JP2008221178A - Cleaning method of hollow fiber membrane module - Google Patents
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本発明は中空糸膜モジュールの洗浄方法に関する。 The present invention relates to a method for cleaning a hollow fiber membrane module.
近年、中空糸膜による分離技術の開発が進み、水の濾過をはじめ様々な用途に広く用いられている。しかし、中空糸膜による濾過の過程では、SSと呼ばれる原液中の懸濁物質等の固形物が中空糸膜表面に付着し、又は微多孔に侵入し、経時的に透過流束の低下が生じる。そこで、安定して長期的に濾過運転を継続するためには、濾過条件の設定と同時に有効な中空糸膜の洗浄方法の開発が不可欠とされている。 In recent years, the development of separation technology using hollow fiber membranes has progressed, and it is widely used for various applications including water filtration. However, in the process of filtration with a hollow fiber membrane, solid matter such as suspended solids in a stock solution called SS adheres to the surface of the hollow fiber membrane or penetrates into the micropores, and the permeation flux decreases with time. . Therefore, in order to continue the filtration operation stably for a long time, it is indispensable to develop a method for cleaning the hollow fiber membrane that is effective at the same time as setting the filtration conditions.
従来、中空糸膜モジュールの洗浄方法として、種々の方法が検討されてきたが、これらは物理的洗浄方法と、化学的洗浄方法とに大別できる。物理的洗浄方法としては、スポンジボール、高圧水流などにより強制的に付着物質をかき取る方法、水、透過液などの液体を濾液側から原液側へ通過させる液体逆洗法、加圧気体を濾液側から原液側へ通過させる気体逆洗法(例えば、特許文献1および2 参照)、中空糸膜の原液側から気体が放出される圧力よりも小さい圧力の気体を濾液側から導入する加圧操作、原液側に気泡を噴出させるバブリング法、超音波法、電気泳動法などをはじめ、多種多様の方法が提案されている。また、化学的洗浄方法としては、酸、アルカリ水溶液、洗浄剤などの薬液により、付着物を溶解除去する方法が知られている。 Conventionally, various methods have been studied as a method for cleaning a hollow fiber membrane module, and these can be roughly classified into a physical cleaning method and a chemical cleaning method. Physical cleaning methods include a method of forcibly removing adhering substances with a sponge ball, high-pressure water flow, etc., a liquid back-washing method in which liquid such as water and permeate is passed from the filtrate side to the stock solution side, and pressurized gas as filtrate. Gas back-washing method (for example, refer to Patent Documents 1 and 2) passing from the side to the stock solution side, pressurizing operation for introducing a gas having a pressure smaller than the pressure at which the gas is released from the stock solution side of the hollow fiber membrane from the filtrate side A wide variety of methods have been proposed, including a bubbling method in which bubbles are ejected to the stock solution side, an ultrasonic method, and an electrophoresis method. As a chemical cleaning method, a method of dissolving and removing deposits with a chemical solution such as an acid, an aqueous alkali solution, or a cleaning agent is known.
これらの方法の中で、原液が中空糸膜の外表面から供給され、中空糸膜の内表面側から濾液が取り出される外圧濾過方式の物理洗浄方法としては、原液側に気泡を噴出させるバブリング法が広く採用されている。また、バブリング法と液体逆洗法、気体逆洗法、加圧操作などとを組み合わせて実施されることもある。特に中空糸膜の原液側から気体が放出される圧力よりも小さい圧力の気体を濾液側から導入する加圧操作を行った後にバブリングを実施する方法は、長期間安定的に連続した濾過運転を可能にする有効な物理洗浄方法である(例えば、特許文献3 参照)。 Among these methods, the stock solution is supplied from the outer surface of the hollow fiber membrane, and the physical washing method of the external pressure filtration method in which the filtrate is taken out from the inner surface side of the hollow fiber membrane is a bubbling method in which bubbles are ejected to the stock solution side. Is widely adopted. Further, the bubbling method, the liquid backwashing method, the gas backwashing method, the pressurizing operation and the like may be performed in combination. In particular, the method of carrying out the bubbling after performing the pressurizing operation for introducing a gas having a pressure smaller than the pressure at which the gas is released from the raw solution side of the hollow fiber membrane from the filtrate side is a continuous filtration operation for a long period of time. This is an effective physical cleaning method that enables it (see, for example, Patent Document 3).
しかし、この洗浄方法を、原液が中空糸膜の外表面から供給され、中空糸膜の内表面側から濾液が取り出される外圧濾過方式に利用して中空糸膜濾過装置の運転を行った場合に、中空糸膜束に経時的に捻れや絡みが生じ、これが徐々に激しくなり洗浄効率の低下を招き、最終的には中空糸膜の濾過性能を低下させる可能性があることが判明した。また、捻れや絡みに起因する、中空糸膜同士の擦れによる膜損傷を発生させる可能性があることも判明した。 However, when the hollow fiber membrane filtration apparatus is operated by using this cleaning method for the external pressure filtration method in which the stock solution is supplied from the outer surface of the hollow fiber membrane and the filtrate is taken out from the inner surface side of the hollow fiber membrane. It has been found that twists and entanglements occur in the hollow fiber membrane bundle over time, which gradually becomes severe, leading to a reduction in cleaning efficiency, and ultimately possibly reducing the filtration performance of the hollow fiber membrane. It has also been found that there is a possibility of causing membrane damage due to rubbing between hollow fiber membranes due to twisting and entanglement.
