JPS5874126A - Treatment for waste gas - Google Patents
Treatment for waste gasInfo
- Publication number
- JPS5874126A JPS5874126A JP56170789A JP17078981A JPS5874126A JP S5874126 A JPS5874126 A JP S5874126A JP 56170789 A JP56170789 A JP 56170789A JP 17078981 A JP17078981 A JP 17078981A JP S5874126 A JPS5874126 A JP S5874126A
- Authority
- JP
- Japan
- Prior art keywords
- absorption tower
- absorption
- tower
- slurry
- amount
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Abstract
Description
【発明の詳細な説明】
本発明はボイラ排ガスの如き８０Ｊを含む排ガスから有
害なＳＯ，を除去する方法に関する４ので、ＣａＣＯ３
４’ Ｃａ（ＯＨ）１などの難溶性カルシウム化合物を
８０１の吸収剤とし、副生物として２水石膏を回収する
湿式石灰・石膏法による排煙脱硫方法の改良に係わる本
のである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for removing harmful SO from exhaust gas containing 80J, such as boiler exhaust gas.
4' This book concerns an improvement of a flue gas desulfurization method using a wet lime/gypsum method, which uses a sparingly soluble calcium compound such as Ca(OH)1 as an 801 absorbent and recovers dihydrate gypsum as a by-product.
最近の社会情勢から大気に放散する有害なＳＱＪの□排
出量を極力低減させることが必要とされており、それに
対応するための一手段として湿式排煙脱硫装置の高性能
化が進められている。Due to recent social conditions, it is necessary to reduce as much as possible the amount of harmful SQJ released into the atmosphere, and as a means of responding to this, the performance of wet flue gas desulfurization equipment is being improved. .
脱硫率の向上を図る手段として従来から寸でに用いられ
ている方法としては、吸収塔を複数設け、排ガスを第１
吸収塔でまず洗浄した後、次いで第２吸収塔へ導いて洗
浄し、その後本必要に応じて順次洗浄して行く方法、即
ち吸収工程な単に直列に連結する方法である。A method that has been widely used in the past as a means of improving the desulfurization rate is to install multiple absorption towers and absorb the exhaust gas into the first
This is a method in which the material is first washed in an absorption tower, then introduced into a second absorption tower for washing, and then sequentially washed as required, that is, the absorption process is simply connected in series.
第１図に上記公知の吸収塔を２塔設けた場合の具体例を
示す。FIG. 1 shows a specific example in which two of the above-mentioned known absorption towers are provided.
ＳＯ，を含む排ガス１を第１吸収塔２に導き、更に脱硫
する為に第１吸収塔２の出口ガス３を第・２吸収塔４に
導いて、殆んど完全Ｋ ８０．を除去された浄化ガス５
として系外へ排出される。The exhaust gas 1 containing SO is led to the first absorption tower 2, and the outlet gas 3 of the first absorption tower 2 is led to the second absorption tower 4 for further desulfurization, so that almost complete K80. Purified gas 5
is discharged from the system as
第１ａ収塔２でのＳへ吸収量に見合ったカルシウム化合
物を含む吸収剤スラリー６を第１吸収塔２へ供給し、亜
硫酸カルシウム及び亜硫酸カルシウムの一部が偽によっ
て酸化され生成した２水石膏とを含むスラリー７がバラ
ンスによって抜き出される。一方第２吸収塔４でのＳＯ
。An absorbent slurry 6 containing calcium compounds commensurate with the amount absorbed by S in the 1a collection tower 2 is supplied to the first absorption tower 2, and calcium sulfite and a portion of the calcium sulfite are oxidized to form dihydrate gypsum. A slurry 7 containing the following is extracted by balance. On the other hand, SO in the second absorption tower 4
.
