201223885 六、發明說明： 【發明所屬之技術領域】 本發明係關於-種排水處理裝置，其藉由 將含有β〇ΐ)成分的有機性排水進行生物處理。7泥而 【先前技術】 士好氣性之活性污泥法開始適用於排水處理裝置之 :太係藉由將每批次處理含Β㈤成分之處理對象的有機性 从批次式活性污泥法來進行排水處理。批次式活 4係將原水之流入步驟、反應步驟、沉降步驟 1 驟作^個循環而加以處理者。然而，批次式活性污^法步 對應水量或負荷之大變動係困難的，又由於當初並無自動 =技術，必須以手動進行運轉循環，有操作煩雜的缺點 、因此，可連續地使有機性排水流入的標準活性汚 被開發出來。 尼法 “、、:而，連續式的標準活性污泥法中因生物污泥之沉降 不良，有生物污泥分離困難而有所謂的「增容（bulkbg) 的問題。活性污泥法之處理能力因強烈地仰賴於可保持^ 生物污泥量，故由於起因於增容的沉降不良，於處理水， 生物污泥流出的問題為一大課題。對於如此之課題，已開 發許多稱為活性污泥之改變法的技術（例如，參照非專利 文獻1)。 ,近年來，關於批次式活性污泥法，已報告使用具有非 常快速的沉降速度之稱為「微粒（啊㈤」的微生物自201223885 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a wastewater treatment apparatus for biological treatment of an organic wastewater containing a β〇ΐ component. 7 mud and [previous technology] The aerobic activated sludge method is applied to the drainage treatment device: the system uses the organic matter of the treatment target containing bismuth (five) components from the batch type activated sludge method. Drainage treatment. The batch type 4 system processes the raw water inflow step, the reaction step, and the sedimentation step 1 by one cycle. However, batch-type active pollution method is difficult to respond to large changes in water volume or load, and since there is no automatic = technology at the beginning, it is necessary to manually operate the cycle, which has the disadvantage of being complicated, so that it can be continuously organic. Standard active fouling of influent drainage has been developed. Nifa ",": In the continuous standard activated sludge process, the sedimentation of biological sludge is poor, and there is a problem that the separation of biological sludge is difficult, and there is a so-called "bulkbg" problem. Because of the strong ability to maintain the amount of biological sludge, the problem of treating water and biological sludge outflow is a major issue due to poor sedimentation due to compatibilization. For such a problem, many activities have been developed. The technique of the method of changing the sludge (for example, refer to Non-Patent Document 1). In recent years, regarding the batch type activated sludge method, it has been reported to use a microorganism called "fine particles (ah (five)") having a very rapid sedimentation speed. from
S 3 201223885 己造粒體下，可提高污泥濃度而實現高的處理能力者（例 如，參照專利文獻1)。 又，關於連續法之活性污泥法，亦已提出將微粒作為 種污泥而使生物污泥微粒化的手法（例如，參照專利文獻 2) ° [先前技術文獻] [專利文獻] [專利文獻1] 特表2005-538825號公報 [專利文獻2] 特開2002-336885號公報 [非專利文獻] [非專利文獻1 ] Jiri Wanne，「活性污泥之增容與生物 發泡之控制」，技報堂出版，2〇〇〇年。 【發明内容】 [發明概要] [發明所欲解決的課題] 藉由使用微粒的批次式活性污泥法的排水處理方法 由於不會有增容的.問題，而且因為生物污泥之沉降性高， =獲=的處理能力的觀點來看係為有益的。但批次式 雜之運轉控制必須有許多感應器，故裝置變複 本、操作管理方面係為不利的。 物〉可泥形成微粒的機構，因為某些原因 201223885 而使得微粒會崩壞的情形下，必須再度添加微粒情形 為種污泥，於運轉管理上發生問題。 目此，本發明_提供可提高生物污泥之崎性的排 水處理裝置為目的。或者，以提供於連續式之活性污泥法 中，使污泥微粒化、可提高生物污泥之沉降性的排水處理 裝置為目的。 [用以解決課題之手段] (1)本發明係一種排水處理裝置，其具有將含 成分的有機性排水藉由生物污泥的生物處理的反應槽、及 將别述反應槽所獲得的處理水與前述污泥分離的污泥分 離槽，前述反應槽係含有無氧生物處理槽、第一生物處理 槽及第二生物處理槽來供給前述生物處理所必要的氧；前 述有機性排水係連續地流入至前述第一生物處理槽’前述 第一生物處理槽及前述第二生物處理槽中經生物處理之 前述污泥分離槽内的污泥被送回前述第二生物處理槽及 刚述無氧生物處理槽；前述無氧生物處理槽内之污泥至少 被供給到前述第一生物處理槽，前述第一生物處理槽之 MLSS負荷較前述第二生物處理槽之MLSS負荷更高。 (2) 如上述（i)之排水處理裝置，其中前述第一生 物處理槽之MLSS負荷為0.8kgBOD/kgMLSS/da上之範 圍，前述第二生物處理槽之MLSS負荷為 〇.5kgBOD/kgMLSS/d以下之範圍者較佳。 (3) 如上述〇)或（2)之排水處理裝置，其中前 述第一生物處理槽及前述第二生物處理槽之被處理水之 5 201223885 滞留時間總計為3小時以上者為較佳。 [發明之效果] 依據本發明，可提高生物污泥之沉降性。 【實施方式】 [用以實施發明之形態] 以下’况明本發明之實施形態。又，本實施形態係實 施本發明之一例，本發明並未受限於本實施形態。 其中，於本說明書之「微粒」係指微生物自己造粒體， 其並未特別限制，例如係指其粒徑為1〇〇μιηα上者。 又’於本5兄明書，「連續式」係指連續將排水供給至 反應槽而運轉的方式’但亦可藉由利用如隔膜式果 (diaphragm pump)等之往復運動的原理’將排水供給至 反應槽而運轉的方式等。又，亦可為於反應槽之前段設置 原水槽，因應此原7]c槽之水位而控制泵之作動停止（水 位高時，將泵啟動，水位低時則停止I)，將排水供給至 反應槽的模減續it水方鱗。射式於未伴隨反應槽内 積極排水之點，與批次式處理、半批次式處理可作區別。 