JP2018001072A - Cleaning method of electric demineralizer - Google Patents
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Abstract
【課題】残留塩素等の酸化剤が流入することで通水差圧が上昇した電気脱イオン装置の差圧を、簡易な洗浄操作で短時間に効果的に回復させる。【解決手段】陽極１，陰極２の間に複数のアニオン交換膜３及びカチオン交換膜４が交互に配列して濃縮室５と脱塩室６とを交互に形成され、脱塩室６にイオン交換樹脂１０が充填されている電気脱イオン装置の脱塩室５の通水差圧が上昇してきた場合、通電を停止した後、流出口から流入口へ向う方向に、該電気脱イオン装置の規定流量の３０〜１００％の流量で純水又は超純水を５〜３０分程度通水する。【選択図】図１PROBLEM TO BE SOLVED: To effectively recover a differential pressure of an electric deionization device in which a water passage differential pressure has increased due to an inflow of an oxidizing agent such as residual chlorine in a short time by a simple cleaning operation. SOLUTION: A plurality of anion exchange membranes 3 and cation exchange membranes 4 are alternately arranged between an anode 1 and a cathode 2 to form a concentrating chamber 5 and a desalting chamber 6 alternately, and an ion is stored in the desalting chamber 6. When the water flow differential pressure of the deionization chamber 5 of the electric deionization apparatus filled with the exchange resin 10 increases, after stopping the energization, the electric deionization apparatus of the electric deionization apparatus moves in the direction from the outlet to the inlet. Pure water or ultrapure water is passed at a flow rate of 30 to 100% of the specified flow rate for about 5 to 30 minutes. [Selection diagram] Figure 1
Description
本発明は電気脱イオン装置の洗浄方法に係り、詳しくは、純水又は超純水の製造等に用いられる電気脱イオン装置において、酸化剤の流入により通水差圧が上昇した際に、簡易な操作で効果的に差圧を回復させる洗浄方法に関する。 The present invention relates to a method for cleaning an electrodeionization apparatus, and more particularly, in an electrodeionization apparatus used for production of pure water or ultrapure water, it is simplified when the water flow differential pressure increases due to the inflow of an oxidant. The present invention relates to a cleaning method that effectively recovers a differential pressure with a simple operation.
電気脱イオン装置は、カチオン交換膜とアニオン交換膜で形成される室にイオン交換樹脂を充填して脱塩室とし、この脱塩室に被処理水を通過させると共に、前記両イオン交換膜を介して直流電流を作用させて、両イオン交換膜の外側に流れている濃縮水中に被処理水中のイオンを電気的に排除しながら脱イオン水を製造するよう構成されている。 In the electrodeionization apparatus, a chamber formed by a cation exchange membrane and an anion exchange membrane is filled with an ion exchange resin to form a desalination chamber, and water to be treated is passed through the demineralization chamber. The deionized water is produced while electrically removing the ions in the water to be treated in the concentrated water flowing outside the two ion exchange membranes by applying a direct current through the two.
この電気脱イオン装置の脱塩室に被処理水を通水すると、被処理水中の不純物イオンは脱塩室内のイオン交換樹脂に吸着されて高度に脱塩された純水が製造される。一方、脱塩室内のイオン交換樹脂には不純物イオンが吸着されるが、このイオン交換樹脂に直流電流を通電することにより、イオンは濃縮室に移動するので、イオン交換樹脂は連続的に再生される。 When the water to be treated is passed through the demineralization chamber of this electric deionization apparatus, impurity ions in the water to be treated are adsorbed by the ion exchange resin in the demineralization chamber to produce highly demineralized pure water. On the other hand, impurity ions are adsorbed to the ion exchange resin in the desalination chamber. When a direct current is passed through the ion exchange resin, the ions move to the concentration chamber, so that the ion exchange resin is continuously regenerated. The
このような電気脱イオン装置に通水を継続すると、種々の原因により、通水差圧が次第に上昇してくる。 If water is continuously passed through such an electrodeionization apparatus, the water flow differential pressure gradually increases due to various causes.
