1308504 ⑴ 九、發明說明 【發明所屬之技術領域】 本發明係關於薄膜過濾裝置的操作方法’用於使包 括：河水、湖水、地下水、污水、國內廢水'工業流出物 及二次流出物的水（以下稱爲原水）受到處理，以及由使 用安裝於密封槽之薄膜過濾裝置或安裝於水頭型或吸入型 的敞槽之薄膜過濾裝置清除水中的濁度及微生物。 【先前技術】 傳統上，於處理水的過程中，諸如水澄清、污水處理 及工業流出物處理，以凝結沉澱、重力分離或類似方法將 原水分離成固體及液體物質。然而’隨著薄膜技術的進 步，薄膜分離處理已被使用於各種過濾裝置，因爲薄膜於 分離性能或分離的銳利性方面係極優的，且佔有安裝用之 較小空間，以及更容易控制其操作。近年來，已使用薄膜 模組配置於送至上述的不同敞槽的每一者之原水以及原水 分離成固體及液體物質之方法。因此，薄膜模組係配置於 含有送至敞槽的懸浮物質之原水，原水係由吸入作用或水 位差以這些薄膜模組而過濾，且已通過薄膜模組之過瀘水 自敞槽而引出。此種過程使液相的懸浮物質留在敞槽內成 爲薄膜模組的送入側上的固體物質，且去除濁度及微生物 之乾浮過濾水被獲得在薄膜模組的輸出側上。 於此種薄膜過濾裝置中，當原水中的懸浮物質隨著過 濾的延續而黏在薄膜表面且阻塞其細孔時，其過濾性能逐 -4- (2) (2)1308504 漸劣化，最後使工廠無法過濾。爲穩定對抗其阻塞之過 濾，其需要實施物理清洗，諸如氣體清潔，其由空氣或某 些其它氣體導引至分離薄膜的原水側（以下稱爲氣體（或 空氣）洗滌），及回壓清洗，其由將諸如過濾水的回洗介 質或來自過濾液體側的乾淨水噴射於與過濾的方向相反之 方向，以移除已累積在分離薄膜表面上的物質（以下稱爲 BW (回洗）），因此使已累積在薄膜表面上的懸浮物質 剝離，且進一步自該系統排出剝離的懸浮物質。於此過程 中，如果敞槽中的原水量（維持容量）係大，排出由物理 清洗自該系統所剝離的整個懸浮物質量將伴隨著大量的原 水，導致於過濾水量對所使用的原水量的比的下降，也就 是說，回收比。 鑑於此問題，已有提議柱狀流系統的操作方法，藉由 此系統，回收比係由將固定量的原水恆定送至配置薄膜模 組之敞槽予以控制，且在同時自該系統排_出原水（例如， 見專利文件1 )。然而，由揭示於專利文件1之習知薄膜 過濾裝置的上述操作方法，例如，如果9 9 %或更高的高 回收比將被獲得，敞槽中僅1 %或更少的原水可自該系統 而排出，且由物理清洗或其它方法所剝離之所有懸浮物質 不能自該系統而排出，結過，敞槽中之懸浮物質的濃度將 逐漸地上升。因此’爲了完成穩定濾膜，這是需要操作在 低薄膜過瀘通量或增加來自該系統之含有懸浮物質的原水 的排出量（以降低回收比）。 其它已知方法包括一方法，在自薄膜模組下方噴出氣 (3) (3)1308504 泡時’由此方法降低濾膜的原水側之液體位準以增強氣體 洗滌的功效（例如，見專利文件2及3)，及另一方法， 由此方法將臭氧化空氣以氣泡的形式射入濾膜的原水側 (例如’見專利文件4 )。顯示於專利文件4及5利用氣 泡消失在氣體/液體介面上的功效或液體表面由於氣泡的 破裂的大振盪之氣體洗滌方法係有利於增強清洗功效，而 它們涉及使由於氣泡的上升所引起之交叉流動的清洗功效 或伴隨著排除氣泡的相等體積的功效之濾膜的振動的清洗 功效而減半的問題。並且，因爲液體位準的降低消除濾膜 周圍的水，由於氣泡的振動所造成之濾膜間的直接接觸及 磨擦可能引起濾膜的受損或破裂。更者，因爲當液體位準 下降時由氣體洗滌一旦自薄膜表面剝離之懸浮物質再次黏 至薄膜表面，有濃縮懸浮物質不能自該系統完全排出之問 題，且因此使清洗功效減半。 更者，因爲自接近薄膜模組的入口之濾膜至入口之距 離係短以及濾膜的側上之流體（處理水）的壓力損失係小 的，引起濾膜的原水側及處理水側間之壓力差的增加，也 就是說，薄膜壓力差，結果是，比起在其它位置快速污染 且於過濾性能中劣化之濾膜，上述位置中之濾膜過濾更大 量的原水。鑑於此問題，提議實施過濾同時保持部份的濾 膜未浸於原水之方法（見專利文件5)。 然而，當應用至上述的習知裝置時，揭示於專利文件 5之薄膜過濾裝置的操作方法引起濾膜的乾化，因爲濾膜 一直部份地外露在大氣中。並且，當整個濾膜未被使用 -6- (4) (4)1308504 時，有一有效薄膜面積減小之問題。 [專利文件 1 ]WO 00/30742 [專利文件2]〗P-B2-6-71 540 [專利文件 3] JP-B 2-3 3 5 1 03 7 [專利文件 4]JP-A-63-42703 [專利文件 5]JP-A-1 1 -147028 【發明內容】 本發明預期提供一種操作方法，其使穩定濾膜操作成 爲可能，同時由減小濾膜上的負載來確保高產量及實施有 效清洗。 由於本案發明人之徹底的硏究，發現該操作方法可達 到穩定濾膜操作，同時確保高回收比，其藉由自該系統排 出敞槽中之廢水，其在重複過濾步驟及物理清洗步驟二次 或更多次以及結合於浸入所有濾膜的狀態中而完成過濾之 過濾步驟,與於部份浸入濾膜的狀態中而完成過濾之另一過 濾步驟之後，因此減少濾膜的長度方向之污染點，其用來 增強物理清洗的功效，且降低敞槽中的原水量，亦即，維 持容量，因此自該系統排出由物理清洗所剝離之懸浮物質 以及留於敞槽中的小量原水，最後成功完成本發明。 因此，本發明可摘要如下： (1)一種薄膜過濾裝置的操作方法，其中包含大量外 露式（exposed )中空纖維薄膜之薄膜模組係安裝於原水 敞槽，該方法包含：過濾步驟，在過濾步驟，原水係由給 (5) (5)1308504 定不同壓力於該等中空纖維薄膜的主要側（原水側）及次 要側（處理水側）之間予以過濾；氣體清洗的物理清洗步 驟係藉由將氣態清洗介質噴射至該薄膜模組的主要側上， 而該回壓清洗係藉由自該等中空纖維薄膜的次要側進給回 洗介質以及使該回洗介質送至該等中空纖維薄膜的原水 側；及排泄步驟，在重複該過濾步驟及該物理清洗步驟二 或更多次之後，自該系統排出該敞槽中的廢水。 (2) 如上述（1)之薄膜過濾裝置的操作方法，其中該 過濾步驟另包括過濾步驟（過瀘步驟A)，其包含將原水 送至該敞槽以及於ί部份外露構成該薄膜模組之該等中空纖 維薄膜的狀態屯啓動該原水的過濾的次步驟、及於浸漬構 成該薄膜模組的所有中空纖維薄膜的狀態中過濾該原水的 後續次步驟。 (3) 如上述（1 )或一fl)之薄膜過濾裝置的操作方 法，其中該過濾步驟另包括過濾步驟（過濾步驟Β)，其 包含在該物理清洗步驟的完成之後/過濾原水而無需將原水 送至該敞槽直到如份外露構成該薄膜模組之該等中空纖維 薄膜> 止的次步驟、及將原水送入該敞槽以及於辑漬構成 該薄膜模組的所有該等中空纖維薄膜的狀態中;過濾該原水 的後續次步驟。 (4) 如以上（1)至（3)任一者之薄膜過濾裝置的 操作方法， 其中該物理清洗步驟係將被執行於浸漬構成該薄膜模 組的所有該等中空纖維薄膜的狀態中之步驟（物理清洗步 -8 - 1308504 ⑹ 驟A )、及將被執行於部份外露構成該薄膜模組之該等中 空纖維薄膜的狀態之另一步驟（物理清洗步驟B )的組 合。 (5) 如以上（1)至（〇任一者之薄膜過濾裝置的 操作方法， 其中該薄膜模組的兩端係由藉由黏著劑所固定的大量 外露中空纖維薄膜予以組成，在頂端係開口的中空纖維薄 膜，而在底端係關閉之中空纖維薄膜。 (6) 如以上（1)至（5)任一者之薄膜過濾裝置的 操作方法， 其中在該過濾步驟A及該物理清洗步驟被執行以及 該過濾步驟B及該物理清洗步驟被重複一或更多次之後， 該敞槽中之廢水自該系統而排出。 依據本發明，其係可能實施有效物理清洗，同時減弱 在濾膜上的負載及降低敞槽中之原水量，也就是說，維持 容量，因此致能穩定濾膜操作，同時自該系統由物理清洗 與小量原水一起所剝離之懸浮物質排出來保持高回收比。 以下將專注在實施本發明的最佳模式來詳細說明本發 明。 與本發明有關之原水係河水 '湖水、地下水、儲存的 水、二次流出物、工業流出物、污水或類似水。以習知方 式用於薄膜過濾上述之任一種原水涉及懸浮物質或比含於 原水之薄膜的孔徑具有更大粒徑的任何其它物質的阻塞， 且因此’傾向引起所謂的濃度極化或塊狀層的形成，且在 (7) 1308504 同時，薄膜被此種懸浮物質或物質所阻塞，或者薄膜中的 , 薄膜孔吸收此種物質。結果，當過濾原水時之薄膜的過濾 流速降至只有當過爐乾水時之流速的一部份或十分之幾， 且過濾流速隨著過濾的延續而逐漸下降。 於此種薄膜過濾裝置中，爲了穩定過濾，其需要由已 傳輸的水或空氣自濾膜的次要側回流至主要側的物理清洗 使已累積在薄膜表面上之懸浮物質剝離，且進一步排出自 # ) 該系統排出剝離的所有懸浮物質之量。於此過程中，如果 敞槽中的原水量（維持容量）係大，自該系統排出由物理 清洗所剝離之懸浮物質的總量將伴隨著大量的原水，導致 過濾水量對所使用的原水量的比之下降，亦即，回收比》 並且，因爲接近薄膜模組的入口自濾膜至入口之距離係短 的以及濾膜的側上之流體（處理水）的壓力損失係小的， 濾膜的原水側及處理水側間之壓力差增加，亦即，薄膜差 壓，結果是，上述位置之濾膜比其它位置的濾膜過濾更大 • } 量的原水，快速污染且劣化於過濾性能》 依據本發明之操作薄膜過濾裝置的方法係以下的方 法，其中敞槽中之原水的液體位準係控制在配置於敞槽之 薄膜模組的上端面以上，過濾步驟A包括一過濾步驟， • 在該過濾步驟，除了以所有濾膜實施過濾之正常過濾步驟 . 之外，原水送至敞槽以及懸浮物質係於部份暴露構成薄膜 模組之濾膜的狀態中藉由啓動原水的過濾而黏附至構成薄 膜模組之濾膜的下部，且過濾步驟B包括一過濾步驟，在 該過濾步驟，在完成物理清洗步驟之後，懸浮物質係由過 -10- (8) (8)1308504 濾原水而黏附至構成薄膜模組之濾膜的下部直到構成部份 暴露的薄膜模組之濾膜而無需實施原水的送入敞槽，以 及，在重複過濾步驟及物理清洗步驟二次或更多次之後> 濃縮懸浮物質自該系統而排出。 現在，於使用2m有效長度的中空纖維薄膜作爲濾膜 之例子中，中空纖維薄膜的壓力損失的理論計算顯示，距 薄膜模組的入口約20%長度的濾膜實施約50%的所需水 的過濾以進行過濾處理，這意指前者過濾比其它區由濾膜 所過濾的原水更大體積的原水，導致薄膜污染的快速進行 及過濾性能的劣化。由導入依據本發明之過濾步驟A及 過濾步驟B，能夠有效使用由於壓力損失的影響來防止有 助於過濾之濾膜，且因此可能減少濾膜的長度方向之污染 點。再者，重複過濾步驟及物理清洗步驟二次或更多次以 及因此減小薄膜過濾裝置的維持體積，當自該系統排出由 物理清洗所剝離之懸浮物質時，懸浮物質係與僅小量原水 一起排出，因此使穩定濾膜操作在高回收比成爲可能。 在此，部份暴露構成薄膜模組之濾膜的狀態之薄膜過 濾流率可被控制在如正常過濾步驟的相同位準或更低位準 或更高位準，而較佳地在正常過濾步驟控制在不高於薄膜 過濾流率之位準·> 更佳地，構成薄膜模組之濾膜的長度於垂直方向係由 L表示，而於部份暴露濾膜的狀態中之濾膜在敞槽中的原 水的液體表面上未與原水接觸的垂直長度係由L’表示’ 以在薄膜過濾流率F2於部份暴露濾膜的狀態中實施過 -11 - (9) (9)1308504 濾，該薄膜過濾流率F2滿足相對於在正常過濾步驟的薄 膜過濾F 1之以下條件： F2SF1S (L-L，）/L(L>L’、L>0、L>L’S〇) 再者，如果回洗介質（其可以是過濾水 '清潔水或類 似水）係於與過濾的方向相反之方向自過濾液體側傳送至 原水側以移除已累積在分離薄膜表面上的物質之回洗係使 用作爲物理清洗的方法，已被使用在物理清洗步驟之過濾 水、清潔水或類似水可全部或部份儲存於敞槽以重新使用 作爲原水的一部份。因此，在執行由物理清洗所剝離的懸 浮物質的總量自該系統排出之排泄步驟之前，由重複過濾 步驟及物理清洗步驟二次或更多次之操作可在比其它方式 更高的回收比而完成。 附帶地，爲了增強物理清洗步驟的清洗功效，較佳地 將諸如次氯化鈉或臭氧的氧化劑加至將使用於回洗的回洗 介質’再者’在濾膜的原水側上於作爲氣泡的空氣或類似 物的導引氣體的氣體洗滌中含有臭氧或某些其它氧化劑》 然而’如以上狀態，依據有關濾膜的耐久性的限制，在習 知條件下的氣體洗條未一直證明是足夠有效的。 依據本發明之濾膜清洗方法，由結合執行於全部浸漬 構成薄膜模組的中空纖維薄膜之狀態中的步驟（以下稱爲 物理清洗步驟A )及執行於部份暴露構成薄膜模組的中空 纖維薄膜之狀態中的步驟（以下稱爲物理清洗步驟B )， -12- (10) 1308504 可提供所有濾膜以下的功效：（a )由伴隨氣泡的上升的 • 交叉流之清洗功效，（b )由自排除相對於氣泡的體積之 . 液體等量的功效繼續發生之濾膜的振動之清洗功效，及 (c)氣體-液體介面的氣泡消失的功效及由於氣泡的破裂 之液體表面的實質振盪之清洗功效，進一步可能有（d) 自該系統完全排出由濾膜所剝離之懸浮物質，因爲一旦由 氣體清洗所剝離薄膜表面之懸浮物質不會再次黏至薄膜表 ♦ 5 面，以及（e )相較於習知氣體洗滌方法，更有效率地自 濾膜表面剝離懸浮物質，因爲足夠長的時間可被確定，接 近入口的薄膜模組的濾膜在此期間保持與氣泡接觸。 當薄膜模組中的原水一旦在物理清洗步驟B由過濾或 排出而降低時，原水的液體表面的位準於濾膜的垂直方向 可在任何高度，而爲了提供上述的清洗之五個功效給所有 濾膜，較佳地於其垂直方向降低位準至濾膜的最底部。 且，作爲在氣體洗滌步驟B自下部上升濾膜周圍的原水的 ^ f 液體表面至上部之替代方法，有濾膜周圍之原水的液體表 面上升同時實施回洗之方法，及濾膜周圍之原水的液體表 面上升同時送入原水之另一方法，而由回洗上升濾膜周圍 之原水的液體表面的方法更佳地。附帶地，（1 )回洗在 ' 一直實施在如氣體洗滌的同時，而（2)同樣地可在回洗 • 的導入之前單獨實施氣體洗滌。或者，（3)亦可在回洗 的導入之後單獨實施氣體洗滌。再者，（4)亦可瞭解 到，導入回洗同時讓水進入且在同時實施氣體洗滌，或可 替代地結合（1 )至（4 )。 -13- (11) (11)1308504 現在，在清洗濾膜的步驟，物理清洗步驟A及物理 清洗步驟B在整個清洗期間可以是任何比例，而較佳地設 定於〗：10至10: 1的範圍。 再者，當實施氣體洗滌同時上升液體表面時，因爲濾 膜周圍之水的不足將僅持續一小段時間，經由直接接觸之 濾膜的受損及破裂及兩者間之磨擦以及薄膜的乾化可被防 止。並且，因爲清洗功效比習知氣體洗滌方法更大，所使 用之氣態清洗介質的量可被減少，且因此這是在濾膜及薄 膜模組的耐久性及能量效率的方面之優點》 或者，當氣體洗滌係依據本發明以氣泡形式朝向濾膜 的原水側噴射同時上升濾膜的原水的液體表面而完成時， 如果含有包括氯、二氧化氯、過氧化氫及臭氧氣體之氧化 劑的至少一者之氣體被使用作爲氣態清洗介質或以含有這 些氧化劑的至少一者的氣體而回洗被結合地使用，清洗功 效可進一步增強。氣體洗滌的耐久性可考慮到過濾壓力的 回收比及過濾設備的時間利用比之適當決定。1308504 (1) IX. INSTRUCTIONS OF THE INVENTION [Technical Field of the Invention] The present invention relates to a method of operating a membrane filtration device for water including: river water, lake water, ground water, sewage, domestic wastewater, industrial effluent and secondary effluent (hereinafter referred to as raw water) is treated, and turbidity and microorganisms in the water are removed by using a membrane filtration device mounted in a sealed tank or a membrane filtration device installed in an open head or a suction type open tank. [Prior Art] Conventionally, in the process of treating water, such as water clarification, sewage treatment, and industrial effluent treatment, raw water is separated into solid and liquid substances by coagulation sedimentation, gravity separation or the like. However, with the advancement of thin film technology, membrane separation treatment has been used in various filtration devices because the film is excellent in separation performance or separation sharpness, and it occupies less space for installation and easier to control. operating. In recent years, a raw material of a film module disposed in each of the above-mentioned different open grooves and a method in which raw water is separated into solid and liquid substances have been used. Therefore, the membrane module is disposed in the raw water containing the suspended matter sent to the open tank, and the raw water is filtered by the thin film module by suction or water level difference, and has been extracted from the open tank by the membrane module. . This process leaves the suspended matter in the liquid phase in the open tank as a solid material on the feed side of the membrane module, and the dry floating filtered water which removes turbidity and microorganisms is obtained on the output side of the membrane module. In the membrane filtration device, when the suspended matter in the raw water adheres to the surface of the membrane and blocks the pores as the filtration continues, the filtration performance is gradually deteriorated by -4-(2) (2) 1308504, and finally The factory cannot filter. In order to stabilize the filtration against its clogging, it is necessary to carry out physical cleaning, such as gas cleaning, which is guided by air or some other gas to the raw water side of the separation membrane (hereinafter referred to as gas (or air) washing), and back pressure cleaning. It is sprayed in a direction opposite to the direction of filtration by spraying backwashing medium such as filtered water or clean