成為處理對象的排水係食品加工工廠排水、化學工廠 排水、半導體工廠排水、機械工廢排水、下水道、人類排 泄物、何川水等之含有生物分解性有機物的排水。又，處 理生物難分解性之有機物的情形，藉由預先施予物理化學 的處理，而變換為生物分解性之物f的處理成為可能。 以下係將食品工廠排水作為處理對象的情形作為一 201223885 例’說明本實施形態有關之排水處理方法及排水處理裝置 之適用。 第1圖係顯示本實施形態有關之排水處理裝置之一例 的概略構成圖。第1圖所示的排水處理裝置丨係具備無氧生 物處理槽10、第一生物處理槽12、第二生物處理槽14、污 泥分離槽16。 第一生物處理槽12與排水流入管線18a連接，第一生 物處理槽12與第二生物處理槽14之間，以排水流入管線 18b連接，第二生物處理槽14與污泥分離槽μ之間，以排 水流入管線18c連接，污泥分離槽16與無氧生物處理槽1〇 之間，以污泥送回管線20a連接，污泥分離槽16與第二生 物處理槽14之間，以污泥送回管線20b直接連接或以由污 泥送回管線20a分支的污泥送回管線2〇b連接，無氧生物處 理槽10與第一生物處理槽12之間，以污泥送回管線2〇c連 接。又’污泥分離槽16與處理水排出管線22連接。 於本實施形態之排水處理裝置1之動作説明之前，先 說明生物污泥之微粒化之條件。 第2圖係顯示批次式活性污泥法中的丨批次之 度與時間之關係圖。如前述之批次式活性污泥法係將原辰火 之流入步驟、反應步驟、沉降步驟、排出步驟作為1個尨 環加以處理者。如第2圖所示，經由原水之流入来 ^ v驟，移 至反應步驟時，BOD濃度因微生物之分解作用而、滅小 時，作為微生物之一般的性質，B0D濃度高時，輿3^〇二 度低時相比，若為相同之MLSS濃度，則其處理逮度變^ 201223885 速P成為MLSS負荷高、且微生物為飽食狀態。於反 ^步，進行以微生物之生物處理，反應槽内之BOD濃度 复，才處理速度會降低，很快地會變成0。即，成為MLSS 負_何低、且微生物為飢餓狀態。之後，經由無氧狀態，移 行至ΐ物污泥之沉降步驟、處理水之排出步驟。藉由重複 此循環’反應槽内產生生物污泥之微粒化。#，生物污泥 之微粒化係除了無氧狀態，控制由飽食狀態至飢餓狀態之 遷移者為重要的。 因此’以本實施形態之排水處理裝置’藉由批次式活 性污泥法而於連續式之活性污泥法_再現無氧狀態、飽食 狀態、飢餓狀態，可容易地設定發生污泥之微粒化的條件。 首先’於污泥微粒化中必要的無氧狀態係藉由本實施 形態之無氧生物處理槽10來實行。關於無氧生物處理槽10 之具體的生物處理係如後述，但無氧生物處理槽10内，脱 氮菌等之微生物、由後述的污泥分離槽16所供給的生物污 泥會滯留’於彼等之生物污泥之内生呼吸下成為無氧狀 悲。其中’無氧狀態其中係指溶氧（dissolved oxygen)並 不存在，但來自亞硝酸或硝酸之氧等存在的狀態。 其次’於污泥之微粒化為必要的飽食狀態係藉由本實 施形態之第一生物處理槽12來實行。第一生物處理槽12 内，微生物、由後述的無氧生物處理槽10所供給的生物污 泥會滯留。第一生物處理槽12内，藉由曝氣或攪拌等供給 氧，又，藉由提供較第二生物處理槽14為高的MLSS負荷， 生物污泥會成為飽食狀態。第二生物處理槽14内，微生 201223885 物、由後述的第—生物處理槽12所供給的生物污泥會滞 留。第二生物處理槽14内，藉由曝氣或攪拌等來供給氧， 藉由提供較第一生物處理槽12為低的MLSS負荷，生物污 泥會成為飢餓狀態。 而且，使此荨無氧生物處理槽1〇、苐—生物處理槽 12、第二生物處理槽14直列式連結，而將無氧狀態、飽食 狀態、飢餓狀態於連續式之活性污泥法再現。 以下’説明本實施形態之排水處理裝置丨之動作。 由食品工廠等排出的含BOD成分的排水係通過排水 流入管線18a，而連續地流入第一生物處理槽12。由食品 工廢等排出的排水係於供給至第一生物處理槽12之前， 被送到原水貯留槽（未圖示），而進行排水之水質安定化 者為較佳。又’此時，最好將排水中含有固形物的情形， 藉由過篩等，將固形去除。又，因係於原水貯留槽中進行 排水之均一化，最好設置攪拌裝置（機械攪拌、空氣攪拌 等）。 本實施形態中，雖以各式各樣的BOD成分為對象，但 與油脂分有關者係因附著於污泥或微粒而有不良影響，故 於供給至第一生物處理槽12之前，預先藉由浮集分離 (floatation separation )、凝集加壓浮集裝置、吸著裝置等 之既存手法最好將油脂分去除至150mg/L以下左右。 第一生物處理槽12係於好氣條件下（藉由曝氣或攪拌 等來供給氧）’經由槽内之微生物及自無氧生物處理槽1〇 所供給的生物污泥，排水中之B0D成分會被分解。如此， 201223885 於第一生物處理槽12中，因自無氧生物處理槽1〇之污泥被 含BOD成分的排水稀釋，可保持槽内之MLSS濃度於低 值。即，確保前述高的MLSS負荷，而將生物污泥作成飽 食狀恶。亦因BOD成分或槽之容積等，第一生物處理槽12 中MLSS負荷為(UkgBOD/kgMLSS/d以上〜低於 1.8kgBOD/kgMLSS/d的範圍為較佳，於此情形，流入的 BOD成分於第一生物處理槽12中幾乎被分解。第一生物處 理槽12中MLSS負荷為HgBOD/kgMLSS/d以上〜低於 5.0kgBOD/kgMLSS/d之範圍時，雖然自第一生物處理槽12 排出的處理水中有殘存BOD成分，但因其量少，對後段之 弟一生物處理槽14中]VILSS負荷的影響小。即，不會變得 較第一生物處理槽12中MLSS負荷為大。第一生物處理槽 12中之MLSS負荷為5.0kgBOD/kgMLSS/d以上的情形，依 BOD成分之種類，流入後段之第二生物處理槽μ的b〇d成 分會變多’將第二生物處理槽14之MLSS負荷作成較第一 生物處理槽12之MLSS負荷為小者有變困難的情形。 其次，第一生物處理槽12所處理的排水（亦含有污泥） 係通過排水流入管線18b，而連續地流入至第二生物處理 槽14。第二生物處理槽14係於好氣條件下（藉由曝氣或攪 拌等之氧供給）’藉由槽内之微生物、自第一生物處理槽 12所供給的生物污泥及後段之污泥分離槽丨6所供給的生 物污泥，排水中未反應之BOD成分會被分解。第二生物處 理槽14中，除了較第一生物處理槽12所流入的b〇d成分為 少之外，因MLSS濃度經由自後段污泥分離槽16所供給的 201223885 生物污泥流入而增加，故可控制成較第一生物處理槽12更 低的MLSS負射。即，可確保第二生物處理槽μ之mlss 負荷幾乎為無的狀態或非常低的狀態，故可將生物污泥作 成飢餓狀態。第二生物處理槽14中MLSS負荷亦因BOD成 分或槽之容積等作成S 3 201223885 Under the granulated body, the sludge concentration can be increased to achieve high processing capacity (for example, refer to Patent Document 1). In addition, the activated sludge method of the continuous method has also proposed a method of micronizing biological sludge by using fine particles as a seed sludge (for example, refer to Patent Document 2) ° [Prior Art Document] [Patent Literature] [Patent Literature] [Patent Document 2] JP-A-2002-336885 [Non-Patent Document] [Non-Patent Document 1] Jiri Wanne, "Compatibilization of Activated Sludge and Control of Biological Foaming", Technical newspaper published, 2 years. [Summary of the Invention] [Problems to be Solved by the Invention] The wastewater treatment method by the batch type activated sludge method using fine