JP2007090249A - Method for cleaning membrane deaerator - Google Patents
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本発明は膜脱気装置の洗浄方法に係り、特に、ボイラ給水系や冷却水系の腐食防止のために設置される膜脱気装置を効率的に洗浄して、経時的な圧力損失の上昇、流量低下、脱気性能の低下や膜劣化を防止する方法に関する。 The present invention relates to a method for cleaning a membrane deaerator, and in particular, effectively cleans a membrane deaerator installed to prevent corrosion of a boiler feed water system and a cooling water system, thereby increasing the pressure loss with time. The present invention relates to a method for preventing a decrease in flow rate, a decrease in deaeration performance, and film deterioration.
ボイラ給水系や冷却水系では、水中の溶存酸素や炭酸ガスによる系内腐食を防止するために、水道水又は工業用水等を脱気処理した後給水することが行われている。従来、この脱気処理には、脱気塔や脱炭酸塔が用いられてきたが、最近では、装置の小型化が可能で安価な膜脱気装置が用いられるようになってきている。 In a boiler water supply system and a cooling water system, in order to prevent corrosion in the system due to dissolved oxygen or carbon dioxide in water, tap water or industrial water is degassed and then supplied. Conventionally, a deaeration tower or a decarbonation tower has been used for this deaeration treatment, but recently, an inexpensive membrane deaeration apparatus capable of reducing the size of the apparatus has come to be used.
膜脱気装置は、ポリテトラフルオロエチレン膜、ポリプロピレン膜等の疎水性の高分子膜で内部を原水側と透過側とに仕切った脱気膜モジュールの透過側を真空ポンプで減圧することにより、原水側に流入させた被処理水中の溶存気体を膜透過させて除去するものであり、一般的には、前処理用のフィルタ（以下「プレフィルタ」と称す場合がある。）と脱気膜モジュールとの組み合わせで用いられている。 The membrane deaerator is a vacuum pump that depressurizes the permeation side of a deaeration membrane module that is divided into a raw water side and a permeation side with a hydrophobic polymer membrane such as a polytetrafluoroethylene membrane and a polypropylene membrane. Dissolved gas in the water to be treated that has flowed into the raw water side is removed by permeation through a membrane. Generally, a pretreatment filter (hereinafter sometimes referred to as “prefilter”) and a degassing membrane are used. Used in combination with modules.
膜脱気装置では、脱気処理を継続することにより、水道水や工業用水等の給水中に含有される無機物（酸化鉄、酸化アルミニウム、酸化カルシウム、酸化ケイ素）や有機物（微生物、藻類、油分、多糖類ポリマー等の有機化合物）が脱気膜やプレフィルタで析出し、このために脱気膜やプレフィルタの細孔（水の流路）が閉塞して、圧力損失が上昇すると共に、流量が低下し、また脱気性能が低下するという問題がある。 In membrane deaerators, by continuing deaeration treatment, inorganic substances (iron oxide, aluminum oxide, calcium oxide, silicon oxide) and organic substances (microorganisms, algae, oil content) contained in tap water and industrial water supply water , Organic compounds such as polysaccharide polymers) are deposited in the degassing membrane or prefilter, which causes the pores (water flow paths) of the degassing membrane or prefilter to close up, increasing the pressure loss, There is a problem that the flow rate is lowered and the deaeration performance is lowered.
従来、この問題に対して、次の(1)又は(2)の対策が講じられている。
(1) 運転を停止して、プレフィルタの交換や脱気膜モジュールの薬品洗浄を実施する。通常、このプレフィルタの交換や脱気膜モジュールの薬品洗浄は３〜６ヶ月に１回の頻度で実施されている。
(2) 使い捨て型のプレフィルタの代りに、ＭＦ（精密濾過）膜モジュールを用いて脱気膜モジュールの汚染を防止し、ＭＦ膜モジュールについては、定期的にＭＦ膜の透過水側からの逆洗や空気洗浄を行う。
Conventionally, the following countermeasure (1) or (2) has been taken for this problem.
(1) Stop the operation and replace the prefilter and clean the degassing membrane module. Usually, the replacement of the prefilter and the chemical cleaning of the deaeration membrane module are performed once every 3 to 6 months.
(2) Instead of a disposable prefilter, an MF (microfiltration) membrane module is used to prevent contamination of the degassing membrane module. For the MF membrane module, the reverse of the MF membrane from the permeate side Wash and air wash.
