1235682 玖、發明說明： 【發明所屬之技術領域】 本發明係關於一種分離膜模組及分離膜模組之運轉方 法，可有效除去蓄積於繞捲在螺旋型膜元件上的原水隔片 上的濁質。 【先前技術】 以往，作為獲得海水的淡水化、超純水、各種製造製程 用水的方法，已知曉有使用以逆滲透膜（R 0膜）、毫微過濾 膜（N F膜）作為透過膜的螺旋型膜元件，而從原水中將離子 成份或低分子成份分離的方法。另外，在分離低分子及高 分子成份或在低分子及高分子成份内僅分離高分子成份的 限外過濾法、及分離微粒子的精密過濾法中，也使用螺旋 型膜元件。如圖8所例示，以往所使用的螺旋型膜元件的 一例，係藉由在透過水隔片8 2的兩面使逆滲透膜81重疊 而接合著3條邊以形成袋形膜8 3，將該袋形膜8 3的開口 部安裝於透過水集水管8 4，與網狀的原水隔片8 5 —起以 螺旋狀繞捲在透過水集水管8 4的外周面上而構成。接著， 從螺旋型膜元件8 0的一端的端面側8 9 a供給原水8 6，沿 著原水隔片8 5流動，並從螺旋型膜元件8 0的另一端的端 面側8 9 b作為濃縮水8 8而排出。原水8 6係在沿著原水隔 片85流動的過程中，透過逆滲透膜81而成為透過水87。 該透過水8 7係沿著透過水隔片8 2流入透過水集水管8 4 的内部，並從透過水集水管8 4的端部排出。如此，藉由配 置於被繞捲的袋形膜8 3間的原水隔片8 5而形成原水路徑。 5 312/發明說明書(補件)/92-11 /92122684 1235682 另外，以往係採用將安裝著上述螺旋型膜元件的分離膜 模組依每一段並行排列配置為1座或2座以上的分離膜裝 置群，連接成2段以上的多段式分離膜裝置，用以提高水 的回收率及水的處理量。例如，在圖9之多段式分離膜裝 置9 0中，藉由水泵9 1所供給的原水通過原水供給主配管 9 2、原水供給分歧配管9 3 a及9 3 b，由並行排列的第1段 的分離膜模組9 4 a及9 4 b進行處理，並藉由透過水流出配 管9 6 a及9 6 b獲得透過水，而藉由濃縮水流出配管9 5 a及 9 5 b獲得濃縮水。從該分離膜模組9 4 a及9 4 b流出的該濃 縮水係由濃縮水集水配管9 7 a及9 7 b來集水，從中間濃縮 水供給主配管（後段的原水供給主配管）9 8而於第2段的分 離膜模組9 9進行通水。於是，即可從透過水流出配管1 0 1 獲得透過水，而從濃縮水流出配管1 0 0獲得濃縮水。如上 述般，利用將在前段所得到的中間濃縮水作為後段的分離 膜模組的供給水進行處理，以提升水的回收率，另外，利 用於每一段並行排列配置複數個分離膜模組，以增加水的 處理量。 在以如此般構成的逆滲透膜螺旋型膜元件，用以得到海 水的淡化、超純水、各種製造製程用水的情況，通常係以 除去原水的濁質等為目的而進行前處理。進行該種前處 理，係為了如下的目的，即、為了盡量不斷能確保原水流 路及增加與逆滲透膜的接觸面積，通常，逆滲透膜螺旋型 膜元件的原水隔片的厚度，係設為1 m m以下的較薄膜厚， 因而有濁質被蓄積於原水流路上的原水隔片上，成為容易 6 312/發明說明書(補件)/92-11 /92122684 1235682 阻塞原水流路的構造的情況，為此，需要預先除去原水中 的濁質以避免因濁質蓄積引起的通水壓差的上升及透過水 量、透過水質的降低，而可長期間保持穩定的運轉。此種 以除濁為目的的前處理裝置，例如，係包含有凝集污泥處 理、過濾處理及膜處理等的各裝置者，此等設置有不僅使 得設置成本、運轉成本上升，同時，還需要大的設置面積 等的問題。 但是，若可將對於安裝著螺旋型膜元件的分離膜模組的 前處理裝置省略的話，即可無前處理而將工業用水或自來 水供給逆滲透膜模組，從而可達成系統的簡略化、設置面 積的減低及低成本化，而可極大地提高產業上的利用價 值。據此，若開發具有不易蓄積濁質的構造的原水隔片、 或是，即便濁質蓄積於原水隔片上，但利用運轉方法的改 變或沖洗等仍可除去濁質的方法，將成為極為有用的技 術。尤其是，利用運轉方法的改變或沖洗等以除去濁質的 方法，因其具有可直接利用於習知的螺旋型膜元件的情 況，而不失為一最佳選擇。 曰本特開平1 1 - 1 〇 4 6 3 6號公報中揭示有，以與通常的原 水流動相反的方向的逆方向的流向，供給加壓後的氣液二 層流，以便逆向沖洗逆滲透膜模組的方法。但是，該逆向 沖洗僅除去黏著於中空絲型逆滲透膜模組的該中空絲膜面 上的濁質，但並無法除去黏著於螺旋型逆滲透膜模組的原 水隔片上的濁質。 因此，本發明之目的在於，提供一種分離膜模組及分離 7 312/發明說明書(補件)/92-11 /92122684 1235682 膜模組之運轉方法，可有效除去蓄積於繞捲在 件上的原水隔片上的濁質。 【發明内容】 在上述實際情況中，本發明者經過刻意檢討 現在透過水集水管的外周面安裝著將袋形分離 片一起繞捲而組成的螺旋型膜元件的分離膜模 中的濁質係蓄積在與原水隔片的線材交叉的交 現象；在分離膜模組的運轉時，藉由定期或不 反方向邊改變原水的流動方向邊進行運轉，即 蓄積於原水隔片上的濁質的現象；在原水的流 時，利用進行複數次的沖洗（f 1 u s h i n g )，可以 除去效果的現象；及在分離膜模組的運轉方法 進行沖洗的同時，每次沖洗中的最初階段所進 係以與該沖洗剛開始前流動過來的原水流動方 向來進行，可進一步增大濁質的除去的現象等 了本發明。 也就是說，本發明提供一種分離膜模組的運 為安裝著將袋形分離膜與原水隔片一起繞捲在 管的外周面而組成的螺旋型膜元件的分離膜模 法（以下，又稱為分離膜模組的運轉方法（I )) 將安裝著並行排列配置為1座或2座以上的螺 的前段分離膜模組或分離膜模組群的中間水， 裝著並行排列配置為1座或2座以上的螺旋型 段分離膜模組或分離膜模組群的2段以上的多 312/發明說明書(補件)/92] 1 /92122684 螺旋型膜元 的結果，發 膜與原水隔 組中，原水 叉點部份的 定期向著相 可容易除去 動方向改變 增大濁質的 中，在適宜 行的沖洗， 向相反的方 ，進而促成 轉方法，係 透過水集水 組的運轉方 ，或是，為 旋型膜元件 順序供給安 膜元件的後 段式分離膜 8 1235682 模組的運轉方法（以下，又稱為分離膜模組的運轉方法 (Π )，另外，又稱上述分離膜模組的運轉方法（I )或分離 膜模組的運轉方法（Π)，為分離膜模組的運轉方法（I )或 (π ))，其定期或不定期向著相反方向改變該分離膜模組的 原水的流動方向。藉由採用上述構成方法，可容易剝落除 去蓄積於原水隔片的交叉點部份上的濁質。 另外，本發明提供一種分離膜模組的運轉方法（I )或 (Π )，其在原水的流動方向改變時，從兩個方向交錯進行 複數次的沖洗。藉由採用上述構成方法，可確實除去蓄積 於原水隔的交叉點部份上的濁質。 另外，本發明提供一種分離膜模組的運轉方法（I )或 (π )，其每次沖洗中的最初階段所進行的沖洗，係以與該 沖洗剛開始前流動過來的原水流動方向相反的方向來進 行。藉由採用上述構成方法，利用最初的沖洗有效剝離、 而容易除去蓄積於原水隔片的交叉點部份上的濁質。 另外，本發明提供一種分離膜模組的運轉方法（I )或 (Π )，係為安裝著將袋形分離膜與原水隔片一起繞捲在透 過水集水管的外周面而組成的螺旋型膜元件的分離膜模組 的運轉方法，該運轉方法係於途中包含有一次至多次的沖 洗，該沖洗中的最初階段所進行的沖洗，係以與該沖洗剛 開始前流動過來的原水流動方向相反的方向來進行。藉由 採用上述構成方法，可獲得與上述發明相同的效果。 另外，本發明提供一種分離膜模組的運轉方法（I )或 (Π )，係於沖洗時將透過水側的閥全部關閉。若打開透過 9 312/發明說明書(補件)/92-11/92122684 1235682 水側的閥，在高壓用分離膜模組的情況，在沖洗 則無屬沖洗液的原水透過，但在低壓或超低壓用 組卻透過原水，以致產生沖洗流量減低，且水質 透過的問題。 另外，還有藉由在剛關閉透過水側的閥後所產 以使沉積於膜面的污染物質浮游的效果，其可進 沖洗效果。 另外，本發明提供一種分離膜模組的運轉方法 (Π )，其於上述沖洗進行前，抽去原水供給側的 為利用抽去原水供給側的壓力，可解除抵壓於膜 力，因此，使得膜略微浮起，而可使蓄積於膜面 片的濁質浮游。 另外，本發明提供一種分離膜模組的運轉方法 (Π )，其將上述多段式分離膜模組的沖洗，分為 一分離膜模組、或每一分離模組群來進行。藉由 構成方法，可防止從前段的螺旋型膜元件剝離的 後段的螺旋型膜元件，而可防止污染。 另外，本發明提供一種分離膜模裝置，其具備 第1配管，係連接原水供給水泵與第1閥；原水 配管，係連接第1閥與分離膜模組；該分離膜模 水流出配管，係連接於該分離膜模組的透過水側 向轉換用配管，具有連接該原水供給第1配管與 模组的濃縮水流出側的濃縮水流出第1分歧配管 閥；及濃縮水流出第2分歧配管，從原水供給第 312/發明說明書(補件)/92-11/92122684 壓力程度 分離膜模 降低的水 生的背壓 一步增加 (I )或 壓力。因 面的壓 及原水隔 (I )或 各段的每 採用上述 濁質流向 原水供給 供給第2 組；透過 ;流動方 該分離膜 與第2 2配管進 10 1235682 行分歧，流出與原水的流動方向成為相反方向的情況 縮水。藉由採用上述構成裝置，可以簡單的裝置確實 上述分離膜模組的運轉方法（I )。 另外，本發明提供一種多段式分離膜模裝置，係為 前段的分離膜裝置或分離膜裝置群的分離膜模組所獲 中間濃縮水，順序供給後段的分離膜裝置或分離膜裝 的分離膜模組的2段以上的多段式分離膜模裝置，構 分離膜裝置或分離膜裝置群的分離膜裝置，具備原水 第1配管，係連接於第1閥；原水供給第2配管，係 第1閥與分離膜模組；該分離膜模組；透過水流出配 係連接於該分離膜模組的透過水側；流動方向轉換用 管，連接該原水供給第1配管與該分離膜模組的濃縮 出側，且設有第2閥；濃縮水流出第1配管，係與該 方向轉換用配管連接，且設有第3閥；及濃縮水流出 配管，係從該原水供給第2配管進行分歧，且設有第^ 藉由採用上述構成裝置，可以簡單的裝置確實實施上 離膜模組的運轉方法（Π )。 【實施方式】 以下，參照圖1來說明本發明之第1實施形態之分 模組的運轉方法。圖1為顯示實施本例之運轉方法之 透膜裝置的流程圖。圖1中，逆滲透膜裝置1 0具備： 供給第1配管1 2，係連接原水供給水泵1 1與第1閥 水供給第2配管1 3，係連接第1閥a與逆滲透膜模組 該逆滲透膜模組1 0 A ;透過水流出配管1 4，係連接於 312/發明說明書(補件)/92-11 /92122684 的濃 實施 將從 得的 置群 成該 供給 連接 管， 配 水流 流動 第2 閥。 述分 離膜 逆滲 原水 i ;原 1 0A； 該逆 11 1235682 滲透膜模組1 Ο A的透過水側；流動方向轉換用配管1 5，具 有連接該原水供給第1配管1 2與該逆滲透膜模組1 Ο A的濃 縮水流出側的濃縮水流出第1分歧配管1 51與第2閥b ; 及濃縮水流出第2分歧配管1 2 1，從原水供給第2配管1 3 進行分歧，流出與原水的流動方向相反方向的情況的濃縮 水。另外，在濃縮水流出第1分歧配管1 5 1途中附設有閥 c ° 在逆滲透膜裝置1 0中，首先，關閉第2閥b及閥d，以 將模組内形成為指定的壓力的方式來調整閥c，並打開第1 閥a及閥e。原水係藉由原水供給水泵1 1而供給逆滲透膜 模組1 Ο A。原水經由逆滲透膜模組1 Ο A處理，從濃縮水流 出第1分歧配管1 5 1得到濃縮水，同時，從透過水流出配 管1 4得到透過水。該情況，雖也依原水的濁度而定，但隨 著運轉時間的經過，在繞捲於元件上的原水隔片上漸漸蓄 積著原水中的濁質等的浮游物質。 當在原水隔片上蓄積有原水中的濁質時，其通水壓差將 上升。在如此之情況，將原水的流動方向改變為反方向。 也就是說，關閉第1閥a及閥c，以將模組内形成為指定 的壓力的方式來調整閥d，並打開第2閥b。藉此，原水係 由逆滲透膜模組1 Ο A的濃縮水流出側流入，經由逆滲透膜 模組1 Ο A處理，從濃縮水流出第2分歧配管1 2 1得到濃縮 水，同時，從透過水流出配管1 4得到透過水。藉由將如此 的原水的流動方向改變為相反方向，可容易剝落除去蓄積 於原水隔片的交叉點部份上的濁質。然後，因為隨著運轉 12 312/發明說明書(補件)/92-11/92122684 1235682 時間的經過，在安裝於元件上的原水隔片上再度蓄 水中的濁質等的浮游物質，因此，再度將原水的流 改變為相反方向。以後，反覆進行此種操作。原水 方向的改變時期係定期或不定期，因此作為改變原 動方向的間隔，可為1小時〜24小時，最好為1小 小時。若未滿1小時，轉換閥的轉換次數增多，將 換閥的壽命降低。另外，若超過24小時，則不易除 的濁質。另外，原水的流動方向的改變時期也可如 在成為指定的通水壓差的時點進行改變，該情況， 頻繁進行改變操作，還可除去蓄積的濁質，因此較J 另外，也可組合在指定時間經過後改變流動方向的 及在成為指定的通水壓差的時點進行改變的方法的 根據本例的逆滲透膜裝置1 0，因為使原水的流動 成為相反方向以抑制濁質的蓄積，因而可省略以往 中用以除去原水中的濁質的目的的凝集污泥處理、 理及膜處理等的前處理裝置的設置。因此，在達成 簡略化、設置面積的減低及低成本化方面，可獲得 效果。 其次，參照圖1來說明本發明之第2實施形態之 模組的運轉方法。第2實施形態例係於第1實施形 滲透膜模組的運轉方法中，在原水的流動方向改變 兩個方向交錯進行複數次的沖洗，藉此，可確實除 於原水隔片的交叉點部份上的濁質。作為從逆滲透 的兩個方向交錯進行複數次的沖洗的方法，可列舉 312/發明說明書(補件)/92-11 /92122684 積著原 動方向 的流動 水的流 時〜1 2 使得轉 去蓄積 上述， 因不用 理想。 方法， 兩者。 方向形 之技術 過丨慮處 系統的 預期的 分離膜 態之逆 時，從 去蓄積 膜模組 出使最 13 1235682 初階段所進行的沖洗以與該沖洗剛開始前流動過來的原水 流動方向相反的方向來進行的方法（以下，又稱為逆方向沖 洗）；及以與該沖洗剛開始前流動過來的原水流動方向相同 的方向來進行的方法，其中，逆方向沖洗利用最初階段所 進行的沖洗可有效剝離蓄積於原水隔片的交叉點部份上的 濁質，因此較為理想。若使最初階段所進行的沖洗與該沖 洗剛開始前流動過來的原水流動方向為相同的方向，雖可 除去一部份的濁質，但反而也會抵壓蓄積於原水隔片的滯 留部份上的濁質，隨著時間的推移而成為蓄積的濁質。逆 方向沖洗之進行，首先，關閉第1閥a及閥c，打開第2 閥b及閥d。然後，將透過處理之原水供給量的約3倍流 量的原水從濃縮水流出側急速供給逆滲透膜模組内，並藉 由原水流入側的原水供給第2配管1 3及濃縮水流出第2 分歧配管1 2 1排出即可。逆方向沖洗結束後，隨後再進行 與逆方向沖洗時之沖洗方向相反方向的沖洗。也就是說， 關閉第2閥b及閥d，打開第1閥a及閥c。以與逆方向沖 洗相同流量的原水從原水流入側急速供給逆滲透膜模組 内，並藉由濃縮水流出側的濃縮水流出第1分歧配管1 5 1 排出。接著，進行與該沖洗時之沖洗方向為相反方向的沖 洗，以後反覆進行相同的操作，即可從兩方向交錯進行複 數次的沖洗。 在最初階段所進行的沖洗與該沖洗剛開始前流動過來 的原水流動方向為相同方向的情況，係先進行上述逆方向 沖洗的情況的第2操作。如此般，藉由從兩方向交錯進行 14 312/發明說明書(補件)/92-11/92122684 1235682 複數次的沖洗，蓄積於原水隔片上的濁質被剝離而確實排 除於元件之外。在進行如此之沖洗的情況，在圖1中，係 藉由濃縮水流出側的壓力調整用的閥c或閥d來進行壓力 開放，但是，作為該壓力開放的方法，並不限定於此，也 可另外設置壓力開放用的閥。該情況，濃縮水流出配管為 取得較多的排出量，而以設置為較具有壓力調整用的閥之 配管之管徑更大管徑為佳。另外，也可在濃縮水流出第1 分歧配管1 5 1及濃縮水流出第2分歧配管1 2 1配置空氣室 (airchamber)(未圖示），藉由運轉而使用蓄積的水進行沖 洗。在此所謂之空氣室係指藉由濃縮水的壓力而加壓的空 氣，使得蓄積於室中的水流出的裝置。 在原水的流動方向改變時，從兩個方向交錯進行複數次 的沖洗的情況，於上述沖洗進行前，抽去原水供給側的壓 力，因為抽去至此為止抵壓於膜面的壓力，使得膜略微浮 起，因而，抽去原水供給側的壓力，因可使蓄積於膜面及 原水隔片的濁質浮游而較為理想。作為抽去原水供給側的 壓力的方法，可列舉出在原水供給水果1 1的排水側的原水 供給第1配管1 2設置排放配管（未圖示），在排放配管途中 附設閥（未圖示），並打開該閥的方法，或是，在將第1閥 a、閥c及閥e打開的運轉中，打開附設於濃縮水流出第2 分歧配管1 2 1的閥d的方法。至於閥的開放速度並無特別 的限制，但是，以瞬間、最好為1秒以内全開閥者為佳。 瞬間減壓的方法較易使膜浮起，另外還可期待因水擊作用 引起的濁質排除效果。另外，該情況最好打開透過水側的 15 312/發明說明書(補件)/92-11/92122684 1235682 閥e。這是因為關閉閥e時膜間壓差消失，而抵壓於膜的 外力亦消失，因此，例如即便抽去原水供給側的壓力，仍 無膜浮起的情況的緣故。 另外，在沖洗時最好將附設於透過水流出管1 4的閥e 全部關閉。若打開附設於透過水流出管1 4的閥e，在高壓 用逆滲透膜模組的情況，在沖洗壓力程度則無屬沖洗液的 原水透過，但在低壓或超低壓用逆滲透膜模組卻有透過原 水，以致產生沖洗流量減低，且水質降低的水透過的問題。 另外，還有藉由在剛關閉附設於透過水側的閥後所產生的 背壓以使沉積於膜面的污染物質浮游的效果，其可進一步 增加沖洗效果。 上述沖洗最好從兩方向交錯進行2次以上、5次以下的 沖洗。該沖洗次數為一次時變得僅為單一方向的沖洗，因 此洗淨效果不夠充分，而有隨著時間的推移而成為蓄積的 濁質的情況。另一方面，若超過5次時，排出的水增多而 降低了回收率。另外，沖洗的每一次的時間並無特別的限 定，但最好為3 0秒〜1 2 0秒。若不滿3 0秒則洗淨效果不 夠充分，若超過1 2 0秒則排放時間增長，使得回收率大幅 降低。另外，也可在沖洗時對於原水中供給壓縮空氣。藉 由將壓縮空氣混入原水中，可進一步提高洗淨效率。壓縮 空氣的供應量並無特別的限定，但最好原水與空氣的體積 比為2 : 1〜1 : 2。 在進行了指定時間的沖洗後，再度進行原水的處理。該 情況，原水的流動方向與最初階段所進行的沖洗剛開始前 16 312/發明說明書(補件)/92-11/92122684 1235682 流動過來的原水流動方向相反。也就是說，關閉第1閥a 及閥c，以將模組内形成為指定的壓力的方式來調整閥d， 並打開第2閥b及閥e，而原水係經由逆滲透膜模組1 0 A 處理。如此般，順序反覆進行原水處理—沖洗—原水處理 —沖洗。原水處理時間可為1小時〜24小時，最好為1小 時〜1 2小時。若原水處理時間未滿1小時，轉換閥的轉換 次數增多，將使得轉換閥的壽命降低，同時連帶造成回收 率的下降。另外，若超過24小時，將招致蓄積的濁質的除 去效果的降低。另外，作為從原水處理轉換為沖洗的形態， 可列舉出在每一次相同時間經過後改變流動方向的方法， 在成為指定的通水壓差的時點進行改變的方法，以及以此 等的組合進行改變的方法。 再者，參照圖1來說明本發明之第3實施形態之分離膜 模組的運轉方法。本例之分離膜模組的運轉方法，係為安 裝著螺旋型膜元件的分離膜模組的運轉方法，該運轉方法 係於途中包含有沖洗，該沖洗中的最初階段所進行的沖 洗，係以與該沖洗剛開始前流動過來的原水流動方向相反 的方向來進行的方法。也就是說，第3實施形態係為在沖 洗後，可將原水流動方向與沖洗剛開始前流動過來的原水 流動方向形成為相同方向，也可形成為相反方向，除此之 外，與第2實施形態例相同。藉此，原水處理時的原水的 最佳形態、沖洗時的閥類的操作形態及沖洗方法的最佳形 態等均與第2實施形態例相同。在第3實施形態例中，在 沖洗時利用反方向的流動可充分除去濁質，因此可獲得與 17 312/發明說明書(補件)/92-11 /92122684 1235682 第2實施形態例相同的效果。 再者，參照圖2來說明本發明之第4實施形態之分離膜 模組的運轉方法。圖2中，對與圖1中相同的構成要件則 賦予相同的元件符號，並省略其說明，以下主要針對各差 異點進行說明。也就是說，圖2中，與圖1的差異點係為 在逆滲透膜模組1 Ο A的下游側設置後段的逆滲透膜模組 1 Ο B，前段的逆滲透膜模組1 Ο A及後段的逆滲透膜模組1 Ο B 係由將前段的逆滲透膜模組1 Ο A的透過水作為後段裝置的 被處理水而供給的一次透過水流出配管1 4所連接，具備將 透過水排出於後段的逆滲透膜模組1 Ο B的透過水流出配管 1 6及使濃縮水返回至原水供給水泵之前的返回配管1 8。另 外，於後段的逆滲透膜模組1 Ο B具備濃縮水流出配管1 7。 前段的逆滲透膜模組1 Ο A係使用本發明的逆滲透膜裝置， 後段的逆滲透膜模組1 Ο B係使用習知的逆滲透膜裝置。也 就是說，在逆滲透膜裝置1 0 a中，原水係藉由原水供給水 泵1 1而供給前段的逆滲透膜模組1 Ο A。原水經由前段的逆 滲透膜模組1 Ο A處理，而從濃縮水流出配管1 5得到一次濃 縮水，同時從透過水流出配管1 4得到一次透過水。接著， 該一次透過水經由後段的逆滲透膜模組1 Ο B處理，而從透 過水流出配管1 6得到二次透過水，同時二次濃縮水從返回 配管1 8返回至原水供給水泵之前。該二次濃縮水係為將已 由前段的逆滲透膜模組1 Ο A脫氣的透過水，再經由後段的 逆滲透膜模組1 Ο B所濃縮者，與原水相比其導電率低。因 此，使得二次濃縮水的全量的循環成為可能，而可提升水 18 312/發明說明書(補件)/92-11 /92122684 1235682 回收率。如此，在逆滲透膜裝置1 0 a中，本發明所適用的 部份為前段的逆滲透膜模組1 Ο A。逆滲透膜裝置1 0 a也可 取代習知型之裝置所使用的僅以濁質除去為目的的前處理 裝置，而於前段使用可實施本發明之運轉方法的逆滲透膜 模組，因此，實質上可2段使用逆滲透膜。習知型之裝置 的前處理裝置當然無脫氯功能，因此逆滲透膜裝置1 0 a與 習知型之逆渗透膜裝置比較，其透過水的水質也極為優良。 再者，參照圖3來說明本發明之第5實施形態之分離膜 模組的運轉方法。圖3為實施本例之運轉方法之多段式分 離膜裝置的流程圖。多段式分離膜裝置2 8係為將從前段分 離膜裝置群2 9 a的各分離膜模組3 0 a、3 0 b所得到的中間濃 縮水，供給後段的分離膜裝置群2 9 b的分離膜模組4 8的2 段的多段式分離膜裝置。也就是說，將具備分離膜模組3 0 a 的分離膜裝置3 1 a及具備分離膜模組3 0 b的分離膜裝置 3 1 b並行排列配置而構成前段分離膜裝置群2 9 a，將分離膜 裝置群2 9 b配置於其後段而構成2段的分離膜裝置。 圖3中，分離膜裝置31 a具備：原水供給第1配管3 2 a， 係連接於閥a 1 ;原水供給第2配管3 3 a，係連接閥a 1與分 離膜模組3 0 a ;該分離膜模組3 0 a ;透過水流出配管3 4 a， 具有連接於該分離膜模組3 0 a的透過水側的閥e 1 ;流動方 向轉換用配管3 5 a，係連接該原水供給第1配管3 2 a與該 分離膜模組3 0 a的濃縮水流出侧，且具有閥b 1 ;濃縮水流 出第1分歧配管3 6 a，與流動方向轉換用配管3 5 a連接， 且附設有閥c 1 ;及濃縮水流出第2分歧配管3 7 a，從原水 19 312/發明說明書(補件)/92-11 /92122684 1235682 供給第2配管3 3 a進行分歧，具有流出使原水的流動方向 成為相反方向的情況的濃縮水的閥d 1。另外，分離膜裝置 3 1 b、3 1 c係採用與分離膜裝置3 1 a相同的構成。而且，分 離膜裝置群2 9 a具備：原水供給主配管3 8，係連接途中附 設有原水流出第1配管閥f的原水流出第1配管3 9 ;原水 供給分歧配管4 0 a、4 0 b，係從原水供給主配管3 8進行分 歧，而連接於分離膜裝置3 1 a、3 1 b的原水供給第1配管 3 2 a、3 2 b ;及分離膜裝置3 1 a及3 1 b。另外，後段的分離 膜裝置群2 9 b具備：後段的第1濃縮水供給主配管（原水供 給主配管）4 1，係連接途中附設有原水流出第2配管闊（後 段的原水流出配管閥）m的原水流出第2配管（原水流出配 管）47;及分離膜裝置31c。多段式分離膜裝置28係於前 段的分離膜裝置群2 9 a、2 9 b的前段更具備泵5 0 ;及濃縮 水集水配管5 1，係從分離膜裝置群2 9 b的第1濃縮水供給 主配管（原水供給主配管）4 1進行分歧，而與分離膜裝置群 2 9 a的濃縮水流出第1配管3 6 a、3 6 b及濃縮水流出第2配 管3 7 a、3 7 b連接。 在多段式分離膜裝置2 8中，首先，關閉閥b 1、b 2、d 1、 d 2、f、h、j及m，以將模組内形成為指定的壓力的方式來 開口調整閥c 1、c 2及i，並打開閥a 1、a 2、e 1、e 2、g及 k。原水係藉由原水供給水泵5 0而供給分離膜模組3 0 a及 3 0 b。原水經由分離膜模組3 0 a及3 0 b處理，從濃縮水流出 第1 S己管3 6 a、3 6 b得到第1濃縮水，同時，從透過水流出 配管3 4 a、3 4 b得到透過水。從分離膜模組3 0 a及3 0 b得到 20 312/發明說明書(補件)/92-11 /92122684 1235682 的該第1濃縮水（中間濃縮水，以下相同），係由濃縮水集 水配管5 1所集中，並供給後段的分離膜模組4 8。然後從 濃縮水流出第1配管4 5得到第2濃縮水，同時，從透過水 流出配管4 3得到透過水。該情況，雖也依原水的濁度而 定，但隨著運轉時間的經過，在繞捲於元件上的原水隔片 上漸漸蓄積著原水中的濁質等的浮游物質。 當在原水隔片上蓄積有原水中的濁質時，其通水壓差將 上升。在如此之情況，將原水的流動方向改變為反方向。 也就是說，關閉閥a 1、a 2、c 1、c 2、g及i，以將模組内 形成為指定的壓力的方式來開口調整閥d 1、d 2及j，並打 開閥b 1、b 2及h。藉此，原水係由分離膜模組3 0 a及3 0 b 的濃縮水流出側流入，經由分離膜模組3 0 a及3 0 b處理， 從濃縮水流出第2配管3 7 a及3 7 b得到第1濃縮水，同時， 從透過水流出配管3 4 a及3 4 b得到透過水。從各分離膜模 組得到的該第1濃縮水，係由濃縮水集水配管5 1所集中， 從後段的分離膜模組4 8的濃縮水流出側流入並處理。然後 從濃縮水流出第2配管4 6得到第2濃縮水，同時，從透過 水流出配管4 3得到透過水。藉由將如此的原水的流動方向 改變為相反方向，可容易剝落除去蓄積於原水隔片的交叉 點部份上的濁質。然後，因為隨著運轉時間的經過，在安 裝於元件上的原水隔片上再度蓄積著原水中的濁質等的浮 游物質，因此，再度將原水的流動方向改變為相反方向。 以後，反覆進行此種操作。原水的流動方向的改變時期係 定期或不定期，因此作為改變原水的流動方向的間隔，可 21 312/發明說明書(補件)/92-11/92122684 1235682 為1小時〜2 4小時，最好為1小時〜1 2小時。若未滿1 小時，轉換閥的轉換次數增多，將使得轉換閥的壽命降低。 另外，若超過2 4小時，則不易除去蓄積的濁質。另外，原 水的流動方向的改變時期，除上述外，也可在成為指定的 通水壓差的時點進行改變，該情況，因不用頻繁進行改變 操作，還可除去蓄積的濁質，因此較為理想。另外，也可 組合在指定時間經過後改變流動方向的方法，及在成為指 定的通水壓差的時點進行改變的方法的兩者。 根據本例的多段式逆滲透膜裝置2 8，因為使原水的流動 方向形成為相反方向以抑制濁質的蓄積，因而可省略以往 之技術中用以除去原水中的濁質的目的的凝集污泥處理、 過濾處理及膜處理等的前處理裝置的設置。因此，在達成 系統的簡略化、設置面積的減低及低成本化方面，可獲得 預期的效果。 再者，參照圖3來說明本發明之第6實施形態之分離膜 模組的運轉方法。第6實施形態例係於第5實施形態之分 離膜模組的運轉方法中，在原水的流動方向改變時，從兩 個方向交錯進行複數次的沖洗，藉此，可確實除去蓄積於 原水隔片的交叉點部份上的濁質。作為從分離膜模組的兩 個方向交錯進行複數次的沖洗的方法，可列舉出使最初階 段所進行的沖洗以與該沖洗剛開始前流動過來的原水流動 方向相反的方向來進行的方法（以下，又稱為逆方向沖 洗）；及以與該沖洗剛開始前流動過來的原水流動方向相同 的方向來進行的方法，其中，逆方向沖洗利用最初階段所 22 312/發明說明書(補件)/92-11/92122684 1235682 進行的沖洗可有效剝離蓄積於原水隔片的交叉點部份上的 濁質，因此較為理想。若使最初階段所進行的沖洗與該沖 洗剛開始前流動過來的原水流動方向為相同的方向，雖可 除去一部份的濁質，但反而也會抵壓蓄積於原水隔片的滯 留部份上的濁質，隨著時間的推移而成為蓄積的濁質。逆 方向沖洗之進行，首先，關閉閥a 1、a 2、c 1、c 2、f、g、 i及m，打開閥b 1、b 2、d 1、d 2、h及j。然後，將透過處 理之原水供給量的約3倍流量的原水從濃縮水流出側急速 供給分離膜模組3 0 a及3 0 b内，並藉由原水流入側的原水 供給第2配管3 3 a及3 3 b及濃縮水流出第2配管3 7 a及3 7 b 排出。從分離膜模組3 0 a及3 0 b排出的原水通過濃縮水集 水配管5 1，再度從濃縮水流出側供給後段的分離膜模組4 8 内，並從原水流入側的原水供給第2配管4 2及濃縮水流出 第2配管4 6排出。逆方向沖洗結束後，隨後再進行與逆方 向沖洗時之沖洗方向相反方向的沖洗。也就是說，關閉閥 bl、 b2、 dl、 d2、 f、 h、 j 及 m，打開閥 al、 a2、 cl、 c2、 g及i。然後，以與逆方向沖洗相同流量的原水從原水流入 側急速供給分離膜模組3 0 a及3 0 b内，並藉由濃縮水流出 側的濃縮水流出第1配管3 6 a及3 6 b排出。從分離膜模組 3 0 a及3 0 b排出的原水則通過濃縮水集水配管5 1，再度從 原水流入側供給分離膜模組4 8内，並從濃縮水流出側的濃 縮水流出第1配管4 5排出。接著，進行與該沖洗時之沖洗 方向為相反方向的沖洗，以後，反覆進行相同的操作，即 可從兩方向交錯進行複數次的沖洗。 23 312/發明說明書(補件)/92-11 /92122684 1235682 在上述沖洗中，最好為分為各段的每一分離膜模組群來 進行沖洗的運轉方法。例如，在上述逆方向沖洗中，打開 原本為關閉的閥m，而關閉原本為打開的閥h及j，首先， 進行前段的分離膜模組3 0 a及3 0 b的沖洗，使原水從原水 流出第2配管4 7流出，經過一定時間之後，關閉閥d 1、 d 2及m，而打開c 1、c 2、h及j，進行後段的分離膜模組 4 8的逆方向沖洗。根據該方法，從前段的分離膜模組3 0 a 及3 0 b的原水隔片上剝離的濁質，不會流入後段的分離膜 模組4 8，而不會污染後段的分離膜模組4 8，從而可快速進 行沖洗。另外，於再度進行與該逆方向的沖洗成為相反方 向的沖洗的情況，例如，打開閥a 1、a 2及m，而關閉閥b 1、 b 2、h及j，首先，進行前段的分離膜模組3 0 a及3 0 b的沖 洗，使原水從原水流出第2配管4 7流出，經過一定時間之 後，關閉閥c 1、c 2及m，而打開d 1、d 2、g及i，進行後 段的分離膜模組4 8的沖洗，以此方式，分為各段的每一分 離膜模組群來進行沖洗，因此較為理想。即便在3段以上 的分離膜模組群組成的多段式分離膜裝置的情況，也以分 為各段的每一分離膜模組群來進行沖洗而較為理想。 在最初階段所進行的沖洗與該沖洗剛開始前流動過來 的原水流動方向為相同方向的情況，係先進行上述逆方向 沖洗的情況的第2操作。如此般，藉由從兩方向交錯進行 複數次的沖洗，蓄積於原水隔片上的濁質被剝離而確實排 除於元件之外。在進行如此之沖洗的情況，在圖3中，係 藉由濃縮水流出側的壓力調整用的閥c 1、c 2、d 1、d 2、i 24 312/發明說明書(補件)/92-11 /92122684 1235682 及j來進行壓力開放，但是，作為該壓力開放的方法，並 不限定於此，也可另外設置壓力開放用的閥。該情況，濃 縮水流出配管為取得較多的排出量，而以設置為較具有壓 力調整用的閥的配管更為較大管徑為佳。另外，也可在濃 縮水流出第1配管3 6 a、3 6 b、4 5及濃縮水流出第2配管 37a、37b、46的任一個或複數個上配置空氣室（未圖示）， 藉由運轉而使用蓄積的水進行沖洗。在此所謂之空氣室係 指藉由濃縮水的壓力而加壓的空氣，使得蓄積於室中的水 流出的裝置。 在原水的流動方向改變時，從兩個方向交錯進行複數 次的沖洗的情況，於上述沖洗進行前，抽去原水供給側的 壓力，因為抽去至此為止抵壓於膜面的壓力，使得膜略微 浮起，因而，抽去原水供給側的壓力，因可緩和蓄積於膜 面及原水隔片的濁質的密壓而較為理想。作為抽去原水供 給側的壓力的方法，可列舉出打開原水供給水泵5 0的排水 側的連接原水供給主配管3 8的原水流出第1配管3 9所附 設的原水流出第1配管閥f的方法，或是，在將第1閥a 1、 a 2、c 1、c 2、e 1、e 2、g、i及k打開的運轉中，打開閥d 1、 d2及ni的方法。至於閥的開放速度並無特別的限制，但是， 以瞬間、最好為1秒以内全開閥者為佳。瞬間減壓的方法 較易緩動膜，另外還可期待因水擊作用引起的濁質排除效 果。另外，該情況最好打開透過水側的閥e 1、e 2及k。這 是因為關閉閥e 1、e 2及k時膜間壓差消失，而抵壓於膜的 外力亦消失，因此，例如即便抽去原水供給側的壓力，仍 312/發明說明書(補件)/92-11/92122684 25 1235682 無法緩動膜的緣故。 另外，在沖洗時最好將附設於透過水流出管3 4 a、 及4 3的閥e 1、e 2及k全部關閉。若打開附設於透過 出管34a、34b及43的閥el、e2及k，在高壓用逆滲 模組的情況，在沖洗壓力程度則無屬沖洗液的原水透 但在低壓或超低壓用逆滲透膜模組卻有透過原水，以 生沖洗流量減低，且水質降低的水透過的問題。另外 有藉由在剛關閉附設於透過水側的閥後所產生的背壓 沉積於膜面的污染物質浮游的效果，其可進一步增加 效果。 上述沖洗最好從兩方向交錯進行2次以上、5次以 沖洗。該沖洗次數為一次時變得僅為單一方向的出沖 因此洗淨效果不夠充分，而有隨著時間的推移而成為 的濁質的情況。另一方面，若超過5次時，排出的水 而降低了回收率。另外，沖洗的每一次的時間並無特 限定，但最好為3 0秒〜1 2 0秒。若不滿3 0秒則洗淨 不夠充分，若超過1 2 0秒則排放時間增長，使得回收 幅降低。另外，也可在沖洗時對於原水中供給壓縮空 藉由將壓縮空氣混入原水中，可進一步提高洗淨效率 縮字氣的供應量祓無特別的限定，但最好原水輿空氣 積比為2: 1〜1: 2。 在進行了指定時間的沖洗後，再度進行原水的處理 情況，原水的流動方向與最初階段所進行的沖洗剛開 流動過來的原水流動方向相反。也就是說，關閉閥a 1 3Π/發明說明書(補件)/92-11/92122684 34b 水流 透膜 過， 致產 ，還 以使 沖洗 下的 洗， 蓄積 增多 別的 效果 率大 氣。 〇壓 的體 。該 始前 、a 2、 26 1235682 c 1、c 2、f、g、i及m，以將模組内形成為指定的壓力的方 式來開口調整閥d 1、d 2及j，並打開閥b 1、b 2、e 1、e 2 及k，而原水係經由分離膜模組3 0 a、3 0 b及4 8處理。如 此般，順序反覆進行原水處理—沖洗—原水處理—沖洗。 原水處理時間可為1小時〜2 4小時，最好為1小時〜1 2 小時。若原水處理時間未滿1小時，轉換閥的轉換次數增 多，將使得轉換閥的壽命降低，同時連帶造成回收率的下 降。另外，若超過2 4小時，將招致蓄積的濁質的除去效果 的降低。另外，作為從原水處理轉換為沖洗的形態，可列 舉出在每一次相同時間經過後改變流動方向的方法，在成 為指定的通水壓差的時點進行改變的方法，以及以此等的 組合進行改變的方法。 再者，參照圖3來說明本發明之第7實施形態之分離膜 模組的運轉方法。本例之分離膜模組的運轉方法，係為安 裝著螺旋型膜元件的多段式的分離膜模組的運轉方法，該 運轉方法係於途中包含有沖洗，該沖洗中的最初階段所進 行的沖洗，係以與該沖洗剛開始前流動過來的原水流動方 向相反的方向來進行的方法。也就是說，第7實施形態係 為在沖洗後，可將原水流動方向與沖洗剛開始前流動過來 的原水流動方向形成為相同方向，也可形成為相反方向， 除此之外，與第6實施形態例相同。藉此，原水處理時的 原水的最佳形態、沖洗時的閥類的操作形態及沖洗方法的 最佳形態等均與第6實施形態例相同。在第7實施形態例 中，在沖洗時利用反方向的流動可充分除去濁質，因此可 312/發明說明書(補件)/92-11 /92122684 27 1235682 獲得與第6實施形態例相同的效果。 作為本例之直接供給逆滲透膜裝置1 0或多段式分離膜 裝置2 8的原水，可舉出工業用水、自來水及回收水。至於 原水的濁度並無特別的限制，對於濁度2左右的螺旋型膜 元件而言，即便為具有較高的濁度者，因為定期或不定期 將原水的流動方向成為反方向，因此在長期間運轉中，其 通水壓差不會上升。