JPH07115020B2 - Recycling treatment method of neutral salt waste liquid - Google Patents
Recycling treatment method of neutral salt waste liquidInfo
- Publication number
- JPH07115020B2 JPH07115020B2 JP15971988A JP15971988A JPH07115020B2 JP H07115020 B2 JPH07115020 B2 JP H07115020B2 JP 15971988 A JP15971988 A JP 15971988A JP 15971988 A JP15971988 A JP 15971988A JP H07115020 B2 JPH07115020 B2 JP H07115020B2
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- Prior art keywords
- salt
- waste liquid
- tank
- water
- solution
- Prior art date
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- Water Treatment By Electricity Or Magnetism (AREA)
Description
【発明の詳細な説明】 （産業上の利用分野） 本発明は、中性塩廃液の再生回収処理方法に関し、詳細
には、バイポーラ膜を有するイオン交換膜電気透析装置
を使用し、塩濃度が比較的高い中性塩廃液を再生回収処
理する方法に関する。Description: TECHNICAL FIELD The present invention relates to a method for regenerating and recovering a neutral salt waste liquid, and more specifically, it uses an ion exchange membrane electrodialysis device having a bipolar membrane and has a high salt concentration. The present invention relates to a method of regenerating and recovering a relatively high neutral salt waste liquid.
（従来の技術） 従来、中性塩廃液は、公共水域へ放流され、廃液処理さ
れていたが、この処理には環境保全面あるいは公害上で
の問題点がある。例えば、硝酸塩廃液の場合は、硝酸性
の窒素による公共水域の富栄養化を招くという問題点が
ある。(Prior Art) Conventionally, a neutral salt waste liquid has been discharged to a public water body and treated as a waste liquid, but this treatment has a problem in terms of environmental protection or pollution. For example, in the case of a nitrate waste liquid, there is a problem that nitrate water causes eutrophication of public water bodies.
そこで、このような問題点を解決すべく、中性塩廃液処
理方法が各方面で検討されてきた。その結果、最近で
は、第２図（原理の概要図）に示すように、バイポーラ
膜（陰陽複合イオン交換膜）を用いたイオン交換膜電気
透析装置を使用して電気透析し、酸とアルカリとに分離
して回収する方法（以降、BP電気透析法という）が開発
され、実用されている。それは、例えば特表昭62−5026
95号公報に提示されている。尚、第２図において、BPは
バイポーラ膜、Ａは陰イオン交換膜、Ｂは陽イオン交換
膜を示すものである。又、第２図は、NaNO3廃液を電気
透析した場合のものである。Therefore, neutral salt waste liquid treatment methods have been studied in various fields in order to solve such problems. As a result, recently, as shown in FIG. 2 (a schematic diagram of the principle), electrodialysis was performed using an ion-exchange membrane electrodialysis device using a bipolar membrane (anion-yang composite ion-exchange membrane) to remove acid and alkali. A method for separating and recovering the same (hereinafter referred to as BP electrodialysis method) has been developed and put into practical use. It is, for example, the special table Sho 62-5026.
It is presented in Japanese Patent Publication No. 95. In FIG. 2, BP is a bipolar membrane, A is an anion exchange membrane, and B is a cation exchange membrane. Further, FIG. 2 shows the case where the NaNO 3 waste solution is electrodialyzed.
従来のBP電気透析法方法の詳細を、以下説明する。従来
のBP電気透析法のフローチャートの概略を第３図に示
す。この図に示すように、中性塩廃液タンク（１）から
塩循環ライン（９）の途中に設けられた塩循環用タンク
（３）へ、中性塩廃液が断続的に導入され、又、後述の
塩循環ライン（９）で得られる脱塩水も導入され、タン
ク（３）内の溶液は所定の塩濃度（略一定値）になるよ
うに調整される。それは、塩濃度が電気透析の効率およ
びイオン交換膜の損傷に大きな影響を及ぼすからであ
る。Details of the conventional BP electrodialysis method will be described below. The outline of the flow chart of the conventional BP electrodialysis method is shown in FIG. As shown in this figure, the neutral salt waste liquid is intermittently introduced from the neutral salt waste liquid tank (1) to the salt circulation tank (3) provided in the middle of the salt circulation line (9), and Demineralized water obtained in a salt circulation line (9) described later is also introduced, and the solution in the tank (3) is adjusted to have a predetermined salt concentration (approximately a constant value). This is because the salt concentration greatly affects the efficiency of electrodialysis and damage to the ion exchange membrane.
