JP2003053341A - Method and apparatus for treating wastewater containing carbonic acid together with boron - Google Patents
Method and apparatus for treating wastewater containing carbonic acid together with boronInfo
- Publication number
- JP2003053341A JP2003053341A JP2001243149A JP2001243149A JP2003053341A JP 2003053341 A JP2003053341 A JP 2003053341A JP 2001243149 A JP2001243149 A JP 2001243149A JP 2001243149 A JP2001243149 A JP 2001243149A JP 2003053341 A JP2003053341 A JP 2003053341A
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- JP
- Japan
- Prior art keywords
- boron
- type
- exchange resin
- ion exchange
- carbonic acid
- 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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- Treatment Of Water By Ion Exchange (AREA)
Abstract
(57)【要約】
【課題】 ホウ素吸着樹脂によりホウ素含有排水を処理
するときに起こる排水中の炭酸（H2CO3、HCO3又はCO3）
によるホウ素吸着の妨害をなくし、排水中に炭酸が相当
量含有されている場合にも樹脂体積当たりのホウ素吸着
除去量が少なくなり、早期に処理塔中の樹脂を交換しな
ければならない事態を防止する。
【解決手段】 ホウ素とともに炭酸を含む排水を、H型
に調整した強酸性陽イオン交換樹脂を充填した第１イオ
ン交換塔に通水して陽イオンを吸着・除去する第１工程
と、OH型に調整した陰イオン交換樹脂を充填した第２イ
オン交換塔に通液して弱酸を除く陰イオンを除去する第
２工程と、OH型に調整した強塩基性陰イオン交換樹脂、
又は強塩基性陰イオン交換樹脂とH型に調整した強酸性
陽イオン交換樹脂の混合樹脂を充填した第3イオン交換
塔に通液してホウ素を吸着除去する第３工程を行って排
水からホウ素を除去するに当たり、前記第１工程と第２
工程及び／又は第２工程と第３工程の間に脱炭酸工程を
行う。
(57) [Summary] [PROBLEMS] Carbonic acid (H 2 CO 3 , HCO 3 or CO 3 ) in wastewater generated when treating boron-containing wastewater with a boron adsorption resin
Eliminates interference with boron adsorption and reduces the amount of boron adsorbed per resin volume even when wastewater contains a considerable amount of carbonic acid, preventing the situation where the resin in the treatment tower must be replaced early. I do. SOLUTION: A first step of adsorbing and removing cations by passing a wastewater containing boron and carbonic acid through a first ion exchange column filled with a strongly acidic cation exchange resin adjusted to H type, and an OH type A second step of removing anions excluding weak acids by passing through a second ion exchange column filled with an anion exchange resin adjusted to a strong anion exchange resin adjusted to an OH type,
Alternatively, a third step of adsorbing and removing boron by passing the solution through a third ion exchange column filled with a mixed resin of a strongly basic anion exchange resin and a strongly acidic cation exchange resin adjusted to H form is performed, and boron is discharged from the wastewater. In removing the first step and the second step
A decarboxylation step is performed between the second step and the third step.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、排水からホウ素を
ホウ素選択吸着樹脂により吸着・除去する方法及び装置
に係り、特に原水にホウ素のほかに炭酸を含有する場合
にその妨害なくホウ素を効率的に吸着除去する方法及び
装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for adsorbing and removing boron from waste water with a boron selective adsorption resin, and particularly when the raw water contains carbonic acid in addition to boron, the boron can be efficiently adsorbed without interference. The present invention relates to a method and an apparatus for adsorbing and removing on a substrate.