しかしながら、上記(1)の方法では、プレフィルタの交換や脱気膜モジュールの薬品洗浄のためのメンテナンス頻度が高く、手間と費用がかかるという問題がある。 However, the method (1) has a problem that the maintenance frequency for exchanging the prefilter and cleaning the degassing membrane module is high, and it takes time and money.
また、上記(2)の方法では、洗浄機能付きのＭＦ膜が高価である上に、逆洗のために処理水の２〜５％程度を使用し、水の回収効率が悪いという問題がある。 In addition, the method (2) has a problem that the MF membrane with a cleaning function is expensive and about 2 to 5% of the treated water is used for backwashing, and the water recovery efficiency is poor. .
脱気膜モジュールの脱気膜の汚染は、膜の目詰まりで膜が劣化する原因となり、また、膜の薬品洗浄による膜劣化の問題もあり、膜寿命の面でも好ましくない。 Contamination of the deaeration membrane of the deaeration membrane module causes the membrane to deteriorate due to clogging of the membrane, and there is also a problem of membrane degradation due to chemical cleaning of the membrane, which is not preferable in terms of membrane life.
本発明は、上記従来の問題点を解決し、膜脱気装置を効率的に洗浄して、経時的な圧力損失の上昇、流量低下、脱気性能の低下や膜劣化を防止する膜脱気装置の洗浄方法を提供することを目的とする。 The present invention solves the above-mentioned conventional problems and efficiently cleans the membrane deaeration device to prevent an increase in pressure loss over time, a decrease in flow rate, a decrease in deaeration performance, and membrane deterioration. An object is to provide a method for cleaning an apparatus.
本発明の膜脱気装置の洗浄方法は、脱気膜モジュールを有する膜脱気装置を洗浄する方法において、該膜脱気装置に供給される給水中に連続又は間欠的に洗浄剤を含有させることを特徴とする。 The method for cleaning a membrane deaerator according to the present invention is a method for cleaning a membrane deaerator having a deaerator module, wherein a cleaning agent is continuously or intermittently contained in the water supplied to the membrane deaerator. It is characterized by that.
本発明では、膜脱気装置への給水中に洗浄剤を含有させることにより、運転中に脱気膜モジュールを洗浄することができる。 In this invention, a deaeration membrane module can be wash | cleaned during a driving | operation by containing a washing | cleaning agent in the water supply to a membrane deaeration apparatus.
この洗浄剤としては、酸又はアルカリ剤が好ましい。 As this cleaning agent, an acid or an alkali agent is preferable.
即ち、無機物による脱気膜モジュールの膜汚染は、イオン状又はコロイド状の酸化鉄、酸化アルミニウム、酸化カルシウム等の無機酸化物が結晶化して膜面で析出し、膜面に付着することにより起こる。これらの無機酸化物の溶解度はｐＨ４であれば、ｐＨ７の場合の約１００倍にもなり、このため、給水に酸を添加してｐＨ４〜６程度とすることにより、これらの無機酸化物を溶解させて、膜面での析出、付着を防止することができる。
That is, the membrane contamination of the deaeration membrane module by the inorganic substance occurs when inorganic oxides such as ionic or colloidal iron oxide, aluminum oxide, calcium oxide, etc. crystallize and deposit on the membrane surface and adhere to the membrane surface. . If the solubility of these inorganic oxides is
一方、給水にアルカリを添加してｐＨ１０〜１２程度とすることにより、例えばカルボキシル基のケン化、タンパク質の溶解などにより、有機物の溶解度を高め、有機物による脱気膜モジュールの膜汚染を防止することができる。 On the other hand, by adding alkali to the water supply to a pH of about 10-12, for example, by increasing the solubility of organic matter by saponification of carboxyl group, dissolving protein, etc., preventing membrane contamination of the deaeration membrane module by organic matter Can do.
従って、本発明では、給水に酸を添加してｐＨ４〜６に調整するか、或いはアルカリを添加してｐＨ１０〜１２に調整することが好ましく、特に、給水のｐＨを４〜６に調整する洗浄操作と、給水のｐＨを１０〜１２に調整する洗浄操作とを組み合わせて行うことが好ましい。 Accordingly, in the present invention, it is preferable to adjust the pH to 4 to 6 by adding an acid to the feed water, or to adjust the pH to 10 to 12 by adding an alkali, and in particular, the washing to adjust the pH of the feed water to 4 to 6. It is preferable to perform the operation in combination with a cleaning operation for adjusting the pH of the feed water to 10-12.