上記塩濃度調整されたタンク（３）内溶液は、塩循環ラ
イン（９）により電気透析装置の本体（７）に導入され
て循環される。該循環溶液は電気透析され、酸ライン
（10）には酸成分、アルカリライン（８）にはアルカリ
成分が得られる。各々が分離して得られる。The solution in the tank (3) whose salt concentration has been adjusted is introduced into the main body (7) of the electrodialysis device by the salt circulation line (9) and circulated. The circulating solution is electrodialyzed to obtain an acid component in the acid line (10) and an alkali component in the alkali line (8). Each is obtained separately.
一方、塩循環ライン（９）には脱塩水が得られ、該脱塩
水は塩循環用タンク（３）へ導入され、前記塩濃度調整
に使用される。尚、余分の脱塩水は、オーバフローさせ
て脱塩水タンク（12）へ導入され、該脱塩水はそのまま
公共水域へ放流される。On the other hand, demineralized water is obtained in the salt circulation line (9), and the demineralized water is introduced into the salt circulation tank (3) and used for adjusting the salt concentration. The excess demineralized water overflows and is introduced into the demineralized water tank (12), and the demineralized water is discharged as it is to the public water area.
上記の如く、BP電気透析法は、再使用可能な酸とアルカ
リと別々に得られるという利点がある。かかる点から、
BP電気透析法が実用されるようになってきた。As described above, the BP electrodialysis method has an advantage that a reusable acid and alkali are separately obtained. From this point,
The BP electrodialysis method has come into practical use.
（発明が解決しようとする課題） ところで、上記のBP電気透析法は、塩循環用タンク
（３）への中性塩廃液の断続的導入、及び脱塩水の循環
・導入により、タンク（３）内溶液の塩濃度調整が行わ
れるので、中性塩廃液の塩濃度が比較的高い場合は、タ
ンク（３）内溶液の液量が次第に減少して水位が低下
し、最終的には塩循環ライン（９）への導入・循環用溶
液が無くなり、そのため廃液処理しようとする中性塩廃
液が残っているのに、運転ができなくなるという問題点
がある。(Problems to be solved by the invention) By the way, in the above BP electrodialysis method, by intermittently introducing the neutral salt waste liquid into the salt circulation tank (3) and circulating and introducing demineralized water, the tank (3) Since the salt concentration of the inner solution is adjusted, when the salt concentration of the neutral salt waste liquid is relatively high, the liquid amount of the solution in the tank (3) gradually decreases and the water level lowers. There is a problem that the solution cannot be operated even though the solution for introduction / circulation to the line (9) is exhausted and therefore the neutral salt waste solution to be treated as waste solution remains.
例えば、中性塩廃液が40％NaNo3、塩循環用タンク
（３）内溶液の所定塩濃度を５％とし、今電気透析装置
の本体（７）に10kg（NaNo3:500g,H2O:9.5kg）が導入さ
れ、塩循環ライン（９）を循環したとする。この導入時
点より15HAの電気量を通電した後には、アルカリライン
（８）にNa+:69g,H2O:363gが移行、酸ライン（10）にNo
3イオン:186g、H2O:363gが移行した結果、NaNo3:255g、
H2O:726gが電気透析で消費された事になる。又、これは
NaNo3として濃度換算すると26％であるので、５％NaNo3
から26％NaNo3が消費された事に相当する。For example, a neutral salt waste liquid 40% NaNO 3, a predetermined salt concentration of the salt circulation tank (3) the solution was 5%, now in the body of the electrodialysis device (7) 10kg (NaNo 3: 500g, H 2 O : 9.5 kg) was introduced and circulated through the salt circulation line (9). After supplying electricity of 15HA from the time of this introduction, Na + : 69g, H 2 O: 363g was transferred to the alkali line (8) and the acid line (10) was
As a result of migration of 3 ions: 186 g, H 2 O: 363 g, NaNo 3 : 255 g,
This means that 726 g of H 2 O was consumed by electrodialysis. This is also
The concentration converted to NaNo 3 is 26%, so 5% NaNo 3
This corresponds to the consumption of 26% NaNo 3 from.
この結果、一方では9.019kgの脱塩水が塩循環用タンク
（３）に残ることになる。このとき、中性塩廃液の導入
がなければ、タンク（３）内溶液は脱塩水で希釈され、
2.7％となる。そこで、40％の中性塩廃液を導入添加
し、５％になるように調整すると、塩循環用タンク
（３）内溶液量は9.607kg（NaNo3:480g、H2O:9.127kg）
になり、前記電気透析前での10kgより減少する。As a result, on the one hand, 9.019 kg of demineralized water will remain in the salt circulation tank (3). At this time, if the neutral salt waste liquid is not introduced, the solution in the tank (3) is diluted with demineralized water,
2.7%. Therefore, 40% neutral salt waste liquid was introduced and added to adjust to 5%, and the solution amount in the salt circulation tank (3) was 9.607 kg (NaNo 3 : 480 g, H 2 O: 9.127 kg).
It becomes less than 10 kg before the electrodialysis.