吸収量に見合ったカルシウム化合物、を含む吸収剤スラ
リー８を第２吸収塔４へ供給し、亜硫酸カルシウム及び
亜硫酸カルシウムの一部がＯＡＫよって酸化され生成し
た工水石膏とを含むスラリー９がバランスによって抜き
出される。An absorbent slurry 8 containing calcium compounds commensurate with the absorption amount is supplied to the second absorption tower 4, and a slurry 9 containing calcium sulfite and engineered water gypsum produced by oxidizing a part of the calcium sulfite with OAK is supplied to the second absorption tower 4. being extracted.
従来は第１図に於ける第１吸収塔２の出口ガス３中のＳ
Ｏ，排出量が排出規制を十分満足し得る本のであったが
厳しい排出制限を満足すぺ〈＃まは完全に脱硫する為に
第２吸収塔４を設けたのであるから、第２吸収塔−での
８偽吸収量は第１吸収塔２でのＳＯＪ吸収吸収化べると
少な、〈ｊ・屯
通常は全８偽吸収量の約９０モル％が第１吸収塔２で吸
収除去され、全ＳＯｓ吸収量の約１０モル％が第２吸収
塔４で吸収される。Conventionally, S in the outlet gas 3 of the first absorption tower 2 in FIG.
O, the amount of emissions was enough to satisfy the emission regulations, but it was not enough to satisfy the strict emission limits. -The amount of 8 false absorption in the first absorption tower 2 is smaller than that of SOJ absorption in the first absorption tower 2. Normally, about 90 mol% of the total amount of 8 false absorption is absorbed and removed in the first absorption tower 2. , about 10 mol% of the total amount of SOs absorbed is absorbed in the second absorption tower 4.
第１図の従来方式では、吸収剤スラリーを供給する装置
が２式必要であること、第１吸収塔２の出口スラリ−７
及び第２吸収塔４の出口スラリ−９をライン１０によっ
て酸化装置１１［送動亜硫酸カルシウムを空気酸化して
工水石膏とする工程が必要であり、酸化を促進する為に
硫酸１２４必要である。In the conventional system shown in FIG.
And the slurry 9 at the outlet of the second absorption tower 4 is passed through the line 10 to the oxidizer 11 [a step of air oxidizing the fed calcium sulfite to produce water gypsum is necessary, and sulfuric acid 124 is necessary to promote the oxidation. .
そこで第２図のように、吸収剤スラリー供給装置を１つ
和して酸化装置での硫−を不快する方式がすでに知られ
ている。Therefore, as shown in FIG. 2, a method is already known in which one absorbent slurry supply device is combined to make the sulfur in the oxidation device unpleasant.
第２図について説明する。FIG. 2 will be explained.
８偽を含む排ガス１０１を第１吸収塔１０２に導き脱硫
する。更に脱硫する為に第１吸収塔１０２の出ロガ、＊
１０５を第２吸収塔１０４に導き、殆んど完全Ｋ ８０
．を除去した後、浄化ガス１０５を系外し卜排出する。Exhaust gas 101 containing 8.8% is led to the first absorption tower 102 to be desulfurized. For further desulfurization, the output logger of the first absorption tower 102,*
105 to the second absorption tower 104, almost completely K 80
．． After removing the purified gas 105, the purified gas 105 is discharged from the system.
′１ニ
一方、全８ｏｊ：吸１収量に見合ったカルシウム化１゜
合物を含む吸収剤スラリー１０６を第２吸収塔１０４へ
供給し、第２吸収塔１０４で吸収剤の約１０モル％を消
−資したのち、ライン１０７Ｑ経由して第１吸収塔１０
２に送る。第１吸収塔１Ｇ２では全８へ吸収量のうち約
９０モル％のＳＯ，がライン１０７からのスラリー中に
含まれる未反応の吸収剤（約９０モル％の吸収剤が残存
している）によって脱硫される０次いで、亜硫酸カルシ
ウム及び亜硫酸カルシウムの一部が０１によって家化さ
れ生成し九二水石膏とを含むスラリー１０８が酸化装置
１０９に送られ、亜硫酸カルシウムは空気酸化されて工
水石膏となる。On the other hand, the absorbent slurry 106 containing the calcified 1° compound corresponding to the total 80j:absorption amount is supplied to the second absorption tower 104, where about 10 mol% of the absorbent is After consumption, the first absorption tower 10 is transferred via line 107Q.