water from the side of the filtered liquid to remove substances accumulated on the surface of the separation membrane (hereinafter referred to as BW (backwashing) Therefore, the suspended matter accumulated on the surface of the film is peeled off, and the peeled suspended matter is further discharged from the system. In this process, if the amount of raw water (maintenance capacity) in the open tank is large, the mass of the entire suspended solids discharged from the system by physical cleaning will be accompanied by a large amount of raw water, resulting in the amount of filtered water used for the amount of raw water used. The ratio of the drop, that is, the recycling ratio. In view of this problem, there has been proposed a method of operating a columnar flow system by which the recovery ratio is controlled by a constant supply of a fixed amount of raw water to an open tank in which the membrane module is disposed, and at the same time from the system. Raw water (see, for example, Patent Document 1). However, according to the above-described operation method of the conventional membrane filtration device disclosed in Patent Document 1, for example, if a high recovery ratio of 99% or more is to be obtained, only 1% or less of the raw water in the open tank can be obtained therefrom. All suspended matter that is discharged by the system and stripped by physical cleaning or other methods cannot be discharged from the system, and the concentration of the suspended matter in the open tank will gradually rise. Therefore, in order to complete the stabilization of the membrane, it is necessary to operate at a low membrane permeate flux or to increase the discharge of raw water from the system containing suspended matter (to reduce the recovery ratio). Other known methods include a method of ejecting gas (3) (3) 1308504 bubbles from beneath the membrane module. 'This method reduces the liquid level of the raw water side of the membrane to enhance the efficiency of gas scrubbing (see, for example, see patent Documents 2 and 3), and another method, in which ozonized air is injected as bubbles into the raw water side of the filter (for example, see 'Patent Document 4'). The gas washing method shown in Patent Documents 4 and 5 which utilizes the effect of the bubble disappearing on the gas/liquid interface or the large oscillation of the liquid surface due to the rupture of the bubble is advantageous for enhancing the cleaning effect, and they are related to the rise of the bubble due to the rise of the bubble. The cross-flow cleaning effect or the problem of halving the cleaning effect of the vibration of the filter accompanying the elimination of the equal volume of the bubbles. Also, since the liquid level is reduced to eliminate the water around the filter, direct contact and friction between the filters due to the vibration of the bubbles may cause damage or breakage of the filter. Furthermore, since the suspended matter peeled off from the surface of the film adheres again to the surface of the film when the liquid level is lowered, there is a problem that the concentrated suspended matter cannot be completely discharged from the system, and thus the cleaning effect is halved. Furthermore, since the distance from the filter membrane near the inlet of the membrane module to the inlet is short and the pressure loss of the fluid (treatment water) on the side of the membrane is small, the raw water side and the treated water side of the membrane are caused. The increase in the pressure difference, that is, the difference in film pressure, results in a larger amount of raw water being filtered by the filter in the above position than the filter which is rapidly contaminated at other locations and deteriorates in the filtration performance. In view of this problem, it is proposed to carry out the filtration while keeping a part of the filter film immersed in the raw water (see Patent Document 5). However, when applied to the above-described conventional device, the operation method of the membrane filtration device disclosed in Patent Document 5 causes the filtration membrane to be dried because the filtration membrane is always partially exposed to the atmosphere. Also, when the entire filter is not used -6-(4)(4)1308504, there is a problem that the effective film area is reduced. [Patent Document 1] WO 00/30742 [Patent Document 2] P-B2-6-71 540 [Patent Document 3] JP-B 2-3 3 5 1 03 7 [Patent Document 4] JP-A-63- 42703 [Patent Document 5] JP-A-1 1 -147028 SUMMARY OF THE INVENTION The present invention is intended to provide an operation method which makes it possible to stabilize a membrane operation while ensuring high throughput and implementation by reducing the load on the membrane. Effective cleaning. Due to the thorough research of the inventor of the present invention, it was found that the operation method can achieve stable filtration membrane operation while ensuring high recovery ratio, which is discharged from the open tank by the system, in the repeated filtration step and the physical cleaning step 2 One or more times and a filtration step of performing filtration in a state of being immersed in all of the filtration membranes, and after another filtration step of partially filtering in a state of being partially immersed in the filtration membrane, thereby reducing the length direction of the filtration membrane a point of contamination that enhances the effectiveness of physical cleaning and reduces the amount of raw water in the open tank, that is, maintains capacity, thereby discharging suspended matter removed by physical cleaning from the system and a small amount of raw water remaining in the open tank Finally, the present invention was successfully completed. Therefore, the present invention can be summarized as follows: (1) A method for operating a membrane filtration device, wherein a membrane module comprising a plurality of exposed hollow fiber membranes is installed in a raw water open tank, the method comprising: a filtration step, in filtering In the step, the raw water system is filtered between the main side (raw water side) and the secondary side (treated water side) of the hollow fiber membrane by different pressures of (5) (5) 1308504; the physical cleaning step of gas cleaning is By injecting a gaseous cleaning medium onto the major side of the film module, the back pressure cleaning by feeding back the backing medium from the minor side of the hollow fiber membranes and delivering the backwashing medium to the a raw water side of the hollow fiber membrane; and a draining step of discharging the wastewater in the open tank from the system after repeating the filtering step and the physical washing step two or more times. (2) The method of operating a membrane filtration device according to (1) above, wherein the filtering step further comprises a filtering step (passing step A), comprising: sending raw water to the open tank and partially exposing the film to form the thin film mold The state of the hollow fiber membranes of the group, the secondary step of filtering the raw water, and the subsequent substep of filtering the raw water in a state of impregnating all of the hollow fiber membranes constituting the membrane module. (3) The method of operating a membrane filtration device according to (1) or (fl) above, wherein the filtering step further comprises a filtration step (filtration step ,), which comprises after the completion of the physical cleaning step/filtering the raw water without The raw water is sent to the open trough until the hollow fiber film constituting the film module is removed, and the raw water is fed into the open trough and all the hollows forming the thin film module are formed. In the state of the fibrous film; the subsequent substep of filtering the raw water. (4) The method of operating a membrane filtration device according to any one of (1) to (3) above, wherein the physical cleaning step is performed in a state of impregnating all of the hollow fiber membranes constituting the membrane module. The step (physical cleaning step -8 - 1308504 (6) step A), and a combination of another step (physical cleaning step B) that will be performed to partially expose the state of the hollow fiber membranes constituting the membrane module. (5) The method of operating a membrane filtration device according to any of the above (1) to (1), wherein both ends of the membrane module are composed of a plurality of exposed hollow fiber membranes fixed by an adhesive, at the apex system (6) A method of operating a membrane filtration device according to any one of (1) to (5) above, wherein the filtration step A and the physical cleaning are performed. After the step is performed and the filtration step B and the physical washing step are