このことから判るように、更に溶液を電気透析装置の本
体（７）に導入し、電気透析を続けると、その進行に応
じて次第に塩循環用タンク（３）内溶液量が次第に減少
して水位が低下し、最終的にはタンク（３）内溶液が無
くなり、その結果連続運転ができなくなる。As can be seen from this, when the solution is further introduced into the main body (7) of the electrodialysis device and electrodialysis is continued, the amount of the solution in the salt circulation tank (3) gradually decreases according to the progress of the electrodialysis, and the water level increases. Is lowered, and finally the solution in the tank (3) is exhausted, so that continuous operation cannot be performed.
このように水位低下を生じる理由は、上記例からも判る
ように、塩循環用タンク（３）に導入される中性塩廃液
の塩濃度が、前記電気透析で消費されたNaNo3−H2Ｏの
濃度換算値（前記例では26％）の如く、電気透析で消費
された塩の濃度換算値（以降、消費塩濃度という）より
高いことに基づくものであり、両者の塩濃度の差が大き
い程この水位低下の速度は大きい。尚、両者の塩濃度が
等しい場合は、水位低下を生じない。As can be seen from the above example, the reason why the water level is lowered is that the salt concentration of the neutral salt waste liquid introduced into the salt circulation tank (3) is NaNo 3 -H 2 consumed in the electrodialysis. It is based on the fact that it is higher than the converted value of the concentration of salt consumed by electrodialysis (hereinafter referred to as the consumed salt concentration), such as the converted value of O concentration (26% in the above example). The larger the value, the higher the rate of this water level drop. When the salt concentrations of both are the same, the water level does not decrease.
従って、水位低下を防止するには、前記両者の塩濃度が
等しくなるようにすればよい。その方法として、最も簡
単には、中性塩廃液タンク（１）内の廃液に水を添加し
て直接希釈し、希釈後の塩濃度を消費塩濃度に等しくす
る方法（以降、廃液直接希釈法という）が考えられる。Therefore, in order to prevent lowering of the water level, the salt concentrations of the both may be made equal. The simplest method is to add water to the waste liquid in the neutral salt waste liquid tank (1) to directly dilute it, and make the salt concentration after dilution equal to the consumed salt concentration (hereinafter, waste liquid direct dilution method). That is) possible.
ところが、発生する中性塩廃液の塩濃度は必ずしも一定
しておらず、又、イオン交換膜の能力の低下等に対応し
消費塩濃度は変化する場合が多いので、廃液直接希釈法
による場合、前記両者の塩濃度を常時把握する必要があ
る。この消費塩濃度の常時把握は極めて困難である。
又、通常廃液タンク（１）は容量が極めて大きいので、
水添加された時、暫くは濃度が不均一の状態にあるの
で、タンク（１）内の塩濃度の正確な確認は困難であ
る。従って、廃液直接希釈法は容易に行い得るものでな
く、又、水位低下を確実に防止し得ないという問題点を
有する。However, the salt concentration of the generated neutral salt waste liquid is not always constant, and since the consumed salt concentration often changes in response to a decrease in the capacity of the ion exchange membrane, when the waste liquid direct dilution method is used, It is necessary to constantly grasp the salt concentrations of the both. It is extremely difficult to constantly grasp this consumed salt concentration.
Also, since the waste liquid tank (1) usually has an extremely large capacity,
When water is added, the concentration is inhomogeneous for a while, so it is difficult to accurately check the salt concentration in the tank (1). Therefore, the waste liquid direct dilution method cannot be easily performed, and there is a problem in that the water level cannot be reliably prevented from lowering.
尚、廃液直接希釈法の適用の仕方として、水を余分に添
加する方法が考えられる。例えば、消費塩濃度が最小と
なり、且つ発生する中性塩廃液の塩濃度が最大となる最
悪の時点を想定し、その時点に対応する添加水の量を設
定し、この設定量の水を常時添加する。このようにすれ
ば、水位低下は防止されるが、総合的に観ると、水が余
分に添加されるので、塩循環用タンクに導入される中性
塩廃液の塩濃度が消費塩濃度より低くなり、そのためタ
ンク（３）内の水位が上昇し、脱塩水がオーバフローす
る。従って、脱塩素タンクが必要であり、又、脱塩水は
公共水域へ放流されることになる。脱塩水は塩濃度が小
さくなっているが、それでも塩を含んでいるので公共水
域への放流は望ましいことではない。As a method of applying the waste liquid direct dilution method, a method of adding extra water can be considered. For example, assuming the worst time when the consumed salt concentration is the minimum and the generated salt concentration of the neutral salt waste liquid is the maximum, the amount of added water corresponding to that time is set, and this set amount of water is constantly maintained. Added. By doing this, the water level is prevented from lowering, but when viewed comprehensively, since extra water is added, the salt concentration of the neutral salt waste liquid introduced into the salt circulation tank is lower than the consumed salt concentration. Therefore, the water level in the tank (3) rises and the demineralized water overflows. Therefore, a dechlorination tank is required, and demineralized water will be discharged to public water bodies. Although desalinated water has a low salt concentration, it still contains salt and is not desirable for release to public water bodies.