本発明者らは既に、濾液側からの加圧操作後に圧力を開放し、その後バブリングを実施することで、上記方法を行うことに起因した経時的な捻れや絡みによる中空糸膜の性能低下を防ぐことが可能であることを提案した(例えば、特許文献4 参照)。この濾液側からの加圧操作時に濾液側から原液側に移動してくる液体又は気体は濾過容器側面の気体排出口から排出されていた。 The present inventors have already released the pressure after the pressurizing operation from the filtrate side, and then carried out bubbling, thereby reducing the performance of the hollow fiber membrane due to twisting and entanglement over time due to performing the above method. It was proposed that this can be prevented (see, for example, Patent Document 4). During the pressurizing operation from the filtrate side, the liquid or gas moving from the filtrate side to the stock solution side was discharged from the gas discharge port on the side surface of the filtration container.
この発明に関連する先行技術文献としては次のものがある。
しかしこの方法を、原液が中空糸膜の外表面側すなわち原水側に供給され、中空糸膜の内表面側すなわち濾過側から濾液が取り出される外圧濾過方式の中空糸膜モジュールの洗浄を行う場合に、これら液体は濾過容器側面の気体排出口から一気に流出するが、このときのモジュール内液体の流れに影響を受け、中空糸膜に激しい捻れや絡み現象が発生することが判明した。ここで発現した捻れや絡みは、中空糸膜洗浄効率低下の一要因となるほか、中空糸膜同士の擦れを起こし、中空糸膜損傷の要因となることも判明した。 However, this method is used when cleaning the external pressure filtration type hollow fiber membrane module in which the stock solution is supplied to the outer surface side of the hollow fiber membrane, that is, the raw water side, and the filtrate is taken out from the inner surface side of the hollow fiber membrane, that is, the filtration side. These liquids flowed out from the gas outlet on the side of the filtration container at once, but it was found that the twisted and entangled phenomenon occurred in the hollow fiber membrane due to the influence of the liquid flow in the module at this time. It was also found that the twists and entanglements expressed here cause the hollow fiber membranes to be rubbed against each other, and cause damage to the hollow fiber membranes.
本発明は、上記の課題を解決するためになされたもので、濾液側からの加圧操作時に生じる中空糸膜捻れや絡みに起因する中空糸膜束の洗浄不良および中空糸膜損傷を低減した中空糸膜モジュールの洗浄方法を提供することにある。 The present invention has been made to solve the above-described problems, and has reduced the poor cleaning of the hollow fiber membrane bundle and the hollow fiber membrane damage caused by the twisting and entanglement of the hollow fiber membranes that occur during the pressurizing operation from the filtrate side. It is providing the washing | cleaning method of a hollow fiber membrane module.
上記の課題を解決する本発明の中空糸膜モジュールの洗浄方法は、中空糸膜の外表面から原液が供給され、中空糸膜の内表面側から濾液が取り出される外圧濾過方式で使用される中空糸膜モジュールの洗浄方法であって、中空糸膜の原液側に液体を満たした状態で、中空糸膜の濾液側を加圧することにより液体又は気体を原液側に排出する間に、原液側の液体又は気体を中空糸膜の下部に設けた原液排出口より排出する中空糸膜モジュールの洗浄方法である。 The method for cleaning a hollow fiber membrane module of the present invention that solves the above problems is a hollow fiber used in an external pressure filtration system in which a stock solution is supplied from the outer surface of the hollow fiber membrane and the filtrate is taken out from the inner surface side of the hollow fiber membrane. A method for cleaning a thread membrane module, in which the liquid side of the hollow fiber membrane is filled with liquid and the liquid side or gas is discharged to the stock side by pressurizing the filtrate side of the hollow fiber membrane. This is a method for cleaning a hollow fiber membrane module in which liquid or gas is discharged from a stock solution discharge port provided at the bottom of the hollow fiber membrane.
本発明において、中空糸膜の下部に設けた原液排出口からの排出のためのバルブ開放は、濾液側からの加圧気体の導入と同時に行うことが好ましく、その開放は加圧気体の注入終了まで持続させることが好ましい。 In the present invention, the valve opening for discharging from the stock solution outlet provided in the lower part of the hollow fiber membrane is preferably performed simultaneously with the introduction of the pressurized gas from the filtrate side, and the opening is completed when the injection of the pressurized gas is completed. It is preferable to continue to
本発明の中空糸膜モジュールの洗浄方法によって、中空糸膜モジュール濾液側への気体加圧による中空糸膜捻れや絡みに起因する中空糸膜の洗浄不良を低減することが可能となり、中空糸膜へのSS付着による負荷を軽減することが可能となるとともに、中空糸膜同士の擦れによる膜損傷を軽減することが可能となる。 According to the method for cleaning a hollow fiber membrane module of the present invention, it becomes possible to reduce poor cleaning of the hollow fiber membrane due to twisting or entanglement of the hollow fiber membrane due to gas pressurization to the filtrate side of the hollow fiber membrane module. It is possible to reduce the load caused by the adhesion of SS to the membrane and to reduce membrane damage caused by rubbing between the hollow fiber membranes.
