550113 A7 __ B7_ 一 五、發明說明（I )550113 A7 __ B7_ I. V. Description of the invention (I)
V 一、 發明所屬之技術領域] 本發明係有關可適用於固液分離、離子除去、溶解性 有機物除去、膠乳濃縮、膠態矽酸濃縮、有價物回收、廢 液處理、金屬分級、自來水過濾、活性污泥處理、自來水 管污泥處理、食品廢液處理、COD(化學需氧量）減低、 BOD(生化需氧量）減低、淤漿及膠乳成份的過濾濃縮法 (diafiltration)等的旋轉型膜分離裝置及使用旋轉型膜分離 裝置之膜分離方法。 二、 先前技術 爲了將水中溶解了各種物質的液體(被處理液)分離成 淨水(透過液)與粒子濃度高的濃縮液，係使用膜分離裝置 。膜分離裝置雖有各種形式，不過，例如廣泛施行使用錯 流(crossflow)方式的膜分離。如第44圖所示，此錯流方式 ，是藉供給泵52對具有分離成透過液與濃縮液之功能的膜 模組51壓送被處理液，經過路徑53自膜模組51取出透過 液，經過路徑54自模組51取出濃縮液，經過路徑54使此 濃縮液回流至膜模組51，之後，沿著路徑54與55循環多 數次濃縮液，來增加其濃縮度的方式。然而，爲了以錯流 方式進行高濃縮，雖然其於減低濃差極化、積化（fouling) 或流路堵塞而須藉供給泵52高流速循環被處理液，但卻因 此需要大型供給泵，使得泵所需能量增大。雖說泵需要能 量，卻由於形成於膜表面附近的速度界限膜的影響，以致 於不易減低積垢或濃差極化，其結果，無法進行高濃縮。 ^__3_ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） ---I------------— — — — — $111-- (請先閲讀背面之注意事項再填寫本頁) 550113 A7 ____ B7_______ 五、發明說明（ 而且，即使高流速循環被處理液，亦由於透過流速小，故 爲了濃縮至一定程度以上的濃度，須增加循環次數，不過 ，若循環次數增多，被處理液受到泵的進給扇葉等剪切的 次數即增加，而有被處理液變質的情形發生。 又，亦已知有藉蒸發濃縮裝置或離心分離器被處理液 分離成淨水與濃縮液的方法，不過，此方法之缺點爲液體 分離所需之能量大，又，精密之分離困難，因此水的潔淨 度低。 於是，作爲膜不易堵塞、透過流量高、且能濃縮至高 濃度的膜分離裝置，出現了一種旋轉型膜分離裝置。此旋 轉型膜分離裝置，一般來說，係以貫通容器中心部之方式 配設旋轉軸，沿此軸的軸長邊方向安裝多數個膜體，一面 使旋轉軸與膜體一起旋轉，一面進行膜分離的方式。此膜 體，具備表面形成有防止一定程度以上粒子通過的小孔的 多孔質構造，將具有可輸送透過液的路徑的透過性膜安裝 於板兩面，藉由僅使投入容器內的被處理液中的極微細物 質穿過膜體之小孔，而能獲得透過液。於此情形下，爲了 防止被處理液中一定程度以上大小的粒子堵塞膜的小孔、 或粒子附著、堆積於膜表面的積垢，因此係使旋轉軸旋轉 ，以旋轉安裝於旋轉軸的膜體。不過由於僅藉由旋轉，來 使被處理液與膜體一起旋轉，因此無法充份發揮膜體的旋 轉效果，故膜孔的堵塞防止效果不彰。因此，作爲更有效 的謀求膜孔堵塞防止的手段，提出了一種藉由於膜體表面 發生亂流以防止一起旋轉，以有效轉換膜體表面的被處理 4 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公髮1 ' (請先閱讀背面之注意事項再填寫本頁) •裝 訂·- -線· 550113 A7 ___ B7___ 五、發明說明) 液的方法。又，藉由發生亂流，亦可達濃差極化的減低， 藉此，可達到高濃縮。此外，亦可提高膜的阻止性能。 例如，如第45(b)圖所示，以貫通具有加壓被處理液的 供給入口 61的圓筒狀容器62的中心部之方式配設中空旋 轉軸63，將具有可輸送透過液的構造的多數個膜體64安 裝於旋轉軸63，使透過膜體64的液體自膜體64，經設於 旋轉軸63的小孔通過中空旋轉軸63內部，自出口 65、66 排出，將濃縮液自出口 67排出，於膜體64兩側、與膜體 64相隔一間隙，設置能大致全面覆蓋膜體64之環形擋件 68，固定於容器62的旋轉型膜分離裝置較爲人知(以下， 稱「習知膜分離裝置1」）。例如，日本特開平6-277465號 揭露了一種與習知膜分離裝置1相同種類的裝置。 根據習知膜分離裝置1，若藉未圖示之馬達使旋轉軸 63與膜體64 —齊旋轉，即能積極的在旋轉的膜體64表面 與靜止的環與構件68之間的間隙產生亂流，而能期待具有 膜孔堵塞防止效果。不過，由於環形擋件68完全分隔膜體 之間，擋件68覆蓋膜體64的面積廣大，容器62內的被處 理液通過狹長流路69，故壓力損失增大，無法有效率地透 過。又，由於壓力損失，故若施加於膜體64的壓力產生不 均勻時膜體64之撓曲便會大，造成膜體64與環形擋件68 接觸’而造成強度較弱的膜體64產生破損的情形。再者， 於裝入容器62之際，需交互的組裝膜體64與環形擋件68 ，裝置組裝非常繁瑣。 因此，如第46(a)圖所示，爲了減低上述壓力損失，提 _______5 _ 本紙張尺度適用中國國家標準（CNS)A4規格（21〇 χ 297公釐） II------ (請先閲讀背面之注意事項再填寫本頁) 訂·- --線- 550113 A7 _____B7___ 五、發明說明（f) 出了一種於環形擋件之周緣部開設孔70的開孔擋件71(以 下，稱「習知膜分離裝置2」）。不過，習知膜分離裝置2 由於係在擋件上開孔，故加工成本升高，與習知膜分離裝 置1相同的，於裝入容器62之際，需交互組裝膜體64與 開孔擋件71，而有裝置組裝非常繁瑣的缺點。 又，由於習知膜分離裝置1、2的擋件68與71都均 勻的覆蓋於膜表面，故亦有被處理液亂流小的缺點。 再者，習知旋轉型膜分離裝置1、2，其有效發揮膜分 離性能之適當的膜分離條件及裝置規格不明確，無法保證 經濟而又有效的膜分離裝置的運轉。 本發明有鑑於習知技術所具有之上述問題點，其目的 在於，提供一裝置組合不費事、成本低，且壓力損失小， 有效率地進行透過處理，能有效發揮膜分離性能的旋轉型 膜分離裝置以及使用旋轉型模分離裝置的膜分離方法。 三、發明內容 爲達成上述目的，本發明，係於旋轉型模分離裝置的 旋轉軸的膜體兩側，與膜體間相隔間隙配設複數個長方形 擋件，且作成隔著旋轉軸、將複數個長方形擋件自容器之 一內壁附近至另一內壁附近彼此平行配置，由於擋件係非 均勻的覆蓋膜面，故亂流大，濃差極化與積垢的減低效果 較大，因此透過流量顯著增大，因擋件的存在所造成之壓 力損失小，由於構件形狀簡單，故無需施以特別加工成本 較低，且由於可在將膜體安裝於旋轉軸後插入擋件，故裝 _6_ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） I!--丨！ — 丨！ i I (請先閱讀背面之注意事項再填寫本頁) 訂·- 線. 550113 A7 _ B7 ___ 五、發明說明（f ) v/ 置的組裝簡單。 亦即，本發明爲一種旋轉膜分離裝置’係以貫通具有 被處理液供給入口之容器的方式配設旋轉軸者’其特徵在 於：於上述容器內，將具有可輸送透過液構造的膜體安裝 於上述旋轉軸，具有連接於上述膜體用以排出透過液的出 口，於上述膜體兩側與膜體間相隔一間隙配設複數個長方 形擋件，於容器內壁面設置連接於被處理液供給入口的液 體流路，隔著旋轉軸、自容器之一內壁附近至另一內壁附 近，彼此平行配置複數個長方形擋件。 根據以上述方式構成之本發明的膜分離裝置’如第7 圖所示，當使膜體12如箭頭A所示般向右方向旋轉時’ 自供給入口供至容器內的加壓被處理液，即在長方形構件 13的左側’如箭頭B所不’由沿者谷窃內壁15之流路16 ，沿長方形擋件朝容器內側流動’另一方面’於長方形擋 件13的左側，如箭頭C所示，膜體12表面的被處理液， 沿容器內壁15之流路16排出。藉形成於此種沿著膜體表 面與容器內壁的流路的被處理液的液流，使被處理液不致 於停滯在膜表面，平穩進行朝容器內部外側流動的液體與 朝外部側流動的液體的轉換。復由於被處理液藉非均勻安 裝的擋件而產生亂流，故能降低積垢、濃差極化，有效率 地進行膜分離。 以下，就有關本發明之旋轉型膜分離裝置及使用旋轉 型膜分離裝的膜分離方法的特徵及有利效果加以說明。 (1)擋件的支持固定 ____2_ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） (請先閱讀背面之注意事項再填寫本頁) •-裝 ·.線· 550113 A7 ____B7_____ 五、發明說明（L ) 若藉獨立於容器壁外的支持體來支持固定擋件的兩端 部的話，裝置的組裝即變得容易，可謀求成本之降低。 (2) 擋件形狀 ① 鉤形擋件、S形擋件與圓弧形擋件 可於膜體兩側與膜體間相隔一間隙配設鈞形擋件，隔 著旋轉軸、將複數個鈞形擋件相對膜體直徑配置成線對稱 或相對旋轉軸配置成點對稱。又，亦可於膜體兩側與膜體 間相隔一間隙配設S形擋件，隔著旋轉軸、將複數個S形 擋件相對旋轉軸配置成點對稱。及，亦可於膜體兩側與膜 體間相隔一間隙配設圓弧形擋件，隔著旋轉軸，將複數個 圓弧形擋件相對膜體直徑配置成線對稱或相對旋轉軸配置 成點對稱。無論使用鈞形擋件、S形擋件或圓弧形擋件， 均可期待與長方形擋件相同的效果。此外，若使用釣形擋 件、S形擋件或圓弧形擋件的話，具有可增大膜面的亂流 ，提高膜分離性能的效果。又，亦具有促進膜體間流體轉 換的效果。 ② 輻射狀擋件 若擋件係非均勻的覆蓋膜面時，由於亂流增大、濃差 極化與積垢的減低效果變大，故透過流量增大’檔件存在 所造成之壓力損失變小。例如，若採用以旋轉軸爲中心向 容器內面成輻射狀配設複數個擋件而構成的擋件(轄射狀擋 件)的話’透過流量即變大。 (3) 擋件相對於膜體表面積的投影面積 ①長方形擋件、釣形擋件、S形擋件與圓弧形擋件的情形 _8_ —_ 本紙張尺度適用中_家標準（CNS)A4規格（21G x 297公楚 1 (請先閱讀背面之注意事項再填寫本頁) ;裝 · 550113 A7 ______Β7___ 五、發明說明（^1) 若係長方形擋件、釣形擋件、S形擋件與圓弧形擋件 時，擋件相對膜體表面積之投影面積以1至90%較佳。其 原因在於，不滿1%的話，膜體表面的亂流促進效果即變少 ，若超過90%，被處理液的壓力損失即變得過大。其原因 在於，如後述實施例(參考第22圖），即使擋件相對於膜體 表面積的投影面積爲1%，透過流量亦較無擋件之場合明顯 增加，並超過90%，透過流量會大幅降低。 再者，本發明對象的技術領域，雖因被處理液的性質 、處理目的或處理成本而有不同，但大多要求在某一定値 以上的透過流量，由於要求平均透過流量在30L(升）/m2 /hr以上，因此，如後述第22圖所示，爲了滿足此種透 過流量的要求，在長方形擋件、釣形擋件、S形擋件與圓 弧形擋件之場合，擋件相對於膜體表面積的投影面積以1〇 至90%較佳，爲了使裝置內的壓力損不上昇而僅增加透過 流量，尤佳的是擋件相對於膜體表面積的投影面積爲26至 70%。 ©輻射狀擋件的情形 若係輻射狀擋件時，擋件相對於膜體表面積的投影面 積若不滿30%，則膜體表面的亂流促進效果將變少，若超 過70%，被處理液的壓力損失將過大。因此，輻射狀擋件 相對於膜體表面積的投影面積以30至70%較佳。 (4)膜體直徑與膜體轉數 ①長方形擋件、鈞形擋件、S形擋件與圓弧形擋件情形下 在使用長方形擋件、釣形擋件、S形擋件和圓弧形擋 _9_____ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） ----I---II----i I (請先閱讀背面之注意事項再填寫本頁) · 線- 550113 A7 B7_ — 五、發明說明（f) 件時，膜體直徑以200至1100mm較佳。其原因在於’若 不滿200mm的話，爲了作成具有充份膜分離能力的裝置’ 膜體片數將會過多，裝置與旋轉軸過長，超過1100mm的 裝置在製造上很困難，會導致製造成本大幅增加，又’旋 轉所需動力亦會大幅增大之故。此外，如後述實施例(參考 第24圖)所示，若膜體直徑不滿200mm，膜體轉數較慢時 ，無法獲得充份實用程度大小的透過流量，當膜體之轉數 較慢時(例如，在20rpm以下時），雖然膜體之直徑增加透 過流量亦會增加，但即使膜體直徑超過1100mm，透過流 量亦不會上升之故。 又，在使用長方形擋件、鈞形擋件、S形擋件與圓弧 形擋件時，膜體轉數以20〜180〇rpm較佳。其原因在於， 若不滿20rpm的話，將幾無膜孔堵塞防止效果與濃差極化 降低效果，若超過1800rpm的話，則因離心力變得過大， 而如上述般，降低透過效率，此外，旋轉所需動力會大幅 增大之故。其原因復在於，如後述實施例(參考第25圖)所 示’若膜體轉數不滿2Grpm的話，透過流量會顯著變小， 即使超過1800rpm，透過流量亦不會上升之故。 ©輻射狀擋件的情形 爲了作成能確保既定透過流量、現實要求的處理量的 工業裝置，需有一定程度以上(例如1〇m2以上)的膜面積。 然而’在膜體直徑不滿300mm時，爲了確保所需的膜面積 ，需要非常多片的膜體，裝置與旋轉軸會過長，不易作爲 一現貫的工業裝置。另一方面，若膜體直徑大，透過量即 張尺度適用中國國家標準（CNS)A4規格（210 X 297公餐^ ---- (請先閲讀背面之注意事項再填寫本頁) •裝 --線- 550113 A7 _ _ B7________ 五、發明說明Ο ) 增加，又，雖然可縮短旋轉軸，但旋轉所需動力部會增大 至膜體直徑的5次方，有無法很經濟運轉的不當情形發生 。並且，即使膜體直徑大到一定程度以上，透過流量的上 昇量仍少。 因此，在使用輻射狀擋件情形下，膜體直徑在30()至 1000mm的範圍內，由於能實現經濟且有效率的膜分離裝 置，以此較佳。在旋轉具有此範圍的直徑的膜體時’若膜 體轉數不滿5〇rpm，即幾無膜孔堵塞防止效果、積垢防止 效果或濃差極化減低效果，無法獲得可充份實用程度的大 小的透過流量。另一方面，若膜體轉數超過i〇〇〇rpm，離 心力會變得過大，施加於加壓被處理液的對透過有效的壓 力會抵消而使透過效率降低，又，旋轉所需動力會大增加 。因此，在使用輻射狀構件情形下，膜體轉數最好是在50 至lOOOrpm的範圍內。 (5)擋件數量 ① 長方形擋件、鈞形擋件、S形擋件與圓弧形擋件情形下 若設於膜體一側的檔件數太多，即有安裝困難的缺點 ，又由於如後述實施例(參考第21圖)所不，即使檔件數增 加到超過2〇個’透過流量亦不會上昇，故長方形擋件、鈞 形擋件、s形擋件與圓弧形擋件的數量，以1至20個較佳 〇 ② 輻射狀擋件的情形 若輻射狀擋件的個數少，透過流量即小，若擋件數量 增加，透過流量即增大，但將輻射擋件數量增加至一定數 ___ 11____ 1本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐7" " (請先閱讀背面之注意事項再填寫本頁) •裝 訂： --線· 550113 A7 ____B7_ 五、發明說明（//(；) 目以上’透過流量亦不會變大。因此，輻射狀擋件的數量 以4至12個較佳。 (6) 膜體與擋件的間隙 ① 長方形擋件、鈞形擋件、S形擋件與圓弧形擋件情形下 在長方形擋件、鈞形擋件、S形擋件與圓弧形擋件時 ’月旲體與擋件之間隙最好是能作成2〜18mm。若不滿2mm ’月旲體與擋件容易接觸，膜體有可能破損，若超過18mm ’旋轉軸即變長，收容膜體的容器的容積過大而不實際， 又’膜體與擋件之距離會變得過於分開，使得擋件所產生 的亂流促進效果變小。其原因復在於，若如後述實施例(參 考第26圖）所示，膜體與擋件之間隙不滿2mm或超過 18mm ’即無法獲得可充份實用程度大小的透過流量。 ② 輻射狀構件 若係輻射狀構件時，膜體與擋件的間隙以2至12mm 較佳。其原因在於，不滿2mm的話，膜體與輻射狀擋件即 容易接觸，會有膜體破損的情形發生，若超過12mm，膜 體與輻射狀構件的距離即會過於分開，無法期待輻射狀構 件的亂流促進效果，爲確保所需之膜面積，裝置全長會變 長而不經濟。 (7) 膜體的旋轉速度 若係長方形擋件、釣形擋件、S形擋件與圓弧形擋件時， 膜體的旋轉速度，在外周以1至30m(米)/sec(秒)較佳。 其原因在於，若是不滿lm/sce的低速的話，幾乎沒有膜 孔堵塞防止效果與濃差極化減低效果，若超過30m/sce的 ____12_ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） (請先閱讀背面之注意事項再填寫本頁) -裝 i線- 550113 A7 _____B7_ 五、發明說明（11 ) --------------裝--- (請先閱讀背面之注意事項再填寫本頁) 話，因離心力變得過大’施加於加壓被處理液的對透過有 效的壓力會被抵消而使得透過效率降低’此外，旋轉所需 動力會大幅增大之故。其原因復在於，若如後述實施例(參 考第23圖)所示，若膜外周速度不滿lm/sce，則無法獲 得可充分實用程度大小的透過流量，不論是低濃度的液體 或是高濃度的液體，只要膜外周速度超過30m/SeC，透過 流量即會降低之故。（8)擋件的厚度 -線· 無論是長方形擋件、釣形擋件、S形擋件與圓弧形擋 件，或是輻射狀擋件，使用任何形狀的擋件，擋件皆應與 旋轉的膜體之間相隔一間隙而設置，以使此擋件不會與膜 體接觸。另一方面，爲了使擋件不會佔據大的容積，最好 是能使其厚度儘量薄。不過，如果太薄，由於易於撓曲而 會有與膜體接觸產生破損的情形，因此，擋件以1mm以上 的厚度較佳。然而，爲求不佔據大的容積，又爲求膜體間 的間隙不致於過大，裝置與旋轉軸不致於又長又大，擋件 的厚度以在20mm以下較佳。又，爲求不易撓曲，擋件的 材質雖未特別限定，但以鐵、不銹鋼等各種金屬、塑膠、 陶瓷、玻璃纖維強化塑膠較佳。 (9) 擋件的寬度 若係長方形擋件、鈞形擋件、S形擋件和圓弧形擋件 時，擋件的寬度最好是膜體直徑的0.1至40%。其原因在 於’不滿0.1%的話，膜體表面的亂流促進效果即少，若超 過40°/。，被處理液的壓力損失會過大。 (10) 容器直徑與膜體直徑之比 _____13_ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公楚） 550113 A7 ___B7____ 玉、發明說明（f L) 容器內徑與膜體直徑之比以1·〇〇3至3.000較佳。其 原因在於，不滿1.003的話，膜體所佔面積過大，被處理 液的壓力損失會變得過大之故。另一方面，若超過3·000 的話，膜體所佔面積過小，以致於膜分離效率降低’因此 不佳。 (11) 被處理液的壓力 若導入容器內的被處理液的壓力超過20mm，即有容 器的耐壓困難的不當情形發生，要是不滿〇.〇〇5MPa，實際 上容器內的水位即不滿〇.5m，而有膜體未浸入被處理液的 不當情形發生，因此，導入容器內的被處理液壓力以 0.005MPa 至 20MPa 較佳。 (12) 膜體旋轉時的徑向加速度 當旋轉膜體時，朝向圓外側的徑向加速度即作用於與 膜體一起旋轉的膜體附近的被處理液。根據發明人的發現 ，顯然此徑向加速度對膜分離性能有影響。亦即，在被處 理液爲高濃度時，於膜體旋轉時的徑向加速度在200m/ see2以上的範圍的運轉，在被處理液爲低濃度時，膜體旋 轉時的徑向加速度在lOOm/sce2以上的範圍內運轉，藉此 ，對應被處理液的黏性而對透過有效的剪力施加於被處理 液，使透過流量變大。 (13) 膜體的厚度 膜體的厚度以1至20mm較佳。其原因在於，不滿 1mm的話，強度即不充份，若超過20mm的話，收容膜體 的容器容積即會變得過大之故。 ____14 _ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐〉 (請先閱讀背面之注意事項再填寫本頁) •—裝 )0J· --線- 550113 A7 ____ B7_____ 五、發明說明)) (14) 膜體的形狀 膜體的形狀雖可採用圓形’不過’不限於圓形’亦可 爲五角形以上的多角形。 (15) 裝置的小型化 若採用旋轉軸爲中空，且於軸縱長方向的膜體安裝部 份設有小孔，膜體爲將具有可輸送透過液的路徑的透過性 膜安裝於板兩面的構造’使上述透過性fe的透過液輸送路 徑與設於旋轉軸的小孔連通的配置的話’即亦可利用旋轉 軸來作爲透過液的排出裝置，因此’有膜分離裝置小型化 的優點。 (16) 直徑的意涵 於本說明書中，「直徑」除意指「通過圓或球的中心 ，於圓周或球面上具有兩端的線段份」’亦意指「於多角 形中，自其中心至一頂點的距離2倍長度的線段份」。 由於本發明旋轉型膜分離裝置及使用旋轉型膜與分離 裝置之分離裝置如上述構成，故可獲得如次效果。 (1)根據申請專利範圍第1項、第2項、第3項及第4項所 記載之旋轉型膜分離裝置，由於構件不是完全隔開膜體間 的構造，故擋件所造成被處理液的壓力損失少，具有優異 的膜分離性能。 復由於無需交替裝上膜體與構件，故可在裝上旋轉軸 與膜體後，自層疊膜體的橫向插入擋件，故安裝不費事。 進一步的由於擋件形狀簡單，故加工簡單，成本低。 並且，由於可對應被處理液的性狀，任意變更擋件寬 _____J15__ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） (請先閲讀背面之注意事項再填寫本頁) 裝 訂· · 550113 A7 _B7_ 五、發mm (\十 (請先閱讀背面之注意事項再填寫本頁) 度、厚度或個數，故作爲對象的被處理液的種類沒有限制 ，應用性優異。 (2) 特別是，申請專利範圍第2項、第3項及第4項所記載 之旋轉型膜分離裝置具有於膜面發生的亂流大，可提高膜 分離性能的優點。又，亦具有促進膜體間流體的轉換的優 點。 (3) 特別是申請專利範圍第5項、第6項、第7及第8項所 載之旋轉型膜分離裝置，由於其擋件相對於膜體表面積的 投影面積在適當範圍內，故透過流量變成極大。 (4) 特別是申請專利範圍第9項、第10項、第11項及第12 項所記載之旋轉型膜分離裝置，由於其將長方形擋件、鈞 形擋件、S形擋件或圓弧形擋件的兩端部支持固定，故裝 置的組裝容易，可謀求成本降低。 _線- (5) 特別是申請專利範圍第13項所記載之旋轉型膜分離裝 置具有容易安裝擋件的優點。 (6) 特別是申請專利範圍第28項所記載之旋轉型膜離裝置 ，具有膜分離效率極優的效果。 (7) 特別是申請專利範圍第15項所記載之旋轉型膜分離裝 置具有裝置的大小適當，具有可壓低製造成本及運轉成本 的優點。 (8) 特別是根據申請專利範圍第17項及第19項所記載之旋 轉型膜分離裝置，具有擋件不易撓曲，膜體不易破損的優 (9) 特別是申請專利範圍第21項所記載之旋轉型膜分離裝 _16_ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） 550113 A7 ——_,__SI______ 五、發明說明（/() 置’具有裝置小型化的優點。 (請先閱讀背面之注意事項再填寫本頁) (10) 特別是根據申請專利範圍第22項、第23項、第24項 、第25項及第26項所記載之發明，可提供有效發揮膜分 離性能的旋轉型膜分離裝置。 (11) 特別是根據申請專利範圍第29項及第30項所記載之 膜分離方法，膜不易堵塞，透過流量高，可濃縮至高濃度 。復由於無需高流速供給被處理液，不用大型的泵等壓送 裝置，故動能成本低，由於無需增加循環次數來增加濃度 ，故被處理液鮮少被泵的進給扇剪切，有被處理液不易變 質的效果。 (12) 特別是，根據申請專利範圍第31項、第32項及第33 項所記載之發明，可提供有效發揮膜分離性能的旋轉型膜 分離裝置的運轉條件。 ;線. 四、實施方式 以下，參照圖式就本發明實施形態加以說明，惟本發 明並不因下述實施形態而受到任何限制，於不悖離本發明 技術範圍的範疇內，該業者可適當變更或修正實例。又， 於後述有關膜分離特性的比較檢查實驗中，本發明實施形 態雖然顯示主要係用長方形擋件或輻射狀擋件的情形，不 過，亦可於本發明技術範圍內，就申請專利範圍所載之外 的其他形狀的擋件指出其具有相同效果，並不限於實驗所 用的擋件。 第1圖是本發明旋轉型膜分離裝置的立體圖。1係被 一 —_____17____ 本紙張尺度適用中國國家標準（CNS)A4規格（210 χ 297公釐） 550113 A7 ____B7___ 五、發明說明（I L) --------------裝--- (請先閲讀背面之注意事項再填寫本頁) 處理液供給入口，以貫通圓筒狀容器2的中心部之方式配 設中空旋轉軸3，透過安裝了中空旋轉軸3的多數膜片(第 2圖中標號12)的液體，通過中空旋轉軸3內部自出口 4、 5排出，濃縮液則自出口 6排出。7係使膜體與旋轉軸3同 時旋轉的馬達，馬達7的旋轉力，係藉皮帶8傳輸至旋轉 軸3。旋轉力的傳輸不限於此，亦可使用馬達直接耦合型 、齒輪減速機、撓帶傳動裝置。 如第5a、b圖所示，本實施例所用膜體是將聚醚楓製 透過性膜11安裝於聚丙烯製板體9兩面，其間介有織布的 隔離布10的構造。且，除了本實施例所用塑膠板外，亦可 使用金屬板或陶瓷板來作爲透過性膜安裝板，亦即，最好 是採用不易變形，耐破損的強固材質。 ，線· 於本說明書中，透過性膜係具有多孔質構造，於內部 形成可移送藉由經多孔質部份透過的液體的路徑(藉由連接 多孔質部份所形成的流路），只要是具有此種功能的膜，除 上述有機膜以外，亦可採用陶瓷或金屬膜。 隔離布10亦可輸送透過液，隔離布10內的透過液流 路的直徑較透過性膜11的透過液輸送路徑27大，透過液 容易流入隔離布10內。 如第2圖所示，將塑膠製板體9、隔離布10以及由透 過性膜11構成的膜體12安裝於旋轉軸3，於膜12兩側， 與膜體間相隔一間隙，自容器2之一內壁附近至另一內壁 附近，隔著旋轉軸3分別相互平行配置2不綉鋼製長方形 檔件13，（參考第2a圖），複數長方形擋件13的兩端藉連 18 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐) 〜^' 550113 A7 ___B7____ 五、發明說明（丨 接容器2的面2a與2b的貫通螺釘14支持固定。又，連於 被處理液供給入口 1的液體流路16，係沿容器2的內壁面 15形成。 如第5a圖所示，旋轉軸3爲中空，於軸長班方向的膜 體12安裝部份設置小孔π，構成膜體12透過性膜11的 透過液輸送路徑以及隔離布10的透過液輸送流路連通小孔 Π。18是在膜體12的旋轉軸安裝部份，夾裝於上下相鄰 的膜體12、12間的隔件。又，亦可採用如第5b圖所示， 沿旋轉軸3安裝隔件18與膜體12部份的軸長邊方向設置 複數條開縫19，利用此開縫19作爲透過液輸送流路，於 旋轉軸3的端部設置小孔17，使透過性膜11的透過液輸 送路徑以及隔離布10的透過液輪送路徑連通小孔17的構 造。第5b圖中雖省略，不過，亦於旋轉軸3的任意位置設 置小孔17。 第3圖係顯示在膜體12兩側，與膜體間相隔一間隙， 自容器2之一內附近至另一內壁附近，夾著旋轉軸3，分 別平行配置4個不綉鋼製長方形擋件20的例子。且，擋件 的材質除了上述金屬製外，亦可使用塑膠或陶瓷。 若供給加壓(約O.IMPa以上的壓力）的被處理液至如以 上構成的膜分離裝置的容器2內，或以被處理液注滿容器 2內，通過旋轉軸3減壓或吸引，使旋轉軸3旋轉時，即 如第6a圖的箭頭24所示，因離心力而產生朝徑向外側流 動的液流。並且由於在膜體12兩側設有擋件13，故會產 生防止堵塞膜體12的膜孔的粒子作用或濃差極化的液流 一___19 __ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） (請先閱讀背面之注意事項再填寫本頁) 丨裝 tl· •-線_ A7 550113 ________B7_____ 五、發明說明（f) 23，如第6b圖所示，膜孔26不會堵塞，自連接於多孔質 部份所形成的路徑27流經隔離布10內流路的透過液經由 第5a、b圖所示小孔π，經由中空旋轉軸3內部，自第1 圖所示出口 4、5排出，另一方面，濃縮液則自出口 6排出 。由於透過液容易自透過性膜內的狹窄透過液輸送路徑27 流過隔離布10內的寬廣流路，故自透過液輸送路徑27直 接流自小孔17的透過液較少，經過隔離布10內的寬廣流 路到達小孔17的透過液較多。就此點而言，爲了確保透過 液容易流過的流路，亦可於板體9形成透過液流路，於此 情形下，無需隔離布10。不過，由於形成透過液流路於板 體9會使成本增高，故就經濟性這一點看來，以採用隔離 布10較佳。 又，作爲擋件，亦可使用如第8圖所示輻射狀擋件。 第8圖係顯示於膜體12兩側，與膜體相隔一間隙，以旋轉 軸3爲中心，成輻射狀向容器2的內壁面15配置8個擋件 28的例子。擋件28的端部藉連接容器2的面2a與2b的 貫通螺釘14支持固定。復且，亦可採用第9圖所示圓弧形 擋件29a，第10圖所示的鈞形擋件29b或第11圖所示S 形擋29C。即使使用這些擋件29a、29b、29c，亦可期待 其具有與長方形擋件相同的效果。並且’根據圓弧形擋件 29a、釣形擋件29b及29c及S形擋件29c，可增大膜面的 亂流，具有提高膜分離性能的效果。又’亦具有促進膜體 間流體的轉換的效果。至於圓弧擋件29a與鈞形擋件29b ，如第9圖及第10圖所示，可於旋轉軸3，相對於旋轉軸 _ 20 _____ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） --------------裝--- (請先閱讀背面之注意事項再填寫本頁) 0 · ;線· 550113 A7 ____一 _B7____ 五、發明說明（j/) 成線對稱配置複數個圓弧形擋件29a或複數個鈞形擋件 29b，或相對於旋轉軸3成點對稱配置複數個圓弧形擋件 29a或複數個釣形擋件29b。至於S形擋件29c，則如第11 圖所示，可夾著旋轉軸3，相對於旋轉軸3成點對稱配置 複數個S形擋件。第9至11圖中雖未圖示，但於膜體12 的另一側亦同樣配置相同數目的擋件29a、29b、29c，除 了擋件形狀不同外，其他構造基本上與第1相同。又，圓 弧形構件29a、釣形擋件29b及S形擋件29C的兩端部分 別連接容器2的面2a與2b(參考第2圖）的貫通螺釘14支 持。 進一步如第12c圖所示，亦可採用類似翼截面形狀的 擋件30。根據此構件30，具有不易與膜體接觸的優點。復 且，亦具有可減低旋轉動力的優點。又，第2圖所示長方 形擋件13、第3圖所示長方形擋件30的長邊方向的截面 ，並未如第2c圖或第3c圖一般變化截面尺寸。本發明的 長方形擋件不限於此處所例示。 其次，就本發明膜分離裝置與習知膜分離裝置於有關 各種特性方面所作比較檢查加以說明。又，以下各實驗中 所用圓筒狀容器2的內徑爲350mm(毫米），除特別揭示外 ，膜體的直徑爲300mm，這些數値於各實驗中共通。 (1)膜分離系統 首先，就可適用本發明膜分離裝置的膜分離系統加以 說明。 亦即，如第13圖所示，經過路徑31貯存於被處理液 ____21_ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公爱) 一 --- --------------裝—— (請先閱讀背面之注意事項再填寫本頁) Ίδτ· -丨線· 550113 A7 _____B7_____ 五、發明說明（/) — — I! — — ! — — · ·11 (請先閱讀背面之注意事項再填寫本頁) 貯存槽的被處理液33以攪拌機34加以攬拌，以泵35對被 處理液加壓至約0.005至20MPa，經過路徑36，壓送至膜 分離裝置37。38是用來除去被處理液中的過濾器，藉膜分 離裝置37膜分離的透過液經由路徑39排出，濃縮液流經 路徑40、41，再度回到貯存槽32，進一步經過路徑36， 供至膜分離裝置37予以膜分離。反覆進行此種膜分離操作 ，逐漸增高濃縮液的濃度。在達到預定濃度時，將此濃縮 液經由路徑42取出。43是閥，44是馬達。又，濃縮液並 不一定非循環不可，藉膜分離裝置37予以膜分離而濃縮的 液體，既可經由路徑42保持原狀排出，亦可一部份回到貯 存槽，一部份排出。在貯存槽32的某性狀的被處理液貯存 於貯存槽32，以相同操作進行膜分離。 ;線. 第14圖顯示設置泵35於膜分離裝置37的透過液排 出路徑39的構造，以此方式藉泵35吸引被處理液而供至 膜分離裝置37情形下，亦可將膜分離裝置37作成開放式 ，可減少膜分離裝置的附屬設備，故具有裝置全體小型的 效果。復由於在第14圖的膜分離系統情形下，供至膜分離 裝置37的被處理液的壓力較小，故亦可期待有不易發生積 垢的效果。 (2)擋件形狀及膜分離時有無旋轉對透過流量的影響 第15圖中顯示了使用第13圖所示膜分離系統來進行 膜分離，檢查濃縮液的濃度與透過流量的關係的結果。本 發明膜分離裝置使用如第2圖所示，於膜體一側及另一側 分別具有2個長方形擋件者，習知膜分離裝置使用如第45 — 22 氏張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） "" 550113 A7 ___ B7___ 五、發明說明（yj) 圖所示旋轉型膜分離裝置以及第44圖所示錯流方式的膜分 離裝置。其膜分離條件如下。 1. 共通條件 a.膜體 UF(超濾)膜(超濾膜，直徑265mm) b·溫度 25^ c.被處理液 膠乳，初期濃度3.3重量％ d·操作壓力 450kpa 2. 旋轉型膜分離裝置的旋轉條件 a.膜體的外圓速度12m/秒 於第15圖中，符號「〇」、「▲」、「#」分別表示 本發明分離方法(使用第2圖的旋轉型膜分離裝置者），使 用第45圖所示旋轉型膜分離裝置的膜分離方法，使用錯流 方式的膜分離方法(於第13圖的膜分離系統中，膜分離裝 置37爲非旋轉型）。如第15圖所示，本發明的膜分離方法 (符號〇)顯示其透過流量遠較錯流方式(符號·)者大，顯示 其透過流量亦較使用第45圖所示旋轉型膜分離裝置的膜分 離方法（符號▲)優異。此係因第45圖的旋轉型膜分離裝 置中，環形擋件68係將膜體之間完全隔開，擋件68覆蓋 膜體64的面積大，容器62內的被處理液通過狹長的流路 69，故壓力損失度大，無法擴大透過流量之故。又，由於 第45圖的旋轉型膜分離裝置中，擋件68係均勻覆蓋膜表 面，故亦有被處理液的亂流小的缺點。 又，錯流方式中，在濃度22.6%下的透過量大致爲〇 ，而無法進一步加以濃縮，不過，本發明膜分離方法即使 一____23___ 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） ----------------- (請先閱讀背面之注意事項再填寫本頁) 訂·- -丨線· 550113V I. Technical Field to Which the Invention belongs] The present invention relates to solid-liquid separation, ion removal, dissolved organic matter removal, latex concentration, colloidal silicic acid concentration, valuables recovery, waste liquid treatment, metal classification, and tap water filtration. Rotation of activated sludge treatment, water pipe sludge treatment, food waste liquid treatment, reduction of COD (chemical oxygen demand), reduction of BOD (biochemical oxygen demand), filtration of slurry and latex ingredients (diafiltration), etc. Membrane separation device and membrane separation method using rotary membrane separation device. 