本発明はこの様な事情に着目してなされたものであっ
て、その目的は従来のものがもつ以上のような問題点を
解消し、バイポーラ膜を有するイオン交換膜電気透析装
置を使用する中性塩廃液の再生回収処理方法であって、
中性塩廃液の塩濃度が消費塩濃度より高い場合において
も、水位低下およびオーバフロー脱塩水の発生を生じる
事なく、廃液処理しようとする中性塩廃液が無くなるま
で、イオン交換膜電気透析装置の塩循環ラインへの導入
・循環用溶液を常に有し、連続運転ができる中性塩廃液
の再生回収処理方法を提供しようとするものである。The present invention has been made by paying attention to such a situation, and an object thereof is to solve the above-mentioned problems of the conventional one and to use an ion exchange membrane electrodialysis device having a bipolar membrane. A method for reclaiming and recovering a strong salt waste liquid,
Even if the salt concentration of the neutral salt waste liquid is higher than the consumed salt concentration, the ion level of the ion-exchange membrane electrodialysis device is reduced until the neutral salt waste liquid to be treated is eliminated without causing the water level to drop and overflow demineralized water to be generated. It is an object of the present invention to provide a method for regenerating and recovering a neutral salt waste liquid which always has a solution for introduction / circulation to a salt circulation line and can be continuously operated.
（課題を解決するための手段） 上記の目的を達成いするために、本発明は次のような構
成の中性塩廃液の再生回収処理方法としている。即ち、
本発明は、バイポーラ膜、陰イオン交換膜及び陽イオン
交換膜を有し、且つ酸ライン、アルカリライン及び塩循
環用タンクをその途中に持つ塩循環ラインを有するイオ
ン交換膜電気透析装置の該タンク内に中性塩廃液を断続
的に導入し、該タンク内溶液の塩濃度を略一定値に調整
し、該タンク内溶液を塩循環ラインにより電気透析装置
に導入し、塩循環ラインを循環させ、電気透析を行って
酸とアルカリと脱塩水とを分離して得る中性塩廃液の再
生回収処理方法であって、該タンク内へ断続的に水を添
加して前記タンク内溶液の液量調整を行い、且つ導入中
性塩廃液により該タンク内溶液の塩濃度の調整を行うこ
とを特徴とする中性塩廃液の再生回収処理方法。(Means for Solving the Problems) In order to achieve the above object, the present invention provides a method for regenerating and recovering a neutral salt waste liquid having the following constitution. That is,
The present invention relates to an ion exchange membrane electrodialyzer having a bipolar membrane, an anion exchange membrane and a cation exchange membrane, and an acid line, an alkali line and a salt circulation line having a salt circulation tank in the middle thereof. Neutral salt waste liquid is intermittently introduced into the tank, the salt concentration of the solution in the tank is adjusted to a substantially constant value, the solution in the tank is introduced into the electrodialysis device by a salt circulation line, and the salt circulation line is circulated. A method for regenerating and recovering a neutral salt waste liquid obtained by separating an acid, an alkali, and demineralized water by performing electrodialysis, in which water is intermittently added to the tank to measure the amount of the solution in the tank. A method for regenerating and recovering a neutral salt waste liquid, which comprises adjusting and adjusting the salt concentration of the solution in the tank by introducing the neutral salt waste liquid.
（作用） 上記の如く、本発明に係る中性塩廃液の再生回収処理方
法は、塩循環用タンク内に中性塩廃液を断続的に導入
し、又、塩循環用タンク内に断続的に水を添加するよう
にしているので、中性塩廃液は添加水で希釈されながら
導入されることになる。この希釈の程度は自由に変えら
れる。故に、上記希釈されながら導入される中性塩廃液
の塩濃度は、概ね消費塩濃度の水準にし得る。従って、
該両者の塩濃度を常時確実に把握できれば、該両者の塩
濃度を常時確実に等しくし得、そのため水位低下を確実
に防止し得ることになる。尚、上記の希釈されながら導
入される中性塩廃液の塩濃度とは、導入される中性塩廃
液と添加される水とが混合されたとした場合に得られる
混合体の塩濃度をいう。(Operation) As described above, the method for regenerating and recovering the neutral salt waste liquid according to the present invention, the neutral salt waste liquid is intermittently introduced into the salt circulation tank, and intermittently into the salt circulation tank. Since the water is added, the neutral salt waste liquid is introduced while being diluted with the added water. The degree of this dilution can be freely changed. Therefore, the salt concentration of the neutral salt waste liquid introduced while being diluted can be almost at the level of the consumed salt concentration. Therefore,
If the salt concentrations of the both can be reliably grasped at all times, the salt concentrations of the both can always be made equal to each other, so that the water level lowering can be surely prevented. The salt concentration of the neutral salt waste liquid introduced while being diluted means the salt concentration of the mixture obtained when the introduced neutral salt waste liquid and the added water are mixed.