本発明の膜脱気装置の洗浄方法によれば、膜脱気装置をその運転中に効率的に洗浄することができる。 According to the method for cleaning a membrane deaerator of the present invention, the membrane deaerator can be efficiently cleaned during its operation.
このため、脱気膜モジュールの前段にプレフィルタを設けた場合にはプレフィルタの交換頻度を、またプレフィルタを設けない場合には、脱気膜モジュールの薬品洗浄頻度を従来に比べて１／３〜１／４に低減することができ、メンテナンスのための手間と費用を大幅に削減した上で、長期に亘り、安定かつ効率的な脱気処理を行うことが可能となる。また、脱気膜モジュールへの汚染物質の付着量が低減することにより、安定した脱気性能を確保することができると共に、薬品洗浄や脱気膜の目詰まり等による膜劣化も防止され、膜寿命を延長することができる。 For this reason, when a prefilter is provided in the front stage of the degassing membrane module, the replacement frequency of the prefilter is reduced. When no prefilter is provided, the chemical cleaning frequency of the degassing membrane module is reduced to It can be reduced to 3 to 1/4, and it is possible to perform a stable and efficient deaeration process over a long period of time while greatly reducing the labor and cost for maintenance. In addition, by reducing the amount of contaminants attached to the degassing membrane module, it is possible to ensure stable degassing performance and prevent membrane deterioration due to chemical cleaning, clogging of the degassing membrane, etc. Life can be extended.
以下に図面を参照して本発明の膜脱気装置の洗浄方法の実施の形態を詳細に説明する。 Embodiments of a cleaning method for a membrane degassing apparatus of the present invention will be described below in detail with reference to the drawings.
図１は本発明の膜脱気装置の洗浄方法の実施の形態を示す系統図である。 FIG. 1 is a system diagram showing an embodiment of a cleaning method for a membrane deaerator of the present invention.
図１は、ボイラ給水系の膜脱気装置の洗浄方法を示し、水道水、工業用水等の原水は、イオン交換樹脂塔等の軟水器１で硬度成分が除去された後、ポンプＰ１により、プレフィルタ２で前処理され、その後脱気膜モジュール３に導入される。脱気膜モジュール３の原水側に導入された水は、脱気膜の透過側が真空ポンプ４で減圧されることにより脱気処理され、脱気処理水は給水タンク５に貯留される。給水タンク５の脱気処理水はポンプＰ２によりボイラに給水される。
FIG. 1 shows a cleaning method of a boiler water supply system membrane deaerator. Raw water such as tap water and industrial water is removed by a soft water device 1 such as an ion exchange resin tower, and then pumped by a pump P 1. The pre-filter 2 is then pretreated, and then introduced into the degassing membrane module 3. The water introduced to the raw water side of the degassing membrane module 3 is degassed by depressurizing the permeation side of the degassing membrane by the
プレフィルタ２への給水配管には、薬品タンク６内の洗浄剤がダイヤフラム式等の薬注ポンプＰ３により注入されるが、図１（ａ）では、この薬注ポンプＰ３の作動をタイマー７で制御することにより、洗浄剤が注入される。 The cleaning agent in the chemical tank 6 is injected into the water supply pipe to the pre-filter 2 by a diaphragm-type chemical injection pump P 3. In FIG. 1A, the operation of the chemical injection pump P 3 is a timer. By controlling at 7, the cleaning agent is injected.
また図１（ｂ）では、脱気膜モジュール３の入口側に設けられたｐＨ測定器８の測定結果が入力される制御器９により薬注ポンプＰ３の作動が制御される。 Also in FIG. 1 (b), the operation of the dosing pump P 3 is controlled by the controller 9 to the measurement results of the pH measurement device 8 provided on the inlet side of the degassing membrane module 3 is inputted.
図１（ａ）の方法は、原水の水質が安定しており、かつ、通水量が一定の場合に有利であり、タイマー７による薬注ポンプＰ３の作動制御で薬品タンク６内の洗浄剤が給水配管に連続的又は間欠的に注入される。 The method of FIG. 1A is advantageous when the quality of the raw water is stable and the water flow rate is constant, and the cleaning agent in the chemical tank 6 is controlled by the operation of the chemical injection pump P 3 by the timer 7. Is continuously or intermittently injected into the water supply pipe.
