal power plants, etc.
Sulfur oxides (80,
), the resulting calcium sulfite is oxidized, and the most common method is to recover it as calcium sulfate, that is, gypsum.
この石灰石または石灰（以下、吸収剤と略す）を用いる
従来の排煙脱硫装置の系統を第１図に示し、その概要を
以下に述べる。ボイラ等の排ガスは、煙道１によシ除じ
ん塔２°に導入され、ここで除しん塔循環タンク５から
循環ボンダ４によシ供給される循環液との気液接触によ
シ、飽和温度まで冷却されるとともに、排ガス中に含有
されるダストが除去された後、吸収塔７に送られる。な
お、場合によっては、吸収塔７に送られるガス中のミス
トを除去するために、ミストエリミネータ６が設置され
る場合もある。吸収塔７で循環ポンプ１０により配管４
０を経て供給され九吸収液スラリとの気液接触により排
ガス中のＳＯ工が吸収、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から清浄ガスが・排出され
る。なお、１２はミストエリミネータ６およびデミスタ
８への補給水配管である。The system of a conventional flue gas desulfurization device using this limestone or lime (hereinafter abbreviated as absorbent) is shown in FIG. 1, and its outline will be described below. Exhaust gas from the boiler, etc. is introduced into the dust removal tower 2° through the flue 1, where it is brought into gas-liquid contact with the circulating liquid supplied from the dust removal tower circulation tank 5 to the circulation bonder 4. After being cooled to saturation temperature and removing dust contained in the exhaust gas, it is sent to the absorption tower 7. In some cases, a mist eliminator 6 may be installed to remove mist from the gas sent to the absorption tower 7. In the absorption tower 7, the circulation pump 10 connects the piping 4.
After the SO gas in the exhaust gas is absorbed and removed by gas-liquid contact with the absorbing liquid slurry supplied through the demister 8, the entrained mist is removed by the demister 8, and clean gas is discharged from the flue 9. Note that 12 is a make-up water pipe to the mist eliminator 6 and demister 8.
吸収塔７にはガス中のｓｏ工を吸収するに必要なスラリ
か吸収剤スラリタンク２５からポンプ２６によシ供給さ
れる一方、吸収塔ブリードポンプ１１により、ｓｏ−を
吸収し、生成した亜硫酸カルシウムを含有するスラリの
一部が抜き出され、酸化塔供給タンク１３に供給される
。酸化塔供給タンク１３では、未反応の吸収剤が硫酸２
８と反応しテ石膏ニなるとともに、ＰＨ調整された後、
ポンプ１４によシ酸化塔１５に送られ、空気圧縮機２１
により空気槽２２を介して供給される空気にょシ酸化さ
れ、スラリ中の亜硫酸カルシウムは石膏となる。得られ
た石膏スラリは、石膏シラフナ１６、スラリタンク１７
および脱水機１９を経て脱水され、石膏２ｏが回収され
る。なお、図中、３．１８．２４はポンプ、２３は濾過
水ポンプ、２７は吸収剤、２９は排水を示す。The absorption tower 7 is supplied with slurry necessary for absorbing the SO- in the gas from the absorbent slurry tank 25 through the pump 26, while the absorption tower bleed pump 11 absorbs SO- and the generated sulfur dioxide. A portion of the slurry containing calcium is extracted and supplied to the oxidation tower supply tank 13. In the oxidation tower supply tank 13, unreacted absorbent is converted into sulfuric acid 2
After reacting with 8 and forming gypsum, the pH was adjusted.
The air is sent to the oxidation tower 15 by the pump 14, and then sent to the air compressor 21.
The air supplied through the air tank 22 is oxidized, and the calcium sulfite in the slurry becomes gypsum. The obtained gypsum slurry was transferred to gypsum Shirafuna 16 and slurry tank 17.
The gypsum 2o is then dehydrated through a dehydrator 19 and recovered. In addition, in the figure, 3, 18, and 24 are pumps, 23 is a filtered water pump, 27 is an absorbent, and 29 is a drainage water.