以下に本発明の実施態様の一例を、図面を用いて説明する。図1は本発明の中空糸膜モジュールの洗浄方法を行うために使用することができる外圧型中空糸膜モジュールの一例の概略図である。この中空糸膜モジュールにおいて、中空糸膜エレメント4が収納された濾過容器1は、上部が濾液側A、下部が原液側Bになるように仕切板2によって仕切られている。濾液側Aには濾液出口5および加圧気体導入口6が設けられており、原液側Bには原液導入口7、気体排出口8、気体導入口9および原液排出口10が設けられている。
Hereinafter, an example of an embodiment of the present invention will be described with reference to the drawings. FIG. 1 is a schematic view of an example of an external pressure type hollow fiber membrane module that can be used for performing the method for cleaning a hollow fiber membrane module of the present invention. In this hollow fiber membrane module, the filtration container 1 in which the hollow fiber membrane element 4 is housed is partitioned by a partition plate 2 so that the upper part is the filtrate side A and the lower part is the stock solution side B. The filtrate side A is provided with a
図2には、図1に示す中空糸膜モジュールを使用した、外圧全濾過方式の中空糸膜モジュールの概略構成を示す。図2にしたがって本発明を適用した中空糸膜モジュールの運転方法の一例を説明する。全てのバルブを閉じた状態から、気体排出口バルブ24、原液導入口バルブ21を開き、送液ポンプを作動させて濾過容器25の原液側Eに原液を導入し、気体排出口バルブ24から原液が溢れた後、濾液出口バルブ23を開け、かつ気体排出口バルブ24を閉じて濾過を開始する。濾過時間の経過に伴い中空糸膜エレメント26の膜表面にはSS成分が付着し、濾過能力が低下するため、続いて本発明の方法により中空糸膜モジュールを洗浄する。すなわち、送液ポンプを停止した後、濾過工程で開いている原液導入口バルブ21および濾液出口バルブ23を閉じて濾過を停止し、次いでエアーコンプレッサー29を作動させながら加圧気体導入口バルブ22を開くと同時に、気体排出口バルブ24ではなく、原液排出口バルブ27を開く。そして、中空糸膜の濾液側Dに導入された加圧気体が中空糸膜を通過して原液側Eに抜けるのに必要な加圧気体の圧力(以下、この圧力のことを「バブルポイント」と呼ぶ。)よりも小さい圧力の加圧気体を濾過容器25の濾液側Dに導入して加圧工程を行う。この加圧操作により中空糸膜の壁面を通じて原液側に押し出された中空糸膜内の濾液および濾過容器25内液が、原液排出口バルブ27より外部へ排出される。以上の加圧工程を所定時間行った後、加圧気体導入口バルブ22と原液排出口バルブ27を閉じ、その後気体排出口バルブ24と濾液バルブ23を開いて濾液側Dの加圧状態を開放し、所定の時間経過させた後、濾液バルブ23を閉じて濾液側Dで気体及び液体の移動が生じない状態にして、原液導入口バルブ21を開き、送液ポンプを作動させ濾過容器25内を原液で満たす。気体排出口バルブ24より原液が溢れ出る頃に送液ポンプを停止させ、原液導入口バルブ21を閉め、次に気体導入口バルブ28を開けることにより、バブリング洗浄を所定時間行う。上述した洗浄工程終了後、気体導入バルブ28を閉じ、原液排出口バルブ27を開いてドレンを排出した後、濾過工程へ戻る。
FIG. 2 shows a schematic configuration of a hollow fiber membrane module of the external pressure total filtration system using the hollow fiber membrane module shown in FIG. An example of a method for operating the hollow fiber membrane module to which the present invention is applied will be described with reference to FIG. From a state in which all the valves are closed, the gas
本発明において、中空糸膜モジュールの濾液側加圧時に原液排出口バルブを開けた状態では、濾液側と原液側との間で気体の移動は理想的には起こらないはずだが、実際は、中空糸膜仕切板のシール不良、中空糸膜リークなどにより気体の移動が起こる場合がある。この時、濾過容器原液側の水面は低下し、場合によっては液体全てが排出する可能性があり、この状態ではこの後の工程のバブリング洗浄の効果を損なうことが考えられるため、バブリング洗浄を実施する直前に原液排出口バルブを閉じ、原液導入口バルブ及び気体排出口バルブを開け、濾過容器内を原液で満たしておく必要がある。この、濾過容器を原液で満たすために原液導入口バルブを開けておく時間は、運転工程のうち充水工程で設定している時間と同等であることが好ましい。 In the present invention, in the state where the stock solution outlet valve is opened at the time of pressurizing the filtrate side of the hollow fiber membrane module, gas movement should not ideally occur between the filtrate side and the stock solution side. Gas migration may occur due to poor sealing of the membrane partition plate, hollow fiber membrane leakage, or the like. At this time, the water surface of the filtration container undiluted solution side is lowered, and in some cases, all the liquid may be discharged. In this state, the bubbling washing effect of the subsequent process may be impaired, so the bubbling washing is performed. It is necessary to close the stock solution outlet valve immediately before opening, open the stock solution inlet valve and gas exhaust port valve, and fill the filtration container with the stock solution. The time during which the stock solution inlet valve is opened to fill the filtration container with the stock solution is preferably equal to the time set in the water filling step in the operation process.
本発明において、加圧状態を開放し、次いで濾液側を閉鎖する操作をした後、中空糸膜モジュールの原液側に気体を導入してバブリング洗浄を行う際の気体の供給量は特に限定されないが、膜洗浄効果が高く、膜破損のおそれが小さいことから、中空糸膜の有効膜面積1m2あたり10〜500NL/hrの範囲内であることが好ましく、20〜300NL/hrの範囲内であることがより好ましい。またバブリング洗浄を実施する時間としては、5〜120秒間の範囲内であることが好ましく、20〜60秒間の範囲内であることがより好ましい。 In the present invention, the amount of gas supply when performing bubbling washing by introducing gas into the stock solution side of the hollow fiber membrane module after opening the pressurized state and then closing the filtrate side is not particularly limited. Since the membrane cleaning effect is high and the risk of membrane damage is small, it is preferably within the range of 10 to 500 NL / hr per 1 m 2 of the effective membrane area of the hollow fiber membrane, and within the range of 20 to 300 NL / hr. It is more preferable. Further, the time for carrying out the bubbling cleaning is preferably within a range of 5 to 120 seconds, and more preferably within a range of 20 to 60 seconds.