另外，原水係在加溫至4 0〜6 0 °C後進 行供給，因此可防止並除去膜面產生的污泥（s 1 i m e )而較為 理想。若原水的溫度未滿4 0 °C，則幾乎不具備污泥的除去 效果，而若超過6 0 °C時，雖具有污泥的除去效果，但卻超 過了水處理裝置的耐熱溫度。另外，加溫至4 0〜6 0 °C的原 水，可連續供給、也可斷斷續續地供給。斷續供給可以1 小時以上1週以内的間隔斷斷續續地供給，因不作無謂的 能量消耗而可有效除去膜面產生的污泥而較為理想。若供 給間隔未滿1小時，則會造成多餘的加溫，以致無端浪費 能量。另一方面，若超過1週側容易引起污泥的產生，從 而降低了效果。另外，係以p Η值為2 . 0以上7. 0以下的酸 性狀態作供給，酸性水具有較大的殺菌效果，在可抑制污 泥的產生，同時，可減低濁質對膜面的蓄積而較為理想。 若ρ Η值未滿2 . 0，則會產生系統的耐藥品性的問題，若ρ Η 值超過7. 0時，則無法期待抑制污泥的產生的效果。另外， 在原水中含有砂粒等的粗大顆粒的情況，也包含添加分散 劑者，該分散劑用以預先防止通過網眼大的過濾網的處理 水、水垢及水渣。藉由分散劑的添加，可進一步抑制濁質 28 312/發明說明書(補件)/92-11 /92122684 1235682 對原水隔片及膜面的蓄積。作為分散劑例如可舉出市售品 的「hypersperseMSI300」、「hypersperseMDC200」（均為 ARGO SCIENTIFIC 公司製）。 作為安裝於本發明所使用之分離膜模組的螺旋型膜元 件，只要為可將袋形的分離膜與原水隔片一起繞捲於透過 水集水管的外周面者，並無特別的限制，該原水隔片（I ) / 係由從原水的流入側向著流出側以柔軟曲線作蛇行的形狀 延伸的第1線材及第2線材所組成，該第1線材係沿著分 離膜中的對向側的一膜面延伸，在鄰接之第1線材彼此間 形成一原水流路，該第2線材係沿著分離膜中的對向側的 另一膜面延伸，在鄰接之第2線材彼此間形成另一原水流 路，該第1線材與第2線材的一部份重疊，並在該重疊部 份結合而形成者；（Π )係固定於分離膜的原水流入側端部 或原水流入側端部與濃縮水流出側端部者；（ΠΙ )在上述（Π ) 中，將原水隔片固設於分離膜的原水流入側端部或原水流 入側端部與濃縮水流出側端部的方法，係為將一摺為二的 原水隔片以從兩側夾住該端部的方式進行固定者；（IV )構 成原水隔片的線材的平均交點數係為在隔片的每一 1 m2為 5 0 0以上、1 0 0 0 0以下者；（V )構成原水隔片的線材的交點 數密度係沿著原水的流動方向逐漸減少，或斷斷續續地減 少；（VI )構成原水隔片的線材的交點數密度也可使用沿著 原水的流動方向逐漸增加，或斷斷續續地增加者。在上述 (I )中，進一步使以柔軟曲線作蛇行的形狀成為無彎曲點 的具有規則性的形狀，而振幅Η與波長L的比（H / L )為0 . 0 2 29 312/發明說明書(補件)/92-11/92122684 1235682 〜2，並且，一根線材的每一 1 m為1〜1 Ο 0波長者，其交點 數處在較適合的範圍，同時，原水邊於原水流路内緩緩蛇 行便以大致直線狀從流入側向著流出側流動，可進一步防 止濁質在原水流路内的蓄積，因而較為理想。在上述（Π ) 及（m )中，該分離膜的原水流入側端部或濃縮水流出側端 部的相對上述透過水集水管的長度方向上的長度，係分別 從該分離膜的原水流入側端或濃縮水流出側端向著内側， 最好為相對上述透過水集水管的長度方向上的長度的1〜 1 〇 % 者。 本發明之分離膜模組的運轉方法中，安裝著具備上述 (I )、（ Π )、（皿）及（IV )的原水隔片的螺旋型膜元件的分 離膜模組，可適用於上述第1實施形態例〜第7實施形態 例的任一者。安裝著具備上述（V )、（ VI )的原水隔片的螺 旋型膜元件的分離膜模組，因為其原水隔片的交點數密度 係由原水的流動方向所限定，因此無法適用於將原水的方 向改變為相反方向的上述第1實施形態例、第2實施形態 例、第5實施形態例及第6實施形態例。安裝著具備上述（V ) 的原水隔片的螺旋型膜元件的分離膜模組，雖使用第3實 施形態例及第7實施形態例的逆方向沖洗，但必須特意在 原水隔片的入口附近採用使濁質蓄積的構造。另外，安裝 著具備上述（VI )的原水隔片的螺旋型膜元件的分離膜模 組，可適用於上述第3實施形態例及第7實施形態例。 上述 （Π )〜（IV )的原水隔片，如可舉出由複數根第1 線材及複數根第2線材所構成的網眼狀的隔片。該情況， 30 312/發明說明書(補件)/92-11 /92122684 1235682 作為網眼的形狀雖無特別的限制，但可舉出菱形、四角形 及波形等，作為該線材彼此間的交叉形態，雖無特別的限 制，但可舉出線材彼之間作編織而接合的形態、依平紋編 織的交叉形態及依斜紋編織的交叉形態。另外，交點係指 第1線材及第2線材相交的點，例如，如第1線材及第2 線材為波形的情況的交點，即便第1線材及第2線材具有 略微重疊的部份亦可。另外，作為第1線材及第2線材的 剖面形狀，雖無特別的限制，但可舉出三角形、四角形等。 另外，第1線材及第2線材係使用相同尺寸、相同剖面形 狀者。原水隔片的厚度係配合於第1線材的直徑及第2線 材的直徑者，或較此為略薄者，是在0.4〜3. Omm的範圍。 另外，作為原水隔片的材質雖無特別的限制，但使用聚丙 烯、聚乙烯，從成形性及成本面考量較為理想。另外，原 水隔片的製造方法雖無特別的限制，但可適用公知的方 法、如射出成形性法，其從成本面及精度面考量較為理想。 該螺旋型膜元件，係將袋形的分離膜與上述原水隔片一 起繞捲於透過水集水管的外周面，可繞捲一片的袋形的分 離膜，或繞捲複數片的袋形的分離膜。作為分離膜可舉出 精密過濾膜、限外過濾膜及逆滲透膜等。其中，逆滲透膜 係用於從原子中分離離子成份及低分子成份之目的，而從 以往為必須有前處理者的情況考量可進一步發揮其效果。 作為逆滲透膜可舉出具有對於食鹽水中的氯化納的9 0 °/◦以 上的高除去率的通常的逆滲透膜、及低脫氯率的毫微過濾 膜、低離子去除率逆滲透膜（1 ο 〇 s e R 0 )。毫微過濾膜、低 31 312/發明說明書(補件)/92-11 /92122684 1235682 離子去除率逆滲透膜具有脫氯性能，但較通常的逆滲透膜 的脫氣性能低，因此，特為具有C a、M g等的硬度成份的分 離性能者。又，毫微過濾膜、低離子去除率逆滲透膜也有 被稱為N F膜的情況。 本例中所使用的逆滲透膜模組，只要為具備上述螺旋型 膜元件者並無特別的限制，例如可舉出具有圖4所示構造 的逆滲透膜模組。如圖4所示，將袋形的逆滲透膜6 1與原 水隔片一起呈螺旋狀繞捲於透過水集水管6 0的外周面，由 外裝體6 2覆被其上部。然後，為防止以螺旋狀繞捲之逆滲 透膜61的凸出，在兩端安裝具有數根放射狀的凸緣的可伸 縮擋止塊6 4。由此等透過水集水管6 0、逆滲透膜61、外 裝體6 2及可伸縮擋止塊6 4形成一個螺旋型膜元件6 5，由 連接器（未圖示）與各個透過水集水管60連通，在室66内 裝設複數個螺旋型膜元件6 5。又，在螺旋型膜元件6 5的 外周與室66的内周之間形成間隙67，但由鹽封（Brine s e a 1 ) 6 8予以閉塞。又，在室6 6的一端附設使原水流入室 内部用的原水流入管（未圖示）、或於另一端設置連通透過 水集水管60的處理水管（未圖示）及非透過水水管（未圖 示），由室6 6、其内部的零件及配管（喷嘴）等構成逆滲透 膜模組6 9。 在由如此之構造的逆滲透膜模組6 9處理原水的情況， 從室6 6的一端使用水泵壓入原水，在圖4中如箭頭所示， 原水通過可伸縮擋止塊6 4的各放射狀的凸緣6 3之間而侵 入最初的螺旋型膜元件6 5内，一部份原水通過由螺旋型膜 32 312/發明說明書(補件)/92-11/92122684 1235682 元件6 5的膜間的原水隔片所區隔的原水流路後到達下一 螺旋型膜元件6 5，而其餘的原水透過逆滲透膜6 1成為透 過水，該逆過水由透過水集水管6 0所集水。如此之後，原 水接連不斷地通過螺旋型膜元件6 5，而未透過逆滲透膜的 原水作為以高濃度包含濁質及離子性雜質的濃縮水被從透 過水集水管6 0的另一端抽出，另外，透過逆滲透膜的透過 水介由透過水集水管60而被取出於室66外。又，本發明 所使用之逆滲透膜模組除為安裝著複數個螺旋型膜元件者 外，例如，也可為安裝1個螺旋型膜元件者。 本例之多段式分離膜裝置，係為將從前段的分離膜裝置 或分離膜裝置群的分離膜模組所獲得的中間濃縮水，順序 供給後段的分離膜裝置或分離膜裝置群的分離膜模組的2 段以上的多段式分離膜模裝置，例如，也可舉出從並行排 列配置4座的分離膜模組7 1 a〜7 1 d的前段的分離膜裝置群 7 2 a、並行排列配置2座的分離膜模組7 1 e、7 1 f的中段的, 分離膜裝置群7 2 b及並行排列配置1座的分離膜模組7 1 g 的後段的分離膜裝置群7 2 c組成的4 — 2 — 1型的3段式分 離膜裝置（參照圖5 );從並行排列配置3座的分離膜模組 7 4 a〜7 4 c的前段的分離膜裝置群7 3 a及並行排列配置2座 的分離膜模組7 4 d、7 4 e的後段的分離膜裝置群7 3 b組成的 3 — 2型的2段式分離膜裝置（參照圖6 ( A ));從並行排列配 置2座的分離膜模組7 6 a、7 6 b的前段的分離膜裝置群7 5 a 及並行排列配置1座的分離膜模組7 6 c的後段的分離膜裝 置群7 5 b組成的2 — 1型的2段式分離膜裝置（參照圖 33 312/發明說明書(補件)/92-11/92122684 1235682 6 ( B ));從並行排列配置1座的分離膜模組7 8 a的前段的分 離膜裝置群7 7 a及並行排列配置1座的分離膜模組7 8 b的 後段的分離膜裝置群7 7 b組成的1 — 1型的2段式分離膜裝 置（參照圖6 ( C ))。又，圖6 ( B )係與圖3相同的配置形態。 另外，圖5及圖6為模式圖，來自分離膜模組的2個流出 線，雖顯示濃縮水流出第1配管及濃縮水流出第2配管， 但與實際配置位置不同。此等多段式的分離膜裝置係藉由 所要求的水的回收率及水的處理量，而可設為適當的形 態。本發明之多段式的分離膜裝置，可以簡單的裝置確實 實施本發明之多段式分離膜模組的運轉方法。 (實施例） 以下，以實施例為例更為具體說明本發明，然，此等僅 為例示，並非以此限制本發明。 <實施例1 > 由圖1所示流程的逆滲透膜裝置來處理濁度2度、導電 率2 0 m S / m的工業用水，在如下的運轉條件下，進行2 0 0 0 小時的耐久運轉。逆滲透膜裝置係使用1個逆滲透膜模 組，該逆滲透膜模組安裝有1個繞捲著網眼狀的原水隔片 的8吋元件E S - 1 0 (日東電工製）。逆滲透膜模組的性能評 價，係在測定運轉初期及2 0 0 0小時的通水壓差（Μ P a )、透 過水量（1/分）及透過水的導電率（mSm)下所進行。另外， 2 0 0 0小時後，將逆滲透膜模組解體，觀察原水流路内的濁 質的黏附狀況。表1顯示該測定值的結果，表2顯示原水 流路的目視觀察結果。 34 312/發明說明書(補件)/92_ 11/92122684 1235682 (運轉條件） 如上述第2實施形態例所示，依照於原水的流動方向改 變時，從兩方向交錯進行3次沖洗，使最初階段所進行的 沖洗以與該沖洗剛開始前流動過來的原水流動方向相反的 方向來進行的方法。也就是說，將原處理時間8小時—逆 方向沖洗6 0秒―順方向沖洗6 0秒—逆方向沖洗6 0秒作為 1個循環，反覆進行此操作。又，順方向沖洗係指以與該 沖洗剛開始前流動過來的原水流動方向相同的方向來進行 的沖洗。 透過處理條件：操作壓力為0 . 7 5 Μ P a、濃縮水流量為 2 . 7 m3 /小時、水溫為2 5 °C 、原水p Η值為7 . 0。 沖洗條件：將閥c或閥d全開，沖洗流量為8. 0 m3/小 時、水溫為2 5 °C。 <實施例2 > 於實施例1之每一次的沖洗時，除以原水與空氣的體積 比成為1 : 1的方式混入空氣外，其他均以與實施例1相同 的運轉方法進行2 0 0 0小時的耐久運轉。表1及表2顯示逆 滲透膜模組的性能評價結果。 <實施例3 > 除取代連續供給原水處理用之溫度為2 5 °C的原水，而改 以1日1次且斷續供給1小時供給、溫度為5 0 °C的原水外， 其他均以與實施例1相同的運轉方法進行2 0 0 0小時的耐久 運轉。5 0 °C的原水係利用加熱器加熱2 5 °C的原水而獲得。 表1及表2顯示逆滲透膜模組的性能評價結果。 35 312/發明說明書(補件)/92-11/92122684 1235682 <實施例4 > 除取代原水處理用之P Η值為7. 0的原水，而改以使用 ρ Η值為4. 0的原水外，其他均以與實施例1相同的運轉方 法進行2 0 0 0小時的耐久運轉。ρ Η值為4. 0的原水係藉由 添加鹽酸於ρ Η值為7. 0的原水中調製而成。表1及表2 顯示逆滲透膜模組的性能評價結果。 <實施例5 > 除將 5mg/l 的分散劑「hypersperse MSI300」 （ARGO SCIENTIFIC公司製）添加於濁度為2度、導電率為20mS/m 的工業用水内外，其他均以與實施例1相同的運轉方法進 行2 0 0 0小時的耐久運轉。表1及表2顯示逆滲透膜模組的 性能評價結果。 <實施例6 > 由圖2所示流程的逆滲透膜裝置來處理濁度2度、導電 率2 0 m S / m的工業用水，在如下的運轉條件下，進行2 0 0 0 小時的耐久運轉。前段的逆滲透膜模組1 0 A及後段的逆滲 透膜模組1 0 B係為安裝有1個各自繞捲著網眼狀的原水隔 片的8吋元件ES-10(日東電工製）的模組，逆滲透膜裝置 分別使用1個此等模組。逆滲透膜模組的性能評價，以與 實施例1相同的運轉方法所進行。 (運轉條件） 前段逆滲透膜模組1 0 A及後段逆滲透膜模組1 0 B，以操 作壓力為0 . 7 5 Μ P a、濃縮水流量為2 . 7 m3 /小時、水溫為2 5 °C 、原水ρ Η值為7. 0的條件，僅在前段的逆滲透膜模組 36 312/發明說明書(補件)/92-11 /92122684 1235682 1 Ο A於每8小時1次，進行與實施例1相同的沖洗。又， 原水的流動方向的改變，僅在前段的逆滲透膜模組1 Ο A進 行，而並不在後段逆滲透膜模組1 Ο B進行。又，表1的值 為後段逆滲透膜模組的值。 <比較例1 > 除將由膜處理構成的公知前處理裝置配置於前段，且不 進行原水的流動方向的改變及沖洗以外，其他均以與實施 例1相同的方法來進行。亦即，由前處理裝置來處理濁度 2度、導電率2 0 m S / Hi的工業用水，再由習知的市售逆滲透 膜模組對該處理水進行通常的處理。表1及表2顯示其結 果。 <比較例2 > 除取代實施例1的運轉條件而改以如下的運轉條件以 外，其他均以與實施例1相同的方法來進行。亦即，不由 前處理裝置來處理濁度2度、導電率20mS/m的工業用水， 而是直接由習知的市售分離膜模組來進行通常的處理。表 1及表2顯示其結果。又，該比較例2中，在8 0 0小時左 右，通水壓差極端上升，而無法獲得透過水，因此在此時 點停止運轉。 (運轉條件） 在操作壓力為0 . 7 5 Μ P a、濃縮水流量為2 . 7 m3 /小時、水 溫為2 5 °C 、原水p Η值為7. 0的條件下進行。另外，原水 處理係於每8小時，中斷原水處理，將附設於濃縮水流出 第1分歧配管1 5 1的閥c全開，以透過處理之原水供給量 37 312/發明說明書(補件)/92-11 /92122684 1235682 的約3倍流量，使原水流入逆滲透膜模組内6 0秒鐘，進行 使洗淨排水從濃縮水流出管流出的所謂順方向沖洗。 [表1] 通水差壓[MPa] 透過水量（1 /分） 透過水導電率fmS/m] 運轉初期 2000hr 運轉初期 2000hr 運轉初期 2000hr 實施例 1 0. 020 0.035 20 15 0.30 0. 45 實施例 2 0. 020 0.031 20 16 0. 30 0.42 實施例 3 0.020 0.035 20 17 0. 30 0. 39 實施例 4 0.020 0.035 20 17 0. 30 0.39 實施例 5 0.020 0.033 20 18 0.30 0.38 實施例 6 0.020 0.020 20 20 0.03 0.03 比較例 1 0.020 0.022 20 20 0. 30 0. 30 比較例 2 0.020 — 20 - 0. 30 — [表2] 2 0 0 0小時後的原水流路的目視觀察結果 ΊΊ ΊΊ ΊηΊ JJ, ίηΊ ruj, ΊΊ JnJ. rnj. 施施施施施施施較較 實實實實實實實比比 123 6 (前段R Ο ) 6 (後段R Ο )1 2 完全阻塞原 附黏 質 濁 質質質附附附6¾ 質質濁濁濁黏黏黏>t 濁濁附附附質質質ίι 附附黏黏黏濁濁濁之 黏黏少少少無無無吣 微微微微微乎全乎>4 略略極極極幾完幾κ> <實施例7 > 由圖7所示流程的多段式分離膜裝置來處理濁度2度、 導電率20mS/m的工業用水，在如下的運轉條件下，進行 2 0 0 0小時的耐久運轉。多段式分離膜裝置係使用安裝有1 個繞捲著網眼狀的原水隔片的8吋元件E S - 1 0 (日東電工製） 的分離膜模組。分離膜模組的性能評價，係在測定第1段 的分離膜模組的運轉初期及2 0 0 0小時的通水壓差（MPa )、 透過水量（1/分）及透過水的導電率（mS/m)下所進行。另 外，2 0 0 0小時後，將第1段的分離膜模組解體，觀察原水 38 312/發明說明書(補件)/92-11 /92122684 1235682 内的濁質的黏附狀況。另外，表8顯示第1段的分離膜模 組的各測定值的結果，表9顯示第1段的分離膜模組的原 水流路（分離膜模組内的原水隔片存在的部份）的目視觀察 結果。又，表8及表9之實施例8〜1 2及比較例3〜5的結 果也相同。 (運轉條件） 根據表3所示步驟表進行各閥的開閉，將表3之N 〇. 1 〜N 〇. 1 6的步驟作為1個循環，反覆進行此操作。透過處 理條件（採水A及B )係以操作壓力為0 . 7 5 Μ P a、濃縮水流量 (最終段）為2 . 7 m3 /小時、水溫為2 5 °C 、原水p Η值為7 . 0 的條件。另外，沖洗條件（沖洗A1、A 2、Β1及Β 2)係為沖 洗水流量8 . 0 m3 /小時、水溫2 5 °C 。 [表3 ]1235682 玖, Description of the invention: [Technical field to which the invention belongs] The present invention relates to a separation membrane module and a method for operating the same, The turbidity accumulated on the raw water separator wound around the spiral membrane element can be effectively removed. [Prior art] In the past, As desalination to obtain seawater, Ultra-pure water, Various manufacturing process water methods, It is known to use reverse osmosis membrane (R 0 membrane), Spiral membrane element with nanofiltration membrane (N F membrane) as transmissive membrane, The method of separating ionic components or low molecular components from raw water. In addition, Out-of-limit filtration methods that separate low-molecular and high-molecular components or only high-molecular components within low-molecular and high-molecular components, And precision filtration for separating fine particles, Spiral membrane elements are also used. As illustrated in Figure 8, An example of a conventional spiral membrane element, By forming the reverse osmosis membrane 81 on both sides of the water-permeable spacer 8 2 to overlap, the three sides are joined to form a bag-shaped membrane 83. The opening of the bag-shaped film 8 3 is attached to the permeate water collecting pipe 8 4. It is constituted by being spirally wound around the outer peripheral surface of the permeate water collecting pipe 84 with the net-like raw water separator 8 5. then, The raw water 8 6 is supplied from the end surface side 8 9 a of one end of the spiral type membrane element 80, Flowing along the raw water separator 8 5, It is discharged from the end surface side 8 9 b of the other end of the spiral type membrane element 80 as concentrated water 8 8. Raw water 8 6 is flowing along the raw water separator 85, The reverse osmosis membrane 81 passes through and becomes permeate water 87. The permeate water 8 7 flows into the permeate water collecting pipe 8 4 along the permeate spacer 8 2, It is discharged from the end of the permeate water collecting pipe 84. in this way, A raw water path is formed by a raw water spacer 85 arranged between the rolled bag-shaped films 83. 5 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 In addition, Conventionally, a separation membrane device group in which the above-mentioned spiral membrane element is installed is arranged in parallel in each segment into one or more separation membrane device groups. Multi-stage separation membrane device connected to more than two stages, It is used to improve water recovery and water treatment capacity. E.g, In the multi-segment separation membrane device 90 of FIG. 9, The raw water supplied by the water pump 9 1 passes through the raw water supply main pipe 9 2. Raw water supply branch pipes 9 3 a and 9 3 b, Processed by the separation membrane modules 9 4 a and 9 4 b of the first stage arranged in parallel, Permeate water is obtained through the permeate water outflow pipes 9 6 a and 9 6 b. On the other hand, concentrated water flows out of the pipes 9 5 a and 9 5 b to obtain concentrated water. The concentrated and condensed water flowing out of the separation membrane modules 9 4 a and 9 4 b collects water through concentrated water collecting pipes 9 7 a and 9 7 b. The concentrated water is supplied to the main pipe (the raw water supply main pipe in the subsequent stage) 9 8 and water is passed through the separation membrane module 9 9 in the second stage. then, The permeated water can be obtained from the permeated water outflow pipe 1 0 1 Concentrated water is obtained from the concentrated water flowing out of the pipe 100. As mentioned above, The intermediate concentrated water obtained in the previous stage is used as the supply water for the separation membrane module in the subsequent stage. To improve water recovery, In addition, It is used to arrange multiple separation membrane modules in parallel in each section. To increase the amount of water treated. In the spiral membrane element of the reverse osmosis membrane configured in this way, To get desalination of sea water, Ultra-pure water, The conditions of various manufacturing processes, Pretreatment is usually performed for the purpose of removing turbidity of raw water. Performing this kind of pre-treatment, For the following purposes, which is, In order to continuously ensure the raw water flow path and increase the contact area with the reverse osmosis membrane, usually, The thickness of the raw water separator of the reverse osmosis spiral type membrane element, It is set to a thin film thickness of 1 m or less, Therefore, turbidity is accumulated on the raw water separator on the raw water flow path, It becomes easy 6 312 / Invention specification (Supplement) / 92-11 / 92122684 1235682 When the structure of the raw water flow path is blocked, to this end, It is necessary to remove the turbidity in the raw water in advance to avoid the increase of the water pressure difference caused by the accumulation of turbidity, the amount of permeated water, Through the degradation of water quality, And can maintain stable operation for a long time. This kind of pretreatment device for turbidity removal, E.g, The system includes agglomerated sludge treatment, For each device such as filtration treatment and membrane treatment, These settings not only make setup costs, Rising operating costs, Simultaneously, Problems such as a large installation area are also required. but, If it is possible to omit the pre-treatment device for the separation membrane module on which the spiral membrane element is installed, It can supply industrial water or tap water to the reverse osmosis membrane module without pretreatment. So that the system can be simplified, Reduction of installation area and cost reduction, And can greatly increase the value of industrial use. Accordingly, If you develop a raw water separator with a structure that does not easily accumulate turbidity, Or, Even if the turbidity accumulates on the raw water separator, However, turbidity can be removed by changing the operation method or washing, etc. Will be extremely useful technology. especially, The method of removing turbidity by changing the operation method or washing, etc. Because it has a helical membrane element that can be used directly, It's the best choice. Japanese Patent Publication No. 1 1-1 0 4 6 3 6 discloses that In the direction opposite to the normal flow of raw water, Supply pressurized gas-liquid laminar flow, In order to reversely flush the reverse osmosis membrane module. but, The reverse washing only removes the turbidity on the hollow fiber membrane surface of the hollow fiber type reverse osmosis membrane module, However, it is not possible to remove the turbidity on the raw water separator attached to the spiral reverse osmosis membrane module. therefore, The object of the invention is to: Provide a separation membrane module and separation 7 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 operation method of the membrane module, It can effectively remove the turbidity accumulated on the raw water separator wound on the coil. [Summary of the Invention] In the above actual situation, The present inventors deliberately reviewed that the turbidity system in the separation membrane mold of the spiral membrane element formed by winding the bag-shaped separation sheet together around the outer peripheral surface of the water collecting pipe is accumulated in the wire which crosses the raw water separator wire. Turn phenomenon During the operation of the separation membrane module, By changing the flow direction of raw water periodically or not in the opposite direction, That is, the phenomenon of turbidity accumulated on the raw water separator; During the flow of raw water, By performing multiple rinses (f 1 u s h i n g), Can remove the phenomenon of effect; And while the operation method of the separation membrane module is being rinsed, The initial stage of each flush is carried out in the direction of the raw water