上記排煙脱硫装置における吸収剤スラリの供給方法およ
び供給量の制御方法は、第２図に示すように、脱硫装置
に流入する排ガス量とＳＯ！濃度を各々計器３０と３１
によシ検出し、掛算器３５によりＳＯ工量を算出し、こ
れに一定の比率（定数）を掛けて必要な吸収剤スラリ量
とし、これと吸収剤スラリ流量計３２で検出した実際の
流量を比較し、これらの差が可及的に小さくなるように
吸収剤スラリ流量調整弁３４を制御するものである。こ
の方は流入ＳＯ工量にかかわらず一定となる。The method for supplying the absorbent slurry in the flue gas desulfurization equipment and the method for controlling the supply amount are as shown in FIG. Concentration meters 30 and 31 respectively
The amount of SO work is calculated by the multiplier 35, and this is multiplied by a certain ratio (constant) to obtain the required amount of absorbent slurry, and this is combined with the actual flow rate detected by the absorbent slurry flowmeter 32. The absorbent slurry flow rate regulating valve 34 is controlled so that the difference between the two is as small as possible. This amount remains constant regardless of the amount of inflow SO.
ところが、脱硫装置の吸収塔の特性として吸収液のｐＨ
が高い程、また流入ＳＯ工量が少ない程、脱硫性能は高
くな９、また、吸収塔スラリのｐＨは液中の吸収剤濃度
が高い程、また流入ＳＯ□量が低い程上昇する。即ち、
脱硫装置を低負荷で運転した場合、流入ＳＯ，量の低下
によってのみでなく、流入ＳＯ！量の低下に起因する吸
収塔スラリのｐＨ上昇によっても、脱硫性能が上昇する
。これは低負荷運転時において、必要以上の吸収剤を消
費し、またその結果として多量に硫酸を消費し、運転費
を高くすることになる。However, as a characteristic of the absorption tower of the desulfurization equipment, the pH of the absorption liquid
The higher the concentration of the absorbent, and the lower the amount of inflow SO, the higher the desulfurization performance. That is,
When the desulfurization equipment is operated at low load, not only the amount of inflow SO! An increase in the pH of the absorber slurry due to a decrease in volume also increases desulfurization performance. This consumes more absorbent than necessary during low-load operation, and as a result, a large amount of sulfuric acid is consumed, increasing operating costs.
このような従来技術の欠点をなくすために１．第３図に
示すように、吸収液ス２すｐ’Ｈ計３３、調節計３６お
よび加算器３８を設け、各負荷において吸収液＼ラリの
ｐＨが一定゛になるような補正回路を付加する制御方法
が考えられている。これは、上記したように低負荷時の
脱硫率を計画値に維持するために、各負荷帯においてＰ
Ｈがあらかじめ設定した直になるように吸収剤スラリの
供給量を制御するものである。In order to eliminate such drawbacks of the conventional technology, 1. As shown in FIG. 3, an absorption liquid pH meter 33, a controller 36, and an adder 38 are provided, and a correction circuit is added to keep the pH of the absorption liquid constant at each load. Control methods are being considered. As mentioned above, in order to maintain the desulfurization rate at the planned value at low loads, P
The supply amount of the absorbent slurry is controlled so that H is equal to a preset value.
しかしながら、吸収塔スラリのｐＨは、上述のように吸
収Ｓ０８、量と吸収液スラリ中の吸収剤濃度に依存する
だめ、流入ＳＯ□量が減少した場合、Ｐ Ｈを一定に保
つと吸収、剤濃度は低下することになる。However, as mentioned above, the pH of the absorber slurry depends on the amount of absorbed SO8 and the absorbent concentration in the absorbent slurry. The concentration will decrease.
