201210953 六、發明說明： 【發明所屬之技術領域】 本發明是有關於：可以利用在生活上的排廢水、下水 道、食品工廠或紙漿工廠等廣泛排廢水濃度範圍之有機性 排廢水處理的有機性排廢水的生物處理方法及裝置，特別 是關於不會使處理水質惡化，並提升處理效率，且可以減 少剩餘污泥產生量的有機性排廢水的生物處理方法及裝置 【先前技術】 將有機性排廢水作生物處理的情況下所利用的活性污 泥法，因處理水質良好，且維護容易等優點，而廣泛應用 在下水道處理或產業廢水處理等。但是，由於活性污泥法 中BOD容積負荷一般爲0.5〜0.8kg/m3/d左右，而需要寬 廣的基地面積。又，已分解之BOD的20〜40%爲了轉換 成菌體，亦即污泥，大量的剩餘污泥處理也成了問題。 關於有機性排廢水的高負荷處理，皆知有添加載體的 流動床法。使用該方法時，以3kg/m3/d以上之BOD容積 負荷來運轉是可能的。但是，以該方法所產生污泥量爲已 分解之BOD的30〜50%左右，比一般活性污泥法要高， 而成了缺點。 日本特開昭55 -20649號公報中記載：先將有機性排 廢水在第一處理槽藉細菌作處理，再氧化分解被包含在排 廢水的有機物並轉換成非凝集性細菌之菌體後，在第二處 -5- 201210953 理槽藉著使固著性原生動物捕食除去而達到剩餘污泥的減 量化。更者，在本方法中可高負荷運轉，也可提升活性污 泥法的處理效率。 已提出多種如此類利用位於細菌高階的原生動物或後 生動物之捕食的廢水處理方法。 例如，在日本特開2000-210692號公報中，以日本特 開昭55-20649號公報的處理方法，提出針對因原水水質 變動導致處理性能惡化之問題的對策。具體的方法是提出 :「將被處理水之BOD變動從平均濃度的中間値調整到 50%以內」、「經過一定時間測量第一處理槽內及第一處 理水之水質」、「第一處理水之水質惡化時，將種污泥或 微生物製劑添加至第一處理槽」等方法。 日本特公昭60-23 83 2號公報中，提案讓細菌、酵母 、放射菌、藻類、黴菌類或廢水處理的初次沈澱污泥或剩 餘污泥，使原生動物或後生動物捕食時，藉由超音波處理 或機械攪拌，將這些餌的絮凝體大小作成比動物的口更小 的方法。 又，關於流動床與活性污泥法之多段處理的發明，有 日本特許第34 1 0699號公報所記載者。在該方法中，藉著 將後段的活性污泥法以 BOD污泥負荷O.lkg-BOD/kg-MLSS/d的低負荷下運轉，使污泥自我氧化，而能大幅減 低污泥抽除量。 此類利用微生物之捕食作用的多段活性污泥法，實際 上已被利用在有機性廢水處理上，依據處理對象的排廢水 -6- 201210953 ，能提升處理效率，並減少50%左右的污泥產生量。對該 污泥減量有貢獻的微生物中，有濾過捕食型與凝集體捕食 型。其中，凝集體捕食型之微生物，因爲可以啃咬並捕食 絮凝體化的污泥，所以使凝集體捕食型微生物佔優勢的情 況下，處理水質會惡化。因而，爲了提升處理水質，微生 物中，使濾過捕食型佔優勢雖然有效，但以往，並沒有提 出方法來控制濾過捕食型微生物與凝集體捕食型微生物的 繁殖，在排廢水處理中使用微生物進行污泥減量時，依據 運轉條件，會產生無法預期的處理水質惡化的問題。 活性污泥法中，有在污泥與處理水之固液分離時利用 膜分離裝置的膜式活性污泥法，和使用沉澱池的沉澱池型 活性污泥法。 比起沉澱池型活性污泥法，膜式活性污泥法的優點是 能維持提高污泥濃度，並以高容積負荷來運轉，而且不需 要沉澱池之類的污泥管理，即能得到良好水質的處理水。 但是，在膜式活性污泥法中，藉由活性污泥槽內之污 泥的性質，膜容易閉塞，膜的洗淨頻率提高成爲課題。 在日本特開平9-294996號公報中，提出藉由對曝氣 槽添加載體，減少污泥附著在膜上，以防止膜閉塞的方法 〇 但是，對曝氣槽添加載體的方法中，也有無法充分防 止膜閉塞的情況。 又，即使在以低負荷運轉活性污泥處理的情況下，污 泥的解體中產生細微SS (懸浮固體物Suspend Solid)， 201210953 使膜閉塞。再者，依據水温、負荷、SRT (固體物滯留時 間），一但在活性污泥內補食絮凝體的微生物急增，即會 促使污泥的細微化，導致處理水的惡化，而使得將處理水 作固液分離之膜分離裝置的運轉管理變得困難。 [先前技術文獻] [專利文獻] [專利文獻1]日本特開昭5 5-20649號公報 [專利文獻2]日本特開2000-210692號公報 [專利文獻3]日本特公昭60-23832號公報 [專利文獻4]日本特許第341 0699號公報 [專利文獻5]日本特開平9-294996號公報 【發明內容】 [發明所欲解決之課題] 本發明中所提供之第1形態的發明（以下稱作「第1 發明」。），是提供一種利用微生物之捕食作用的多段活 性污泥法中，使濾過捕食型之微生物優勢化，在提升處理 效率及減量污泥的同時，更進一步謀求處理水質提升的有 機性排廢水的生物處理方法及裝置（課題I)。 本發明中所提供之第2形態的發明（以下稱作「第2 發明」。），是提供一種適用膜式活性污泥法之有機性排 廢水的生物處理中，能大幅地減少產生的污泥量，同時防 止膜閉塞，降低膜的洗淨頻率，並謀求高負荷運轉提升處 201210953 理效率，與穩定之處理水質的有機性排廢水的生物處理方 法及裝置（課題II)。 [解決課題之手段] 本案發明者們，爲解決上述課題I而深入檢討的結果 ，是藉著抽除後段生物處理槽污泥，並使其經由無氧槽， 可以抑制游泳性凝集體捕食型微生物的繁殖並防止處理水 質的惡化，再加上，藉著在後段生物處理槽中設置微生物 保持載體，可以保持固著性濾過捕食型微生物，即使抽除 後段生物處理槽之污泥並進行導入至無氧槽的處理，這些 微生物也不受影響，此結果得知能使濾過捕食型微生物佔 優勢。 第1發明即基於該見解所達成，以下說明其主旨。 第1發明之第1形態的有機性排廢水的生物處理方法 ，是：將有機性排廢水導入至設置成二段以上之多段好氧 性生物處理槽的第一生物處理槽，並藉細菌作生物處理， 再將包含來自第一生物處理槽之分散狀態的細菌的第一生 物處理水朝第二生物處理槽以後的生物處理槽流通，並作 生物處理之有機性排廢水的生物處理方法，其特徵爲：該 第二生物處理槽以後的生物處理槽中設有保持微生物的載 體，且抽除該第二生物處理槽以後的生物處理槽內之一部 分污泥，並在無氧槽中作處理後，再送回該第二生物處理 槽以後的生物處理槽。 第1發明之第2形態的有機性排廢水的生物處理方法 -9- 201210953 ，其特徵是在第1形態中，將上述第一生物處理水 —部分經由上述無氧槽並朝上述第二生物處理槽以 物處理槽流通。 第1發明之第3形態的有機性排廢水的生物處 ，其特徵是在第1形態或第2形態中，將上述有機 水的一部分導入上述無氧槽，再將殘留部分導入至 —生物處理槽。 第1發明之第4形態的有機性排廢水的生物處 ，其特徵是在第1形態至第3形態的任一形態中， 氧槽保持載體。 第1發明之第5形態的有機性排廢水的生物處 ，其特徵是在第1形態至第4形態的任一形態中， 第二生物處理槽以後的生物處理槽中設有保持微生 體。 第1發明之第6形態的有機性排廢水的生物處 ，其特徵是在第1形態至第5形態的任一形態中， 上述第二生物處理槽以後的生物處理槽之SRT (固 留時間）定在60日以下而抽除污泥。 第1發明之第7形態的有機性排廢水的生物處 ，其特徵是在第1至第6形態的任一形態中，將上 生物處理槽以後的生物處理槽之處理水作固液分離 分離污泥的至少一部分送回到上述第二生物處理槽 生物處理槽。 第1發明之第8形態的有機性排廢水的生物處 的至少 後的生 理方法 性排廢 上述第 理方法 上述無 理方法 上述該 物之載 理方法 爲了將 體物滞 理方法 述第二 ，再將 以後的 理裝置 -10- 201210953 ，是具備設置成二段以上之多段好氧性生物處理槽，並將 有機性排廢水導入第一生物處理槽並藉細菌作生物處理， 再將包含有來自第一生物處理槽之分散狀態的細菌的第一 生物處理水朝第二生物處理槽以後的生物處理槽流通，並 作生物處理的有機性排廢水的生物處理裝置，其特徵爲： 在該第二生物處理槽以後的生物處理槽中設有保持微生物 之載體，設置抽除該第二生物處理槽以後的生物處理槽內 之一部分污泥並作處理後，再送回該第二生物處理槽以後 的生物處理槽的無氧槽。 第1發明之第9形態的有機性排廢水的生物處理裝置 ，其特徵是在第8形態中，具有將上述第一生物處理水的 至少一部分經由上述無氧槽，並朝上述第二生物處理槽以 後的生物處理槽流通的手段。 第1發明之第1 〇形態的有機性排廢水的生物處理裝 置，其特徵是在第8形態或第9形態中，具有將上述有機 性排廢水之一部分導入上述無氧槽的手段，和將該有機性 排廢水之殘留部分導入上述第一生物處理槽的手段。 第1發明之第Π形態的有機性排廢水的生物處理裝 置，其特徵是在第8形態至第1 〇形態的任一形態中，載 體被保持在上述無氧槽中。 第1發明之第1 2形態的有機性排廢水的生物處理裝 置，其特徵是在第8形態至第1 1形態的任一形態中，上 述該第二生物處理槽以後的生物處理槽中設有保持微生物 的載體。 -11 - 201210953 第1發明之第1 3形態的有機性排廢水 置，其特徵是在第8形態至第12形態的任 了將上述第二生物處理槽以後的生物處理槽 物滯留時間）定在60日以下而抽除污泥。 第1發明之第1 4形態的有機性排廢水 置，其特徵是在第8形態至第1 3形態的任 有將上述第二生物處理槽以後的生物處理槽 液分離，再將分離污泥的至少一部分送回到 處理槽以後的生物處理槽的手段。 本案發明者們，爲解決上述課題II深 是在利用微生物之捕食作用的多段活性污泥 生物處理槽中設置以瞬時法處理有機物的槽 生，再在後段生物處理槽中，積極地使必要 化，以抑制引起膜閉塞的凝集體（絮凝體） 的繁殖；爲此，藉著在後段生物處理槽中設 載體，用來保持可有效率地捕食分散菌，且 分離性與提升處理水質有貢獻的固著性濾過 ;由上得知可以在膜式活性污泥法中防止膜 定的高負荷處理。 第2發明即基於該見解所達成，以下說 第2發明之第1形態的有機性排廢水的 ，是：將有機性排廢水導入設成二段以上之 物處理槽的第一生物處理槽，並藉細菌作生 包含來自第一生物處理槽之分散狀態的細菌 的生物處理裝 一形態中，爲 之SRT (固體 的生物處理裝 一形態中，具 之處理水作固 上述第二生物 入檢討結果， 法中，在前段 ，使分散菌產 之微生物優勢 捕食型微生物 置微生物保持 對污泥之固液 捕食型微生物 閉塞並執行穩 明主旨》 生物處理方法 多段好氧性生 物處理，再將 的第一生物處 -12- 201210953 理水朝第二生物處理槽以後的生物處理槽流通，並作生物 處理，再將該第二生物處理槽以後的生物處理槽之處理水 作固液分離的有機性排廢水的生物處理方法，其特徵爲： 在該第二生物處理槽以後的生物處理槽中設有保持微生物 的載體，且依據膜分離處理來進行該第二生物處理槽以後 的生物處理槽之處理水的固液分離。 第2發明之第2形態的有機性排廢水的生物處理方法 ，其特徵是在第1形態中，在槽外型膜分離裝置進行上述 膜分離處理。 第2發明之第3形態的有機性排廢水的生物處理方法 ，其特徵是在第1形態或第2形態中，設在上述第二生物 處理槽以後的生物處理槽內之載體是被固定在該生物處理 槽。 第2發明之第4形態的有機性排廢水的生物處理方法 ，其特徵是在第1形態至第3形態的任一形態中，將上述 有機性排廢水之一部分不經由上述第一生物處理槽而導入 上述第二生物處理槽以後的生物處理槽。 第2發明之第5形態的有機性排廢水的生物處理方法 ，其特徵是在第1形態至第4形態的任一形態中，爲了將 上述第二生物處理槽以後的生物處理槽之SRT (固體物滞 留時間）定在60日以下而抽除污泥。 第2發明之第6形態的有機性排廢水的生物處理方法 ，其特徵是在第1形態至第5形態的任一形態中，抽除上 述第二生物處理槽以後的生物處理槽內之一部分污泥，並 -13- 201210953 在無氧槽作處理後，再送回該第二生物處理槽以後的生物 處理槽。 第2發明之第7形態的有機性排廢水的生物處理裝置 ，是：具備設成二段以上之多段好氧性生物處理槽，並將 有機性排廢水導入第一生物處理槽，並藉細菌作生物處理 ，再將包含來自第一生物處理槽之分散狀態的細菌的第一 生物處理水朝第二生物處理槽以後的生物處理槽流通，並 作生物處理，再將第二生物處理槽以後的生物處理槽之處 理水作固液分離的有機性排廢水的生物處理裝置，其特徵 爲：該第二生物處理槽以後的生物處理槽中設有保持微生 物的載體，且具備膜分離處理裝置作爲該第二生物處理槽 以後的生物處理槽之處理水的固液分離手段。 第2發明之第8形態的有機性排廢水的生物處理裝置 ，其特徵是在第7形態中，上述膜分離裝置爲槽外犁膜分 離裝置。 第2發明之第9形態的有機性排廢水的生物處理裝置 ，其特徵是在第7形態或第8形態中，設在上述第二生物 處理槽以後的生物處理槽內之載體是被固定在該生物處理 槽中。 第2發明之第10形態的有機性排廢水的生物處理裝 置’其特徵是在第7形態至第9形態的任一形態中，具有 將上述有機性排廢水之一部分不經由上述第一生物處理槽 ’而導入上述第二生物處理槽以後的生物處理槽的手段。 第2發明之第Π形態的有機性排廢水的生物處理裝 -14- 201210953 置，其特徵是在第7形態至第1 0形態的任一形態中，爲 了將上述第二生物處理槽以後的生物處理槽之SRT (固體 物滞留時間）定在60日以下而抽除污泥。 第2發明之第1 2形態的有機性排廢水的生物處理裝 置，其特徵是在第7形態至第1 1形態的任一形態中，設 有將上述第二生物處理槽以後的生物處理槽內之一部分污 泥抽除並作處理後，再送回該第二生物處理槽以後的生物 處理槽的無氧槽。 [發明效果] 在第1發明，利用微生物之捕食作用的多段活性污泥 法中，藉著在生物處理槽中設置保持微生物的微生物保持 載體，且抽除該生物處理槽內污泥並在無氧槽作處理後送 回，可在保持微生物的生物處理槽內，抑制凝集體捕食型 微生物的繁殖並使濾過捕食型微生物優先繁殖，而能求得 處理水質的提升。 在第2發明，利用微生物之捕食作用的多段活性污泥 法中，藉著在生物處理槽中設置保持微生物的微生物保持 載體，可於該生物處理槽內保持住有效率地捕食分散菌， 且對污泥之固液分離性與提升處理水質有貢獻的固著性濾 過捕食型微生物，藉此，能防止將該生物處理槽之生物處 理水作膜分離處理之膜分離裝置的膜閉塞，並能降低膜的 藥品洗淨頻率。 因此，根據第1發明及第2發明，能有效地將有機性 -15- 201210953 排廢水作生物處理，且達到以下效果。 1 )排廢水處理時所產生之污泥大幅地減少 2) 依據高負荷運轉提升處理效率 3) 維持穩定的處理水質 【實施方式】 以下參考圖面詳細說明本發明之有機性排廢水 處理方法及裝置的實施形態。 [第1發明] 圖1〜5是表示第1發明之有機性排廢水的生 方法及裝置的實施形態系統圖。 在圖1〜5中，1是第一生物處理槽，2是第二 理槽’ 3是沉澱槽，4是無氧槽，5是膜分離裝置 21是散氣管，22是微生物保持載體，41是攪拌手 是載體；圖1〜5中表達同一功能的構件以相同符 〇 在圖1的形態中，原水（有機性排廢水）被導 生物處理槽1，並藉分散性細菌（非凝集性細菌） 分解有機成分（溶解性BOD)的70%以上，最好爲 上’ 90%以上更佳。該第一生物處理槽1的pH値: 上，最好爲8以下。但是，原水中包含較多油分時 也可爲8以上。 又，朝第一生物處理槽1的流通，通常爲瞬時 的生物 物處理 生物處 >11' 段，42 號表示 入第一 ，氧化 8 0 %以 專6以 pH値 法，而 -16- 201210953 以第一生物處理槽1之BOD容積負荷爲lkg/m3/d以上， 例如1〜20kg/m3/d，HRT (原水滯留時間）爲24小時以 下，最好爲8小時以下，例如〇 · 5〜8小時’可以得到分 散性細菌佔優勢的處理水，再者，藉著縮短HRT ’可以高 負荷處理BOD濃度較低的排廢水。 第一生物處理槽1中，藉著將來自後段生物處理槽之 —部分污泥送回，將該第一生物處理槽1作成二槽以上的 多段構造，並添加載體，使B0D容稂負荷5kg/m3/d以上 的高負荷處理成爲可能。 第一生物處理槽1中添加載體時，載體的形狀’可爲 球狀、平板狀、中空筒狀、線狀、板狀等任意形狀’大小 也在直徑0.1〜左右內均可隨意。又，載體的材料 可爲天然素材、無機素材、高分子素材等任一種素材，也 可以使用凝膠狀物質。再者，添加於第一生物處理槽1之 載體的塡充率較高時，不會產生分散菌，細菌附著於載體 ，或絲狀細菌繁殖。因而，藉著添加於第一生物處理槽1 之載體的塡充率定在10%以下，最好爲5%以下，不會影 響濃度變動，也能產生容易捕食的分散菌。 又，將該第一生物處理槽1的溶氧（DO)濃度設在 lmg/L以下，最好爲0.5mg/L以下，也可抑制絲狀細菌的 繁殖。 再者，在第一生物處理槽1將溶解性有機物完全分解 時，在第二生物處理槽2中不會形成絮凝體，又，微生物 繁殖所須的營養也不足，形成僅有壓密性較低之污泥佔優 -17- 201210953 勢的生物處理槽。因而，在第一生物處理槽1中的有機成 分之分解率不是100%，而是95%以下，最好是在85〜 9 0%。 第一生物處理槽1之處理水（第一生物處理水），朝 後段第二生物處理槽2流通，在此，依據殘存的有機成分 之氧化分解、分散性細菌的自我分解以及微生物的捕食來 進行剩餘污泥的減量化。 第二生物處理槽2中，由於利用了繁殖速度比細菌較 慢之微生物的運動與細菌的自我分解，而有必要使用能將 微生物與細菌留存在系統內的運轉條件及處理裝置。因而 第二生物處理槽2中，最好使用進行污泥回送的活性污泥 法或膜分離式活性污泥法。又，該第二生物處理槽2也可 爲二槽以上的多段構造。 在第1發明中，藉著在該第二生物處理槽2內設置微 生物保持載體22，可提高微生物的槽內保持量。 設在第二生物處理槽2之載體22的形狀，爲流動床 的情況可爲球狀、平板狀、中空筒狀、線狀等任意形狀， 大小爲直徑0.1〜l〇mm左右即可。也可以使用固定床， 此時載體22的形狀爲可線狀、板狀等任意形狀。再者， 載體22之材料爲天然素材、無機素材、高分子素材等任 意素材，也可使用凝膠狀物質》 在第二生物處理槽2中，必須要有用來維持微生物的 大量立足處，添加之載體的塡充率會依據流動床、固定床 的形式不同或材質而有差異，但最好爲0.5〜40%。 -18- 201210953 此外，如前所述，第二生物處理槽2中，不只有捕食 分散狀態之菌體的濾過捕食型微生物，也繁殖有能捕食絮 凝體化之污泥的凝集體捕食型微生物。後者邊游泳，邊捕 食絮凝體，所以佔優勢的情況下，污泥被咬的散亂，形成 微細化之絮凝體片分散的污泥。沉澱池型的活性污泥中因 該絮凝體片使處理水s S濃度上昇，而在膜式活性污泥中 產生膜的堵塞。因而，第1發明中，設置無氧槽4，藉著 在該無氧槽4中讓從第二生物處理槽2抽除之污泥滯留預 定時間，以妨礙游泳性之微生物的繁殖，求得生物相的穩 定化。此時，第二生物處理槽2中設有微生物保持載體 22，因濾過捕食型微生物定著在載體22側，幾乎不會從 第二生物處理槽2被抽除並流入無氧槽4，因而不會妨礙 濾過捕食型微生物的繁殖。從第二生物處理槽2被抽除， 且在無氧槽4被作處理的污泥被送回第二生物處理槽2中 〇 從第二生物處理槽2被抽除到無氧槽4的污泥量，以 及在無氧槽4污泥的滯留時間，是因應處理狀況再作適當 決定，但通常污泥的抽除量相對於槽容量爲1/30倍量/日 以上，又，在無氧槽4中的污泥滯留時間最好爲0.5小時 以上。 在第1發明，無氧槽4中，爲了妨礙微生物的繁殖， 必須將ORP定在OmV以下。爲此，最好不在無氧槽4進 行曝氣，而僅以機械作攪拌。再者，爲了促進ORP的降 低也可讓第一生物處理水或原水流通，並依據酸生成反應 -19- 201210953 或脫氮反應來降低ORP。 此外，爲了使無氧槽4中的ORP降低（脫氮反應、 酸生成反應）能穩定進行，也可以於無氧槽4添加載體》 若無氧槽4中的〇RP降低，因促使游泳性微生物的活性 降低，所以能縮短在無氧槽4之第二生物處理槽污泥的滯 留時間，能讓無氧槽4小型化。添加之載體爲流動床的情 況下，形狀可爲球狀、平板狀、中空筒狀、線狀的任意形 狀，大小也爲直徑0.1〜10 mm左右的任意尺寸。也可使 用固定床，此時的載體22之形狀爲線狀、板狀等任意形 狀。更者，材料可爲天然素材、無機素材、高分子素材等 任意素材，也可使用凝膠狀物質。 於無氧槽4添加載體時，其塡充率會因流動床、固定 床的形式不同或材質而有差異，但最好在0.5〜40 %。 再者’在該第二生物處理槽2中，定期替換槽污泥， 亦即’爲了剔出微生物或糞便，將SRT (固體物滯留時間 )固定控制在60日以下，最好是45日以下，更好是在 10日以上45日以下的範圍內。但是，第二生物處理槽2 內之污泥濃度（MLSS )形成2000mg/L以下時，即使 SRT>60日也可以。在此，SRT=(槽內污泥濃度X曝氣槽 容積）+(抽除污泥濃度XI日左右的抽除量），而槽內污 泥濃度（MLS S )是指浮游污泥的濃度，不包含載體附著 污泥部分。 此外，第1發明中，朝第二生物處理槽2投入的第一 生物處理水中殘存大量有機物時，其氧化分解在後段的處 -20- 201210953 理槽中進行。在微生物大量存在的第二生物處理槽2中， 若發生藉細菌的有機物氧化分解，作爲逃脫微生物捕食的 對策，皆知是在難以被捕食的形態下繁殖，如此一來所繁 殖之細菌群不會被微生物捕食，這些分解僅能仰賴自我消 化，導致污泥產生量減量的效果降低。因而，如前所述， 有必要將第一生物處理槽中有機物的大部分，亦即原水 BOD的70%以上，最好爲80%以上作分解，並轉換爲菌體 。因而，若以依據朝向後段生物處理槽之溶解性 BOD的 污泥負荷來表示，最好是以 0.25〜0.50kg-BOD/kg-MLSS/d作運轉。此處的MLSS也是指浮游污泥的濃度， 不包含附著在載體的污泥。 圖1中，來自第二生物處理槽2的處理水，接著在沉 澱槽3中被固液分離成污泥與處理水，分離水被取出作爲 處理水，而分離污泥的一部分作爲返送污泥被送回第二生 物處理槽2，而殘留部分作爲剩餘污泥被排出系統外。 再者，也可使用膜分離裝置取代該沉澱槽3作爲固液 分離手段。以往，活性污泥的膜分離處理中，因膜的堵塞 而減少流出水，使得藥品洗淨成爲課題，但根據本發明， 可以防止突發性的污泥分散化，而使膜分離裝置的運轉管 理變得容易。 圖2中所表示的形態’將來自第一生物處理槽1的第 —生物處理槽處理水之一部分，例如將1 〇〜2 0 %左右導入 無氧槽4,再將殘留部分導入至第二生物處理槽2此點與 圖1所表示的形態不同，其他均爲相同構造。如前所述， -21 - 201210953 如此一來，藉著將第一生物處理槽水之一部分導入無氧槽 4，使無氧槽4的ORP降低，可以提高在無氧槽4中妨礙 微生物繁殖的效果。 圖3中表示的形態，將原水之一部分’例如1 〇〜2 0 % 左右直接導入至無氧槽4，再將殘留部分導入至第一生物 處理槽1此點與圖1表示之形態不同，其他爲相同構造。 如前所述，如此一來，藉著將原水之一部分導入至無氧槽 4，使無氧槽4之ORP降低，可以提高在無氧槽4中妨礙 微生物繁殖的效果。 圖4表示之形態，使用膜分離裝置5取代沉澱槽3, 並將膜分離裝置5之透過水作爲處理水取出，同時將濃縮 水送回第二生物處理槽2，再將剩餘污泥從第二生物處理 槽2直接抽除此點與圖1表示之形態不同，其他爲相同構 造。如前所述，使用膜分離裝置5作爲固液分離手段時， 根據第1發明，由於能抑制凝集體捕食型微生物的繁殖， 減輕以往活性污泥之膜分離處理中膜的堵塞問題，使膜流 出水穩定而可降低藥品洗淨頻率。 圖5表示之形態，於無氧槽4添加載體42此點與圖 1表示之形態不同，其他爲相同的構造。如前所述，如此 一來，藉著在無氧槽4添加載體，使無氧槽4之ORP降 低，可以提高無氧槽4中妨礙微生物繁殖的效果。 圖1〜5，是表示第1發明之實施形態的一例，第1 發明並沒有限定於任一圖所表示者。例如，第一生物處理 槽、第二生物處理槽，如前所述，可以爲2段以上的多段 -22- 201210953 構造，因而，在第1發明中，也可以將生物處理槽設成3 段以上。 又，作爲固液分離手段，除了沉澱槽以外，也可使用 膜分離裝置或上浮式分離槽等，後段的生物處理槽，作爲 兼具生物處理槽與固液分離手段的膜浸漬型生物處理槽， 也可進行膜分離式好氧處理。 在任一形態中，根據第1發明，藉著在第二生物處理 槽以後的生物處理槽中設置微生物保持載體，且將第二生 物處理槽以後的生物處理槽污泥在無氧槽中作處理，可以 抑制凝集體捕食型微生物的優勢化，並同時達到污泥減量 與處理水水質的提升。 [第2發明] 圖6〜8是表示第2發明之有機性排廢水的生物處理 方法及裝置的實施形態系統圖。 在圖6〜8中，1是第一生物處理槽，2是第二生物處 理槽，4是無氧槽，5是膜分離裝置，11、21是散氣管， 22是微生物保持載體，41是攪拌手段；圖6〜8中達到相 同功能的構件以相同符號表示。 