repeated one or more times, the wastewater in the open tank is discharged from the system. According to the present invention, it is possible to perform effective physical cleaning while weakening the filtration. The load on the membrane and the reduction of the amount of raw water in the open tank, that is, the maintenance of the capacity, thus enabling the operation of the membrane to be stabilized, while the suspended matter discharged from the system by physical cleaning and a small amount of raw water is discharged to maintain high recovery. The invention will be described in detail below with reference to the best mode for carrying out the invention. The original water system of the invention is related to the lake water, ground water, stored water and secondary flow. , industrial effluent, sewage or similar water. Used in the conventional manner for membrane filtration. Any of the above raw waters involves the clogging of suspended matter or any other substance having a larger particle size than the pore size of the film containing raw water, and thus ' The tendency to cause the formation of a so-called concentration polarization or a bulk layer, and at (7) 1308504, the film is blocked by such suspended matter or substance, or the film pores absorb the substance in the film. As a result, when the raw water is filtered At this time, the filtration flow rate of the film is reduced to a part or a few tenths of the flow rate when the dry water is passed through the furnace, and the filtration flow rate gradually decreases as the filtration continues. In this membrane filtration device, in order to stabilize the filtration, It requires the physical washing of the water or air from the secondary side of the filter membrane to the main side to cause the suspended matter accumulated on the surface of the film to be peeled off, and further discharged from the system. the amount. In this process, if the amount of raw water (maintenance capacity) in the open tank is large, the total amount of suspended matter discharged from the system by physical washing will be accompanied by a large amount of raw water, resulting in the amount of filtered water to the amount of raw water used. The ratio of the reduction, that is, the recovery ratio, is also because the pressure near the inlet of the membrane module from the membrane to the inlet is short and the pressure loss of the fluid (treated water) on the side of the membrane is small. The pressure difference between the raw water side of the membrane and the treated water side increases, that is, the membrane differential pressure, and as a result, the membrane at the above position is filtered more than the filter at other locations. • The amount of raw water is rapidly contaminated and degraded by filtration. The method for operating a membrane filtration device according to the present invention is the method wherein the liquid level of the raw water in the open tank is controlled above the upper end surface of the membrane module disposed in the open tank, and the filtering step A includes a filtration step , • In this filtration step, in addition to the normal filtration step of filtering through all the membranes, the raw water is sent to the open tank and the suspended matter is partially exposed to form a membrane module. The state of the membrane is adhered to the lower portion of the membrane constituting the membrane module by the filtration of the activated raw water, and the filtration step B includes a filtration step in which the suspended matter is passed after the physical cleaning step is completed - 10- (8) (8)1308504 Filter the raw water and adhere to the lower part of the membrane constituting the membrane module until the membrane of the partially exposed membrane module is formed without the need to carry the raw water into the open trough, and, in the repeated filtration After the step and the physical washing step two or more times > the concentrated suspended matter is discharged from the system. Now, in the case of using a 2 m effective length hollow fiber membrane as a filter membrane, the theoretical calculation of the pressure loss of the hollow fiber membrane shows that about 20% of the filter membrane from the inlet of the membrane module is subjected to about 50% of the required water. The filtration is carried out for filtration treatment, which means that the former filters a larger volume of raw water than the raw water filtered by the filtration membrane in other regions, resulting in rapid progress of membrane fouling and deterioration of filtration performance. By introducing the filtration step A and the filtration step B according to the present invention, it is possible to effectively use the filter which contributes to filtration due to the influence of the pressure loss, and thus it is possible to reduce the contamination point in the longitudinal direction of the filtration membrane. Furthermore, the filtration step and the physical cleaning step are repeated two or more times and thus the maintenance volume of the membrane filtration device is reduced, and when the suspended material separated by the physical cleaning is discharged from the system, the suspended matter is only a small amount of raw water. Discharged together, thus making it possible to stabilize the membrane operation at a high recovery ratio. Here, the membrane filtration flow rate of partially exposing the state of the membrane constituting the membrane module can be controlled at the same level or lower or higher level as the normal filtration step, and is preferably controlled in the normal filtration step. Preferably, the length of the membrane constituting the membrane module is represented by L in the vertical direction, and the membrane is in the state of partially exposing the membrane in the state of the filter membrane. The vertical length of the liquid surface of the raw water in the tank that is not in contact with the raw water is represented by L''. In the state where the membrane filtration flow rate F2 is partially exposed to the filter membrane, -11 - (9) (9) 1308504 The membrane filtration flow rate F2 satisfies the following conditions with respect to the membrane filtration F 1 in the normal filtration step: F2SF1S (LL,) / L (L > L', L > 0, L > L'S〇) The washing medium (which may be filtered water 'cleaning water or the like) is used as a backwashing line that is transported from the filtered liquid side to the raw water side in the opposite direction to the filtration direction to remove the substance accumulated on the surface of the separated film. Physical cleaning method has been used in physical cleaning Step of filtered water, clean water or the like may be all or part of the water stored in the open tank for reuse as a part of the raw water. Therefore, before the discharge step of discharging the total amount of suspended matter stripped by the physical cleaning from the system, the recovery ratio of the repeated filtration step and the physical cleaning step can be higher than other methods. And finished. Incidentally, in order to enhance the cleaning effect of the physical washing step, it is preferred to add an oxidizing agent such as sodium hypochlorite or ozone to the backwashing medium to be used for backwashing 'again' on the raw water side of the filter as a bubble The gas or the like of the guided gas contains ozone or some other oxidant. However, as in the above state, according to the limitation of the durability of the filter, the gas washing under the conventional conditions has not always been proved to be Enough and effective. The membrane cleaning method according to the present invention comprises a step of performing a state in which all of the hollow fiber membranes constituting the membrane module are impregnated (hereinafter referred to as a physical cleaning step A) and a hollow fiber which is partially exposed to form a membrane module. The steps in the state of the film (hereinafter referred to as the physical cleaning step B), -12-(10) 1308504 provide all the effects below the filter: (a) the cleaning effect of the cross flow accompanying the rise of the bubble, (b) By self-excluding the volume relative to the bubble. The effect of the liquid equivalent effect continues to occur on the vibration cleaning effect of the filter, and (c) the gas-liquid interface bubble disappearance effect and the essence of the liquid surface due to bubble rupture The cleaning effect of the oscillation may further have (d) completely discharging the suspended matter peeled off from the filter membrane by the system, because the suspended matter on the surface of the peeled film once cleaned by the gas does not stick to the surface of the film again, and e) more efficient removal of suspended matter