本発明において、中空糸膜の濾液側に加圧気体を注入する加圧工程およびバブリング操作を行うときに用いる気体としては、空気、窒素などが挙げられる。加圧工程で注入する気体の圧力としては、中空糸膜の素材、孔径および中空糸膜を気体が通過する圧力などに応じて設定する必要があるが、例えば親水化処理されたポリスルホン系樹脂からなり、平均孔径0.1μmの中空糸膜を使用して、バブルポイントよりも小さい圧力の気体を注入する加圧操作を行う場合には、圧力0.1〜0.3MPa範囲内であることが好ましく、加圧操作を実施する時間は、1〜60秒間の範囲内であることが好ましく、5〜30秒間の範囲内であることがより好ましい。 In the present invention, examples of the gas used when performing a pressurizing step for injecting a pressurized gas into the filtrate side of the hollow fiber membrane and a bubbling operation include air and nitrogen. As the pressure of the gas injected in the pressurizing step, it is necessary to set according to the material of the hollow fiber membrane, the pore diameter, the pressure at which the gas passes through the hollow fiber membrane, etc., for example, from a polysulfone resin hydrophilized Thus, when performing a pressurizing operation for injecting a gas having a pressure smaller than the bubble point using a hollow fiber membrane having an average pore diameter of 0.1 μm, the pressure may be within a range of 0.1 to 0.3 MPa. Preferably, the time for performing the pressurizing operation is preferably within a range of 1 to 60 seconds, and more preferably within a range of 5 to 30 seconds.
本発明で使用される中空糸膜としては、ポリビニルアルコール系樹脂により親水化処理されたポリスルホン系樹脂、親水性高分子が添加されたポリスルホン系樹脂、ポリビニルアルコール系樹脂、ポリアクリロニトリル系樹脂、酢酸セルロース系樹脂、親水化処理されたポリエチレン系樹脂などの親水性素材からなるものが、高い親水性を有するためにSS成分の難付着性、付着したSS成分の剥離性に優れている点で好ましいが、他の素材で構成された中空糸膜を用いることもできる。例えば、ポリオレフィン系、ポリスルホン系、ポリエーテルスルホン系、エチレンービニルアルコール共重合体系、ポリアクリロニトリル系、酢酸セルロース系、ポリフッ化ビニリデン系、ポリパーフルオロエチレン系、ポリメタクリル酸エステル系、ポリエステル系、ポリアミド系などの有機高分子系の素材で構成された中空糸膜、セラミック系などの無機系の素材で構成された中空糸膜などを使用条件、所望する濾過性能などに応じて選択することができる。ここで、ポリビニルアルコール系樹脂により親水化処理されたポリスルホン系樹脂、親水性高分子が添加されたポリスルホン系樹脂又はポリビニルアルコール系樹脂からなる中空糸膜は、上記した親水性に優れるのみならず、耐熱性にも優れることから、特に好ましい。有機高分子系の素材を使用する場合、30モル%以内の量で他成分を共重合したもの、又は30重量%以内の量で他の素材をブレンドしたものであってもよい。 The hollow fiber membrane used in the present invention includes polysulfone resin hydrophilized with polyvinyl alcohol resin, polysulfone resin to which hydrophilic polymer is added, polyvinyl alcohol resin, polyacrylonitrile resin, cellulose acetate. It is preferable in that it is made of a hydrophilic material such as a polyethylene resin or a hydrophilized polyethylene resin because it has high hydrophilicity and is excellent in the difficulty of SS component adhesion and exfoliation of the attached SS component. Hollow fiber membranes made of other materials can also be used. For example, polyolefin, polysulfone, polyethersulfone, ethylene-vinyl alcohol copolymer, polyacrylonitrile, cellulose acetate, polyvinylidene fluoride, polyperfluoroethylene, polymethacrylate, polyester, polyamide Hollow fiber membranes composed of organic polymer materials such as ceramics, hollow fiber membranes composed of inorganic materials such as ceramics can be selected according to the use conditions, desired filtration performance, etc. . Here, a polysulfone resin hydrophilized with a polyvinyl alcohol-based resin, a polysulfone-based resin to which a hydrophilic polymer is added, or a hollow fiber membrane made of a polyvinyl alcohol-based resin is not only excellent in the above-described hydrophilicity, Since it is excellent also in heat resistance, it is especially preferable. When an organic polymer material is used, it may be a copolymer obtained by copolymerizing other components in an amount of 30 mol% or less, or a blend of other materials in an amount of 30 wt% or less.
有機高分子系の中空糸膜を使用する場合、中空糸膜の製造方法は特に限定されることはなく、素材の特性および所望する中空糸膜性能に応じて、公知の方法から適宜選択した方法を採用することができる。一般的には溶融紡糸法、湿式紡糸法、乾湿式紡糸法などが採用される。また、透水性の観点から、中空糸膜は緻密層と支持層とを有する非対称構造を持つことが好ましいが、一般に溶融紡糸法により製造される中空糸膜は対称構造となることから、湿式紡糸法、乾湿式紡糸法などの相転換法により製造することが好ましい。 When an organic polymer hollow fiber membrane is used, the method for producing the hollow fiber membrane is not particularly limited, and a method appropriately selected from known methods depending on the characteristics of the material and the desired hollow fiber membrane performance Can be adopted. Generally, a melt spinning method, a wet spinning method, a dry / wet spinning method, or the like is employed. From the viewpoint of water permeability, the hollow fiber membrane preferably has an asymmetric structure having a dense layer and a support layer. However, since a hollow fiber membrane generally produced by a melt spinning method has a symmetrical structure, wet spinning is preferable. It is preferable to produce by a phase change method such as a method or a dry-wet spinning method.