【０００２】[0002]
【従来の技術】一般にニッケルめっき液あるいはアルミ
表面処理液中にはホウ素化合物（ホウ酸等）が含まれて
おり、これらを扱う工場においてはホウ素を含有する排
水が発生する。またガラス、釉薬、アルミコンデンサー
等ホウ素を使用する工場においてもホウ素を含む排水が
発生する。ホウ素化合物は植物にとっては必須微量元素
であり、海水には4〜5mg/1程度含まれていることは周知
のことである。一方、ホウ素が人体に与える影響は必ず
しも明確ではないものの低濃度の継続摂取において生殖
機能の低下などの健康障害を起こす可能性が指摘されて
いる。平成11年2月、ホウ素の環境基準として1mg/1以下
が告示され、平成13年6月、排水基準も公布、7月1日よ
り施行されたため、これらのホウ素を含む工程排水中の
ホウ素除去処理が必要となる。2. Description of the Related Art Generally, a nickel plating solution or an aluminum surface treatment solution contains a boron compound (boric acid or the like), and a waste water containing boron is generated in a factory handling these compounds. Wastewater containing boron is also generated in factories that use boron such as glass, glaze, and aluminum capacitors. It is well known that boron compounds are essential trace elements for plants, and seawater contains about 4-5 mg / 1. On the other hand, although the effect of boron on the human body is not always clear, it has been pointed out that continued ingestion of low concentrations may cause health problems such as reduced reproductive function. In February 1999, 1 mg / 1 or less was announced as an environmental standard for boron, and since June 2001, the drainage standard was also promulgated and it came into effect on July 1. Processing is required.
【０００３】排水中のホウ素の除去方法としては、ホウ
素含有排水にアルミニウム化合物及びカルシウム化合物
を用いて凝集沈殿によりホウ素化合物を分離除去する方
法（特公昭58-15193号公報、同59-24876号公報）あるい
はニッケルめっき洗浄排水にマグネシウム塩を添加して
凝集沈殿によりホウ素を分離除去する方法等（平成11年
度東京都立産業技術研究所発表会予稿集ｐ52）が知られ
ている。しかし、これらの方法は、ホウ素を不溶化させ
るために多量の薬剤を使用する必要があり、発生汚泥も
多くその処理が困難であるという問題がある。As a method of removing boron in wastewater, a method of separating and removing the boron compound by coagulation precipitation using an aluminum compound and a calcium compound in the boron-containing wastewater (Japanese Patent Publication Nos. 58-15193 and 59-24876). ) Or a method of adding magnesium salt to the nickel plating cleaning wastewater and separating and removing boron by coagulation precipitation (1999 Proceedings of the Tokyo Metropolitan Institute of Industrial Technology, p52). However, these methods have a problem that it is necessary to use a large amount of chemicals for insolubilizing boron, and a lot of sludge is generated, which makes it difficult to treat the sludge.
【０００４】このような問題を解決するために、本発明
者はホウ素含有排水を強酸性陽イオン交換樹脂と弱塩基
性陰イオン交換樹脂に通液後、ホウ素選択吸着樹脂、例
えば強塩基性陰イオン交換樹脂やN-メチルグルカミンを
有するホウ素選択樹脂に通液して樹脂単位体積当たりの
ホウ素吸着量を飛躍的に増大させ、効率的に排水中のホ
ウ素を除去する方法及び装置を提案している（特願2000
-22785号）。In order to solve such a problem, the present inventor has passed the boron-containing wastewater through a strongly acidic cation exchange resin and a weakly basic anion exchange resin, and thereafter, selects a boron selective adsorption resin, for example, a strongly basic anion resin. We propose a method and device for efficiently removing boron in wastewater by passing it through an ion-exchange resin or a boron-selective resin containing N-methylglucamine to dramatically increase the amount of adsorbed boron per unit volume of resin. (Patent application 2000
-22785).
【０００５】[0005]
【発明が解決しようとする課題】しかしながら、本発明
者が経験したところによれば、上述の手段によりホウ素
含有排水を処理した場合に、意外にも樹脂単位体積当た
りのホウ素吸着除去量が少なくなり、早期に処理塔中の
樹脂を交換しなければならない事態に至ることがあっ
た。そのような事態は特に排水中にホウ素濃度が20mg/1
以下で、炭酸（H2CO 3、HCO3又はCO3）濃度が40mg/1以上
含有されているようなホウ素に対して炭酸の含有率が高
い場合に顕著に生ずる。この発明は、かかる場合にも、
ホウ素含有排水から効率的にホウ素を除去しうるよう、
上記発明を改良することを目的とする。However, the present invention
The person has experienced that boron is
Unexpectedly, the resin unit volume was applied when the contained wastewater was treated.
The amount of boron adsorbed and removed from
Sometimes it may be necessary to replace the resin.