ここで、発生する中性塩廃液の塩濃度および消費塩濃度
が一定の場合は、比較的容易に前者両者の塩濃度を把握
し得、両者の塩濃度を常時確実に等しくし得る。従っ
て、容易に水位低下の防止が図れることになる。Here, when the salt concentration and the consumed salt concentration of the generated neutral salt waste liquid are constant, the former salt concentration can be grasped relatively easily, and the both salt concentrations can always be made equal. Therefore, it is possible to easily prevent the water level from decreasing.
しかし、発生する中性塩廃液の塩濃度および消費塩濃度
は一定でない場合が多い。この場合は、前記両者の塩濃
度を常時確実に把握する事が困難であるので、両者の塩
濃度を常時確実に等しくて水位低下の防止を確実に達成
する事は容易でない。However, the salt concentration and consumed salt concentration of the generated neutral salt waste liquid are often not constant. In this case, it is difficult to always grasp the salt concentrations of the both, so it is not easy to surely make the salt concentrations of the both equal to each other and reliably prevent the water level from being lowered.
そこで、本発明に係る方法は、塩循環用タンク内へ中性
塩廃液を断続的に導入し、また、断続的に水を添加する
だけでなく、更に塩循環用タンク内溶液の塩濃度調整を
行い、且つ該タンク内溶液の液量の調整を行うようにし
ている。Therefore, the method according to the present invention intermittently introduces a neutral salt waste liquid into the salt circulation tank, and not only intermittently adds water, but also adjusts the salt concentration of the solution in the salt circulation tank. And the amount of the solution in the tank is adjusted.
ここで、上記塩循環用タンクは、容量が小さいものでよ
く、容量が小さいと、水添加後の濃度が均一になり易
く、タンク内の正確な塩濃度を確認し得る。また、水位
は、比較的容易に把握し得る。故に、塩循環用タンク内
の水位および塩濃度を確実に確認しながら、水および中
性塩廃液を導入し得る事になる。Here, the tank for salt circulation may have a small capacity, and when the capacity is small, the concentration after water addition is likely to be uniform, and the accurate salt concentration in the tank can be confirmed. Further, the water level can be grasped relatively easily. Therefore, it is possible to introduce the water and the neutral salt waste liquid while surely confirming the water level and the salt concentration in the salt circulation tank.
このとき、塩循環用タンクに導入される中性塩廃液の塩
濃度が消費塩濃度より大であれば、水位低下を生じ、こ
の逆に小であれば、水位上昇を生じ、又、両者の濃度が
等しければ、水位が一定となる。これは、換言すると、
塩循環用タンクの水位および塩濃度が一定であれば、前
記両者の塩濃度が等しくなっている事を示している。従
って、塩循環用タンク内の水位および塩濃度が一定とな
るように、水で希釈さながら中性塩廃液を導入すれば、
前記両者の塩濃度を確実に等しくし得る。At this time, if the salt concentration of the neutral salt waste liquid introduced into the salt circulation tank is higher than the consumed salt concentration, the water level is lowered, and conversely, if it is low, the water level is raised, and If the concentrations are equal, the water level will be constant. This, in other words,
If the water level and the salt concentration in the salt circulation tank are constant, it means that the salt concentrations of the both are equal. Therefore, if the neutral salt waste liquid is introduced while being diluted with water so that the water level and the salt concentration in the salt circulation tank become constant,
It is possible to ensure that the salt concentrations of the both are equal.
本発明に係る方法は、前記の如く、塩循環用タンク内の
水位および塩濃度を確実に確認しながら、水および中性
塩廃液を導入し得るので、塩循環用タンク内の水位およ
び塩濃度が一定となるように水で希釈しながら中性塩廃
液を導入し得る。故に、前記両者の塩濃度を確実に等し
くし得る。As described above, the method according to the present invention can introduce water and a neutral salt waste solution while surely confirming the water level and the salt concentration in the salt circulation tank. The neutral salt waste liquor can be introduced while diluting with water so that the concentration becomes constant. Therefore, it is possible to ensure that the salt concentrations of the both are equal.
