JPS6045957B2 - Treatment method for fluorine in flue gas desulfurization wastewater - Google Patents
Treatment method for fluorine in flue gas desulfurization wastewaterInfo
- Publication number
- JPS6045957B2 JPS6045957B2 JP57147827A JP14782782A JPS6045957B2 JP S6045957 B2 JPS6045957 B2 JP S6045957B2 JP 57147827 A JP57147827 A JP 57147827A JP 14782782 A JP14782782 A JP 14782782A JP S6045957 B2 JPS6045957 B2 JP S6045957B2
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- JP
- Japan
- Prior art keywords
- fluorine
- wastewater
- aluminum
- cooling process
- flue gas
- 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.)
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- Treating Waste Gases (AREA)
- Removal Of Specific Substances (AREA)
Description
【発明の詳細な説明】
本発明は石灰炭ボイラの排脱廃水中のフゾ素の処理方法
に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for treating fuzomine in wastewater discharged from a lime coal boiler.
石炭焚ポイラの排脱排水中のフッ素濃度を１５ｍ９ｌｌ
以下（全国一律基準）とする方法として、従来、第１図
に示すように廃水に石灰乳あるいは消石灰粉を加え、ｐ
Ｈ７〜１１程度にし、ＣａＦ２として析出させ、固液分
離する方法等がある。Fluorine concentration in wastewater discharged from coal-fired boilers was reduced to 15ml9ll
Conventionally, as shown in Figure 1, lime milk or slaked lime powder is added to wastewater to achieve the following (uniform nationwide standard).
There is a method in which the temperature is adjusted to about H7 to 11, precipitated as CaF2, and solid-liquid separation is performed.
第１図について以下に簡単に説明する。FIG. 1 will be briefly explained below.
石炭を燃料とする燃焼排ガスは石炭−石膏法による脱硫
装置により処理される。Combustion exhaust gas using coal as fuel is treated by a desulfurization device using the coal-gypsum method.
すなわち、燃焼排ガスは冷却工程１において冷却、除聖
され、ついて吸収工程２に導かれ吸収液により硫黄酸化
物が吸収除去されたのち清浄ガスとして放出される。そ
の際、冷却工程１からは燃料に起因するＣ１。That is, the combustion exhaust gas is cooled and decontaminated in a cooling step 1, and then led to an absorption step 2, where sulfur oxides are absorbed and removed by an absorption liquid, and then released as clean gas. At this time, from the cooling step 1, C1 is caused by the fuel.
、Ｆ、Ｂ、重金属等を含む冷却工程廃水２１が、フライ
アッシュを固液分離したのち、もしくはそのまま排出さ
れる。また、吸収工程２、酸化工程３を経て石膏分離工
程４からは排煙処理システムに起因する難分解性のニチ
オン酸イオン等のＣＯＤ成分を含む上澄水２２が排出さ
れ、副生石膏１１が回収される。, F, B, heavy metals, etc., is discharged after solid-liquid separation of fly ash or as it is. Furthermore, after passing through the absorption process 2 and oxidation process 3, supernatant water 22 containing COD components such as persistent nithionic acid ions caused by the flue gas treatment system is discharged from the gypsum separation process 4, and by-product gypsum 11 is recovered. Ru.