通水差圧上昇の原因が、スケールや微生物の場合の洗浄方法としては、酸洗浄やアルカリ洗浄、過炭酸洗浄が知られている。 Acid cleaning, alkali cleaning, and percarbonate cleaning are known as cleaning methods in the case where the cause of the increase in water flow differential pressure is scale or microorganisms.
例えば、特許文献１には、内部にスライムが蓄積した電気脱イオン装置をヒドラジン水和物とアルカリを含有する薬液で洗浄する方法が記載されている。
特許文献２には、シリカが蓄積した電気脱イオン装置にアルカリ性液を通水する洗浄方法が記載されている。
For example, Patent Document 1 describes a method of cleaning an electrodeionization apparatus in which slime is accumulated with a chemical solution containing hydrazine hydrate and alkali.
Patent Document 2 describes a cleaning method in which an alkaline liquid is passed through an electrodeionization apparatus in which silica is accumulated.
電気脱イオン装置が、酸化剤に弱いことは知られており、給水中の残留塩素許容値等はカタログ等で厳しく定められているが、従来、電気脱イオン装置の給水に残留塩素などの酸化剤が混入して通水差圧が上昇した場合に、この差圧を回復させるための洗浄方法は提案されていない。 Electrodeionization equipment is known to be vulnerable to oxidizers, and the allowable residual chlorine value in feed water has been strictly determined in catalogs and other sources. No cleaning method has been proposed for recovering the differential pressure when the water flow differential pressure increases due to the mixing of the agent.
本発明は、残留塩素等の酸化剤が流入することで通水差圧が上昇した電気脱イオン装置の差圧を、簡易な洗浄操作で短時間に効果的に回復させることができる洗浄方法を提供することを課題とする。 The present invention provides a cleaning method capable of effectively recovering the differential pressure of an electrodeionization apparatus whose water flow differential pressure has increased due to inflow of an oxidant such as residual chlorine in a short time with a simple cleaning operation. The issue is to provide.
本発明者らは、上記課題を解決すべく、酸化剤の流入による電気脱イオン装置の通水差圧上昇のメカニズムを詳細に検討した結果、純水又は超純水を通水運転時とは逆方向に通水することにより、少ない洗浄水量で、短時間で効果的に差圧を回復させることができることを見出した。
即ち、本発明は以下を要旨とする。
In order to solve the above problems, the present inventors have studied in detail the mechanism of the water flow differential pressure increase of the electrodeionization apparatus due to the inflow of the oxidant. It has been found that the differential pressure can be effectively recovered in a short time with a small amount of washing water by passing water in the reverse direction.
That is, the gist of the present invention is as follows.
［１］ イオン交換樹脂を収容した室（以下、「イオン交換樹脂収容室」という）と、該イオン交換樹脂収容室に設けられた第１通水口及び第２通水口を有し、脱塩処理時には該第１通水口から第２通水口へ通水される電気脱イオン装置の該イオン交換樹脂収容室に、酸化剤が流入して通水差圧が上昇した際に、該イオン交換樹脂収容室の差圧を回復させるための洗浄方法であって、該電気脱イオン装置への通電を停止した状態で、該イオン交換樹脂収容室の第２通水口から第１通水口へ、該電気脱イオン装置における該イオン交換樹脂収容室の規定流量の３０〜１００％の流量で、純水又は超純水を通水することを特徴とする電気脱イオン装置の洗浄方法。 [1] Desalination treatment having a chamber containing ion exchange resin (hereinafter referred to as “ion exchange resin storage chamber”) and a first water inlet and a second water outlet provided in the ion exchange resin storage chamber. Sometimes the ion exchange resin is accommodated when an oxidant flows into the ion exchange resin accommodation chamber of the electrodeionization device that is passed from the first water inlet to the second water inlet and the water differential pressure rises. A cleaning method for recovering the differential pressure in the chamber, wherein the electrodeionization device is moved from the second water inlet to the first water outlet in the ion exchange resin storage chamber in a state where energization to the electrodeionization device is stopped. A cleaning method for an electrodeionization apparatus, wherein pure water or ultrapure water is passed at a flow rate of 30 to 100% of a prescribed flow rate of the ion exchange resin storage chamber in the ion device.