また一般に、吸収塔７は酸化塔供給タンク１３への抜き
出し量に対して約２０時間分のスラリを保有しているた
め、流入ガス側の負荷変化速度に比べて液組成の変化に
遅れを生じる。従って、上記従来技術の制御方法では、
低負荷で安定したＰ Ｈｚ吸収液スラリ性状で運転して
いる状態から負荷上昇を行なった場合、負荷上昇に対し
液組成の変化が遅れ、一時的にｐＨが低下して脱硫率の
低下を招くことになる。これは、特に負荷変動の多いボ
イラ等に設置される脱硫装置においてはｈ安定運転がで
きないという欠点を生じることになる。Additionally, since the absorption tower 7 generally holds about 20 hours worth of slurry for the amount withdrawn to the oxidation tower supply tank 13, there is a delay in the change in liquid composition compared to the rate of load change on the inflow gas side. . Therefore, in the conventional control method described above,
If the load is increased from a state where the system is operating with stable P Hz absorption liquid slurry properties at low load, the change in liquid composition will be delayed in response to the increase in load, resulting in a temporary drop in pH and a decrease in desulfurization rate. It turns out. This results in the disadvantage that stable operation cannot be achieved, particularly in desulfurization equipment installed in boilers and the like that experience frequent load fluctuations.
本発明の目的は、上記した従来技術の欠点をなくシ、ボ
イラ等の負荷変動に対する追従性が良く、かつ吸収剤お
よび硫酸の消費量を低減することができる湿式排煙脱硫
装置を提供することにある。An object of the present invention is to provide a wet flue gas desulfurization device that eliminates the drawbacks of the prior art described above, has good followability to load fluctuations of a boiler, etc., and can reduce consumption of absorbent and sulfuric acid. It is in.
本発明は、硫黄酸化吻（ｓｏ工）を含む排ガスが流通す
る吸収塔゛に吸収液を循“環させ、気液接触を行なわせ
てＳＯ工を吸収除去する湿式排煙脱硫装置に゛おいて、
吸収塔スラリ循環配管または吸収塔に、濃度が低濃度か
ら高濃度に上昇する時点で吸収剤濃度が所定値以上にな
るように前記吸収剤、スラリの直接供給配管系から所定
量の吸収剤を急速供給する′吸収剤供給制御系を設けた
ことを特徴とする。The present invention is applicable to a wet flue gas desulfurization device that circulates an absorption liquid through an absorption tower through which exhaust gas containing sulfur oxidizer (SO) flows, and performs gas-liquid contact to absorb and remove SO. There,
A predetermined amount of absorbent is supplied to the absorption tower slurry circulation piping or the absorption tower from the direct supply piping system for the absorbent and slurry so that the absorbent concentration reaches a predetermined value or more at the point when the concentration increases from a low concentration to a high concentration. It is characterized by the provision of an absorbent supply control system that rapidly supplies the absorbent.
すなわち、本発明は、吸収塔内でボイラ等の排ガスと気
液接触を行なわせ、Ｓ０１を吸収、除去するための吸収
液スラリの循環配管または吸収塔タンクに、吸収剤スラ
リの供給配管を直接、接続し、低負荷時（低排ガス量又
は低ＳＯｘ濃度時）において、吸収剤当量比を下げるよ
うに吸収剤スラリの供給量を制御し、一方、負荷上昇（
低排ガス量又はＳ０８濃度上昇）と同時に循環スラリ中
の吸収剤濃度を該負荷上昇にと４−／ｚつて、その負荷
に必要な濃度まで高めるように、前記スラリ供給配管か
ら吸収剤スラリを急速供給するようにしたものである。That is, the present invention connects the absorbent slurry supply pipe directly to the absorbent slurry circulation pipe or the absorption tower tank for making gas-liquid contact with the exhaust gas from a boiler or the like in the absorption tower and absorbing and removing S01. , and control the supply amount of absorbent slurry to lower the absorbent equivalence ratio at low load (low exhaust gas amount or low SOx concentration), while controlling the supply amount of absorbent slurry to lower the absorbent equivalence ratio when the load increases (
The absorbent slurry is rapidly supplied from the slurry supply pipe so as to increase the absorbent concentration in the circulating slurry to the concentration required for the load at the same time as the load increase (low exhaust gas amount or increase in S08 concentration). It was designed to be supplied.