この石膏分離工程４からの上澄水２２はＣＯＤ酸分離工
程５に導き、硫酸３１を添加し、蒸気３・２により加熱
して排水中のニチオン酸イオンを分解したのち、冷却工
程１に回収し冷却工程１の補給水として再利用する。一
方、冷却工程１からのＦ、Ｂ、重金属を含む冷却工程排
水２１は第１ｐＨ調整工程７に導き、消石灰３４を加え
てＰＨ７〜１１に調整し、排水中のＦおよび重金属をそ
れぞれ難溶性のフッ化カルシウムおよび水酸化物等とし
て析出させ、ついで固液分離工程８に導き、高分子凝集
剤３５を添加して該フッ化カルシウムおよび水酸化物等
を粗大フロック化したのち沈殿分離する。The supernatant water 22 from this gypsum separation process 4 is led to the COD acid separation process 5, where sulfuric acid 31 is added and heated with steam 3 and 2 to decompose the nitionate ions in the waste water, and then recovered in the cooling process 1. Reuse as make-up water for cooling process 1. On the other hand, the cooling process wastewater 21 containing F, B, and heavy metals from the cooling process 1 is led to the first pH adjustment process 7, where slaked lime 34 is added to adjust the pH to 7 to 11, and the F and heavy metals in the wastewater are removed by slightly soluble Calcium fluoride, hydroxide, etc. are precipitated, and then led to a solid-liquid separation step 8, where a polymer flocculant 35 is added to form coarse flocs of calcium fluoride, hydroxide, etc., and then precipitated and separated.
沈殿分離した固液分離工程分離スラリー２３は脱水工程
１０に導き、脱水したのちライン１２から抜出し、処分
する。Ｆ等を除去して固液分離工程８からの排水か第２
ＰＨ調整工程９に導き、硫酸３１を添加して、ＰＨを放
流規制範囲内に調整し、処理水２４として放流する。The precipitated solid-liquid separation step separated slurry 23 is led to a dehydration step 10, and after being dehydrated, it is extracted from a line 12 and disposed of. After removing F etc., the waste water from solid-liquid separation step 8 or the second
The water is led to a pH adjustment step 9, where sulfuric acid 31 is added to adjust the pH to within the discharge regulation range, and the treated water is discharged as treated water 24.
しかし、上記の従来の方法は以下のような欠点があつた
。However, the above conventional method has the following drawbacks.
石炭焚ボイラ排脱廃水の冷却工程廃水はＦ，重金属以外
にフッ素の処理性に悪影響を与えるＢ（ホウフッ化物他
）等を含んでおり、かつその水質は燃料条件（炭種、石
炭混焼率）および排ガス処理システムの構成、操作条件
等により大幅に変動するため、従来の方法ては処理水Ｆ
濃度を安定して１５ｍ９１′以下にすることは困難てあ
つた。The wastewater from the cooling process of coal-fired boiler discharge wastewater contains F and heavy metals as well as B (borofluoride, etc.), which have a negative effect on the processability of fluorine, and the quality of the water depends on the fuel conditions (coal type, coal co-combustion rate). The conventional method uses treated water
It was difficult to keep the concentration stably below 15m91'.
以上のように、フッ素処理は石炭焚ボイラ排脱廃水処理
システムの重要な部分を構成しているが、上記したよう
に、従来の方法では処理水Ｆ濃一度か１５ｍｇＩ′以下
（全国一律基準）を安定して得られない欠点があつた。
従来法では、該Ｆ濃度は通常２０〜３０ｍ９１′程度て
あつた）。そこて本発明者らは上記の対策として、当該
廃水中に共存し、かつＦと鎖体（ＡｌＦｇ−Ｎ，ここで
２ｎは１〜６）を形成してＦ−イオンの活性を失わせ、
冷却工程の装置材料に対する腐食抑制効果を生せせしめ
るＡ１（特開昭５５−１５９７６号公報参照）を利用す
ることを考え、本発明に到達したものである。As mentioned above, fluorine treatment constitutes an important part of the coal-fired boiler discharge wastewater treatment system, but as mentioned above, in the conventional method, the treated water F concentration is 1 or less than 15 mg I' (national uniform standard). The drawback was that it was not possible to obtain stable results.
In the conventional method, the F concentration was usually about 20 to 30 m91'). Therefore, the present inventors have taken as a countermeasure against the above problem, coexisting in the wastewater and forming a chain with F (AlFg-N, where 2n is 1 to 6) to lose the activity of F- ions.
The present invention was developed by considering the use of A1 (see Japanese Unexamined Patent Publication No. 15976/1983) which produces a corrosion inhibiting effect on equipment materials in the cooling process.