It was In such a situation, the boron concentration in the wastewater is 20 mg / 1
Below, carbonic acid (H2CO 3, HCO3Or CO3) Concentration is 40mg / 1 or more
High carbonic acid content relative to boron content
It occurs remarkably when The present invention, even in such a case,
To efficiently remove boron from boron-containing wastewater,
It is an object to improve the above invention.
【０００６】[0006]
【課題を解決するための手段】本発明は上記課題を解決
するために、ホウ素とともに炭酸を含む排水を、H型に
調整した強酸性陽イオン交換樹脂を充填した第１イオン
交換塔に通水して陽イオンを吸着除去する第１工程と、
OH型に調整した陰イオン交換樹脂を充填した第２イオン
交換塔に通液して弱酸を除く陰イオンを除去する第２工
程と、OH型に調整した強塩基性陰イオン交換樹脂、又は
強塩基性陰イオン交換樹脂とH型に調整した強酸性陽イ
オン交換樹脂の混合樹脂を充填した第3イオン交換塔に
通液してホウ素を吸着除去する第３工程を行って排水か
らホウ素を除去するに当たり、前記第１工程と第２工程
及び／又は第２工程と第３工程の間に脱炭酸工程を行
う。In order to solve the above problems, the present invention passes wastewater containing carbonic acid together with boron through a first ion exchange column filled with a strongly acidic cation exchange resin adjusted to H type. The first step of adsorbing and removing the cations,
The second step of removing the anions except the weak acid by passing through a second ion exchange column filled with an anion exchange resin adjusted to an OH type, and a strong basic anion exchange resin adjusted to an OH type, or a strong base anion exchange resin. Boron is removed from wastewater by performing a third step of adsorbing and removing boron by passing through a third ion exchange column filled with a mixed resin of basic anion exchange resin and strongly acidic cation exchange resin adjusted to H type In doing so, a decarboxylation step is performed between the first step and the second step and / or the second step and the third step.
【０００７】上記発明において、脱炭酸は、第２工程又
は第３工程に供する処理水中の炭酸含有量（H2CO3、HCO
3又はCO3含有量）が10mg/1以下となるように行うことが
好ましく、また、本発明を例えば、ホウ素濃度が20mg/1
以下で炭酸濃度が40mg以上含有する原水のように、ホウ
素に比べて炭酸の比率が高い場合に対して行うのが効率
的である。In the above invention, the decarbonation is carried out by the carbon dioxide content (H 2 CO 3 , HCO) in the treated water to be subjected to the second step or the third step.
3 or CO 3 content) is preferably 10 mg / 1 or less.
In the following, it is efficient to carry out when the ratio of carbonic acid is higher than that of boron, such as raw water containing carbonic acid concentration of 40 mg or more.
【０００８】上記発明を実施するに当たっては、ホウ素
とともに炭酸を含む排水の流入側から順に、H型に調整
した強酸性陽イオン交換樹脂を充填した第１イオン交換
塔、OH型に調整した陰イオン交換樹脂を充填した第２イ
オン交換塔、OH型に調整した強塩基性陰イオン交換樹脂
又は強塩基性陰イオン交換樹脂とH型に調整した強酸性
陽イオン交換樹脂の混合樹脂を充填した第3イオン交換
塔を配設し、前記第１イオン交換塔と第２イオン交換塔
及び/又は第２イオン交換塔と第３イオン交換塔の間に
脱炭酸塔を設けてなる排水の処理装置を利用するのがよ
く、また、第1工程と第2工程との間に配設する脱炭酸塔
は、強制通風式ばっ気設備とし、第２工程と第３工程と
の間に配設する脱炭酸塔は、OH型に調整したI型若しく
はII型強塩基性陰イオン交換樹脂を充填したものとする
のがよい。In carrying out the above-mentioned invention, a first ion exchange column filled with a strongly acidic cation exchange resin adjusted to H type and an anion adjusted to OH type in order from the inflow side of the waste water containing carbonic acid together with boron. A second ion exchange column packed with an exchange resin, a strong basic anion exchange resin adjusted to an OH type or a mixed resin of a strong basic anion exchange resin and a strongly acidic cation exchange resin adjusted to an H type An apparatus for treating waste water comprising three ion exchange towers, and a decarbonation tower provided between the first ion exchange tower and the second ion exchange tower and / or between the second ion exchange tower and the third ion exchange tower. It is often used, and the decarbonation tower installed between the first step and the second step should be a forced ventilation type aeration facility, and the decarbonation tower installed between the second step and the third step. Carbonic acid tower is type I or type II strong basic anion exchange adjusted to OH type It is preferable to those filled with fat.