以下、本発明を図面によシさらに詳細に説明する。Hereinafter, the present invention will be explained in more detail with reference to the drawings.
第４図は、本発明の一実施例を示す脱硫装置の吸収塔廻
りの配管系統図でオシ、第５図は対応する制御系統図で
ある。第４図において、吸収塔７には、第１図と同様に
吸収剤スラリタンク２５、同ポンプ２６、および吸収剤
スラリ調節弁３４からなる吸収剤スラリ供給系統と、吸
収剤循環配管４０およびポンプ１０からなる吸収剤スラ
リ循環系統とが設けられ、さらに吸収剤スラリタンク２
５には、吸収剤循環配管４３および吸収剤スラリ戻り調
整弁４４と、吸収剤急速供給配管４２およびその供給バ
ルブ４１が設けられている。FIG. 4 is a piping system diagram around an absorption tower of a desulfurization apparatus showing an embodiment of the present invention, and FIG. 5 is a corresponding control system diagram. In FIG. 4, the absorption tower 7 includes an absorbent slurry supply system consisting of an absorbent slurry tank 25, an absorbent slurry pump 26, and an absorbent slurry control valve 34, as well as an absorbent circulation pipe 40 and a pump, as in FIG. An absorbent slurry circulation system consisting of 10 and an absorbent slurry tank 2 is provided.
5 is provided with an absorbent circulation pipe 43, an absorbent slurry return adjustment valve 44, and an absorbent rapid supply pipe 42 and its supply valve 41.
上記構成において、流入ＳＯ工量が減少した時には循環
スラリ中の吸収剤濃度を下げるように吸収剤スラリの供
給量が吸収剤スラリ供給配管ラインの調節弁３４で制御
される。その手段としては、第５図に示す通夛前述のＰ
Ｈ一定制御も一手段でワシ、更に低負荷時にｐＨを下げ
るような制御も考えられる。本実施例では、負荷上昇開
始と同時に、吸収剤スラリの供給量を急速に増加させ、
循環スラリ中の吸収剤濃度を、負荷上昇にともなって、
その負荷に必要な濃度まで高める。具体的には、第５図
に示す過多給電指令等によシ、ゲイ２側の負荷変化をボ
イラ負荷指令５０として逸早くとらえ、この負荷信号を
関数発生器５１によシその負荷において所要脱硫率を維
持するために必要な吸収液ｐＨに変換し、とのＰＨ設定
値と、ＰＨ計３３によシ検出された実際のｐＨ値との偏
差信号と負荷変化信号（負荷の微分信号）の加算信号で
吸収剤スラリ急速供給弁４１を制御し、循環スラリ中の
吸収剤濃度を必要な濃度まで高める。なお、５２は調節
計、５３は切替器、５４は微分器、５５は関数発生器で
ある。ここで吸収剤スラリ供給ラインの吸収剤スラリ供
給タンク２５に戻る循環ライン４３に戻り調整弁（自動
０Ｎ−ＯＦＦ弁）４４を設け、通常運転時には骸自動０
Ｎ−ＯＦＦ弁４４は全開とし、弁４１は閉として一定量
のスラリ、をタンク２５内に循環させて運転し、負荷上
昇開始時には負荷変化信号（微分信号）により、吸収剤
スラリ急速供給弁４１を上述の通９制御すると共に、自
動０Ｎ−ＯＦＦ弁４４および吸収剤スラリ調節弁３４を
全閉させることにより、吸収剤スラリの供給量を急速に
増加させる。このようにして負荷上昇時にその負荷に必
要な吸収剤濃度まで時間遅れなく吸収剤濃度を高めるこ
とができ本実施例での負荷変化試験結果を従来技術と比
較して第６図＠）、←）、ｒ）Ｋ示す。０）は吸収剤当
量比を過剰にし、低負荷時に計画脱硫率を達成すること
はできるが、吸収剤スラリ量が多くなる場合、←）は低
負荷時、吸収剤尚量り少なくすることができるが、負荷
上昇時に計画脱硫率が維持できなくなる場合、（ハ）は
本発明の場合をそれぞれ示す。In the above configuration, the supply amount of the absorbent slurry is controlled by the control valve 34 of the absorbent slurry supply piping line so as to lower the absorbent concentration in the circulating slurry when the inflow SO production amount decreases. As a means for this, the above-mentioned P
Constant H control is one option, and control that lowers the pH at low loads is also conceivable. In this example, the supply amount of absorbent slurry is rapidly increased at the same time as the load starts to increase.