particles has no problem of compatibilization, and because of the sedimentation property of biological sludge It is beneficial to view the processing power of high, = =. However, there must be many sensors for batch-type operation control, so the device is complicated and the operation management is unfavorable. In the case where the particles can form particles, for some reasons 201223885, the particles may collapse. In the case where the particles are added again, the sludge is added, and there is a problem in operation management. Accordingly, the present invention has an object of providing a water discharge treatment device capable of improving the roughness of biological sludge. Alternatively, it is intended to provide a wastewater treatment device which is provided in a continuous activated sludge process to atomize sludge and improve sedimentation of biological sludge. [Means for Solving the Problem] (1) The present invention relates to a wastewater treatment apparatus comprising a reaction tank for biological treatment of biological wastewater containing components by biological sludge, and treatment obtained by the reaction tank described elsewhere a sludge separation tank separating water from the sludge, wherein the reaction tank includes an oxygen-free biological treatment tank, a first biological treatment tank, and a second biological treatment tank to supply oxygen necessary for the biological treatment; the organic drainage system is continuous The sludge flowing into the first biological treatment tank and the biological treatment-treated sludge separation tank in the first biological treatment tank and the second biological treatment tank is sent back to the second biological treatment tank and The oxygen biological treatment tank; the sludge in the oxygen-free biological treatment tank is supplied to at least the first biological treatment tank, and the MLSS load of the first biological treatment tank is higher than the MLSS load of the second biological treatment tank. (2) The drainage treatment device according to (i) above, wherein the MLSS load of the first biological treatment tank is in a range of 0.8 kg BOD/kg MLSS/da, and the MLSS load of the second biological treatment tank is 〇.5 kg BOD/kg MLSS/ The range below d is preferred. (3) The wastewater treatment apparatus according to the above-mentioned 〇) or (2), wherein the residence time of the first biological treatment tank and the second biological treatment tank 5 201223885 is preferably 3 hours or longer. [Effect of the Invention] According to the present invention, the sedimentation property of the biological sludge can be improved. [Embodiment] [Embodiment for Carrying Out the Invention] Hereinafter, embodiments of the present invention will be described. Further, this embodiment is an example of the present invention, and the present invention is not limited to the embodiment. Here, the "fine particles" in the present specification means the microorganism itself granules, and it is not particularly limited, and for example, it means that the particle diameter is 1 〇〇 μηηα. In addition, 'the continuous type' refers to a mode in which the drainage is continuously supplied to the reaction tank and operated, but the drainage can be performed by using the principle of reciprocating motion such as a diaphragm pump. A method of supplying to a reaction tank and operating it. In addition, the raw water tank may be disposed in the front stage of the reaction tank, and the operation of the pump is stopped according to the water level of the original 7]c tank (when the water level is high, the pump is started, and when the water level is low, the water is stopped), and the drainage is supplied to The mold of the reaction tank is reduced to the water scale. The spot type can be distinguished from the batch treatment and semi-batch treatment at the point where the positive drainage is not accompanied by the reaction tank. Drainage system containing wastewater, chemical plant drainage, semiconductor plant drainage, mechanical waste water, sewer, human waste, Hechuan water, etc., containing biodegradable organic matter. Further, in the case of treating an organic substance which is difficult to be biodegradable, it is possible to convert it into a biodegradable substance f by a treatment in which physical chemistry is applied in advance. The following is a description of the drainage treatment method and the drainage treatment apparatus according to the present embodiment. Fig. 1 is a schematic block diagram showing an example of a drainage treatment apparatus according to the present embodiment. The wastewater treatment device shown in Fig. 1 includes an anaerobic biological treatment tank 10, a first biological treatment tank 12, a second biological treatment tank 14, and a sludge separation tank 16. The first biological treatment tank 12 is connected to the drainage inflow line 18a, and the first biological treatment tank 12 and the second biological treatment tank 14 are connected by a drainage inflow line 18b, and between the second biological treatment tank 14 and the sludge separation tank μ Connected by the drain inflow line 18c, between the sludge separation tank 16 and the anaerobic biological treatment tank 1 , connected by the sludge return line 20a, and between the sludge separation tank 16 and the second biological treatment tank 14 The mud return line 20b is directly connected or connected by a sludge return line 2〇b branched from the sludge return line 20a, and between the anaerobic biological treatment tank 10 and the first biological treatment tank 12, the sludge is sent back to the pipeline. 2〇c connection. Further, the sludge separation tank 16 is connected to the treated water discharge line 22. Before the description of the operation of the wastewater treatment apparatus 1 of the present embodiment, the conditions for the atomization of the biological sludge will be described. Figure 2 is a graph showing the relationship between the batch size and the time in the batch type activated sludge process. The batch type activated sludge method as described above treats the original inflow step, the reaction step, the sedimentation step, and the discharge step as one annulus. As shown in Fig. 2, when the raw water is introduced into the reaction step, the concentration of BOD is reduced by the decomposition of microorganisms. As a general property of microorganisms, when the concentration of B0D is high, 舆3^〇 Compared with the second MLSS concentration, if the MLSS concentration is the same, the treatment catching degree becomes 201223885. The speed P becomes a high MLSS load and the microorganism is in a saturated state. In the reverse step, the treatment with the microorganisms is carried out, and the BOD concentration in the reaction tank is repeated, and the treatment speed is lowered, and it becomes 0 quickly. That is, the MLSS is negative and the microorganism is in a state of starvation. Thereafter, the process proceeds to the sedimentation step of the sludge and the discharge step of the treated water via the anaerobic state. The micronization of the biological sludge