本発明で使用される中空糸膜の孔径は特に限定されないが、0.001〜5μmの範囲内であることが、高い透水性を有し、濾過効率が低下するおそれが小さいことから好ましい。なお、ここでいう孔径とは、コロイダルシリカ、エマルジョン、ラテックスなどの粒子径が既知の各種基準物質を中空糸膜で濾過した際に、その90%が排除される基準物質の粒子径をいう。孔径は均一であることが好ましい。限外濾過膜であれば、上記のような基準物質の粒子径に基づいて、孔径を求めることは不可能であるが、分子量が既知の蛋白質を用いて同様の測定を行ったときに、分画分子量が3000以上であるものが好ましい。 The pore diameter of the hollow fiber membrane used in the present invention is not particularly limited, but it is preferably in the range of 0.001 to 5 μm because it has high water permeability and is less likely to reduce the filtration efficiency. Here, the pore diameter refers to the particle diameter of a reference material from which 90% is excluded when various reference substances with known particle diameters such as colloidal silica, emulsion, and latex are filtered through a hollow fiber membrane. The pore diameter is preferably uniform. With an ultrafiltration membrane, it is impossible to determine the pore size based on the particle size of the reference material as described above. However, when a similar measurement is performed using a protein with a known molecular weight, Those having a molecular weight of 3000 or more are preferred.
中空糸膜の力学的性質およびモジュールとしての膜面積の観点から、中空糸膜の外径は200〜3000μmの範囲内に設定することが好ましく、500〜2000μmの範囲内であることがより好ましい。同様に中空糸膜の厚さは50〜700μmの範囲内にあることが好ましく、100〜600μmの範囲内であることがより好ましい。 From the viewpoint of the mechanical properties of the hollow fiber membrane and the membrane area as a module, the outer diameter of the hollow fiber membrane is preferably set in the range of 200 to 3000 μm, and more preferably in the range of 500 to 2000 μm. Similarly, the thickness of the hollow fiber membrane is preferably in the range of 50 to 700 μm, and more preferably in the range of 100 to 600 μm.
本発明において、該中空糸膜はモジュール化されて濾過に使用される。濾過方法、濾過条件、洗浄方法などに応じてモジュールの形態を適宜選択することができ、1本又は複数本の中空糸膜エレメントを装着して中空糸膜モジュールを構成しても良い。モジュールの形態としては、例えば、数十本から数十万本の中空糸膜を束ねてモジュール内でU字型にしたもの、中空糸膜束の一端を適当なシール材により一括封止したもの、中空糸膜束の一端を一括で固定し、もう一端は中空糸膜同士を固定しないフリー状態で端部を一本毎に封止した片端フリー型のもの、中空糸膜束の両端を開口したものなどが挙げられる。また、中空糸膜モジュールの形状も特に限定されることはなく、例えば円筒状であってもスクリーン状であってもよい。本発明の洗浄方法では、中空糸膜の捻じれや絡みやそれに伴う中空糸膜の損傷が少なく、高い膜表面洗浄効果が発現し、かつ剥離したSSの排出がきわめて容易であることから、中空糸膜束の一端特に下端をフリー状態とした片端フリー型の中空糸膜モジュールを用いることが特に好ましい。 In the present invention, the hollow fiber membrane is modularized and used for filtration. The form of the module can be appropriately selected according to the filtration method, filtration conditions, washing method, and the like, and a hollow fiber membrane module may be configured by mounting one or a plurality of hollow fiber membrane elements. As the form of the module, for example, several tens to hundreds of thousands of hollow fiber membranes are bundled into a U-shape in the module, and one end of the hollow fiber membrane bundle is collectively sealed with an appropriate sealing material , One end of the hollow fiber membrane bundle is fixed together, and the other end is a free state in which the hollow fiber membranes are not fixed to each other in a free state. And the like. Further, the shape of the hollow fiber membrane module is not particularly limited, and may be, for example, a cylindrical shape or a screen shape. In the cleaning method of the present invention, the hollow fiber membrane is twisted or entangled and the resulting damage to the hollow fiber membrane is small, a high membrane surface cleaning effect is exhibited, and the discharged SS can be discharged very easily. It is particularly preferable to use a one-end free type hollow fiber membrane module in which one end, particularly the lower end, of the yarn membrane bundle is free.
本発明において、中空糸膜は単数又は複数の中空糸膜エレメントに収納され、この中空糸膜エレメントは筐体内に固定されるが、固定の方法が特に限定されることはない。例えば中空糸膜エレメントを筐体に接着しても良く、筐体に金具などでカートリッジ型中空糸膜エレメントを固定しても良い。 In the present invention, the hollow fiber membrane is housed in one or a plurality of hollow fiber membrane elements, and the hollow fiber membrane elements are fixed in the housing, but the fixing method is not particularly limited. For example, the hollow fiber membrane element may be bonded to the housing, and the cartridge type hollow fiber membrane element may be fixed to the housing with a metal fitting or the like.