2. Prior art In order to separate a liquid (to-be-treated liquid) in which various substances are dissolved in water into a purified water (permeate) and a concentrated liquid with a high particle concentration, a membrane separation device is used. There are various types of membrane separation devices, but, for example, membrane separation using a crossflow method is widely performed. As shown in FIG. 44, this cross-flow method is to feed the liquid to be processed by the supply pump 52 to the membrane module 51 having the function of separating into permeate and concentrated liquid, and take out the permeate from the membrane module 51 through the path 53. The method of taking out the concentrated liquid from the module 51 through the path 54 and returning the concentrated liquid to the membrane module 51 through the path 54 and then circulating the concentrated liquid many times along the paths 54 and 55 to increase its concentration. However, in order to perform high concentration in a cross-flow manner, although it is necessary to circulate the treated liquid at a high flow rate through the supply pump 52 in order to reduce concentration polarization, fouling, or blockage of the flow path, a large supply pump is required. This increases the energy required by the pump. Although the pump requires energy, due to the influence of the velocity-limiting film formed near the membrane surface, it is difficult to reduce the scale or concentration polarization. As a result, high concentration cannot be achieved. ^ __ 3_ This paper size applies to China National Standard (CNS) A4 (210 X 297 mm) --- I -------------- — — — — $ 111-- (Please read the back first Please pay attention to this page before filling in this page) 550113 A7 ____ B7_______ V. Description of the invention (Moreover, even if the treated liquid is circulated at a high flow rate, the permeation flow rate is small, so in order to concentrate to a concentration above a certain level, the number of cycles must be increased, but, If the number of cycles increases, the number of times the liquid to be processed is cut by the feed fan blades of the pump increases, and the liquid to be processed deteriorates. It is also known that the liquid to be processed is concentrated by an evaporation concentration device or a centrifugal separator. The method of separating into purified water and concentrated liquid. However, the disadvantages of this method are that the energy required for liquid separation is large, and precise separation is difficult, so the cleanliness of water is low. Therefore, it is not easy to block as a membrane, and the permeate flow is high. In addition, a membrane separation device capable of concentrating to a high concentration has appeared a rotary membrane separation device. Generally speaking, this rotary membrane separation device is provided with a rotating shaft so as to penetrate the center of the container, and the axis along this axis A plurality of membrane bodies are installed in the side direction, and the membrane is separated while rotating the rotating shaft together with the membrane body. This membrane body has a porous structure with small holes formed on the surface to prevent particles from passing through to a certain degree. A permeable membrane that transports a permeated liquid is installed on both sides of the plate, and the permeated liquid can be obtained by passing only extremely fine substances in the liquid to be processed put into the container through the small holes of the membrane. In this case, in order to To prevent particles in the treated liquid from clogging the pores of the membrane, or particles to adhere to and accumulate on the membrane surface, the rotating shaft is rotated to rotate the membrane body mounted on the rotating shaft. Rotating the liquid to be processed rotates with the membrane body, so the rotation effect of the membrane body cannot be fully exerted, so the effect of preventing membrane hole clogging is not good. Therefore, as a more effective means for preventing membrane hole clogging, it is proposed It is a kind of treatment that can prevent the rotation of the film body by turbulent flow on the surface of the film body to effectively convert the surface of the film body. S) A4 specification (210 X 297 issued 1 '(Please read the precautions on the back before filling in this page) • Binding ·--Thread · 550113 A7 ___ B7___ V. Description of the invention). The turbulent flow can also reduce the concentration polarization, thereby achieving high concentration. In addition, it can also improve the barrier performance of the membrane. For example, as shown in Figure 45 (b), it can be treated with pressure through penetration. A hollow rotary shaft 63 is provided as a central portion of the cylindrical container 62 of the liquid supply inlet 61, and a plurality of membrane bodies 64 having a structure capable of transmitting a liquid is attached to the rotary shaft 63, so that the liquid passing through the membrane body 64 From the membrane body 64, through the small hole provided in the rotation shaft 63, it passes through the inside of the hollow rotation shaft 63, and is discharged from the outlets 65 and 66. The concentrated liquid is discharged from the outlet 67, and is separated from the membrane body 64 by a gap. A rotary membrane separation device that is capable of covering the membrane body 64 in its entirety and is fixed to the container 62 is relatively known (hereinafter, referred to as "the conventional membrane separation device 1"). For example, Japanese Patent Application Laid-Open No. 6-277465 discloses a device of the same kind as the conventional membrane separation device 1. According to the conventional membrane separation device 1, if the rotating shaft 63 and the membrane body 64 are rotated together by a motor (not shown), a gap between the surface of the rotating membrane body 64 and the stationary ring and the member 68 can be actively generated. Turbulent flow can be expected to have an effect of preventing membrane pore clogging. However, since the ring-shaped stopper 68 completely separates the membrane bodies, the area of the stopper 68 covering the membrane body 64 is large, and the processed liquid in the container 62 passes through the narrow flow path 69, so the pressure loss is increased and it cannot pass through efficiently. In addition, due to the pressure loss, if the pressure applied to the membrane body 64 is uneven, the deflection of the membrane body 64 will be large, causing the membrane body 64 to contact the annular stopper 68, and the weaker membrane body 64 will be generated. Damaged condition. Furthermore, when the container 62 is loaded, the membrane body 64 and the ring stopper 68 need to be assembled interactively, and the device assembly is very complicated. Therefore, as shown in Figure 46 (a), in order to reduce the above pressure loss, _______5 _ This paper size applies the Chinese National Standard (CNS) A4 specification (21〇χ 297 mm) II ------ ( Please read the precautions on the back before filling in this page.) Order · --- Line- 550113 A7 _____B7___ V. Description of the invention (f) An opening stopper 71 (hereinafter referred to as an opening stopper 71) is provided at the periphery of the annular stopper. , Called "the conventional membrane separation device 2"). However, the conventional membrane separation device 2 has holes in the stopper, so the processing cost is increased. As in the conventional membrane separation device 1, the membrane body 64 and the openings need to be assembled alternately when the container 62 is loaded. The stopper 71 has the disadvantage that the assembly of the device is very complicated. In addition, since the stoppers 68 and 71 of the conventional membrane separation devices 1 and 2 are uniformly covered on the membrane surface, there is also a disadvantage that the turbulent flow of the treated liquid is small. Furthermore, the conventional rotary membrane separation devices 1 and 2 are not clear in proper membrane separation conditions and device specifications for effectively exerting membrane separation performance, and cannot guarantee the operation of an economical and effective membrane separation device. The present invention has been made in view of the above-mentioned problems of the conventional technology, and an object thereof is to provide a rotary type which is not complicated, has low cost, has a small pressure loss, efficiently performs a permeation process, and can effectively exert membrane separation performance. Membrane separation device and membrane separation method using rotary die separation device. 3. Summary of the Invention In order to achieve the above object, the present invention relates to two sides of a film body of a rotating shaft of a rotary die separation device, and a plurality of rectangular stoppers are arranged at a distance from the film body. A plurality of rectangular stoppers are arranged parallel to each other from the vicinity of one inner wall to the other inner wall of the container. Since the stoppers are non-uniform covering film surfaces, the turbulent flow is large, and the effect of reducing the concentration polarization and scale is greater. Therefore, the permeate flow is significantly increased, and the pressure loss due to the existence of the stopper is small. Because the shape of the component is simple, there is no need to apply special processing. The cost is low, and the stopper can be inserted after the membrane body is installed on the rotating shaft. ， 6_ This paper size is applicable to China National Standard (CNS) A4 (210 X 297 mm) I!-丨! — 丨! i I (Please read the notes on the back before filling this page) 550113 A7 _ B7 ___ V. Description of the invention (f) The assembly of v / position is simple. That is, the present invention is a rotating membrane separation device 'where a rotating shaft is provided so as to pass through a container having a liquid supply inlet to be processed', and is characterized in that a membrane body having a structure capable of transporting permeated liquid is provided in the container. It is installed on the rotating shaft and has an outlet connected to the membrane body to discharge the permeated liquid. A plurality of rectangular stoppers are arranged on the two sides of the membrane body with a gap between the membrane bodies, and the inner wall surface of the container is connected to the processed object. A plurality of rectangular stoppers are arranged in parallel with each other from the vicinity of one inner wall to the other inner wall of the container through the rotation axis of the liquid flow path of the liquid supply inlet. According to the membrane separation device of the present invention configured as described above, as shown in FIG. 7, when the membrane body 12 is rotated to the right as shown by arrow A, the pressurized liquid to be treated is supplied from the supply inlet to the container. That is, on the left side of the rectangular member 13 'as indicated by the arrow B', the flow path 16 of the inner wall 15 is stolen by the follower, and flows along the rectangular stopper toward the inside of the container 'on the other hand' is on the left side of the rectangular stopper 13, such as As shown by arrow C, the liquid to be treated on the surface of the membrane body 12 is discharged along the flow path 16 of the inner wall 15 of the container. By the liquid flow of the liquid to be processed formed along the flow path along the surface of the membrane body and the inner wall of the container, the liquid to be processed does not stagnate on the surface of the film, and the liquid flowing toward the outside of the container and the flow to the outside are smoothly performed. Liquid conversion. Due to the turbulent flow of the liquid to be treated by the non-uniformly installed stoppers, it can reduce fouling, concentration polarization, and efficiently perform membrane separation. The features and advantageous effects of the rotary membrane separation device and the membrane separation method using the rotary membrane separation device of the present invention will be described below. (1) The support of the stopper is fixed ____2_ This paper size is applicable to the Chinese National Standard (CNS) A4 specification (210 X 297 mm) (Please read the precautions on the back before filling this page) • -installation ·. Line · 550113 A7 ____B7_____ 5. Description of the invention (L) If the two ends of the fixed stopper are supported by a support body independent of the container wall, the assembly of the device becomes easy, and the cost can be reduced. (2) Shape of stopper ① Hook-shaped stopper, S-shaped stopper and arc-shaped stopper can be provided with a Jun-shaped stopper at a gap between the two sides of the film body and between the film body. The Jun-shaped stopper is arranged symmetrically with respect to the diameter of the membrane body or symmetrically with respect to the axis of rotation. In addition, S-shaped stoppers may be arranged at a gap between the two sides of the film body and between the film bodies, and a plurality of S-shaped stoppers may be arranged point-symmetrically with respect to the rotation axis across the rotation axis. And, arc-shaped stoppers can also be arranged at a gap between the two sides of the membrane body and between the membrane bodies, and a plurality of arc-shaped stoppers are arranged in line symmetry or relative to the axis of rotation with respect to the diameter of the membrane body through the rotation axis. Symmetrical. Whether using a Jun-shaped stopper, an S-shaped stopper, or an arc-shaped stopper, the same effect as that of a rectangular stopper can be expected. In addition, if a fishing-shaped stopper, an S-shaped stopper, or an arc-shaped stopper is used, it has the effect of increasing the turbulent flow on the membrane surface and improving the membrane separation performance. It also has the effect of promoting fluid transfer between membrane bodies. ② If the radial stopper is a non-uniform covering film surface, the pressure loss caused by the existence of the stopper will increase due to the increase of turbulent flow, the reduction of concentration polarization and the reduction of scale. Get smaller. For example, if a stopper (radial stopper) formed by arranging a plurality of stoppers radially toward the inner surface of the container with the rotation axis as the center is used, the permeation flow rate increases. (3) Projection area of the stopper with respect to the surface area of the membrane body ① Cases of rectangular stopper, fishing stopper, S-shaped stopper, and circular stopper _8_ —_ This paper is applicable in China _ House Standard (CNS) A4 specification (21G x 297 male Chu 1 (please read the precautions on the back before filling out this page); 550113 A7 ______ Β7 ___ 5. Description of the invention (^ 1) If it is a rectangular stopper, fishing-shaped stopper, S-shaped stopper In the case of a piece and an arc-shaped stopper, the projected area of the stopper relative to the surface area of the membrane body is preferably 1 to 90%. The reason is that if it is less than 1%, the turbulent flow promotion effect of the surface