また、図１（ｂ）の方法は、ｐＨ測定器８の測定結果に基いて、脱気膜モジュール３の給水のｐＨが所定のｐＨとなるように薬注ポンプＰ３の作動を制御するため、原水水質や通水量に変動がある場合でも、脱気膜モジュール３の給水を所望のｐＨ値に調整することができる。 Further, the method of FIG. 1B is for controlling the operation of the medicinal pump P 3 so that the pH of the feed water of the deaeration membrane module 3 becomes a predetermined pH based on the measurement result of the pH measuring device 8. Even when the raw water quality and the flow rate vary, the water supply of the deaeration membrane module 3 can be adjusted to a desired pH value.
本発明において、給水に注入する洗浄剤としては、酸又はアルカリが好ましく、前述の如く、酸を添加して給水のｐＨを４〜６に調整することにより、既にプレフィルタ２や脱気膜モジュール３の脱気膜に付着した無機物を溶解させて除去すると共に、プレフィルタ２や脱気膜モジュール３の脱気膜へのこれらの無機物の付着を防止して、無機物による汚染を防止することができる。 In the present invention, the cleaning agent to be injected into the feed water is preferably an acid or an alkali. As described above, by adjusting the pH of the feed water to 4 to 6 by adding an acid, the prefilter 2 or the degassing membrane module has already been used. 3 to dissolve and remove the inorganic substances adhering to the degassing membrane 3 and prevent the inorganic substances from adhering to the degassing membrane of the prefilter 2 and the degassing membrane module 3 to prevent contamination by the inorganic substances. it can.
この場合、添加する酸としては、塩酸（ＨＣｌ）、硫酸（Ｈ２ＳＯ４）、リン酸（Ｈ３ＰＯ４）等の鉱酸や、クエン酸、リンゴ酸等の有機酸を用いることができ、これらは１種を単独で用いても良く、２種以上を併用しても良い。 In this case, as the acid to be added, a mineral acid such as hydrochloric acid (HCl), sulfuric acid (H 2 SO 4 ), phosphoric acid (H 3 PO 4 ), or an organic acid such as citric acid or malic acid can be used. These may be used alone or in combination of two or more.
また、アルカリを添加して給水のｐＨを１０〜１２に調整することにより、既にプレフィルタ２や脱気膜モジュール３の脱気膜に付着した有機物を溶解させて除去すると共に、プレフィルタ２や脱気膜モジュール３の脱気膜へのこれらの有機物の付着を防止して、有機物による汚染を防止することができる。 Further, by adjusting the pH of the feed water to 10 to 12 by adding alkali, the organic substances already attached to the prefilter 2 and the degassing membrane of the degassing membrane module 3 are dissolved and removed, and the prefilter 2 and By preventing these organic substances from adhering to the degassing membrane of the degassing membrane module 3, contamination by the organic materials can be prevented.
この場合、添加するアルカリとしては、水酸化ナトリウム（ＮａＯＨ）、水酸化カリウム（ＫＯＨ）等のアルカリ性物質を用いることができ、これらは１種を単独で用いても良く、２種以上を併用しても良い。 In this case, as the alkali to be added, alkaline substances such as sodium hydroxide (NaOH) and potassium hydroxide (KOH) can be used, and these may be used alone or in combination of two or more. May be.
本発明において、酸又はアルカリは、連続注入であっても良く、間欠注入であっても良い。間欠注入の場合、連続運転している膜脱気装置の給水に対して、１日に１〜１０回、１回当たり１〜１０分程度酸又はアルカリを注入し、全通水時間のうちの０．１〜１０％程度の時間について、給水のｐＨを４〜６又は１０〜１２に調整することが好ましい。 In the present invention, the acid or alkali may be continuous injection or intermittent injection. In the case of intermittent injection, acid or alkali is injected 1 to 10 times a day for 1 to 10 minutes per time for the water supply of the membrane deaerator that is continuously operated. For a time of about 0.1 to 10%, it is preferable to adjust the pH of the feed water to 4 to 6 or 10 to 12.