from the surface of the membrane than conventional gas scrubbing methods, because a sufficiently long time can be determined, close to the inlet thin The membrane of the membrane module remains in contact with the bubbles during this time. When the raw water in the membrane module is lowered by filtration or discharge in the physical cleaning step B, the liquid surface of the raw water can be at any height in the vertical direction of the filter, and in order to provide the above five functions of cleaning All filters, preferably in the vertical direction, are lowered to the bottom of the filter. Further, as an alternative method of raising the liquid surface of the raw water around the filter from the lower portion in the gas washing step B to the upper portion, the liquid surface of the raw water around the filter membrane rises while the backwashing method is performed, and the raw water around the filter membrane The liquid surface rises while feeding the raw water in another method, and the method of backwashing the liquid surface of the raw water around the filter membrane is more preferable. Incidentally, (1) backwashing is performed at the same time as 'gas washing, and (2) gas washing can be separately performed before the introduction of backwashing. Alternatively, (3) gas washing may be separately performed after the introduction of the backwashing. Further, (4) it is also known that the introduction of backwashing allows water to enter and simultaneously performs gas washing, or alternatively (1) to (4). -13- (11) (11) 1308504 Now, in the step of cleaning the filter, the physical cleaning step A and the physical cleaning step B may be any ratio during the entire cleaning period, and are preferably set at: 10 to 10: 1 The scope. Furthermore, when the gas washing is performed while raising the surface of the liquid, the shortage of water around the filter membrane will only last for a short period of time, the damage and rupture of the membrane through direct contact, and the friction between the two and the drying of the film. Can be prevented. Moreover, since the cleaning effect is greater than the conventional gas washing method, the amount of the gaseous cleaning medium used can be reduced, and thus this is an advantage in the durability and energy efficiency of the filter membrane and the membrane module. When the gas washing is performed in the form of bubbles toward the raw water side of the filter while lifting the liquid surface of the raw water of the filter, at least one if it contains an oxidizing agent including chlorine, chlorine dioxide, hydrogen peroxide and ozone gas. The gas of the person is used as a gaseous cleaning medium or backwashed with a gas containing at least one of these oxidizing agents, and the cleaning effect can be further enhanced. The durability of the gas washing can be appropriately determined in consideration of the recovery ratio of the filtration pressure and the time utilization of the filtration equipment.
依據本發明之將被使用的濾膜的材料可包括，然而未 限制例如，諸如聚乙烯、聚丙烯或聚丁烯之聚烯；諸如 PFA、FEP、EPE、ETFE、PCTFE、ECTFE 或 PVDF 的氟 樹脂；諸如聚碾、聚醚颯、聚醚酮、聚醚醚嗣或聚苯硫之 超工程用塑膠；諸如醋酸纖維或乙基纖維之纖維；聚丙烯 腈；或聚乙烯乙醇，每一材料可以是單一者或超過上述其 中一者的混合物。當諸如臭氧之強力氧化劑將被結合使用 時，陶瓷或某些其它無機薄膜或諸如PVDF薄膜、PTFE -14 - (12) (12)1308504 薄膜、ETFE薄膜或PFA薄膜之氟樹脂的有機薄膜可被應 用。在這些濾膜中，可較佳地使用範圍自奈米過濾 (NF )膜至微米過濾（MF )膜的孔徑。平均孔徑切開成 不超過10 // m的MF之約100分子的NF係特佳的。濾膜 可以是中空纖維狀、具有波形之中空纖維狀、扁平膜狀、 打褶狀、螺旋狀、管狀或任何其它想要形狀，而每單位體 積容許更大薄膜面積之中空纖維狀係更佳的。 使用於本發明之薄膜模組係如此形成爲，以大量濾膜 組成之一束薄膜的頂及底端係由黏著劑所固定，該等端的 一或兩者被開啓，且由黏著劑所固定之端的剖面狀不僅可 以是圓形亦可以是三角形、矩形、六角形、橢圓形或類似 形狀，而具有在頂端之薄膜的開口、讓氣體進來的裙狀結 構部及讓氣體流至在底端之0052的外部表面之氣體入口 孔之薄膜模組係較佳的。薄膜模組可被安裝於相對於地表 面之垂直或水平方向，而垂直安裝係特佳的》再者，當數 個薄膜模組配置於相同敞槽時，對於配置薄膜模組的位置 沒有特別限制，而將它們配置於維持容積係最小之最緊密 充塡的位置係較佳的。過濾的系統可以是交叉流過濾的總 量過濾。施加過濾壓力的方法可以是吸入或由水頭來過 濾。當中空纖維薄膜被使用時，內壓力過濾或外壓力過濾 可被使用。 當本發明形成如上述時，本發明使穩定薄膜過濾操作 成爲可能同時維持高回收比以及確定地含有來自系統的懸 浮物質之足夠量的原水。 -15- (13) (13)1308504 【實施方式】 關於本發明，以下將參考附圖詳細說明實施薄膜過濾 裝置的操作方法的模式的實例。 圖1A係顯示藉由使用具有一束薄膜的薄膜模組102 之正常過濾步驟中的操作的狀態之示意圖，該束薄膜由大 量濾膜101而組成，薄膜模組係安裝於敞槽103中的 垂直方向，薄膜模組的兩端係由黏著所固定，以及薄 膜模組1 02具有薄膜的開口在頂端’而在底端（以下稱 爲”薄膜模組”）具有讓空氣進入的裙形結構部及讓氣體流 至濾膜的外表面上之氣體進入孔，以控制原水的液體表面 在安裝於敞槽103之薄膜模組102的頂端面上方，以及過 濾器在所有濾膜1 〇 1的原水，而圖1 B係顯示於部份暴露 構成以上薄膜模組1 02的濾膜1 0 1的狀態中過濾該原水之 過濾步驟的操作狀態之示意圖。 在圖1A中之正常過濾步驟，當敞槽103中之原水的 液體表面被控制在薄膜模組1 02的頂端面上方時，由構成 薄膜模組1 02之所有濾膜1 0 1所達成之過濾。作爲正常過 濾步驟中控制液體表面的方法，送入敞槽1 03之原水的量 可利用液體位準計或柱狀流所控制，於柱狀流中，恆定量 的原水一直送入敞槽，以及部份的原水同時自系統排出。 另一方面，在圖1B中部份暴露濾膜10〗的狀態而過 濾的原水之過濾步驟，因爲過濾可被實施於原水暫停送入 薄膜模組〗〇2之狀態或在原水送入敞槽1 03之過程中，過 -16- (14) (14)1308504 濾係由薄膜模組102的部份濾膜]〇1所達成，同時敞槽 1 03中的原水的液體表面逐漸變得比薄膜模組1 〇2的頂端 面更低或更高。 較佳地在此以下述方式決定在此過濾步驟之薄膜過濾 流率。當濾膜1 〇 1的長度L = 2m，於部份暴露之濾膜1 0 1 的狀態在過濾步驟的結束或開始相對於敞槽1 03中之原水 的液體表面未與原水接觸之濾膜101的長度L’=0.5m，及 在正常過濾步驟的薄膜過濾流率Fl=5.0m3/hr (單薄膜模 組每小時提供5.0m3的過濾水之流率），在部份暴露濾膜 1 〇 1之過濾步驟之薄膜過濾流率F 2將如以下關係式：The material of the filter to be used according to the present invention may include, but is not limited to, for example, a polyolefin such as polyethylene, polypropylene or polybutene; fluorine such as PFA, FEP, EPE, ETFE, PCTFE, ECTFE or PVDF Resin; ultra-engineering plastics such as polypulverized, polyether oxime, polyether ketone, polyether ether or polyphenylene sulfide; fibers such as acetate or ethyl fibers; polyacrylonitrile; or polyethylene ethanol, each material It may be a single or a mixture of more than one of the above. When a strong oxidizing agent such as ozone is to be used in combination, a ceramic or some other inorganic film or an organic film such as a PVDF film, a PTFE-14-(12) (12)1308504 film, an ETFE film or a PFA film fluororesin may be application. Among these filters, a pore diameter ranging from a nanofiltration (NF) membrane to a microfiltration (MF) membrane can be preferably used. The average pore diameter is cut into NF of about 100 molecules of MF which is not more than 10 // m. The filter membrane may be hollow fiber, wavy hollow fiber, flat membrane, pleated, spiral, tubular or any other desired shape, and a hollow fiber-like system that allows for a larger membrane area per unit volume is preferred. of. The film module used in the present invention is formed such that a plurality of filter films are formed, and the top and bottom ends of the film are fixed by an adhesive, one or both of which are opened and fixed by an adhesive. The cross-section of the end may be not only a circular shape but also a triangular shape, a rectangular shape, a hexagonal shape, an elliptical shape or the like, and has an opening at the top end of the film, a skirt-like structure for allowing gas to enter, and allowing gas to flow to the bottom end. The film module of the gas inlet hole of the outer surface of the 0052 is preferred. The film module can be mounted in a vertical or horizontal direction with respect to the ground surface, and the vertical mounting system is particularly good. Further, when a plurality of film modules are disposed in the same open groove, there is no special position for the film module. Limitations, and it is preferred to arrange them in the most compact position where the volume is maintained to be the smallest. The filtered system can be a total amount of cross-flow filtration. The method of applying the filtration pressure may be inhalation or filtration by a water head. When a hollow fiber membrane is used, internal pressure filtration or external pressure filtration can be used. When the present invention is formed as described above, the present invention makes it possible to stabilize the membrane filtration operation while maintaining a high recovery ratio and surely containing a sufficient amount of raw water from the suspension material of the system. -15- (13) (13) 1308504 [Embodiment] With regard to the present invention, an example of a mode of carrying out the operation method of the membrane filtration device will be described in detail below with reference to the drawings. 