［２］ ［１］において、前記純水又は超純水を５〜３０分通水ことを特徴とする電気脱イオン装置の洗浄方法。 [2] A cleaning method for an electrodeionization apparatus according to [1], wherein the pure water or ultrapure water is passed for 5 to 30 minutes.
［３］ ［１］又は［２］において、前記イオン交換樹脂収容室の通水差圧が初期差圧の２．０倍以下の時点で前記純水又は超純水の通水を行うことを特徴とする電気脱イオン装置の洗浄方法。 [3] In [1] or [2], passing the pure water or ultrapure water when the water flow differential pressure in the ion exchange resin storage chamber is 2.0 times or less the initial differential pressure. A method for cleaning an electrodeionization apparatus.
本発明によれば、残留塩素等の酸化剤が流入することで通水差圧が上昇した電気脱イオン装置に、通水運転時と逆方向に純水又は超純水を所定の流量で通水するという簡易な洗浄操作により、比較的少ない洗浄水量で、短時間で効果的に差圧を回復させることができる。 According to the present invention, pure water or ultrapure water is passed at a predetermined flow rate in an opposite direction to that in the water-flowing operation through the electrodeionization apparatus whose water-flow differential pressure has increased due to the inflow of oxidant such as residual chlorine. By a simple washing operation of rinsing, the differential pressure can be effectively recovered in a short time with a relatively small amount of washing water.
以下に本発明の実施の形態を説明する。 Embodiments of the present invention will be described below.
＜メカニズム＞
本発明者らは、酸化剤の流入により通水差圧が上昇した電気脱イオン装置の差圧を効果的に回復させる洗浄方法を見出すべく、まず、電気脱イオン装置に塩素が流入した場合の劣化メカニズムにつき鋭意研究を行った。
その結果、以下の点が明らかになった。
<Mechanism>
In order to find a cleaning method that effectively recovers the differential pressure of the electrodeionization apparatus in which the water flow differential pressure has increased due to the inflow of the oxidant, first, the present inventors first described the case where chlorine flows into the electrodeionization apparatus. We conducted intensive research on the deterioration mechanism.
As a result, the following points became clear.
（１） 残留塩素が給水中に含まれて電気脱イオン装置に流入すると、電気脱イオン装置内の直流印加条件下で、流入した残留塩素の形態が一部変化して酸化力が増大する。これは、残留塩素が一部ラジカル化していることによると考えられる。
（２） その増大した残留塩素の酸化力により、電気脱イオン装置に充填されているイオン交換樹脂が酸化劣化で粉砕される。通常の塩素では、イオン交換樹脂は粉砕に到るまでに劣化することは稀であり、このことからも、電気脱イオン装置内に流入した残留塩素が増大した酸化力を有すると考えられる。
（３） このようなイオン交換樹脂の破砕は、給水の入口部から出口側に向けて経時的に順次起こる。これは、流入した残留塩素の酸化力が強力であるため、イオン交換樹脂が、それ自体、粉となって反応することで、これらの酸化物質が消費され、逆にそれにより、それよりも下流側のイオン交換樹脂には酸化力が達しないようになるためと考えられる。
（４） （３）より、一時的な給水への残留塩素の流入であれば、給水入口部のみのイオン交換樹脂が粉々になってるだけであり、それよりも下流側のイオン交換樹脂は劣化の問題は殆どない。
（５） このように粉砕されたイオン交換樹脂が給水入口部のみにある場合、すなわち劣化がまだ初期段階にある場合は、処理水出口側から水（純水又は超純水）を入れ、入口側から排出させる、いわゆる逆洗を行うことで破砕樹脂が排出され、通水差圧を回復させることができる。この場合、濾過塔等の逆洗とは異なり、通常の通水量またはそれよりも少ない量、具体的には通水量の３分の１程度の逆洗水量でも、微細樹脂を排出することができるため、極めて簡易に洗浄を行える。
（６） 塩素劣化が長期にわたる場合、差圧上昇が激しい場合や差圧だけでなく得られる処理水の水質までもが低下している場合においては、（５）の逆洗は必ずしも有効とは言えず、この洗浄方法は、塩素等の酸化剤による酸化劣化の初期段階の劣化による差圧上昇を回復させるために有効である。
(1) When residual chlorine is contained in the feed water and flows into the electrodeionization apparatus, the form of the residual chlorine that has flowed in partially changes under the direct current application condition in the electrodeionization apparatus, and the oxidizing power increases. This is considered to be because the residual chlorine is partially radicalized.