Send to 2. In the first absorption tower 1G2, about 90 mol% of the total absorbed amount of SO is due to unreacted absorbent (about 90 mol% of the absorbent remains) contained in the slurry from line 107. 0 to be desulfurized Next, a slurry 108 containing calcium sulfite and a part of the calcium sulfite is converted into aqueous gypsum by 01, and is sent to an oxidizer 109, where the calcium sulfite is oxidized in the air and converted into industrial gypsum. Become.
第２図の従来法では第２吸収塔１０４で、全８偽吸収量
の約１０モル％の８偽を吸収させるのに、約９０モル％
本過剰の吸収剤（この吸収剤は、後で第１吸収塔１０２
での脱硫に供される。）を含んだスラリーと接触させる
のであるから、極めて高い効率でＳＯ，吸収反応を行な
わしめ得る利点がある。しかしながら難溶性のカルシウ
ム化合物を含むスラリーで脱硫する場合に吸収剤の過剰
供給は吸収塔内で固形物付着によるガス及びスラリー〇
流路狭隘化を来たす欠点がある。吸収剤が大過剰に存在
すると、スラリーがアルカリ性側に移行しＯａＯＯｇや
Ｃａ８０３の溶解度が崗一層小さくなる結果、スケール
が付着しやすくなるためである。In the conventional method shown in FIG. 2, the second absorption tower 104 absorbs about 90 mol% of the 8-false, which is about 10 mol% of the total 8-false absorbed amount.
This excess absorbent (this absorbent will be added to the first absorption tower 102 later)
It is subjected to desulfurization at ), it has the advantage that the SO absorption reaction can be carried out with extremely high efficiency. However, when desulfurization is performed using a slurry containing a hardly soluble calcium compound, excessive supply of absorbent has the disadvantage that the flow path of the gas and slurry becomes narrowed due to the adhesion of solid matter within the absorption tower. This is because if the absorbent is present in large excess, the slurry shifts to the alkaline side and the solubility of OaOOg and Ca803 becomes even lower, making it easier for scale to adhere.
そζで、スケールを少しで本軽減させる為、第２吸収＄
１０４のスラリー中に極めて多く残存する吸収剤を少な
くする方法が取られる。このことは第１吸収塔１０２で
吸収剤が若干不足することＫなり第１吸収塔１０２から
バランスによって抜き出されるスラリー１０８Ｆｉ酸性
を示すようＫなる。従って、酸化装置１０９では硫酸を
加えて酸性圧する必要はなくなるのである。Therefore, in order to reduce the scale slightly, the second absorption $
A method is taken to reduce the amount of absorbent remaining in the slurry of No. 104, which is extremely large. This means that there is a slight shortage of absorbent in the first absorption tower 102, and the slurry 108Fi extracted from the first absorption tower 102 by balance becomes acidic. Therefore, there is no need to add sulfuric acid to create acidic pressure in the oxidizer 109.
現在、湿式石灰石膏法排煙脱硫装置で２基の吸収塔を直
列にして排ガスを処理している本のはその基本的フロー
は第２図のようになってｉる。At present, the basic flow of a wet lime gypsum method flue gas desulfurization system that uses two absorption towers in series to treat flue gas is shown in Figure 2.