圖ό的形態中’原水（有機性排廢水）被導入至第一 生物處理槽1 ’並藉分散性細菌（非凝集性細菌），氧化 分解有機成分（溶解性BOD)的70%以上，最好氧化分 解80%以上，90°/。以上更佳。該第—生物處理槽i之ρΗ 値爲ό以上’最好爲8以下。但是，原水中包含過多油分 -23- 201210953 時pH値也可爲8以上。 又，朝第一生物處理槽1的流通，—般是瞬時法，第 —生物處理槽1之BOD容積負荷爲lkg/m3/d以上，例如 1〜20kg/m3/d，HRT (原水滯留時間）爲24小時以下，最 好爲8小時以下，例如在0.5〜8小時的情況下，可以得 到分散性細菌佔優勢的處理水，此外，藉著縮短HRT，能 以高負荷處理B OD濃度較低的排廢水。 第一生物處理槽1中，藉著將來自後段生物處理槽之 一部分污泥送回，且將第一生物處理槽1作成二槽以上之 多段構造，並添加載體，使BOD容積負荷5kg/m3/d以上 的高負荷處理成爲可能。 在第一生物處理槽1中添加載體時，載體的形狀爲球 狀、平板狀、中空筒狀、線狀、板狀等任意形狀，大小爲 直徑0.1〜10mm左右的任意尺寸。又，載體的材料可爲 天然素材、無機素材、高分子素材等任意素材，也可使用 凝膠狀物質。又，添加於第一生物處理槽1之載體的塡充 率較高時，不會產生分散菌，細菌附著於載體，或絲狀細 菌繁殖。因而，藉著將添加於第一生物處理槽1之載體的 塡充率定在20%以下，最好爲1 〇%以下，不會影響濃度變 動，可產生較易捕食的分散菌。 再者’該第一生物處理槽1將溶氧（DO)濃度定在 lmg/L以下，最好爲0.5mg/L以下，也可抑制絲狀細菌的 繁殖。 此外’在第一生物處理槽1中完全分解溶解性有機物 -24- 201210953 時，在第二生物處理槽2不會產生絮凝體，又，微生物用 以繁殖的營養也不足，而形成僅有壓密性較低之污泥佔優 勢的生物處理槽。因而，在第一生物處理槽1中有機成分 之分解率不是100%，而是95%以下，最好是在85〜90% 較佳。 第一生物處理槽1之處理水（第一生物處理水），朝 後段之第二生物處理槽2流通，在此，是依據殘存之有機 成分的氧化分解、分散性細菌的自我分解及微生物的捕食 來進行剩餘污泥的減量化。 在第二生物處理槽2中，爲了利用繁殖速度比細菌較 慢之微生物的運動與細菌的自我分解，而有必要使用把微 生物與細菌留在系統內的運轉條件及處理裝置。因而在第 二生物處理槽2中，最好使用進行污泥回送的活性污泥法 或膜式活性污泥法。又，該第二生物處理槽2也可爲二槽 以上的多段構造。膜式活性污泥法的情況，膜分離裝置爲 槽內型、槽外型任一者均可，但若爲槽外型，可以防止在 高負荷時，因捕食較慢的分散菌造成膜的堵塞。 第2發明中，藉著在該第二生物處理槽2內設置微生 物保持載體22，能提高微生物，特別是有效率地捕食分 散菌’對污泥之固液分離性與處理水質提升有貢獻的固著 性濾過捕食型微生物的槽內保持量。 亦即，第二生物處理槽2中，不只有捕食分散狀態之 菌體的濾過捕食型微生物，也有繁殖能捕食絮凝體化之污 泥的凝集體捕食型微生物。後者邊游泳，邊捕食絮凝體， -25- 201210953 所以優勢化的情況下，污泥被吃的散亂，形成微細化之絮 凝體片分散存在的污泥。在膜式活性污泥法中因該絮凝體 片而產生膜的堵塞。因而，在第2發明，該第二生物處理 槽2中，定期替換槽污泥，亦即，爲了剔出微生物或糞便 ，最好將SRT (固體物滯留時間）控制固定在60日以下 ，最好爲45日以下，更好爲10日以上45日以下的範圍 內。只是，第二生物處理槽2內之污泥濃度（MLSS)形 成2000mg/L以下時，SRT>60日也可以》在此，SRT=( 槽內污泥濃度X曝氣槽容積）+(抽除污泥濃度xl日左右 的抽除量），槽內污泥濃度（MLSS)是指浮游污泥之濃 度，不包含載體附著污泥部分。 再加上，爲了將捕食分散狀態之菌體的濾過捕食型微 生物維持在第二生物處理槽2內，而在第二生物處理槽2 內設置微生物保持載體22。亦即，此種微生物固著在污 泥絮凝體上，並被維持在系統內，但因爲污泥在一定的滯 留時間被抽除到系統外，所以必須在系統內設置供給源。 此時，若將載體作成粒狀或角型流動床，因流動的剪力， 不只無法保持在高濃度中的穩定，且有機物在流動床被完 全處理，導致污泥絮凝體的微細化，因此造成膜的閉塞。 因而，第2發明中，作爲設置在第二生物處理槽2之 載體，不是流動載體，而最好是載體的至少一部分，被固 定在第二生物處理槽2之底面、側面、上部等任一面的固 定載體。此時的載體22之形狀爲線狀、板狀、薄長方形 等任意形狀。又，載體22之材料爲天然素材、無機素材 -26- 201210953 、高分子素材等任意素材，也可使用凝膠狀物質。最好是 多孔質的胺基甲酸酯發泡體（Urethane foam )，例如作 成 100〜400cm><50〜200cmx0.5〜5cm厚度的板狀或者薄 長方形，並設置在不會接觸到曝氣空氣的位置爲佳。 第二生物處理槽.2中，爲了維持微生物需要有大量的 立足處，但載體之塡充率過多，則發生槽內的混合不足， 污泥腐敗等，因而添加之載體的塡充率在0.1〜20%左右 爲佳。 第2發明中，朝第二生物處理槽2投入的第一生物處 理水中殘存大量有機物時，其氧化分解是在後段處理槽進 行。微生物大量存在的第二生物處理槽2中，若發生藉細 菌的有機物氧化分解，作爲逃脫微生物捕食的對策，皆知 是在難以被捕食的形態下繁殖，如此一來所繁殖的細菌群 不會被微生物捕食，這些分解僅能仰賴自我消化，導致污 泥產生量減量的效果降低。因而，如前所述，有必要將第 一生物處理槽中有機物的大部分，亦即原水BOD之70% 以上，最好爲80%以上作分解，並轉換爲菌體。因而，以 依據朝向後段生物處理槽之溶解性BOD的污泥負荷來表 示，最好是以0.25〜0.50kg-BOD/kg-MLSS/d作運轉。此 處的MLSS也是指浮游污泥的濃度，不包含附著在載體的 污泥。 圖6中，來自第二生物處理槽2的處理水，被送到槽 外型之膜分離裝置5,將膜分離裝置5之透過水作爲處理 水取出，同時將濃縮水送回第二生物處理槽2之上游，再 -27- 201210953 將剩餘污泥從第二生物處理槽2直接抽除。如此使用膜分 離裝置5作爲固液分離手段的情況下，根據第2發明，因 抑制凝集體捕食型微生物之繁殖，能減輕以往活性污泥之 膜分離處理般的膜堵塞問題，使膜流出水穩定並可減少藥 品洗淨頻率，且能防止突發性的污泥分散化，使膜分離裝 置的運轉管理變得更容易》 沒有特別限制槽外型之膜分離裝置5，可以使用超濾 法（UF)膜分離裝置、微濾法（MF)膜分離裝置等。 圖7所表示之形態，是將原水的一部分，例如，將原 水5〜50%左右不經由第一生物處理槽1而直接導入至第 二生物處理槽2這一點與圖6所表示之形態不同，其他爲 相同構造。如此，藉著將原水之一部分直接導入至第二生 物處理槽2,能達到避免原水變動時（負荷降低時）第二 生物處理槽負荷不足的效果。 圖8所表示之形態，是藉著將保持有微生物之第二生 物處理槽2內的一部分污泥抽除並在無氧槽4作處理後送 回，在保持微生物的生物處理槽2內，更抑制凝集體捕食 型微生物的繁殖並使濾過捕食型微生物優先繁殖，其他， 與圖6之形態爲相同構造。 亦即，如此，設置無氧槽4,在該無氧槽4中使從第 二生物處理槽2所抽除的污泥滯留預定時間，以妨礙游泳 性微生物的繁殖，能求得生物相的穩定化。此時，第二生 物處理槽2中設有微生物保持載體22,濾過捕食型微生 物有一定數量被保持在載體22側，因而不會妨礙濾過捕 -28- 201210953 食型微生物的繁殖。而從第二生物處理槽2被抽除，且在 無氧槽4被處理的污泥被送回第二生物處理槽2。 從第二生物處理槽2抽除到無氧槽4的污泥量，以及 在無氧槽4的污泥滯留時間，是因應處理狀況再作適宜決 定，但通常污泥的抽除量相對於槽容攙爲1/30倍量/日以 上，又，在無氧槽4中的污泥滯留時間最好爲0.5小時以 上。 第2發明中，在無氧槽4,爲了妨礙微生物的繁殖， 必須將ORP定在OmV以下。爲此，最好不在無氧槽4進 行曝氣，而僅以機械作攪拌。再者，爲了促進ORP的降 低，也可讓第一生物處理水或原水的一部分流通，並依據 酸生成反應或脫氮反應來降低ORP。 此外，爲了使在無氧槽4的ORP降低（脫氮反應、 酸生成反應）能穩定進行，也可在無氧槽4添加載體。若 在無氧槽4的ORP降低，因促使游泳性微生物的活性降 低，所以能縮短在無氧槽4之第二生物處理槽污泥的滯留 時間，能讓無氧槽4小型化。添加之載體爲流動床的情況 ’形狀可爲球狀、平板狀、中空筒狀、線狀的任意形狀， 大小也在直徑0.1〜10mm左右的任意尺寸。也可使用固 定床，此時的載體22之形狀可爲線狀、板狀等任意形狀 。更者，材料可爲天然素材、無機素材、高分子素材等任 意素材，也可使用凝膠狀物質。 無氧槽4中添加載體時，其塡充率會因流動床、固定 床的形式不同或材質而有差異，但最好爲0.5〜40%。 -29- 201210953 圖6〜8是表示第2發明之實施形態的一例，但第2 發明並不限定於任一圖示。例如，第一生物處理槽、第二 生物處理槽，如前所述，可爲2段以上的多段構造，因而 ，在第2發明中，也可將生物處理槽設成3段以上。 在任一形態中，根據第2發明，藉著在第二生物處理 槽以後的生物處理槽中設置微生物保持載體，可以抑制凝 集體捕食型微生物的優勢化，並能同時達到污泥減量與提 升處理水水質，且藉著將該第二生物處理槽以後的生物處 理水在膜分離裝置作固液分離，能防止膜分離裝置的膜閉 塞，使穩定的高負荷處理成爲可能。 [實施例] 以下舉出實施例及比較例更具體說明本發明。 [第1發明的實施例及比較例] [實施例1-1] 如圖1所表示，使用連結容量爲3.6L的第一生物處 理槽1、容量爲15L的第二生物處理槽2、容量爲5L的 無氧槽4與容量爲5L的沉澱槽3的實驗裝置，來進行本 發明之有機性排廢水的處理。原水中包含 CODCr : 1000mg/L，BOD: 640mg/L 之人工基質。 各生物處理槽的處理條件如下所述。 <第一生物處理槽> -30- 201210953201210953 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to the organic nature of wastewater treatment in a wide range of wastewater discharge ranges such as wastewater discharge, sewer, food factory or pulp mill in life. Biological treatment method and device for discharging waste water, in particular, biological treatment method and device for organic waste water discharge which does not deteriorate treatment water quality and improve treatment efficiency, and can reduce excess sludge production amount [Prior Art] Organic The activated sludge method used in the case of biological treatment of wastewater discharge is widely used in sewer treatment or industrial wastewater treatment because of its advantages in good water quality and easy maintenance. However, since the volumetric load of BOD in the activated sludge process is generally 0. 5~0. It is about 8kg/m3/d and requires a wide base area. Further, 20 to 40% of the decomposed BOD is a problem in that a large amount of excess sludge is treated in order to convert into a bacterial body, that is, sludge. Regarding the high-load treatment of organic waste water, a fluidized bed method in which a carrier is added is known. When this method is used, it is possible to operate at a BOD volume load of 3 kg/m3/d or more. However, the amount of sludge produced by this method is about 30 to 50% of the decomposed BOD, which is higher than that of the conventional activated sludge process, which is a disadvantage. Japanese Patent Publication No. Sho 55-20649 discloses that the organic waste water is first treated by bacteria in the first treatment tank, and then oxidatively decomposed and contained in the organic matter discharged from the waste water and converted into the cells of the non-aggregating bacteria. In the second place -5 - 201210953, the trough reduced the excess sludge by preying on the fixed protozoa. Moreover, in this method, high-load operation can be performed, and the treatment efficiency of the active sludge method can also be improved. A variety of such wastewater treatment methods have been proposed which utilize predation of protozoa or metazoans located in the higher order of bacteria. In the method of the Japanese Patent Publication No. Sho 55-20649, a countermeasure against a problem of deterioration in processing performance due to fluctuations in raw water quality is proposed. The specific method is: "Adjust the BOD variation of the treated water from the middle of the average concentration to less than 50%", "Measure the water quality in the first treatment tank and the first treated water after a certain period of time", "First treatment" When the water quality of the water deteriorates, the sludge or the microbial preparation is added to the first treatment tank or the like. In Japanese Patent Publication No. 60-23 83 No. 2, it is proposed to allow bacteria, yeast, radiation bacteria, algae, molds, or waste water to be treated with primary sedimentation sludge or excess sludge to prey on protozoa or metazoans. Sonic processing or mechanical agitation, the floc size of these baits is made smaller than the mouth of the animal. Further, the invention of the multi-stage treatment of the fluidized bed and the activated sludge method is described in Japanese Patent No. 34 1 0699. In this method, the BOD sludge is loaded by the activated sludge process in the latter stage. The operation of lkg-BOD/kg-MLSS/d under low load makes the sludge self-oxidize, which can greatly reduce the amount of sludge pumping. Such a multi-stage activated sludge method utilizing the predation action of microorganisms has actually been utilized in the treatment of organic wastewater, and according to the discharge wastewater of the treatment object-6-201210953, the treatment efficiency can be improved, and the sludge is reduced by about 50%. The amount produced. Among the microorganisms contributing to the sludge reduction, there are filtered predation type and aggregate predation type. Among them, the agglomerated predatory type microorganisms can bite and prey on flocculating sludge, so that the aggregated predatory microorganisms predominate, and the treated water quality deteriorates. Therefore, in order to improve the treatment of water quality, it is effective to make the filtration predation dominant in microorganisms. However, in the past, no method has been proposed to control the propagation of filtered predatory microorganisms and agglutinant predatory microorganisms, and microorganisms are used for sewage treatment in wastewater treatment. When the amount of mud is reduced, depending on the operating conditions, unpredictable problems in the treatment of water quality deterioration may occur. Among the activated sludge processes, there are a membrane activated sludge method using a membrane separation device for separating solid and liquid from sludge and treated water, and a sedimentation tank type activated sludge method using a sedimentation tank. Compared with the sedimentation tank type activated sludge method, the membrane activated sludge method has the advantages of maintaining the sludge concentration and operating at a high volume load, and does not require sludge management such as a sedimentation tank, that is, good water quality can be obtained. Treatment of water. However, in the membrane type activated sludge method, the film is easily blocked by the nature of the sludge in the activated sludge tank, and the cleaning frequency of the membrane is increased. In Japanese Laid-Open Patent Publication No. Hei 9-294996, it is proposed to reduce the adhesion of sludge to the membrane by adding a carrier to the aeration tank to prevent the membrane from being blocked. However, in the method of adding a carrier to the aeration tank, there is also a possibility that Fully prevent membrane occlusion. Further, even in the case of operating the activated sludge treatment at a low load, fine SS (suspended solid) is generated in the disintegration of the sludge, and 201210953 occludes the membrane. Furthermore, depending on the water temperature, load, and SRT (solids retention time), once the microbes that supplement the floc in the activated sludge increase