1A is a schematic view showing a state of operation in a normal filtering step by using a film module 102 having a bundle of films, which is composed of a plurality of filter films 101 which are mounted in the open grooves 103. In the vertical direction, both ends of the film module are fixed by adhesion, and the film module 102 has a film opening at the top end and a bottom end (hereinafter referred to as "film module") has a skirt structure for allowing air to enter. And a gas inlet gas for allowing gas to flow to the outer surface of the filter membrane to control the liquid surface of the raw water above the top end surface of the membrane module 102 mounted to the open tank 103, and the filter at all of the membranes 1 〇1 The raw water, and Fig. 1B, is a schematic view showing the operation state of the filtration step of filtering the raw water in a state in which the filter 101 of the above film module 102 is partially exposed. In the normal filtering step of FIG. 1A, when the liquid surface of the raw water in the open space 103 is controlled above the top end surface of the film module 102, it is achieved by all the filter films constituting the thin film module 102. filter. As a method of controlling the surface of the liquid in the normal filtration step, the amount of raw water fed into the open tank 103 can be controlled by a liquid level meter or a column flow, in which a constant amount of raw water is fed into the open tank. And part of the raw water is discharged from the system at the same time. On the other hand, the filtration step of the raw water filtered in the state in which the filter membrane 10 is partially exposed in FIG. 1B, because the filtration can be carried out in the state in which the raw water is suspended and fed into the membrane module 〇2 or in the raw water is fed into the open tank. In the course of 1 03, the -16-(14) (14)1308504 filter system is achieved by the partial filter membrane 〇1 of the membrane module 102, and the liquid surface of the raw water in the open groove 103 is gradually become The top surface of the film module 1 〇 2 is lower or higher. Preferably, the membrane filtration flow rate at this filtration step is determined herein in the following manner. When the length of the filter 1 〇1 is L = 2m, the state of the partially exposed filter membrane 10 at the end of the filtration step or at the beginning of the filtration step relative to the liquid surface of the raw water in the open tank 103 is not in contact with the raw water. The length of 101 is L'=0.5m, and the membrane filtration flow rate in the normal filtration step is Fl=5.0m3/hr (single membrane module provides 5.0m3 of filtered water flow rate per hour), and partially exposed filter 1 The membrane filtration flow rate F 2 of the filtration step of 〇1 will be as follows:
F2 ^ Fix ( L-L5) /L ^ 5.0x ( ( 2.0-0.5) /2.0 ) ^3.7 5m3/hr (單薄膜模組之流率每小時提供 3.75m3的過濾 水）。此意指於此例中控制不超過3.75m3/hr之薄膜過濾 流率於部份暴露濾膜101之狀態。在部份暴露濾膜1〇1之 狀態中的過濾步驟，爲了防止已累積在未與原水接觸的濾 膜101上之懸浮物質的壓縮及濾膜101的乾化，較佳地， 達到在給定液體位準的早期到達及結束部份暴露的濾膜 1〇1的狀態之過濾步驟。 圖2顯示使用應用依據本發明的操作方法之以上薄膜 模組的流程的實例。原水1係由原水進給泵3送至安裝有 -17- (15) (15)1308504 薄膜模組之浸入開口箱1 1，且以吸入泵1 2獲得過濾水係 貯存於過濾水箱5，其亦作爲回洗箱。雖然過濾水箱5中 在回洗的時候係由回洗泵6送至將被回洗的薄膜模組，在 此這係可能以氧化劑進給泵8在自回洗泵6至薄膜模組的 管路的過程中將氧化劑箱7中的氧化劑加至回洗水。將空 氣導入薄膜模組之氣體洗滌係由將壓縮機9所壓縮的空氣 送至薄膜模組的原水側來完成的。在此將使用於氣體洗滌 之壓縮空氣源可以是取代壓縮機之鼓風機。 薄膜過濾裝置之操作方法通常是獲得過濾水的過濾步 驟、移除已累積在薄膜表面上之懸浮物質及自該系統排出 已累積於敞槽的懸浮物質之排泄步驟的組合。現在依據本 發明，較佳地實施過濾步驟A及物理清洗步驟（包括物 理清洗步驟A及B)，以及在一或更多次的重複過濾步驟 B及物理清洗步驟之後，自該系統排出敞槽中之廢水的總 量。 再者，當由重複過濾步驟及物理清洗步驟數次以使濃 度比達到給定位準時（回收比上升），較佳地由重複過濾 步驟及物理清洗步驟可能的最少次數以達到給定濃度比。 因此，作爲薄膜模組將安裝於薄膜過濾裝置之敞槽，較佳 地使用此種敞槽，該敞槽將最小化安裝的薄膜模組的部份 中的維持容積；也就是說，（=在自薄膜模組安裝部份的 容量減去構成薄膜模組之中空纖維薄膜的體積後之剩餘水 量）每單位薄膜容積之原水的量。 接著，將參照其實施例更詳細說明本發明。 -18- (16) (16)1308504 (實施例1 ) 所使用的薄膜模組（每一薄膜模組量測有6英吋的直 徑及2m的薄膜長’度）係三束（50m2的薄膜面積）〇」μπι 的額定孔尺寸的聚偏二氟乙烯（polyvinylidene fiuoride )製成的中空纖維型微過濾薄膜。薄膜模組的頂及底端係 由黏著所固定，其中在頂端面的中空纖維薄膜係開啓，而 在底端面的中空纖維薄膜係關閉。作爲薄膜模組直立安裝 於其中之敞槽，一敞槽被使用，其中該敞槽的薄膜模組安 裝部份將佔有0.109m2的安裝底空間及其有效水深度將爲 2.3m ’且用於儲存來自物理清洗的回洗廢水，0.25ιη2底面 積及〇.6m有效水深度的緩衝敞槽係設在敞槽上。 此薄膜過濾裝置的薄膜模組安裝部份中之維持容積， 也就是說，（=在自薄膜模組安裝部份的容量減去構成薄 膜模組之中空纖維薄膜的容積後之剩餘水量）每單位薄膜 面積之原水的量係1.3 6 L/m2。 由使用薄膜過濾裝置，連續操作係實施在作爲原水1 至3度混濁値的河水上。原水給進步驟、依據本發明的過 濾步驟及物理清洗步驟、及排泄步驟被結合作爲操作的步 驟。 關於操作的步驟之設定條件，在原水給進步驟，將送 入敞槽之原水的量被設定在12m3/hr。在過濾步驟，（步 驟1)當原水達到薄膜長度的一半時，過濾操作被啓動； 然後（步驟2)於浸漬所有薄膜之狀態中，過濾操作被實 -19- (17) (17)1308504 施達2 6分鐘’以及（步驟3 )立即在物理清洗步驟被實 施之前’過濾操作被繼續進行直到原水達到薄膜長度的一 半爲止。過濾操作被實施，其中差動薄膜壓力被施加至作 爲負壓側之薄膜的次要側。在各別過濾步驟之薄膜過濾流 率係6m3/hr ( 2m3/hr每一薄膜模組）在（步驟1)及（步 驟3 ) ’及12m3/hr ( 4m3/hr每一薄膜模組）在（步驟2 ) 。自（步驟1 )至（步驟3 )之總過濾過程持續期間係約 28分鐘。附帶地，在（步驟2)進給的原水量等於薄膜過 濾流率。 在過濾步驟的完成之後，物理清洗步驟被實施。在物 理清洗步驟，回洗及以空氣的氣體清洗被同時實施。回洗 的流率被設在12m3/hr ( 4m3/hr每一薄膜模組），而使用 氣體清洗之空氣的流率被設在l2Nm3/hr ( 4Nm3/hr每一薄 膜模組）。 在敞槽中的濃度係藉由重複過濾步驟及物理清洗步驟 5次來增加100倍之後（99.0%產量），排出敞槽中的濃 縮廢水之排泄步驟被實施。在排出物理清洗步驟中所剝離 的懸浮物質之排泄步驟，在安裝在敞槽的底部之壓力型液 體位準感測器檢測到槽中的水深來到之後，由安裝在 敞槽的底部符合：FIS之完全開口 80A管路以及保持該閥開 啓達1 5秒所排出之懸浮物質’濃縮的廢水係自敞槽完全 排出。 在這些操作條件下達約七個月之操作提供不超過 70kPa之薄膜間差動壓力，其顯示穩定操作係可能的。 -20- (18) (18)1308504 (實施例2) 量測有3英吋的直徑及lm的薄膜長度所使用之薄膜 模組係一束6.8m2薄膜面積的具有0.1μπ1額定孔尺寸之聚 偏二氟乙烯製成的中空纖維型微過濾濾膜。薄膜模組的頂 及底端係由黏著劑所固定，其中在頂端面之中空纖維薄膜 係開啓而在底端面的中空纖維薄膜係關閉。作爲薄膜模組 將被直立安裝的敞槽，薄膜模組安裝部份的槽將佔用 0.0134m2的安裝底面空間及其有效水深將爲〗.18m之敞槽 被使用’以及用於儲存使用在物理清洗的回洗廢水，具有 0.049m2底面積及〇.35m有效水深的緩衝槽係設在敞槽 上。 此薄膜過濾裝置的薄膜模組安裝部之維持真空，也就 是說’每單位薄膜面積的原水量（=在薄膜模組安裝部的 容量減去構成薄膜模組的中空纖維薄膜的體積之後剩餘的 水量），係 2.00L/m2。 藉由使用薄膜過濾裝置，連續操作係實施在作爲原水 之平均渾濁値爲10度及最大渾濁値爲200至300度的工 業水上。作爲操作的步驟’原水進給步驟、依據本發明之 過濾步驟及物理清洗步驟以及排泄步驟被結合。 關於操作步驟的設定條件，在原水進給步驟，將送入 敞槽之原水量被設在2m3/hr。在過濾步驟，（步驟])當 原水達到薄膜長度的一半時，過濾操作被啓動；則（步驟 2 )於浸入所有薄膜之狀態中，過濾操作被實施達20分 -21 - (19) (19)1308504 鐘，以及（步驟3 )立即在物理清洗步驟被實施之前，過 濾操作被實施在直到原水達到薄膜長度的一半。過濾操作 被實施，其中差動薄膜壓力被施加在作爲負壓側之薄膜的 次要側。在各別過濾步驟係〇.】m3/hr在（步驟1 )及（步 驟3 )以及0.1 7m3/hr在（步驟2 )之薄膜過濾流率。自 (步驟1 )至（步驟3 )之整個過率過程持序時間係約 22.0分鐘。 在過濾步驟的完成之後，物理清洗步驟被實施。在物 理清洗步驟，回洗及以空氣的氣體清洗被同時實施。回洗 的流率被設在〇.28m3/hr，而使用氣體清洗之空氣的流率 被設在1.2Nm3/hp 在敞槽中的濃度係藉由重複過濾步驟及物理清洗步驟 六次來增加2 0倍之後（9 5.0%產量），排出敞槽中的濃 縮廢水之排泄步驟被實施。在排出物理清洗步驟中所剝離 的懸浮物質之排泄步驟，藉由安裝在敞槽的底部之壓力型 液體位準感測器檢測到槽中的水深來到之後，由安裝 在敞槽的底部符合JIS之完全開口 50A管路以及保持該閥 開啓達5秒所排出之懸浮物質，濃縮的廢水係自敞槽完全 排出。 在這些操作條件下達約七個月之操作提供不超過 3 OkPa之薄膜間差動壓力，其顯示穩定操作係可能的。 (比較例1 ) 使用於比較例1之薄膜模組及薄膜過濾裝置係相同如 -22- (20) (20)1308504 使用餘實施例2的薄膜模組及薄膜過濾裝置β藉由使用薄 膜過濾裝置，連續操作係實施在作爲原水之平均渾濁値爲 10度及最大渾濁値爲200至300度的工業水上。作爲操 作的步驟，原水進給步驟、過濾步驟及物理清洗步驟以及 排泄步驟被結合。 關於操作步驟的設定條件，在原水進給步驟，將送入 敞槽之原水量被設在2m3/hr。在過濾步驟，爲了達到如實 施例2之濃度的相同位準，過濾操作係於浸入所有薄膜的 狀態實施達約120分鐘。附帶地，過濾操作被實施，其中 差動薄膜壓力被施加在作爲負壓側之薄膜的次要側。在過 濾步驟之薄膜過濾流率係〇.17m3/hr。 在過濾步驟的完成之後，物理清洗步驟被實施。在物 理清洗步驟，回洗及以空氣的氣體清洗被同時實施。回洗 的流率被設在0.28 m3/hr，而使用氣體清洗之空氣的流率 被設在 1.2Nm3/hr。 在敞槽中的濃度係藉由實施過濾步驟及物理清洗步驟 各一次來增加20倍之後（95.0%產量），排出敞槽中的 濃縮廢水之排泄步驟被實施。在排出物理清洗步驟中所剝 離的懸浮物質之排泄步驟，藉由安裝在敞槽的底部之壓力 型液體位準感測器檢測到敞槽中的水深來到0m之後，由 安裝在敞槽的底部之完全開口 5〇A管路以及保持該閥開 啓達5秒所排出之懸浮物質’濃縮的廢水係自敞槽完全排 出。 當操作係在這些操作條件實施達約兩週’薄膜間差動 -23 - (21) 1308504 壓力勝於80kP a ’使其不可能不再提供負壓，且穩定操作 • 變成不可能。 . 於實施例3中，如實施例1之相同說明的—薄膜模組 被使用。作爲薄膜模組直立安裝於其中之敞槽，一敞槽被 使用，其中該敞槽的薄膜模組安裝部份將佔有0.0 283m2 的安裝底空間及其有效水深度將爲2.72m，且用於儲存來 自物理清洗的回洗廢水’ 〇」26m2底面積及〇.46m有效水 • > 深度的緩衝槽係設在敞槽上。 此薄膜過濾裝置的薄膜模組安裝部份中之維持容積， 也就是說’（=在自薄膜模組安裝部份的容量減去構成薄 膜模組之中空纖維薄膜的容積後之剩餘水量）係 I .2 1 L/m2。 由使用薄膜過濾裝置，連續操作係實施在作爲原水5 度於平均混濁値及最大渾濁値爲300至500度的壩水。原 水給進步驟、依據本發明之過濾步驟及物理清洗步驟、以 ^ 1 及排泄步驟被結合作爲操作的步驟。 關於操作的步驟之設定條件，在原水給進步驟，將送 入敞槽之原水的量被設定在2 m 3/hr。在過濾步驟，（步驟 1 )當原水達到薄膜長度的一半時，過濾操作被啓動；然 ' 後（步驟2)於浸漬所有薄膜之狀態中，過濾操作被實施 ， 達]5分鐘’以及（步驟3)立即在物理清洗步驟被實施 之前’過濾操作被實施直到原水達到薄膜長度的一半爲 止。過濾操作被實施，其中差動薄膜壓力被施加至作爲負 壓側之薄膜的次要側。在各別過濾步驟之薄膜過濾流率係 -24- (22) (22)1308504 0.9m3/hr在（步驟1)及（步驟3)，及1.83m3/hr在（步 驟2)。自（步驟1)至（步驟3)之總過濾過程持續期 間係約1 7分鐘。 在過濾步驟的完成之後，物理清洗步驟被實施。在物 理清洗步驟，回洗及以空氣的氣體清洗被同時實施。回洗 的流率被設在2m3/hr，而使用氣體清洗之空氣的流率被設 在 4Nm3/hr。 在敞槽中的濃度係藉由重複過濾步驟及物理清洗步驟 六次來增加2 0倍之後（9 5.0%產量），排出敞槽中的濃 縮廢水之排泄步驟被實施。在排出物理清洗步驟中所剝離 的懸浮物質之排泄步驟，在安裝在敞槽的底部之壓力型液 體位準感測器檢測到敞槽中的水深來到0m之後，由安裝 在敞槽的底部之完全開口 50A管路以及保持該閥開啓達 1 5秒所排出之懸浮物質，濃縮的廢水係自敞槽完全排 在這些操作條件下達約八個月之操作提供不超過 3OkPa之薄膜間差動壓力，其顯示穩定操作係可能的。 (比較例2) 量測有6英吋的直徑及2m的薄膜長度所使用之薄膜 模組係一束50m2薄膜面積的具有0.1 μιη額定孔尺寸之聚 偏二氟乙烯製成的中空纖維型微過濾濾膜。薄膜模組的頂 及底端係由黏著劑所固定，其中在頂端面之中空纖維薄膜 係開啓而在底端面的中空纖維薄膜係關閉。作爲薄膜模組 -25- (23) (23)1308504 將被直立安裝的敞槽，具有0.] 73 τη2的底部面積及3.0m 的有效水深之敞槽被使用。 此薄膜過濾裝置的薄膜模組安裝部之維持真空，也就 是說，每單位薄膜面積的原水量（=在薄膜模組安裝部的 容量減去構成薄膜模組的中空纖維薄膜的體積之後剩餘的 水量），係 10.0L/m2。 藉由使用薄膜過濾裝置，連續操作係實施在作爲原水 之平均渾濁値爲5度及最大渾濁値爲300至500度的壩水 上。作爲操作的步驟，原水進給步驟、過濾步驟及物理清 洗步驟以及原水的固定排出部份的柱狀流步驟被結合。 關於操作步驟的設定條件，在原水進給步驟，將送入 敞槽之原水量被設在2m3/hr。在過濾步驟，過濾操作係於 浸入所有薄膜之狀態中實施達約1 5分鐘。過濾操作被實 施，其中差動薄膜壓力被施加在作爲負壓側之薄膜的次要 側。在過濾步驟之薄膜過濾流率係1.83m3/hr。 在過濾步驟的完成之後，物理清洗步驟被實施。在物 理清洗步驟，回洗及以空氣的氣體清洗被同時實施。回洗 的流率被設在2m3/hr，而使用氣體清洗之空氣的流率被設 在 4Nm3/hr。 部份的原水係恆定排出以提高至約5.9倍之敞槽中的 濃度（83%產量）。 在這些操作條件下達約四個月之操作提供不超過 40kPa之薄膜間差動壓力，其顯示穩定操作係可能的。 -26- (24) (24)1308504 (實施例4) 使用於實施例4之薄膜模組及薄膜過濾裝置係相同如 使用餘實施例I的薄膜模組及薄膜過濾裝置。藉由使用薄 膜過濾裝置’連續操作係實施在作爲原水之平均渾濁値爲 5至10度及最大渾濁値爲200至300度的河水上。次氯 化鈉被加至原水以使剩餘氯的濃度在約0.5mg/L。作爲操 作的步驟，原水進給步驟、依據本發明之過濾步驟及物理 清洗步驟以及排泄步驟被結合。 關於操作步驟的設定條件，在原水進給步驟，將送入 敞槽之原水量被設在13.5m3/hr。在過濾步驟，（步驟 1)當原水達到薄膜長度的一半時，過濾操作被啓動；然 後（步驟2)於浸漬所有薄膜之狀態中，過濾操作被實施 達26分鐘，以及（步驟3 )立即在物理清洗步驟被實施 之前，過濾捧作被實施直到原水達到薄膜長度的一半爲 止。過濾操作被實施，其中差動薄膜壓力被施加至作爲負 壓側之薄膜的次要側。在各別過濾步驟之薄膜過濾流率係 7.5m3/hr ( 2.5m3/hr每一薄膜模組）在（步驟1 )及（步 驟3 )，以及13.5m3/hr ( 4.5m3/hr每一薄膜模組）在（步 驟2)。自（步驟1)至（步驟3)之總過濾過程持續期 間係約28分鐘。 在過濾步驟的完成之後，物理清洗步驟被實施β在物 理清洗步驟，回洗及以空氣的氣體清洗被同時實施。回洗 的流率被設在20.25m3/hr(6.75Nm3/hr每一薄膜模組）， 而使用氣體清洗之空氣的流率被設在]2Nm3/hr ( 4Nm3/hr -27- (25) 1308504 每一薄膜模組）。 ^ 在敞槽中的濃度係藉由重複過濾步驟及物理清洗步驟 ， 兩次來增加20倍之後（95.0%產量），排出敞槽中的濃 縮廢水之排泄步驟被實施。在排出物理清洗步驟中所剝離 的懸浮物質之排泄步驟，在安裝在敞槽的底部之壓力型液 體位準感測器檢測到敞槽中的水深來到〇m之後，由安裝 在敞槽的底部之完全開口 50A管路以及保持該閥開啓達 •丨1 5秒所排出之懸浮物質，濃縮的廢水係自敞槽完全排 出。 在這些操作條件下達約一個月之操作提供不超過 5 OkPa之薄膜間差動壓力，其顯示穩定操作係可能的。 (比較例3 ) 使用於比較例3之薄膜模組及薄膜過濾裝置係相同如 使用實施例1的薄膜模組及薄膜過濾裝置。藉由使用薄膜 過濾裝置，連續操作係實施在作爲原水之平均渾濁値爲5 至10度及最大渾濁値爲200至300度的河水上。次氯化 鈉被加至原水以使剩餘氯的濃度在約0.5 m g/ L。作爲操作 的步驟，原水進給步驟、過濾步驟及物理清洗步驟以及排 泄步驟被結合。 關於操作步驟的設定條件，在原水進給步驟，將送入 敞槽之原水量被設在13.5m3/hr。在過濾步驟，過濾操作 被實施達約40分鐘於浸入所有薄膜之狀態中。過濾操作 被實施，其中差動薄膜壓力被施加在作爲負壓側之薄膜的 -28- (26) (26)1308504 次要側。在過濾步驟係13.5m3/hr ( 4.5Nm3/hr每一薄膜模 組）之薄膜過濾流率。 在過濾步驟的完成之後，物理清洗步驟被實施。在物 理清洗步驟，回洗及以空氣的氣體清洗被同時實施。回洗 的流率被設在20.2 5m3/hr ( 6.75Nm3/hr每一薄膜模組）， 而使用氣體清洗之空氣的流率被設在1 2Nm3/hr ( 4Nm3/hr 每一薄膜模組）。 在敞槽中的濃度係藉由實施過濾步驟及物理清洗步驟 各一次來增加20倍之後（95.0%產量），排出敞槽中的 濃縮廢水之排泄步驟被實施。