このように、前記両者の塩濃度を把握する事なく、容易
に両者の塩濃度を常時確実に等しくし得るので、発生す
る中性塩廃液の塩濃度および消費塩濃度が一定でない場
合においても、容易に水位低下の防止が図れるようにな
る。As described above, since it is possible to easily and surely make the salt concentrations of both of them always equal without grasping the salt concentrations of the both, even when the salt concentration and the consumed salt concentration of the generated neutral salt waste liquid are not constant, The water level can be easily prevented from lowering.
又、確実に水位低下を防止し得るので、水を余分に添加
する必要なく、そのため脱塩水のオーバフローを生じな
いようにし得る。Further, since it is possible to surely prevent the water level from being lowered, it is not necessary to add extra water, so that the overflow of the demineralized water can be prevented.
（実施例） 30lの40％NaNO3廃液について、本発明に係る方法により
25％HNO3と８％NaOHとを分離して得る再生回収処理を行
った。第１図に、第１実施例に係る40％NaNO3廃液の再
生回収処理方法のフローシートの概略図を示す。この図
に示すように、処理系は、この系から廃液および処理液
を全く出さないクローズドシステムとした。第１図を参
照しながら以下説明する。(Example) About 30 l of 40% NaNO 3 waste liquid, by the method according to the present invention
Regeneration and recovery treatment was performed by separating 25% HNO 3 and 8% NaOH. FIG. 1 shows a schematic diagram of a flow sheet of the method for regenerating and recovering 40% NaNO 3 waste liquid according to the first embodiment. As shown in this figure, the treatment system was a closed system in which no waste liquid or treatment liquid was emitted from this system. This will be described below with reference to FIG.
第１図において、（７）はイオン交換膜電気透析装置の
本体であって、バイポーラ膜，陰イオン交換膜，陽イオ
ン交換膜を一組とするセルを８セル有し、有効膜面積10
dm2のものである。In FIG. 1, (7) is the main body of the ion-exchange membrane electrodialysis device, which has 8 cells each including a bipolar membrane, an anion-exchange membrane and a cation-exchange membrane, and an effective membrane area of 10
It is from dm 2 .
塩循環用タンク（３）へ、中性塩廃液タンク（１）から
前記40％NaNO3廃液を導入すると共に、廃液希釈用水タ
ンク（２）から水を導入して、塩循環用タンク（３）内
溶液の量を10kg、濃度を所定塩濃度の５％に調整した。The 40% NaNO 3 waste solution is introduced from the neutral salt waste solution tank (1) into the salt circulation tank (3), and the water is introduced from the waste solution dilution water tank (2), and the salt circulation tank (3) The amount of the internal solution was adjusted to 10 kg and the concentration was adjusted to 5% of the predetermined salt concentration.
この調整液を、塩循環ライン（９）により電気透析装置
（７）に導入し、循環した。一方、酸ライン（10）に配
した酸循環タンク（11）内に水を入れ、該水を酸ライン
（10）に循環した。また、アルカリライン（８）に配し
たアルカリ循環タンク（５）へ、タンク（５）への注水
用水タンク（４）から水を入れ、該水をアルカリライイ
（８）に循環した。これらの準備の後、電気透析を開始
した。尚、この電気透析条件、即ち、電気透析装置
（７）の運転転条件は、溶液の温度30℃、電流密度10A/
dm2、膜面循環流速5cm/secとした。図中（６）は、アル
カリオーバフロータンクである。This adjusted solution was introduced into the electrodialysis device (7) through the salt circulation line (9) and circulated. On the other hand, water was put in the acid circulation tank (11) arranged in the acid line (10), and the water was circulated in the acid line (10). Further, water was poured from the water tank (4) for pouring water into the tank (5) into the alkaline circulation tank (5) arranged in the alkaline line (8), and the water was circulated through the alkaline reservoir (8). After these preparations, electrodialysis was started. In addition, this electrodialysis condition, that is, the operation conversion condition of the electrodialysis device (7), is such that the solution temperature is 30 ° C. and the current density is 10 A /
dm 2 and the flow velocity on the membrane surface were 5 cm / sec. (6) in the figure is an alkaline overflow tank.
電気透析の進行に伴い、酸ライン（10）は再生されたHN
O3によりHNO3溶液になり、アルカリライン（８）は再生
されたNaOHによりNaOH溶液になり、それぞれの濃度が大
きくなっていった。これらの溶液は継続して循環した。
一方、塩循環ライン（９）の溶液は脱塩され、脱塩水に
なる。この脱塩水も継続して循環した。また、これらの
変化に伴い、塩循環用タンク（３）内溶液の塩濃度およ
び水位が徐々に低下してきた。The acid line (10) was regenerated with the progress of electrodialysis.
O 3 became a HNO 3 solution, and the alkali line (8) became a NaOH solution by the regenerated NaOH, and the respective concentrations increased. These solutions were continuously circulated.
On the other hand, the solution in the salt circulation line (9) is desalted and becomes desalinated water. This demineralized water was also continuously circulated. Further, along with these changes, the salt concentration and the water level of the solution in the salt circulation tank (3) have gradually decreased.