is produced in the reaction tank by repeating this cycle. #, The micronization of biological sludge is important in controlling the migration from the saturated state to the starvation state in addition to the anaerobic state. Therefore, in the "drainage treatment apparatus of the present embodiment", the continuous activated sludge method can be used to reproduce an anaerobic state, a saturated state, and a starvation state by the batch type activated sludge method, and the sludge particles can be easily set. Condition. First, the anaerobic state necessary for sludge micronization is carried out by the anaerobic biological treatment tank 10 of the present embodiment. The specific biological treatment system of the anaerobic biological treatment tank 10 will be described later, but in the anaerobic biological treatment tank 10, microorganisms such as denitrifying bacteria and biological sludge supplied from the sludge separation tank 16 to be described later may be retained. The biological sludge of their biological sludge becomes anaerobic. The 'anaerobic state' refers to a state in which dissolved oxygen is not present but is derived from oxygen such as nitrous acid or nitric acid. Next, the state of satiety in which the micronization of the sludge is necessary is carried out by the first biological treatment tank 12 of the present embodiment. In the first biological treatment tank 12, microorganisms and biological sludge supplied from the anaerobic biological treatment tank 10 to be described later are retained. In the first biological treatment tank 12, oxygen is supplied by aeration or stirring, and by providing a higher MLSS load than the second biological treatment tank 14, the biological sludge becomes a saturated state. In the second biological treatment tank 14, the biological sludge supplied by the microbial 201223885 and the first biological treatment tank 12 to be described later is retained. In the second biological treatment tank 14, oxygen is supplied by aeration or agitation, and by providing a lower MLSS load than the first biological treatment tank 12, the biological sludge becomes starved. Further, the anaerobic biological treatment tank 1〇, the 苐-biological treatment tank 12, and the second biological treatment tank 14 are connected in series, and the anaerobic state, the saturated state, and the starvation state are reproduced in the continuous activated sludge method. . The operation of the drainage treatment device 本 according to the present embodiment will be described below. The BOD-containing drainage discharged from the food factory or the like flows into the first biological treatment tank 12 through the drainage inflow line 18a. It is preferable that the drainage discharged from the food waste or the like is sent to the raw water storage tank (not shown) before being supplied to the first biological treatment tank 12, and the water quality of the drainage is stabilized. Further, in this case, it is preferable to remove the solid matter in the case where the solid matter is contained in the drainage, by sieving or the like. Further, it is preferable to provide a stirring device (mechanical stirring, air agitation, etc.) because the drainage is uniform in the raw water storage tank. In the present embodiment, various types of BOD components are targeted, but those associated with fats and oils are adversely affected by adhesion to sludge or fine particles, so they are borrowed before being supplied to the first biological treatment tank 12. It is preferable to remove the fat and oil to about 150 mg/L