本発明は第２図で代表される従来法が第２吸収塔でスケ
ール、付着と−う欠点を生じること、酸化装置が必要で
経済的に割高であることの欠点を克服する為罠なされた
ものであり、排ガスを第１吸収塔、第２吸収塔と順次導
くと同時に、カルシウム化合物を含むＳＯ，吸収用スラ
リーを第１吸収塔に導ｉ、次いで第１吸収塔から抜き出
されたスラリーを第２吸収塔に導くと共に第１吸収塔で
の８へ吸収量を観１及び第２吸収塔での全８０１吸収量
の５０モル％以上となし、第２吸収塔での亜硫酸カルシ
ウムの酸化量を第２峡収塔でのＳＯ，吸収量よ秒多くし
て二本石膏スラリーとなし別途に酸化装置を不要とする
ことを特徴とする排ガス処理方法に関するものである。The present invention was made to overcome the disadvantages of the conventional method as shown in Fig. 2, which suffers from scale and adhesion in the second absorption tower, and requires an oxidizer, which is economically expensive. At the same time, the exhaust gas is introduced into the first absorption tower and then the second absorption tower, and at the same time, the SO and absorption slurry containing calcium compounds is introduced into the first absorption tower, and then the slurry extracted from the first absorption tower is is introduced into the second absorption tower, and the amount of absorption into 801 in the first absorption tower is set to be 50 mol% or more of the total absorption amount of 801 in the first and second absorption towers, and the oxidation of calcium sulfite is carried out in the second absorption tower. This invention relates to an exhaust gas treatment method characterized in that the amount of SO and absorption in the second absorption tower is increased to form a two-layer gypsum slurry, thereby eliminating the need for a separate oxidizing device.
本発明方法の具体例を第３図によって説明する。A specific example of the method of the present invention will be explained with reference to FIG.
石炭焚きボイラ排ガスを脱硝、集じん、冷却処理した後
食なくとも８〜と偽を含む排ガスとし−（２０１よ１１
）第１吸収塔ｚ、、Ｏ，、、２Ｋ導＜、＠１吸収塔２０
２Ｉｒｉスプレー塔やグリッド充填塔などの気液接触装
置であれば良い。第１吸収塔２０２で脱硫処理された排
ガスはライン２０５を通って第２吸収塔２０４に人動は
とんど完全にＳＱＪを吸収除去された後、ライン２０５
から浄化ガスとして系外へ排出される。第２吸収塔２０
４本一般に知られてｖｈイ気液接触装置が適用できる。Coal-fired boiler exhaust gas is treated with denitrification, dust collection, and cooling treatment, and is treated as exhaust gas that contains at least 8 to 80% of the amount of food after denitrification, dust collection, and cooling treatment. (201 to 11)
) 1st absorption tower z, , O, , 2K conduct<, @1 absorption tower 20
Any gas-liquid contact device such as a 2Iri spray tower or a grid packed tower may be used. The exhaust gas that has been desulfurized in the first absorption tower 202 passes through a line 205 to the second absorption tower 204 where SQJ is almost completely absorbed and removed.
is discharged from the system as purified gas. Second absorption tower 20
Four commonly known gas-liquid contact devices are applicable.
第１吸収塔２０２ ヘＦｉＣａＯＯ１やｃａ（ＯＨ）２
などのｅｏ、吸収剤となり得ゐカルシウム化合物を含む
スラリー２０６が第１吸収塔２０２及び第２吸収塔２０
４で脱硫される全ｓｏ！吸収量［１合って供給される。First absorption tower 202 to FiCaOO1 and ca(OH)2
A slurry 206 containing a calcium compound that can be used as an absorbent is sent to the first absorption tower 202 and the second absorption tower 20.
All so desulfurized in 4! The amount of absorption [1] is supplied.
第１吸収塔２０２でけ全ＳＱＪ吸収量の約９０モル％が
吸収されるので、吸収剤も約９０モル％が反応して亜硫
酸カルシウムとなる。第１吸収塔２０２でガスに接触す
るスラリーは約１０モル％の未反応吸収剤を有している
が、その量はスケール付着を促がすに足りない量であ艶
、間・題ない。Since about 90 mol% of the total amount of SQJ absorbed by the first absorption tower 202 is absorbed, about 90 mol% of the absorbent also reacts and becomes calcium sulfite. The slurry that comes into contact with the gas in the first absorption tower 202 has about 10 mol % of unreacted absorbent, but this amount is insufficient to promote scale adhesion and is glossy, causing no problems.