of the membrane body will be reduced, and if it exceeds 90% %, The pressure loss of the treated liquid becomes too large. The reason is that, as in the embodiment described later (refer to FIG. 22), even if the projection area of the stopper with respect to the surface area of the membrane body is 1%, the permeate flow rate is less than that without the stopper. Occasionally it will increase significantly and exceed 90%, and the permeate flow rate will be greatly reduced. Moreover, although the technical field of the present invention is different depending on the nature of the liquid to be treated, the purpose of the treatment, or the cost of the treatment, most of them require a certain level. The above permeate flow, because the average permeate flow is required The volume is more than 30L (liter) / m2 / hr. Therefore, as shown in Figure 22 below, in order to meet the requirements of this permeate flow rate, the rectangular stopper, fishing stopper, S-shaped stopper and arc stopper In the case of a piece, the projection area of the stopper with respect to the surface area of the membrane body is preferably 10 to 90%. In order to prevent the pressure loss in the device from increasing and only increase the permeate flow rate, it is particularly preferred that the stopper piece is relative to the surface area of the membrane body. The projected area is 26 to 70%. © In the case of a radial stopper, if the projection area of the stopper with respect to the surface area of the film body is less than 30%, the effect of promoting turbulence on the surface of the film body will be reduced. If it exceeds 70%, the pressure loss of the treated liquid will be too large. Therefore, the projection area of the radial stopper with respect to the surface area of the membrane body is preferably 30 to 70%. (4) Diameter of the membrane body and the number of revolutions of the membrane body① Rectangle In the case of stoppers, Jun-shaped stoppers, S-shaped stoppers, and circular-shaped stoppers, rectangular stoppers, fishing-shaped stoppers, S-shaped stoppers, and circular-shaped stoppers are used. _9_____ This paper size applies to Chinese national standards ( CNS) A4 specification (210 X 297 mm) ---- I --- II ---- i I (Please read the note on the back first Please fill in this page for further information) · Line-550113 A7 B7_ — V. In the description of the invention (f), the diameter of the membrane is preferably 200 to 1100mm. The reason is that if it is less than 200mm, it has sufficient membrane separation ability. The device will have too many diaphragms, and the device and the rotation axis are too long. Devices exceeding 1100mm are difficult to manufacture, which will cause a significant increase in manufacturing costs, and the power required for rotation will also increase significantly. In addition, As shown in the embodiment described below (refer to Figure 24), if the membrane diameter is less than 200mm and the membrane rotation speed is slow, a sufficient practical flow rate cannot be obtained. When the membrane rotation speed is slow ( For example, at 20 rpm or less) Although the diameter of the membrane increases, the permeate flow rate will increase, but even if the membrane diameter exceeds 1100 mm, the permeate flow rate will not increase. In addition, when a rectangular stopper, a Jun-shaped stopper, an S-shaped stopper, and an arc-shaped stopper are used, the number of revolutions of the film body is preferably 20 to 180 rpm. The reason is that if the speed is less than 20 rpm, the effect of preventing membrane clogging and the effect of reducing concentration polarization will be reduced. If it exceeds 1800 rpm, the centrifugal force will be too large. As described above, the transmission efficiency will be reduced. The demand will increase significantly. The reason lies in the fact that, as shown in the example described later (refer to FIG. 25), if the membrane rotation speed is less than 2 Grpm, the permeate flow rate will be significantly reduced, and even if it exceeds 1800 rpm, the permeate flow rate will not increase. © In the case of a radial stopper In order to create an industrial device that can ensure a predetermined permeate flow rate and a practically required throughput, a membrane area of a certain degree or more (for example, 10 m2 or more) is required. However, when the diameter of the membrane body is less than 300mm, in order to ensure the required membrane area, a large number of membrane bodies are needed, and the device and the rotating shaft are too long, which makes it difficult to be a consistent industrial device. On the other hand, if the diameter of the membrane is large, the transmission rate or the scale is applicable to the Chinese National Standard (CNS) A4 specification (210 X 297 meals ^ ---- (Please read the precautions on the back before filling out this page). --Line- 550113 A7 _ _ B7________ V. Description of the invention 〇) Increase, and although the rotation axis can be shortened, the power part required for rotation will increase to the fifth power of the membrane diameter, and there is an improper operation that cannot be very economical. The situation happened. In addition, even if the diameter of the membrane body is larger than a certain level, the increase in the permeate flow rate is small. Therefore, in the case of using a radial stopper, the diameter of the membrane body is in the range of 30 () to 1000 mm, which is preferable because an economical and efficient membrane separation device can be realized. When rotating a membrane with a diameter in this range, 'if the membrane rotation speed is less than 50 rpm, there are few membrane hole blocking prevention effects, scale prevention effects, or concentration polarization reduction effects, and sufficient practicality cannot be obtained. Of the size of the passing traffic. On the other hand, if the number of revolutions of the membrane body exceeds 1000 rpm, the centrifugal force becomes too large, and the effective pressure applied to the pressurized to-be-processed liquid to permeate will be offset, thereby reducing the permeation efficiency, and the power required for rotation will be reduced. Big increase. Therefore, in the case where a radial member is used, the number of revolutions of the membrane body is preferably in the range of 50 to 1,000 rpm. (5) Number of stoppers ① In the case of rectangular stoppers, Jun-shaped stoppers, S-shaped stoppers, and arc-shaped stoppers, if the number of stoppers provided on the side of the membrane is too large, it has the disadvantage of difficulty in installation, and As in the embodiment described later (refer to FIG. 21), even if the number of gears is increased to more than 20 ', the permeate flow rate will not increase, so the rectangular stopper, the Jun-shaped stopper, the s-shaped stopper, and the arc shape The number of stoppers is preferably from 1 to 20. ② In the case of radial stoppers, if the number of radial stoppers is small, the transmission flow is small. If the number of stoppers increases, the transmission flow increases, but the radiation The number of stoppers has increased to a certain number ___ 11____ 1 This paper size applies to China National Standard (CNS) A4 (210 X 297 mm 7 " " (Please read the precautions on the back before filling this page) • Binding:- -Line · 550113 A7 ____B7_ 5. Description of the invention (// (;) above the mesh will not increase the flow rate. Therefore, the number of radial stopper is preferably 4 to 12. (6) Membrane body and stopper Clearance of the pieces ① In the case of rectangular stops, Jun-shaped stops, S-shaped stops and arc-shaped stops , Jun-shaped stoppers, S-shaped stoppers and arc-shaped stoppers, the gap between the moon body and the stopper should preferably be 2 ~ 18mm. If it is less than 2mm, the moon body and the stopper are easy to contact, and the membrane body It may be damaged. If it exceeds 18mm, the rotation axis will become longer, the volume of the container containing the membrane body will be too large and impractical, and the distance between the membrane body and the stopper will become too separated, which will promote the turbulent flow generated by the stopper. The effect is reduced. The reason is that if the gap between the membrane body and the stopper is less than 2mm or more than 18mm, as shown in the example described later (refer to Figure 26), a sufficient practical flow rate cannot be obtained. ② If the radial member is a radial member, the gap between the film body and the stopper is preferably 2 to 12mm. The reason is that if the radius is less than 2mm, the film body and the radial stopper are easy to contact, and the film body may be damaged. Occurrence, if it exceeds 12mm, the distance between the membrane body and the radiating member will be too separated, and the turbulent flow promotion effect of the radiating member cannot be expected, and the total length of the device will be long and uneconomical in order to ensure the required film area. If the rotation speed of the membrane is rectangular In the case of a stopper, a fishing stopper, an S-shaped stopper, and an arc-shaped stopper, the rotation speed of the membrane is preferably 1 to 30 m (meters) / sec (seconds) on the outer periphery. The reason is that if it is less than lm At a low speed of / sce, there is almost no membrane hole blocking prevention effect and concentration polarization reduction effect. If it exceeds ____12_ of 30m / sce, this paper size applies the Chinese National Standard (CNS) A4 specification (210 X 297 mm) (please Read the precautions on the back before filling this page) -Install i-line- 550113 A7 _____B7_ V. Description of the invention (11) -------------- Install --- (Please read the back If you need to fill in this page again, the centrifugal force will become too large. 'The effective pressure on permeation of the liquid to be treated will be cancelled and the permeation efficiency will be reduced. In addition, the power required for rotation will be greatly increased. The reason is that if the peripheral speed of the membrane is less than lm / sce, as shown in the example described later (refer to FIG. 23), a sufficient flow rate cannot be obtained, whether it is a low concentration liquid or a high concentration. As long as the outer peripheral speed of the liquid exceeds 30m / SeC, the permeate flow rate will decrease. (8) Thickness of the stopper-line · Whether it is a rectangular stopper, a fishing stopper, an S-shaped stopper, a circular stopper, or a radial stopper, any stopper of any shape should be used. It is arranged with a gap from the rotating film body, so that the stopper will not contact the film body. On the other hand, in order to prevent the stopper from occupying a large volume, it is desirable to make it as thin as possible. However, if it is too thin, it may be damaged due to contact with the membrane due to easy bending. Therefore, the thickness of the stopper is preferably 1 mm or more. However, in order not to occupy a large volume, and to ensure that the gap between the membrane bodies is not too large, and the device and the rotating shaft are not to be long and large, the thickness of the stopper is preferably less than 20mm. In addition, in order not to be easily bent, the material of the stopper is not particularly limited, but various metals such as iron and stainless steel, plastic, ceramic, and glass fiber reinforced plastic are preferred. (9) Width of the stopper If it is a rectangular stopper, a Jun-shaped stopper, an S-shaped stopper, and an arc-shaped stopper, the width of the stopper is preferably 0. 1 to 40%. The reason for this is' less than 0. If it is 1%, the turbulent flow promotion effect on the surface of the membrane will be small, if it exceeds 40 ° /. The pressure loss of the treated liquid will be too large. (10) The ratio of the diameter of the container to the diameter of the membrane _____13_ This paper size is applicable to the Chinese National Standard (CNS) A4 (210 X 297 cm) 550113 A7 ___B7____ Jade and description of the invention (f L) The diameter of the container and the diameter of the membrane The ratio ranges from 1.03 to 3. 000 is better. The reason is that dissatisfaction 1. If it is 003, the area occupied by the membrane is too large, and the pressure loss of the treated liquid may become too large. On the other hand, if it exceeds 3,000, the area occupied by the membrane body is too small, so that the membrane separation efficiency is lowered ', which is unfavorable. (11) Pressure of the liquid to be treated If the pressure of the liquid to be treated introduced into the container exceeds 20 mm, an improper situation in which the pressure resistance of the container is difficult occurs, if it is not satisfied. 〇〇5MPa, the water level in the container is actually not full. 5m, and there is an improper situation in which the membrane is not immersed in the liquid to be treated, so the pressure of the liquid to be introduced into the container is 0. 