すなわち本発明は、排煙脱硫廃水中のフゾ素を処理する
方法において、排煙の冷却工程にアルミニウム化合物を
注入し、冷却工程廃水中に含まれるホウフッ化物を分解
してフッ素−アルミニウム鎖体を生成させ、次いで冷却
工程廃水にカルシウィム化合物を添加し、析出するフッ
化カルシウムを分離することを特徴とする排煙脱硫廃水
中のフッ素の処理方法に関するものである。That is, the present invention provides a method for treating fluorine in flue gas desulfurization wastewater, in which an aluminum compound is injected into the flue gas cooling process to decompose borofluoride contained in the cooling process wastewater to form fluorine-aluminum chains. The present invention relates to a method for treating fluorine in flue gas desulfurization wastewater, which is characterized by adding a calciwim compound to the cooling process wastewater and separating precipitated calcium fluoride.
本発明方法によれば、石炭焚ボイラ脱硫装置の冷却工程
廃水中にＦ−イオンとともに共存するホウフッ化物を分
解することによつて処理水Ｆ濃度を１５ｍ９１ｅ以下と
し、Ｆの処理性の安定を図ることができると同時に、Ｆ
−イオンがＡｌによりマスキング（錯体形成）されるこ
とによつて、冷却工程の装置材料に対する腐食抑制効果
が期待され、また、冷却工程廃水はフライアッシュの溶
解等によるアルミニウムを含有しており、上記錯体のＮ
源として利用できるため好都合である等の効フ果を奏し
得る。According to the method of the present invention, by decomposing borofluoride coexisting with F- ions in the cooling process wastewater of a coal-fired boiler desulfurization equipment, the F concentration in treated water is reduced to 15 m91e or less, and the F treatment performance is stabilized. At the same time, F
- Masking (complex formation) of ions with Al is expected to have a corrosion inhibiting effect on equipment materials in the cooling process, and the cooling process wastewater contains aluminum due to dissolution of fly ash, etc. Complex N
Since it can be used as a source, it can produce effects such as convenience.
以下、添付図面等を参照して本発明方法を詳細に説明
する。Hereinafter, the method of the present invention will be explained in detail with reference to the accompanying drawings and the like.
第２図は本発明方法の一実施態様例を示すフローシー
トである。FIG. 2 is a flow sheet showing an embodiment of the method of the present invention.
第２図中、第１図を同一符号は門第１図と同一機能部品
を示す。 第２図に示すように、アルミニウム調整工程
６からアルミニウム化合物３３としてアルミニウムの水
酸化物、塩（硫酸塩、塩酸塩他）、アルミン酸の塩、例
えば水酸化アルミニウム、硫酸アルミ身ニウム、ポリ塩
化アルミニウム、アルミニウム酸ソーダ等の１種または
２種以上を直接もしくはＣＯＤ酸分解工程５からの排水
を経て冷却工程１に流入させ、冷却工程１において、Ｆ
−イオンとともに該廃水に含まれかつ難処理性てあるホ
ウフッ化物を第１式に示すように分解し、フッ素一アル
ミニウム錯体を生成させる。In FIG. 2, the same reference numerals as in FIG. 1 indicate the same functional parts as in FIG. 1. As shown in FIG. 2, from the aluminum preparation step 6, aluminum compounds 33 include aluminum hydroxides, salts (sulfates, hydrochlorides, etc.), aluminic acid salts, such as aluminum hydroxide, aluminum sulfate, polychloride. One or more types of aluminum, sodium aluminate, etc. are introduced into the cooling process 1 directly or through the waste water from the COD acid decomposition process 5, and in the cooling process 1, F
- Borofluoride, which is contained in the wastewater together with ions and is difficult to treat, is decomposed as shown in the first formula to generate a fluorine-aluminum complex.
Ａｌ３＋＋ＢＦｎ（０Ｈ）−４−。Al3++BFn(0H)-4-.