flowing just before the flush, The phenomenon that the removal of turbidity can be further increased and the like of the present invention. That is, The present invention provides a separation membrane module for a separation membrane mold method (hereinafter, a spiral membrane element composed of a bag-shaped separation membrane and a raw water separator wound around an outer peripheral surface of a tube). Also known as the operation method of the separation membrane module (I)) The intermediate water of the front separation membrane module or the separation membrane module group with the screws arranged in parallel in one or two or more, 312 / Invention Manual (Supplement) / 92] 1/92122684 spiral-shaped membrane element with two or more spiral-type separation membrane modules or separation membrane module groups arranged in parallel arranged as one or two or more the result of, In the group of hair mask and raw water, In the raw water, the cross-point of the water is periodically directed toward the phase, which can be easily removed and the direction of movement can be increased to increase the turbidity. Rinse at the right line, To the opposite side, Which in turn facilitates the transformation method, The operator of the permeated water collection group, Or, Back-separated membrane for sequential supply of rotary membrane elements to the membrane element 8 1235682 Module operation method (hereinafter, Also called the operation method of the separation membrane module (Π), In addition, It is also called the operation method (I) of the separation membrane module or the operation method (Π) of the separation membrane module, Is the operation method (I) or (π) of the separation membrane module, It periodically or irregularly changes the flow direction of the raw water of the separation membrane module in the opposite direction. By adopting the above construction method, It can be easily peeled off to remove the turbidity accumulated on the intersection portion of the raw water separator. In addition, The present invention provides a method (I) or (Π) for operating a separation membrane module, When the flow direction of raw water changes, Multiple rinses were staggered from both directions. By adopting the above construction method, The turbidity accumulated at the intersection of the original water partition can be reliably removed. In addition, The present invention provides a method (I) or (π) for operating a separation membrane module. The rinsing performed in the first stage of each rinsing, It is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. By adopting the above construction method, Effective peeling with initial rinse, It is easy to remove the turbidity accumulated at the intersection portion of the raw water separator. In addition, The present invention provides a method (I) or (Π) for operating a separation membrane module, This is a method for operating a separation membrane module equipped with a spiral membrane element formed by winding a bag-shaped separation membrane together with a raw water separator around an outer peripheral surface of a water collecting pipe. This operation method involves one or more flushes on the way, The rinsing performed in the first stage of the rinsing, This is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. By adopting the above construction method, The same effects as the above-mentioned invention can be obtained. In addition, The present invention provides a method (I) or (Π) for operating a separation membrane module, At the time of flushing, all the valves on the permeate side are closed. If you open the valve through the water side of 9 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682, In the case of high-pressure separation membrane modules, In the rinse, the raw water that is not a rinse solution passes through, However, in the low-pressure or ultra-low pressure group, the raw water is permeated. Resulting in reduced flushing flow, And the problem of water permeability. In addition, There is also the effect of floating the pollutants deposited on the membrane surface immediately after closing the valve on the permeate side, It has a flushing effect. In addition, The invention provides a method (Π) for operating a separation membrane module, Before the above flushing, In order to use the pressure on the raw water supply side, Can release the pressure against the membrane, therefore, Makes the membrane slightly float, This allows the turbidity accumulated in the membrane sheet to float. In addition, The invention provides a method (Π) for operating a separation membrane module, It rinses the above-mentioned multi-stage separation membrane module, Divided into a separation membrane module, Or each separate module group. With the composition method, Spiral membrane element at the rear stage which prevents peeling from the spiral membrane element at the front stage, It prevents pollution. In addition, The invention provides a separation membrane mold device, It has the first piping, It is connected to the raw water supply pump and the first valve; Raw water piping, Connect the first valve and the separation membrane module; The separation membrane mold flows out of the piping, It is a water-transmitting side conversion pipe connected to this separation membrane module. A concentrated water outflow first branch piping valve connected between the raw water supply first piping and the concentrated water outflow side of the module; And concentrated water flows out of the second branch pipe, Separate membrane die from raw water supply No. 312 / Invention Specification (Supplements) / 92-11 / 92122684 Pressure level Reduced aquatic back pressure Increase by one step (I) or pressure. Due to the surface pressure and raw water separation (I) or each section, the above turbidity flow is used to supply raw water to the second group; Through; Flow side The separation membrane diverges from the second 2 piping line 10 1235682. When the outflow is in the opposite direction to the flow direction of the raw water, it shrinks. By using the above-mentioned constituent device, The operation method (I) of the separation membrane module can be confirmed by a simple device. In addition, The present invention provides a multi-segment separation membrane mold device, It is the middle concentrated water obtained by the separation membrane device or the separation membrane module of the separation membrane device group. Multi-segment separation membrane mold device with two or more stages supplied to the separation membrane device in the subsequent stage or the separation membrane module equipped with the separation membrane in sequence. Structure of a separation membrane device or a separation membrane device group of separation membrane devices, With raw water first piping, Connected to the first valve; Raw water supply second piping, 1st valve and separation membrane module; The separation membrane module; The permeate water outflow system is connected to the permeate water side of the separation membrane module; Flow direction switching tube, Connect the raw water supply first piping with the concentration outlet side of the separation membrane module, And has a second valve; The concentrated water flows out of the first pipe, It is connected to the direction changing piping, And a third valve is provided; And concentrated water flowing out of the piping, It is divided from this raw water supply second pipe, And the first ^ By using the above-mentioned constituent device, A simple device can surely implement the operation method (Π) of the upper membrane module. [Embodiment] The following, A method of operating the sub-module according to the first embodiment of the present invention will be described with reference to FIG. Fig. 1 is a flowchart showing a permeation membrane device for implementing the operation method of this example. In Figure 1, The reverse osmosis membrane device 10 has: To the first piping 12 Is connected to the raw water supply pump 11 and the first valve water supply second pipe 1 3, The first valve a is connected to the reverse osmosis membrane module 10 A of the reverse osmosis membrane module; The water flows out of the pipes 1 4 The thick implementation connected to 312 / Invention Specification (Supplement) / 92-11 / 92122684 will group the obtained connection into the supply connection pipe, Water distribution flow 2nd valve. Delineate the membrane and reverse osmosis raw water i; Original 1 0A; The inverse 11 1235682 osmosis membrane module 1 〇 A penetrates the water side; Flow direction switching piping 1 5 Concentrated water having the concentrated water outflow side connecting the raw water supply first pipe 12 and the reverse osmosis membrane module 10A flows out of the first branch pipe 1 51 and the second valve b; And the concentrated water flows out of the second branch pipe 1 2 1, Diverging from raw water supply second pipe 1 3, Concentrated water flowing out of the direction opposite to the flow direction of the raw water. In addition, A valve is attached during the flow of the concentrated water out of the first branch pipe 1 51. In the reverse osmosis membrane device 10, First of all, Close the second valve b and valve d, Adjust the valve c so that the inside of the module becomes a specified pressure. Then, the first valve a and the valve e are opened. The raw water is supplied to the reverse osmosis membrane module 1 0 A by a raw water supply pump 11. Raw water is processed through reverse osmosis membrane module 1 〇 A, The first branch pipe 1 5 1 flows out from the concentrated water to obtain concentrated water. Simultaneously, Permeated water is obtained from the permeated water outflow pipe 14. The situation, Although it depends on the turbidity of the raw water, But as the running time passed, The raw water separator wound around the element gradually accumulates suspended matter such as turbidity in the raw water. When turbidity in raw water is accumulated on the raw water separator, Its water pressure differential will rise. In this case, Change the direction of raw water flow to the opposite direction. That is, Close the first valve a and valve c, Adjust the valve d so that the inside of the module is formed to a specified pressure, And open the second valve b. With this, Raw water system flows in from the concentrated water outflow side of reverse osmosis membrane module 1 〇 A, Processed by reverse osmosis membrane module 1 〇 A, The second branch pipe 1 2 1 flows out from the concentrated water to obtain concentrated water. Simultaneously, Permeated water is obtained from the permeated water outflow pipe 14. By changing the flow direction of such raw water to the opposite direction, It can be easily peeled off to remove the turbidity accumulated on the intersection portion of the raw water separator. then, Because with the running of time 12 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682, Re-storing suspended matter such as turbidity in the raw water separator mounted on the element, therefore, Once again, the flow of raw water was reversed. after, Repeat this operation. The direction of changing the direction of the raw water is regular or irregular. Therefore, as an interval to change the direction of the motion, Can be from 1 hour to 24 hours, It is preferably 1 hour. If less than 1 hour, The number of switching times of the switching valve increases, Reduces valve life. In addition, If more than 24 hours, It is not easy to remove the turbidity. In addition, The period of change in the direction of flow of raw water can also be changed, for example, at the point of time when the specified water pressure difference is reached. The situation, Make frequent changes Also removes accumulated turbidity, So compared to J, A reverse osmosis membrane device 10 according to this example may also be used in combination with a method of changing the flow direction after a specified time elapses and a method of changing at a point when a specified water pressure difference becomes. Because the flow of raw water is reversed to suppress the accumulation of turbidity, Therefore, the conventional sludge treatment for the purpose of removing turbidity in raw water can be omitted, Pretreatment equipment such as processing and membrane processing. therefore, Simplifying, In terms of reduction of installation area and cost reduction, The effect can be obtained. Secondly, A method of operating a module according to a second embodiment of the present invention will be described with reference to FIG. The second embodiment example is based on the operation method of the osmosis membrane module of the first embodiment. Change the direction of the flow of raw water With this, It can be surely removed by the turbidity at the intersection of the raw water separator. As a method of rinsing multiple times from two directions of reverse osmosis, For example, 312 / Invention Specification (Supplement) / 92-11 / 92122684 When the flow of flowing water in the original motion direction accumulates ~ 1 2 so that the rotation is accumulated. Because it is not ideal. method, Both. Directional technology When the system is expected to reverse the state of the separation membrane, From the de-accumulation membrane module, the method of rinsing at the beginning of 13 1235682 is performed in a direction opposite to the flow direction of the raw water flowing immediately before the rinsing (hereinafter, (Also known as reverse flushing); And the method in the same direction as the flow direction of the raw water flowing just before the flushing, among them, The reverse rinsing uses the rinsing performed in the initial stage to effectively remove the turbidity accumulated on the intersection of the raw water separator. So it is ideal. If the flushing performed in the initial stage is the same as the flow direction of the raw water flowing before the flushing, Although it can remove a part of the turbidity, However, it will also oppose the turbidity accumulated on the retained part of the raw water separator. It becomes accumulated turbidity over time. Rinse in the opposite direction, First of all, Close the first valve a and valve c, Open the second valve b and valve d. then, The raw water, which has a flow rate of about 3 times the raw water supply through the treatment, is rapidly supplied from the concentrated water outflow side into the reverse osmosis membrane module Then, the raw water is supplied to the second pipe 13 and the concentrated water flows out of the second branch pipe 1 21 through the raw water inflow side. After the reverse flushing, After that, rinse in the opposite direction to that in the reverse direction. That is, Close the second valve b and valve d, Open the first valve a and the valve c. The raw water that is flushed at the same flow rate as the reverse direction is rapidly supplied into the reverse osmosis membrane module from the raw water inflow side. At the same time, the concentrated water flows out from the concentrated water outflow side to the first branch pipe 1 5 1 and is discharged. then, Flushing in the opposite direction to the flushing direction during the flushing, Repeat the same operation in the future. Multiple rinses can be staggered from both directions. When the flushing in the initial stage is in the same direction as the flow direction of the raw water flowing immediately before the flushing, This is the second operation when the above-mentioned reverse flushing is performed first. So so By interleaving 14 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 from both directions, The turbidity accumulated on the raw water separator is peeled off and is surely excluded from the device. In the case of such a flush, In Figure 