005MPa to 20MPa is preferred. (12) Radial acceleration during membrane rotation When the membrane is rotated, the radial acceleration toward the outside of the circle acts on the liquid to be treated near the membrane that rotates with the membrane. According to the findings of the inventors, it is clear that this radial acceleration has an influence on the membrane separation performance. That is, when the liquid to be processed is at a high concentration, the radial acceleration during the rotation of the membrane is in the range of 200m / see2 or more. When the liquid to be processed is at a low concentration, the radial acceleration during the rotation of the membrane is 100m. By operating within the range of / sce2 or more, an effective shear force is applied to the liquid to be processed according to the viscosity of the liquid to be processed, thereby increasing the permeation flow rate. (13) Thickness of the film body The thickness of the film body is preferably 1 to 20 mm. The reason is that if it is less than 1 mm, the strength is insufficient, and if it exceeds 20 mm, the volume of the container for storing the membrane body becomes excessively large. ____14 _ This paper size is in accordance with China National Standard (CNS) A4 (210 X 297 mm) (Please read the precautions on the back before filling this page) • —Packing] 0J · --Line- 550113 A7 ____ B7_____ V. (Explanation of the invention)) (14) Shape of the film body Although the shape of the film body may be circular, but it is not limited to a circular shape, and may be a polygon having a pentagon or more. (15) If the device is miniaturized, if the rotating shaft is hollow, and there are small holes in the membrane installation part in the longitudinal direction of the shaft, the membrane is to install a permeable membrane with a path that can transport permeate on both sides of the board. The structure 'is arranged so that the permeated liquid conveying path of the above-mentioned permeable fe communicates with a small hole provided on a rotating shaft', that is, the rotating shaft can also be used as a permeating liquid discharge device. Therefore, there is an advantage of miniaturization of the membrane separation device . (16) The meaning of diameter is used in this specification. "Diameter" means "through the center of a circle or sphere, line segments with two ends on the circumference or sphere" "also means" in a polygon, from its center A line segment that is twice the distance from a vertex. " Since the rotary membrane separation device of the present invention and the separation device using the rotary membrane and separation device are configured as described above, the following effects can be obtained. (1) According to the rotary membrane separation device described in items 1, 2, 3, and 4 of the scope of the patent application, because the members are not completely separated from the structure of the membrane body, the blocking member is treated. The pressure loss of the liquid is small, and the membrane separation performance is excellent. Since there is no need to alternately install the film body and the component, after the rotation shaft and the film body are installed, the stopper can be inserted from the lateral direction of the laminated film body, so the installation is not laborious. Further, since the shape of the stopper is simple, the processing is simple and the cost is low. In addition, the width of the stopper can be arbitrarily changed because of the properties of the liquid to be treated. _____J15__ This paper size is applicable to China National Standard (CNS) A4 (210 X 297 mm) (Please read the precautions on the back before filling this page) Binding · · 550113 A7 _B7_ Five, hair mm (\ ten (please read the precautions on the back before filling this page) degree, thickness or number, so there is no restriction on the type of the liquid to be treated, and the applicability is excellent. ( 2) In particular, the rotary membrane separation device described in the scope of patent application Nos. 2, 3, and 4 has the advantages of large turbulence on the membrane surface, which can improve the membrane separation performance. It also has the advantage of promoting Advantages of fluid conversion between membrane bodies. (3) In particular, the rotary membrane separation device contained in the scope of patent applications Nos. 5, 6, 7, and 8 due to the blocking member's relative to the surface area of the membrane body. The projected area is within a proper range, so the permeate flow becomes extremely large. (4) Especially the rotary membrane separation devices described in the scope of patent applications Nos. 9, 10, 11 and 12, because they block the rectangle Pieces, Jun-shaped stoppers, S The two ends of the stopper or arc-shaped stopper are supported for fixing, so the device is easy to assemble and the cost can be reduced. _Line- (5) Especially the rotary membrane separation device described in item 13 of the scope of patent application has The advantage of easy installation of the stopper. (6) Especially the rotary membrane separation device described in the scope of patent application No. 28 has an excellent membrane separation efficiency. (7) Especially the scope of the patent scope of patent application No. 15 Rotary membrane separation devices have the advantages of proper device size and the advantage of reducing manufacturing costs and operating costs. (8) Especially the rotary membrane separation devices described in item 17 and item 19 of the scope of patent application, have stoppers. It is not easy to flex and the membrane is not easy to break. (9) Especially the rotary membrane separation package described in item 21 of the scope of patent application. _16_ This paper size applies to China National Standard (CNS) A4 (210 X 297 mm). 550113 A7 ——_, __ SI______ 5. Description of the invention (/ () The device has the advantage of miniaturization of the device. (Please read the precautions on the back before filling this page) (10) Especially according to item 22 of the scope of patent application, The inventions described in items 23, 24, 25, and 26 can provide a rotary membrane separation device that effectively exerts membrane separation performance. (11) Especially according to items 29 and 30 of the scope of patent application The described membrane separation method is not easy to block the membrane, and can be concentrated to a high concentration with a high permeate flow rate. Because it does not need to supply the liquid to be treated at a high flow rate, and does not require a large-scale pump or other pressure feeding device, the kinetic energy cost is low. Increase the concentration, so the treated liquid is rarely sheared by the pump's feed fan, which has the effect that the treated liquid is not easily deteriorated. (12) In particular, according to the 31st, 32nd, and 33rd patent application scope According to the invention, it is possible to provide an operating condition of a rotary membrane separation device that effectively exerts membrane separation performance. ;line. 4. Embodiments Hereinafter, the embodiments of the present invention will be described with reference to the drawings, but the present invention is not limited by the following embodiments. The industry may appropriately change or within the scope not departing from the technical scope of the present invention. Corrected examples. Also, in a comparative inspection experiment on membrane separation characteristics described later, although the embodiment of the present invention shows a case where a rectangular stopper or a radial stopper is mainly used, it is also within the technical scope of the present invention to apply for a patent. Stoppers of other shapes other than the load indicate that they have the same effect, and are not limited to the ones used in experiments. Fig. 1 is a perspective view of a rotary membrane separation device of the present invention. 1 series quilt —_____ 17____ This paper size is applicable to Chinese National Standard (CNS) A4 (210 χ 297 mm) 550113 A7 ____B7___ V. Description of Invention (IL) -------------- --- (Please read the precautions on the back before filling this page) The processing liquid supply inlet is provided with a hollow rotating shaft 3 so as to penetrate the center of the cylindrical container 2 and penetrates most of the membranes where the hollow rotating shaft 3 is installed. The liquid of the sheet (reference numeral 12 in FIG. 2) is discharged from the outlets 4 and 5 through the inside of the hollow rotating shaft 3, and the concentrated liquid is discharged from the outlet 6. 7 is a motor that rotates the membrane body and the rotating shaft 3 at the same time. The rotating force of the motor 7 is transmitted to the rotating shaft 3 through the belt 8. The transmission of rotational force is not limited to this, and a direct motor coupling type, a gear reducer, and a flexible belt transmission can also be used. As shown in Figs. 5a and b, the membrane used in this embodiment has a structure in which a permeable membrane 11 made of polyether maple is mounted on both sides of a polypropylene plate 9 with a woven fabric interposed therebetween. Moreover, in addition to the plastic plate used in this embodiment, a metal plate or a ceramic plate can also be used as the permeable film mounting plate, that is, it is preferable to use a strong material that is not easily deformed and resistant to breakage. In this specification, the permeable membrane system has a porous structure, and a path (a flow path formed by connecting the porous part) that can transport liquid that has passed through the porous part is formed inside, as long as It is a film having such a function. In addition to the organic film described above, a ceramic or metal film can also be used. The barrier cloth 10 can also transmit permeate. The diameter of the permeate channel in the barrier cloth 10 is larger than the permeate transport path 27 of the permeable membrane 11, and the permeate can easily flow into the barrier cloth 10. As shown in Fig. 2, a plastic plate body 9, a spacer cloth 10, and a membrane body 12 composed of a permeable membrane 11 are mounted on the rotation shaft 3, and a gap is provided between the membrane body on both sides of the membrane 12 and the container. 2 near one of the inner walls to the other inner wall, are arranged in parallel with each other via the rotation axis 3 2 stainless steel rectangular stoppers 13 (refer to FIG. 2a), two ends of the plurality of rectangular stoppers 13 are connected by 18 This paper size applies the Chinese National Standard (CNS) A4 specification (210 X 297 mm) ~ ^ '550113 A7 ___B7____ 5. Description of the invention (丨 The through screws 14 connected to the surfaces 2a and 2b of the container 2 support fixing. Also, connected to The liquid flow path 16 of the to-be-processed liquid supply inlet 1 is formed along the inner wall surface 15 of the container 2. As shown in Fig. 5a, the rotating shaft 3 is hollow, and a small hole is provided in the mounting portion of the membrane body 12 in the direction of the shaft shift. π, the permeated liquid transport path constituting the membrane 12 permeable membrane 11 and the permeated liquid transport flow path of the isolation cloth 10 communicate with the small hole Π. 18 is a part of the rotation axis of the membrane body 12 and is sandwiched between the upper and lower adjacent parts. Membrane body 12, a spacer between 12. Also, as shown in Figure 5b, it can also be installed along the rotation axis 3 A plurality of slits 19 are provided in the long axis direction of the member 18 and the membrane body 12 portion, and the slits 19 are used as a permeate liquid conveying channel. A small hole 17 is provided at the end of the rotating shaft 3 to make the transmissive membrane 11 The structure in which the permeated liquid conveying path and the permeate liquid conveying path of the barrier cloth 10 communicate with the small holes 17. Although omitted in Fig. 5b, a small hole 17 is also provided at any position of the rotating shaft 3. Fig. 3 shows the film An example in which four sides of the body 12 are spaced apart from the membrane body, from the vicinity of one of the containers 2 to the vicinity of the other inner wall, four non-embroidered steel rectangular stoppers 20 are arranged in parallel with the rotation axis 3 interposed therebetween. In addition to the above-mentioned metal, the material of the stopper can also be plastic or ceramic. If supply pressure (about O. When the liquid to be processed is pressed into the container 2 of the membrane separation device configured as above, or the container 2 is filled with the liquid to be processed, and the rotary shaft 3 is decompressed or sucked by the rotary shaft 3, that is, As indicated by the arrow 24 in FIG. 6a, a centrifugal force generates a liquid flow flowing radially outward. And because the stoppers 13 are provided on both sides of the membrane body 12, a liquid flow that prevents particle action or concentration polarization of the membrane pores of the membrane body 12 will be produced. _19 __ This paper size applies to Chinese National Standards (CNS) A4 specification (210 X 297 mm) (Please read the precautions on the back before filling this page) 丨 install tl · • -line _ A7 550113 ________B7_____ 5. Description of the invention (f) 23, as shown in Figure 6b, the film The hole 26 will not be blocked, and the permeate flowing from the path 27 formed by the porous portion through the flow path in the insulation cloth 10 passes through the small hole π shown in Figs. 5a and b, and passes through the hollow rotating shaft 3 from the first 1 The outlets 4 and 5 shown in the figure are discharged. On the other hand, the concentrated liquid is discharged from the outlet 6. Since the permeate easily flows through the narrow permeate transport path 27 in the permeable membrane through the wide flow path in the barrier cloth 10, less permeate directly flows from the small hole 17 through the permeate transport path 27 and passes through the isolator cloth 10 A wide flow path in the inside reaches a large amount of permeate reaching the small hole 17. In this regard, in order to ensure a flow path through which the permeated liquid easily flows, a permeate flow path may be formed in the plate body 9, and in this case, the spacer 10 is not necessary. However, since the formation of the permeated liquid flow path on the plate body 9 increases the cost, it is preferable to use the spacer cloth 10 in terms of economy. As the stopper, a radial stopper as shown in FIG. 8 may be used. Fig. 8 shows an example in which eight stoppers 28 are arranged radially on the inner wall surface 15 of the container 2 with a gap from the film body 12 on both sides of the film body 12 with the gap as the center. The end of the stopper 28 is supported and fixed by a through screw 14 connecting the surfaces 2a and 2b of the container 2. In addition, a circular arc-shaped stopper 29a shown in FIG. 9, a Jun-shaped stopper 29b shown in FIG. 10, or an S-shaped stopper 29C shown in FIG. 11 can also be used. Even when these stoppers 29a, 29b, and 29c are used, the same effects as those of the rectangular stoppers can be expected. Further, according to the arc-shaped stopper 29a, the fishing-shaped stoppers 29b and 29c, and the S-shaped stopper 29c, the turbulent flow on the membrane surface can be increased, and the effect of improving membrane separation performance can be improved. It also has the effect of promoting the conversion of fluid between membranes. As for the circular-arc stopper 29a and Jun-shaped stopper 29b, as shown in Figure 9 and Figure 10, they can be used on the rotation axis 3, relative to the rotation axis _ 20 _____ This paper size applies to China National Standard (CNS) A4 specifications ( 210 X 297 mm) -------------- install --- (Please read the precautions on the back before filling this page) 0 ·; line · 550113 A7 ____ 一 _B7____ 5 2. Description of the invention (j /) A plurality of arc-shaped stoppers 29a or a plurality of Jun-shaped stoppers 29b are arranged in line symmetry, or a plurality of arc-shaped stoppers 29a or a plurality of fishes are symmetrically disposed in a point relative to the rotation axis 3形 block 件 29b. As for the S-shaped stopper 29c, as shown in FIG. 11, a plurality of S-shaped stoppers may be arranged symmetrically with respect to the rotation shaft 3 with the rotation shaft 3 interposed therebetween. Although not shown in Figs. 9 to 11, the same number of stoppers 29a, 29b, and 29c are also arranged on the other side of the membrane body 12, except that the shape of the stoppers is different, and other structures are basically the same as the first. Further, both end portions of the arc-shaped member 29a, the fishing stopper 29b, and the S-shaped stopper 29C are supported by through screws 14 connecting the surfaces 2a and 2b (see Fig. 2) of the container 2 respectively. Further, as shown in Fig. 12c, a stopper 30 having a wing-like cross-sectional shape can also be used. According to this member 30, there is an advantage that it is not easy to contact the film body. Moreover, it also has the advantage of reducing the rotational power. In addition, the cross-sectional dimensions of the rectangular stopper 13 shown in FIG. 2 and the rectangular stopper 30 shown in FIG. 3 in the longitudinal direction do not change the cross-sectional dimensions as shown in FIG. 2c or 3c. The rectangular stopper of the present invention is not limited to that exemplified here. Next, a description will be given of a comparison check between the membrane separation device of the present invention and a conventional membrane separation device with respect to various characteristics. In addition, the inner diameter of the cylindrical container 2 used in each of the following experiments is 350 mm (millimeters), and unless otherwise disclosed, the diameter of the membrane body is 300 mm. These numbers are common to each experiment. (1) Membrane separation system First, a membrane separation system to which the membrane separation device of the present invention can be applied will be described. That is, as shown in FIG. 13, stored in the liquid to be processed via path 31 ____21_ This paper size applies the Chinese National Standard (CNS) A4 specification (210 X 297 public love) A --- ------- ------- Installation—— (Please read the precautions on the back before filling this page) Ίδτ ·-丨 line · 550113 A7 _____B7_____ V. Description of the invention (/) — — I! — —! — — · · · 11 (Please read the precautions on the back before filling this page) The treated liquid 33 in the storage tank is stirred by the mixer 34, and the treated liquid is pressurized to about 0 by the pump 35. 