在排出物理清洗步驟中所剝 離的懸浮物質之排泄步驟，藉由安裝在敞槽的底部之壓力 型液體位準感測器檢測到槽中的水深來到0m之後，由安 裝在敞槽的底部之完全開口 50A管路以及保持該閥開啓 達1 5秒所排出之懸浮物質，濃縮的廢水係自敞槽完全排 出。 當在這些操作條件下達約一週之操作、提供勝過 80kPa之薄膜間差動壓力時，使其不可能不再提供負壓， 且穩定操作變成不可能。 (工業利用性） 適當使用於濾膜施加至諸如河水、湖水、地下水、儲 存的水、二次流出物、工業流出物、污水或類似水的原水 或者濾膜施加至貴重品的分離或濃縮的這些領域係可能 的。 -29- (27) (27)1308504 【圖式簡單說明】 圖1 A係顯示正常過濾步驟的槪述之示意圖。 圖1 B係顯示部份暴露的濾膜的狀態中之過濾步驟的 槪要之示意圖。 圖2係顯示結合依據本發明之薄膜的清洗方法之處理 流程的實例之流程圖。 1主要元件符號說明】 1 :原水 3 ·原水進給栗 5 :過濾水箱 6 :回洗泵 7 ··氧化劑箱 8 =氧化劑進給泵 9 :壓縮機 Μ :電磁閥 U :浸入箱 1 2 :吸入泵 Ml :濾膜 102 :薄膜模組 :敞槽 F I :正常過濾步驟的薄膜過德流率 F2 :過濾器構件部份暴露的狀態之薄膜過濾流率 -30- (28) (28)1308504 _ L :濾膜之有效長度 L’ ：於濾膜部份地暴露的狀態中未與原水接觸之濾膜 的長度 -31 -F2 ^ Fix ( L-L5) /L ^ 5.0x ( ( 2.0-0.5) /2.0 ) ^3.7 5m3/hr (The flow rate of the single membrane module provides 3.75m3 of filtered water per hour). This means that the membrane filtration flow rate of not more than 3.75 m3/hr in this example is controlled to partially expose the membrane 101. In the filtration step in a state in which the filter membrane is partially exposed, in order to prevent the compression of the suspended matter accumulated on the membrane 101 which is not in contact with the raw water and the drying of the membrane 101, it is preferable to achieve The filtration step of the early arrival and end of the partially exposed filter membrane 1〇1 of the liquid level. Fig. 2 shows an example of the flow of the above film module using the operation method according to the present invention. The raw water 1 is sent from the raw water feed pump 3 to the immersed open box 1 1 to which the -17-(15) (15) 1308504 film module is mounted, and the filtered water is obtained by the suction pump 12 to be stored in the filtered water tank 5, which Also as a backwash box. Although the filter tank 5 is returned to the membrane module to be backwashed by the backwash pump 6 during backwashing, it is possible here to feed the pump 8 from the backwash pump 6 to the membrane module of the membrane module. The oxidant in the oxidizer tank 7 is added to the backwash water during the road. The gas washing system for introducing air into the membrane module is carried out by feeding the air compressed by the compressor 9 to the raw water side of the membrane module. The source of compressed air used for gas scrubbing herein may be a blower that replaces the compressor. The membrane filtration apparatus is generally operated by a filtration step of obtaining filtered water, a combination of removing the suspended matter accumulated on the surface of the membrane, and discharging the suspended matter accumulated in the open tank from the system. According to the present invention, it is preferred to carry out the filtration step A and the physical cleaning step (including the physical cleaning steps A and B), and after one or more repeated filtration steps B and physical cleaning steps, the open tank is discharged from the system. The total amount of wastewater in the process. Further, when the filtration step and the physical cleaning step are repeated several times to bring the concentration ratio to the timing of the positioning (the recovery ratio is increased), it is preferable to achieve the given concentration ratio by repeating the filtration step and the minimum number of possible physical cleaning steps. Therefore, as the film module is to be mounted in the open space of the membrane filtration device, it is preferred to use such an open groove which will minimize the maintenance volume in the portion of the installed membrane module; that is, (= The amount of raw water per unit film volume is subtracted from the capacity of the membrane module mounting portion minus the volume of the hollow fiber membrane constituting the membrane module. Next, the present invention will be described in more detail with reference to the embodiments thereof. -18- (16) (16)1308504 (Example 1) The film modules used (each film module measures 6 inches in diameter and 2m film length 'degrees) are three bundles (50m2 film) A hollow fiber type microfiltration membrane made of polyvinylidene fiuoride having a nominal pore size of "μπι". The top and bottom ends of the film module are fixed by adhesion, wherein the hollow fiber membrane at the top end is opened, and the hollow fiber membrane at the bottom end is closed. As an open slot in which the film module is erected, an open slot is used, wherein the open film module mounting portion will occupy an installation bottom space of 0.109 m2 and its effective water depth will be 2.3 m 'and The buffered open space from the physical cleaning, the 0.25 ft 2 bottom area and the 6.6 m effective water depth are placed on the open trough. The maintenance volume in the mounting portion of the membrane module of the membrane filtration device, that is, (= the amount of water remaining after subtracting the volume of the hollow fiber membrane constituting the membrane module from the capacity of the membrane module mounting portion) The amount of raw water per unit film area was 1.3 6 L/m2. By using a membrane filtration device, a continuous operation system is carried out on river water as a raw water of 1 to 3 degrees of turbidity. The raw water feeding step, the filtration step and the physical washing step according to the present invention, and the draining step are combined as steps of the operation. Regarding the setting conditions of the steps of the operation, in the raw water feeding step, the amount of raw water to be fed into the open tank was set at 12 m3/hr. In the filtration step, (Step 1), when the raw water reaches half the length of the film, the filtration operation is initiated; and then (Step 2) in the state of immersing all the films, the filtration operation is carried out by the actual operation - 19 - (17) (17) 1308504 Up to 6 minutes ' and (step 3) immediately before the physical washing step is carried out 'filtering operation is continued until the raw water reaches half the length of the film. A filtering operation is carried out in which a differential film pressure is applied to the secondary side of the film as the negative pressure side. The membrane filtration flow rate in each filtration step is 6m3/hr (2m3/hr per membrane module) at (step 1) and (step 3) ' and 12m3/hr (4m3/hr per membrane module) at (Step 2). The total filtration process from (Step 1) to (Step 3) lasts for about 28 minutes. Incidentally, the amount of raw water fed in (step 2) is equal to the membrane filtration flow rate. After the completion of the filtration step, the physical cleaning step is carried out. In the physical cleaning step, backwashing and air cleaning with air are simultaneously performed. The flow rate of backwashing was set at 12 m3/hr (4 m3/hr per membrane module), and the flow rate of air purged with gas was set at 12 Nm3/hr (4 Nm3/hr per membrane module). The concentration in the open tank was increased by 100 times by repeating the filtration step and the physical washing step 5 times (99.0% yield), and the draining step of discharging the concentrated waste water in the open tank was carried out. The draining step of the suspended material stripped during the discharge physical cleaning step is performed by the pressure type liquid level sensor installed at the bottom of the open tank after the water depth in the tank is detected, by the bottom mounted on the open tank: The FIS's fully open 80A line and the suspended solids discharged from the valve for up to 15 seconds are completely discharged from the open tank. Operation for up to seven months under these operating conditions provides differential pressure between the membranes of no more than 70 kPa, which indicates that a stable operating system is possible. -20- (18) (18)1308504 (Example 2) The film module used for measuring the diameter of 3 inches and the film length of lm is a bundle of 6.8 m2 film area with a nominal pore size of 0.1 μπι. A hollow fiber type microfiltration membrane made of vinylidene fluoride. The top and bottom ends of the film module are fixed by an adhesive, wherein the hollow fiber membrane at the top end is opened and the hollow fiber membrane at the bottom end is closed. As the open module of the film module will be installed upright, the groove of the film module mounting part will occupy 0.0134m2 of the installation bottom space and its effective water depth will be used for the .18m open groove 'and for storage and use in physics The washed backwashing wastewater has a buffer tank having a bottom area of 0.049 m 2 and an effective water depth of 〇35 m, which is provided on the open tank. The membrane module mounting portion of the membrane filtration device maintains a vacuum, that is, the amount of raw water per unit membrane area (= remaining after the capacity of the membrane module mounting portion minus the volume of the hollow