＋（ｎ−１）Ｈ２Ｏ＝ＡｌＦｋ？ｎ＋Ｂ（０Ｈ）３＋（
ｎ−１）Ｈ＋ 第１式 この反応は冷却工程１の条件（
温度５０〜６０゜Ｃ，ＰＨ５〜２，滞留時間１０〜２０
Ｈｒ）で可能であるため、特にこの反応のための工程を
必要としない利点がある。 また、アルミニウム化合物
３３の添加量はアルミニウム化合物３３を添加したのち
の冷却工程廃水２１中における溶解性アルミニウムのフ
ッ素に対するモル比が０．４Ｊ））．上、好ましくは０
．５以上となるようにする。+(n-1)H2O=AlFk? n+B(0H)3+(
n-1) H+ Formula 1 This reaction is carried out under the conditions of cooling step 1 (
Temperature 50~60°C, PH5~2, Residence time 10~20
Hr), there is an advantage that no special step for this reaction is required. Further, the amount of the aluminum compound 33 added is such that the molar ratio of soluble aluminum to fluorine in the cooling process wastewater 21 after adding the aluminum compound 33 is 0.4 J)). above, preferably 0
．． Make it 5 or more.
ついで、フッ素−アルミニウム錯体を含む冷却工程廃
水２１を第１ＰＨ調整工程７に導き、消石灰【 等の
カルシウム化合物を添加してＰＨを７〜１１，好ましく
は７〜９に調整し、第２式に示すようにフッ素−アルミ
ニウム錯体を分解し、難溶性のフッ化カルシウムとして
析出させる。Next, the cooling process wastewater 21 containing the fluorine-aluminum complex is led to the first pH adjustment process 7, and a calcium compound such as slaked lime is added to adjust the pH to 7 to 11, preferably 7 to 9, and the pH is adjusted to 7 to 11, preferably 7 to 9. As shown, the fluorine-aluminum complex is decomposed and precipitated as poorly soluble calcium fluoride.
同時に、冷却工程廃水２１中に存在するＦ−イオンは、
第３式に示すように反応して、難溶性のフッ化カルシウ
ムとして析出させる。At the same time, the F- ions present in the cooling process wastewater 21 are
It reacts as shown in the third equation and is precipitated as poorly soluble calcium fluoride.
ｆ−＋Ｃａ（０Ｈ）２＝ＣａＦ２＋０Ｈ−・・ ・・
・第３式上記フッ化カルシウムの他に水酸化アルミニウ
ム、重金属水酸化物等を含む第１ＰＨ調整工程７のＪ排
水は固液分離工程８に導き、高分子凝集剤３５を添加し
て該フッ化カルシウム等を粗大フロック化したのち沈殿
分離する。f-+Ca(0H)2=CaF2+0H-...
・Formula 3 The J wastewater from the first PH adjustment step 7, which contains aluminum hydroxide, heavy metal hydroxides, etc. in addition to the above calcium fluoride, is led to the solid-liquid separation step 8, where a polymer flocculant 35 is added to remove the fluoride. Calcium chloride, etc. are formed into coarse flocs and then separated by precipitation.
この際、第２式に示す反応により生成した水酸化アルミ
ニウムは凝集剤としての作用を有するものであるから、
この沈殿ｊ分離を促進させる効果がある。沈殿分離した
固液分離工程分離スラリー２３は、脱水工程１０に導き
、脱水したのち処分される。At this time, since the aluminum hydroxide produced by the reaction shown in the second equation acts as a flocculant,
It has the effect of promoting this precipitation separation. The precipitated solid-liquid separation step separated slurry 23 is led to a dehydration step 10, dehydrated, and then disposed of.