005 to 20 MPa, pressure is sent to the membrane separation device 37 through the path 36. 38 is used to remove the filter in the liquid to be processed. The permeate separated by the membrane separation device 37 is discharged through the path 39, and the concentrated liquid flows through the path 40. , 41, return to the storage tank 32 again, and further pass through the path 36 to be supplied to the membrane separation device 37 for membrane separation. Repeat this membrane separation operation to gradually increase the concentration of the concentrate. When the predetermined concentration is reached, this concentrated liquid is taken out through the path 42. 43 is a valve, and 44 is a motor. In addition, the concentrated liquid is not necessarily circulated. The liquid separated by the membrane separation device 37 and concentrated can be discharged through the path 42 as it is, or partly returned to the storage tank and partly discharged. The liquid to be treated having a certain property in the storage tank 32 is stored in the storage tank 32, and membrane separation is performed by the same operation. ;line. FIG. 14 shows a structure in which a pump 35 is provided in the permeate discharge path 39 of the membrane separation device 37. In this manner, the pump 35 can be used to suck the liquid to be processed and supply it to the membrane separation device 37. The membrane separation device 37 can also be opened. It can reduce the auxiliary equipment of the membrane separation device, so it has the effect of reducing the size of the entire device. In the case of the membrane separation system of Fig. 14, the pressure of the liquid to be treated supplied to the membrane separation device 37 is small, so that an effect of preventing scale from occurring is also expected. (2) Effect of the shape of the stopper and the presence or absence of rotation on the permeation flow rate in the membrane separation. Fig. 15 shows the results of membrane separation using the membrane separation system shown in Fig. 13 to check the relationship between the concentration of the concentrate and the permeation flow rate. The membrane separation device of the present invention is used as shown in FIG. 2 and has two rectangular stoppers on one side and the other side of the membrane body. The conventional membrane separation device is used as the 45th to 22nd scale standard of China ( CNS) A4 specification (210 X 297 mm) " " 550113 A7 ___ B7___ V. Description of the invention (yj) Rotary membrane separation device shown in the figure and a cross flow type membrane separation device shown in Figure 44. The membrane separation conditions are as follows. 1. Common conditions a. Membrane UF (ultrafiltration) membrane (ultrafiltration membrane, diameter 265mm) b · temperature 25 ^ c. Processed liquid latex, initial concentration 3. 3% by weight d · Operating pressure 450kpa 2. Rotation conditions of rotary membrane separation device a. The outer circle speed of the membrane body is 12m / sec. In Fig. 15, the symbols "0", "▲", and "#" denote the separation method of the present invention (who use the rotary membrane separation device in Fig. 2). The membrane separation method of the rotary membrane separation device shown in the figure uses a cross-flow membrane separation method (in the membrane separation system of FIG. 13, the membrane separation device 37 is a non-rotation type). As shown in FIG. 15, the membrane separation method (symbol 0) of the present invention shows that the permeation flow rate is much larger than that of the cross-flow method (symbol ·), and the permeation flow rate is also larger than that of the rotary membrane separation device shown in FIG. 45. The membrane separation method (symbol ▲) is excellent. This is because in the rotary membrane separation device of FIG. 45, the annular stopper 68 completely separates the membrane bodies, the area of the stopper 68 covering the membrane body 64 is large, and the liquid to be processed in the container 62 passes through a narrow and long flow. Road 69, so the degree of pressure loss is large, and the transmission flow cannot be increased. In the rotary membrane separation device of Fig. 45, the stopper 68 uniformly covers the surface of the membrane, so there is also a disadvantage that the turbulent flow of the liquid to be treated is small. In the cross-flow method, the concentration is 22. The transmission at 6% is approximately 0, and it cannot be further concentrated. However, even if the membrane separation method of the present invention is ____23___, this paper size applies the Chinese National Standard (CNS) A4 specification (210 X 297 mm) ---- ------------- (Please read the notes on the back before filling in this page) Order ·--丨 Line · 550113
Ϊ 一 V A7 B7 五、發明說明（yb 用於濃度22·6%以上，其透過流量亦超過3〇L(升)/瓜2/ hr(小時），而能進一步的加以高濃縮。 (3)擋件形狀對壓力損失的影響 使用桌13圖所不膜分離系統，於第2圖所示旋轉型膜 分離裝置及第45圖所示旋轉型膜分離裝置中，膜體爲 膜(直徑265mm)，在ln3/hr、〇.2Mpa下將溫度25。(：、初 期濃度爲3·3重量％的膠乳供至上述各膜分離裝置，膜體的 外周速度爲l2/m秒情形下，檢查透過流量、濃縮液流量 及濃縮液的壓力。將其結果列示於以下表1中。 [表1] 濃縮液的壓力降低情形，另一方面，使用全隔開型撞件之 第45圖之旋轉型膜分離裝置的濃縮液出口壓力，降至被胃 理液供給壓力的1/4。又，本發明旋轉型膜分離裝置的透 過液流量較使用全隔開型擋件之第45圖之裝置多，相反％ ，本發明旋轉型膜分離裝置的濃縮液流量爲使用全隔開型 構件之第45圖之裝置之一半。亦即，根據本發明膜分離方 法，可濃縮至5倍，不過，第45圖之膜分離裝置卻僅能濃 縮至2.5倍。如此，根據本發明膜分離方法，可提供在高 透過流量下濃縮至高濃度，壓力極小的膜分離方法。 (4)擋件形狀的不同對操作壓力與透過流量的影響 24 (請先閱讀背面之注意事項再填寫本頁} 訂· · 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） 550113 B7 五、發明說明（V|) (a) 長方浓擋件與環形擋件情形 (請先閲讀背面之注意事項再填寫本頁) 第16圖中顯示了檢查操作壓力與透過流量之關係的結 果，其係使用第13圖所示膜分離系統，作爲本發明膜分離 裝置，則如第2圖所示，使用於膜體一側及另一側分別具 有2個長方形擋件之裝置，作爲具有環形擋件之習知膜分 離裝置，則使用第45圖所示裝置。又，操作壓力係指自被 處理液供給壓力扣掉離心力的有效壓力，實際上其爲利用 於被處理液透過的壓力。 如第16圖所示，膜外周速度爲8m/sec、16m/sec、 24m/SeC之任一速度下，具有長方形擋件的本發明膜分離 裝置（符號△、□、〇）的透過流量均較具有環形擋件之習 知膜分離裝置(符號▲、、·)大。 (b) 長方形擋件與棒狀擋件情形 -線. 第18圖顯示了檢查操作壓力與透過流量關係的結果， 其係使用第13圖所示膜分離系統，作爲本發明之膜分離裝 置，則使用如第3圖所示，於膜體一側及另一側分別具有 4個長方形擋件者，作爲具有棒狀擋件的膜分離裝置，係 使用如第17圖所示，於膜體12 —側具有4根棒狀擋件21 者。又，第17圖中雖未圖示，不過，於膜體12另一側亦 同樣配置相同數目的棒狀擋件，除了棒狀構件不同這一點 以外，其他構造基本上與第4圖相同，棒狀擋件21連接容 器2的兩面2a與2b，與第4(c)圖所示分段連結具22的凹 部卡合。 如第18圖所示，不論膜外周速度爲8m/sce或16m 25 ^紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） " " ""~~ 550113 B7 五、發明說明（γ+)Ϊ 一 V A7 B7 V. Description of the invention (yb is used for a concentration of 22 · 6% or more, and its permeate flow is more than 30L (liter) / melon 2 hr (hour), which can be further concentrated. (3 ) The influence of the shape of the stopper on the pressure loss. The membrane separation system shown in Figure 13 is used. In the rotary membrane separation device shown in Figure 2 and the rotary membrane separation device shown in Figure 45, the membrane body is a membrane (diameter 265mm). ), The temperature was 25 at ln3 / hr, 0.2Mpa. (:, The latex with an initial concentration of 3.3% by weight was supplied to each of the above membrane separation devices, and the outer peripheral speed of the membrane body was 1 / msec, check The permeate flow rate, the concentrate flow rate, and the pressure of the concentrate. The results are shown in Table 1. [Table 1] The pressure drop of the concentrate, on the other hand, is shown in Figure 45 of the fully-spaced striker. The pressure of the concentrated liquid outlet of the rotary membrane separation device is reduced to 1/4 of the pressure supplied by the gastric fluid. In addition, the permeate flow rate of the rotary membrane separation device of the present invention is larger than that shown in FIG. There are many devices. Conversely, the flow rate of the concentrated liquid of the rotary membrane separation device of the present invention is the use of a fully partitioned member. One and a half of the device of Fig. 45. That is, according to the membrane separation method of the present invention, it can be concentrated to 5 times, but the membrane separation device of Fig. 45 can only be concentrated to 2.5 times. Thus, according to the membrane separation method of the present invention It can provide membrane separation method which can be concentrated to high concentration and high pressure under high permeation flow rate. (4) The effect of the different shape of the stopper on the operating pressure and permeation flow rate 24 (Please read the precautions on the back before filling this page} Order · · This paper size is in accordance with Chinese National Standard (CNS) A4 (210 X 297 mm) 550113 B7 V. Description of the invention (V |) (a) Cases of rectangular thick stoppers and ring stoppers (please read the back Note that this page is to be filled in again.) Figure 16 shows the result of checking the relationship between the operating pressure and the permeate flow. The membrane separation system shown in Figure 13 is used. As the membrane separation device of the present invention, it is shown in Figure 2. For the device with two rectangular stoppers on one side and the other side of the membrane body, as a conventional membrane separation device with a ring stopper, the device shown in Figure 45 is used. In addition, the operating pressure refers to the self-covered Supply pressure of process liquid The effective pressure of deducting the centrifugal force is actually the pressure used for permeation of the liquid to be processed. As shown in Fig. 16, the outer peripheral speed of the membrane is 8m / sec, 16m / sec, 24m / SeC. The permeation flow rate of the membrane separation device (symbols △, □, 〇) of the present invention having a rectangular stopper is larger than that of a conventional membrane separation device (symbols ▲, ...) with a ring-shaped stopper. (B) Rectangular stopper and rod shape Stopper situation-line. Fig. 18 shows the result of checking the relationship between the operating pressure and the permeate flow. The membrane separation system shown in Fig. 13 is used. As the membrane separation device of the present invention, it is used as shown in Fig. 3, Those who have four rectangular stoppers on one side and the other side of the membrane body. As a membrane separation device with a rod-shaped stopper, as shown in Fig. 17, there are four rod-shaped stoppers on the 12-side of the membrane body. 21 people. Although not shown in FIG. 17, the same number of rod-shaped stoppers are also arranged on the other side of the membrane body 12. The structure is basically the same as that of FIG. 4 except that the rod-shaped members are different. The rod-shaped stopper 21 is connected to both sides 2a and 2b of the container 2 and engages with the recessed portion of the segmented connection tool 22 shown in FIG. 4 (c). As shown in Figure 18, regardless of the film peripheral speed is 8m / sce or 16m 25 ^ Paper size applies Chinese National Standard (CNS) A4 (210 X 297 mm) " " " " ~~ 550113 B7 5 Description of the invention (γ +)
V /sec，具有長方形擋件的本發明膜分離裝置(符號△、□) 的透過流量均較遠較具有棒狀擋件的膜分離裝置(符號▲、 )大。 (c)長方形擋件與開孔板狀擋件的情形 第20圖顯示了檢查操作壓力與透過流量之關係的結果 ，作爲本發明之膜分離裝置，係使用如第3圖所示，於膜 體一側及另一側具有4個長方形擋件者，作爲具有開孔板 狀構件的膜分離裝置，則係使用如第19圖所示，自容器的 內壁15至旋轉軸3附近設置開孔板狀擋件45者。又，第 19圖中雖未圖示，但於膜體12的另一側亦同樣配置相同 數目的開孔擋件，除了擋件形狀不同這一點外，其他構造 基本上與第3圖相同。 如第20圖所示，不論膜外周速度爲8m/Sec、16m/ sec或24m/SeC，具有長方形擋件的本發明膜分離裝置(符 號八、□、〇）的透過流量均遠較具有開孔板狀擋件的膜分 離裝置(符號▲、、·）大。 (5)長方形擋件個數與透過流量 使用第13圖所示膜分離系統，在擋件相對於膜體表面 積的投影面積爲50%之一定情形下，檢查於膜體一側及另 一側，自容器之一內壁附近至另一內壁附近配置的長方形 擋件的數目與透過流量的關係，第21圖顯示其結果。 如第21圖所示，不論膜外周速度爲8m/sec(A)、或 24m/sec(〇），藉由具有1個長方形擋件，透過流量較不 具有長方形擋件情形顯著增加，隨著長方形擋件數目增加 26 ^紙張尺度適用中國國家標準（CNS)A4規格（210 x 297公釐)~" (請先閲讀背面之注意事項再填寫本頁) 裝 線-V / sec, the permeation flow rate of the membrane separation device (symbols △, □) of the present invention with a rectangular stopper is much larger than that of a membrane separation device (symbols ▲,) with a rod-shaped stopper. (c) Situation of rectangular stopper and perforated plate-shaped stopper Fig. 20 shows the result of checking the relationship between the operating pressure and the permeated flow rate. As the membrane separation device of the present invention, as shown in Fig. 3, One with four rectangular stoppers on one side and the other side of the body, as a membrane separation device with a perforated plate-like member, is used as shown in Figure 19, from the inner wall 15 of the container to the vicinity of the rotation axis 3 Perforated plate-shaped stopper 45. Although not shown in FIG. 19, the same number of opening stoppers are also arranged on the other side of the membrane body 12. The structure is basically the same as that of FIG. 3 except that the stoppers have different shapes. As shown in FIG. 20, the permeation flow rate of the membrane separation device (symbols VIII, □, 〇) of the present invention with a rectangular stopper is much larger than that of the open-air membrane, regardless of whether the outer peripheral speed of the membrane is 8m / Sec, 16m / sec, or 24m / SeC. The membrane separation device (symbols ▲ ,, ·) of the orifice plate-shaped stopper is large. (5) Number of rectangular stoppers and permeated flow rate Use the membrane separation system shown in Fig. 13. When the projection area of the stopper with respect to the surface area of the membrane body is 50%, check on one side and the other side of the membrane body. The relationship between the number of rectangular stoppers arranged near one inner wall of the container and the other inner wall and the permeate flow rate is shown in FIG. 21. As shown in Fig. 21, regardless of the film peripheral speed of 8m / sec (A) or 24m / sec (〇), by having a rectangular stopper, the transmission flow rate is significantly increased compared with the case without a rectangular stopper. The number of rectangular stops is increased by 26 ^ The paper size is applicable to the Chinese National Standard (CNS) A4 specification (210 x 297 mm) ~ " (Please read the precautions on the back before filling this page)