(2) Due to the increased oxidizing power of residual chlorine, the ion exchange resin filled in the electrodeionization apparatus is pulverized by oxidative degradation. With ordinary chlorine, the ion exchange resin rarely deteriorates before pulverization. From this, it is considered that the residual chlorine flowing into the electrodeionization apparatus has an increased oxidizing power.
(3) Such crushing of the ion exchange resin occurs sequentially with time from the inlet portion toward the outlet side of the water supply. This is because the oxidizing power of the residual chlorine that flows in is strong, so that the ion exchange resin itself reacts as a powder, so that these oxidizing substances are consumed, and conversely, it is further downstream. This is probably because the ion exchange resin on the side does not reach the oxidizing power.
(4) From (3), if the residual chlorine flows into the temporary water supply, only the ion exchange resin at the inlet of the water supply is shattered, and the ion exchange resin on the downstream side is degraded. There is almost no problem.
(5) When the ion-exchange resin thus pulverized is only in the feed water inlet, that is, when deterioration is still in the initial stage, water (pure water or ultrapure water) is introduced from the treated water outlet side, and the inlet By performing so-called back washing, which is discharged from the side, the crushed resin is discharged, and the water flow differential pressure can be recovered. In this case, unlike the backwashing of a filtration tower or the like, the fine resin can be discharged even with a normal water flow rate or an amount smaller than that, specifically, with a backwash water amount of about one third of the water flow rate. Therefore, cleaning can be performed very easily.
(6) Backwashing in (5) is not always effective when chlorine degradation is prolonged, when the differential pressure rises severely, or when not only the differential pressure but also the quality of the treated water is reduced. Needless to say, this cleaning method is effective for recovering an increase in differential pressure due to deterioration in the initial stage of oxidative deterioration due to an oxidizing agent such as chlorine.
以上のメカニズムから、本発明では、イオン交換樹脂を収容した室と、該室に設けられた第１通水口及び第２通水口を有し、脱塩処理時には該第１通水口から第２通水口へ通水される電気脱イオン装置の該室に酸化剤が流入して通水差圧が上昇した際に、該イオン交換樹脂収容室の差圧を回復させるための洗浄方法として、該電気脱イオン装置への通電を停止した状態で、該イオン交換樹脂収容室の第２通水口から第１通水口へ、該電気脱イオン装置の規定流量の３０〜１００％の流量で、好ましくは５〜３０分程度純水又は超純水を通水する洗浄を行う。 From the above mechanism, the present invention has a chamber containing the ion exchange resin, and a first water inlet and a second water outlet provided in the chamber. As a cleaning method for recovering the differential pressure in the ion exchange resin storage chamber when an oxidant flows into the chamber of the electrodeionization apparatus that is passed to the water port and the water differential pressure rises, In a state where energization to the deionization device is stopped, the flow rate is 30 to 100% of the prescribed flow rate of the electrodeionization device from the second water inlet to the first water inlet of the ion exchange resin storage chamber, preferably 5 Wash with pure water or ultrapure water for about 30 minutes.