なお、通常、ボイラ給水のｐＨは５．８〜９．５の範囲であることが好ましいが、上述の如く、酸又はアルカリの間欠注入で洗浄操作中の給水のｐＨが上記好適ｐＨ範囲から外れても、洗浄操作を行っていないときの脱気処理水により洗浄操作中の脱気処理水が給水タンク５内で希釈されるため、ｐＨの変動が問題となることはない。ただし、給水タンク５内のｐＨが上記好適ｐＨから外れる場合には、給水タンク５内に酸又はアルカリを添加してｐＨ調整を行っても良い。 Normally, the pH of boiler feed water is preferably in the range of 5.8 to 9.5. However, as described above, the pH of the feed water during the cleaning operation by intermittent injection of acid or alkali is out of the preferred pH range. However, since the degassed water during the washing operation is diluted in the water supply tank 5 by the degassed water when the washing operation is not performed, fluctuations in pH do not become a problem. However, when the pH in the water supply tank 5 deviates from the above-mentioned preferred pH, the pH may be adjusted by adding acid or alkali to the water supply tank 5.
本発明においては、有機物又は無機物による汚染を共に防止するために、酸の注入による洗浄操作とアルカリの注入による洗浄操作を適宜組み合わせて行うことが好ましい。 In the present invention, in order to prevent both contamination by organic substances or inorganic substances, it is preferable to carry out an appropriate combination of washing operation by injecting acid and washing operation by injecting alkali.
この場合には、例えば、酸を注入して給水のｐＨを１〜１０分間にわたって、４〜６とする酸洗浄操作と、アルカリを注入して給水のｐＨを１〜１０分間にわたって１０〜１２とするアルカリ洗浄操作とを、交互に各洗浄操作との間の時間間隔が６〜１２時間程度となるように、各々１日に１〜４回程度行い、全通水時間に対する酸洗浄操作時間が０．５〜２．０％程度、アルカリ洗浄時間が０．５〜２．０％程度となるように洗浄操作を組み入れることが好ましい。この場合においても、酸洗浄操作時の脱気処理水とアルカリ洗浄操作時の脱気処理水とが給水タンク５内で非洗浄操作時の脱気処理水と混合されることで、ボイラへのｐＨの影響は防止される。 In this case, for example, an acid washing operation in which an acid is injected to adjust the pH of the feed water to 4 to 6 over 1 to 10 minutes, and an alkali is injected to adjust the pH of the feed water to 10 to 12 over 1 to 10 minutes. The alkaline cleaning operation is alternately performed about 1 to 4 times a day so that the time interval between the respective cleaning operations is about 6 to 12 hours. It is preferable to incorporate the washing operation so that the alkali washing time is about 0.5 to 2.0%. Even in this case, the degassed water at the time of the acid cleaning operation and the degassed water at the time of the alkali cleaning operation are mixed with the degassed water at the time of the non-cleaning operation in the water supply tank 5, thereby The effect of pH is prevented.
なお、このように給水タンクにおいて、ｐＨを安定化させるために、給水タンク内の水の滞留時間が１〜２時間程度となるように、給水タンクの容量設計を行うことが好ましい。 In order to stabilize pH in the water supply tank, it is preferable to design the capacity of the water supply tank so that the residence time of water in the water supply tank is about 1 to 2 hours.
また、脱気膜の洗浄によって溶出した無機物又は有機物の量によってボイラ缶内でのスケール化、スラッジ化が懸念される場合は、給水タンクの後段にフィルターを設けても良いし、分散剤等の薬品を添加しても良い。 Also, if there is a concern about scaling or sludge generation in the boiler can due to the amount of inorganic or organic substances eluted by washing the degassing membrane, a filter may be provided after the water supply tank, Chemicals may be added.
このような本発明の膜脱気装置の洗浄方法によれば、図１に示す如く、脱気膜モジュール３の入口側にプレフィルタ２を設けた場合において、プレフィルタ２、更には脱気膜モジュール３の汚染を防止して、プレフィルタ２の交換頻度を大幅に低減することができるが、本発明の方法はプレフィルタを設けていない脱気膜モジュールであっても有効に適用することができ、また、プレフィルタの代りにＭＦ膜モジュールを設けた脱気膜モジュールであっても良好な洗浄効果で脱気膜モジュールの薬品洗浄頻度の低減ないしはＭＦ膜モジュールの逆洗間隔の延長を図ることができる。 According to the cleaning method of the membrane deaerator of the present invention, as shown in FIG. 1, when the prefilter 2 is provided on the inlet side of the deaeration membrane module 3, the prefilter 2 and further the deaeration membrane are provided. Although the contamination of the module 3 can be prevented and the replacement frequency of the prefilter 2 can be greatly reduced, the method of the present invention can be effectively applied even to a degassing membrane module without a prefilter. In addition, even in the case of a degassing membrane module provided with an MF membrane module instead of a prefilter, the chemical cleaning frequency of the degassing membrane module can be reduced or the backwashing interval of the MF membrane module can be extended with a good cleaning effect. be able to.