550113 A7 B7 五、發明說明（ ，透過流;量變大。不過，即使長方形擋件增加到大於20個 ，透過流量亦不上升。 医[此，爲了避免擋件安裝煩瑣，並且爲了獲得充份的 透過流量，擋件數以1至20個較佳。 (6)檔件相對於膜體表面積的投影面積與透過流量 使用第13圖所示膜分離系統’如第2圖所示’在設於 膜體一側及另一側的長方形擋件的數目分別爲2個的情形 下，檢查長方形擋件相對膜體表面積的投影面積(％)與透過 流量的關係，第22圖顯示其結果，將第22圖的透過流量 (L(升）/m2/hr)相對各擋件投影面積(％)的數値於膜外周 速度8m/sec下的情形列示於下表2 ’將其在膜外周速度 24m/sec下的情形列示於下表3。 (請先閱讀背面之注意事項再填寫本頁) 訂· · 投影面積(％) 0 1 10 12 26 37 51 70 90 100 透過流量 11 27 30 31 40 59 63 48 31 18 -線- 投影面積(％) 0 1 10 12 26 37 51 70 90 100 透過流量 22 48 53 57 67 86 93 80 62 42 如第22圖所示，不論膜外周速度爲8m/sec(A)或 24m/sce(〇），即使擋件相對膜體表面積的投影面積爲1% ，透過適量亦較無長方形擋件的情形顯著增加’隨著此檔 件的投影面積增加，透過流量變大。不過’顯然地’擋件 的投影面積一超過90%，透過流量即大幅降低。其原因在 於，擋件的投影面積一超過90%，即會如同上述習知環形 擋件，擋件覆蓋膜體的面積多，被處理液的壓力損失增大 27 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐〉 550113 A7 ____B7_____ 五、發明說明C/^) ，從而降低透過效率之故。 於第22圖中，固然在膜外週邊速度24m/sec下透過 流量較在8m/sec下大，另一方面有膜外周速度一變大， 旋轉所需力即增加(旋轉所需動力大致按轉數的3次方增加 )的不當情形發生，不過，若是8m/SeC程度的膜外周速度 ’旋轉所需動力即不會過大。復由於在本發明對象的技術 領域中，大多要求平均透過通30L/m2/hr以上，故爲了 滿足經濟性與本發明對象的技術領域所需的透過流量的雙 方面要求，最好是能如第26圖及表2所示，擋件相對於膜 體表面積的投影面積爲10至90%，又，爲求裝置內的壓力 損失不上昇，增加透過流量，尤佳者係擋件相對膜體表面 積的投影面積爲26至70%。 (7)膜外周速度與透過流量 使用第13圖所示膜分離系統，如第2圖所示，在設於 膜體一側及另一側的長方形擋件的數目爲2個時(在擋件相 對膜體表面積的投影面積爲50%的情形下），檢查膜外週速 度與透過流量的關係，第23圖顯示其結果。 於第23圖中，符號「❿」、「△」、「」、「◊」 分別表示被處理液的濃度爲10%、20%、30%、50%。如第 23圖所示，膜外周速度不滿lm/sec的話，即無法獲得充 份實用程度的大小的透過流量。特別是，若在超過30%的 高濃度中膜外周速度低，透過流量即變得極低。其原因在 於，爲了進行高濃度液體的膜分離，需要盡可能克服高黏 性的充分動能，而由於動能爲速度的平方，因此在不滿lm 28 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） <請先閱讀背面之注意事項再填寫本頁) 裝 訂· -線· 550113 A7 ~ 7\ --------- 五、發明說明（/ ) / /sec的膜體旋轉速度中，無法供給在膜分離上充份的動能 之故。 ----------------- (請先閱讀背面之注意事項再填寫本頁) 雖然20%以下的低濃度中，膜外周速度一超過15m/ sec，透過流量即大致一定，不過，於3〇%以上的高濃度中 ，膜外周速度一達到30m/sec，透過流量即增加。不過， 月旲外周速度一超過30m/sec，不論是低濃度或高濃度，透 過流量均變小。 因此’爲了使低濃度至高濃度皆能獲得充份的透過流 量，膜外周速度以1至30m/ sec較佳。 (8)膜體直徑與透過流量 使用第13圖所示膜分離系統，在設於膜體一側及另一 側的長方形擋件數目爲2個時(在擋件相對膜體表面積的投 影面積爲50%的情形下），檢查膜體直徑與透過流量的關係 ，第24圖顯示其結果。 線- 於第14圖中，符號「#」、「▲」、「」、「命」 、「▼」分別表示膜體旋轉數爲200fpm、600rpm、 lOOOrpm、1400rpm、1800rpm。於轉數爲 1800rpm 的超高 速中，即使膜體直徑增加，透過流量亦僅增加一點點。其 原因在於，膜分離動能爲轉數的平方，轉數的效果效益極 大，於超高速旋轉中，膜體直徑的大小差異，不致於成爲 問題之故。 另一方面，雖然旋轉數爲1400rpm以下中，膜體直徑 一增加，透過流量即變大，不過，至膜體直徑超過 llOOrpm，透過流量即不會增加到超過此程度以上。又， 29 木紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） 550113 A7 B7550113 A7 B7 V. Explanation of the invention (, permeate flow; the amount becomes larger. However, even if the rectangular block is increased to more than 20, the permeate flow does not increase. Medical [This, in order to avoid the cumbersome installation of the block, and in order to obtain sufficient The permeation flow rate is preferably 1 to 20. (6) The projected area and permeation flow rate of the perturbation member relative to the surface area of the membrane body use the membrane separation system shown in Fig. 13 'as shown in Fig. 2' When the number of rectangular stoppers on one side and the other side of the film body is two, check the relationship between the projected area (%) of the rectangular stopper with respect to the surface area of the film body and the permeate flow rate. The results are shown in FIG. 22. The permeation flow rate (L (liter) / m2 / hr) in Figure 22 relative to the projected area (%) of each stopper is shown below in the case where the film peripheral speed is 8m / sec. The conditions at a speed of 24m / sec are listed in the following table 3. (Please read the precautions on the back before filling in this page) Order · · Projection area (%) 0 1 10 12 26 37 51 70 90 100 Through flow 11 27 30 31 40 59 63 48 31 18 -line-projected area (%) 0 1 10 12 26 37 51 70 90 100 transparent Flow rate 22 48 53 57 67 86 93 80 62 42 As shown in Figure 22, regardless of the film peripheral speed is 8m / sec (A) or 24m / sce (〇), even if the projection area of the stopper relative to the surface area of the membrane is 1% The amount of transmission is also significantly increased compared with the case without a rectangular stopper. As the projection area of the stopper increases, the transmission flow becomes larger. However, once the projection area of the stopper exceeds 90%, the transmission flow is greatly reduced. The reason is that once the projected area of the stopper exceeds 90%, it will be like the above-mentioned conventional ring-shaped stopper. The stopper covers a large area of the membrane body, and the pressure loss of the treated liquid increases. This paper standard applies Chinese national standards ( CNS) A4 specification (210 X 297 mm> 550113 A7 ____B7_____ V. Description of the invention C / ^), which reduces the transmission efficiency. In Figure 22, although the permeate flow rate at the outer peripheral speed of the film is 24m / sec. At 8m / sec, on the other hand, if the peripheral speed of the membrane increases, the force required for rotation will increase (the power required for rotation will increase approximately by the third power of the revolution), but if it is 8m / SeC The peripheral speed of the membrane 'power required for rotation That is, it will not be too large. Since most of the technical fields targeted by the present invention require an average permeation rate of 30 L / m2 / hr or more, in order to meet the two requirements of economy and the required permeate flow in the technical field targeted by the present invention, It is preferable that the projected area of the stopper with respect to the surface area of the membrane body is 10 to 90% as shown in FIG. 26 and Table 2. In addition, in order to prevent the pressure loss in the device from increasing and increase the permeate flow rate, the most preferred is The projection of the stopper with respect to the surface area of the membrane body is 26 to 70%. (7) Use the membrane separation system shown in Figure 13 for the peripheral speed and permeate flow of the membrane. As shown in Figure 2, when the number of rectangular stoppers provided on one side and the other side of the membrane body is two (on the stop) When the projected area of the film relative to the surface area of the film is 50%), the relationship between the outer peripheral speed of the film and the permeate flow rate is examined, and the results are shown in FIG. 23. In Fig. 23, the symbols "❿", "△", "", and "◊" indicate that the concentration of the liquid to be treated is 10%, 20%, 30%, and 50%, respectively. As shown in Fig. 23, if the peripheral speed of the membrane is less than lm / sec, a sufficient permeate flow rate cannot be obtained. In particular, when the peripheral velocity of the membrane is low at a high concentration of more than 30%, the permeation flow rate becomes extremely low. The reason is that in order to perform membrane separation of high-concentration liquids, it is necessary to overcome sufficient kinetic energy of high viscosity as much as possible, and because kinetic energy is the square of speed, the paper standard of China is applicable to the Chinese National Standard (CNS) A4 ( 210 X 297 mm) < Please read the notes on the back before filling in this page) Binding · -Line · 550113 A7 ~ 7 \ --------- 5. Description of the invention (/) / / sec In the membrane rotation speed, sufficient kinetic energy for membrane separation cannot be supplied. ----------------- (Please read the precautions on the back before filling this page) Although the low-level concentration below 20%, the outer peripheral speed of the membrane exceeds 15m / sec. That is, it is almost constant. However, at a high concentration of 30% or more, as soon as the outer peripheral speed of the film reaches 30 m / sec, the permeate flow rate increases. However, as soon as the outer velocity of the lunar iris exceeds 30m / sec, the permeate flow becomes small regardless of the low or high concentration. Therefore, in order to obtain a sufficient permeate flow from a low concentration to a high concentration, the peripheral speed of the membrane is preferably 1 to 30 m / sec. (8) Diameter and permeate flow rate of the membrane body Use the membrane separation system shown in Figure 13 when the number of rectangular stoppers provided on one and the other side of the membrane body is two (the projected area of the stopper relative to the surface area of the membrane body) In the case of 50%), check the relationship between the membrane diameter and the permeate flow rate, and the results are shown in Figure 24. Line-In Figure 14, the symbols "#", "▲", "", "Life", and "▼" indicate that the membrane rotations are 200fpm, 600rpm, 1000rpm, 1400rpm, and 1800rpm, respectively. At ultra-high speeds of 1800 rpm, even if the membrane diameter increases, the permeate flow rate increases only a little. The reason is that the kinetic energy of membrane separation is the square of the number of revolutions, and the effect of the number of revolutions is extremely large. In ultra-high-speed rotation, the difference in the diameter of the membrane is not a problem. On the other hand, although the number of revolutions is 1400 rpm or less, as the membrane diameter increases, the permeate flow rate increases. However, until the membrane diameter exceeds 110 rpm, the permeate flow rate does not increase beyond this level. In addition, 29 wood paper standards are applicable to China National Standard (CNS) A4 (210 X 297 mm) 550113 A7 B7
五、發明說明（ 膜體直徑不滿200mm的話，即無法於轉數不滿600rpm的 低速旋轉中獲得充份實用程度的大小的透過流量。 因此，爲了抑制旋轉所需動力大幅增加’並爲了使低 速至高速旋轉皆能獲得充分的透過流量，膜體直徑以200 至llOOmm較佳。 (10)膜體轉數與透過流量 使用第13圖所示膜分離系統’在設於膜體一側及另一 側的長方形擋件數目爲2個時(擋件相對膜體表面積的投影 面積爲50%的情形下），檢查膜體轉數與透過流量的關係， 第25圖顯示其結果。 於第25圖中，符號「·」、「▲」、「」、「♦」 、「▼」分別表示膜體直徑爲η⑻mm、750mm、3000mm 、2000mm。轉數不滿20rpm的話，不管膜體直徑如何，均 無法獲得充份實用程度的大小的透過流量。雖然隨著轉數 增加至大於20rpm，透過流量變大，不過於1800rpm ’不 管膜體直徑如何，透過流量均大致相同，即使轉數大於 1800rpm，透過流量亦不會上昇到超過此程度。 因此，爲了抑制旋轉所需動力大幅增加，並且爲了獲 得無關乎膜體直徑大小的充份透過流量，膜體轉數以20至 1800rpm 較佳。 (10)膜體的擋件的間隔與透過流量 使用第13圖所示膜分離系統，如第2圖所示，在設於 膜體一側及另一側的長方形擋件的數目爲2個時(擋件相對 膜體面積的投影面積爲50%的情形下），檢查膜體與擋件的 30 (請先閱讀背面之注意事項再填寫本頁) :裝 訂： --線- 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） 12550113 A7 B7 五、發明說明 間隔與透過流量的關係’第26圖顯不其結果。 如第26圖所示，不論膜體與擋件的間隔不滿2mm或 超過2mm，均無法獲得充份實用程度的大小的透過流量。 因此，爲了使膜體不破損，並爲了獲得充份的透過流 量，膜體與擋件的間隔以2至18mm較佳。 (11) 透過流量的穩定性 使用第13圖所示膜分離系統’作爲本發明膜分離裝置 ，如第2圖所示，使用分別於膜體一側及另一側具有2個 長方形擋件者，來檢查透過流量相對於運轉時間的變化， 第27圖顯示其結果。如第27圖所示，即使進行8小時的 膜分離，透過流量亦不變化，顯然，本發明膜分離裝置在 透過流量的穩定性方面很優異。 (12) 濃差極化減低效果 (a)MgS04阻止率 使用第13圖所示膜分離系統，作爲本發明膜分離裝置 ，如第3圖所示，使用於膜體一側及另一側分別具有4個 長方形擋件者，檢查相對於膜外周速度的濃差極化減低效 果，第18圖顯示其結果。又，MgS04阻止率(#)係指次式 所定義的比率。V. Description of the invention (If the diameter of the membrane is less than 200mm, it is impossible to obtain a sufficient practical flow rate in low-speed rotation with a number of revolutions of less than 600rpm. Therefore, the power required to suppress the rotation is greatly increased, and to lower the speed to A sufficient permeation flow rate can be obtained at high speeds, and the diameter of the membrane body is preferably 200 to 110 mm. (10) The number of revolutions and the permeation flow rate of the membrane body use the membrane separation system shown in Fig. 13 'on one side of the membrane body and the other When the number of rectangular stoppers on the side is two (when the projection area of the stopper with respect to the surface area of the membrane body is 50%), check the relationship between the number of rotations of the membrane body and the permeate flow rate, and the results are shown in Fig. 25. Fig. 25 The symbols "·", "▲", "", "♦", and "▼" indicate that the membrane diameter is η⑻mm, 750mm, 3000mm, and 2000mm. If the number of revolutions is less than 20rpm, it will not be obtained regardless of the membrane diameter. The permeate flow rate is sufficient and practical. Although the permeate flow rate increases as the number of revolutions increases to more than 20 rpm, the permeate flow rate is approximately the same regardless of the membrane diameter, even If the number is greater than 1800 rpm, the permeate flow rate will not rise to more than this level. Therefore, in order to suppress the power required to significantly increase the rotation, and in order to obtain a sufficient permeate flow rate regardless of the size of the membrane, the membrane rotation number is 20 to 1800 rpm. (10) The interval and permeate flow rate of the stopper of the membrane body use the membrane separation system shown in Fig. 13, as shown in Fig. 2, the number of rectangular stoppers provided on one side and the other side of the membrane body is 2 pieces (when the projection area of the stopper relative to the film body area is 50%), check 30% of the film body and the stopper (please read the precautions on the back before filling this page): binding: --line-this Paper size applies Chinese National Standard (CNS) A4 specification (210 X 297 mm) 12550113 A7 B7 V. Description of the invention The relationship between the interval and the permeated flow 'Figure 26 shows the results. As shown in Figure 26, regardless of the membrane body If the distance between the stopper and the stopper is less than 2mm or more than 2mm, it is impossible to obtain a sufficient practical flow rate. Therefore, in order to prevent the membrane body from being damaged and to obtain a sufficient permeation flow rate, the interval between the film body and the stopper is 2 to 18mm is preferred. (11) The stability of the permeate flow rate is checked by using the membrane separation system shown in FIG. 13 as the membrane separation device of the present invention. As shown in FIG. 2, a person with two rectangular stoppers on one side and the other side of the membrane body is used to check. The change of the permeation flow rate with respect to the operating time is shown in Fig. 27. As shown in Fig. 27, the permeation flow rate does not change even if the membrane separation is performed for 8 hours. Obviously, the stability of the permeation flow rate of the membrane separation device of the present invention is stable. (12) Concentration polarization reduction effect (a) MgS04 blocking rate Use the membrane separation system shown in Figure 13 as the membrane separation device of the present invention, as shown in Figure 3, used on the side of the membrane body and On the other side, each with four rectangular stoppers was examined for the effect of reducing the polarization difference with respect to the outer peripheral velocity of the film. The results are shown in FIG. 18. The MgS04 blocking rate (#) refers to the ratio defined by the following formula.
MgS04阻止率=[1 —(透過濃度)/(原液MgS04濃度)] X 100(%) 亦即，其顯示阻止率的數値越大，濃差極化減低效果 越優異，本發明之膜分離裝置具有充份實用程度高的 MgS04阻止率。 31 衣紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） ---— — — — — — — —---· I I (請先閱讀背面之注意事項再填寫本頁) 訂· 線- 550113 A7 ___B7____ 五、發明說明（ / (b)NaCl阻止率 使用第13圖所示膜分離系統，作爲本發明膜分離裝置 ，如第3圖所示，使用於膜體一側及另一側分別具有4個 長方形擋件者，檢查相對膜外周速度的濃差極化減低效果 ，第29圖顯示其結果。又，NaCl阻止率(鲁)係指次式所定 義的比率。MgS04 blocking rate = [1 — (transmittance concentration) / (stock solution MgS04 concentration)] X 100 (%) That is, the larger the number showing the blocking rate, the more excellent the effect of concentration polarization reduction, and the membrane separation of the present invention The device has a sufficient practical degree of MgS04 blocking rate. 31 The size of the paper is applicable to the Chinese National Standard (CNS) A4 (210 X 297 mm) ----- — — — — — — ——— II (Please read the precautions on the back before filling this page) Order · Line-550113 A7 ___B7____ 5. Explanation of the invention (/ (b) The NaCl blocking rate uses the membrane separation system shown in Figure 13 as the membrane separation device of the present invention, as shown in Figure 3, used on one side of the membrane body and the other For those who have four rectangular stoppers on one side, check the effect of reducing the polarization difference with respect to the peripheral speed of the membrane, and the results are shown in Fig. 29. The NaCl blocking rate (Lu) refers to the ratio defined by the equation.