＜電気脱イオン装置の洗浄方法＞
以下、図面を参照して本発明の電気脱イオン装置の洗浄方法をより詳細に説明する。
図１は、一般的な電気脱イオン装置の一例を示す模式的な断面図であり、陽極１，陰極２の間に複数のアニオン交換膜３及びカチオン交換膜４を交互に配列して濃縮室５と脱塩室（イオン交換樹脂収容室）６とを交互に形成し、脱塩室６にイオン交換樹脂１０が充填されている。濃縮室５にはイオン交換樹脂又はスペーサが充填または配置される。陽極１が配置された陽極室７は、それに直近の濃縮室５とカチオン交換膜４を介して隔てられている。陰極３２が配置された陰極室８は、それに直近の濃縮室５とアニオン交換膜３を介して隔てられている。被処理水（給水）は、この脱塩室６に対し図の上端側の流入口（第１通水口）から流入し、処理水が図の下端側の流出口（第２通水口）から取り出される。
<Cleaning method for electrodeionization equipment>
Hereinafter, the cleaning method of the electrodeionization apparatus of the present invention will be described in more detail with reference to the drawings.
FIG. 1 is a schematic cross-sectional view showing an example of a general electrodeionization apparatus, in which a plurality of
このイオン交換樹脂１０の平均粒径は、好ましくは０．４〜１．０ｍｍ特に０．５〜０．７ｍｍ程度である。脱塩室６の流入口（第１通水口）及び流出口（第２通水口）には、通常、それぞれ目開き０．１〜０．３ｍｍ特に０．２〜０．３ｍｍ程度のストレーナが設けられている。
The average particle diameter of the
このような電気脱イオン装置において、酸化剤を含む水、例えば水道水、塩素を添加して凝集沈殿処理を行った処理水等の酸化剤を残留塩素として０．０５〜１．０ｍｇ−Ｃｌ２／Ｌ程度含む水、具体的には水道水、凝集処理水、ＵＦ膜処理水などを給水として脱塩処理を行うと、イオン交換樹脂が、前述の通り、酸化劣化を受けて粉砕されることで通水差圧が上昇してくる。電気脱イオン装置の通水差圧の上昇が認められたら、通常運転（被処理水の脱塩を行う運転）を停止し、脱塩室６の流出口（第２通水口）から純水又は超純水を通水して流入口（第１通水口）から排出させる配管を組み立て、流出口（第２通水口）より純水又は超純水を通水して脱塩室６内の洗浄を行う（既設の配管を利用可能な場合は、特に配管を組み立てる必要はない。）。
In such an electrodeionization apparatus, water containing an oxidant, for example, tap water, and an oxidant such as treated water that has been subjected to a coagulation sedimentation treatment by adding chlorine, 0.05 to 1.0 mg-Cl 2 as residual chlorine. When demineralization treatment is performed using water containing about / L, specifically tap water, flocculated water, UF membrane treated water, etc., the ion exchange resin is pulverized due to oxidative degradation as described above. The water flow differential pressure increases. When an increase in the water flow differential pressure of the electrodeionization apparatus is observed, the normal operation (operation for performing desalting of the water to be treated) is stopped, and pure water or water is discharged from the outlet (second water flow port) of the
前述の通り、脱塩室６内のイオン交換樹脂の酸化劣化が進行し、差圧上昇が大きくなった場合や更に処理水水質までも低下している場合には、このように逆方向の通水を行っても差圧を回復し得ない場合がある。このため、本発明に従う洗浄は、差圧上昇が激しくないときに、例えば、脱塩室の差圧が通水初期（脱塩処理運転開始時）の差圧に対して２．０倍以下、好ましくは１．５〜２．０倍程度となった時点で行うことが好ましい。
As described above, when the oxidative deterioration of the ion exchange resin in the
前述の通り、本発明の洗浄方法は、電気脱イオン装置内のイオン交換樹脂が、給水に含まれて流入した酸化剤により劣化して粉砕されることにより差圧が上昇してきたときの初期段階の洗浄に有効であり、それ以外の要因による差圧上昇に対しては有効でない場合がある。
例えば、電気脱イオン装置の前段にイオン交換樹脂塔やホウ素吸着樹脂塔が設置されている場合、これらの樹脂塔からの流出水中に、塔内充填樹脂の微細樹脂が含まれて電気脱イオン装置に流入することで電気脱イオン装置の差圧が上昇することがあるが、このような原因で差圧が上昇した場合、本発明のような低流量かつ短時間の洗浄では差圧を回復させることができない場合がある。従って、本発明の洗浄方法は、電気脱イオン装置の直前にイオン交換樹脂塔やホウ素吸着樹脂塔などの樹脂充填塔が設けられていない場合に好適である。