rapidly, the sludge will be refined, resulting in deterioration of the treated water. The operation management of the membrane separation apparatus for treating water for solid-liquid separation becomes difficult. [PRIOR ART DOCUMENT] [Patent Document 1] Japanese Laid-Open Patent Publication No. 2000-210692 (Patent Document 3) Japanese Patent Publication No. Sho 60-23832 [Patent Document 4] Japanese Patent Laid-Open No. Hei 9-294996 (Patent Document 5) [Problem to be Solved by the Invention] The invention of the first aspect provided in the present invention (hereinafter, It is called "the first invention".) In the multi-stage activated sludge method using the predation action of microorganisms, the microorganisms that filter the predatory type are dominant, and the processing efficiency is improved and the sludge is reduced, and further processing is sought. Biological treatment method and device for organic wastewater discharge with improved water quality (Question I). The invention according to the second aspect of the present invention (hereinafter referred to as "the second invention") provides a biological treatment for the organic wastewater discharged by the membrane type activated sludge method, and can greatly reduce the generated pollution. Mud volume, prevention of membrane occlusion, reduction of membrane washing frequency, and high-load operation to improve the efficiency of 201210953, and a stable biological treatment method and apparatus for treating wastewater discharge (Question II). [Means for Solving the Problem] As a result of in-depth review to solve the above-mentioned problem I, the inventors of the present invention can suppress the swimming condensate predation type by removing the sludge from the downstream biological treatment tank and passing it through the anaerobic tank. The growth of microorganisms prevents the deterioration of the treated water quality. In addition, by providing the microorganism-maintaining carrier in the biological treatment tank in the latter stage, it is possible to maintain the solid-filtered predatory microorganisms, even if the sludge of the biological treatment tank is removed and introduced. These microorganisms were also unaffected by the treatment to the anaerobic tank, and as a result, it was found that the filtered predatory microorganisms predominate. The first invention is based on this finding, and the gist thereof will be described below. The biological treatment method for organic waste water according to the first aspect of the first aspect of the invention is that the organic waste water is introduced into a first biological treatment tank provided in a plurality of aerobic biological treatment tanks of two or more stages, and the bacteria are used as a biological treatment tank. Biological treatment, wherein the first biological treatment water containing the bacteria in the dispersed state of the first biological treatment tank is circulated to the biological treatment tank after the second biological treatment tank, and the biological treatment method for biologically treated organic wastewater is The utility model is characterized in that: the biological treatment tank after the second biological treatment tank is provided with a carrier for holding microorganisms, and a part of the sludge in the biological treatment tank after the second biological treatment tank is removed, and is used in the anaerobic tank. After the treatment, the biological treatment tank after the second biological treatment tank is returned. A biological treatment method for organic waste water according to a second aspect of the present invention, in the first aspect, characterized in that, in the first aspect, the first biologically treated water is partially passed through the anaerobic tank to the second organism The treatment tank is circulated in the treatment tank. In the first aspect or the second aspect, the organic matter of the organic waste water discharge according to the third aspect of the present invention is characterized in that a part of the organic water is introduced into the oxygen-free tank, and the residual portion is introduced into the biological treatment. groove. In the biological form of the organic waste water discharge according to the fourth aspect of the present invention, in the first aspect to the third aspect, the oxygen tank holds the carrier. In the biological part of the organic waste water discharge of the fifth aspect of the present invention, in the first aspect to the fourth aspect, the biological treatment tank after the second biological treatment tank is provided with the micro organism. . The biological site of the organic waste water discharge according to the sixth aspect of the present invention, characterized in that, in any one of the first aspect to the fifth aspect, the SRT (retention time) of the biological treatment tank after the second biological treatment tank ) The sludge is removed after 60 days. The biological part of the organic waste water discharge of the seventh aspect of the present invention is characterized in that, in any one of the first to sixth aspects, the treated water of the biological treatment tank after the upper biological treatment tank is subjected to solid-liquid separation and separation. At least a portion of the sludge is returned to the second biological treatment tank biological treatment tank. According to the eighth aspect of the invention, in the biological discharge of the organic waste water, at least the following physiological method wastes the above-described first method, the above-mentioned unreasonable method, the above-described method of carrying the material, in order to describe the method of the body stagnation, and then The later device -10- 201210953 is a multi-stage aerobic biological treatment tank set up in two or more stages, and the organic waste water is introduced into the first biological treatment tank and treated by bacteria for biological treatment, and then contains The biological treatment device for circulating the first biological treatment water of the bacteria in the dispersed state of the first biological treatment tank toward the biological treatment tank after the second biological treatment tank, and for biological treatment of the organic wastewater discharge, characterized in that: The biological treatment tank after the biological treatment tank is provided with a carrier for maintaining microorganisms, and a part of the sludge in the biological treatment tank after the second biological treatment tank is removed and treated, and then returned to the second biological treatment tank. The anaerobic tank of the biological treatment tank. A biological treatment apparatus for organic waste water discharge according to a ninth aspect of the present invention, characterized in that, in the eighth aspect, at least a part of the first biological treatment water is passed through the oxygen-free tank to the second biological treatment Means of circulation of biological treatment tanks after the tank. The biological treatment apparatus for organic waste water discharge according to the first aspect of the present invention is characterized in that, in the eighth aspect or the ninth aspect, the organic wastewater discharge unit is introduced into the oxygen-free tank, and The means for introducing the residual portion of the organic waste water into the first biological treatment tank. The biological treatment apparatus for organic wastewater discharge according to the first aspect of the invention is characterized in that, in any one of the eighth aspect to the first aspect, the carrier is held in the oxygen-free tank. The biological treatment apparatus for organic waste water discharge according to the first aspect of the present invention, characterized in that, in any one of the eighth aspect to the first aspect, the biological treatment tank after the second biological treatment tank is provided There are carriers that keep microorganisms. -11 - 201210953 The organic waste water discharge device of the first aspect of the first aspect of the present invention is characterized in that, in the eighth aspect to the twelfth aspect, the biological treatment tank retention time after the second biological treatment tank is determined The sludge is removed after 60 days or less. In the organic waste water discharge of the first aspect of the first aspect of the present invention, the biological treatment tank after the second biological treatment tank is separated in any of the eighth aspect to the first aspect, and the separated sludge is further separated. At least a portion of the means for returning to the biological treatment tank after the treatment tank. In order to solve the above-mentioned problem, the inventors of the present invention have placed a groove in the multi-stage activated sludge biological treatment tank which utilizes the predation action of microorganisms to instantaneously process the organic matter, and then actively made it necessary in the subsequent biological treatment tank. In order to inhibit the proliferation of aggregates (flocs) that cause membrane occlusion; for this reason, by providing a carrier in the latter biological treatment tank, it is used to maintain the efficient predation of the dispersed bacteria, and the separation and the water quality of the treatment are contributed. The fixation is fixed; it is known from the above that the membrane-loaded activated sludge process can prevent the high-load treatment of the membrane. According to the second aspect of the invention, the organic wastewater discharged in the first aspect of the second aspect of the invention is the first biological treatment tank in which the organic waste water is introduced into the material treatment tank of two or more stages. And taking the bacteria as a biological treatment device containing the bacteria from the dispersed state of the first biological treatment tank, for the SRT (solid biological treatment package, in the form of treated water for solidification of the second organism into the review) As a result, in the middle stage, in the preceding stage, the microbial predatory microbial microorganisms produced by the dispersed bacteria are kept in the microbial occlusion of the solid-liquid predatory microorganisms of the sludge and the stabilizing principle is carried out. The biological treatment method is a multi-stage aerobic