Nad阻止率=[1 一（透過濃度）/(原液Nad濃度）]X 100(%) 亦即，其顯示Nad阻止率的數値越大，濃差極化減低 效果越優異，本發明之膜分離裝置具有充份實用程度高的 Nacl阻止率。 (13)使用輻射狀擋件情形下，膜體直徑與膜體轉數對透過 流量發生的效果 第30圖，是在使用第13圖所示膜分離系統，使用濃 度1重量％的膠乳，膜間差壓（自對膜體施加的流入側壓力 扣掉透過側壓力所得壓力，實際利用於被處理液透過的壓 力）爲200kpa，溫度爲25°C，膜爲超瀘膜(UF膜），擋件爲 第8圖所示輻射狀擋件(擋件數目爲8個），擋件相對膜體 表面積的投影面積爲40%的情形下，於300至1250mm的 範圍內改變膜體的直徑，檢查膜體轉數與透過流量的關係 的結果。 第31圖，是在使用第13圖所示膜分離系統，使用濃 度30重量％的膠乳，膜間差壓爲40kpa，溫度爲25°C，膜 爲UF膜，擋件爲第8圖所示放射狀擋件(擋件數目爲8個) 32 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） --------------裝--- (請先閱讀背面之注意事項再填寫本頁) 訂·· 線- 550113 A7 __B7 五、發明說明（$i) ，擋件相對膜體表面積的投影面積爲40%的情形下，在 300至1250mm的範圍內改變膜體直徑，檢查膜體轉數與 透過流量的關係的結果，可以說，第30圖是顯示低壓力、 低濃度的低負荷狀態下膜分離性能的圖表，第31圖則是顯 示高壓力、高濃度的高負荷狀態下的膜分離性能的圖表。 如第30圖所示，於低負荷狀態下，在膜體直徑爲300 至1250mm之間，若轉數達到50rpm，透過流量即急遽增 加，不過在轉數增至50rpm以下情形下，透過流量的上昇 量少。 如第31圖所示，於高負荷狀態下，膜體直徑變大時透 過流量相對於轉數增加的增加比例雖然變大，不過，顯然 地，即使膜體直徑自1000mm增至1250mm，透過流量並 未如此上昇。又，膜體直徑爲300至1250mm範圍的透過 流量最大値大約相同，即使是直徑300mm的膜體，在轉數 lOOOrpm下，透過流量亦達到最大値。 在考慮提供裝置不致於過長的實際膜片數的裝置、以 及避免與膜體直徑成正比的旋轉所需動力過大之點時，由 第30圖及第31圖可知，在使用輻射狀擋件的情形下，膜 體直徑以300mm至1000mm爲適當範圍，膜體轉數則以 50至lOOOrpm爲經濟而又效率的運轉範圍。 (14)膜體與輻射狀擋件的間隙對透過流量的影響 第32圖，是在使用第13圖所示膜分離系統，使用濃 度20重量％的膠乳，膜間差壓爲400kpa，溫度爲25t， 膜爲UF膜，擋件爲第8圖所示輻射狀擋件(擋件數目爲8 33 木紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） ____I I I I______· I I (請先閱讀背面之注意事項再填寫本頁) · -線· A7 550113 — B7 ---------- 五、發明説明 〆 -------------裝—— (請先閱讀背面之注意事項再填寫本頁) 個），擋件相對膜體表面積的投影面積爲40% ’膜體轉數爲 550rpm的情形下’檢查透過流量相對膜體與輻射狀擋件的 間隙的關係的結果。 如第32圖所示，於膜體與輻射擋件的間隙達到12mm 之前，雖然在透過流量方面看不到有大的變化，不過，若 此間隙趦過12mm，透過流量即急遽降低。 在膜體與擋件的間隙不滿2mm情形下，有膜體與擋件 容易接觸’膜體會破損的情形發生，若膜體與輻射狀擋件 的間隙超過12mm，透過流量即如第32圖所示，大幅降低 。並且，若膜體與擋件過於疏遠，爲了確保必要的膜面積 ，裝置全長即會變長，就現實工業裝置而言，這難以成立 。因此，膜體與輻射狀擋件的間隙以2至12mm的範圍較 佳。 (15)輻射狀擋件與環形擋件的膜分離性能 線丨. 第33圖是在使用第13圖所示膜分離系統，使用濃度 30重量％的膠乳，溫度爲25t，膜爲uF膜，膜體轉數爲 550rpm情形下，以及使用第4圖所示環形擋件和使用第8 圖所示輻射狀擋件28(擋件個數有8個，擋件相對於膜體 表面積的投影面積爲40%)情形下，檢查膜間差壓與透過流 量關係的結果。 於第33圖中，符號「〇」表示輻射狀擋件，符號「φ 」表示環形擋件。如第33圖所示，膜間差壓一增大，輻射 狀擋件的透過流量即較環形擋件大，顯然，輻射狀擋件的 膜分離性能較環形檔件優異。 34 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公餐巧 550113 A7 ____B7____ 五、發明說明 (16) 輻射狀擋件的個數與透過流量 ——— — — — — — — — — —II · I I (請先閱讀背面之注意事項再填寫本頁) 第34圖，是在使用第13圖所示膜分離系統，使用濃 度20重量％的膠乳，膜間差壓爲400kpa，溫度爲25°C， 膜爲UF膜，擋件爲第8圖所示輻射狀擋件，擋件相對膜 體表面積的投影面積爲40%，膜體轉數爲550rpm情形下 ，檢查輻射狀擋件數目與透過流量的關係的結果。 如第34圖所示，若擋件數目少於4個，透過流量即很 小，擋件數目一增，透過流量亦變大，不過，顯然地，即 使增加到大於12個，透過流量亦已經不會變大。 因此，顯然輻射狀擋件數目4至12個是有效率進行膜 分離的範圍。 (17) 輻射狀擋件相對膜體表面積的投影面積與透過流量 .線· 第35圖，是在使用第13圖所示膜分離系統，使用濃 度20重量％的膠乳，膜間差壓400kpa，溫度爲25°C，膜 爲UF膜，擋件爲第8圖所示輻射狀擋件(擋件數目爲8個) ，膜體轉數爲550rpm的情形下，檢查輻射狀擋件相對膜 體表面積的投影面積(％)與透過流量的關係的結果。 如第35圖所示，顯然在輻射狀擋件相對膜體表面積的 投影面積在30%以上時，透過流量急遽增加，若此投影面 積超過90%，透過流量即降低。 因此，顯然輻射狀擋件相對膜體表面的投影面積30% 至70%的範圍是有效率進行膜分離的範圍。 (18) 膜體旋轉時的徑向加速度與透過流量 第36至42圖顯示使用第13圖所示膜分離系統，檢 35 1紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐「 一"" ' 550113 A7 _____Β7_____ 五、發明說明（if 查透過流量相對膜體旋轉時的半徑方向加速度的關係的結 果。 第36至42圖是在溫度爲25°C，膜爲UF膜，擋件爲 第45圖所示環形擋件68，以膜間差壓(操作壓力)爲參數， 檢查透過流量相對膜體旋轉時的徑向加速度的結果。第36 圖、第37圖、第38圖、第39圖分別顯示膠乳濃度1重量 %、10重量％、20重量％、30重量％的情形。由第36圖至 39圖可知，與膠乳濃度的高低無關，於所有運轉條件下， 徑向加速度透過流量之間呈現大致一定的比例關係，操作 壓力越高，透過量變得越大。又，雖然徑向加度一增加， 透過流量即變大，不過，膠乳濃度越低，低加速度區域的 此種關係即越顯著。由第37至39圖可知，雖然在膠乳濃 度爲10重量％以上的高濃度中，若徑向加速度在200m/ see2以上，無法獲得某一程度的透過流量，不過，由第36 圖可知，於膠乳濃度不滿10重量％的低濃度中，在徑向加 速度爲100m/SCe2以上的範圍內，都可獲得實用上很充份 的透過流量。 第40至42圖是以別的參數對第36至39圖加以整理 者，其係溫度爲25°C膜，膜爲UF膜，擋件爲第45圖所示 環形擋件68，以膠乳濃度爲參數，檢查透過流量相對膜體 旋轉時的徑向加速度的關係的結果。第40圖、第41圖、 第42圖分別顯示膜間差壓(操作壓力）爲200kpa、300kpa、 400kpa的情形。由第40至42圖可知，與操作壓力的高低 無關，在所有運轉條件下，徑向加速度與透過流量之間呈 36 幸、紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） (請先閱讀背面之注意事項再填寫本頁) 裝 ;線- 550113 A7 五、發明說明（>>) 現大致一定的比例關係，濃度越低，透過流量越大。 又，就擋件而言，可使用如第43(a)圖所示，沖出多數 個預定形狀的孔的擋件，或如第43(b)圖所示’施以蝕刻’ 使擋件表裡面粗糙的擋件，或如第43(c)所示，將擋件壓緊 於帶有凹凸花紋（進行壓花加工），於擋件表裡面施有凹凸 花紋的擋件，第43(a)圖雖然顯示輻射狀擋件的情形，不過 ，亦可於其他形狀的擋件設置沖孔，第43(b)圖的蝕刻處理 ，第43(c)圖的壓花加工可適用於所有形狀的擋件。藉由此 種沖孔、蝕刻或壓花加工，增大擋件的溫流促進效果，使 透過流量變大。 又，容器2亦可爲圓筒以外的形狀，例如四角形以上 的多角形或無上蓋的槽形。 於本實施例中雖然舉橫置裝置的例子，不過，不限於 此，亦可使用縱置裝置。若使用縱置裝置，膜體負載即不 會直接加諸旋轉軸，故可使旋轉軸較橫置裝置者，可製作 大型膜分離裝置。 由於本發明如以上說明構成，故適於來作爲裝置組裝 不費事，成本低，並且，壓力損失小，有效率地進行透過 處理，有效發揮膜分離性能的旋轉型膜分離裝置。 五、圖式之簡單說明 第1圖是本發明旋轉型膜分離裝置之一實施例之立體 圖。 37 木紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公楚 1 -----— ----I — — — — —------ (請先閱讀背面之注意事項再填寫本頁) I · •線 550113 A7 ____B7____ 五、發明說明（少 第2a圖是顯示本發明旋轉型膜分離裝置之長方形擋件 、膜體與容器之一實施例之剖面圖；第2b圖是使用此長方 形擋件之旋轉型分離裝置之包含剖面之側視圖，其省略旋 轉裝置；第2c圖是第2a圖之II-II方向剖面圖。 第3a圖是顯示本發明旋轉型膜分離裝置之長方形擋件 、膜體與容器之另一實施例之剖面圖；第3b圖是使用此長 方形擋件之旋轉型膜分離裝置之包含剖面之側視圖，其省 略旋轉裝置；第3c圖是第3a圖ΙΙΙ-ΙΙΙ方向剖面圖。 第4a圖是顯示於膜體之兩側，與膜體間相隔一間隙， 自容器之一內壁附近之另一內壁附近，夾著旋轉軸，分別 平行配置8個棒狀檔件的旋轉型膜分離裝置之棒狀擋件、 膜體與容器之一例子之剖面圖；第4b圖是使用此棒狀擋件 之旋轉型膜分離裝置之含有剖面之側視圖，其省略旋轉裝 置；第4c圖是顯示棒狀擋件之連結方法之圖面。 第5a圖是放大顯示於本發明旋轉型膜分離裝置之一實 施例中，膜體安裝於旋轉軸處之剖面圖；5b圖是放大顯示 其他實施例之膜體安裝旋轉軸處之剖面圖。 第6a圖是放大顯示於本發明旋轉型膜分離裝置之一實 施例，容器內壁附近之膜體與長方形擋件之剖面圖；第6b 圖是放大顯示透過性膜內之透過液輸送路徑之圖面。 第7圖顯示本發明旋轉型膜分離裝置中被處理液之流 程之圖面。 第8a圖是顯示本發明旋轉型膜分離裝置之輻射狀擋件 、膜體和容器之一實施例之剖面圖，第8b圖是第8a圖之 38 本紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） -------------裝—— (請先閱讀背面之注意事項再填寫本頁) 訂： -線. 550113 A7 _B7__ 五、發明說明（） 第21圖是顯示長方形擋件之數量與透過流量之關係之 圖表。 第22圖是顯示長方形擋件相對於膜體表面積之投影面 積(％)與透過流量之關係之圖表。 第23圖是顯示膜外周速度與透過流量之關係之圖表。 第24圖是顯示膜體直徑與透過流量之關係之圖表。 第25圖是顯示膜體旋轉數與透過流量之關係之圖表。 第26圖是顯示膜體與擋件之間隔與透過流量之關係之 圖表。 第27圖是顯示本發明旋轉型膜分離裝置之透過流量之 時間變化圖表。 第28圖是顯示本發明旋轉型膜分離裝置之濃差極化減 低效果之圖表。 第29圖是顯示本發明旋轉型膜分離裝置之濃差極化減 低果之另一圖表。 第30圖是顯示在使用輻射狀構擋件膜分離低濃度膠乳 情形下，以膜體直徑爲參數，膜體旋轉數與透過流量之關 係之圖表。 第31圖是顯示在使用輻射狀擋件膜分離高濃度膠乳情 形下，以膜體直徑爲參數，膜體旋轉數與透過流量之關係 之圖表。 第32圖是顯示在使用輻射狀擋件膜分離情形下，透過 流量相對於膜體與擋件之間隙之關係之圖表。 第33圖是顯示在使用環形擋件或輻射狀擋件膜分離情 40 木紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） (請先閱讀背面之注意事項再填寫本頁)Nad blocking rate = [1-(transmission concentration) / (stock solution Nad concentration)] X 100 (%) That is, the larger the number of Nad blocking rates, the more excellent the effect of reducing concentration polarization, and the film of the present invention The separation device has a highly practical Nacl blocking rate. (13) Effect of membrane diameter and membrane revolution on permeation flow when using a radial stopper Figure 30 shows the use of the membrane separation system shown in Figure 13 with a 1% by weight latex. The differential pressure (the pressure obtained by deducting the pressure on the permeate side from the pressure on the inflow side applied to the membrane body, the pressure actually used for permeation of the treated liquid) is 200kpa, the temperature is 25 ° C, and the membrane is an ultra-thin membrane (UF membrane). The stopper is a radial stopper shown in FIG. 8 (the number of stoppers is eight). When the projection area of the stopper with respect to the surface area of the film body is 40%, the diameter of the film body is changed within the range of 300 to 1250mm. The result of examining the relationship between the number of revolutions of the membrane body and the permeation flow rate. Figure 31 shows the use of the membrane separation system shown in Figure 13, using a latex with a concentration of 30% by weight, a differential pressure between the membranes of 40kpa, a temperature of 25 ° C, a membrane of UF, and a stopper as shown in Figure 8. Radial stopper (the number of stoppers is 8) 32 This paper size is applicable to China National Standard (CNS) A4 specification (210 X 297 mm) -------------- install --- (Please read the precautions on the back before filling in this page) Order ·· Thread-550113 A7 __B7 V. Description of the invention ($ i), when the projection area of the stopper relative to the surface area of the membrane is 40%, in the range of 300 to 1250mm The results of changing the membrane diameter within the range of the membrane and examining the relationship between the number of revolutions of the membrane and the permeate flow rate can be said that FIG. 30 is a graph showing membrane separation performance under low pressure and low concentration and low load state, and FIG. 31 is Graph showing membrane separation performance under high pressure, high concentration and high load conditions. As shown in Figure 30, under low load conditions, when the membrane diameter is between 300 and 1250 mm, if the number of revolutions reaches 50 rpm, the transmission flow rate increases sharply, but when the number of revolutions increases below 50 rpm, the transmission rate The amount of rise is small. As shown in Figure 31, under high load conditions, the increase in the permeation flow rate relative to the increase in the number of revolutions when the diameter of the membrane becomes larger, although it is clear that even if the membrane diameter increases from 1000 mm to 1250 mm, the permeation flow rate It has not risen that way. In addition, the maximum permeation flow rate of the membrane body in the range of 300 to 1250 mm is approximately the same. Even for a membrane body with a diameter of 300 mm, the permeation flow rate reaches the maximum at a revolution of 1,000 rpm. When considering the provision of a device that does not cause the actual number of diaphragms to be too long, and the point that the power required to avoid rotation that is proportional to the diameter of the membrane is too large, it can be seen from Figures 30 and 31 that the use of radial stoppers In the case of a film body diameter of 300mm to 1000mm is an appropriate range, and the number of revolutions of the film body is an economical and efficient operating range of 50 to 1000rpm. (14) The influence of the gap between the membrane body and the radial stop on the permeate flow. Figure 32 shows the use of the membrane separation system shown in Figure 13. The latex with a concentration of 20% by weight is used. The differential pressure between the membranes is 400kpa and the temperature is 25t, the film is UF film, and the stopper is a radial stopper as shown in Figure 8 (the number of stoppers is 8 33) The size of wood and paper is applicable to China National Standard (CNS) A4 (210 X 297 mm) ____I II I ______ · II (Please read the precautions on the back before filling this page) · -line · A7 550113 — B7 ---------- V. Description of the invention〆 ------------- —— (Please read the precautions on the back before filling in this page)), the projection area of the stopper relative to the surface area of the membrane is 40% 'in the case of membrane revolutions of 550rpm' check the transmission flow relative to the membrane and the radiation The result of the relationship of the clearance of the stopper. As shown in Figure 32, before the gap between the membrane body and the radiation stopper reaches 12 mm, although there is no significant change in the transmission flow rate, if the gap exceeds 12 mm, the transmission flow rate decreases sharply. In the case where the gap between the membrane body and the stopper is less than 2mm, there is a case where the membrane body and the stopper are easy to contact. 'The membrane body may be damaged. If the gap between the membrane body and the radial stopper exceeds 12mm, the transmission flow is as shown in Figure 32. Display, greatly reduced. In addition, if the membrane body and the stopper are too far apart, in order to ensure the necessary membrane area, the overall length of the device will become longer, which is difficult to establish in terms of actual industrial devices. Therefore, the gap between the film body and the radial stopper is preferably in the range of 2 to 12 mm. (15) Membrane separation performance line of the radial stopper and the ring stopper. Figure 33 is using the membrane separation system shown in Figure 13, using a latex with a concentration of 30% by weight, the temperature is 25t, and the membrane is a uF membrane. When the membrane rotation speed is 550 rpm, and the annular stopper shown in Fig. 4 and the radial stopper 28 shown in Fig. 8 are used (the number of the stopper is 8, the projection area of the stopper relative to the surface area of the film body) In the case of 40%), check the relationship between the differential pressure between the membranes and the permeate flow. In FIG. 33, the symbol "0" indicates a radial stopper, and the symbol "φ" indicates a ring stopper. As shown in Fig. 33, as the differential pressure between the membranes increases, the permeate flow of the radial stopper is larger than that of the annular stopper. Obviously, the membrane separation performance of the radial stopper is superior to that of the annular stopper. 34 This paper size applies to Chinese National Standard (CNS) A4 specifications (210 X 297 catering 550113 A7 ____B7____ V. Description of the invention (16) Number and transmission flow of radial stoppers ——— — — — — — — — — — —II · II (Please read the precautions on the back before filling out this page) Figure 34 is using the membrane separation system shown in Figure 13, using a latex with a concentration of 20% by weight, the differential pressure between the membranes is 400kpa, and the temperature The temperature is 25 ° C, the film is a UF film, the stopper is a radial stopper as shown in Figure 8, the projection area of the stopper relative to the surface area of the film body is 40%, and the film body revolution is 550rpm, check the radial stopper The result of the relationship between the number and the permeated flow rate. As shown in Figure 34, if the number of stoppers is less than 4, the permeate flow rate is small, and the increase in the number of blockers increases the permeate flow rate, but obviously, even if the increase If it is more than 12, the permeate flow will not increase. Therefore, it is obvious that the number of radial stopper 4 to 12 is the range for efficient membrane separation. (17) The projected area of the radial stopper with respect to the surface area of the membrane body and Transmitted flow. Line · Figure 35 is making use of The membrane separation system shown in FIG. 13 uses a latex with a concentration of 20% by weight, a differential pressure between the membranes of 400 kpa, a temperature of 25 ° C, a membrane of UF, and a stopper as the radial stopper shown in FIG. 8 (the number of stoppers). When the number of revolutions of the membrane is 550 rpm, the relationship between the projection area (%) of the radial stopper with respect to the surface area of the membrane body and the permeate flow rate is checked. As shown in FIG. 35, it is clear that When the projected area of the film relative to the surface area of the film is more than 30%, the transmission flow rate increases sharply. If the projected area exceeds 90%, the transmission flow rate decreases. Therefore, it is clear that the projected area of the radial stopper on the film surface is 30% to 70 The range of% is the range for efficient membrane separation. (18) Radial acceleration and permeate flow when the membrane body rotates. Figures 36 to 42 show the use of the membrane separation system shown in Figure 13. Inspection 35 1 Paper size is applicable to China Standard (CNS) A4 specification (210 X 297 mm "" " " "550113 A7 _____ Β7 _____ V. Description of the invention (if the result of checking the relationship between the permeate flow and the radial acceleration when the membrane rotates. Figures 36 to 42 Is at a temperature of 25 ° C The membrane is a UF membrane, and the stopper is a