As described above, the cleaning method of the present invention is an initial stage when the differential pressure increases due to the ion exchange resin in the electrodeionization apparatus being deteriorated and pulverized by the oxidant contained in the feed water. It may be effective for cleaning water and may not be effective for increasing differential pressure due to other factors.
For example, when an ion exchange resin tower or a boron adsorption resin tower is installed in the previous stage of the electrodeionization apparatus, the ionized ion apparatus contains fine resin of the resin packed in the tower in the effluent water from these resin towers. The differential pressure of the electrodeionization device may increase due to flow into the gas, but when the differential pressure increases due to such a cause, the differential pressure is recovered by washing at a low flow rate for a short time as in the present invention. It may not be possible. Therefore, the cleaning method of the present invention is suitable when a resin-filled tower such as an ion exchange resin tower or a boron adsorption resin tower is not provided immediately before the electrodeionization apparatus.
また、洗浄時の脱塩室６内の純水又は超純水の通水流量は、当該電気脱イオン装置の規定流量以下でよく、規定流量の３０〜１００％、好ましくは３０〜５０％程度の流量で十分な洗浄効果を得ることができる（以下、この規定流量に対する洗浄時の純水又は超純水の通水流量の割合の百分率を「規定流量比」と称す場合がある。）。また、その洗浄時間についても、規定流量比にもよるが、５〜３０分、特に５〜２０分程度でも十分な効果を得ることができる。
特に本発明では、規定流量比（％）と洗浄時間（分）との積が１００〜５００（％・分）となるように純水又は超純水を通水することが好ましい。この値が小さ過ぎると十分な差圧回復効果が得られないが、この値が大き過ぎても、徒に洗浄水流量が増大し、洗浄時間が長くなるだけであり、非効率である。
Further, the flow rate of pure water or ultrapure water in the
In particular, in the present invention, it is preferable to pass pure water or ultrapure water so that the product of the specified flow rate ratio (%) and the cleaning time (min) is 100 to 500 (% · min). If this value is too small, a sufficient differential pressure recovery effect cannot be obtained, but if this value is too large, the washing water flow rate increases and the washing time is increased, which is inefficient.
このように、純水又は超純水を流出口（第２通水口）から通水して流入口（第１通水口）から排出される洗浄排水中には、微細に粉砕されたイオン交換樹脂が含まれたものとなる。従って、この流入口（第１通水口）から排出される洗浄排水は、凝集処理等を含む排水処理系統へ送給して処理することが好ましい。 In this way, finely pulverized ion exchange resin is contained in the cleaning wastewater discharged from the inflow port (first water flow port) by passing pure water or ultrapure water from the flow port (second flow port). Will be included. Therefore, it is preferable that the cleaning waste water discharged from the inflow port (first water inlet) is supplied to a waste water treatment system including agglomeration treatment and the like.