biological treatment, and then The first biological department-12-201210953 Lishui is distributed to the biological treatment tank after the second biological treatment tank, and is biologically treated, and then the organic treatment tank after the second biological treatment tank is treated as solid-liquid separation organic A biological treatment method for discharging wastewater, characterized in that: a carrier for maintaining microorganisms is provided in a biological treatment tank after the second biological treatment tank, and In the membrane separation treatment, the solid-liquid separation treatment of the biological treatment tank after the second biological treatment tank is performed. The biological treatment method for the organic wastewater discharged according to the second aspect of the present invention is characterized in that, in the first aspect, The method of biological treatment of organic waste water according to the third aspect of the present invention is characterized in that, in the first aspect or the second aspect, the second biological treatment is provided. The biological treatment method of the organic waste water according to the fourth aspect of the present invention is characterized in that the carrier in the biological treatment tank after the tank is fixed to the biological treatment tank. In the biological treatment tank of the organic waste water of the fifth aspect of the second aspect of the present invention, the biological treatment method of the organic waste water discharged from the first biological treatment tank is not passed through the first biological treatment tank. In any one of the first to fourth aspects, the SRT (solids retention time) of the biological treatment tank after the second biological treatment tank is set to be 60 days or less. The biological treatment method of the organic waste water according to the sixth aspect of the present invention, characterized in that, in any one of the first aspect to the fifth aspect, the biological treatment tank after the second biological treatment tank is removed The biological treatment device for the organic waste water discharged from the second biological treatment tank according to the seventh aspect of the present invention, after the treatment of the anaerobic tank is carried out in the anaerobic tank. Yes: It has a plurality of aerobic biological treatment tanks set up in two or more stages, and introduces the organic waste water into the first biological treatment tank, and uses the bacteria for biological treatment, and then contains the dispersed state from the first biological treatment tank. The first biological treatment water of the bacteria is circulated to the biological treatment tank after the second biological treatment tank, and is biologically treated, and the treated water of the biological treatment tank after the second biological treatment tank is used for solid-liquid separation of the organic wastewater. The biological treatment device is characterized in that: the biological treatment tank after the second biological treatment tank is provided with a carrier for holding microorganisms, and a membrane separation treatment device is provided as the second biological treatment Solid-liquid separation means for treating water in the biological treatment tank after the tank. According to a seventh aspect of the present invention, in the biological treatment apparatus for organic waste water discharge according to the eighth aspect of the invention, the membrane separation apparatus is an out-of-tank furrow separation apparatus. A biological treatment apparatus for organic wastewater discharge according to a ninth aspect of the present invention, characterized in that in the seventh aspect or the eighth aspect, the carrier provided in the biological treatment tank after the second biological treatment tank is fixed The biological treatment tank. The biological treatment apparatus for organic waste water discharge according to the tenth aspect of the present invention, characterized in that, in any one of the seventh aspect to the ninth aspect, the organic waste water discharge portion is not subjected to the first biological treatment The means for introducing the tank into the biological treatment tank after the second biological treatment tank. According to a second aspect of the present invention, in the biological treatment of the organic waste water of the first aspect of the present invention, in the seventh aspect to the first aspect, the second biological treatment tank is used. The SRT (solids retention time) of the biological treatment tank is set to be below 60 days to remove the sludge. The biological treatment apparatus for organic waste water discharge according to the first aspect of the present invention, characterized in that, in any one of the seventh aspect to the first aspect, the biological treatment tank after the second biological treatment tank is provided After a part of the sludge is removed and treated, it is returned to the anaerobic tank of the biological treatment tank after the second biological treatment tank. [Effect of the Invention] In the multi-stage activated sludge method using the predation action of microorganisms, the microorganism holding carrier for holding microorganisms is provided in the biological treatment tank, and the sludge in the biological treatment tank is removed and The oxygen tank is returned after being treated, and the growth of the treated water can be improved by suppressing the propagation of the aggregated predatory microorganisms and preferentially multiplying the predatory microorganisms in the biological treatment tank holding the microorganisms. According to the second aspect of the invention, in the multi-stage activated sludge method using the predation action of microorganisms, by disposing a microorganism-maintaining carrier for holding microorganisms in the biological treatment tank, the dispersed bacteria can be efficiently retained in the biological treatment tank, and a fixed-filtered predatory microorganism that contributes to the solid-liquid separation property of the sludge and the water quality of the treated water, thereby preventing the membrane of the membrane separation device that treats the biological treatment water of the biological treatment tank as a membrane separation device, and It can reduce the washing frequency of the drug in the film. Therefore, according to the first invention and the second invention, the organic wastewater of -15 - 201210953 can be effectively treated biologically, and the following effects can be obtained. 1) The sludge generated during the wastewater treatment is greatly reduced 2) The treatment efficiency is improved according to the high-load operation 3) The stable treatment water quality is maintained. [Embodiment] The organic wastewater treatment method of the present invention will be described in detail below with reference to the drawings. An embodiment of the device. [First Invention] Figs. 1 to 5 are system diagrams showing an embodiment of a method and an apparatus for producing organic waste water according to a first aspect of the invention. In Figs. 1 to 5, 1 is a first biological treatment tank, 2 is a second treatment tank '3 is a sedimentation tank, 4 is an oxygen-free tank, 5 is a membrane separation device 21 is a gas diffusion tube, and 22 is a microbial retention carrier, 41 The stirring hand is the carrier; the members expressing the same function in FIGS. 1 to 5 are in the same manner as in the form of FIG. 1, the raw water (organic waste water) is guided to the biological treatment tank 1, and the dispersing bacteria (non-aggregating property) Bacteria) Decompose more than 70% of the organic component (soluble BOD), preferably above 90%. The pH of the first biological treatment tank 1 is preferably 8 or less. However, when the raw water contains more oil, it may be 8 or more. Further, the flow toward the first biological treatment tank 1 is usually a transient biological treatment organism at the >11' section, 42 indicates the first, and 80% of the oxidation is performed by the pH 6 method, and -16- 201210953 The BOD volume load of the first biological treatment tank 1 is lkg/m3/d or more, for example, 1 to 20 kg/m3/d, and the HRT (raw water retention time) is 24 hours or less, preferably 8 hours or less, for example, 〇· 5 to 8 hours 'the treatment water with the advantage of dispersing bacteria can be obtained, and the wastewater with lower BOD concentration can be treated with high load by shortening HRT'. In the first biological treatment tank 1, the first biological treatment tank 1 is formed into a multi-stage structure of two or more tanks by returning a part of the sludge from the subsequent biological treatment tank, and a carrier is added to make the B0D load capacity 5 kg. High-load processing of /m3/d or more is possible. When the carrier is added to the first biological treatment tank 1, the shape ' of the carrier' may be spherical, flat, hollow, linear, plate-like, or the like, and the size is also 0. 