ｗＩｔ１吸収塔２０２では排ガス中のへが吸収され、亜
硫酸カルシウムの一部を酸化して三水石膏が生成する反
応本併発するので、第１吸収塔２０２から抜き出される
スラリ−２０７ａ約１０モル％の未反応吸収剤（ｃａｃ
ｏ、） と亜硫酸カルシウムと三水石膏を含むスラリ
ーとなっている。In the wIt1 absorption tower 202, 207a in the exhaust gas is absorbed, and a reaction occurs in which part of the calcium sulfite is oxidized to produce trihydrate. Therefore, about 10 mol% of the slurry 207a extracted from the first absorption tower 202 of unreacted absorbent (cac
o, ), calcium sulfite, and gypsum trihydrate.
このスラリー２０７Ｆｉ第２吸収塔２０４へ送られ、排
ガスと接触しながら全ＳＯ，吸収量の約１０モル％のＥ
ＩＯ，を吸収する。This slurry 207Fi is sent to the second absorption tower 204, and while in contact with the exhaust gas, total SO and about 10 mol% of the absorbed amount of E
Absorbs IO.
第２吸収塔２０４で気液接触するスラリーはほとんど吸
収剤が消費されてしまう６でアルカリ性を示さず、亜硫
酸カルシウムの酸化反応が進行し易い。第２吸収塔２０
４でのＳＯ，吸収量は第１ｒＩＬ収塔でのＳｏｎ吸収量
に比べて少ないから、第２吸収塔２０４で生成する亜硫
酸カルシウムはすべて三水石膏に酸化することができｂ
と共に第１吸収塔２０２からライン２Ｄ”ｉＫよって持
ち込まれる亜硫酸カルシウム４ｍ！！化することができ
る利点がある。The slurry that comes into contact with gas and liquid in the second absorption tower 204 does not exhibit alkalinity since most of the absorbent is consumed, and the oxidation reaction of calcium sulfite easily progresses. Second absorption tower 20
Since the amount of SO and absorption in the second absorption tower 204 is smaller than the amount of Son absorbed in the first rIL absorption tower 204, all of the calcium sulfite produced in the second absorption tower 204 can be oxidized to trihydrate.
At the same time, there is an advantage that 4 m of calcium sulfite brought in from the first absorption tower 202 via line 2D"iK can be converted into 4m!!.
第１吸収塔及び第２吸収塔に全く同じ形式の吸収塔、例
えｄグリッド充填塔を使用した場合、各吸収塔で９へガ
ス吸収速度はほぼ同一である。When the first absorption tower and the second absorption tower are of exactly the same type, for example, a d-grid packed tower, the gas absorption rate to 9 in each absorption tower is almost the same.
そして偽ガス全吸収量が全８０１吸収量と同じになった
場合にスラリー中の亜硫酸カルシウムｄ全部開化されて
三水石膏となる為酸化装置は不要メ會る。When the total absorption amount of pseudo gas becomes the same as the total absorption amount of 801, all of the calcium sulfite d in the slurry is liberated and becomes trihydrate, making an oxidation device unnecessary.
全ＳＯ，吸収量をＡモル／時、第１吸収塔での８偽吸収
量をＡ４モル／時、第２吸収塔でのＳ鳴吸収量をム（１
−りモル／時、第１吸収塔及び第２吸収塔でのへ吸収量
を各々９モル７時とする。Total SO, absorption amount is A mol/hour, 8 false absorption amount in the first absorption tower is A4 mol/hour, S sound absorption amount in the second absorption tower is M(1
The absorption amount in the first absorption tower and the second absorption tower is each 9 mol/hour.
なお、ここで第１吸収塔及び第２吸収塔でのへ吸収モル
数をＢと同じ値にしたのは、の反応速度が、排ガス中の
へが液中に溶けこむ速度で定まり、ａａｓｏｌ−／２％
Ｏの濃度に左右されない反応特性に基づく本のである。The reason why the number of moles absorbed by aasol in the first absorption tower and the second absorption tower is set to the same value as B is that the reaction rate of aasol- /2%
This book is based on reaction characteristics that are not affected by O concentration.