各溶液循環および電気透析を継続した状態の下、塩循環
用タンク（３）内溶液について濃度計による塩濃度の測
定および水位計による水位の測定を行いながら、塩循環
用タンク（３）へ、中性塩廃液タンク（１）から40％Na
NO3廃液を導入すると共に、廃液希釈用水タンク（２）
から水を導入して、塩循環用タンク（３）内溶液の水位
を所定水位に保った。また、溶液の塩濃度は常に５％と
なるようにした。尚、水位計（図中、LICで示される）
は廃液希釈用水タンク（２）の弁と連動し、水位が低下
すると自動的に弁が開いて水が導入され、所定水位にな
ると弁が閉じるようにした。濃度計（図中、CICで示さ
れる）は中性塩廃液タンク（１）の弁と連動し、濃度が
低下すると自動的に弁が開いて廃液が導入され、所定濃
度になると弁が閉じるようにした。While continuing the solution circulation and electrodialysis, to the salt circulation tank (3) while measuring the salt concentration of the solution in the salt circulation tank (3) with a densitometer and the water level with a water gauge. 40% Na from the neutral salt waste liquid tank (1)
Water tank for diluting the waste liquid (2) while introducing NO 3 waste liquid
The water in the salt circulation tank (3) was maintained at a predetermined water level by introducing water from the tank. Also, the salt concentration of the solution was always set to 5%. A water level gauge (indicated by LIC in the figure)
Is linked with the valve of the waste water diluting water tank (2), and when the water level drops, the valve automatically opens and water is introduced, and when the water level reaches a predetermined level, the valve closes. The densitometer (indicated by CIC in the figure) works in conjunction with the valve of the neutral salt waste liquid tank (1), so that when the concentration decreases, the valve automatically opens and the waste liquid is introduced, and when the concentration reaches the specified value, the valve closes. I chose
以降、このような各溶液の循環、電気透析、塩循環用タ
ンク（３）内溶液の塩濃度および水位測定を継続して行
い、また、塩循環用タンク（３）への40％NaNO3廃液お
よび水の導入・添加による塩循環用タンク（３）内溶液
の水位および塩濃度調整を断続的に繰り返して行った。Thereafter, such circulation of each solution, electrodialysis, and measurement of salt concentration and water level of the solution in the salt circulation tank (3) are continuously carried out, and 40% NaNO 3 waste solution to the salt circulation tank (3) is continuously measured. The adjustment of the water level and the salt concentration of the solution in the salt circulation tank (3) by introducing and adding water were intermittently repeated.
その結果、塩循環用タンク（３）内溶液の極度な水位低
下を招くことなく、所定の塩濃度が確保された。そのた
め、途中運転を停止することなく、準備した30lの40％N
aNO3廃液の全てを連続して廃液処理することができた。As a result, a predetermined salt concentration was ensured without causing an extreme drop in the water level of the solution in the salt circulation tank (3). Therefore, without stopping the operation on the way, 40% N of 30l prepared
It was possible to treat all of the aNO 3 waste liquid continuously.
また、670AHの電気量で70.5lの８％NaOH溶液および35.5
lの25％NNO3溶液を再生して回収することができた。
尚、消費した廃液希釈用水は、16.2lであった。Also, with an electric quantity of 670 AH, 70.5 l of 8% NaOH solution and 35.5 l
l of 25% NNO 3 solution could be regenerated and recovered.
The water used for diluting the waste liquid was 16.2 l.
（発明の効果） 本発明に係る中性塩廃液の再生回収処理方法によれば、
中性塩廃液塩の濃度が消費塩濃度に比較して高い場合に
おいても、水位低下およびオーバフロー脱塩水の発生を
生じる事なく、廃液処理しようとする中性塩廃液が無く
なるまで、イオン交換膜電気透析装置の塩循環ラインへ
の導入・循環用溶液を常に有し、連続運転ができるの
で、処理効率を向上し得るようになる。(Effects of the Invention) According to the method for regenerating and recovering neutral salt waste liquid according to the present invention,
Neutral salt waste liquid Even when the salt concentration is higher than the consumed salt concentration, the ion-exchange membrane electrolysis is performed until there is no neutral salt waste liquid to be treated without causing water level drop and overflow demineralized water. Since a solution for introduction / circulation to the salt circulation line of the dialysis machine is always present and continuous operation is possible, the treatment efficiency can be improved.
また、この再生回収処理方法は、廃液処理されるたけで
なく、本来的に酸およびアルカリが分離して得られるも
のであり、更に上記の如くオーバフロー脱塩水の発生を
生じなくし得るので、処理液を全く出さないクローズド
システムにし得るようになる。In addition, this regeneration and recovery treatment method is not limited to waste liquid treatment, but is originally obtained by separation of acid and alkali, and as described above, it is possible to prevent the generation of overflow demineralized water. It will be possible to make a closed system that does not emit any at all.