フッ素等を除去した固液分離工程８からの排水は、第２
ＰＨ調整工程９に導き、硫酸３１を添加２してＰＨを放
流規制範囲内に調整し、フッ素濃度１５ｍｇＩｆ以下の
処理水２４として放流される。本発明方法の具体例を以
下に示す。実施例１
出力１５０ＭＷの石炭火力発電設備から排出され−る排
ガス（４０００００ＮｄＩＨ）を石炭一石膏法て脱硫し
た際に発生する冷却工程廃水中のフッ素を第２図に示す
フローで処理した。The wastewater from the solid-liquid separation process 8 from which fluorine etc. have been removed is
The water is led to a pH adjustment step 9, where sulfuric acid 31 is added 2 to adjust the pH to within the discharge regulation range, and the water is discharged as treated water 24 with a fluorine concentration of 15 mg If or less. Specific examples of the method of the present invention are shown below. Example 1 Fluorine in cooling process wastewater generated when exhaust gas (400,000 NdIH) discharged from a coal-fired power generation facility with an output of 150 MW was desulfurized using the coal-gypsum method was treated according to the flow shown in FIG. 2.
条件および結果は以下の通りてあつた。The conditions and results were as follows.
（１）アルミニウム調整工程６からのアルミニウム化合
物３３の添加条件アルミニウム化合物の種類 アルミン
酸ソーダ添加量 ３．２ｋｇＡ
１１Ｈ（２）冷却工程１からの冷却工程廃水２１の水量
および水質水量 ８．０ＲＩＨ
ＰＨ１．０Ｓｓ１８０００ｍ
９１ｅＦ９５０ｍｇ
ノ′
ＢｌＯＯｍｇＩｌＡｌ７５ＯｍｇＩ
′
Ａ１／Ｆ（モル比）０．５６
（３）第１ＰＨ調整工程７のＰＨ調整条件カルシウム化
合物の種類 消石灰
Ｒｎυ
滞留時間 ？
：４） 第１ＰＨ調整工程７の出口水量および水質水量
８．６ｄ１ＨＰＨ８．１ＳＳ３６０００ｍ
ｇ１ｆ
（５）固液分離工程８の分離条件
高分子凝集剤の種類 サンポリー３０５
添加量 ３ｐｐｍ
滞留時間 ？
（６）固液分離工程８の出口水量および水質水量
８．４ｒｒ１ＩＨＰＨ８．１ＳＳ６ｍｇＩｅＦ
９ｍ９１ｅＡ１２
７ｍ９１′
（７）固液分離工程８からの固液分離工程分離スラリー
２３の量および水質スラリー量 ０．２ｄ１Ｈ
ＰＨ８．２ｓｓ１８Ｗｔ
％
（８）第２ＰＨ調整工程９ＰＨ調整条件
ＰＨ７．５
滞留時間 １０１１１１ｎ
（９）処理水２４の量および水質
水量 ８．４ぼＩＨ
ＰＨ７．６ＳＳ８ｍｇＩ
′
Ｆ９ｍ９ｌｅ
実施例２
実施例１のアルミニウム調整工程６からのアルミニウム
化合物３３の添加量を変えて、実施例１と同様に第２図
に示すフローで処理し、アルミニウム化合物３３の添加
擁と処理水Ｆ濃度との関係）−を調べた結果は第３図に
示す通りであつた。(1) Addition conditions for aluminum compound 33 from aluminum adjustment step 6 Type of aluminum compound Addition amount of sodium aluminate 3.2 kgA
11H (2) Water quantity and quality of cooling process wastewater 21 from cooling process 1 8.0RIH PH1.0Ss18000m 91eF950mg No'BlOOmgIlAl75OmgI' A1/F (molar ratio) 0.56 (3) PH adjustment in first PH adjustment process 7 Conditions Type of calcium compound Slaked lime Rnυ Residence time ? :4) Outlet water volume and water quality of the first PH adjustment step 7
8.6d1HPH8.1SS36000m g1f (5) Separation conditions for solid-liquid separation step 8 Type of polymer flocculant Sunpoly 305 Addition amount 3ppm Residence time ? (6) Outlet water volume and water quality of solid-liquid separation step 8
8.4rr1IHPH8.1SS6mgIeF 9m91eA12 7m91' (7) Amount of solid-liquid separation step separation slurry 23 from solid-liquid separation step 8 and water quality slurry amount 0.2d1H PH8.2ss18Wt% (8) Second PH adjustment step 9 PH adjustment conditions PH7. 5 Residence time 101111n (9) Amount and quality of treated water 24 Quantity 8.4 IH PH7.6SS8mgI'F9m9le Example 2 Example 2 by changing the amount of aluminum compound 33 from aluminum adjustment step 6 of Example 1 Similarly to 1, the treatment was carried out according to the flow shown in FIG. 2, and the relationship between the addition of aluminum compound 33 and the F concentration of the treated water was investigated. The results were as shown in FIG.