【０００９】[0009]
【発明の実施の形態】以下、本発明の実施形態を具体的
に説明する。本発明において処理対象とする液は、ガラ
ス製造工場から排出される排液のようなホウ素とともに
炭酸を含有する排液である。このような排液の代表的な
組成は表１に示されている。このようにホウ素濃度が20
mg/1以下で炭酸濃度（H2CO3、HCO3又はCO3含有量）が40
mg/1以上含有する排水を処理するとき、後に示すように
ホウ素選択吸着樹脂にホウ素とともに炭酸が吸着してホ
ウ素の吸着量が低下するという問題が顕著になる。BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be specifically described below. The liquid to be treated in the present invention is an effluent containing carbonic acid with boron, such as effluent discharged from a glass manufacturing plant. A typical composition of such drainage is shown in Table 1. Thus, the boron concentration is 20
Carbon dioxide concentration (H 2 CO 3 , HCO 3 or CO 3 content) of 40 mg / mg or less
When treating wastewater containing mg / 1 or more, as will be shown later, the problem that carbon dioxide is adsorbed together with boron on the boron selective adsorption resin and the adsorbed amount of boron is reduced.
【００１０】[0010]
【表１】 [Table 1]
【００１１】本発明では、このようなホウ素とともに炭
酸を含む排水を、まず、H型に調整した強酸性陽イオン
交換樹脂を充填した第１イオン交換塔に通水して陽イオ
ンを吸着除去する。この工程により排液中のNaイオンや
Caイオンのような陽イオンはH型に調整した強酸性陽イ
オン交換樹脂により吸着・除去される。ホウ素はホウ酸
の形で溶液中に存在しており、第１イオン交換塔からそ
のまま漏出する。In the present invention, such waste water containing carbonic acid together with boron is first passed through a first ion exchange column filled with a strongly acidic cation exchange resin adjusted to H type to adsorb and remove cations. . By this process, Na ions in the drainage and
Cations such as Ca ions are adsorbed and removed by a strongly acidic cation exchange resin adjusted to H type. Boron is present in the solution in the form of boric acid and leaks out of the first ion exchange column as it is.
【００１２】上記第１工程を経た溶液は、次いでOH型に
調整した陰イオン交換樹脂を充填した第２イオン交換塔
に通液する。陰イオン交換樹脂には弱塩基性陰イオン交
換樹脂とI型若しくはII型の強塩基性陰イオン交換樹脂
が含まれる。この工程で、処理液中の塩化物イオン、硫
酸イオンなどの強酸の陰イオン、いいかえれば弱酸を除
く陰イオンが除去される。ホウ素は、ホウ酸あるいは弱
酸の形で存在し、Cl、SO4等の陰イオンと共存する状態
では陰イオン交換樹脂に吸着されず、そのまま漏出す
る。炭酸も同様である。The solution that has undergone the first step is then passed through a second ion exchange column filled with an anion exchange resin adjusted to the OH type. The anion exchange resin includes a weakly basic anion exchange resin and a type I or type II strong basic anion exchange resin. In this step, anions of strong acids such as chloride ions and sulfate ions in the treatment liquid, in other words, anions except weak acids are removed. Boron exists in the form of boric acid or a weak acid, and when coexisting with anions such as Cl and SO 4 , it is not adsorbed on the anion exchange resin and leaks as it is. The same applies to carbonic acid.
