JPH0785795B2 - Water sampling method for denitration ion-treated water - Google Patents
Water sampling method for denitration ion-treated waterInfo
- Publication number
- JPH0785795B2 JPH0785795B2 JP61217207A JP21720786A JPH0785795B2 JP H0785795 B2 JPH0785795 B2 JP H0785795B2 JP 61217207 A JP61217207 A JP 61217207A JP 21720786 A JP21720786 A JP 21720786A JP H0785795 B2 JPH0785795 B2 JP H0785795B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- treated water
- ion
- hco
- concentration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は飲料水中の硝酸イオンを除去して、脱硝酸イン
オン処理水を得る際の採水方法、更に詳しくは塩化物形
イオン交換樹脂塔から採水される処理水中の炭酸水素イ
オンの減少度を抑え、処理水中のpHを飲料水基準内に収
める採水方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial field of application] The present invention relates to a water sampling method for removing nitrate ions in drinking water to obtain denitrified in-on-treated water, more specifically a chloride ion exchange resin tower. The present invention relates to a water sampling method that suppresses the degree of decrease of hydrogen carbonate ions in the treated water sampled from the water and keeps the pH of the treated water within the drinking water standard.
飲料水中の硝酸性窒素及び亜硫酸性窒素は水質基準に関
する省令（昭和53年８月31日厚生省令第56号）による10
mgN/以下であることとされている。Nitrate nitrogen and sulfite nitrogen in drinking water are based on the Ministerial Ordinance on Water Quality Standards (Ministry of Health and Welfare Ordinance No. 56 of August 31, 1978) 10
It is supposed to be less than mgN /.
原水中にこれ等が多く含まれている場合の処理方法の一
つに食塩などで再生した塩化物形の陰イオン交換樹脂層
（以後Cl形樹脂と称する）に通水し、原水中の硝酸イオ
ン等を陰イオン交換樹脂に吸着させ代りに塩化物イオン
を放出させ処理水の硝酸性窒素及び亜硫酸性窒素を減ず
る方式がある。One of the treatment methods when the raw water contains a large amount of these is to pass water through a chloride-type anion exchange resin layer (hereinafter referred to as Cl-type resin) regenerated with sodium chloride, etc. There is a method in which ions such as ions are adsorbed on an anion exchange resin and chloride ions are released instead to reduce nitrate nitrogen and sulfite nitrogen in the treated water.
これは水中の陰イオンのイオン交換樹脂との親和力（選
択係数）の差を利用したものである。水中の硝酸イオン
（▲SO2- 4▼），硝酸イオン（▲NO- 3▼）等は塩化物イ
オンより親和力が強く、そのため前述の反応が進み硝酸
性窒素および亜硝酸性窒素の基準値を満すことが可能と
なる。This utilizes the difference in affinity (selection coefficient) of anions in water with ion exchange resins. Water nitrate (▲ SO 2- 4 ▼), nitrate ion (▲ NO - 3 ▼) or the like has a strong affinity than chloride ions, therefore the reference value of the reaction proceeds nitrate nitrogen and nitrite nitrogen described above It is possible to fill up.
一方水中の炭酸水素イオン（▲HCO- 3▼）は▲SO2- 4▼，
▲NO- 3▼等と比べ親和力が弱いが、イオン交換樹脂が再
生直後の場合、即ちCl形の存在比率が高く、HCO3形の存
在比率が低い場合に限り塩化物イオンと交換し処理水中
より減少する。Whereas water bicarbonate (▲ HCO - 3 ▼) is ▲ SO 2- 4 ▼,
▲ NO - 3 ▼ but affinity is weak compared with like, if immediately after the regeneration the ion exchange resin, i.e., high abundance ratio of Cl form, exchange treated water and chloride ions only when a low existence ratio of HCO 3 form It decreases more.
しかし、炭酸水素イオンはイオン交換樹脂に対して親和
力が弱いため、HCO3形樹脂の存在比率が増加すると間も
なく処理水中の▲HCO- 3▼の濃度は原水のそれと殆ど同
じになる。However, since the hydrogen carbonate ion has a weak affinity for the ion exchange resin, the concentration of ▲ HCO - 3 ▼ in the treated water will be almost the same as that of the raw water as soon as the proportion of HCO 3 type resin increases.
一般的な水のpHは下記式の如く水中に存在する▲HCO- 3
▼と二酸化炭素（CO2）の比率に依存している。The general pH of water is ▲ HCO - 3
It depends on the ratio of ▼ and carbon dioxide (CO 2 ).