なお、上述の説明では、脱塩室を本発明に従って洗浄する場合を例示して説明したが、本発明によれば、脱塩室に限らず、イオン交換樹脂が充填された濃縮室の洗浄についても上記と同様に行うことができ、同様に優れた洗浄効果を得ることができる。 In the above description, the case where the desalting chamber is cleaned according to the present invention has been described as an example. However, according to the present invention, not only the desalting chamber but also the concentration chamber filled with an ion exchange resin is cleaned. Can be performed in the same manner as described above, and an excellent cleaning effect can be obtained in the same manner.
本発明では、洗浄水としては、純水又は超純水を用いるが、特に脱塩室の洗浄に当っては、洗浄時の系内汚染で洗浄後の脱塩処理運転再開時の生産水（処理水）の水質が低下するのを防止するために超純水を用いることが好ましい。洗浄に用いる純水又は超純水は、系外から導入されるものであってもよく、当該電気脱イオン装置で製造された純水又は超純水であってもよい。 In the present invention, pure water or ultrapure water is used as the washing water. In particular, when washing the desalting chamber, the production water (when the desalination treatment operation is resumed after washing due to internal contamination during washing) ( It is preferable to use ultrapure water in order to prevent deterioration of the water quality of the (treated water). The pure water or ultrapure water used for washing may be introduced from outside the system, or pure water or ultrapure water produced by the electrodeionization apparatus.
以下に実施例及び比較例を挙げて本発明をより具体的に説明する。 Hereinafter, the present invention will be described more specifically with reference to Examples and Comparative Examples.
［実施例１］
静岡県吉田町水道水由来の残留塩素を０．１〜０．３ｍｇ−Ｃｌ２／Ｌ含む給水を処理することで、電気脱イオン装置（エボクア社製「ＣＤＩ−ＶＮＸ」）の脱塩室の差圧が０．４ｋｇ／ｃｍ２から０．８ｋｇ／ｃｍ２（初期差圧の２倍）に上昇したため、本発明に従って洗浄を行った。
この電気脱イオン装置は、脱塩室にイオン交換樹脂が充填されたものであり、通水運転時の規定流量は１５ｍ３／ｈｒである。
この電気脱イオン装置を処理水系から取り外し、電気脱イオン装置の処理水出口側から超純水を５ｍ３／ｈｒで１０分間通水し、給水入口側から排出した。
その結果、脱塩室の差圧が０．４５ｋｇ／ｃｍ２まで回復した。
[Example 1]
By treating water containing 0.1 to 0.3 mg-Cl 2 / L of residual chlorine derived from tap water in Yoshida-shi, Shizuoka Prefecture, the deionization chamber of the electrodeionization device (“CDI-VNX” manufactured by Evoqua) Since the differential pressure increased from 0.4 kg / cm 2 to 0.8 kg / cm 2 (twice the initial differential pressure), cleaning was performed according to the present invention.
This electrodeionization apparatus is one in which a demineralization chamber is filled with an ion exchange resin, and the specified flow rate during water flow operation is 15 m 3 / hr.
This electrodeionization apparatus was removed from the treated water system, ultrapure water was passed through the treated water outlet side of the electrodeionization apparatus for 10 minutes at 5 m 3 / hr, and discharged from the feed water inlet side.
As a result, the differential pressure in the desalting chamber was recovered to 0.45 kg / cm 2 .