なお、第３図の横赳Ａ１／Ｆ（モル比）は、アルミニウ
ム化合物３３を添加した後の冷却工程廃水２１について
のＡ１／Ｆ（モル比）てある。以上の実施例から明らか
なように、本発明方法に従つて石炭焚ボイラ排脱廃水の
フッ素化処理に際し、硫酸装置の冷却工程にアルミニウ
ム化合物を添加することにより下記の効果を得ることが
できる。Note that the horizontal A1/F (molar ratio) in FIG. 3 is the A1/F (molar ratio) for the cooling process wastewater 21 after adding the aluminum compound 33. As is clear from the above examples, the following effects can be obtained by adding an aluminum compound to the cooling process of the sulfuric acid equipment during fluorination treatment of coal-fired boiler discharged wastewater according to the method of the present invention.
（１）冷却工程廃水中にＦ−イオンとともに共存するホ
ウフッ化物は脱硫装置の冷却工程においてフゾ素−アル
ミニウム錯体への分解が可能であり、特に分解反応のた
めの別途工程を必要としない。(1) Cooling process The borofluoride coexisting with F- ions in the wastewater can be decomposed into a fusorine-aluminum complex in the cooling process of the desulfurizer, and no special process for the decomposition reaction is required.
（Ｉｉ）冷却工程廃水中にはフライアッシュの溶解等に
起因するアルミニウムを含んでおり、このアルミニウム
をフッ素−アルミニウム錯体生成のためのアルミニウム
源として利用できるため、アルミニウム化合物の添加量
を低減できる。(Ii) Cooling process wastewater contains aluminum resulting from dissolution of fly ash, etc., and since this aluminum can be used as an aluminum source for producing a fluorine-aluminum complex, the amount of aluminum compounds added can be reduced.
（Ｉｉｉ）アルミニウム化合物の添加量は、アルミニウ
ム化合物を添加したのちの冷却工程廃水中における溶解
性アルミニウムのフッ素に対するモル比（Ａ１／Ｆ）が
０．似上、好ましくは０．５以上となるようにすること
により、処理水Ｆ濃度１５ｍ９１ｆ以下（約１０ｍ９１
ｆ）で、かつ安定したフッ素処理性が得られる。（Ｉｖ
）上記のフッ素処理性以外にアルミニウムによりフッ素
イオンがマスキングされることにより、冷却工程の装置
材料に対する腐食抑制効果も得られる。(Iii) The amount of the aluminum compound added is such that the molar ratio (A1/F) of soluble aluminum to fluorine in the cooling process wastewater after adding the aluminum compound is 0. Similarly, by setting the value to preferably 0.5 or more, the treated water F concentration is 15 m91f or less (approximately 10 m91
f) and stable fluorine treatment properties can be obtained. (Iv
) In addition to the above-mentioned fluorine treatment properties, the masking of fluorine ions by aluminum also provides a corrosion inhibiting effect on equipment materials during the cooling process.