【００１３】上記第２工程を経た溶液は、OH型に調整し
た強塩基性陰イオン交換樹脂を充填した第３イオン交換
塔に通液する。この段階で溶液はpHがほぼ5〜6程度とな
っており、このpHではホウ素の大部分は未解離のホウ酸
といわれており、一般に陰イオン交換樹脂によりホウ素
を吸着することは困難と思われるが、発明者の試験によ
れば強塩基性陰イオン交換樹脂に極めて効率的にホウ素
が吸着する。おそらくホウ素はB(OH)4 -の形の陰イオン
として存在し、上記陰イオン交換樹脂に吸着されるため
であろう。なお、OH型に調整した強塩基性陰イオン交換
樹脂に変えてOH型に調整した強塩基性陰イオン交換樹脂
と強酸性陽イオン交換樹脂の混合樹脂とすることもでき
る。それにより、例えば第１工程の処理の際、何らかの
陽イオンが漏出することがあっても、この段階で吸着除
去でき、最終のホウ素溶液中に陽イオンが混入すること
が避けられる。The solution which has undergone the second step is passed through a third ion exchange column filled with a strongly basic anion exchange resin adjusted to the OH type. At this stage, the solution has a pH of about 5 to 6, and most of the boron is said to be undissociated boric acid at this pH, and it is generally considered difficult to adsorb boron with an anion exchange resin. However, according to the test by the inventor, boron is adsorbed to the strongly basic anion exchange resin very efficiently. Presumably, boron exists as an anion in the form of B (OH) 4 − and is adsorbed on the anion exchange resin. Instead of the strongly basic anion exchange resin adjusted to the OH type, a mixed resin of the strongly basic anion exchange resin and the strongly acidic cation exchange resin adjusted to the OH type can be used. Thereby, for example, even if some cations leak out during the treatment of the first step, they can be adsorbed and removed at this stage, and cations are prevented from being mixed in the final boron solution.
【００１４】しかしながら、上記処理液中に炭酸が存在
すると、上記第３工程における樹脂単位体積当たりのホ
ウ素吸着量が著しく減少する。このことは、以下の実験
により明らかである。However, the presence of carbonic acid in the treatment liquid significantly reduces the amount of boron adsorbed per unit volume of resin in the third step. This is clear from the following experiment.
【００１５】内径750ｍｍ、高さ1500ｍｍのステンレス
製樹脂塔を３塔用意し、図１に示すように第１塔３にH
型に調整した強酸性陽イオン交換樹脂500lを、第２塔５
にOH型に調整した弱塩基性陰イオン交換樹脂500lを、第
３塔６にOH型に調整した強塩基性陰イオン交換樹脂600l
を充填し、表２に示す成分を有する工場排水A及びBを流
速5,000l/hで、第３塔よりホウ素がリークしてくるまで
通液した。Three stainless steel resin towers having an inner diameter of 750 mm and a height of 1,500 mm were prepared, and as shown in FIG.
500 liters of strongly acidic cation exchange resin adjusted to the mold
500l of weakly basic anion exchange resin adjusted to OH type and 600l of strong basic anion exchange resin adjusted to OH type in third tower 6
Was charged, and factory effluents A and B having the components shown in Table 2 were passed at a flow rate of 5,000 l / h until boron leaked from the third tower.
【００１６】[0016]
【表２】 [Table 2]
【００１７】通液終了後、第３塔を大まかに上部、中
部、下部と分けてその中に充填されている樹脂に吸着さ
れているホウ素量及び炭酸量を分析して調査した。結果
は、表３、表４に示したとおりである。表３は原水Aを
通水した場合であり、表４は原水Bを通水した場合であ
る。表３に示されているように原水のホウ素に対する炭
酸含有比率が小さい場合には、樹脂に対する炭酸の吸着
量が3〜14ｇ/1-Rであり、ホウ素は5〜10g/1-Rの高い吸
着量を示したが、表４に示すように、原水のホウ素に対
する炭酸含有比率が大きい場合には、樹脂に対する炭酸
の吸着量が30〜50g/l-Rと多くなり、これに伴いホウ素
の吸着量が0.1〜3g/1-Rと著しく下がった。なお、単
位、ｇ/1-R、は樹脂1l当たりに吸着される物質の量を質
量（g）で表したものである。After the completion of passing the liquid, the third column was roughly divided into an upper part, a middle part and a lower part, and the amount of boron and the amount of carbonic acid adsorbed on the resin filled therein were analyzed and investigated. The results are as shown in Tables 3 and 4. Table 3 shows the case of passing raw water A, and Table 4 shows the case of passing raw water B. As shown in Table 3, when the carbon dioxide content ratio of raw water to boron is small, the adsorption amount of carbonic acid to the resin is 3 to 14 g / 1-R, and boron is as high as 5 to 10 g / 1-R. Although the adsorption amount was shown, as shown in Table 4, when the carbonic acid content ratio to the boron in the raw water is high, the adsorption amount of carbonic acid to the resin increases to 30 to 50 g / lR, and the adsorption amount of boron is accordingly Was significantly reduced to 0.1 to 3g / 1-R. The unit, g / 1-R, represents the amount of the substance adsorbed per liter of resin in mass (g).