従って、環境保全、省資源、経済性等の面に優れた廃液
処理、並びに、廃液からの酸およびアルカリの再生回収
処理を、高い処理効率の下で行い得るようになる。Therefore, it becomes possible to perform waste liquid treatment excellent in environmental protection, resource saving, economical efficiency, etc., and regeneration and recovery treatment of acid and alkali from the waste liquid with high treatment efficiency.
第１図は第１実施例に係る40％NaNO3廃液の再生回収処
理方法のフローシートの概略図、第２図はBP電気透析法
の原理の概要図、第３図は従来のBP電気透析法のフロー
チャートの概略図である。 （１）……中性塩廃液タンク （２）……廃液希釈用水タンク、（３）……塩循環用タ
ンク （４）……タンク（５）への注入用水タンク （５）……アルカリ循環タンク （６）……アルカリオーバフロータンク （７）……イオン交換膜電気透析装置の本体 （８）……アルカリライン、（９）……塩循環ライン （10）……酸ライン、（11）……酸循環タンク （12）……脱塩水タンクFIG. 1 is a schematic diagram of a flow sheet of the method for regenerating and recovering 40% NaNO 3 waste liquid according to the first embodiment, FIG. 2 is a schematic diagram of the principle of BP electrodialysis, and FIG. 3 is a conventional BP electrodialysis. 1 is a schematic diagram of a method flow chart. (1) …… Neutral salt waste liquid tank (2) …… Waste water dilution water tank, (3) …… Salt circulation tank (4) …… Injection water tank to tank (5) (5) …… Alkaline circulation Tank (6) …… Alkaline overflow tank (7) …… Main body of ion exchange membrane electrodialyzer (8) …… Alkaline line, (9) …… Salt circulation line (10) …… Acid line, (11)… … Acid circulation tank (12) …… Demineralized water tank
Claims (1)
ン交換膜を有し、且つ酸ライン、アルカリライン及び塩
循環用タンクをその途中に持つ塩循環ラインを有するイ
オン交換膜電気透析装置の該タンク内に中性塩廃液を断
続的に導入し、該タンク内溶液の塩濃度を略一定値に調
整し、該タンク内溶液を塩循環ラインにより電気透析装
置に導入し、塩循環ラインを循環させ、電気透析を行っ
て酸とアルカリと脱塩水とを分離して得る中性塩廃液の
再生回収処理方法であって、該タンク内へ断続的に水を
添加して前記タンク内溶液の液量調整を行い、且つ導入
中性塩廃液により該タンク内溶液の塩濃度の調整を行う
ことを特徴とする中性塩廃液の再生回収処理方法。1. An ion exchange membrane electrodialysis apparatus comprising a bipolar membrane, an anion exchange membrane and a cation exchange membrane, and an acid line, an alkali line and a salt circulation line having a salt circulation tank in the middle thereof. Neutral salt waste liquid is intermittently introduced into the tank, the salt concentration of the solution in the tank is adjusted to a substantially constant value, and the solution in the tank is introduced into the electrodialysis device by the salt circulation line and circulated in the salt circulation line. A method for regenerating and recovering a neutral salt waste liquid obtained by separating an acid, an alkali, and demineralized water by performing electrodialysis, in which water is intermittently added to the tank to prepare a solution of the solution in the tank. A method for regenerating and recovering a neutral salt waste liquid, which comprises adjusting the amount and adjusting the salt concentration of the solution in the tank by introducing the neutral salt waste liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15971988A JPH07115020B2 (en) | 1988-06-28 | 1988-06-28 | Recycling treatment method of neutral salt waste liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15971988A JPH07115020B2 (en) | 1988-06-28 | 1988-06-28 | Recycling treatment method of neutral salt waste liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH029493A JPH029493A (en) | 1990-01-12 |
| JPH07115020B2 true JPH07115020B2 (en) | 1995-12-13 |
Family
ID=15699784
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15971988A Expired - Lifetime JPH07115020B2 (en) | 1988-06-28 | 1988-06-28 | Recycling treatment method of neutral salt waste liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH07115020B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3482306B2 (en) * | 1996-09-04 | 2003-12-22 | オルガノ株式会社 | Supercritical water oxidation method and apparatus for organic chlorine compounds |
| KR100707191B1 (en) | 2005-05-25 | 2007-04-13 | 삼성전자주식회사 | Salt concentration control device using electrodialysis, lab-on-a-chip comprising the same and salt concentration control method using the same |
-
1988
- 1988-06-28 JP JP15971988A patent/JPH07115020B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH029493A (en) | 1990-01-12 |
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