The absorbent concentration in the circulating slurry is increased as the load increases.
Increase to the concentration required for that load. Specifically, the load change on the gay 2 side is quickly detected as the boiler load command 50 by using the excessive power supply command shown in FIG. Addition of the deviation signal between the pH set value and the actual pH value detected by the PH meter 33 and the load change signal (load differential signal) The signal controls the absorbent slurry rapid supply valve 41 to increase the absorbent concentration in the circulating slurry to the required concentration. In addition, 52 is a controller, 53 is a switch, 54 is a differentiator, and 55 is a function generator. Here, a return regulating valve (automatic 0N-OFF valve) 44 is provided in the circulation line 43 that returns to the absorbent slurry supply tank 25 of the absorbent slurry supply line, and during normal operation, the automatic zero
The N-OFF valve 44 is fully opened and the valve 41 is closed to circulate a certain amount of slurry into the tank 25. When the load starts to increase, the absorbent slurry rapid supply valve 41 is activated by the load change signal (differential signal). is controlled as described above, and the automatic ON-OFF valve 44 and the absorbent slurry control valve 34 are fully closed, thereby rapidly increasing the amount of absorbent slurry supplied. In this way, when the load increases, the absorbent concentration can be increased to the absorbent concentration required for that load without any time delay. Figure 6 shows a comparison of the load change test results in this example with the conventional technology. ), r) K is shown. 0) allows the absorbent equivalent ratio to be excessive and achieve the planned desulfurization rate at low loads, but if the amount of absorbent slurry increases, ←) allows the amount of absorbent to be reduced at low loads. However, when the planned desulfurization rate cannot be maintained when the load increases, (c) shows the case of the present invention.
試験条件 負荷モデル 第６図
負荷変化速度 ５チ／分
入口ＳＯｘ濃度 １０００ＰＩＩＩ
吸収剤当量比 定格時１，０５
本試験の結果、負荷上昇速度に追従して、吸収液ス２す
中の吸収剤濃度を急速に高くすることができるため、低
負荷時に吸収剤スラリ供給量を低減することが可能とな
る。上記試験結果では、通常運転時、吸収剤当量比１．
０５に対し、３〇−負荷時１．０１まで低減できること
がわかった。従って第６図の斜線部に相当する吸収剤ス
ラリ供給量を低減することができることになる。Test conditions Load model Figure 6 Load change rate 5 inches/min Inlet SOx concentration 1000 PIII Absorbent equivalent ratio 1.05 at rated time As a result of this test, the absorbent concentration in the absorbent liquid follows the load increase rate. can be rapidly increased, making it possible to reduce the amount of absorbent slurry supplied during low loads. The above test results show that during normal operation, the absorbent equivalent ratio is 1.
It was found that it can be reduced to 1.01 at 30-load compared to 05. Therefore, the amount of absorbent slurry supplied corresponding to the shaded area in FIG. 6 can be reduced.