1, The pressure is released by the pressure adjustment valve c or valve d on the outflow side of the concentrated water. but, As a way to release this pressure, Is not limited to this, An additional valve for pressure release may be provided. The situation, Concentrated water flows out of the piping in order to obtain a larger discharge. It is preferable that the pipe diameter is larger than that of a pipe having a valve for pressure adjustment. In addition, An air chamber (not shown) may also be provided in the concentrated water outflow first branch pipe 1 5 1 and the concentrated water outflow second branch pipe 1 2 1. Rinse with accumulated water during operation. The so-called air chamber here refers to air pressurized by the pressure of concentrated water. A device for allowing water accumulated in a chamber to flow out. When the flow of raw water changes, When multiple rinses are staggered from two directions, Before the above flushing is performed, Remove the pressure on the raw water supply side, Because the pressure that has hit the film surface so far is removed, Makes the membrane slightly float, thus, Remove the pressure on the raw water supply side, It is preferable because the turbidity accumulated on the membrane surface and the raw water separator can float. As a method to remove the pressure on the raw water supply side, For example, a drain pipe (not shown) is provided on the raw water supply first pipe 12 of the raw water supply side of the raw water supply fruit 11 1, A valve (not shown) is attached to the discharge pipe. And how to open the valve, Or, After the first valve a, During operation with valve c and valve e open, A method of opening the valve d attached to the concentrated water outflow second branch pipe 1 2 1. As for the opening speed of the valve, there is no particular limitation. but, In an instant, It is best to fully open the valve within 1 second. The method of instantaneous decompression is easier to make the membrane float, In addition, the effect of removing turbidity due to water hammer can be expected. In addition, In this case, it is better to open the valve e of 15 312 / Instruction of the Invention (Supplement) / 92-11 / 92122684 1235682 on the water side. This is because the pressure difference between the membranes disappears when the valve e is closed, The external force that is pressing against the membrane also disappears, therefore, For example, even if the pressure on the raw water supply side is removed, There is still no reason for the film to float. In addition, It is preferable to close all the valves e attached to the permeated water outflow pipe 14 during flushing. If the valve e attached to the permeated water outflow pipe 14 is opened, In the case of reverse osmosis membrane modules for high pressure, Under the pressure of washing, the raw water which is not the washing liquid permeates. However, the reverse osmosis membrane module for low pressure or ultra low pressure has passed through the raw water. Resulting in reduced flushing flow, In addition, the problem of water permeation caused by the degradation of water quality. In addition, There is also the effect of floating back the pollutants deposited on the membrane surface immediately after closing the valve attached to the permeate side It can further increase the flushing effect. The above rinsing is preferably carried out twice from two directions, Rinse less than 5 times. When the number of rinses is one, it becomes a single-direction rinse, Therefore, the cleaning effect is insufficient, On the other hand, it may become accumulated turbidity over time. on the other hand, If more than 5 times, More water is drained and the recovery rate is reduced. In addition, There is no particular limitation on the time of each rinse. However, it is preferably 30 seconds to 120 seconds. If it is less than 30 seconds, the cleaning effect is insufficient, If it exceeds 120 seconds, the emission time will increase, This leads to a significant reduction in recovery. In addition, It is also possible to supply compressed air to raw water during flushing. By mixing compressed air into the raw water, Can further improve the cleaning efficiency. The supply of compressed air is not particularly limited. But preferably the volume ratio of raw water to air is 2: 1 ~ 1: 2. After rinsing for the specified time, The raw water was treated again. The situation, The flow direction of raw water is the opposite of the flow direction of raw water just before the start of the flushing 16 312 / Instruction Manual (Supplement) / 92-11 / 92122684 1235682. That is, Close the first valve a and valve c, The valve d is adjusted so that the inside of the module is formed to a predetermined pressure, And open the second valve b and e, The raw water system is processed through a reverse osmosis membrane module 10 A. So so Sequentially carry out raw water treatment-rinse-raw water treatment-rinse. Raw water treatment time can be from 1 hour to 24 hours, It is preferably from 1 hour to 12 hours. If the raw water treatment time is less than 1 hour, The number of switching times of the switching valve increases, Will reduce the life of the switching valve, At the same time, the recovery rate is reduced. In addition, If more than 24 hours, This will cause a reduction in the accumulated turbidity removal effect. In addition, As a form of conversion from raw water treatment to rinsing, Examples include methods for changing the flow direction after the same time has elapsed. A method of changing the time when it becomes a specified water pressure difference, And how to make changes in these combinations. Furthermore, A method of operating a separation membrane module according to a third embodiment of the present invention will be described with reference to Fig. 1. The operation method of the separation membrane module in this example, This is the operation method of a separation membrane module with a spiral membrane element. This operation method involves flushing on the way, The first stage of the rinse, The method is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. That is, In the third embodiment, after washing, The direction of raw water flow can be made the same as the direction of raw water flowing just before the flush, Can also be formed in the opposite direction, In addition, This is the same as the second embodiment. With this, Optimal form of raw water during raw water treatment, The operation form of the valves and the optimal form of the flushing method during flushing are the same as those of the second embodiment. In the third embodiment, When flushing, the turbidity can be sufficiently removed by using the reverse flow. Therefore, it is possible to obtain the same effects as in the second embodiment of 17 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682. Furthermore, A method of operating a separation membrane module according to a fourth embodiment of the present invention will be described with reference to Fig. 2. In Figure 2, The same constituent elements as those in FIG. 1 are assigned the same element symbols, And omit its description, The following mainly describes the differences. That is, In Figure 2, The point of difference from FIG. 1 is that the reverse osmosis membrane module 1 〇 B is provided on the downstream side of the reverse osmosis membrane module 1 〇 A, The reverse osmosis membrane module 1 〇 A at the front stage and the reverse osmosis membrane module 1 〇 B at the rear stage are primary permeate water supplied by using the permeated water of the reverse osmosis membrane module 1 〇 A at the front stage as the treated water of the rear stage device. Connected to outflow piping 14 The permeate water outflow pipe 16 for the reverse osmosis membrane module 10B which discharges the permeate water to the rear stage, and the return pipe 18 before returning the concentrated water to the raw water supply water pump are provided. In addition, The reverse osmosis membrane module 10B at the rear stage is provided with a concentrated water outflow pipe 17. The reverse osmosis membrane module 1 0 A of the previous stage is using the reverse osmosis membrane device of the present invention. The reverse osmosis membrane module 100B at the rear stage uses a conventional reverse osmosis membrane device. In other words, In the reverse osmosis membrane device 10 a, The raw water is supplied to the reverse osmosis membrane module 1 0 A at the previous stage by a raw water supply water pump 11. Raw water is processed through the reverse osmosis membrane module 1 〇 A The concentrated water flows out of the pipe 15 to obtain a concentrated shrinkage. At the same time, permeate water is obtained from the permeate water outflow pipe 14 at one time. then, This once permeated water is processed through the reverse osmosis membrane module 1 〇 B at the rear stage. The second permeate water is obtained from the permeate outflow pipe 16. At the same time, the secondary concentrated water is returned from the return pipe 18 to the original water supply water pump. The secondary concentrated water system is permeate water which has been degassed by the reverse osmosis membrane module 10 A of the previous stage. And then concentrated by the reverse osmosis membrane module 1 〇 B Compared with raw water, its conductivity is low. Therefore, Makes the full circulation of secondary concentrated water possible, And it can improve the water recovery rate of 18 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682. in this way, In the reverse osmosis membrane device 10 a, The applicable part of the present invention is the reverse osmosis membrane module 10 A of the previous stage. The reverse osmosis membrane device 10a can also replace the pretreatment device used only for turbidity removal in the conventional type. In the previous section, a reverse osmosis membrane module capable of implementing the operation method of the present invention is used. therefore, A reverse osmosis membrane can be used in substantially two stages. Of course, the pretreatment device of the conventional device has no dechlorination function. Therefore, the reverse osmosis membrane device 10 a is compared with the conventional reverse osmosis membrane device. The quality of its permeated water is also excellent. Furthermore, A method of operating a separation membrane module according to a fifth embodiment of the present invention will be described with reference to Fig. 3. Fig. 3 is a flowchart of a multi-stage separation membrane device for implementing the operation method of this example. The multi-stage separation membrane device 28 is a separation membrane module 3 0 a of a separation membrane device group 2 9 a from the front stage. The middle concentration obtained by 3 0 b shrinks, A two-stage multi-stage separation membrane device which supplies the separation membrane device group 2 9 b in the subsequent stage with a separation membrane module 4 8. That is, A separation membrane device 3 1 a provided with a separation membrane module 3 0 a and a separation membrane device 3 1 b provided with a separation membrane module 3 0 b are arranged in parallel to form a front separation membrane device group 2 9 a The separation membrane device group 2 9 b is arranged at the subsequent stage to constitute a two-stage separation membrane device. In Figure 3, The separation membrane device 31 a includes: Raw water supply to the first pipe 3 2 a, Connected to valve a 1; Raw water supply to the second pipe 3 3 a, The connection valve a 1 and the separation membrane module 3 0 a; The separation membrane module 30a; The water flowing out of the pipe 3 4 a, A water-permeable valve e 1 connected to the separation membrane module 30 a; Flow direction conversion piping 3 5 a, The concentrated water outflow side connecting the raw water supply first pipe 3 2 a and the separation membrane module 30 a, And has a valve b 1; The concentrated water flows out of the first branch pipe 3 6 a, Connected to the pipe 3 5 a for flow direction conversion, And attached with a valve c 1; And concentrated water flows out of the second branch pipe 3 7 a, Divergence from raw water 19 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 to the second pipe 3 3 a, There is a valve d1 for flowing out concentrated water when the flow direction of the raw water is reversed. In addition, Separation membrane device 3 1 b, The 3 1 c system has the same configuration as the separation membrane device 3 1 a. and, The separation membrane device group 2 9 a has: Raw water supply main piping 3 8, The raw water flowing out of the first piping valve f 9 is attached with a raw water flowing out of the first piping 3 9; Raw water supply branch piping 4 0 a, 4 0 b, It is divided from the raw water supply main pipe 38. And connected to the separation membrane device 3 1 a, 3 1 b Raw water supply to the first pipe 3 2 a, 3 2 b; And separation membrane devices 3 1 a and 3 1 b. In addition, The later-stage separation membrane device group 2 9 b includes: The first concentrated water supply main pipe in the latter stage (raw water supply main pipe) 4 1, At the middle of the connection is a raw water outflow 2 piping (raw water outflow piping valve at the back) m raw water outflow 2 (raw water outflow piping) 47; And separation membrane device 31c. The multi-stage separation membrane device 28 is a separation membrane device group 2 9 a at the front stage. The front section of 2 9 b is further equipped with a pump 50; And concentrated water collecting pipes 5 1, It is divided from the first concentrated water supply main pipe (raw water supply main pipe) 4 1 of the separation membrane device group 2 9 b, The concentrated water with the separation membrane device group 2 9 a flows out of the first pipe 3 6 a, 3 6 b and concentrated water flowing out of the second pipe 3 7 a, 3 7 b connection. In the multi-stage separation membrane device 28, First of all, Close the valve b 1. b 2, d 1, d 2, f, h, j and m, Open the regulating valve c by forming the inside of the module to a specified pressure. c 2 and i, And open the valve a 1. a 2, e 1, e 2, g and k. The raw water is supplied to the separation membrane modules 30 a and 30 b by a raw water supply pump 50. Raw water is processed through separation membrane modules 3 a and 30 b. Out of the concentrated water, the first S tube 3 6 a, 3 6 b to obtain the first concentrated water, Simultaneously, Out of permeated water Piping 3 4 a, 3 4 b gets permeated water. The first concentrated water (middle concentrated water, 20 312 / invention specification (Supplement) / 92-11 / 92122684 1235682 is obtained from the separation membrane modules 3 0 a and 3 0 b. The same below), Concentrated by concentrated water collecting pipe 51, And supply the later-stage separation membrane module 48. Then, the first pipe 4 5 flows out from the concentrated water to obtain the second concentrated water. Simultaneously, Permeated water is obtained from the permeated water outflow pipe 43. The situation, Although it depends on the turbidity of the raw water, But as the operating time elapses, The raw water separator wound around the element gradually accumulates suspended matter such as turbidity in raw water. When turbidity in raw water is accumulated on the raw water separator, Its water pressure differential will rise. In this case, Change the direction of raw water flow to the opposite direction. That is, Close the valve a 1. a 2, c 1. c 2. g and i, Open the adjustment valve d so that the inside of the module becomes a predetermined pressure. d 2 and j, And open the valve b 1. b 2 and h. With this, Raw water flows in from the concentrated water outflow side of the separation membrane modules 30a and 30b, Processed