1~ can be free. Further, the material of the carrier may be any material such as a natural material, an inorganic material, or a polymer material, or a gel-like substance may be used. Further, when the charge rate of the carrier added to the first biological treatment tank 1 is high, no scattered bacteria are generated, the bacteria adhere to the carrier, or the filamentous bacteria multiply. Therefore, the charge rate of the carrier added to the first biological treatment tank 1 is set to 10% or less, preferably 5% or less, and the dispersed bacteria which are easy to prey can be produced without affecting the concentration fluctuation. Further, the dissolved oxygen (DO) concentration of the first biological treatment tank 1 is set to be 1 mg/L or less, preferably 0. Below 5 mg/L, the growth of filamentous bacteria can also be inhibited. Furthermore, when the first biological treatment tank 1 completely decomposes the dissolved organic matter, no floc is formed in the second biological treatment tank 2, and the nutrients required for microbial growth are also insufficient, and only the compaction is formed. The low sludge dominates the biological treatment tank of -17-201210953. Therefore, the decomposition rate of the organic component in the first biological treatment tank 1 is not 100%, but is 95% or less, preferably 85 to 90%. The treated water (first biologically treated water) of the first biological treatment tank 1 flows toward the second biological treatment tank 2 in the latter stage, and here, depending on the oxidative decomposition of the remaining organic components, the self-decomposition of the dispersed bacteria, and the predation of microorganisms. The reduction of excess sludge is carried out. In the second biological treatment tank 2, since the movement of the microorganisms which are slower than the bacteria and the self-decomposition of the bacteria are utilized, it is necessary to use operating conditions and treatment means capable of leaving the microorganisms and bacteria in the system. Therefore, in the second biological treatment tank 2, an activated sludge method or a membrane separation type activated sludge method for carrying out sludge recovery is preferably used. Further, the second biological treatment tank 2 may have a multi-stage structure of two or more grooves. In the first aspect of the invention, by providing the microorganism holding carrier 22 in the second biological treatment tank 2, the amount of retention of the microorganisms in the tank can be increased. The shape of the carrier 22 provided in the second biological treatment tank 2 may be any shape such as a spherical shape, a flat shape, a hollow cylindrical shape or a linear shape, and the size is a diameter of 0. 1~l〇mm can be around. It is also possible to use a fixed bed, in which case the shape of the carrier 22 is any shape such as a linear shape or a plate shape. Further, the material of the carrier 22 is any material such as a natural material, an inorganic material, or a polymer material, and a gel-like substance may be used. In the second biological treatment tank 2, a large number of footholds for maintaining microorganisms must be added. The charge rate of the carrier may vary depending on the form of the fluid bed, the fixed bed, or the material, but is preferably 0. 5 to 40%. -18- 201210953 In addition, as described above, in the second biological treatment tank 2, not only the filtered predatory microorganisms which prey on the dispersed state, but also the aggregated predatory microorganism capable of preying on the flocculating sludge . The latter swims while trapping floc, so in the case of predominance, the sludge is bitten and scattered, forming a finely dispersed floc sheet dispersed sludge. In the activated sludge of the sedimentation tank type, the membrane clogging occurs in the membrane type activated sludge because the floc sheet increases the concentration of the treated water s S . Therefore, in the first aspect of the invention, the anaerobic tank 4 is provided, and the sludge which has been removed from the second biological treatment tank 2 is retained in the anaerobic tank 4 for a predetermined period of time to prevent the growth of the swimming microorganisms. Stabilization of the biological phase. At this time, the second biological treatment tank 2 is provided with the microorganism holding carrier 22, and the filtered predatory microorganism is fixed on the side of the carrier 22, and is hardly removed from the second biological treatment tank 2 and flows into the anaerobic tank 4, thereby It does not hinder the propagation of filtered predatory microorganisms. The sludge removed from the second biological treatment tank 2, and the sludge treated in the anaerobic tank 4 is sent back to the second biological treatment tank 2, and is withdrawn from the second biological treatment tank 2 to the anaerobic tank 4. The amount of sludge and the residence time of the sludge in the anaerobic tank 4 are appropriately determined depending on the treatment conditions, but usually the amount of sludge is 1/30 times/day or more relative to the tank capacity, and The sludge residence time in the anaerobic tank 4 is preferably 0. More than 5 hours. In the first invention, in the anaerobic tank 4, in order to prevent the growth of microorganisms, it is necessary to set the ORP to be equal to or less than OmV. For this reason, it is preferable not to aerate the anaerobic tank 4, but only mechanically. Furthermore, in order to promote the reduction of ORP, the first biological treatment water or raw water can be circulated, and the ORP can be lowered according to the acid formation reaction -19-201210953 or the denitrification reaction. In addition, in order to stabilize the ORP in the anaerobic tank 4 (the denitrification reaction and the acid formation reaction), the carrier may be added to the anaerobic tank 4, and if the 〇RP in the anaerobic tank 4 is lowered, the swimming property is promoted. Since the activity of the microorganisms is lowered, the residence time of the sludge in the second biological treatment tank of the anaerobic tank 4 can be shortened, and the anaerobic tank 4 can be miniaturized. When the carrier to be added is a fluidized bed, the shape may be spherical, flat, hollow, or linear, and the diameter is also 0. Any size from 1 to 10 mm. A fixed bed can also be used, and the shape of the carrier 22 at this time is any shape such as a line shape or a plate shape. Further, the material may be any material such as a natural material, an inorganic material, or a polymer material, or a gel-like substance may be used. When the carrier is added to the anaerobic tank 4, the charge rate may vary depending on the form of the fluidized bed or the fixed bed or the material, but it is preferably 0. 5 to 40%. Furthermore, in the second biological treatment tank 2, the tank sludge is periodically replaced, that is, the SRT (solids retention time) is fixed to 60 days or less, preferably 45 days or less, in order to remove microorganisms or feces. It is better to be in the range of 10 days or more and 45 days or less. However, when the sludge concentration (MLSS) in the second biological treatment tank 2 is 2000 mg/L or less, even SRT > 60 days may be used. Here, SRT = (sludge concentration in the tank X aeration tank volume) + (extraction of the sludge concentration XI day), and the sludge concentration in the tank (MLS S ) refers to the concentration of the suspended sludge Does not contain the carrier-attached sludge portion. Further, in the first aspect of the invention, when a large amount of organic matter remains in the first biologically treated water supplied to the second biological treatment tank 2, the oxidative decomposition is carried out in the later stage at -20 - 201210953. In the second biological treatment tank 2 in which a large amount of microorganisms are present, if the organic matter of the bacteria is oxidatively decomposed, as a countermeasure against the microbial predation, it is known that it is propagated in a form that is difficult to be preyed, and thus the bacterial population that is propagated is not It will be preyed by microorganisms, and these decompositions can only rely on self-digestion, resulting in a decrease in the amount of sludge production. Therefore, as described above, it is necessary to decompose most of the organic matter in the first biological treatment tank, that is, 70% or more, preferably 80% or more of the raw water BOD, and convert it into a bacterial body. Therefore, if it is expressed by the sludge load according to the solubility BOD of the biological treatment tank to the rear stage, it is preferably 0. 25~0. 50kg-BOD/kg-MLSS/d for operation. The MLSS here also refers to the concentration of the floating sludge, and does not include the sludge attached to the carrier. In Fig. 1, the treated water from the second biological treatment tank 2 is then separated into sludge and treated water by solid-liquid separation in the sedimentation tank 3, and the separated water is taken out as treated water, and a part of the separated sludge is used as return sludge. It is sent back to the second biological treatment tank 2, and the remaining portion is discharged as the excess sludge outside the system. Further, a membrane separation device may be used instead of the precipitation tank 3 as a solid-liquid separation means. Conventionally, in the membrane separation treatment of activated sludge, it is a problem to reduce the effluent water due to clogging of the membrane, and the pharmaceutical washing is a problem. However, according to the present invention, it is possible to prevent the sudden sludge from being dispersed and to operate the membrane separation device. Management is easy. The form shown in Fig. 2 is to introduce one part of the treated water from the first biological treatment tank of the first biological treatment tank 1, for example, about 1 to about 20% into the anaerobic tank 4, and then introduce the residual portion to the second portion. The biological treatment tank 2 differs from the configuration shown in Fig. 1 in that it is the same structure. As described above, -21 - 201210953 Thus, by introducing one of the first biological treatment tank water into the anaerobic tank 4, the ORP of the anaerobic tank 4 is lowered, and the microbial growth can be prevented in the anaerobic tank 4. Effect. In the embodiment shown in Fig. 3, a part of the raw water is directly introduced into the anaerobic tank 4, for example, about 1 〇 to 20%, and the remaining portion is introduced into the first biological treatment tank 1, which is different from the form shown in Fig. 1. The other is the same structure. As described above, by introducing a part of the raw water into the anaerobic tank 4, the ORP of the anaerobic tank 4 is lowered, and the effect of preventing microbial growth in the anaerobic tank 4 can be enhanced. Fig. 4 shows a form in which the membrane separation device 5 is used instead of the precipitation tank 3, and the permeated water of the membrane separation device 5 is taken out as treated water, and the concentrated water is returned to the second biological treatment tank 2, and the remaining sludge is removed from the first The point where the two biological treatment tanks 2 are directly removed is different from the form shown in Fig. 1, and the others are of the same configuration. As described above, when the membrane separation device 5 is used as the solid-liquid separation means, according to the first aspect of the invention, the growth of the aggregated predatory microorganisms can be suppressed, and the clogging of the membrane in the membrane separation treatment of the conventional activated sludge can be reduced. The