ring-shaped stopper 68 shown in FIG. 45. Using the differential pressure (operating pressure) between the membranes as a parameter, the results of checking the radial acceleration of the permeate flow relative to the rotation of the membrane body are shown. Figures 37, 38, and 39 show the latex concentration of 1%, 10%, 20%, and 30% by weight. From Figures 36 to 39, it can be seen that it has nothing to do with the latex concentration Under operating conditions, there is a roughly constant proportional relationship between the radial acceleration transmission flow. The higher the operating pressure, the larger the transmission volume becomes. In addition, although the permeation flow rate increases as the radial acceleration increases, the lower the latex concentration, the more significant this relationship is in the low acceleration region. From Figures 37 to 39, it can be seen that although the latex concentration is 10% by weight or more, if the radial acceleration is 200m / see2 or more, a certain amount of permeate flow cannot be obtained, but from Figure 36, it can be seen that In low concentrations with a latex concentration of less than 10% by weight, a practically sufficient permeate flow rate can be obtained in a range where the radial acceleration is 100 m / SCe2 or more. Figures 40 to 42 are the other parameters for finishing Figures 36 to 39. The temperature is 25 ° C, the film is UF, and the stopper is the ring stopper 68 shown in Figure 45. As a parameter, the result of examining the relationship between the permeate flow rate and the radial acceleration when the membrane body was rotated. Figures 40, 41, and 42 show the cases where the differential pressure (operating pressure) between the membranes is 200 kpa, 300 kpa, and 400 kpa, respectively. As can be seen from Figures 40 to 42, it has nothing to do with the operating pressure. Under all operating conditions, the radial acceleration and the permeate flow are 36. Fortunately, the paper size applies the Chinese National Standard (CNS) A4 specification (210 X 297 mm). ) (Please read the precautions on the back before filling out this page) Assembly; line-550113 A7 V. Description of the invention (> >) Now there is a roughly proportional relationship, the lower the concentration, the greater the permeate flow. As for the stopper, as shown in Fig. 43 (a), a stopper punched out with a plurality of holes having a predetermined shape, or "etching" the stopper as shown in Fig. 43 (b) can be used. Rough stopper on the inside of the watch, or as shown in 43 (c), press the stopper on the stopper with embossing (embossing), and apply a stopper on the inside of the stopper. a) Although the figure shows the situation of the radial stopper, punching holes can also be provided in the stopper of other shapes. The etching process of Fig. 43 (b) and the embossing process of Fig. 43 (c) can be applied to all Shaped stop. By such punching, etching or embossing, the temperature-flow promoting effect of the stopper is increased, and the permeate flow is increased. In addition, the container 2 may have a shape other than a cylinder, for example, a polygonal shape with a quadrangular shape or more, or a slot shape without a lid. Although an example of a horizontal device is used in this embodiment, the invention is not limited to this, and a vertical device may be used. If a vertical device is used, the load of the membrane body will not be directly applied to the rotating shaft. Therefore, if the rotating shaft is relatively horizontal, the large-scale membrane separation device can be manufactured. Since the present invention is structured as described above, it is suitable for a rotary membrane separation device that is not complicated to assemble as a device, has low cost, has a small pressure loss, efficiently performs permeation processing, and effectively exerts membrane separation performance. V. Brief Description of Drawings Figure 1 is a perspective view of an embodiment of a rotary membrane separation device of the present invention. 37 Wood paper scale is applicable to China National Standard (CNS) A4 (210 X 297 Gong Chu 1 -----— ---- I — — — — — ------ (Please read the precautions on the back first) Fill out this page again) I · • Line 550113 A7 ____B7____ 5. Explanation of the invention (less Figure 2a is a sectional view showing one embodiment of the rectangular stopper, membrane body and container of the rotary membrane separation device of the present invention; Figure 2b It is a side view including a cross section of a rotary separation device using the rectangular stopper, and the rotation device is omitted; FIG. 2c is a sectional view taken along the direction II-II of FIG. 2a. FIG. 3a is a view showing the rotary membrane separation device of the present invention. Sectional view of another embodiment of the rectangular stopper, the membrane body and the container; FIG. 3b is a side view including a cross section of the rotary membrane separation device using the rectangular stopper, and the rotation device is omitted; FIG. Figure 3a is a cross-sectional view in the direction of III-III. Figure 4a is shown on both sides of the membrane body, separated from the membrane body by a gap, from the inner wall near one of the container to the other inner wall, sandwiching the rotation axis, respectively parallel One of the rotary membrane separators equipped with 8 rod-shaped stops Sectional view of an example of a stopper, a membrane body, and a container; FIG. 4b is a side view containing a cross section of a rotary membrane separation device using the rod-shaped stopper, and the rotation device is omitted; FIG. 4c is a bar-shaped display Figure 5a of the method of connecting the stoppers. Figure 5a is an enlarged sectional view of the membrane mounted on the rotating shaft in an embodiment of the rotary membrane separation device of the present invention; Figure 5b is an enlarged view of the membrane of other embodiments Sectional view of the rotary shaft where the body is installed. Figure 6a is an enlarged sectional view of a membrane body and a rectangular stopper near the inner wall of the container; Figure 7 shows the transmission path of the permeated liquid in the membrane. Figure 7 shows the flow of the liquid to be processed in the rotary membrane separation device of the present invention. Figure 8a shows the radial stopper of the rotary membrane separation device of the present invention. A sectional view of one embodiment of the membrane, the container and the container. Figure 8b is Figure 38 of Figure 8a. The paper size is applicable to Chinese National Standard (CNS) A4 (210 X 297 mm) --------- ---- install—— (Please read the note on the back first Please fill in this page again) Order:-line. 550113 A7 _B7__ 5. Description of the invention () Figure 21 is a graph showing the relationship between the number of rectangular stoppers and the permeate flow. Figure 22 shows the rectangular stoppers relative to the membrane. A graph showing the relationship between the projected area (%) of the surface area and the permeation flow rate. Fig. 23 is a graph showing the relationship between the peripheral speed of the membrane and the permeation flow rate. Fig. 24 is a graph showing the relation between the membrane diameter and the permeation flow rate. Fig. 25 It is a graph showing the relationship between the number of rotations of the membrane body and the permeate flow rate. Fig. 26 is a graph showing the relationship between the interval of the membrane body and the stopper and the permeation flow rate. Fig. 27 is a graph showing the permeation flow rate of the rotary membrane separation device of the present invention. Time change chart. Fig. 28 is a graph showing the concentration polarization reduction effect of the rotary membrane separation device of the present invention. Fig. 29 is another graph showing the reduction in the concentration polarization of the rotary membrane separation device of the present invention. Fig. 30 is a graph showing the relationship between the number of rotations of the membrane body and the permeate flow rate in the case of separating a low-concentration latex using a radial barrier film. Fig. 31 is a graph showing the relationship between the number of rotations of the membrane body and the permeate flow rate in the case of separating a high-concentration latex using a radial stopper membrane, with the membrane diameter as a parameter. Fig. 32 is a graph showing the relationship between the permeate flow rate and the gap between the membrane body and the stopper when the radial stopper film is used for separation. Figure 33 shows the separation of the film using a ring stopper or a radial stopper. 40 Wood paper size is applicable to China National Standard (CNS) A4 (210 X 297 mm) (Please read the precautions on the back before filling out this page. )
----I tr--------- 550113 B7 五、發明說明（） 形下，膜間差壓與透過流量之關係之圖表。 (請先閱讀背面之注意事項再填寫本頁) 第34圖是顯示在使用輻射擋件膜分離情形下，輻射狀 擋件個數與透過流量之關係之圖表。 第35圖是顯示在使用輻射狀擋件膜分離情形下，輻射 狀擋件相對於膜體表面積之投影面積(％)與透過流量之關係 之圖表。 第36圖是顯示在使用環形擋件膜分離情形下，以膜間 差壓（操作壓力）爲參數，透過流量相對於膜體旋轉時的半 徑方向加速度之關係之圖表。 第37圖是顯示在使用環形擋件膜分離情形下，以膜間 差壓（操作壓力）爲參數，透過流量相對於膜體旋轉時之徑 向加速度之關係，有別於第36圖之圖表。 第38圖是顯示在使用環形構件膜分離情形下，以膜間 差壓（操作壓力）爲參數，顯示透過流量相對於膜體旋轉時 之徑面加速度之關係，有別於第36圖及第37圖之圖表。 第39圖是顯示在使用環形構件分離情形下，以膜間差 壓（操作壓力）爲參數，透過流量相對於膜體旋轉時之徑向 加速度之關係，有別於第36圖、第37圖及第38之圖表。 第40圖是顯示在使用環形擋件膜分離情形下，以膠乳 濃度爲參數，透過流量相對於膜體旋轉時之徑向加速度之 關係之圖表。 第41圖是顯示在使用環形擋件膜分離情形下，以膠乳 濃度爲參數，透過流量相對於膜體旋轉時之徑向加速度之 關係有別於第40圖之圖表。 41 木紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐) — 550113 A7 ___J7____ 五、發明說明（） 第42圖是顯示在使用環形擋件膜分離情形下，以膠乳 濃度爲參數，透過流量相對於膜體旋轉時之徑向加速度之 關係之有別於第40圖及第41圖之圖表。 第43a圖是顯示於擋件設有數種沖孔之例之俯視圖； 第43b圖是顯示於擋件之表、裡面施以蝕刻之例之剖面圖 :第43c圖是顯示於擋件之表、裡面施以壓花加工之例之 剖面圖。 第44圖是顯示用錯流方式之膜分離裝置之槪略構造之 圖面。 第45a圖是顯示習知旋轉型膜分離裝置之環形擋件、 膜體和容器之剖面圖；第45b圖是使用此環形擋件之旋轉 型膜分離裝置之含有剖面之側視圖，其省略旋轉裝置。 第46a圖是顯示習知旋轉型膜分離裝置之開孔環形擋 件、膜體與容器之剖面圖；第46b圖是使用此開孔環形擋 件之旋轉型膜分離裝置之含有截面之側視圖，其省略旋轉 裝置。 (請先閱讀背面之注意事項再填寫本頁) I 0 emam ϋ ϋ n ·ϋ n n 一 n ϋ n ϋ 1 n · •線®-.---- I tr --------- 550113 B7 V. Description of the invention () Under the shape, the graph of the relationship between the differential pressure between membranes and the permeate flow. (Please read the precautions on the back before filling out this page.) Figure 34 is a graph showing the relationship between the number of radial barriers and the permeate flow when the radiation barrier membrane is used for separation. Fig. 35 is a graph showing the relationship between the projected area (%) of the radial stopper with respect to the surface area of the membrane body and the permeate flow when the radial stopper film is used for separation. Fig. 36 is a graph showing the relationship between the permeate flow rate and the radial acceleration when the membrane body rotates when the membrane is separated using an annular stopper and the differential pressure (operating pressure) between the membranes is used as a parameter. Fig. 37 shows the relationship between the permeate flow rate and the radial acceleration when the membrane body rotates with the differential pressure between the membranes (operating pressure) as a parameter when the membrane is separated using an annular stopper, which is different from the graph in Fig. 36 . Fig. 38 shows the relationship between the permeate flow rate and the radial acceleration when the membrane body rotates with the differential pressure between the membranes (operating pressure) as a parameter in the case of membrane separation using an annular member, which is different from Fig. 36 and Fig. Figure 37 chart. Fig. 39 shows the relationship between the permeation flow rate and the radial acceleration when the membrane body rotates with the differential pressure (operating pressure) as a parameter when the annular member is used for separation, which is different from Figs. 36 and 37. And chart of the 38th. Fig. 40 is a graph showing the relationship between the permeate flow rate and the radial acceleration when the membrane body rotates with the latex concentration as a parameter when the membrane is separated using an annular stopper. Fig. 41 is a graph showing the relationship between the permeate flow rate and the radial acceleration when the membrane body rotates with the latex concentration as a parameter when the membrane is separated using a ring-shaped stopper, which is different from the graph of Fig. 40. 41 Wood paper scale is applicable to China National Standard (CNS) A4 (210 X 297 mm) — 550113 A7 ___J7____ 5. Description of the invention () Figure 42 shows the latex concentration as a parameter in the case of separation using a ring-shaped stopper film The relationship between the permeate flow rate and the radial acceleration when the membrane rotates is different from the graphs in Figures 40 and 41. Fig. 43a is a plan view showing an example in which several kinds of punching holes are provided on the stopper; Fig. 43b is a cross-sectional view showing an example of etching on the surface of the stopper; Fig. 43c is a table showing the stopper, A cross-sectional view of an example in which embossing is applied. Fig. 44 is a diagram showing a schematic structure of a membrane separation device using a cross-flow method. Fig. 45a is a sectional view showing a ring stopper, a membrane body and a container of a conventional rotary membrane separation device; Fig. 45b is a side view including a cross section of a rotary membrane separation device using the ring stopper, and the rotation is omitted Device. Fig. 46a is a cross-sectional view showing a ring-shaped stopper, a membrane body and a container of a conventional rotary membrane separation device; Fig. 46b is a side view containing a cross-section of a rotary-type membrane separation device using the ring-shaped stopper. , Which omits the rotating device. (Please read the notes on the back before filling this page) I 0 emam ϋ ϋ n · ϋ n n-n ϋ n ϋ 1 n
[符號說明] 1 供給入口 2 容器 3 旋轉軸 4、5 透過液出口 6 濃縮液出口 7 馬達 42 木紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐） 550113 A7 B7 五、發明說明（ 9 10 11 12 13、20 21 26 27 28 29a 29b 30 45 68 板體 隔離布 透過性膜 膜體 長方形擋件 棒狀擋件 膜孔 透過液輸送路徑 輻射狀擋件 圓弧形擋件 鈞形擋件 翼形擋件 鑿孔板狀擋件 環狀擋件 (請先閱讀背面之注意事項再填寫本頁) ·111111 丨 ^ · I--I I I I I . 木紙張尺度適用中國國家標準（CNS)A4規格（210 X 297公釐）[Description of symbols] 1 Supply inlet 2 Container 3 Rotary shafts 4, 5 Permeate outlet 6 Concentrated liquid outlet 7 Motor 42 Wood and paper standards are applicable to China National Standard (CNS) A4 (210 X 297 mm) 550113 A7 B7 V. Invention Description (9 10 11 12 13, 20 21 26 27 28 29a 29b 30 45 68 Plate insulation cloth Permeable membrane Membrane rectangular stopper Rod stopper Film hole Transmission liquid transmission path Radial stopper Arc stopper Jun Shape stopper Wing stopper Chisel plate stopper Ring stopper (Please read the precautions on the back before filling out this page) · 111111 丨 ^ · I--IIIII. Wood paper size applies to Chinese National Standard (CNS) A4 size (210 X 297 mm)