HCO3/CO2の比が 10 のとき pH＝7.35 1 〃 ＝6.35 0.1 〃 ＝5.35 となり、その比率が1/10になる毎にpHは１減少する。そ
こで前述のイオン交換樹脂の再生直後の反応により水中
の▲HCO- 3▼が極端に減少するとCO2の量は不変のため、
HCO3/CO2の比率が小さくなりpHが省令の基準値pH5.8以
上、8.6以下を満すことが不可能となる。 When the HCO 3 / CO 2 ratio is 10, pH = 7.35 1 〃 = 6.35 0.1 〃 = 5.35, and the pH decreases by 1 each time the ratio becomes 1/10. Therefore, if the ▲ HCO - 3 ▼ in the water decreases extremely due to the reaction immediately after the regeneration of the ion exchange resin, the amount of CO 2 does not change,
The ratio of HCO 3 / CO 2 becomes small, and it becomes impossible for the pH to satisfy the standard value of the Ministerial Ordinance of pH 5.8 or more and 8.6 or less.
そこで従来このような塩化物形イオン交換樹脂塔から採
水される処理水中の炭酸水素イオンの減少度を抑え、処
理水中のpHを飲料水基準内に収める方法としては下記の
方法が行われている。Therefore, the following method has been performed as a method of keeping the pH of the treated water within the drinking water standard by suppressing the degree of decrease of hydrogen carbonate ions in the treated water collected from the chloride type ion exchange resin tower. There is.
1.アルカリ剤を添加してpHを調節する方法 2.CaCO3（石灰石，貝ガラ等）と接触させる方法 3.再生後の洗浄時間を延長し、pHの上昇を待つ方法 4.再生の際にNaCl＋NaHCO3を再生剤を用いてHCO3形の樹
脂の存在比率を上げる方法 5.曝気してCO2の溶存量を減じる方法 6.原水と混合して▲HCO- 3▼分を補う方法 しかしこれらの方法はイオン量の増加,pHの大きな変動
幅，水の無駄，管理の複雑化，装置費の増大，硝酸性窒
素が余り減らない等の欠点がある。1. Method of adjusting pH by adding alkaline agent 2. Method of contacting with CaCO 3 (limestone, shellfish, etc.) 3. Method of extending washing time after regeneration and waiting for increase of pH 4. During regeneration A method of increasing the abundance of HCO 3 type resin by using NaCl + NaHCO 3 as a regenerant 5. A method of reducing the dissolved amount of CO 2 by aeration 6. A method of supplementing ▲ HCO - 3 ▼ by mixing with raw water These methods have drawbacks such as an increase in the amount of ions, a large fluctuation range of pH, waste of water, complicated management, an increase in equipment cost, and a decrease in nitrate nitrogen.
本発明はこのような欠点を解消するためになされたもの
で、その要旨とする所は塩化物形陰イオン交換樹脂を用
いて飲料水中の脱硝酸イオンを行う方法において、並列
運転される２塔以上のイオン交換塔を用い、かつ各々の
イオン交換塔からの採水開始直後の炭酸水素イオン濃度
の減少した処理水を、既に炭酸水素イオン濃度の回復し
た他のイオン交換塔からの処理水と混合することを特徴
とする脱硝酸イオン処理水の採水方法に存するものであ
る。The present invention has been made to solve such a drawback, and the gist of the present invention is a method of denitrifying ions in drinking water using a chloride-type anion exchange resin. Using the above ion exchange tower, and treated water with a reduced hydrogen carbonate ion concentration immediately after the start of water sampling from each ion exchange tower, and treated water from another ion exchange tower with a restored hydrogen carbonate ion concentration. The present invention resides in a method for collecting denitrated ion-treated water, which is characterized by mixing.
〔発明の効果〕 本発明はこの一時的に▲HCO- 3▼が減少した処理水とす
でに▲HCO- 3▼濃度が回復している別の塔の処理水を混
合して▲HCO- 3▼の減少量を調節しイオン交換樹脂の再
生に関係なく常に処理水のpHの値を満足させようとする
ものである。[Effect of the invention The present invention relates to the temporarily ▲ HCO - 3 ▼ is reduced treated water already ▲ HCO - 3 ▼ concentration by mixing treated water of another tower is recovering ▲ HCO - 3 ▼ It is intended to always satisfy the pH value of the treated water regardless of the regeneration of the ion-exchange resin by adjusting the decrease amount of.