by separation membrane modules 3 a and 30 b, The second pipes 3 7 a and 3 7 b flow out of the concentrated water to obtain the first concentrated water. Simultaneously, Permeated water was obtained from the permeated water outflow pipes 3 4 a and 3 4 b. The first concentrated water obtained from each separation membrane module, Concentrated by concentrated water collecting pipe 51, The concentrated water from the separation membrane module 48 in the subsequent stage flows in and is processed. Then, the second pipe 4 6 flows out from the concentrated water to obtain the second concentrated water. Simultaneously, Permeated water is obtained from the permeated water outflow pipe 43. By changing the flow direction of such raw water to the opposite direction, It is easy to peel off and remove the turbidity accumulated on the intersection of the raw water separator. then, Because with the passage of time, On the raw water separator mounted on the element, suspended matter such as turbidity in raw water is accumulated again, therefore, The flow direction of the raw water was changed to the opposite direction again. after, Repeat this operation. The changing direction of the flow of raw water is regular or irregular, Therefore, as an interval to change the direction of flow of raw water, Yes 21 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 for 1 hour to 24 hours, It is preferably 1 hour to 12 hours. If less than 1 hour, The number of switching times of the switching valve increases, Will reduce the life of the switching valve. In addition, If more than 24 hours, It is difficult to remove the accumulated turbidity. In addition, When the direction of flow of raw water changes, In addition to the above, It can also be changed at the time when it becomes the specified water pressure difference, The situation, Because you do n’t need to make frequent changes, Also removes accumulated turbidity, So it is ideal. In addition, You can also combine methods that change the flow direction after a specified time has elapsed. And both of the methods of changing at the point when the specified water pressure difference becomes. The multi-stage reverse osmosis membrane device 28 according to this example, Because the direction of raw water flow is reversed to suppress the accumulation of turbidity, Therefore, the conventional sludge treatment for the purpose of removing turbidity in raw water, Installation of pretreatment devices such as filtration and membrane treatment. therefore, In achieving system simplification, In terms of reduction of installation area and cost reduction, Can get the expected results. Furthermore, A method of operating a separation membrane module according to a sixth embodiment of the present invention will be described with reference to Fig. 3. The sixth embodiment is based on the operation method of the separation membrane module of the fifth embodiment. When the flow of raw water changes, Multiple flushes are staggered from two directions, With this, The turbidity accumulated at the intersection of the raw water separator can be reliably removed. As a method of performing multiple washings alternately from two directions of the separation membrane module, Examples include a method in which the rinsing at the first stage is performed in a direction opposite to the flow direction of the raw water flowing immediately before the rinsing (hereinafter, (Also known as reverse flushing); And the method in the same direction as the flow direction of the raw water flowing just before the flushing, among them, The flushing in the reverse direction uses the flushing performed in the initial stage 22 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 to effectively peel off the turbidity accumulated on the intersection of the raw water separator So it is ideal. If the flushing performed in the initial stage is the same as the flow direction of the raw water flowing before the flushing, Although it can remove a part of the turbidity, However, it will also oppose the turbidity accumulated on the retained part of the raw water separator. It becomes accumulated turbidity over time. Rinse in the opposite direction, First of all, Close the valve a 1. a 2, c 1. c 2. f, g, i and m, Open valve b 1. b 2, d 1, d 2, h and j. then, The raw water, which is about three times the flow rate of the raw water supply that has passed through the processing, is rapidly supplied from the concentrated water outflow side to the separation membrane modules 3 0 a and 3 0 b. The raw water is supplied to the second pipes 3 3 a and 3 3 b through the raw water inflow side, and the concentrated water flows out of the second pipes 3 7 a and 3 7 b to be discharged. The raw water discharged from the separation membrane modules 3 0 a and 3 0 b passes through the concentrated water collecting pipe 51, The separation membrane module 4 8 in the subsequent stage is again supplied from the concentrated water outflow side, The raw water supply second pipe 42 and the concentrated water outflow second pipe 46 from the raw water inflow side are discharged. After the reverse flushing, After that, rinse in the opposite direction to that in the reverse direction. That is, Close the valve bl, b2, dl, d2 f, h, j and m, Open the valve al, a2, cl, c2, g and i. then, Raw water is flushed at the same flow rate in the reverse direction from the raw water inflow side and is rapidly supplied to the separation membrane modules 3 0 a and 3 0 b. The concentrated water is then discharged from the first pipes 3 6 a and 3 6 b by the concentrated water outflow side. The raw water discharged from the separation membrane modules 30a and 30b passes through the concentrated water collecting pipe 51, Again supplied from the raw water inflow side into the separation membrane module 48, The concentrated water from the concentrated water outflow side flows out of the first pipe 45 and is discharged. then, Flushing in the opposite direction to the flushing direction during the flushing, after, Repeat the same operation, That is, multiple rinses can be staggered from both directions. 23 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 In the above flush, It is preferable to perform a flushing operation method for each separation membrane module group divided into sections. E.g, In the above reverse washing, Open the valve m which was originally closed, And closing the previously opened valves h and j, First of all, Rinse the separation membrane modules 3 0 a and 3 0 b at the previous stage. The raw water flows out from the raw water to the second pipe 4 7, After a certain period of time, Close the valve d 1. d 2 and m, And open c 1, c 2. h and j, Rinse the separation membrane module 48 of the rear stage in the reverse direction. According to this method, The turbidity peeled from the raw water separators of the separation membrane modules 3 0 a and 30 b in the previous stage, The separation membrane module that does not flow into the rear stage 4 8 Without contaminating the separation membrane module 4 8 This allows quick rinsing. In addition, When the flushing in the opposite direction to the flushing in the reverse direction is performed again, E.g, Open valve a 1. a 2 and m, While closing the valve b 1, b 2, h and j, First of all, Rinse the separation membrane modules 3 0 a and 3 0 b at the previous stage. The raw water flows out from the raw water outflow second pipe 4 7, After a certain period of time, Closing valve c 1. c 2 and m, And open d 1, d 2, g and i, Rinse the separation membrane module 48 in the subsequent stage, In this way, Divide each separation membrane module group into sections to rinse, So it is ideal. Even in the case of a multi-stage separation membrane device composed of a separation membrane module group of 3 or more stages, It is also preferable to wash each separation membrane module group divided into sections. When the flushing in the initial stage is in the same direction as the flow direction of the raw water flowing immediately before the flushing, This is the second operation when the above-mentioned reverse flushing is performed first. So so By interleaving multiple rinses from both directions, The turbidity accumulated on the raw water separator is peeled off and is surely excluded from the device. In the case of such a flush, In Figure 3, The valve is used for pressure adjustment on the outflow side of the concentrated water. c 2. d 1, d 2, i 24 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 and j for pressure release, but, As a way to release this pressure, Is not limited to this, Alternatively, a valve for pressure release may be provided. The situation, In order to obtain a larger discharge volume, It is preferable that the pipe diameter is larger than the piping provided with the valve for pressure adjustment. In addition, It can also flow out of the first pipe 3 6 a. 3 6 b, 4 5 and concentrated water flowing out of the second pipe 37a, 37b, An air chamber (not shown) is arranged on any one or more of 46, Rinse with accumulated water by operation. The so-called air chamber here means air pressurized by the pressure of concentrated water. A device for allowing the water accumulated in the chamber to flow out. When the flow of raw water changes, In the case of multiple flushes staggered from two directions, Before the above flushing is performed, Remove the pressure on the raw water supply side, Because the pressure that has hit the film surface so far is removed, Makes the membrane slightly float, thus, Remove the pressure on the raw water supply side, This is preferable because it can reduce the dense pressure of the turbidity accumulated on the membrane surface and the raw water separator. As a method to remove the pressure on the raw water supply side, The method of opening the drain side of the raw water supply water pump 50 to connect the raw water supply main pipe 38 to the raw water flow out of the first pipe 3 9 is provided. Or, In the first valve a 1, a 2, c 1. c 2. e 1, e 2, g, When i and k are on, Open valve d 1. d2 and ni methods. There is no particular restriction on the opening speed of the valve. but, In an instant, It is best to fully open the valve within 1 second. The method of instantaneous decompression is easier to slow the membrane, In addition, the effect of removing turbidity due to water hammer can be expected. In addition, In this case, it is best to open the valve e 1 on the water side. e 2 and k. This is because the valve e1 is closed, The pressure difference between the membranes disappears at e 2 and k, The external force that is pressing against the membrane also disappears, therefore, For example, even if the pressure on the raw water supply side is removed, Still 312 / Invention Note (Supplement) / 92-11 / 92122684 25 1235682 The reason why the membrane cannot be slowed down. In addition, When flushing, it is best to attach it to the permeate water outflow pipe 3 4 a. And 4 3 valve e 1, e 2 and k are all off. If it is attached to the transmission outlet pipe 34a, Valves 34b and 43 e2 and k, In the case of high-pressure reverse osmosis modules, In the degree of flushing pressure, the raw water is not permeated by the flushing liquid, but the reverse osmosis membrane module for low pressure or ultra-low pressure has permeated the raw water. Reduced flushing flow, In addition, the problem of water permeation caused by the degradation of water quality. In addition, the back pressure generated immediately after closing the valve attached to the permeate side has the effect of floating pollutants deposited on the membrane surface, It can further increase the effect. The above rinsing is preferably carried out twice from two directions, Rinse 5 times. When the number of rinses is once, it becomes only a single-direction flush, so the cleaning effect is insufficient, However, it may become cloudy with time. on the other hand, If more than 5 times, Drained water reduces recovery. In addition, The timing of each rinse is not limited. However, it is preferably 30 seconds to 120 seconds. If it is less than 30 seconds, the washing is insufficient, If it exceeds 120 seconds, the emission time will increase, Makes the recovery margin lower. In addition, Compressed air can also be supplied to raw water during flushing. By mixing compressed air into raw water, It can further improve the cleaning efficiency. The supply amount of shrink gas is not particularly limited. However, it is best that the raw water concentration ratio is 2: 1 ~ 1: 2. After rinsing for the specified time, Once again the treatment of raw water, The flow direction of the raw water is opposite to the flow direction of the raw water flowing from the rinsing just after the initial stage. That is, Shut-off valve a 1 3Π / Invention specification (Supplement) / 92-11 / 92122684 34b Water flowing through the membrane, To produce So that under washing, Accumulation is increasing, and the effect rate is great. 〇 压 的 体。 Pressure body. The Before, a 2, 26 1235682 c 1. c 2. f, g, i and m, Open the regulating valve d by forming the inside of the module to a specified pressure. d 2 and j, And open the valve b 1. b 2, e 1, e 2 and k, The raw water system passes through the separation membrane module 30a, 3 0 b and 4 8 processing. Like this, Sequentially carry out raw water treatment-rinse-raw water treatment-rinse. Raw water treatment time can be from 1 hour to 24 hours, It is preferably 1 hour to 12 hours. If the raw water treatment time is less than 1 hour, The number of switching times of the switching valve increases, Will reduce the life of the switching valve, At the same time, the recovery rate is reduced. In addition, If more than 24 hours, This will reduce the effect of removing accumulated turbidity. In addition, As a form of conversion from raw water treatment to rinsing, List the methods to change the flow direction after the same time elapses. The method of changing at the point of time when it becomes the specified water pressure difference, And how to make changes in these combinations. Furthermore, A method of operating a separation membrane module according to a seventh embodiment of the present invention will be described with reference to Fig. 3. The operation method of the separation membrane module in this example, This is a method for operating a multi-segment separation membrane module with a spiral membrane element. This operation method involves flushing on the way, The rinsing performed in the initial stage of the rinsing, The method is performed in a direction opposite to the flow direction of the raw water flowing immediately before the flushing. That is, In the seventh embodiment, after rinsing, The direction of raw water flow can be made the same as the direction of raw water flowing just before the flushing, Can also be formed in the opposite direction, In addition, This is the same as the sixth embodiment. With this, Optimal form of raw water during raw water treatment, The operation mode of the valves and the best mode of the flushing method during flushing are the same as those of the sixth embodiment. In the seventh embodiment, The turbidity can be sufficiently removed by using the reverse flow during washing, Therefore, 312 / Invention Specification (Supplement) / 92-11 / 92122684 27 1235682 can obtain the same effect as that of the sixth embodiment. As the raw water directly supplied to the reverse osmosis membrane device 10 or the multi-stage separation membrane device 28 in this example, Examples include industrial water, Tap water and recycled water. There is no particular limitation on the turbidity of raw water. For a spiral membrane element with a turbidity of about 2, Even those with higher turbidity, Because the direction of raw water flow is reversed regularly or irregularly, Therefore, during a long period of operation, Its water pressure difference will not rise. In addition, Raw water is supplied after it is heated to 40 ~ 60 ° C. Therefore, it is preferable to prevent and remove sludge (s 1 i m e) generated on the membrane surface. If the temperature of the raw water is less than 40 ° C, There is almost no effect of sludge removal, If it exceeds 60 ° C, Although it has the effect of removing sludge, However, it exceeds the heat-resistant temperature of the water treatment unit. In addition, Raw water heated to 40 ~ 60 ° C, Continuous supply, It can also be supplied intermittently. Intermittent supply can be intermittently supplied at intervals of more than 1 hour and 1 week, Since unnecessary energy is not consumed, sludge generated on the membrane surface can be effectively removed, which is preferable. If the supply interval is less than 1 hour, Will cause unnecessary heating, So that energy is wasted for no reason. on the other hand, If it exceeds 1 week side, it is easy to cause sludge, This reduces the effect. In addition, The p Η value is 2. 