【００１８】[0018]
【表３】 [Table 3]
【００１９】[0019]
【表４】 [Table 4]
【００２０】このような実験を成分の異なる種々の工場
排水について実施することにより、炭酸の吸着がホウ素
の吸着を阻害する要因であること、したがって炭酸が除
去できれば、ホウ素の吸着量が著しく増加することが分
かった。本発明では、したがって、最終のホウ素吸着除
去工程である第３工程に入る前に、処理液から炭酸を除
去する脱炭酸工程を行う。具体的には、前記第１工程と
第２工程及び／又は第２工程と第３工程の間に脱炭酸工
程を行う。By carrying out such an experiment with various plant wastewaters having different components, the adsorption of carbonic acid is a factor inhibiting the adsorption of boron. Therefore, if the carbonic acid can be removed, the amount of adsorbed boron is remarkably increased. I found out. In the present invention, therefore, a decarboxylation step of removing carbonic acid from the treatment liquid is performed before the third step, which is the final boron adsorption removal step. Specifically, a decarboxylation step is performed between the first step and the second step and / or the second step and the third step.
【００２１】なお、第１イオン交換塔と第２イオン交換
塔の間に設置する脱炭酸塔は、強制通風式のばっ気設備
等とするのが好ましい。第１イオン交換塔を出た処理水
は強酸性陽イオン交換樹脂により陽イオンが除去され、
基本的には陰イオンしか残っていないため、処理水は酸
性となり、強制通風式のばっ気設備等を用いることによ
り、炭酸が3〜10mg/1まで容易に除去されるからであ
る。The decarbonation tower installed between the first ion exchange tower and the second ion exchange tower is preferably a forced ventilation type aeration equipment or the like. Cations are removed by the strongly acidic cation exchange resin from the treated water leaving the first ion exchange tower,
Basically, since only anions remain, the treated water becomes acidic, and carbon dioxide can be easily removed up to 3 to 10 mg / 1 by using forced ventilation type aeration equipment.
【００２２】これに対し、第２イオン交換塔と第３イオ
ン交換塔の間に設ける脱炭酸塔は、OH型に調整したI型
若しくはII型強塩基性陰イオン交換樹脂とするのがよ
い。この段階では処理液はほぼ中性となっており、ばっ
気設備では炭酸を除去しきることができないが、これら
のイオン交換樹脂により炭酸を容易に除去できる。On the other hand, the decarbonation tower provided between the second ion exchange tower and the third ion exchange tower is preferably a type I or type II strong basic anion exchange resin adjusted to the OH type. At this stage, the treatment liquid is almost neutral, and the carbonic acid cannot be completely removed by the aeration equipment, but the carbonic acid can be easily removed by these ion exchange resins.
【００２３】本発明の実施のためには、図２に一例を示
すようなプラントを用いればよい。この例では、原水を
原水槽内に、強酸性陽イオン交換樹脂塔は第１塔3に、
弱塩基性陰イオン交換樹脂は第２塔5に、強塩基性陰イ
オン交換樹脂は第３塔6に充填して、脱炭酸塔4は上記第
１塔と第２塔の間に設置する。なお、第３塔6のホウ素
選択吸着樹脂塔は２塔直列として順送りで使用してもか
まわない。また、第３塔6のホウ素選択吸着樹脂塔は、
強塩基性陰イオン交換樹脂に加えて強酸性陽イオン交換
樹脂を混じた混合樹脂とすることができる。In order to carry out the present invention, a plant, an example of which is shown in FIG. 2, may be used. In this example, the raw water is stored in the raw water tank, the strong acid cation exchange resin tower is the first tower 3,
The weakly basic anion exchange resin is packed in the second tower 5, the strong basic anion exchange resin is packed in the third tower 6, and the decarboxylation tower 4 is installed between the first tower and the second tower. In addition, the boron selective adsorption resin tower of the third tower 6 may be used as two towers in series and fed in sequence. Also, the boron selective adsorption resin tower of the third tower 6 is
A mixed resin in which a strongly acidic cation exchange resin is mixed with the strongly basic anion exchange resin can be used.