即ち再生直後の塔の処理水の▲HCO- 3▼の濃度が零に近
くなった場合でも▲HCO- 3▼濃度が原水なみに回復して
いる他の塔の処理水と（1:1）に混合すれば▲HCO- 3▼濃
度は1/2になるためそのpHはlog2即ち約0.3だけ下がるこ
とになりpHの変化は少くなる。That is, even if the concentration of ▲ HCO - 3 ▼ in the treated water of the tower immediately after regeneration approaches to zero, the ▲ HCO - 3 ▼ concentration is restored to that of the raw water and the treated water of the other towers (1: 1). If mixed with, the concentration of ▲ HCO - 3 will be halved and its pH will drop by log2, that is, about 0.3, and the change of pH will be small.
▲HCO- 3▼の量が原水と同じ程度に回復した場合にもpH
は原水本来の値に戻るだけであり安定性が高い。かくし
て本発明によればpHの変動巾を減少させ、飲料水中の硝
酸イオン濃度およびpHについての水質基準を夫々常に満
足する方法を提供したものである。Even if the amount of ▲ HCO - 3 ▼ is restored to the same level as the raw water, the pH
Has high stability because it only returns to the original value of raw water. Thus, the present invention provides a method of reducing the fluctuation range of pH and always satisfying the water quality standards for the concentration of nitrate ion and pH in drinking water.
比較例 原水水質 ▲HCO- 3▼＋Cl-＋▲SO2- 4▼＋▲NO- 3▼＝180mgCaCO3/ ▲NO- 3▼:40mgCaCO3/（11.2mgN/） ▲HCO- 3▼:35mgCaCO3/ pH:6.6 CO2:20mg as CaCO3/ 上記の原水水質を有する原水を従来の一塔式の塩化物イ
オン形陰イオン交換樹脂層に通水して脱硝酸イオン処理
を行った。尚上記の塩化物イオン形陰イオン交換樹脂の
再生レベルは３−10％NaCl/−樹脂であった。Comparative Example raw water quality ▲ HCO - 3 ▼ + Cl - + ▲ SO 2- 4 ▼ + ▲ NO - 3 ▼ = 180mgCaCO 3 / ▲ NO - 3 ▼: 40mgCaCO 3 /(11.2mgN/) ▲ HCO - 3 ▼: 35mgCaCO 3 /pH:6.6 CO 2 : 20mg as CaCO 3 / Raw water having the above-mentioned raw water quality was passed through a conventional one-column chloride ion type anion exchange resin layer for denitration ion treatment. The regeneration level of the chloride ion type anion exchange resin was 3-10% NaCl / -resin.
その結果第１図に示すように得られた処理水の▲NO- 3▼
濃度は曲線（Ａ）に示すように900／−樹脂の採水
処理量全体に亘って5mg as CaCO3/で10mgN/以下の
水質基準を満していたが、処理水のpHについては曲線
（Ｂ）に示すように上記のイオン交換樹脂再生直後の処
理倍量150／−樹脂までの間はpHが5.8以下であり、
これは水質基準を満さなかった。As a result, the treated water obtained as shown in Fig. 1 ▲ NO - 3 ▼
As shown in the curve (A), the concentration met the water quality standard of 5 mg as CaCO 3 / and 10 mg N / or less over the entire 900 / -resin sampling amount. As shown in B), the pH is 5.8 or less until the processing amount of 150 / − resin immediately after the above-mentioned ion exchange resin is regenerated,
This did not meet water quality standards.
また処理水の▲HCO- 3▼濃度（mg as CaCO3/）の経時
的変化は曲線（Ｃ）の通りであり、これは上述のpHの経
時的変化を示す曲線と一致した。The time course of the ▲ HCO - 3 ▼ concentration (mg as CaCO 3 /) of the treated water is as shown by the curve (C), which is in agreement with the above-mentioned curve showing the time course of pH.
実施例 比較例と同一の原水水質を有する原水を二塔式の塩化物
イオン形陰イオン交換樹脂層に通水し、その際再生直後
のイオン交換塔からの処理水は採水処理倍量450／
−樹脂の採水中の他のイオン交換塔からの処理水と1:1
に混合した。尚再生条件は比較例の場合と同様に行っ
た。Example Raw water having the same raw water quality as in the comparative example is passed through the two tower type chloride ion type anion exchange resin layer, and the treated water from the ion exchange tower immediately after regeneration is a double treatment amount of 450 times. /
1: 1 with treated water from other ion exchange towers in resin draw
Mixed in. The regeneration conditions were the same as in the comparative example.