0 or more 7. If the acidic state is less than 0, acidic water has a large germicidal effect. It can suppress the generation of sludge and reduce the accumulation of turbidity on the membrane surface. If ρ Η is less than 2. 0, there will be a problem of chemical resistance of the system, if ρ Η value exceeds 7. At 0, the effect of suppressing the generation of sludge cannot be expected. In addition, when coarse particles such as sand grains are included in the raw water, a dispersant is added to prevent the treated water, scale, and slag from passing through a large-mesh filter in advance. The addition of a dispersant can further suppress the accumulation of turbidity 28 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 on the accumulation of raw water separators and membrane surfaces. Examples of the dispersant include commercially available "hypersperseMSI300" and "hypersperseMDC200" (both manufactured by ARGO SCIENTIFIC). As the spiral membrane element mounted on the separation membrane module used in the present invention, there is no particular limitation as long as the bag-shaped separation membrane can be wound around the outer peripheral surface of the permeate water collecting pipe together with the raw water separator. The raw water separator (I) / is composed of a first wire and a second wire extending in a meandering shape with a soft curve from the inflow side of the raw water to the outflow side, and the first wire is arranged along the opposite direction in the separation membrane. A film surface on one side extends to form a raw water flow path between adjacent first wires. The second wire extends along the other film surface on the opposite side of the separation membrane, and between the adjacent second wires. Form another raw water flow path, where the first wire and a part of the second wire overlap and are formed at the overlapping part; (Π) is the end of the raw water inflow side or the raw water inflow side fixed to the separation membrane (Ii) In the above (Π), the raw water separator is fixed to the raw water inflow side end of the separation membrane or the raw water inflow side end and the concentrated water outflow side end. Method is to fold the raw water separator into two to make it from both sides (IV) The average number of intersections of the wires constituting the raw water separator is one in which each 1 m2 of the separator is 500 or more and 100 or less; (V ) The intersection density of the wires constituting the raw water separator is gradually reduced along the flow direction of the raw water, or it is intermittently decreased; (VI) The intersection density of the wires constituting the raw water separator may also be gradually increased along the flow direction of the raw water. , Or increase intermittently. In the above (I), the shape with the soft curve meandering is made into a regular shape without bending points, and the ratio (H / L) of the amplitude Η to the wavelength L is 0. 0 2 29 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 ～ 2, and each 1 m of a wire is 1 ～ 1 0 0 wavelength, the number of intersection points is in a more suitable range, At the same time, while the raw water slowly snakes in the raw water flow path, it flows in a substantially straight line from the inflow side to the outflow side, which can further prevent the accumulation of turbid matter in the raw water flow path, which is ideal. In the above (Π) and (m), the lengths of the raw water inflow side end or concentrated water outflow side end of the separation membrane with respect to the length of the permeated water collecting pipe in the longitudinal direction are respectively from the raw water inflow into the separation membrane. The side end or the outflow side end of the concentrated water faces inward, and it is preferably 1 to 10% of the length in the longitudinal direction of the permeated water collecting pipe. In the operation method of the separation membrane module of the present invention, a separation membrane module equipped with a spiral membrane element including the raw water separators of the above (I), (Π), (Dish), and (IV) is applicable to the above. Any of the first embodiment to the seventh embodiment. A separation membrane module equipped with a spiral membrane element including the above-mentioned raw water separators (V) and (VI), because the number density of the intersections of the raw water separators is limited by the flow direction of the raw water, so it cannot be applied to raw water. The directions of the first embodiment, the second embodiment, the fifth embodiment, and the sixth embodiment are changed to the opposite directions. The separation membrane module equipped with the spiral membrane element including the raw water separator (V) described above is cleaned in the reverse direction of the third embodiment and the seventh embodiment, but it must be deliberately near the entrance of the raw water separator. Adopt a structure that accumulates turbidity. In addition, a separation membrane module having a spiral-type membrane element provided with the raw water separator (VI) described above can be applied to the above-mentioned third and seventh embodiments. Examples of the raw water separators of (Π) to (IV) include a mesh-shaped separator composed of a plurality of first wires and a plurality of second wires. In this case, although there are no particular restrictions on the shape of the mesh as 30 312 / Invention (Supplement) / 92-11 / 92122684 1235682, the shape of the mesh may include a rhombus, a quadrangle, and a wave shape. Although not particularly limited, there may be mentioned a configuration in which the wires are woven with each other, a cross configuration in a plain weave, and a cross configuration in a twill weave. The intersection point refers to a point at which the first wire and the second wire intersect. For example, if the first wire and the second wire are corrugated, the first wire and the second wire may have a slightly overlapping portion. The cross-sectional shapes of the first wire and the second wire are not particularly limited, and examples thereof include a triangle and a quadrangle. The first wire and the second wire are made of the same size and the same cross-sectional shape. The thickness of the raw water separator is matched to the diameter of the first wire and the diameter of the second wire, or it is slightly thinner, which is 0. 4 ~ 3. Omm range. In addition, although the material of the raw water separator is not particularly limited, the use of polypropylene and polyethylene is preferable in terms of moldability and cost. In addition, although the manufacturing method of the raw water separator is not particularly limited, a known method such as an injection molding method can be applied, and it is preferable from the viewpoint of cost and accuracy. The spiral membrane element is a bag-shaped separation membrane that is wound around the outer peripheral surface of a permeate water collecting pipe together with the raw water separator, and a bag-shaped separation membrane that can be wound around one sheet or a plurality of bag-shaped separation membranes. Separation membrane. Examples of the separation membrane include a precision filtration membrane, an outer-limiting filtration membrane, and a reverse osmosis membrane. Among them, the reverse osmosis membrane is used for the purpose of separating ionic components and low-molecular components from the atoms, and the effect can be further exerted in consideration of the case where a pre-treatment is required in the past. Examples of the reverse osmosis membrane include a normal reverse osmosis membrane having a high removal rate of 90 ° / ◦ or more for sodium chloride in saline, a nanofiltration membrane with a low dechlorination rate, and a low ion removal rate reverse osmosis. Membrane (1 οse R 0). Nanofiltration membrane, low 31 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 Ion removal rate Reverse osmosis membrane has dechlorination performance, but it has lower degassing performance than ordinary reverse osmosis membranes. Those with hardness components such as Ca and Mg. In addition, a nanofiltration membrane and a low ion removal rate reverse osmosis membrane may be referred to as an NF membrane. The reverse osmosis membrane module used in this example is not particularly limited as long as it is provided with the above-mentioned spiral-type membrane element. For example, a reverse osmosis membrane module having a structure shown in Fig. 4 may be mentioned. As shown in FIG. 4, a bag-shaped reverse osmosis membrane 61 and a raw water separator are spirally wound around the outer peripheral surface of the permeate water collecting pipe 60, and the upper part is covered with an outer body 62. Then, in order to prevent the osmosis of the reverse osmosis membrane 61 wound in a spiral shape, extendable stoppers 64 having a plurality of radial flanges are mounted at both ends. Thus, the permeate water collecting pipe 60, the reverse osmosis membrane 61, the outer body 62, and the retractable stopper 64 4 form a spiral membrane element 65. A connector (not shown) and each permeate water collection The water pipe 60 communicates, and a plurality of spiral membrane elements 65 are installed in the chamber 66. A gap 67 is formed between the outer periphery of the spiral membrane element 65 and the inner periphery of the chamber 66, but is closed by a salt seal (Brine s e a 1) 6 8. A raw water inflow pipe (not shown) for flowing raw water into the interior of the room is attached to one end of the chamber 66, or a treated water pipe (not shown) and a non-permeable water pipe (not shown) connected to the permeate water collecting pipe 60 are provided at the other end. (Not shown), the reverse osmosis membrane module 69 is constituted by the chamber 66, its internal parts, piping (nozzle), and the like. When the raw water is processed by the reverse osmosis membrane module 69 constructed in this way, raw water is pressed into the raw water from one end of the chamber 66 using a water pump. As shown in FIG. 4, the raw water passes through each of the retractable stoppers 64. Radial flanges 6 and 3 penetrate into the original spiral membrane element 65, and a part of raw water passes through the spiral membrane 32 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 Element 65 The raw water flow path separated by the raw water separator between the membranes reaches the next spiral membrane element 65, and the remaining raw water passes through the reverse osmosis membrane 61 to become permeate water, and the reverse water is passed through the permeate water collecting pipe 60. catchment. After that, the raw water continuously passes through the spiral membrane element 65, and the raw water that has not passed through the reverse osmosis membrane is extracted from the other end of the permeate water collection pipe 60 as concentrated water containing turbidity and ionic impurities at a high concentration. The permeated water that has passed through the reverse osmosis membrane is taken out of the chamber 66 through the permeated water collecting pipe 60. In addition, the reverse osmosis membrane module used in the present invention may be one in which a plurality of spiral membrane elements are mounted, for example, one in which a spiral membrane element is mounted. The multi-stage separation membrane device of this example is to sequentially supply the intermediate concentrated water obtained from the separation membrane device or the separation membrane module group of the separation membrane device group to the separation membrane device or the separation membrane device group of the separation membrane device group in order. The multi-stage separation membrane module device with two or more stages of the module may also include, for example, a group of separation membrane devices 7 1 a to 7 1 d arranged in parallel in front of each other. 7 2 a, parallel In the middle of the separation membrane module 7 1 e, 7 1 f, the separation membrane device group 7 2 b and the separation membrane device group 7 1 g in the rear stage are arranged in parallel. Type 4 — 2 — 1 type three-stage separation membrane device composed of c (see FIG. 5); three-stage separation membrane modules 7 4 a to 7 4 c are arranged in parallel to the front stage separation membrane device group 7 3 a And in parallel arranged two separation membrane modules 7 4 d, 7 4 e in the rear stage separation membrane device group 7 3 b composed of 3-2 type two-stage separation membrane device (refer to Figure 6 (A)); Separate membrane module groups 7 6 a and 7 6 b in front of two separation membrane modules 7 6 a and parallel arrangement in parallel Membrane module 7 6 c The separation membrane device group 7 5 b consists of 2-1 type 2 stage separation membrane device (refer to Figure 33 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 6 ( B)); From the separation membrane device group 7 7 a at the front stage of the separation membrane module 7 8 a arranged in parallel to one and the separation membrane device group 7 at the rear stage of the separation membrane module 7 8 b arranged in parallel to one 7 b type 1-2 type two-stage separation membrane device (refer to Fig. 6 (C)). 