fiber membrane constituting the membrane module) The amount of water) is 2.00 L/m2. By using a membrane filtration device, the continuous operation system is carried out on industrial water having an average turbidity of 10 degrees as raw water and a maximum turbidity of 200 to 300 degrees. As a step of the operation, the raw water feeding step, the filtering step according to the present invention, the physical washing step, and the draining step are combined. Regarding the setting conditions of the operation steps, in the raw water feeding step, the amount of raw water to be fed into the open tank is set at 2 m3/hr. In the filtration step, (step)) when the raw water reaches half the length of the film, the filtering operation is initiated; then (step 2) in the state of immersing all the films, the filtering operation is carried out for 20 minutes - 21 - (19) (19 ) 1308504 clock, and (step 3) immediately before the physical cleaning step is carried out, the filtering operation is carried out until the raw water reaches half the length of the film. A filtering operation is carried out in which a differential film pressure is applied to the minor side of the film as the negative pressure side. In the respective filtration steps, the membrane filtration flow rate of m3/hr in (step 1) and (step 3) and 0.17 m3/hr in (step 2). The entire over-rate course from (Step 1) to (Step 3) is about 22.0 minutes. After the completion of the filtration step, the physical cleaning step is carried out. In the physical cleaning step, backwashing and air cleaning with air are simultaneously performed. The flow rate of the backwashing is set at 〇28m3/hr, and the flow rate of the air purged with gas is set at 1.2Nm3/hp. The concentration in the open tank is increased by repeating the filtration step and the physical washing step six times. After 20 times (9 5.0% yield), the draining step of the concentrated waste water discharged from the open tank was carried out. The excretion step of the suspended material stripped during the discharge physical cleaning step is detected by the pressure type liquid level sensor installed at the bottom of the open tank, after the water depth in the tank comes, and is fitted by the bottom of the open tank JIS's fully open 50A line and the suspended material that is kept open for 5 seconds, the concentrated waste water is completely discharged from the open tank. Operation for up to about seven months under these operating conditions provides differential pressure between the membranes of no more than 3 OkPa, which indicates that a stable operating system is possible. (Comparative Example 1) The film module and the membrane filtration device used in Comparative Example 1 were the same as -22-(20) (20) 1308504. The film module and the membrane filtration device β of the second embodiment were used to filter by using a membrane. The apparatus, the continuous operation system is implemented on industrial water having an average turbidity of 10 degrees as raw water and a maximum turbidity of 200 to 300 degrees. As a step of the operation, the raw water feeding step, the filtering step, the physical washing step, and the draining step are combined. Regarding the setting conditions of the operation steps, in the raw water feeding step, the amount of raw water to be fed into the open tank is set at 2 m3/hr. In the filtration step, in order to achieve the same level of concentration as in Example 2, the filtration operation was carried out for about 120 minutes in a state of being immersed in all the films. Incidentally, a filtering operation is performed in which a differential film pressure is applied to the minor side of the film as the negative pressure side. The membrane filtration flow rate in the filtration step was 1717 m3/hr. After the completion of the filtration step, the physical cleaning step is carried out. In the physical cleaning step, backwashing and air cleaning with air are simultaneously performed. The flow rate of the backwashing was set at 0.28 m3/hr, and the flow rate of the air purged with gas was set at 1.2 Nm3/hr. The concentration in the open tank was increased by 20 times by performing the filtration step and the physical washing step, respectively (95.0% yield), and the draining step of discharging the concentrated waste water in the open tank was carried out. The excretion step of the suspended matter stripped during the discharge physical cleaning step is detected by the pressure type liquid level sensor installed at the bottom of the open tank, after the water depth in the open tank reaches 0 m, and is installed in the open groove The fully open 5 〇 A line at the bottom and the suspended solids discharged from the valve for 5 seconds to open are completely discharged from the open tank. When the operating system is implemented under these operating conditions for about two weeks, the inter-film differential -23 - (21) 1308504 pressure is better than 80kP a ', making it impossible to no longer provide negative pressure, and stable operation becomes impossible. In Embodiment 3, a film module as described in the same manner as in Embodiment 1 is used. As an open slot in which the film module is erected, an open slot is used, wherein the open film module mounting portion will occupy an installation bottom space of 0.0 283 m2 and its effective water depth will be 2.72 m, and Stores backwashed wastewater from physical cleaning '〇' 26m2 bottom area and 〇.46m effective water • > Depth buffer tank is located on the open tank. The maintenance volume in the mounting portion of the membrane module of the membrane filtration device, that is, '(= the amount of remaining water after subtracting the volume of the hollow fiber membrane constituting the membrane module from the capacity of the membrane module mounting portion) I .2 1 L/m2. By using a membrane filtration device, the continuous operation system is carried out in a dam water having an average turbidity of 5 degrees as the raw water and a maximum turbidity of 300 to 500 degrees. The raw water feeding step, the filtering step and the physical washing step according to the present invention, and the step of excretion are combined as steps of the operation. Regarding the setting conditions of the operation steps, in the raw water feeding step, the amount of raw water sent to the open tank was set at 2 m 3 /hr. In the filtration step, (Step 1), when the raw water reaches half the length of the film, the filtration operation is initiated; then [after (Step 2) in the state of immersing all the films, the filtration operation is carried out for 5 minutes' and (step 3) Immediately before the physical washing step is carried out, the 'filtration operation is carried out until the raw water reaches half the length of the film. A filtering operation is carried out in which a differential film pressure is applied to the minor side of the film as the negative pressure side. The membrane filtration flow rate at each filtration step was -24-(22) (22)1308504 0.9 m3/hr at (step 1) and (step 3), and 1.83 m3/hr at (step 2). The total filtration process from (Step 1) to (Step 3) lasts for about 17 minutes. After the completion of the filtration step, the physical cleaning step is carried out. In the physical cleaning step, backwashing and air cleaning with air are simultaneously performed. The flow rate of the backwashing was set at 2 m3/hr, and the flow rate of the air purged with gas was set at 4 Nm3/hr. The concentration in the open tank was increased by 20 times by repeating the filtration step and the physical washing step six times (9 5.0% yield), and the draining step of discharging the concentrated waste water in the open tank was carried out. The draining step of the suspended material stripped during the discharge physical cleaning step is installed at the bottom of the open tank after the pressure type liquid level sensor installed at the bottom of the open tank detects that the water depth in the open tank reaches 0 m. The fully open 50A line and the suspended material discharged by the valve for up to 15 seconds, the concentrated waste water is completely discharged from the open tank under these operating conditions for about eight months to provide an inter-film differential of no more than 3OkPa. Pressure, which shows a stable operating system is possible. (Comparative Example 2) A film module used for measuring a diameter of 6 inches and a film length of 2 m is a hollow fiber type microfiber made of polyvinylidene fluoride having a nominal pore size of 0.1 μm in a 50 m2 film area. Filter the filter. The top and bottom ends of the film module are fixed by an adhesive, wherein the hollow fiber membrane at the top end is opened and the hollow fiber membrane at the bottom end is closed. As a film module -25-(23) (23)1308504, an open groove to be installed upright, an open groove having a bottom area of 0.] 