（また排ガス中のへ濃度は８へ濃度に比べるとは石かに
高く、第１．２吸収塔の偽ガス濃度は同じとみなされゐ
からである。）
吸収された１モルの５ｏｓＦｉ化学当量関係に基づいて
１モルの０ａ８ｏｓ＠′ＡＨ＠Ｏを生成する。一方１モ
ルの０ａ８０３・ ４１１．０は４モルの偽と反応して
１モルの０ａ８ｏ４・２鳥０を生成する。このことけ逆
に云えば１モルの偽で２モルのＣａ８０ｇ・１
／／２穐０ を酸化すること虻なり、更には１モルのへ
で２モルのＢＣ）２相当分を酸化して工水石膏Ｃａ８０
３・２１０を創生することを意味する。(Also, the concentration of F in the exhaust gas is much higher than that of F, and the pseudo gas concentration in the No. 1.2 absorption tower is considered to be the same.) Chemical equivalent of 1 mole of absorbed 5osFi Based on the relationship, one mole of 0a8os@'AH@O is produced. On the other hand, 1 mole of 0a803.411.0 reacts with 4 moles of fake to produce 1 mole of 0a8o4.2bird0. Conversely speaking, it is dangerous to oxidize 2 moles of Ca80g 1 //2 0 with 1 mole of sham, and furthermore, oxidize 2 moles of BC equivalent to 2 with 1 mole of helium. Water gypsum Ca80
It means to create 3.210.
従って、第１吸収塔から抜き出される未酸化のＣａａ８
０３− ．４４ｏ量は、（ムｘ−２Ｂ）であり、これが
第２吸収塔へ供給されるのであるから、第２吸収塔へイ
ンプットされる０ａＥＩ０３・ 、（Ｆ１ａ。Therefore, unoxidized Caa8 extracted from the first absorption tower
03-. The amount of 44o is (Mux-2B), and since this is supplied to the second absorption tower, 0aEI03., (F1a.
は、この（）、ｘ−２Ｂ）と新たに第２吸収塔で８へを
吸収して生成するＡ （１−ｘ ）の合計量（（ｈｘ
−２Ｂ）＋ム（１−Ｘ）） である。is the total amount of A (1-x) ((hx
-2B)+mu(1-X)).
第２吸収塔での酸化量、即ち偽吸収量の２倍量は２Ｂで
あるので、第２吸収塔から抜き出されるスラリーが全て
工水石膏に転化されてしまうための条件は、
（（ＡＩ −２Ｂ） ＋ Ａ（１−ｘ）） −２Ｂ −
（１（１）である。 ・パ・“１
これを解くことによって、
Ｂ ＝ −４−（２）
が得られる。化学当量的には１モルの偽で２毫ルのＳＱ
Ｊ分を酸化し得るから、全８０ｉ！吸収モル量Ａのイの
偽が吸収されることを示す（２）式は、全ＳＯ，吸収モ
ル数の４が工水石膏に転化していることを意味子る。Since the amount of oxidation in the second absorption tower, that is, twice the amount of false absorption, is 2B, the conditions for all of the slurry extracted from the second absorption tower to be converted to water gypsum are ((AI -2B) + A(1-x)) -2B -
(1(1). ・P・“1 By solving this, B = −4−(2) is obtained. In terms of chemical equivalent, 1 mole of false and 2 moles of SQ
Since it can oxidize J, the total is 80i! Equation (2), which shows that the false number A of the absorbed molar amount A is absorbed, means that the total SO, 4 of the absorbed mole number, is converted to water gypsum.
前述した通り、（Ａｘ−２Ｂ）＃ｉ第１吸収塔から抜き
出される未酸化のＣａ８０ｇ・ ’／＆ｉｏのモル量を
表わすものであり、これが負になることはあ秒置ないの
で、第１吸収塔においては（Ａｘ−２Ｂ）≧０（３）
であることが必要である。As mentioned above, (Ax-2B) #i represents the molar amount of unoxidized Ca80g・'/&io extracted from the first absorption tower, and since this is unlikely to become negative in any second, In the absorption tower, it is necessary that (Ax-2B)≧0(3).