6 (B) is the same arrangement form as that shown in FIG. 5 and 6 are schematic diagrams. Although the two outflow lines from the separation membrane module show that concentrated water flows out of the first pipe and concentrated water flows out of the second pipe, the positions are different from the actual arrangement. Such a multi-stage separation membrane device can be set to an appropriate form by the required water recovery rate and water treatment amount. The multi-stage separation membrane device of the present invention can implement the operation method of the multi-stage separation membrane module of the present invention in a simple device. (Embodiments) Hereinafter, the present invention will be described more specifically by taking examples as examples. However, these are merely examples, and the present invention is not limited thereto. < Example 1 > The reverse osmosis membrane device of the flow shown in FIG. 1 was used to process industrial water with a turbidity of 2 degrees and a conductivity of 20 m S / m. The operating conditions were as follows for 2000 hours. Durable operation. The reverse osmosis membrane device uses a reverse osmosis membrane module, and this reverse osmosis membrane module is equipped with an 8-inch element E S-10 (made by Nitto Denko) around a mesh-shaped raw water separator. The performance evaluation of the reverse osmosis membrane module was performed under the measurement of the water pressure difference (MPa), the amount of permeated water (1 / min), and the conductivity (mSm) of permeated water at the beginning of operation and at 2000 hours. . In addition, after 2000 hours, the reverse osmosis membrane module was disassembled, and the turbidity in the raw water flow path was observed. Table 1 shows the results of the measured values, and Table 2 shows the results of visual observation of the raw water flow path. 34 312 / Invention Manual (Supplement) / 92_ 11/92122684 1235682 (Operating Conditions) As shown in the second embodiment above, when the direction of flow of raw water is changed, three flushes are carried out from two directions alternately to make the initial stage The rinsing is performed in a direction opposite to the flow direction of the raw water flowing immediately before the rinsing. In other words, the original processing time is 8 hours-60 seconds in the reverse direction-60 seconds in the forward direction-60 seconds in the reverse direction-1 cycle, and this operation is repeated. The forward rinsing means rinsing in the same direction as the flow direction of the raw water flowing immediately before the rinsing. Permeation treatment conditions: operating pressure is 0.75 MPa, concentrated water flow is 2.7 m3 / hour, water temperature is 25 ° C, and pΗ value of raw water is 7.0. Flushing condition: Fully open valve c or d, flushing flow is 8. 0 m3 / hour, and water temperature is 25 ° C. < Example 2 > During each flushing in Example 1, except that the air was mixed in such a way that the volume ratio of raw water to air became 1: 1, the other operations were performed in the same manner as in Example 1. 20 0 0 hours of durable operation. Tables 1 and 2 show the performance evaluation results of the reverse osmosis membrane module. < Example 3 > Except that instead of continuously supplying raw water at a temperature of 25 ° C for raw water treatment, raw water was supplied once a day and intermittently for 1 hour at a temperature of 50 ° C. All of them were operated for 2000 hours in the same manner as in Example 1. Raw water at 50 ° C is obtained by heating raw water at 25 ° C with a heater. Tables 1 and 2 show the performance evaluation results of the reverse osmosis membrane module. 35 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 < Example 4 > Except that instead of raw water having a pΗ value of 7.0 for raw water treatment, raw water having a pρ value of 4.0 was used instead, and other operations were performed in the same manner as in Example 1. 2000 hours of durable operation. The raw water having a pH value of 4.0 is prepared by adding hydrochloric acid to the raw water having a pH value of 7.0. Tables 1 and 2 show the performance evaluation results of the reverse osmosis membrane module. < Example 5 > A 5 mg / l dispersant "hypersperse MSI300" (manufactured by ARGO SCIENTIFIC) was added to industrial water having a turbidity of 2 degrees and a conductivity of 20 mS / m. 1The same operation method is used for 2000 hours of durable operation. Tables 1 and 2 show the performance evaluation results of the reverse osmosis membrane module. < Example 6 > The reverse osmosis membrane device of the flow shown in FIG. 2 was used to process industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 m S / m. Under the following operating conditions, it was performed for 2000 hours. Durable operation. The reverse osmosis membrane module 10 A at the front stage and the reverse osmosis membrane module 10 B at the rear stage are 8-inch elements ES-10 (manufactured by Nitto Denko) with one raw water separator wound around the mesh. Modules, reverse osmosis membrane devices use one of these modules. The performance evaluation of the reverse osmosis membrane module was performed by the same operation method as in Example 1. (Operating Conditions) The front-stage reverse osmosis membrane module 10 A and the rear-stage reverse osmosis membrane module 10 B, with an operating pressure of 0.75 MPa, a flow rate of concentrated water of 2.7 m3 / hour, and a water temperature of Conditions of 2 5 ° C, raw water ρ value of 7.0, only in the reverse osmosis membrane module 36 312 / Instruction Manual (Supplement) / 92-11 / 92122684 1235682 1 〇 A once every 8 hours The same rinsing as in Example 1 was performed. In addition, the flow direction of the raw water is changed only in the reverse osmosis membrane module 10 A at the front stage, and not in the reverse osmosis membrane module 10 B at the rear stage. The values in Table 1 are the values of the reverse osmosis membrane module in the latter stage. < Comparative Example 1 > A known pretreatment device composed of a membrane treatment was placed in the front stage, and the flow direction of raw water was not changed and rinsed. The other methods were performed in the same manner as in Example 1. < Comparative Example 1 > That is, industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 m S / Hi is processed by a pre-treatment device, and then the processed water is usually processed by a conventional commercially available reverse osmosis membrane module. Tables 1 and 2 show the results. < Comparative Example 2 > Except that the operating conditions of Example 1 were replaced with the following operating conditions, the other methods were performed in the same manner as in Example 1. < Comparative Example 2 > That is, instead of processing industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 mS / m by a pretreatment device, ordinary processing is directly performed by a conventional commercially available separation membrane module. Tables 1 and 2 show the results. Further, in Comparative Example 2, at around 800 hours, the differential pressure of the water flow was extremely increased, and permeated water could not be obtained. Therefore, the operation was stopped at this point. (Operating conditions) The operation was performed under conditions of an operating pressure of 0.75 MPa, a flow rate of concentrated water of 2.7 m3 / hour, a water temperature of 25 ° C, and a pΗ value of raw water of 7.0. In addition, the raw water treatment is interrupted every 8 hours, and the valve c attached to the concentrated water flowing out of the first branch pipe 1 5 1 is fully opened to allow the raw water supply through the treatment 37 312 / Invention Manual (Supplement) / 92 -11 / 92122684 1235682, about 3 times the flow rate, so that raw water flows into the reverse osmosis membrane module for 60 seconds, and the so-called forward flushing for washing and drainage from the concentrated water outflow pipe is performed. [Table 1] Water differential pressure [MPa] Permeated water volume (1 / min) Permeable water conductivity fmS / m] Initial operation 2000hr Operation initial 2000hr Operation initial 2000hr Example 1 0. 020 0.035 20 15 0.30 0. 45 Example 2 0. 020 0.031 20 16 0. 30 0.42 Example 3 0.020 0.035 20 17 0. 30 0. 39 Example 4 0.020 0.035 20 17 0. 30 0.39 Example 5 0.020 0.033 20 18 0.30 0.38 Example 6 0.020 0.020 20 20 0.03 0.03 Comparative Example 1 0.020 0.022 20 20 0. 30 0. 30 Comparative Example 2 0.020 — 20-0. 30 — [Table 2] Visual observation of raw water flow path after 2 0 0 0 hours ΊΊ Ί ΊηΊ JJ, ίηΊ ruj, ΊΊ JnJ. rnj. Shishi Shishi Shishi Shishi is more practical than real 123 6 (front R 〇) 6 (back R R Ο) 1 2 completely obstructs the original attached viscous turbidity附 附 附 6¾ turbidity and stickiness > t turbidity and stickiness &quality; tl turbidity and stickiness, turbidity, stickiness, and stickiness Slightly extremely extremely a few times κ > < Example 7 > The multi-stage separation membrane device of the flow shown in Fig. 7 was used to process industrial water with a turbidity of 2 degrees and a conductivity of 20 mS / m. Under the following operating conditions, it was durable for 2000 hours. Running. The multi-stage separation membrane device uses a separation membrane module equipped with an 8-inch element E S-10 (manufactured by Nitto Denko) with a raw water separator wound around the mesh. The performance evaluation of the separation membrane module is based on measuring the initial operating pressure of the separation membrane module in the first stage and the water pressure difference (MPa), the amount of permeated water (1 / min), and the conductivity of the permeated water at 2000 hours. (MS / m). In addition, after 2000 hours, the separation membrane module of the first stage was disassembled, and the turbidity of the raw water 38 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 was observed. In addition, Table 8 shows the results of each measurement value of the separation membrane module in the first stage, and Table 9 shows the raw water flow path of the separation membrane module in the first stage (the part where the raw water separator in the separation membrane module exists) Visual observation. The results of Examples 8 to 12 and Comparative Examples 3 to 5 of Tables 8 and 9 are also the same. (Operating Conditions) Each valve is opened and closed according to the step table shown in Table 3. The steps of No. 1 to No. 16 of Table 3 are taken as one cycle, and this operation is repeated. The permeation treatment conditions (water extraction A and B) are based on the operating pressure of 0.75 MPa, the flow rate of the concentrated water (the final stage) is 2.7 m3 / hour, the water temperature is 25 ° C, and the p 水 value of the raw water A condition of 7.0. In addition, the flushing conditions (flushing A1, A2, B1, and B 2) are a flushing water flow of 8.0 m3 / hour and a water temperature of 25 ° C. [table 3 ]
No. 步驟| 保持 時間 a3 b 3 c3 d3 e3 f g h i j k m 1 採 水 A I 1 2時間1 ▲ ▲ 2 放 壓 A 10 秒 ▲ Γ3ΠΙΠΙ ▲ 3 沖 洗 B1 60 秒 4 沖 洗 B2 60 秒 5 沖 洗 A1 60 秒 6 沖 洗 A2 60 秒 7 沖 洗 B1 30 秒 8 沖 洗 B2 30 秒 9 採 水 B 1 1 2時間1 ▲ ▲ 10 放 壓 B 10 秒 ▲ ▲ 11 沖 洗 A1 60 秒 1 12 沖 洗 A2 60 秒 13 沖 洗 B1 | 60 秒 14 沖 洗 B2 ! 60 秒 15 沖 洗 A1 30 秒 1 1 1 16 ! 沖 洗 A2 30 秒 1 (注）空欄··閥全閉、··閥全開、▲:以成為適當的壓 39 312/發明說明書(補件)/92-11 /92122684 1235682 力的方式開閥 <實施例8 > 於實施例7之每一次的沖洗A1、A 2、B1及B 2時，除以 原水與空氣的體積比成為1 : 1的方式混入空氣外，其他均 以與實施例7相同的運轉方法進行2 0 0 0小時的耐久運轉。 表8及表9顯示逆滲透膜模組的性能評價結果。 <實施例9 > 除取代連續供給原水處理用之溫度為2 5 °C的原水，而改 以進行2 3小時的2 5 t的原水供給後，反覆進行斷續供給1 小時供給5 0 °C的原水的作業外，其他均以與實施例7相同 的運轉方法進行2 0 0 0小時的耐久運轉。5 0 °C的原水係利用 加熱器加熱2 5 °C的原水而獲得。表8及表9顯示逆滲透膜 模組的性能評價結果。 <實施例1 0 > 除取代原水處理用之pH值為7. 0的原水，而改以使用 p Η值為4. 0的原水外，其他均以與實施例7相同的運轉方 法進行2 0 0 0小時的耐久運轉。ρ Η值為4. 0的原水係藉由 添加鹽酸於pH值為7.0的原水中調製而成。表8及表9 顯示逆滲透膜模組的性能評價結果。 <實施例1 1 > 除將 50mg/l 的分散劑「hypersperse MSI300」 （ARGO SCIENTIFIC公司製）添加衿濁度為2度、導電率為20mS/m 的工業用水内外，其他均以與實施例7相同的運轉方法進 行2 0 0 0小時的耐久運轉。表8及表9顯示逆滲透膜模組的 40 31：2/發明說明書(補件)/92-11/92122684 1235682 性能評價結果。 <比較例3 > 除將以前處理為目的的公知限外過濾裝置配置於前 段，僅進行表4之採水步驟以外，其他均以與實施例7相 同的方法來進行。亦即，由前處理裝置來處理濁度2度、 導電率20mS/m的工業用水，再由2段連接習知的市售分離 膜模組的多段式膜分離裝置對該處理水進行通常的處理。 表8及表9顯示其結果。 [表4]No. Step | Hold time a3 b 3 c3 d3 e3 fghijkm 1 Water intake AI 1 2 time 1 ▲ ▲ 2 Release pressure A for 10 seconds ▲ Γ3ΠΙΠΙ ▲ 3 Flush B1 60 seconds 4 Flush B2 60 seconds 5 Flush A1 60 seconds 6 Flush A2 60 seconds 7 flush B1 30 seconds 8 flush B2 30 seconds 9 water B 1 1 2 time 1 ▲ ▲ 10 release B 10 seconds ▲ ▲ 11 flush A1 60 seconds 1 12 flush A2 60 seconds 13 flush B1 | 60 seconds 14 flush B2! 60 seconds 15 Flush A1 30 seconds 1 1 1 16! Flush A2 30 seconds 1 (Note) Empty column · Valve fully closed, · Valve fully open, ▲: to become appropriate pressure 39 312 / Invention Manual (Supplement) / 92-11 / 92122684 1235682 Open the valve in a force manner < Example 8 > In each flush of A1, A2, B1, and B 2 of Example 7, the volume ratio of raw water to air is divided into 1: Except that air is mixed in the method of 1 and the others are operated in the same manner as in Example 7 for 2000 hours Long run. Table 8 and Table 9 show the performance evaluation results of the reverse osmosis membrane module. < Example 9 > Instead of continuously supplying raw water at a temperature of 25 ° C for raw water treatment, instead of supplying raw water for 2 to 2 hours at a time of 2 5 t, intermittent supply was performed for 1 hour. Supplying 5 0 Except for the operation of raw water at ° C, the endurance operation was performed for 2000 hours in the same operation method as in Example 7. Raw water at 50 ° C is obtained by heating raw water at 25 ° C with a heater. Tables 8 and 9 show the performance evaluation results of the reverse osmosis membrane module. < Example 1 0 > The same operation method as in Example 7 was performed except that raw water for raw water treatment was replaced with raw water having a pH value of 7.0, and raw water having a pΗ value of 4.0 was used instead. 2000 hours of durable operation. Raw water having a pH value of 4.0 is prepared by adding hydrochloric acid to raw water having a pH of 7.0. Tables 8 and 9 show the performance evaluation results of the reverse osmosis membrane module. < Example 1 1 > A 50 mg / l dispersant "hypersperse MSI300" (manufactured by ARGO SCIENTIFIC) was added to industrial water having a turbidity of 2 degrees and a conductivity of 20 mS / m. The same operation method of Example 7 was performed for 2000 hours of endurance operation. Tables 8 and 9 show the performance evaluation results of the reverse osmosis membrane module 40 31: 2 / Invention Specification (Supplement) / 92-11 / 92122684 1235682. < Comparative Example 3 > The method was performed in the same manner as in Example 7 except that the filtration device with a known limit for the purpose of previous processing was placed in the front stage and only the water collecting step in Table 4 was performed. That is, the pre-treatment device processes industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 mS / m, and then a multi-stage membrane separation device connected to a conventional commercially available separation membrane module is used for the treated water. deal with. Table 8 and Table 9 show the results. [Table 4]
No. 步 驟 保持 時 間 a3 b3 c3 d3 e3 f g h i j k m 1 採 水 2 0 0 0 時 間 A ▲ (注）空欄：閥全閉、:閥全開、▲:以成為適當的壓 力的方式開閥 <比較例4 > 除改以如下的運轉條件以外，其他均以與實施例7相同 的方法來進行。亦即，不由前處理裝置來處理濁度2度、 導電率2 0 m S / m的工業用水，而是直接由2段連接習知的市 售分離膜模組的多段式膜分離裝置來進行通常的處理。表 8及表9顯示其結果。又，該比較例4中，在8 0 0小時左 右，通水壓差極端上升，而無法獲得透過水，因此在此時 點停止運轉。 (運轉條件） 在操作壓力為0 . 7 5 Μ P a、濃縮水流量為2 . 7 m3 /小時、水 溫為2 5 °C、原水p Η值為7. 0的條件下進行。另外，依表5 之步驟進行各閥的開閉，將Ν 〇. 1及Ν 〇. 2作為一個循環， 41 312/發明說明書(補件)/92-11/92122684 1235682 反覆進行操作。 [表5 ]No. Step holding time a3 b3 c3 d3 e3 fghijkm 1 Water extraction 2 0 0 0 Time A ▲ (Note) Empty column: valve is fully closed, valve is fully open, ▲: valve is opened to a proper pressure < comparative example 4 > The procedure was the same as in Example 7 except that the following operating conditions were changed. That is, instead of processing industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 m S / m by a pre-treatment device, a multi-stage membrane separation device connected to a conventional commercially-available separation membrane module is used directly. Normal processing. Table 8 and Table 9 show the results. Further, in Comparative Example 4, at around 800 hours, the differential pressure of the water flow was extremely increased, and permeated water could not be obtained. Therefore, the operation was stopped at this point. (Operating conditions) The operation was performed under conditions of an operating pressure of 0.75 MPa, a flow rate of concentrated water of 2.7 m3 / hour, a water temperature of 25 ° C, and a p 水 value of raw water of 7.0. In addition, the valves are opened and closed in accordance with the procedure in Table 5, and N 〇. 1 and Ν 0.2 are used as a cycle, and 41 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 is repeatedly operated. [table 5 ]