73 τη2 and an effective water depth of 3.0 m is used. The membrane module mounting portion of the membrane filtration device maintains a vacuum, that is, the amount of raw water per unit membrane area (= remaining after the capacity of the membrane module mounting portion minus the volume of the hollow fiber membrane constituting the membrane module) The amount of water) is 10.0 L/m2. By using a membrane filtration device, the continuous operation system is carried out on dam water having an average turbidity of 5 degrees as raw water and a maximum turbidity of 300 to 500 degrees. As a step of the operation, the raw water feeding step, the filtering step, the physical cleaning step, and the columnar flow step of the fixed discharge portion of the raw water are combined. Regarding the setting conditions of the operation steps, in the raw water feeding step, the amount of raw water to be fed into the open tank is set at 2 m3/hr. In the filtration step, the filtration operation is carried out in a state of being immersed in all the films for about 15 minutes. A filtering operation is carried out in which a differential film pressure is applied to the minor side of the film as the negative pressure side. The membrane filtration flow rate in the filtration step was 1.83 m3/hr. After the completion of the filtration step, the physical cleaning step is carried out. In the physical cleaning step, backwashing and air cleaning with air are simultaneously performed. The flow rate of the backwashing was set at 2 m3/hr, and the flow rate of the air purged with gas was set at 4 Nm3/hr. Part of the raw water system was continuously discharged to increase the concentration in the open tank (83% yield) to about 5.9 times. Operation for about four months under these operating conditions provides differential pressure between the membranes of no more than 40 kPa, which indicates that a stable operating system is possible. -26- (24) (24) 1308504 (Example 4) The film module and the membrane filtration device used in Example 4 were the same as those used in the film module and the membrane filtration device of Example I. The continuous operation system is carried out on a river water having an average turbidity of 5 to 10 degrees as raw water and a maximum turbidity of 200 to 300 degrees by using a membrane filtration device. Sodium hypochlorite was added to the raw water to bring the residual chlorine concentration to about 0.5 mg/L. As a step of the operation, the raw water feeding step, the filtering step according to the present invention, the physical washing step, and the draining step are combined. Regarding the setting conditions of the operation steps, in the raw water feeding step, the amount of raw water to be fed into the open tank was set at 13.5 m3/hr. In the filtration step, (step 1), when the raw water reaches half the length of the film, the filtration operation is initiated; then (step 2) in the state of immersing all the films, the filtration operation is carried out for 26 minutes, and (step 3) immediately Prior to the physical cleaning step being performed, the filter hand is carried out until the raw water reaches half the length of the film. A filtering operation is carried out in which a differential film pressure is applied to the minor side of the film as the negative pressure side. The membrane filtration flow rate at each filtration step was 7.5 m3/hr (2.5 m3/hr per membrane module) at (step 1) and (step 3), and 13.5 m3/hr (4.5 m3/hr per film). Module) is in (step 2). The total filtration process from (Step 1) to (Step 3) lasts for about 28 minutes. After the completion of the filtration step, the physical cleaning step is carried out by β in the physical cleaning step, and the backwashing and air cleaning with air are simultaneously performed. The flow rate of backwashing was set at 20.25 m3/hr (6.75 Nm3/hr per membrane module), and the flow rate of air purged with gas was set at 2 Nm3/hr (4Nm3/hr -27- (25) 1308504 per membrane module). ^ The concentration in the open tank is increased by 20 times (95.0% yield) by repeating the filtration step and the physical washing step, and the draining step of discharging the concentrated waste water in the open tank is carried out. The step of discharging the suspended matter peeled off during the discharge physical cleaning step, after the pressure type liquid level sensor installed at the bottom of the open tank detects that the water depth in the open groove reaches 〇m, is installed in the open groove The bottom of the fully open 50A line and the suspended material that is discharged from the valve for up to 15 seconds, the concentrated waste water is completely discharged from the open tank. Operation for about one month under these operating conditions provides differential pressure between the membranes of no more than 5 OkPa, which indicates that a stable operating system is possible. (Comparative Example 3) The film module and the membrane filtration device used in Comparative Example 3 were similarly used as in the film module and the membrane filtration device of Example 1. By using a membrane filtration device, the continuous operation system is carried out on river water having an average turbidity of 5 to 10 degrees as raw water and a maximum turbidity of 200 to 300 degrees. Sodium hypochlorite is added to the raw water to bring the residual chlorine concentration to about 0.5 m g/L. As a step of the operation, the raw water feeding step, the filtering step, the physical washing step, and the draining step are combined. Regarding the setting conditions of the operation steps, in the raw water feeding step, the amount of raw water to be fed into the open tank was set at 13.5 m3/hr. In the filtration step, the filtration operation was carried out for about 40 minutes in a state of immersing in all the films. A filtering operation was carried out in which the differential film pressure was applied to the secondary side of the -28-(26) (26) 1308504 which is the film on the negative pressure side. The filtration step was a membrane filtration flow rate of 13.5 m3/hr (4.5 Nm3/hr per membrane module). After the completion of the filtration step, the physical cleaning step is carried out. In the physical cleaning step, backwashing and air cleaning with air are simultaneously performed. The backwash flow rate was set at 20.2 5 m3/hr (6.75 Nm3/hr per membrane module), and the flow rate of air purged with gas was set at 1 2 Nm3/hr (4 Nm3/hr per membrane module) . The concentration in the open tank was increased by 20 times by performing the filtration step and the physical washing step, respectively (95.0% yield), and the draining step of discharging the concentrated waste water in the open tank was carried out. The excretion step of the suspended matter peeled off during the discharge physical cleaning step is detected by the pressure type liquid level sensor installed at the bottom of the open tank, after the water depth in the tank reaches 0 m, and is installed at the bottom of the open tank The fully open 50A line and the suspended matter discharged by the valve for up to 15 seconds are discharged, and the concentrated waste water is completely discharged from the open tank. When operating under these operating conditions for about one week, providing differential pressure between films of more than 80 kPa, it is impossible to provide no negative pressure any more, and stable operation becomes impossible. (Industrial Applicability) Appropriately applied to the separation or concentration of the filter applied to valuables such as river water, lake water, ground water, stored water, secondary effluent, industrial effluent, sewage or water-like raw water or filter. These areas are possible. -29- (27) (27)1308504 [Simple description of the diagram] Figure 1A shows a schematic diagram of the normal filtering step. Figure 1B is a schematic view showing the filtration step in the state of a partially exposed filter. Fig. 2 is a flow chart showing an example of the processing flow of the cleaning method in combination with the film according to the present invention. 1 Description of main components: 1 : Raw water 3 · Raw water feed pump 5 : Filter water tank 6 : Backwash pump 7 · · Oxidizer tank 8 = Oxidizer feed pump 9 : Compressor Μ : Solenoid valve U : Immersion tank 1 2 : Suction pump Ml: Membrane 102: Membrane module: Open trough FI: Membrane flow rate F2 of normal filtration step: Membrane filtration flow rate of partially exposed state of filter member -30- (28) (28)1308504 _ L : effective length L' of the filter: the length of the filter that is not in contact with the raw water in the partially exposed state of the filter -31 -