なお、本発明の中空糸膜モジュールの洗浄方法には、ドレン排出と満水とを繰り返して中空糸膜表面および中空糸膜モジュール内部の洗浄を行う工程、フラッシング洗浄工程など、必要に応じて他の工程を追加することも可能である。 The method for cleaning the hollow fiber membrane module of the present invention may include other steps such as a step of cleaning the surface of the hollow fiber membrane and the inside of the hollow fiber membrane module by repeating drain discharge and full water, and a flushing cleaning step, as required. It is also possible to add a process.
濾過後又は逆洗浄後に中空糸膜を薬液洗浄して、中空糸膜に付着した有機物、無機物などを溶解除去することもできる。ここで、薬液洗浄の方法としては、有機物、無機物などを除去するために水酸化ナトリウム水溶液などのアルカリで処理する方法、金属類を除去するために酸水溶液などの酸で処理する方法、洗浄剤で処理する方法、これらを組み合わせて連続的に行う方法などがあり、これによって中空糸膜の再生が可能である。 The hollow fiber membrane can be washed with a chemical solution after filtration or back washing to dissolve and remove organic substances, inorganic substances, etc. adhering to the hollow fiber membrane. Here, as a chemical cleaning method, a method of treating with an alkali such as an aqueous sodium hydroxide solution to remove organic substances, inorganic materials, a method of treating with an acid such as an acid aqueous solution to remove metals, and a cleaning agent There are a method of treating with, a method of continuously carrying out a combination of these, and the hollow fiber membrane can be regenerated.
これまでに述べてきた濾過工程、気体による加圧工程、気泡による洗浄工程、薬液洗浄工程などの一連の操作は、シーケンスコントロールを行うことにより自動的に行うようにすることができる。例えば一定時間濾過を行った後、気体による加圧および気泡による膜表面洗浄を1回ないし数回実施し、次いで、必要に応じて1回ないし数回水洗を行い、その後薬液洗浄を行うという一連の洗浄工程をシーケンスコントロールにより自動的かつ連続的に行い、濾過と中空糸膜および濾過ラインの洗浄工程とを交互に繰り返しながら長期間安定的に運転を継続することが可能である。また濾過工程と洗浄工程とをシーケンスコントロールにより連続的に繰り返し、目詰まりが大きくなった時点で手動により逆洗浄する、いわゆるセレクトスイッチ方式で長期間安定的に運転を継続することも可能である。 A series of operations such as the filtration step, the gas pressurization step, the bubble washing step, and the chemical solution washing step described so far can be automatically performed by performing sequence control. For example, after filtration for a certain period of time, pressurization with gas and cleaning of the membrane surface with bubbles are performed once or several times, followed by water washing once or several times as necessary, and then chemical solution cleaning. This washing process can be performed automatically and continuously by sequence control, and the operation can be continued stably for a long period of time while alternately repeating the filtration and the washing process of the hollow fiber membrane and the filtration line. It is also possible to continue the operation stably for a long period of time by a so-called select switch method in which the filtration step and the washing step are continuously repeated by sequence control, and the back washing is manually performed when clogging becomes large.
本発明の洗浄方法は、中空糸膜の原液側に液体を満たした状態で、中空糸膜の濾液側を中空糸膜のパブルポイントよりも小さい圧力の気体で加圧するときに洗浄効果が有効に発現されることから、従来知られている河川水、井水、湖沼水などの浄化用途をはじめ、極めて広範な用途で従来よりも高透過流束で長期間連続して安定的な濾過が可能である。例えば、食品工業分野では、原料水の除菌・除鉄・除マンガン、洗浄用水の除菌・微粒子除去、天然水の除菌・微粒子除去、醤油の除菌・精製、清酒の除菌・精製、食酢の除菌・精製、みりんの精製、調味液の除菌・精製、醸造オリからの製品回収、糖液の除菌・微粒子除去・精製、ハチミツの精製、酵素・蛋白質の精製・濃縮、発酵液の精製、チーズホエーからの蛋白質の回収精製、ミルクの濃縮による高蛋白乳の製造、水産加工排水からの蛋白質回収、魚肉蛋白の濃縮、肉加工廃棄物からの肉蛋白質の回収、豚の血液からの赤血球の分離、血液中のアルブミンとグロブリンの濃縮精製、大豆ホエーからの生理活性物質の回収・精製、大豆煮汁からの蛋白質回収、あぶらな蛋白の毒素除去と蛋白質濃縮、じゃがいもでんぷん工業廃水からの有用蛋白質の回収、天然色素の回収精製、各種酵素の回収精製、液体飲料の清澄化と除菌、柑橘類・リンゴペプチン液の濃縮、バクテリア細胞および代謝物質の回収による発酵液の精製などの用途で使用可能であり、医療分野では原料となる純水・超純水製造装置の前処理、洗浄用水のパイロジェン除去、注射用水製造、透析用水製造、透析液の精製、ワクチン・酵素・ビールス・核酸・蛋白質などの生理活性物質の分離・濃縮・精製、ホルモンの精製、人工血液の製造、多糖類の濃縮精製、病院手洗い水の除菌、手術器具洗浄水の除菌などの用途に使用可能であり、電子工業分野では、逆浸透膜の前処理、超純水のファイナルフィルター、超純水のユースポイントフィルター、超純水のユニット組み込みフィルター、洗浄水の微粒子除去、研磨排水の回収、ダイシング排水の回収などの用途で使用可能であり、化学工業分野では、塗料の濃縮・回収、油剤の分離・回収、エマルジョンの分離・回収、コロイドの分離・回収、微粉体の洗浄精製、洗浄水の微粒子除去、メッキ液の精製、電気透析の前処理などの用途で使用可能であり、水処理分野では、中水道のMLSS除去、排水の三次処理、排水の回収・再利用、原子力発電排水の精製、バクテリアの除去などの用途で使用可能であり、繊維・染色加工分野では、PVA糊抜き排水のクローズド化、繊維加工油剤の回収・再利用、洗毛排水からのラノリンの回収、絹糸加工排水からのセリシンの回収などの用途で使用可能であり、鉄鋼・機械加工分野では、バレル研磨排水の回収、バフ研磨排水の回収、圧延油排水処理、水溶性切削油排水処理、動植物油加工排水の処理、脱脂洗浄排水からのエマルジョン除去・洗浄剤回収、リンス水のエマルジョン除去・リンス水回収、スクリーン版洗浄剤からのインク類除去などの用途で使用することが可能であり、さらには蒸気ドレン回収、蓄熱槽を用いた冷暖房システムの熱冷媒水の浄化などの用途で使用可能である。 