次に第７図は、本発明の他の実施例ケ示すもので、吸収
塔７の側５Ｖｒ−吸収剤スラリを貯えたリザーブタンク
４５を設け、負荷上昇開始と同時に該タンク下部に設け
た吸収剤スラリ急速嫁入弁４６によシ、吸収塔循環タン
ク内に、該タンク内の吸収剤濃度が負荷上昇にともなっ
て、その負荷に必要な濃度になるように吸収剤スラリな
供給するようＫしたものである０本実施例においても第
１の実施例と同様の効果が得られる。Next, FIG. 7 shows another embodiment of the present invention, in which a reserve tank 45 storing 5Vr-absorbent slurry is provided on the side of the absorption tower 7, and at the same time as the load starts to rise, an absorption tank 45 is installed at the bottom of the tank. The agent slurry rapid transfer valve 46 is configured to supply absorbent slurry into the absorption tower circulation tank so that as the load increases, the absorbent concentration in the tank becomes the concentration required for the load. In this embodiment, the same effects as in the first embodiment can be obtained.
以上、本発明によれば、ポイＭ）プラント等の負荷上昇
に対して良好に追従し、石灰石等の吸収剤および硫酸の
消費量を低減することができる。As described above, according to the present invention, it is possible to satisfactorily follow an increase in the load of a POI plant, etc., and to reduce the consumption of an absorbent such as limestone and sulfuric acid.
第１図は従来技術による排煙脱硫装置の系統図、第２図
および第３図はそれぞれ従来技術による吸収剤スラリ供
給量制御系統図、第４図および第５図は、それぞれ本発
明の実施例を示す排煙脱硫装置の吸収剤スラリ供給の配
管系統図および制御系統図、第６図は、本発明の実施例
における試験結果の１２例として、負荷変化時における
脱硫率、吸収液スラリ中の吸収剤濃度、吸収剤スラリ供
給量を示した線図であ夛、第６図（イ）、仲）は従来技
術の（ハ）
場合、第６図榊は本発明の場合を示す。第７図は、本発
明の他の実施例を示す吸収剤スラリ供給制御系統図であ
る。
１・・・煙道、２“＝・・除じん器、７・・・吸収塔、
１０・−・吸収塔循環ポンプ、１１・・・吸収塔ブリー
ドポンプ、２５・・・吸収剤スラリタンク、２６・・・
吸収剤スラリポンプ、２７・・・吸収剤スラリ供給配管
、３３・・・吸収塔タンクルＨ計、３４・・・吸収剤ス
ラリ調節弁、４０・・・吸収塔循環配管、４１・・・吸
収剤スラリ急速供給バルブ、４２・・・吸収剤スラリ急
速供給配管、４３・・・吸収剤スラリ戻９配管、４４−
・吸収剤スラリ戻シ調整弁、４５・・・吸収剤リザーブ
タンク、４６・・・吸収剤急速投入弁、５０・−・ボイ
ラ負荷指令、５１・・・関数発生器、５２・−・調節計
、５３・−・切替器、５４・−・微分器、５５・・・関
数発生器。
代理人 弁理士 川 北 武 良
策１１！Ｉ
２乙Ｘ−FIG. 1 is a system diagram of a flue gas desulfurization equipment according to the prior art, FIGS. 2 and 3 are system diagrams of absorbent slurry supply amount control according to the prior art, and FIGS. 4 and 5 are diagrams of an embodiment of the present invention, respectively. FIG. 6 is a piping system diagram and a control system diagram for supplying absorbent slurry in a flue gas desulfurization equipment, which shows examples of the desulfurization rate when the load changes, Fig. 6 (a) and middle) are diagrams showing the absorbent concentration and absorbent slurry supply amount. Fig. 6 (a) and middle) show the case of the prior art (c), and Fig. 6 (sakaki) shows the case of the present invention. FIG. 7 is an absorbent slurry supply control system diagram showing another embodiment of the present invention. 1... Flue, 2"=... Dust remover, 7... Absorption tower,
10... Absorption tower circulation pump, 11... Absorption tower bleed pump, 25... Absorbent slurry tank, 26...