【００２４】上記装置により排水の脱ホウ素処理を行う
ときには、上記第１塔と第２塔の飽和は電気伝導率計10
で、第3塔におけるホウ素吸着の飽和は、ホウ素測定器1
1により管理できる。得られた処理液は処理液槽7に入
れ、さらにポンプ8により、バルブV1〜V2の開閉により
原水槽に戻したり、水洗水として再利用することもでき
る。When the waste water is deboronized by the above apparatus, the saturation of the first tower and the second tower is measured by an electric conductivity meter 10
So, the saturation of boron adsorption in the third tower is measured by the boron measuring instrument 1
Can be managed by 1. The obtained treatment liquid can be put in the treatment liquid tank 7 and returned to the raw water tank by opening / closing the valves V1 to V2 by the pump 8 or reused as washing water.
【００２５】[0025]
【発明の効果】上記装置により、ホウ素を回収すれば、
原水の炭酸持ち込み量の変動にかかわらず、安定的なホ
ウ素吸着量を得ることができる。If boron is recovered by the above apparatus,
It is possible to obtain a stable amount of adsorbed boron regardless of the variation in the amount of carbon dioxide carried in the raw water.
【図１】 本発明の基礎となる実験結果を得るための実
験プラントの構成を示す概念図である。FIG. 1 is a conceptual diagram showing a configuration of an experimental plant for obtaining an experimental result which is a basis of the present invention.
【図２】 本発明を実施するために脱炭酸塔を設置した
プラントの一例を示す概念図である。FIG. 2 is a conceptual diagram showing an example of a plant in which a decarbonation tower is installed to carry out the present invention.
1：原水槽 2、8：ポンプ 3：強酸性陽イオン交換樹脂塔 4：脱炭酸塔 5：弱塩基性陰イオン交換樹脂塔 6：強塩基性陰イオン交換樹脂塔 7：処理液槽 10：電気伝導率計 11：ホウ素測定器 V1、 V2：バルブ 1: Raw water tank 2, 8: Pump 3: Strongly acidic cation exchange resin tower 4: Decarbonation tower 5: Weakly basic anion exchange resin tower 6: Strongly basic anion exchange resin tower 7: Treatment liquid tank 10: Electric conductivity meter 11: Boron measuring instrument V1, V2: Valve
Claims (4)
イオン交換塔に通水して陽イオンを吸着・除去する第１
工程と、 OH型に調整した陰イオン交換樹脂を充填した第２イオン
交換塔に通液して弱酸を除く陰イオンを除去する第２工
程と、 OH型に調整した強塩基性陰イオン交換樹脂、又は強塩基
性陰イオン交換樹脂とH型に調整した強酸性陽イオン交
換樹脂の混合樹脂を充填した第3イオン交換塔に通液し
てホウ素を吸着除去する第３工程を行って排水からホウ
素を除去するに当たり、 前記第１工程と第２工程及び／又は第２工程と第３工程
の間に脱炭酸工程を行うことを特徴とするホウ素ととも
に炭酸を含む排水の処理方法。1. A first method in which wastewater containing carbonic acid together with boron is filled with a strongly acidic cation exchange resin adjusted to H type.
Passing water through an ion exchange tower to adsorb and remove cations No. 1
Step, second step of removing anions excluding weak acid by passing through a second ion exchange column filled with anion exchange resin adjusted to OH type, and strongly basic anion exchange resin adjusted to OH type , Or the third step of adsorbing and removing boron by passing through a third ion exchange column filled with a mixed resin of a strongly basic anion exchange resin and a strongly acidic cation exchange resin adjusted to H type In removing boron, a decarbonation step is performed between the first step and the second step and / or the second step and the third step.
る処理水中の炭酸含有量（H2CO3、HCO3又はCO3含有量）
が質量比で10mg/l以下となるように行うことを特徴とす
る請求項１記載のホウ素とともに炭酸を含む排水の処理
方法。2. Decarbonation is carried out by treating the carbon dioxide content (H 2 CO 3 , HCO 3 or CO 3 content) in the treated water to be subjected to the second step or the third step.
The method for treating wastewater containing carbonic acid together with boron according to claim 1, wherein the treatment is performed so that the mass ratio is 10 mg / l or less.