effluent water is stable and can reduce the frequency of drug washing. Fig. 5 shows a form in which the carrier 42 is added to the anaerobic tank 4, which is different from the embodiment shown in Fig. 1, and the other structures are the same. As described above, by adding a carrier to the anaerobic tank 4, the ORP of the anaerobic tank 4 is lowered, and the effect of preventing microbial growth in the anaerobic tank 4 can be enhanced. Figs. 1 to 5 show an example of an embodiment of the first invention, and the first invention is not limited to those shown in any of the drawings. For example, the first biological treatment tank and the second biological treatment tank may have two or more stages of the-22-201210953 structure as described above. Therefore, in the first invention, the biological treatment tank may be set to three stages. the above. Further, as the solid-liquid separation means, a membrane separation device or an up-and-down separation tank may be used in addition to the precipitation tank, and the biological treatment tank in the latter stage may be used as a membrane-impregnated biological treatment tank having both a biological treatment tank and a solid-liquid separation means. , Membrane separation aerobic treatment is also possible. In either aspect, according to the first invention, the microorganism holding carrier is provided in the biological treatment tank after the second biological treatment tank, and the biological treatment tank sludge after the second biological treatment tank is treated in the oxygen-free tank. It can inhibit the dominance of agglomerated predatory microorganisms and at the same time achieve sludge reduction and treatment water quality improvement. [Second Invention] Figs. 6 to 8 are system diagrams showing an embodiment of a biological treatment method and apparatus for organic wastewater discharge according to a second aspect of the invention. In Figures 6-8, 1 is the first biological treatment tank, 2 is the second biological treatment tank, 4 is the oxygen-free tank, 5 is the membrane separation device, 11, 21 is the diffusing pipe, 22 is the microorganism holding carrier, 41 is Stirring means; members of the same function in FIGS. 6 to 8 are denoted by the same symbols. In the form of Fig. ', 'raw water (organic waste water) is introduced into the first biological treatment tank 1 'by dispersing bacteria (non-aggregating bacteria), oxidizing and decomposing organic components (soluble BOD) by 70% or more, most Good oxidative decomposition of more than 80%, 90 ° /. The above is better. The pH of the first biological treatment tank i is ό or more, and is preferably 8 or less. However, the raw water contains too much oil. -23- 201210953 The pH 値 can also be 8 or more. Further, the flow to the first biological treatment tank 1 is generally a transient method, and the BOD volume load of the first biological treatment tank 1 is lkg/m3/d or more, for example, 1 to 20 kg/m3/d, and HRT (raw water retention time) ) is 24 hours or less, preferably 8 hours or less, for example, at 0. In the case of 5 to 8 hours, treated water in which dispersible bacteria predominate is obtained, and by reducing HRT, waste water having a lower B OD concentration can be treated at a high load. In the first biological treatment tank 1, a portion of the sludge from the downstream biological treatment tank is returned, and the first biological treatment tank 1 is formed into a multi-stage structure of two or more tanks, and a carrier is added to make the BOD volume load 5 kg/m3. High-load processing above /d is possible. When the carrier is added to the first biological treatment tank 1, the shape of the carrier is a spherical shape, a flat shape, a hollow cylindrical shape, a linear shape, a plate shape, or the like, and the size is a diameter of 0. Any size from 1 to 10 mm. Further, the material of the carrier may be any material such as a natural material, an inorganic material or a polymer material, or a gel-like substance may be used. Further, when the charge rate of the carrier added to the first biological treatment tank 1 is high, no scattered bacteria are generated, bacteria adhere to the carrier, or filamentous bacteria multiply. Therefore, by setting the charge rate of the carrier added to the first biological treatment tank 1 to 20% or less, preferably 1% or less, the concentration change is not affected, and a dispersed bacteria which is easier to prey can be produced. Further, the first biological treatment tank 1 has a dissolved oxygen (DO) concentration of 1 mg/L or less, preferably 0. Below 5 mg/L, the growth of filamentous bacteria can also be inhibited. In addition, when the dissolved organic matter-24-201210953 is completely decomposed in the first biological treatment tank 1, no flocculation occurs in the second biological treatment tank 2, and the nutrients used by the microorganisms for reproduction are also insufficient, and only the pressure is formed. A biological treatment tank dominated by sludge with a lower density. Therefore, the decomposition rate of the organic component in the first biological treatment tank 1 is not 100%, but is 95% or less, preferably 85 to 90%. The treated water (first biologically treated water) of the first biological treatment tank 1 flows toward the second biological treatment tank 2 in the latter stage, and is based on the oxidative decomposition of the remaining organic components, the self-decomposition of the dispersed bacteria, and the microorganisms. Predation to reduce the excess sludge. In the second biological treatment tank 2, in order to utilize the movement of microorganisms which are slower than bacteria and the self-decomposition of bacteria, it is necessary to use operating conditions and treatment means for leaving microorganisms and bacteria in the system. Therefore, in the second biological treatment tank 2, an activated sludge method or a membrane activated sludge method for carrying out sludge recovery is preferably used. Further, the second biological treatment tank 2 may have a multi-stage structure of two or more grooves. In the case of the membrane type activated sludge method, the membrane separation apparatus may be either a tank type or a tank type. However, if it is a tank type, it is possible to prevent the film from being caused by a slow-distributing dispersed bacteria at a high load. Blocked. In the second aspect of the invention, by providing the microorganism holding carrier 22 in the second biological treatment tank 2, it is possible to improve microorganisms, and in particular, to efficiently disperse the dispersed bacteria, which contributes to the solid-liquid separation property of the sludge and the improvement of the treated water quality. The amount of retention in the tank of the fixed-filtered predatory microorganism. That is, in the second biological treatment tank 2, not only the predatory microorganisms which prey on the cells in the dispersed state but also the predatory microorganisms which can prey on the flocculated sludge are also propagated. The latter swims while preying on floc, -25- 201210953. In the case of the advantage, the sludge is scattered and the sludge is dispersed in the finely divided floc sheet. In the membrane activated sludge process, clogging of the membrane occurs due to the flocculated sheet. Therefore, in the second invention, in the second biological treatment tank 2, the tank sludge is periodically replaced, that is, in order to remove microorganisms or feces, it is preferable to fix the SRT (solid matter retention time) to 60 days or less. It is preferably 45 days or less, and more preferably 10 days or more and 45 days or less. However, when the sludge concentration (MLSS) in the second biological treatment tank 2 is 2000 mg/L or less, SRT>60 days can also be used here, SRT = (sludge concentration in the tank X aeration tank volume) + (pumping) In addition to the sludge concentration x1 day, the sludge concentration in the tank (MLSS) refers to the concentration of the suspended sludge, and does not include the carrier-attached sludge portion. Further, in order to maintain the filtered predatory microorganism of the predator-preserved cells in the second biological treatment tank 2, the microorganism holding vessel 22 is provided in the second biological treatment tank 2. That is, such microorganisms are fixed on the sludge flocs and are maintained in the system, but since the sludge is pumped out of the system for a certain residence time, it is necessary to provide a supply source in the system. At this time, if the carrier is made into a granular or angular flow bed, the flow shearing force is not only unable to maintain stability in a high concentration, but the organic matter is completely treated in the fluidized bed, resulting in micronization of the sludge floc. Causes occlusion of the membrane. Therefore, in the second aspect of the invention, the carrier provided in the second biological treatment tank 2 is not a flow carrier, but preferably at least a part of the carrier is fixed to the bottom surface, the side surface, the upper portion, and the like of the second biological treatment tank 2. Fixed carrier. The shape of the carrier 22 at this time is any shape such as a line shape, a plate shape, or a thin rectangular shape. Further, the material of the carrier 22 is a natural material, an inorganic material -26-201210953, a polymer material, or the like, and a gel-like substance may also be used. Preferably, it is a porous urethane foam, for example, 100 to 400 cm><50 to 200 cm x 0.5 to 5 cm thick plate shape or thin rectangular shape, and it is preferably placed at a position where it does not come into contact with the aeration air. In the second biological treatment tank, in order to maintain the microorganisms, a large amount of footing is required, but if the carrier has a high filling rate, the mixing in the tank is insufficient, the sludge is spoiled, and the like, and thus the charging rate of the added carrier is 0.1. ~20% or so is better. In the second aspect of the invention, when a large amount of organic matter remains in the first biological treatment water supplied to the second biological treatment tank 2, the oxidative decomposition proceeds in the subsequent treatment tank. In the second biological treatment tank 2 in which a large amount of microorganisms are present, if the organic matter of the bacteria is oxidized and