上記（２） 、 （３）式より
Ｘ≧（Ｌ ５ （４）が
得られる。これは第１吸収塔で全ＳＯ，吸収量の半分以
上を脱硫することを意味する。From the above formulas (2) and (3), X≧(L 5 (4)) is obtained. This means that the first absorption tower desulfurizes more than half of the total amount of SO absorbed.
また（４）式は最小の偽吸収量で、ライン２０８からの
スラリ」：′が工水石膏スラリーとなる為の１１１□
。Equation (4) is the minimum false absorption amount, and the slurry from line 208':' becomes industrial water gypsum slurry, so 111
.
条件であり、換営すれば酸化装置を不要となす為には第
１吸収塔での８偽吸収量を全ｓｏ、吸収量の５０モル％
以上となせば良−ことを示して−る。In order to eliminate the need for an oxidizer if the company is replaced, the amount of 8 false absorption in the first absorption tower should be reduced to 50 mol% of the total SO and absorption amount.
The above shows that it is a good idea to do this.
一方第１図及び第２図の従来法では、第１吸収塔に於い
てＢ＝、なる条件でＸ≧ａ５を満たす脱硫を行なった場
合、Ａｘ−２Ｂ、＝Ｏとなって、亜硫酸カルシウムが残
存したまま系外へ流出するととになるので工水石膏を得
る為には第１図の１１及び第２図の１０９［示すように
酸化装置が不可欠となる。On the other hand, in the conventional method shown in Figs. 1 and 2, when desulfurization is carried out in the first absorption tower under the conditions of B=, satisfying X≧a5, Ax-2B,=O, and calcium sulfite is If it flows out of the system while remaining, it will become a problem, so in order to obtain industrial gypsum, an oxidizing device is indispensable as shown at 11 in Fig. 1 and 109 in Fig. 2.
実施例
８０２１２００ ｐｐｍ、 ０３５％を含む石炭燃焼排
ガス５００ ＆Ｎ／Ｈを第３図に示す７０−シートから
なるパイロットプラントで処理した。第１吸収塔及び第
２吸収塔は、共に同規模のグリッド充填塔を用い、吸収
剤として０ａＯＯ１粉末を水に懸濁したスラリーを調整
した。 ０ａＯＯ１スラリーを全ＳＯＪ吸収量に等しく
なるよう［１９！１吸収塔に約３０Ｌ／ｈで定量ポンプ
によって供給した。EXAMPLE 8 500 &N/H coal flue gas containing 1,200 ppm, 0.35% was treated in a 70-sheet pilot plant as shown in FIG. Both the first absorption tower and the second absorption tower used grid-packed towers of the same scale, and prepared a slurry in which OaOO1 powder was suspended in water as an absorbent. The 0aOO1 slurry was fed to the [19!1 absorption tower at a rate of about 30 L/h by a metering pump so as to be equal to the total SOJ absorption amount.
第１吸収塔では液ガス比１５にωＮで気液接触させ脱硫
本釣９０％を得た。第１吸収塔から出た排ガスを第２吸
収塔に導くと共に第１吸収塔のスラリーを約３０νｈで
抜き取り第２吸収塔罠送液した。第２吸収塔出口の排ガ
ス中の８０１は数ｐｐｍと僅かであった。一方第１吸収
塔から抜き出されたスラリー中ＫＦｉ亜硫酸カルシウム
の結晶が多く存在して−ることか確認されたが、第２吸
収塔からバランスによって抜き出されたスラリー中［１
定常状態に於いて、亜硫酸カルシウム結晶が殆んど検出
されず、工水石膏結晶を含むスラリーであった。従来、
吸収塔を２基直列に用いる方法では前述した通り吸収剤
が過剰に供給される第２吸収塔のスケール付着が問題と
なっていたが本発明方法の実験ではスケール発生が認め
られなかった。In the first absorption tower, gas-liquid contact was carried out at a liquid-gas ratio of 15 at ωN to obtain a desulfurization rate of 90%. The exhaust gas discharged from the first absorption tower was guided to the second absorption tower, and the slurry from the first absorption tower was extracted at about 30 νh and sent to the trap of the second absorption tower. The amount of 801 in the exhaust gas at the outlet of the second absorption tower was as small as several ppm. On the other hand, it was confirmed that there were many KFi calcium sulfite crystals in the slurry extracted from the first absorption tower, but in the slurry extracted from the second absorption tower by balance [1
In the steady state, almost no calcium sulfite crystals were detected, and the slurry contained industrial water gypsum crystals. Conventionally,
As mentioned above, in the method of using two absorption towers in series, there was a problem of scale adhesion in the second absorption tower where an excessive amount of absorbent was supplied, but no scale formation was observed in experiments using the method of the present invention.