以下に実施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.
実施例１（有機物の洗浄除去及び付着防止）
脱気膜モジュールの前段にプレフィルタを設けた膜脱気装置において、ｐＨ７．５、水温５０〜６５℃の給水を通水量８〜６ｔ／ｈｒで処理した場合、差圧０．１ＭＰａにおけるプレフィルタの交換頻度は２週間に１回であった。
Example 1 (Removal of organic substances and prevention of adhesion)
In a membrane deaerator provided with a pre-filter in the previous stage of the deaeration membrane module, when the feed water having a pH of 7.5 and a water temperature of 50 to 65 ° C. is treated at a water flow rate of 8 to 6 t / hr, the pre-filter at a differential pressure of 0.1 MPa The exchange frequency of was once every two weeks.
この膜脱気装置の給水に、タイマー制御により、２５重量％ＮａＯＨ水溶液を１回につき５分間、２０ｍＬ／分で注入して給水のｐＨを１０．５程度に調整する洗浄操作を１日に１回行った。 A cleaning operation for adjusting the pH of the feed water to about 10.5 by injecting a 25 wt% NaOH aqueous solution at a rate of 20 mL / min to the feed water of this membrane deaerator for 5 minutes at a time by a timer control is performed once a day. I went twice.
その結果、差圧０．１ＭＰａにおけるプレフィルタの交換頻度は８週間に１回となり、プレフィルタの交換頻度は大幅に低減した。 As a result, the replacement frequency of the prefilter at a differential pressure of 0.1 MPa was once every 8 weeks, and the replacement frequency of the prefilter was greatly reduced.
実施例２（無機物の洗浄除去及び付着防止）
脱気膜モジュールの前段にプレフィルタを設け、ｐＨ７．５、水温１０〜２５℃の給水を通水量７〜１０ｔ／ｈｒで処理している膜脱気装置において、７５重量％Ｈ２ＳＯ４水溶液をｐＨ測定器と制御器を用いて、給水のｐＨが５．０となるように連続的に注入したところ、ｐＨ７．５の給水を連続通水している場合に比べて、単位面積当たりのプレフィルタの無機物（酸化鉄、酸化アルミニウム等）付着量は約１／３に低減された。
Example 2 (Inorganic removal and adhesion prevention)
In a membrane degassing apparatus in which a prefilter is provided in the front stage of the degassing membrane module and the feed water having a pH of 7.5 and a water temperature of 10 to 25 ° C. is treated at a flow rate of 7 to 10 t / hr, a 75 wt% H 2 SO 4 aqueous solution Using a pH meter and a controller, the feed water was continuously injected so that the pH of the feed water was 5.0, and compared with the case where the feed water of pH 7.5 was continuously passed, The amount of inorganic matter (iron oxide, aluminum oxide, etc.) deposited on the prefilter was reduced to about 1/3.
実施例３（有機物及び無機物の洗浄除去及び付着防止）
脱気膜モジュールの前段にプレフィルタを設け、ｐＨ７．５、水温１５〜４０℃の給水を通水量３〜５ｔ／ｈｒで処理し、０．１ＭＰａでのプレフィルタの交換頻度が１週間に１回の膜脱気装置において、以下の酸洗浄操作とアルカリ洗浄操作とを交互に行った。
Example 3 (Cleaning and removal of organic and inorganic substances and prevention of adhesion)
A pre-filter is provided in the front stage of the deaeration membrane module, water supply at pH 7.5 and a water temperature of 15 to 40 ° C. is processed at a water flow rate of 3 to 5 t / hr, and the pre-filter replacement frequency at 0.1 MPa is 1 per week. The following acid cleaning operation and alkali cleaning operation were alternately performed in a single membrane degassing apparatus.