第１図は従来の排煙脱硫廃水中のフッ素処理方法を示す
フローシート、第２図は本発明方法の一実施態様を示す
フローシート、第３図は本発明の実施例で得られたＡｌ
ｌＦモル比と処理水Ｆ濃度との関係を示す図表である。Figure 1 is a flow sheet showing a conventional method for treating fluorine in flue gas desulfurization wastewater, Figure 2 is a flow sheet showing an embodiment of the method of the present invention, and Figure 3 is an Al
It is a chart showing the relationship between IF molar ratio and treated water F concentration.
Claims (1)
排煙の冷却工程にアルミニウム化合物を注入し、冷却工
程廃水中に含まれるホウフッ化物を分解してフッ素−ア
ルミニウム鎖体を生成させ、次いで冷却工程廃水にカル
シウム化合物を添加し、析出するフッ化カルシウムを分
離することを特徴とする排煙脱硫廃水中のフッ素の処理
方法。1. In a method for treating fluorine in flue gas desulfurization wastewater,
An aluminum compound is injected into the flue gas cooling process to decompose the borofluoride contained in the cooling process wastewater to produce fluorine-aluminum chains, and then a calcium compound is added to the cooling process wastewater to precipitate calcium fluoride. A method for treating fluorine in flue gas desulfurization wastewater, the method comprising separating fluorine from flue gas desulfurization wastewater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57147827A JPS6045957B2 (en) | 1982-08-27 | 1982-08-27 | Treatment method for fluorine in flue gas desulfurization wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP57147827A JPS6045957B2 (en) | 1982-08-27 | 1982-08-27 | Treatment method for fluorine in flue gas desulfurization wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5939385A JPS5939385A (en) | 1984-03-03 |
| JPS6045957B2 true JPS6045957B2 (en) | 1985-10-12 |
Family
ID=15439126
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP57147827A Expired JPS6045957B2 (en) | 1982-08-27 | 1982-08-27 | Treatment method for fluorine in flue gas desulfurization wastewater |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6045957B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2934549B2 (en) * | 1992-02-03 | 1999-08-16 | 三菱重工業株式会社 | Exhaust gas treatment method |
| CN113511739A (en) * | 2021-04-13 | 2021-10-19 | 兰州石化职业技术学院 | Preparation method of low-chlorination external-drainage recycled circulating water |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5310553A (en) * | 1976-07-15 | 1978-01-31 | Kurita Water Ind Ltd | Mehtod of treating waste water containing fluorine and boron |
| JPS5547119A (en) * | 1978-09-29 | 1980-04-03 | Asahi Glass Co Ltd | Treatment of exhaust gas containing fluorine |
| JPS5781881A (en) * | 1980-11-11 | 1982-05-22 | Kurita Water Ind Ltd | Treatment of water containing boron |
| JPS57105284A (en) * | 1980-12-22 | 1982-06-30 | Kurita Water Ind Ltd | Purification of waste water used in desulfurization of exhaust gas |
| JPS57144086A (en) * | 1981-03-03 | 1982-09-06 | Kurita Water Ind Ltd | Treatment of water contg. fluoride |
-
1982
- 1982-08-27 JP JP57147827A patent/JPS6045957B2/en not_active Expired
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5310553A (en) * | 1976-07-15 | 1978-01-31 | Kurita Water Ind Ltd | Mehtod of treating waste water containing fluorine and boron |
| JPS5547119A (en) * | 1978-09-29 | 1980-04-03 | Asahi Glass Co Ltd | Treatment of exhaust gas containing fluorine |
| JPS5781881A (en) * | 1980-11-11 | 1982-05-22 | Kurita Water Ind Ltd | Treatment of water containing boron |
| JPS57105284A (en) * | 1980-12-22 | 1982-06-30 | Kurita Water Ind Ltd | Purification of waste water used in desulfurization of exhaust gas |
| JPS57144086A (en) * | 1981-03-03 | 1982-09-06 | Kurita Water Ind Ltd | Treatment of water contg. fluoride |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5939385A (en) | 1984-03-03 |
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