から順に、H型に調整した強酸性陽イオン交換樹脂を充
填した第１イオン交換塔、OH型に調整した陰イオン交換
樹脂を充填した第２イオン交換塔、OH型に調整した強塩
基性陰イオン交換樹脂又は強塩基性陰イオン交換樹脂と
H型に調整した強酸性陽イオン交換樹脂の混合樹脂を充
填した第3イオン交換塔を配設し、前記第１イオン交換
塔と第２イオン交換塔及び/又は第２イオン交換塔と第
３イオン交換塔の間に脱炭酸塔を設けてなることを特徴
とするホウ素とともに炭酸を含む排水の処理装置。3. A first ion exchange column filled with a strongly acidic cation exchange resin adjusted to H type and a first ion exchange resin filled to OH type in order from the inflow side of the wastewater containing carbonic acid together with boron. 2 ion exchange tower, OH type adjusted strong basic anion exchange resin or strong basic anion exchange resin
A third ion exchange column filled with a mixed resin of a strongly acidic cation exchange resin adjusted to H type is provided, and the first ion exchange column and the second ion exchange column and / or the second ion exchange column and the third ion exchange column. An apparatus for treating wastewater containing carbonic acid with boron, characterized in that a decarbonation tower is provided between ion exchange towers.
酸塔は、強制通風式ばっ気設備であり、第２工程と第３
工程との間に配設する脱炭酸塔は、OH型に調整したI型
若しくはII型強塩基性陰イオン交換樹脂を充填したもの
であることを特徴とする請求項３記載のホウ素とともに
炭酸を含む排水の処理装置。4. The decarbonation tower arranged between the first step and the second step is a forced ventilation type aeration equipment, and the second step and the third step.
The carbon dioxide with boron according to claim 3, wherein the decarbonation tower arranged between the step and the step is filled with a type I or type II strong basic anion exchange resin adjusted to an OH type. Wastewater treatment equipment including.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001243149A JP2003053341A (en) | 2001-08-10 | 2001-08-10 | Method and apparatus for treating wastewater containing carbonic acid together with boron |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2001243149A JP2003053341A (en) | 2001-08-10 | 2001-08-10 | Method and apparatus for treating wastewater containing carbonic acid together with boron |
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| Publication Number | Publication Date |
|---|---|
| JP2003053341A true JP2003053341A (en) | 2003-02-25 |
Family
ID=19073290
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2001243149A Pending JP2003053341A (en) | 2001-08-10 | 2001-08-10 | Method and apparatus for treating wastewater containing carbonic acid together with boron |
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| Country | Link |
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| JP (1) | JP2003053341A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102874899A (en) * | 2012-10-23 | 2013-01-16 | 南京信息工程大学 | Method for removing phthalic acid monoester pollutants in water body through ion exchange resin |
| KR20140065349A (en) * | 2012-11-21 | 2014-05-29 | 오비보 룩셈부르크 에스.에이.알.엘. | Treatment of water, particularly for obtaining ultrapure water |
| JP2018086657A (en) * | 2018-02-21 | 2018-06-07 | 野村マイクロ・サイエンス株式会社 | Pure water production apparatus, ultrapure water production system, and pure water production method |
-
2001
- 2001-08-10 JP JP2001243149A patent/JP2003053341A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102874899A (en) * | 2012-10-23 | 2013-01-16 | 南京信息工程大学 | Method for removing phthalic acid monoester pollutants in water body through ion exchange resin |
| KR20140065349A (en) * | 2012-11-21 | 2014-05-29 | 오비보 룩셈부르크 에스.에이.알.엘. | Treatment of water, particularly for obtaining ultrapure water |
| JP2014100706A (en) * | 2012-11-21 | 2014-06-05 | Ovivo Luxembourg Srl | Water treatment for particularly producing ultrapure water |
| KR102194404B1 (en) * | 2012-11-21 | 2020-12-24 | 오비보 룩셈부르크 에스.에이.알.엘. | Treatment of water, particularly for obtaining ultrapure water |
| JP2018086657A (en) * | 2018-02-21 | 2018-06-07 | 野村マイクロ・サイエンス株式会社 | Pure water production apparatus, ultrapure water production system, and pure water production method |
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