［比較例１］
実施例１において、超純水を処理水出口側から通水する代りに、以下の通り、アルカリ・酸洗浄を行った。
まず、１重量％ＮａＯＨ水溶液を１０ｍ３／ｈｒで３０分間、脱塩室に給水通水方向と同方向で通水し、排出水を入口側に循環するアルカリ洗浄を行った後、１重量％塩酸水溶液を用いて上記と同様に循環洗浄し、更に、超純水を給水通水方向と同方向に１０ｍ３／ｈｒで３時間通水して仕上げ洗浄を行った。
しかし、洗浄後の脱塩室の差圧は０．８ｋｇ／ｃｍ２のままで差圧は回復しなかった。
[Comparative Example 1]
In Example 1, instead of passing ultrapure water from the treated water outlet side, alkali / acid cleaning was performed as follows.
First, a 1% by weight NaOH aqueous solution was passed through the desalting chamber at 10 m 3 / hr for 30 minutes in the same direction as the feed water passing direction, and after washing with alkali to circulate the discharged water to the inlet side, 1% by weight Circulating and washing was performed using an aqueous hydrochloric acid solution in the same manner as described above, and ultra-pure water was further passed for 3 hours at 10 m 3 / hr in the same direction as the feed water flow direction for finish cleaning.
However, the differential pressure in the desalting chamber after washing remained at 0.8 kg / cm 2 and the differential pressure did not recover.
１ 陽極
２ 陰極
３ アニオン交換膜
４ カチオン交換膜
５ 濃縮室
６ 脱塩室
７ 陽極室
８ 陰極室
1 Anode 2
Claims (3)
該電気脱イオン装置への通電を停止した状態で、該イオン交換樹脂収容室の第２通水口から第１通水口へ、該電気脱イオン装置における該イオン交換樹脂収容室の規定流量の３０〜１００％の流量で、純水又は超純水を通水することを特徴とする電気脱イオン装置の洗浄方法。 A chamber containing an ion exchange resin (hereinafter referred to as an “ion exchange resin storage chamber”) and a first water inlet and a second water outlet provided in the ion exchange resin storage chamber; When the oxidant flows into the ion exchange resin storage chamber of the electrodeionization apparatus that is passed from one water inlet to the second water inlet and the water flow differential pressure increases, the difference between the ion exchange resin storage chambers. A cleaning method for recovering pressure,
With the energization to the electrodeionization device stopped, the prescribed flow rate of the ion exchange resin storage chamber in the electrodeionization device is 30 to from the second water inlet of the ion exchange resin storage chamber to the first water inlet. A cleaning method for an electrodeionization apparatus, wherein pure water or ultrapure water is passed at a flow rate of 100%.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JPWO2020203142A1 (en) * | 2019-03-29 | 2020-10-08 | ||
| CN113493240A (en) * | 2020-04-01 | 2021-10-12 | 佛山市云米电器科技有限公司 | Regeneration control method, household water purifying device and computer readable storage medium |
| JP7339473B1 (en) * | 2022-04-15 | 2023-09-05 | オルガノ株式会社 | Deionized water production system operating method and deionized water production system |
| WO2023199676A1 (en) * | 2022-04-15 | 2023-10-19 | オルガノ株式会社 | Method for operating deionized water production system and deionized water production system |
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2016
- 2016-06-29 JP JP2016129004A patent/JP2018001072A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPWO2020203142A1 (en) * | 2019-03-29 | 2020-10-08 | ||
| WO2020203142A1 (en) * | 2019-03-29 | 2020-10-08 | 栗田工業株式会社 | Particle removal device and particle removal method |
| CN113493240A (en) * | 2020-04-01 | 2021-10-12 | 佛山市云米电器科技有限公司 | Regeneration control method, household water purifying device and computer readable storage medium |
| CN113493240B (en) * | 2020-04-01 | 2023-02-28 | 佛山市云米电器科技有限公司 | Regeneration control method, household water purifying device and computer readable storage medium |
| JP7339473B1 (en) * | 2022-04-15 | 2023-09-05 | オルガノ株式会社 | Deionized water production system operating method and deionized water production system |
| WO2023199676A1 (en) * | 2022-04-15 | 2023-10-19 | オルガノ株式会社 | Method for operating deionized water production system and deionized water production system |
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