［酸洗浄操作］
７５重量％Ｈ２ＳＯ４水溶液を、１回につき１０分間、７ｍＬ／分で注入して給水のｐＨを４程度に調整する。
［アルカリ洗浄操作］
２５重量％ＮａＯＨ水溶液を１回につき１０分間、３０ｍＬ／分で注入して給水のｐＨを１１程度に調整する。
[Acid cleaning operation]
A 75 wt% H 2 SO 4 aqueous solution is injected at a rate of 7 mL / min for 10 minutes at a time to adjust the pH of the feed water to about 4.
[Alkaline washing operation]
A 25 wt% NaOH aqueous solution is injected at a rate of 30 mL / min for 10 minutes at a time to adjust the pH of the feed water to about 11.
上記酸洗浄操作とアルカリ洗浄操作とは、各々１日に１回の頻度で行い、酸洗浄操作とアルカリ洗浄操作との間には１２時間の時間間隔を設けた。 The acid cleaning operation and the alkali cleaning operation were each performed once a day, and a time interval of 12 hours was provided between the acid cleaning operation and the alkali cleaning operation.
その結果、差圧０．１ＭＰａにおけるプレフィルタの交換頻度は４週間に１回となり、プレフィルタの交換頻度は大幅に低減した。 As a result, the replacement frequency of the prefilter at a differential pressure of 0.1 MPa was once every four weeks, and the replacement frequency of the prefilter was greatly reduced.
１ 軟水器
２ プレフィルタ
３ 脱気膜モジュール
４ 真空ポンプ
５ 給水タンク
６ 薬品タンク
７ タイマー
８ ｐＨ測定器
９ 制御器
DESCRIPTION OF SYMBOLS 1 Water softener 2 Pre filter 3
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| JP2010185117A (en) * | 2009-02-13 | 2010-08-26 | Ebara Corp | Plating equipment and plating method |
| JP2011255010A (en) * | 2010-06-09 | 2011-12-22 | Chugoku Electric Power Co Inc:The | Method of de-toxifying pcb mixed-in insulating oil and storage method for the same |
| WO2012147534A1 (en) * | 2011-04-25 | 2012-11-01 | 日本碍子株式会社 | Method for washing ceramic filter |
| JP2013202475A (en) * | 2012-03-28 | 2013-10-07 | Sumitomo Metal Mining Engineering Co Ltd | Method of removing ammonia from ammonia-containing wastewater |
| CN105905969A (en) * | 2016-05-16 | 2016-08-31 | 扬州大学 | Pressure reduction and gas release device |
| WO2020209036A1 (en) * | 2019-04-10 | 2020-10-15 | 野村マイクロ・サイエンス株式会社 | Method for cleaning membrane degassing devices and system for producing ultrapure water |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JP2010185117A (en) * | 2009-02-13 | 2010-08-26 | Ebara Corp | Plating equipment and plating method |
| JP2011255010A (en) * | 2010-06-09 | 2011-12-22 | Chugoku Electric Power Co Inc:The | Method of de-toxifying pcb mixed-in insulating oil and storage method for the same |
| WO2012147534A1 (en) * | 2011-04-25 | 2012-11-01 | 日本碍子株式会社 | Method for washing ceramic filter |
| JP6060074B2 (en) * | 2011-04-25 | 2017-01-11 | 日本碍子株式会社 | Cleaning method of ceramic filter |
| US10166512B2 (en) | 2011-04-25 | 2019-01-01 | Ngk Insulators, Ltd. | Method for cleaning ceramic filter |
| JP2013202475A (en) * | 2012-03-28 | 2013-10-07 | Sumitomo Metal Mining Engineering Co Ltd | Method of removing ammonia from ammonia-containing wastewater |
| CN105905969A (en) * | 2016-05-16 | 2016-08-31 | 扬州大学 | Pressure reduction and gas release device |
| WO2020209036A1 (en) * | 2019-04-10 | 2020-10-15 | 野村マイクロ・サイエンス株式会社 | Method for cleaning membrane degassing devices and system for producing ultrapure water |
| JP2020171883A (en) * | 2019-04-10 | 2020-10-22 | 野村マイクロ・サイエンス株式会社 | Washing method of membrane degasifier and ultrapure water production system |
| JP7236313B2 (en) | 2019-04-10 | 2023-03-09 | 野村マイクロ・サイエンス株式会社 | Membrane deaerator cleaning method and ultrapure water production system |
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