The cleaning method of the present invention is effective when the filtrate side of the hollow fiber membrane is pressurized with a gas having a pressure smaller than the puff point of the hollow fiber membrane in a state where the liquid side of the hollow fiber membrane is filled with liquid. Since it is expressed, stable filtration can be performed continuously for a long time with a higher permeation flux than ever before in a wide range of applications, including purification of river water, well water, lake water, etc. It is. For example, in the food industry, sterilization / iron removal / manganese removal of raw water, sterilization / fine particle removal of cleaning water, sterilization / fine particle removal of natural water, sterilization / purification of soy sauce, sterilization / purification of sake , Vinegar sterilization / purification, mirin purification, seasoning sterilization / purification, product recovery from brewing oil, sugar solution sterilization / fine particle removal / purification, honey purification, enzyme / protein purification / concentration, Purification of fermentation broth, recovery and purification of protein from cheese whey, production of high-protein milk by concentrating milk, recovery of protein from fishery processing wastewater, concentration of fish protein, recovery of meat protein from meat processing waste, pork Separation of red blood cells from blood, concentration and purification of albumin and globulin in blood, recovery and purification of physiologically active substances from soybean whey, recovery of protein from soybean juice, oil protein toxin removal and protein concentration, potato starch industrial wastewater from Used for applications such as protein recovery, natural pigment recovery and purification, various enzyme recovery and purification, clarification and sterilization of liquid beverages, concentration of citrus and apple peptin solutions, and purification of fermentation broth by recovery of bacterial cells and metabolites Yes, in the medical field, pretreatment of pure water and ultrapure water production equipment, cleaning water pyrogen removal, injection water production, dialysis water production, dialysate purification, vaccines, enzymes, viruses, nucleic acids, proteins It can be used for applications such as separation, concentration and purification of physiologically active substances such as hormone purification, artificial blood production, polysaccharide concentration and purification, hospital hand washing water sterilization, surgical instrument washing water sterilization, In the electronics industry, reverse osmosis membrane pretreatment, ultrapure water final filter, ultrapure water use point filter, ultrapure water unit built-in filter, cleaning water particulate removal, It can be used for applications such as polishing wastewater recovery and dicing wastewater recovery. In the chemical industry, paint concentration / recovery, oil agent separation / recovery, emulsion separation / recovery, colloid separation / recovery, fine powder It can be used for applications such as washing and purification, removal of washing water particulates, plating solution purification, and electrodialysis pretreatment. In the water treatment field, it removes MLSS from the waterworks, tertiary treatment of wastewater, and collection and reuse of wastewater. It can be used for applications such as purification of nuclear power generation wastewater and removal of bacteria. In the field of textile and dyeing processing, the closure of PVA desizing wastewater, recovery and reuse of textile processing oil, and the use of lanolin from hair washing wastewater. It can be used for purposes such as recovery and recovery of sericin from silk processing wastewater. In the steel and machining field, barrel polishing wastewater recovery, buffing wastewater recovery, rolling oil drainage treatment, water-soluble cutting Use for applications such as cutting oil drainage treatment, animal and vegetable oil processing wastewater treatment, removal of emulsion from degreasing washing wastewater, recovery of cleaning agent, removal of emulsion in rinse water, recovery of rinse water, and removal of ink from screen plate cleaning agent. Further, it can be used for applications such as steam drain recovery and purification of hot refrigerant water in an air conditioning system using a heat storage tank.