以上のよう［’、木本発明法よれば、高脱硫率を得るこ
とができ酸化装置が不要で、スケール付着トラブルのな
い合理的な湿式石灰石膏性排煙脱硫処理が可能となった
。As described above, according to the method of the Kimoto invention, a high desulfurization rate can be obtained, an oxidizing device is not required, and a rational wet lime-gypsum flue gas desulfurization treatment without scale adhesion problems has become possible.
第１図、第２図は従来法、第３図は本発明に係る排ガス
処理方法を示す実施態様図である。
Ｊ′１
１１１
′：、。1 and 2 are conventional methods, and FIG. 3 is an embodiment diagram showing an exhaust gas treatment method according to the present invention. J'1 111':,.
Claims (1)
化合物を含むスラリーで湿式洗浄する方法に於いて、排
ガスを第１吸収塔（導−九後第２吸収塔に導く一方、カ
ルシウム化合物を含むＳＯ吸収用スラリーを前記第１吸
収塔に導き、次いで前記第１吸収塔から抜き出したカル
シウム化合物を含むスラリーを前記第２吸収塔へ導くと
共に１前記第１吸収塔〒０８−吸収量を゛前記第１吸収
塔及び前記第２吸収塔での全８０！吸収量の５０モル％
以上となし、前□記第２吸収塔での偽による亜硫酸塩の
酸化量を前記第２吸収塔でのＳＯ，吸収量よ抄多くする
ことを特徴とする排ガスの処理方法In a method of wet-cleaning exhaust gas containing at least 8 false gas and H2 gas with a slurry containing a calcium compound, the exhaust gas is introduced into a first absorption tower (after being led to a second absorption tower, while containing a calcium compound). The slurry for SO absorption is introduced into the first absorption tower, and then the slurry containing the calcium compound extracted from the first absorption tower is introduced into the second absorption tower. 50 mol% of the total 80! absorption amount in the first absorption tower and the second absorption tower
In accordance with the above, an exhaust gas treatment method characterized in that the amount of oxidized sulfite in the second absorption tower described above is made larger than the amount of SO and absorption in the second absorption tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56170789A JPS5874126A (en) | 1981-10-27 | 1981-10-27 | Treatment for waste gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP56170789A JPS5874126A (en) | 1981-10-27 | 1981-10-27 | Treatment for waste gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS5874126A true JPS5874126A (en) | 1983-05-04 |
Family
ID=15911387
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP56170789A Pending JPS5874126A (en) | 1981-10-27 | 1981-10-27 | Treatment for waste gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS5874126A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4887567A (en) * | 1985-04-10 | 1989-12-19 | Honda Giken Kogyo Kabushiki Kaisha | Connecting arrangement in valve operating system for internal combustion engine |
| CN108905505A (en) * | 2018-07-20 | 2018-11-30 | 协建（江苏）智能装备有限公司 | A kind of chemical industry tail gas purification device |
-
1981
- 1981-10-27 JP JP56170789A patent/JPS5874126A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4887567A (en) * | 1985-04-10 | 1989-12-19 | Honda Giken Kogyo Kabushiki Kaisha | Connecting arrangement in valve operating system for internal combustion engine |
| CN108905505A (en) * | 2018-07-20 | 2018-11-30 | 协建（江苏）智能装备有限公司 | A kind of chemical industry tail gas purification device |
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