Absorbent slurry pump, 27... Absorbent slurry supply piping, 33... Absorption tower tank H meter, 34... Absorbent slurry control valve, 40... Absorption tower circulation piping, 41... Absorbent Slurry rapid supply valve, 42... Absorbent slurry rapid supply piping, 43... Absorbent slurry return 9 piping, 44-
- Absorbent slurry return adjustment valve, 45... Absorbent reserve tank, 46... Absorbent rapid input valve, 50... Boiler load command, 51... Function generator, 52... Controller , 53... Switcher, 54... Differentiator, 55... Function generator. Agent Patent Attorney Takeshi Kawakita Good Plan 11! I 2 Otsu X-
Claims (1)
収塔に吸収液を循環させ、気液接触を行なわせて＄００
を吸収除去する湿式排煙脱硫装置において、吸収塔スラ
リ循環配管または吸収塔に、吸収剤スラリ度から高濃度
に上昇する時点で吸収剤濃度が所定値以上になるように
前記吸収ｉｌＪスラリの直接供給配管系から所定量の吸
収剤を急速供給する吸収剤供給制御系を設けたことを特
徴とする湿式排煙脱硫装置。(1) The absorption liquid is circulated through an absorption tower through which exhaust gas containing sulfur oxides (80 tons) flows, and gas-liquid contact is performed.
In the wet type flue gas desulfurization equipment that absorbs and removes the absorbed ilJ slurry, the absorbed ILJ slurry is directly added to the absorption tower slurry circulation piping or the absorption tower so that the absorbent concentration reaches a predetermined value or more at the time when the absorbent slurry level increases from the absorbent slurry level to a high concentration. A wet flue gas desulfurization device characterized by being provided with an absorbent supply control system that rapidly supplies a predetermined amount of absorbent from a supply piping system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58034617A JPS59160519A (en) | 1983-03-04 | 1983-03-04 | Wet type waste gas desulfurizer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58034617A JPS59160519A (en) | 1983-03-04 | 1983-03-04 | Wet type waste gas desulfurizer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS59160519A true JPS59160519A (en) | 1984-09-11 |
| JPH0417691B2 JPH0417691B2 (en) | 1992-03-26 |
Family
ID=12419331
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58034617A Granted JPS59160519A (en) | 1983-03-04 | 1983-03-04 | Wet type waste gas desulfurizer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS59160519A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61254227A (en) * | 1985-05-01 | 1986-11-12 | Babcock Hitachi Kk | Method for controlling supply amount of limestone slurry |
| US5076818A (en) * | 1990-06-28 | 1991-12-31 | Jonsson Kjartan A | Gas cleaning methods and apparatus |
| WO2019087901A1 (en) | 2017-10-31 | 2019-05-09 | 三菱重工エンジニアリング株式会社 | Gas treatment device, gas treatment method, co2 recovery device, and co2 recovery method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5232895A (en) * | 1975-09-09 | 1977-03-12 | Mitsubishi Heavy Ind Ltd | Process for controlling supplying quantity of lime in the wet recovery process of sulfur in the waste gas as gypsum with lime |
| JPS5343193U (en) * | 1976-09-16 | 1978-04-13 |
-
1983
- 1983-03-04 JP JP58034617A patent/JPS59160519A/en active Granted
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5232895A (en) * | 1975-09-09 | 1977-03-12 | Mitsubishi Heavy Ind Ltd | Process for controlling supplying quantity of lime in the wet recovery process of sulfur in the waste gas as gypsum with lime |
| JPS5343193U (en) * | 1976-09-16 | 1978-04-13 |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61254227A (en) * | 1985-05-01 | 1986-11-12 | Babcock Hitachi Kk | Method for controlling supply amount of limestone slurry |
| US5076818A (en) * | 1990-06-28 | 1991-12-31 | Jonsson Kjartan A | Gas cleaning methods and apparatus |
| WO2019087901A1 (en) | 2017-10-31 | 2019-05-09 | 三菱重工エンジニアリング株式会社 | Gas treatment device, gas treatment method, co2 recovery device, and co2 recovery method |
| US12109529B2 (en) | 2017-10-31 | 2024-10-08 | Mitsubishi Heavy Industries, Ltd. | Air pollution control unit and air pollution control method, and CO2 recovery unit and CO2 recovery method |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0417691B2 (en) | 1992-03-26 |
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