No. 步 驟 保持時間 a3 b3 c3 d3 e3 f g h i j k m 1 採 水 8時間 ▲ ▲ 2 沖 洗 60秒 (注）空欄：閥全閉、:閥全開、▲:以成為適當的壓力 的方式開閥 <實施例1 2 > 由圖3所示流程的多段式分離膜裝置來處理濁度2度、 導電率20mS/ni的工業用水，在如下的運轉條件下，進行 2 0 0 0小時的耐久運轉。多段式分離膜裝置的性能評價，係 在測定第1段的分離膜模組2 0 a的運轉初期及2 0 0 0小時的 通水壓差（MPa)、透過水量（1/分）及透過水的導電率（mSm) 下所進行。另外，2 0 0 0小時後，將第1段的分離膜模組2 0 a 解體，觀察原水流路内的濁質的黏附狀況。另外，表8顯 示測定值的結果，表9顯示原水流路的目視觀察結果。 (運轉條件） 根據表6所示步驟表進行各閥的開閉，將表6之Ν ο · 1 〜N 〇. 1 6的步驟作為1個循環，反覆進行此操作。透過處 理條件（採水A及B )係以操作壓力為0 · 7 5 Μ P a、濃縮水流量 (最終段）為4. 4m3 /小時、水溫為25 °C 、原水pH值為7. 0 的條件，沖洗條件（沖洗A1、A 2、B1及B 2 )係為沖洗水流 量8 . 0 m3 /小時、水溫2 5 °C 。 42 312/發明說明書(補件)/92-11 /92122684 1235682 [表6 ]No. Step holding time a3 b3 c3 d3 e3 fghijkm 1 Water extraction time 8 ▲ ▲ 2 Flush for 60 seconds (Note) Empty column: valve is fully closed, valve is fully open, ▲: valve is opened in such a way as to become appropriate pressure < Example 1 2 > The multi-stage separation membrane device of the flow shown in FIG. 3 was used to process industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 mS / ni. Under the following operating conditions, it was operated for 2000 hours. The performance evaluation of the multi-segment separation membrane device is based on measuring the initial operating pressure of the separation membrane module 20 a in the first stage and the water pressure difference (MPa), permeated water volume (1 / min), and permeation at 2000 hours. Conducted at water conductivity (mSm). In addition, after 2000 hours, the separation membrane module 20 a in the first stage was disassembled, and the turbidity adhesion state in the raw water flow path was observed. In addition, Table 8 shows the results of the measured values, and Table 9 shows the results of visual observation of the raw water flow path. (Operating Conditions) Open and close each valve according to the procedure table shown in Table 6, and repeat the operation by repeating the steps of No. 1 · N to 0.1 6 in Table 6 as one cycle. The permeation treatment conditions (water extraction A and B) are based on an operating pressure of 0.75 MPa, a concentrated water flow rate (the final stage) of 4.4 m3 / hour, a water temperature of 25 ° C, and a raw water pH of 7. The conditions of 0 and the flushing conditions (flushing A1, A2, B1, and B 2) are the flushing water flow rate of 8.0 m3 / hour and the water temperature of 25 ° C. 42 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 [Table 6]
No. 步驟 保持 時間 a 1 a2 bl b2 cl c2 d 1 d2 el e2 f g h i j k m 1 採 水 A 1 2時間 ▲ ▲ ▲ 2 放 壓 A 10 秒 ▲ A ▲ 3 沖 洗 B1 60 秒 4 沖 洗 B2 60 秒 5 沖 洗 A1 60 秒 _ 6 沖 洗 A2 60 秒 7 沖 洗 B1 30 秒 8 沖 洗 B2 30 秒 9 採 水 B 1 2時間 ▲ ▲ 10 放壓 B 10 秒 ▲ A 11 沖 洗 A1 60 秒 12 沖 洗 A2 60 秒 13 沖 洗 B1 60 秒 14 沖 洗 B2 60 秒 15 沖 洗 A1 30 秒 16 沖 洗 A2 30 秒 (注）空欄··閥全閉、:閥全開、▲:以成為適當的壓 力的方式開閥 <比較例5 > 除改以如下的運轉條件以外，其他均以與實施例1 2相 同的方法來進行。亦即，不由前處理裝置來處理濁度2度、 導電率20mS/m的工業用水，而是直接由前段連接2個而後 段連接1個的習知的市售分離膜模組的多段式膜分離裝置 來進行通常的處理。表8及表9顯示其結果。又，該比較 例5中，在8 0 0小時左右，通水壓差極端上升，而無法獲 得透過水，因此在此時點停止運轉。 (運轉條件） 在操作壓力為0. 7 5 MPa、濃縮水流量為4. 4m3/小時、水 溫為2 5 °C、原水p Η值為7. 0的條件下進行。另外，依表7 43 312/發明說明書(補件)/92-11 /92122684 1235682 之步驟進行各閥的開閉，將Ν 〇. 1及Ν 〇. 2作為一個循環， 反覆進行操作。 [表7]No. Step holding time a 1 a2 bl b2 cl c2 d 1 d2 el e2 fghijkm 1 water extraction A 1 2 time ▲ ▲ ▲ 2 release pressure A 10 seconds ▲ A ▲ 3 rinse B1 60 seconds 4 rinse B2 60 seconds 5 rinse A1 60 seconds_ 6 flush A2 60 seconds 7 flush B1 30 seconds 8 flush B2 30 seconds 9 water B 1 2 time ▲ ▲ 10 release pressure B 10 seconds ▲ A 11 flush A1 60 seconds 12 flush A2 60 seconds 13 flush B1 60 seconds 14 Flushing B2 60 seconds 15 Flushing A1 30 seconds 16 Flushing A2 30 seconds (Note) Empty valve · Fully closed valve: Fully open valve, ▲: Open the valve to a proper pressure < Comparative example 5 > Divide by Except for the following operating conditions, everything was performed in the same manner as in Example 12. That is, the pre-treatment device does not process industrial water with a degree of turbidity of 2 degrees and a conductivity of 20 mS / m, but a conventional multi-layer membrane of a commercially-available separation membrane module directly connecting two in the front stage and one in the back stage. The separation device performs normal processing. Table 8 and Table 9 show the results. Further, in Comparative Example 5, the water passing pressure difference extremely increased at about 800 hours, and permeated water could not be obtained. Therefore, the operation was stopped at this point. (Operating conditions) The operation was performed under conditions of an operating pressure of 0.75 MPa, a flow rate of concentrated water of 4.4 m3 / hour, a water temperature of 25 ° C, and a p 原 value of raw water of 7.0. In addition, each valve was opened and closed in accordance with the procedures of Table 7 43 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682, and Ν 〇. 1 and Ν 〇 2 were used as a cycle to repeat the operation. [TABLE 7]
No. 步驟 保持時間 a 1 a2 bl b2 cl c2 dl d2 el e2 f g h i j k m 1 採水 8時間 ▲ ▲ A 2 沖洗 60秒 (注）空欄：閥全閉、:閥全開、▲:以成為適當的壓 力的方式開閥 [表8] 通水差壓「MPal 透過水量（1/分） 透過水導電率「mS/m] 運轉初期 2000hr 運轉初期 2000hr 運轉初期 2000hr 實 施 例 7 0. 020 0. 035 20 15 0.30 0. 45 實 施 例 8 0. 020 0. 031 20 16 0. 30 0. 42 實 施 例 9 0. 020 0. 035 20 17 0.30 0.39 實 施 例 10 0. ,020 0. ,035 20 17 0.30 0.39 實 施 例 11 0. ,020 0_ ,033 20 18 0. 30 0.38 實 施 例 12 0. ,020 0. ,035 20 15 0. 30 0. 45 比 較 例 3 0. 020 0. 022 20 20 0. 30 0.30 比 較 例 4 0· 020 - 20 - 0. 30 - 比 較 例 5 0. 020 一 20 一 0. 30 一 [表9 ] 2 0 0 0小時後的原水流路的目視觀察結果 Λυ 11 7— oo 11 1i 11 oo ^ tnu. ΐηΊΨ rnj. rn^ JU4 fnj tnj, ΐηΊΨ rnu. 合分分伤令分令介介 施施施施施施較較較一 實實實實實實比比比No. Step holding time a 1 a2 bl b2 cl c2 dl d2 el e2 fghijkm 1 Water extraction 8 hours ▲ ▲ A 2 Rinse for 60 seconds (Note) Empty column: valve fully closed: valve fully open, ▲: to become the appropriate pressure Method to open the valve [Table 8] Differential water pressure “MPal Permeated water volume (1 / min) Permeable water conductivity“ mS / m] Initial operation 2000hr Operation initial 2000hr Operation initial 2000hr Example 7 0. 020 0. 035 20 15 0.30 0. 45 Example 8 0. 020 0. 031 20 16 0. 30 0. 42 Example 9 0. 020 0. 035 20 17 0.30 0.39 Example 10 0., 020 0., 035 20 17 0.30 0.39 Example 11 0., 0 20 0_, 033 20 18 0. 30 0.38 Example 12 0., 0 20 0., 035 20 15 0. 30 0. 45 Comparative Example 3 0. 020 0. 022 20 20 0. 30 0.30 Comparative Example 4 0 · 020-20-0. 30-Comparative Example 5 0. 020-20-0. 30-[Table 9] 2 0 0 0 Hours after visual observation of raw water flow path Λυ 11 7— oo 11 1i 11 oo ^ tnu. ΐηΊΨ rnj. rn ^ JU4 fnj tnj, ΐηΊΨ rnu. Split-injury order and order-introduction
附附 黏黏 質質 濁濁 的的 度度 質質質 附程程 質質濁濁濁質黏之之 濁濁附附附濁質路路 附附黏黏黏附濁流流 黏黏少少少黏無水水 微微微微微微乎原原 略略極極極略幾塞塞 阻阻 全全 完完I 例 施 實 的 置 裝 膜 分 段 11 用 使 在 分 式 段 多 用 使 及 離膜裝置的實施例7〜1 2中，2 Ο Ο 0小時經過後幾乎無通水 壓差的上升，亦無透過水量的降低，透過水的水質也高。 44 312/發明說明書(補件)/92-11 /92122684 1235682 在2 Ο Ο 0小時後的性能評價中，雖顯示比較例1未遜色於實 施例1〜6、及比較例3未遜色於實施例7〜1 2的結果’但 這是因為設置有前處理裝置，而有多餘的設置場所及設置 成本等的必要。藉此，實施例1〜5的比較對象為比較例2， 實施例7〜1 1的比較對象為比較例4，實施例1 2的比較對 象為比較例5，但比較例2、4及5的任一者均在約8 0 0小 時、透過水量成為0為止，其濁質的黏附是相當嚴重。實 施例6的比較對象為比較例1，但實施例6顯示非常的優 良性能，而且成本上也便宜。 (產業上的可利用性） 根據本發明之分離膜模組的運轉方法，可容易剝落而確 實除去蓄積於原水隔片的交叉點部份上的濁質。另外，也 無由低壓或超低壓用逆滲透膜模組引起的沖洗流量減低的 問題，同時，還具有藉由在剛關閉透過水側的閥後所產生 的背壓以使沉積於膜面的污染物質的密壓緩和的效果，因 而可進一步提高沖洗效果。另外，利用抽去原水供給側的 壓力，可解除至此為止抵壓於膜面的壓力，因此，使得膜 略鬆緩，而可緩和蓄積於膜面及原水隔片的濁質的密壓。 根據本發明之分離膜裝置，可以簡單的裝置確實實施上述 運轉方法。 【圖式簡單說明】 圖1為顯示實施本發明之實施形態之分離膜模組之運轉 方法之裝置的流程圖。 圖2為顯示實施本發明之另一實施形態之分離膜模組之 45 312/發明說明書(補件)/92-11/92122684 1235682 運轉方法之裝置的流程圖。 圖3為顯示實施本發明之又一實施形態之分離膜模組之 運轉方法之裝置的流程圖。 圖4為顯示本實施形態例之分離膜模組之構造的一例 圖。 圖5為顯示本實施形態例之多段式分離膜裝置的流程 圖。 圖6 ( A )〜（C )為顯示本實施形態例之多段式分離膜裝置 的另一流程圖。 圖7為顯示實施實施例1〜1 1用之多段式分離膜裝置的 流程圖。 圖8為習知逆滲透膜模組的概略圖。 圖9為習知多段式分離膜裝置的一例的流程圖。 (元件 符號 說明 a 第1 閥 a 1 闊 b 第2 閥 bl 閥 c 閥 cl 閥 d 閥 dl 閥 e 閥 el 閥 312/發明說明書(補件)/92-11/92122684 46 1235682 f 原水流出第1配管閥 g 閥 h 閥 I 閥 J 閥 K 閥 1 閥 m 原水流出第2配管閥（後段的原水流出配管閥） 10 逆滲透膜裝置 1 0 A 前段的逆滲透膜模組 10a 逆滲透膜裝置 1 0 B 後段的逆滲透膜模組 11 原水供給水泵 12 原水供給第1配管 13 原水供給第2配管 14 透過水流出配管 15 流動方向轉換用配管 16 透過水流出配管 17 濃縮水流出配管 18 返回配管 28 多段式分離膜裝 29a 前段分離膜裝置群 29b 後段的分離膜裝置群 3 0b 分離膜核組 47 312/發明說明書(補件)/92-11 /92122684 1235682 30b 分離膜模組 31a 分離膜裝置 31b 分離膜裝置 3 1c 分離膜裝置 32a 原水供給第1配管 33a 原水供給第2配管 3 4a 透過水流出配管 3 4b 透過水流出配管 3 5a 流動方向轉換用配管 36a 濃縮水流出第1分歧配管 3 6b 濃縮水流出第1配管 37a 濃縮水流出第2分歧配管 37b 濃縮水流出第2配管 38 原水供給主配管 3 9 原水流出第1配管 4 0a 原水供給分歧配管 4 0b 原水供給分歧配管 4 1 第1濃縮水供給主配管（原水供給主配管） 42 原水供給第2配管 4 3 透過水流出配管 45 濃縮水流出第1配管 46 濃縮水流出第2配管 4 7 原水流出第2配管（原水流出配管） 48 分離膜模組 48 312/發明說明書(補件)/92-11/92122684 1235682 50 泵 5 1 濃縮水集水配管 6 0 透過水集水管 6 1 逆滲透膜 6 2 外裝體 6 3 凸緣 64 可伸縮擋止塊 6 5 螺旋型膜元件 66 室 6 7 間隙 68 鹽封 6 9 逆滲透膜模組 7 1 a〜7 1 d 分離膜模組 7 1 e、7 1 f 分離膜模組 7 1 g 分離膜模組 72a 分離膜裝置群 72b 分離膜裝置群 72c 後段的分離膜裝置群 7 3a 分離膜裝置群 73b 後段的分離膜裝置群 7 4 a〜7 4 c 分離膜模組 7 4 d、7 4 e 分離膜模組 75a 前段的分離膜裝置群 75b 後段的分離膜裝置群 312/發明說明書(補件)/92-11 /92122684 49 1235682 7 6 a、7 6 b 分離膜模組 7 6c 分離膜模組 77a 前段的分離膜裝置群 77b 後段的分離膜裝置群 78a 分離膜模組 7 8b 分離膜模組 12 1 濃縮水流出第2分歧配管 15 1 濃縮水流出第1分歧配管 50 312/發明說明書(補件)/92-11/92122684The degree of turbidity is attached to the viscous and viscous substance. The process is turbid and turbid. The turbidity is attached to the road. The turbidity is attached to the road. The flow is viscous. Slightly slightly slightly original, slightly, extremely, very slightly, a few plugs, and the blockage is completely completed. I. Example of the installation of the film segment 11 is used in the multi-purpose segment of the multi-use and release film device embodiments 7 to 12. After 2 0 0 0 hours, there was almost no increase in the water pressure difference and no decrease in the amount of permeated water, and the quality of the permeated water was also high. 44 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 In the performance evaluation after 200 hours, although Comparative Example 1 is not inferior to Examples 1 to 6, and Comparative Example 3 is not inferior to Implementation Results of Examples 7 to 12 'But this is because the pre-processing device is installed, and there is a need for an extra installation place and installation cost. Thus, the comparison target of Examples 1 to 5 is Comparative Example 2, the comparison target of Examples 7 to 11 is Comparative Example 4, and the comparison target of Example 12 is Comparative Example 5, but Comparative Examples 2, 4 and 5 In any of the cases, the turbidity was extremely serious at about 800 hours and the amount of permeated water became zero. The comparison target of Example 6 is Comparative Example 1, but Example 6 shows very excellent performance and is inexpensive. (Industrial Applicability) According to the operation method of the separation membrane module of the present invention, the turbidity accumulated on the intersection portion of the raw water separator can be easily peeled off and removed. In addition, there is no problem in reducing the flushing flow rate caused by the low-pressure or ultra-low-pressure reverse osmosis membrane module. At the same time, it also has a back pressure generated immediately after the valve on the water side is closed to deposit on the membrane The effect of alleviating the tightness of the contaminated substances can further improve the flushing effect. In addition, the pressure against the membrane surface can be relieved by removing the pressure on the supply side of the raw water. Therefore, the membrane is slightly loosened, and the dense pressure of the turbidity accumulated on the membrane surface and the raw water separator can be relaxed. According to the separation membrane device of the present invention, the above-mentioned operation method can be carried out reliably by a simple device. [Brief description of the drawings] Fig. 1 is a flowchart showing a device for implementing a method for operating a separation membrane module according to an embodiment of the present invention. FIG. 2 is a flowchart showing a device for operating a method of separation membrane module 45 312 / Invention Specification (Supplement) / 92-11 / 92122684 1235682 of another embodiment of the present invention. Fig. 3 is a flowchart showing an apparatus for implementing a method for operating a separation membrane module according to still another embodiment of the present invention. Fig. 4 is a diagram showing an example of the structure of a separation membrane module according to this embodiment. Fig. 5 is a flowchart showing a multi-segment separation membrane device according to an example of this embodiment. Figs. 6 (A) to (C) are another flowcharts showing the multi-segment separation membrane device according to this embodiment. Fig. 7 is a flowchart showing a multi-stage separation membrane device used in Examples 1 to 11; FIG. 8 is a schematic diagram of a conventional reverse osmosis membrane module. FIG. 9 is a flowchart of an example of a conventional multistage separation membrane device. (Description of component symbols a first valve a 1 wide b second valve bl valve c valve cl valve d valve dl valve e valve el valve 312 / Instruction Manual (Supplement) / 92-11 / 92122684 46 1235682 f Raw water flows out of the first Piping valve g valve h valve I valve J valve K valve 1 valve m raw water outflow second piping valve (raw water outflow piping valve in the later stage) 10 reverse osmosis membrane device 1 0 A reverse osmosis membrane module 10a reverse osmosis membrane device 1 0 B Reverse osmosis membrane module at the rear 11 Raw water supply pump 12 Raw water supply first pipe 13 Raw water supply second pipe 14 Permeate water outflow pipe 15 Flow direction changeover pipe 16 Permeate water outflow pipe 17 Concentrated water outflow pipe 18 Return pipe 28 Multi-stage separation membrane installation 29a Front stage separation membrane device group 29b Rear stage separation membrane device group 3 0b Separation membrane core group 47 312 / Instruction manual (Supplement) / 92-11 / 92122684 1235682 30b Separation membrane module 31a Separation membrane device 31b Separating membrane device 3 1c Separating membrane device 32a Raw water supply first pipe 33a Raw water supply second pipe 3 4a Permeate water outflow pipe 3 4b Permeate water outflow pipe 3 5a Flow direction conversion pipe 36a Concentrate Water flows out of the first branch pipe 3 6b Concentrated water flows out of the first pipe 37a Concentrated water flows out of the second branch pipe 37b Concentrated water flows out of the second pipe 38 Raw water supply main pipe 3 9 Raw water flows out of the first pipe 4 0a Raw water supply branches of the pipe 4 0b Raw water Supply branch pipe 4 1 The first concentrated water supply main pipe (raw water supply main pipe) 42 raw water supply second pipe 4 3 permeate water outflow pipe 45 concentrated water outflow first pipe 46 concentrated water outflow second pipe 4 7 raw water outflow second Piping (raw water outflow piping) 48 Separation membrane module 48 312 / Instruction manual (Supplement) / 92-11 / 92122684 1235682 50 Pump 5 1 Concentrated water collection pipe 6 0 Permeate water collection pipe 6 1 Reverse osmosis membrane 6 2 Outside Body 6 3 Flange 64 Telescopic stop 6 5 Spiral membrane element 66 Room 6 7 Gap 68 Salt seal 6 9 Reverse osmosis membrane module 7 1 a ~ 7 1 d Separation membrane module 7 1 e, 7 1 f Separation membrane module 7 1 g Separation membrane module 72a Separation membrane device group 72b Separation membrane device group 72c Separation membrane device group 7 3a Separation membrane device group 73b Separation membrane device group 7 4 a ~ 7 4 c Separation Membrane module 7 4 d, 7 4 e Separation membrane module 7 5a Separate membrane device group in the front stage 75b Separate membrane device group in the later stage 312 / Invention manual (Supplement) / 92-11 / 92122684 49 1235682 7 6 a, 7 6 b Separate membrane module 7 6c Separate membrane module 77a Separation membrane device group 77b Separation membrane device group 78a in the subsequent stage Separation membrane module 7 8b Separation membrane module 12 1 Concentrated water flows out of the second branch piping 15 1 Concentrated water flows out of the first branch piping 50 312 / Instruction book (Supplement) / 92-11 / 92122684