その結果、混合処理水中の▲NO- 3▼濃度は比較例の場合
と同じく基準値を満足しており、かつpHについては曲線
（Ｄ）に示すように処理倍量900／〜−樹脂に亘っ
て6.3を下らず5.8以上8.6以下の水質基準を常に満して
いた。As a result, the ▲ NO - 3 concentration in the mixed treated water satisfied the standard value as in the case of the comparative example, and the pH was over the treated amount 900 / ~ -resin as shown by the curve (D). The water quality standard of 5.8 or more and 8.6 or less was always satisfied, not lower than 6.3.
又その際の処理水中の▲HCO- 3▼濃度（mg as CaCO3/
）の経時的変化は曲線（Ｅ）の通りであった。At that time, the ▲ HCO - 3 ▼ concentration (mg as CaCO 3 /
The change with time in () was as shown by the curve (E).
第１図は本発明における実施例および比較例に係わるNO
3 -およびHCO3 -の濃度並びにpHの変化を示した図表であ
る。 曲線Ａ…比較例における処理水中の▲NO- 3▼濃度の変化
を示す。 曲線Ｂ…比較例における処理水中のpHの変化を示す。 曲線Ｃ…比較例における▲HCO- 3▼濃度の変化を示す。 曲線Ｄ…実施例における処理水中のpHの変化を示す。 曲線Ｅ…実施例における処理水中の▲HCO- 3▼濃度の変
化を示す。FIG. 1 shows NO according to the examples and comparative examples of the present invention.
3 - and HCO 3 - is a chart showing the change in concentration as well as pH of. Curve A: shows the change of ▲ NO - 3 ▼ concentration in the treated water in the comparative example. Curve B ... Changes in pH in treated water in Comparative Example. Curve C ... Shows the change in concentration of HCO - 3 in the comparative example. Curve D ... Changes in pH in treated water in the examples. Curve E: shows changes in ▲ HCO - 3 ▼ concentration in the treated water in the examples.
Claims (1)
中の脱硝酸イオンを行う方法において、並列運転される
２塔以上のイオン交換塔を用い、かつ各々のイオン交換
塔から採水開始直後の炭酸水素イオン濃度の減少した処
理水を既に炭酸水素イオン濃度の回復した他のイオン交
換塔からの処理水と混合することを特徴とする脱硝酸イ
オン処理水の採水方法。1. A method for denitrifying ions in drinking water using a chloride-type anion exchange resin, wherein two or more ion exchange columns operated in parallel are used, and water sampling is started from each ion exchange column. A method for collecting denitrated ion-treated water, characterized in that the treated water having a reduced hydrogen carbonate ion concentration immediately after is mixed with the treated water from another ion exchange column in which the hydrogen carbonate ion concentration has already been recovered.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61217207A JPH0785795B2 (en) | 1986-09-17 | 1986-09-17 | Water sampling method for denitration ion-treated water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61217207A JPH0785795B2 (en) | 1986-09-17 | 1986-09-17 | Water sampling method for denitration ion-treated water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6372392A JPS6372392A (en) | 1988-04-02 |
| JPH0785795B2 true JPH0785795B2 (en) | 1995-09-20 |
Family
ID=16700543
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61217207A Expired - Fee Related JPH0785795B2 (en) | 1986-09-17 | 1986-09-17 | Water sampling method for denitration ion-treated water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0785795B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20010083364A (en) * | 2000-02-11 | 2001-09-01 | 윤창현 | Nitrate removal with silver electrolysis in drinking water |
| JP4537486B2 (en) * | 2009-01-19 | 2010-09-01 | 国立大学法人秋田大学 | Method for producing rice bran leachate from which bad smell was removed, method for producing rice bran leachate from which bad smell was removed, and method for producing γ-aminobutyric acid |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5450476A (en) * | 1977-09-29 | 1979-04-20 | Shin Meiwa Ind Co Ltd | Method and apparatus for removing nitric acid nitrogen |
-
1986
- 1986-09-17 JP JP61217207A patent/JPH0785795B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6372392A (en) | 1988-04-02 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| LAPS | Cancellation because of no payment of annual fees |