decomposed, as a countermeasure against the microbial predation, it is known that it is propagated in a form that is difficult to be preyed, and thus the bacterial population that is propagated does not Preyed by microorganisms, these decompositions can only rely on self-digestion, resulting in a reduced effect of sludge production. Therefore, as described above, it is necessary to decompose most of the organic matter in the first biological treatment tank, i.e., 70% or more of the raw water BOD, preferably 80% or more, and convert it into a bacterial body. Therefore, it is preferable to operate at a flow rate of 0.25 to 0.50 kg-BOD/kg-MLSS/d in accordance with the sludge load toward the soluble BOD of the biological treatment tank in the latter stage. The MLSS here also refers to the concentration of suspended sludge and does not contain sludge attached to the carrier. In Fig. 6, the treated water from the second biological treatment tank 2 is sent to the membrane separation device 5 of the tank type, and the permeated water of the membrane separation device 5 is taken out as treated water, and the concentrated water is returned to the second biological treatment. Upstream of tank 2, again -27-201210953, the excess sludge is directly withdrawn from the second biological treatment tank 2. When the membrane separation apparatus 5 is used as the solid-liquid separation means as described above, according to the second aspect of the invention, the growth of the aggregated predatory microorganisms can be suppressed, and the membrane clogging problem such as the membrane separation treatment of the conventional activated sludge can be reduced, and the membrane can be discharged from the water. It is stable and can reduce the frequency of drug washing, and can prevent sudden sludge decentralization and make the operation and management of the membrane separation device easier. There is no special restriction on the membrane separation device 5 of the tank type, and ultrafiltration can be used. (UF) membrane separation device, microfiltration (MF) membrane separation device, and the like. In the embodiment shown in Fig. 7, a part of the raw water, for example, about 5 to 50% of the raw water is directly introduced into the second biological treatment tank 2 without passing through the first biological treatment tank 1, and is different from the form shown in Fig. 6. Others are of the same construction. By directly introducing one of the raw water directly into the second biological treatment tank 2, it is possible to avoid the effect of insufficient load on the second biological treatment tank when the raw water is changed (when the load is lowered). The form shown in Fig. 8 is obtained by extracting a part of the sludge in the second biological treatment tank 2 in which the microorganisms are held, and returning them in the anaerobic tank 4, and returning them in the biological treatment tank 2 for holding the microorganisms. Further, the aggregation of the predatory microorganisms was inhibited and the predatory microorganisms were preferentially propagated, and the other structures were the same as those of Fig. 6. In other words, the anaerobic tank 4 is provided, and the sludge extracted from the second biological treatment tank 2 is retained in the anaerobic tank 4 for a predetermined period of time to hinder the growth of the swimming microorganisms, and the biological phase can be obtained. Stabilized. At this time, the second biological treatment tank 2 is provided with the microorganism holding carrier 22, and a certain amount of the filtered predatory microorganisms is held on the side of the carrier 22, so that the propagation of the filter-type microorganisms of the -28-201210953 is not hindered. The sludge removed from the second biological treatment tank 2 and treated in the anaerobic tank 4 is sent back to the second biological treatment tank 2. The amount of sludge that is removed from the second biological treatment tank 2 to the anaerobic tank 4 and the sludge retention time in the anaerobic tank 4 are appropriately determined depending on the treatment conditions, but usually the amount of sludge to be withdrawn is relative to The tank volume is 1/30 times/day or more, and the sludge residence time in the anaerobic tank 4 is preferably 0.5 hours or more. In the second aspect of the invention, in the anaerobic tank 4, in order to prevent the growth of microorganisms, it is necessary to set the ORP to be equal to or less than OmV. For this reason, it is preferable not to aerate the anaerobic tank 4, but only mechanically. Further, in order to promote the reduction of the ORP, a part of the first biological treatment water or the raw water may be circulated, and the ORP may be lowered according to the acid formation reaction or the denitrification reaction. Further, in order to stabilize the ORP (the denitrification reaction or the acid formation reaction) in the anaerobic tank 4, the carrier may be added to the anaerobic tank 4. When the ORP of the anaerobic tank 4 is lowered, the activity of the swimming microorganisms is lowered, so that the residence time of the sludge in the second biological treatment tank of the anaerobic tank 4 can be shortened, and the anaerobic tank 4 can be miniaturized. When the carrier to be added is a fluidized bed, the shape may be any shape of a spherical shape, a flat shape, a hollow cylindrical shape, or a linear shape, and the size may be any size of about 0.1 to 10 mm in diameter. It is also possible to use a fixed bed, and the shape of the carrier 22 at this time may be any shape such as a line shape or a plate shape. Further, the material may be any material such as natural material, inorganic material, or polymer material, or a gel-like substance may be used. When the carrier is added to the anaerobic tank 4, the charge rate may vary depending on the form of the fluidized bed or the fixed bed or the material, but it is preferably 0.5 to 40%. -29-201210953 FIGS. 6 to 8 show an example of an embodiment of the second invention, but the second invention is not limited to any one of the drawings. For example, the first biological treatment tank and the second biological treatment tank may have a multi-stage structure of two or more stages as described above. Therefore, in the second aspect of the invention, the biological treatment tank may be provided in three or more stages. In any aspect, according to the second aspect of the invention, by providing the microorganism holding carrier in the biological treatment tank after the second biological treatment tank, the advantage of the aggregate predatory microorganism can be suppressed, and the sludge reduction and lifting treatment can be simultaneously achieved. By the water quality, the biological treatment water after the second biological treatment tank is subjected to solid-liquid separation in the membrane separation device, whereby the membrane of the membrane separation device can be prevented from being closed, and stable high-load treatment can be performed. [Examples] Hereinafter, the present invention will be more specifically described by way of Examples and Comparative Examples. [Examples and Comparative Examples of First Invention] [Example 1-1] As shown in Fig. 1, a first biological treatment tank having a connection capacity of 3.6 L and a second biological treatment tank having a capacity of 15 L were used. The treatment of the organic waste water of the present invention was carried out by an experimental apparatus of a 5 L anaerobic tank 4 and a 5 L sedimentation tank 3. The raw water contains an artificial matrix of CODCr: 1000 mg/L and BOD: 640 mg/L. The processing conditions of each biological treatment tank are as follows. <First Biological Treatment Tank> -30- 201210953
DO : 0 · 5 mg/L BOD 容積負荷：3.85kg-BOD/m3/d HRT : 4小時 pH 値：7.0 <第二生物處理槽>DO : 0 · 5 mg/L BOD Volumetric load: 3.85 kg-BOD/m3/d HRT: 4 hours pH 7.0: 7.0 <Second biological treatment tank>
DO : 4mg/L 載體塡充率：2% HRT ： 1 7小時 SRT : 30 臼 pH 値：7.0 <無氧槽>DO : 4 mg/L carrier charge rate: 2% HRT : 1 7 hours SRT : 30 臼 pH 値: 7.0 < anaerobic tank >
ORP ： -1 OOmV HRT ( =SRT ) : 12 小時 再者’使用板狀之聚氨基甲酸酯發泡體（ Polyurethane foam)作爲第二生物處理槽2之載體12。 又，裝置整體的BOD容積負荷爲0.75kg-BOD/m3/d， 裝置整體的HRT爲21小時。 其結果，第二生物處理槽2內之污泥絮凝體，在載體 上的固著性濾過捕食型微生物（吊鐘蟲Vorticella、蛭形 目 Bdelloida)優勢化，污泥轉換率爲 〇.lkg-MLSS/kg-CODCr。處理水（沉澱槽4之固液分離水）7_K質，SS濃度 -31 - 201210953 爲未滿10mg/L ’溶解性CODCr濃度爲未滿30mg/L，試驗 期間，經常維持良好狀態。 [實施例1-2] 使用UF膜取代沉澱槽作爲膜分離裝置作成圖4所表 示的實驗裝置’以外與實施例1-1在相同的條件下進行處 理。原水的水質’第一、第二生物處理槽及無氧槽的處理 條件’以及整體BOD容積負荷及HRT與實施例1_1相同 〇 其結果，第二生物處理槽內之污泥絮凝體，在載體上 固著性濾過捕食型微.生物（吊鐘蟲 Vorticella、蛭形目 Bdelloida )佔優勢，污泥轉換率爲 0.075kg-MLSS/kg-CODcr。 處理水（膜分離裝置之透過水）水質，溶解性CODCr 濃度爲未滿20mg/L，實驗期間，經常維持良好狀態。又 ，膜間差壓幾乎沒有上升，即使1個月以上不進行藥品洗 淨，也可以維持穩定的流出水。 [比較例1-1] 省略無氧槽，且沒有在第二生物處理槽設置載體此點 以外與實施例I-1在相同條件下進行處理。 原水的水質，第一、第二生物處理槽的處理條件以及 整體BOD容積負荷及HRT與實施例1-1相同》 其結果，污泥轉換率爲〇.13kg-MLSS/kg-CODCr。然 -32- 201210953 而，隔1個月，凝集體捕食型微生物（Euchlanis)優勢化 ，期間，處理水SS濃度爲80mg/L，溶解性CODCr上升到 1 5 Omg/L 〇 [比較例1-2] 省略無氧槽，且沒有在第二生物處理槽設置載體此點 以外與實施例1-2在相同條件下進行·處理。 原水的水質，第一、第二生物處理槽的處理條件以及 整體BOD容積負荷及HRT與實施例1-1相同。 其結果，污泥轉換率爲0.12kg-MLSS/kg-CODCr。.然 而，隔1個月，凝集體捕食型微生物（Euchlanis)優勢化 ，期間，膜間差壓頻繁地上升，經過整個試驗期間，必須 每2週作1次膜的藥品洗淨。 [第2發明的實施例及比較例] [實施例Π-1] 如圖6所表示，使用連結容量爲3.6L的第一生物處 理槽1、容量爲15L的第二生物處理槽2、UF膜分離裝置 5的實驗裝置，來進行本發明之有機性排廢水的處理。原 水包含 CODCr: 1 000mg/L，BOD: 640mg/L 之人工基質。 各生物處理槽的處理條件如下所述。 <第一生物處理槽>ORP: -1 OOmV HRT (=SRT): 12 hours Further, a plate-shaped polyurethane foam was used as the carrier 12 of the second biological treatment tank 2. Further, the BOD volume load of the entire apparatus was 0.75 kg-BOD/m3/d, and the HRT of the entire apparatus was 21 hours. As a result, the sludge floc in the second biological treatment tank 2 is dominant in the fixation of the predatory microorganisms (Vorticella, Bdelloida) on the carrier, and the sludge conversion rate is 〇.lkg- MLSS/kg-CODCr. The treated water (solid-liquid separation water of the sedimentation tank 4) was 7_K, and the SS concentration -31 - 201210953 was less than 10 mg/L. The dissolved CODCr concentration was less than 30 mg/L, and the test period was maintained in a good state. [Example 1-2] The treatment was carried out under the same conditions as in Example 1-1 except that the precipitation tank was replaced with a UF membrane as a membrane separation apparatus to prepare an experimental apparatus shown in Fig. 4 . The water quality of the raw water 'the treatment conditions of the first and second biological treatment tanks and the anaerobic tank' and the overall BOD volume load and HRT are the same as in the example 1_1. As a result, the sludge floc in the second biological treatment tank is in the carrier. The upper fixation-preserved micro-organism (Vorticella, Bdelloida) dominated, and the sludge conversion rate was 0.075 kg-MLSS/kg-CODcr. The water quality of the treated water (permeate water of the membrane separation device) was such that the dissolved CODCr concentration was less than 20 mg/L, and was maintained in a good state during the experiment. Further, the differential pressure between the membranes hardly rises, and even if the drug is not washed for one month or more, stable effluent water can be maintained. [Comparative Example 1-1] The treatment was carried out under the same conditions as in Example I-1 except that the anaerobic tank was omitted and the carrier was not provided in the second biological treatment tank. The water quality of the raw water, the treatment conditions of the first and second biological treatment tanks, and the overall BOD volumetric load and HRT were the same as in Example 1-1. As a result, the sludge conversion rate was 1313 kg-MLSS/kg-CODCr. Ran-32- 201210953 And, every other month, the agglutinating predatory microorganism (Euchlanis) was dominant, during which the treated water SS concentration was 80 mg/L and the dissolved CODCr rose to 150 Omg/L 〇 [Comparative Example 1 2] The anaerobic tank was omitted, and the treatment was carried out under the same conditions as in Example 1-2 except that the carrier was not provided in the second biological treatment tank. The water quality of the raw water, the processing conditions of the first and second biological treatment tanks, and the overall BOD volume load and HRT were the same as in Example 1-1. As a result, the sludge conversion rate was 0.12 kg-MLSS/kg-CODCr. However, every other month, the agglutinating predatory microorganism (Euchlanis) is dominant, and during this period, the inter-membrane differential pressure frequently rises, and it is necessary to wash the membrane once every two weeks during the entire test period. [Embodiment and Comparative Example of Second Invention] [Example Π-1] As shown in Fig. 6, a first biological treatment tank 1 having a connection capacity of 3.6 L and a second biological treatment tank 2 having a capacity of 15 L were used. The experimental apparatus of the membrane separation apparatus 5 performs the treatment of the organic waste water of the present invention. The raw water contains CODCr: 1 000 mg / L, BOD: 640 mg / L artificial substrate. The processing conditions of each biological treatment tank are as follows. <First Biological Treatment Tank>
DO : 〇.5mg/L -33- 201210953 BOD 容積負荷：3.85kg-BOD/m3/d HRT : 4小時 pH 値：7.0 <第二生物處理槽> DO : 4mg/L 載體塡充率：2% HRT ： 1 7小時 SRT : 30 日 pH 値：7.0 再者，使用板狀之聚氨基 1 5mmx300mmx50mm/l 片）作爲第二生 12，設在相對於槽中央之垂直面，與截 置上，並將底部與左右固定在槽壁面上 又，裝置整體之BOD容積負荷爲 裝置整體的HRT爲21小時。 其結果，第二生物處理槽2內之$ 上之固著性濾過捕食型微生物（吊鐘I 目 Bdelloida)優勢化，而污泥轉換率 C Ο D c r。 處理水（膜分離裝置5之透過 CODCr濃度爲未滿20mg/L，實驗期間 態。 甲酸酯發泡體（ 物處理槽2之載體 t氣管2 1對稱的位 〇 0.75kg-BOD/m3/d， Γ泥絮凝體，在載體 畜 Vorticella、輕形 爲 0.1 kg-MLSS/kg- 水）水質，溶解性 ，經常維持良好狀 -34- 201210953 又，膜分離裝置5的膜間差壓幾乎沒有上升，即使1 個月以上不進行藥品洗淨，也可以維持穩定的流出水。 [比較例II-1] 省略第一生物處理槽，將第二生物處理槽之容量定爲 1 8.6L，且沒有在第二生物處理槽設置載體此點以外與實 施例II-1在相同條件下進行處理。 原水的水質、第二生物處理槽之DO及pH値，整體 BOD容積負荷及HRT與實施例II-1相同。 其結果，污泥轉換率爲〇.20kg‘MLSS/kg-CODCr。然 而，隔1個月，凝集體捕食型微生物（Euchlanis)優勢化 ，這期間，因膜間差壓的上升，必須每2週作1次膜的藥 品洗淨。除此之外，處理水質也惡化，溶解性CODCr濃 度上升到70mg/L以上》 [實施例Π-2] 如圖8所表示，設置容量爲5L的無氧槽4,並抽除 第二生物處理槽2內之污泥並在無氧槽4作處理後，再送 回第二生物處理槽2,其他與實施例II-1在相同條件下進 行處理。原水的水質、第一及第二生物處理槽之處理條件 ，以及整體BOD容積負荷及HRT與實施例II-1相同。 無氧槽4的處理條件如以下所述。 <無氧槽> -35- 201210953DO : 〇.5mg/L -33- 201210953 BOD Volumetric load: 3.85kg-BOD/m3/d HRT : 4 hours pH 値: 7.0 <Second biological treatment tank > DO : 4mg/L Carrier charge rate: 2% HRT: 1 7 hours SRT: 30 days pH 値: 7.0 Further, use a plate-shaped polyamino 1 5mm x 300mm x 50mm / l piece) as the second life 12, set in the vertical plane relative to the center of the groove, and cut off And the bottom and the left and right are fixed on the wall surface of the tank, and the bulk load of the whole body of the device is 21 hours for the HRT of the whole device. As a result, the sessile-filtered predatory microorganism (the bell Ib Bdelloida) on the second biological treatment tank 2 is dominant, and the sludge conversion rate C Ο D c r. Treatment water (the permeation CODCr concentration of the membrane separation device 5 is less than 20 mg/L, during the experimental period. Formate foam (the carrier of the treatment tank 2 is symmetrical with the gas tube 2 1 at 0.75 kg-BOD/m3/ d, Γ mud floc, in the carrier animal Vorticella, light weight is 0.1 kg-MLSS/kg-water) water quality, solubility, and often maintain good shape -34- 201210953 Again, the membrane separation device 5 has almost no intermembrane pressure difference When the drug is not washed for more than one month, stable effluent water can be maintained. [Comparative Example II-1] The first biological treatment tank is omitted, and the capacity of the second biological treatment tank is set to 1 8.6 L, and The treatment was carried out under the same conditions as in Example II-1 except that the carrier was not provided in the second biological treatment tank. The quality of the raw water, the DO and pH of the second biological treatment tank, the overall BOD volume load and HRT and Example II The same is true. The result is that the sludge conversion rate is 2020 kg 'MLSS/kg-CODCr. However, every one month, the aggregated predatory microorganism (Euchlanis) is dominant, during which the differential pressure between the membranes rises. It is necessary to wash the film once every 2 weeks. In addition, the treatment The water quality is also deteriorated, and the dissolved CODCr concentration is increased to 70 mg/L or more. [Example Π-2] As shown in Fig. 8, an anaerobic tank 4 having a capacity of 5 L is provided, and the stain in the second biological treatment tank 2 is removed. After the mud is treated in the anaerobic tank 4, it is sent back to the second biological treatment tank 2, and the other treatment is carried out under the same conditions as in the embodiment II-1. The water quality of the raw water, the processing conditions of the first and second biological treatment tanks, The overall BOD volume load and HRT were the same as in Example II-1. The treatment conditions of the anaerobic tank 4 are as follows. <Oxygen-free tank> -35- 201210953
ORP ： -lOOmV HRT ( =SRT ) ： 12 小時 其結果，第二生物處理槽內之污泥絮凝體，在載體上 之固著性濾過捕食型微生物（吊鐘蟲 Vorticella、蛭形目 Bdelloida)優勢化，而污泥轉換率爲 0.075kg-MLSS/kg-CODCr。 處理水水質，溶解性CODCr濃度爲未滿20mg/L，實 驗期間，經常維持良好狀態。又，膜間差壓幾乎沒有上升 ，即使1個月以上不進行藥品洗淨，也可以維持穩定的流 出水。 [產業上的可利用性] 本發明之有機性排廢水的生物處理方法及裝置，可以 利用在生活上的排廢水、下水道、食品工場或紙漿工廠等 廣泛排廢水濃度範圍的有機性排廢水的處理。 已利用特定形態詳細說明本發明，但不背離本發明主 旨及範圍，可以有各種各樣的變化這是本業者明瞭的。 再者，本申請是根據2010年3月31日提出的日本發 明申請（特願2010-083136) 、2010年7月21日提出的 日本發明申請（特願2010-164087) 、2011年3月2日提 出的曰本發明申請（特願2011-044797)及2011年3月2 日提出的日本發明申請（特願201 1 -044798 )，引用其整 體內容並加以援用。 -36- 201210953 【圖式簡單說明】 [圖1]表示第1發明之有機性排廢水的生物處理方法 及裝置的實施形態系統圖。 [圖2]表示第1發明之有機性排廢水的生物處理方法 及裝置的其他實施形態系統圖。 [圖3]表示第1發明之有機性排廢水的生物處理方法 及裝置的其他實施形態系統圖。 [圖4]表示第1發明之有機性排廢水的生物處理方法 及裝置的其他實施形態系統圖。 [圖5]表示第1發明之有機性排廢水的生物處理方法 及裝置的其他實施形態系統圖》 [圖6]表示第2發明之有機性排廢水的生物處理方法 及裝置的實施形態系統圖。 [圖7]表示第2發明之有機性排廢水的生物處理方法 及裝置的其他實施形態系統圖。 [圖8]表示第2發明之有機性排廢水的生物處理方法 及裝置的其他實施形態系統圖。 【主要元件符號說明】 1 :第一生物處理槽ORP : -lOOmV HRT ( =SRT ) : 12 hours of results, the sludge floc in the second biological treatment tank, the sessile filtration of the predatory microorganism on the carrier (Vorticella, Bdelloida) The sludge conversion rate was 0.075 kg-MLSS/kg-CODCr. The water quality was treated, and the dissolved CODCr concentration was less than 20 mg/L. During the test period, it was always in good condition. Further, the differential pressure between the membranes hardly rises, and even if the medicine is not washed for one month or more, stable flowing water can be maintained. [Industrial Applicability] The biological treatment method and apparatus for organic waste water of the present invention can utilize organic wastewater discharged in a wide range of wastewater discharge ranges such as sewage discharge, sewer, food factory or pulp mill in life. deal with. The present invention has been described in detail with reference to the specific embodiments thereof, and various modifications and changes in the scope of the present invention. In addition, this application is based on the Japanese invention application filed on March 31, 2010 (Japanese Patent Application No. 2010-083136), and the Japanese invention application filed on July 21, 2010 (Japanese Patent Application No. 2010-164087), March 2, 2011 The Japanese Patent Application (Japanese Patent Application No. 2011-044797), filed on March 2, 2011, and the entire contents of -36-201210953 [Brief Description of the Drawings] [Fig. 1] Fig. 1 is a system diagram showing an embodiment of a biological treatment method and apparatus for organic wastewater discharge according to a first aspect of the invention. Fig. 2 is a system diagram showing another embodiment of a biological treatment method and apparatus for organic waste water of the first invention. Fig. 3 is a system diagram showing another embodiment of a biological treatment method and apparatus for organic waste water of the first invention. Fig. 4 is a system diagram showing another embodiment of a biological treatment method and apparatus for organic waste water discharge according to the first aspect of the invention. Fig. 5 is a system diagram showing another embodiment of a biological treatment method and apparatus for organic waste water discharge according to the first aspect of the invention. Fig. 6 is a system diagram showing an embodiment of a biological treatment method and apparatus for organic waste water discharge according to a second aspect of the invention. . Fig. 7 is a system diagram showing another embodiment of a biological treatment method and apparatus for organic wastewater discharged according to a second aspect of the invention. Fig. 8 is a system diagram showing another embodiment of a biological treatment method and apparatus for organic wastewater discharged according to a second aspect of the invention. [Main component symbol description] 1: First biological processing tank
I 2:第二生物處理槽 3 :沉澱槽 4 :無氧槽 5 :膜分離裝置 -37-I 2: second biological treatment tank 3: sedimentation tank 4: anaerobic tank 5: membrane separation device -37-