以下に、本発明の実施例について説明するが、本発明はこれにより限定されるものではない。以下の実施例の結果から、本発明によれば、中空糸膜洗浄工程で発現する中空糸膜の捻れおよび絡みが抑えられ、それにより濾過工程において付着するSS成分の除去効率低下の軽減が可能となることが明らかである。 Examples of the present invention will be described below, but the present invention is not limited thereby. From the results of the following examples, according to the present invention, twisting and entanglement of the hollow fiber membrane that is manifested in the hollow fiber membrane washing step can be suppressed, thereby reducing the reduction in the removal efficiency of the SS component adhering in the filtration step. It is clear that
ポリスルホン系樹脂からなり、平均孔径0.02μmであって、バブルポイントが0.5MPa以上である中空糸膜よりなる膜面積7.0m2の「片端フリー」タイプの中空糸膜モジュールを使用し、温度19〜27℃かつ濁度0.88〜3.30度の河川表流水を原水として、外圧全濾過方式、濾過速度0.58m3/hrの条件で定流量濾過を行った。中空糸膜の洗浄は、シーケンスコントロールにより30分に1回、原液排出口バルブを開けた状態で、中空糸膜モジュールの濾液側に圧力0.2MPaの空気を導入することにより10秒間加圧操作し、その後原液排出口バルブを閉じ濾液出口バルブと気体排出口バルブを開いて加圧状態を開放した状態で5秒間置き、次いで濾液出口バルブを閉じ、中空糸膜モジュールの原液側の下部より圧力0.1MPaの空気を0.6Nm3/hrの流量で1分間噴出させて行った。濾液側気体導入工程後の中空糸膜エレメントの状態は、捻れや絡みが見られず整束された状態であり、その後の濾過容器下部よりの空気噴出(バブリング洗浄)による洗浄が効率よく行われることが十分期待できる状態であった。濾過運転期間中、膜間差圧を定期的に測定し、膜間差圧が0.1MPaに達するまでの濾過時間を中空糸膜モジュールの濾過寿命とした場合、濾過寿命は125日間であった。rちゅうくうし
Using a hollow fiber membrane module of “one end free” type having a membrane area of 7.0 m 2 made of a hollow fiber membrane made of a polysulfone-based resin and having an average pore diameter of 0.02 μm and a bubble point of 0.5 MPa or more, A constant flow rate filtration was performed under the conditions of an external pressure total filtration method and a filtration rate of 0.58 m 3 / hr using a river surface water having a temperature of 19 to 27 ° C. and a turbidity of 0.88 to 3.30 degrees as raw water. The hollow fiber membrane is washed once every 30 minutes by sequence control, with the pressure of 10 MPa applied by introducing air at a pressure of 0.2 MPa to the filtrate side of the hollow fiber membrane module with the stock solution outlet valve opened. After that, close the stock outlet valve, open the filtrate outlet valve and gas outlet valve and release the pressurized state for 5 seconds, then close the filtrate outlet valve and press from the lower part of the hollow fiber membrane module on the stock side 0.1 MPa air was ejected at a flow rate of 0.6 Nm 3 / hr for 1 minute. The state of the hollow fiber membrane element after the filtrate-side gas introduction step is a state in which the hollow fiber membrane element is bundled without any twisting or entanglement, and the subsequent washing by air ejection (bubbling washing) from the lower part of the filtration container is efficiently performed. It was in a state that could be expected sufficiently. During the filtration operation, when the transmembrane pressure difference is measured periodically and the filtration time until the transmembrane pressure difference reaches 0.1 MPa is defined as the filtration life of the hollow fiber membrane module, the filtration life is 125 days. . rchukushi
比較例
実施例において、中空糸膜モジュールの濾液側に圧力0.2MPaの空気を導入する際、濾過容器下部の原水排出口バルブではなく側面の気体排出口バルブを開けて行った。この工程後、中空糸膜エレメントには捻れや絡みが発生しており、その後の濾過容器下部からの圧力0.1MPaの空気を0.6Nm3/hrの流量で1分間噴出させる工程において、上昇空気が捻れや絡みの発生したエレメントを揺らしにくかった。濾過運転期間中、膜間差圧を定期的に測定し、膜間差圧が0.1MPaに達するまでの濾過時間を中空糸膜モジュールの濾過寿命とした場合、濾過寿命は103日間であった。
Comparative Example In the example, when air having a pressure of 0.2 MPa was introduced into the filtrate side of the hollow fiber membrane module, the side gas outlet valve was opened instead of the raw water outlet valve at the lower part of the filtration container. After this step, the hollow fiber membrane element is twisted and entangled, and then rises in the step of ejecting air at a pressure of 0.1 MPa from the lower portion of the filtration container for 1 minute at a flow rate of 0.6 Nm 3 / hr. Air was hard to shake the twisted or entangled element. During the filtration operation, when the transmembrane pressure difference is measured periodically and the filtration time until the transmembrane pressure difference reaches 0.1 MPa is defined as the filtration life of the hollow fiber membrane module, the filtration life is 103 days. .
A,D…濾液側
B,E…原液側
1,25…濾過容器
2…仕切板
4,26…中空糸膜エレメント
5…濾液出口
6…加圧気体導入口
7…原液導入口
8…気体排出口
9…気体導入口
10…原液排出口
21…原液導入口バルブ
22…加圧気体導入口バルブ
23…濾液出口バルブ
24…気体排出口バルブ
27…原液排出口バルブ
28…気体導入口バルブ
29…エアーコンプレッサー
A, D: Filtrate side B, E ...
Claims (4)
A washing method for a hollow fiber membrane module used in an external pressure filtration system in which a stock solution is supplied to the outer surface side of the hollow fiber membrane and a filtrate is taken out from the inner surface side of the hollow fiber membrane, While the liquid is filled, pressurize the filtrate side of the hollow fiber membrane to discharge the liquid or gas to the stock solution side, while discharging the liquid or gas on the stock solution side from the stock solution outlet provided at the bottom of the hollow fiber membrane. A method for cleaning a hollow fiber membrane module.
2. The hollow fiber membrane according to claim 1, wherein when the filtrate side of the hollow fiber membrane is pressurized in a state where the liquid side of the hollow fiber membrane is filled with liquid, the hollow fiber membrane is pressurized with a gas having a pressure smaller than a puff point of the hollow fiber membrane. How to clean the module.
The method for cleaning a hollow fiber membrane module according to claim 1 or 2, wherein after the liquid or gas is discharged to the stock solution side, the pressurization on the filtrate side is released, and then the raw water side is filled with the raw water.
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JP2017070915A (en) * | 2015-10-08 | 2017-04-13 | 株式会社クラレ | Washing method of hollow fiber membrane module and filtration device |
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