or less by an existing method such as a floatation separation, a coagulation/pressure floating device, or a absorbing device. The first biological treatment tank 12 is under aerobic conditions (supply of oxygen by aeration or agitation), and the B0D component in the drainage through the microorganisms in the tank and the biological sludge supplied from the anaerobic biological treatment tank 1 Will be broken down. Thus, in 201223885, in the first biological treatment tank 12, since the sludge from the anaerobic biological treatment tank 1 is diluted with the BOD-containing water, the MLSS concentration in the tank can be kept low. That is, the above-mentioned high MLSS load is ensured, and the biological sludge is made into a satiety. Also, the MLSS load in the first biological treatment tank 12 is (the range of UkgBOD/kg MLSS/d or more to less than 1.8 kg BOD/kg MLSS/d is preferable because of the BOD component or the volume of the tank, etc., in this case, the inflowing BOD component It is almost decomposed in the first biological treatment tank 12. When the MLSS load in the first biological treatment tank 12 is in the range of HgBOD/kg MLSS/d or more to less than 5.0 kg BOD/kg MLSS/d, it is discharged from the first biological treatment tank 12. In the treated water, there is a residual BOD component, but since the amount is small, the influence on the VILSS load in the second-stage biological treatment tank 14 is small, that is, it does not become larger than the MLSS load in the first biological treatment tank 12. When the MLSS load in the first biological treatment tank 12 is 5.0 kg BOD/kg MLSS/d or more, depending on the type of the BOD component, the b〇d component of the second biological treatment tank μ flowing into the latter stage becomes more 'the second biological treatment It is difficult for the MLSS load of the tank 14 to be smaller than the MLSS load of the first biological treatment tank 12. Next, the drainage (also containing sludge) treated by the first biological treatment tank 12 passes through the drainage inflow line 18b. And continuously flows into the second biological treatment tank 14. The biological treatment tank 14 is under aerobic conditions (supply by oxygen such as aeration or agitation) 'by the microorganisms in the tank, the biological sludge supplied from the first biological treatment tank 12, and the sludge separation tank in the latter stage. The biological sludge supplied by the 6th, the unreacted BOD component in the drainage is decomposed. The second biological treatment tank 14 is smaller than the b〇d component flowing in the first biological treatment tank 12, due to the MLSS concentration. It is increased by the inflow of 201223885 biological sludge supplied from the subsequent sludge separation tank 16, so that it can be controlled to be lower than the first biological treatment tank 12 by MLSS, that is, the mlss load of the second biological treatment tank μ can be ensured. The biological sludge is starved to a state of almost no state or a very low state. The MLSS load in the second biological treatment tank 14 is also made up of the BOD component or the volume of the tank.
OkgBOD/kgMLSS/d~0.5kgBOD/kgMLSS/d以下之範圍為較 佳。自第一生物處理槽12流入的未反應之b〇d成分多時， 第二生物處理槽14中MLSS負荷有超過 0.5kgBOD/kgMLSS/d的情形。第二生物處理槽14*mlss 負荷超過0.5kgBOD/kgMLSS/d時，通過第一生物處理槽12 而持續給予高的MLSS負荷，故有時會發生自生物污泥之 微粒化誘發增容的可能性提高的情形。 其次，第二生物處理槽14所處理的排水（亦含有污泥） 係通過排水流入管線18c，而連續地流入污泥分離槽16。 污泥分離槽16内，自第二生物處理槽14所排出的排水，生 物污泥會被沉降分離。而且，生物污泥被分離的排水作為 處理水自處理水排出管線22被排出。於污泥分離槽16所渡 縮的生物污泥，自污泥送回管線20a被供給至無氧生物處 理槽10 ’又’自污泥送回管線2〇b被供給於第二生物處理 槽14。於調整污泥送回量的情形，於污泥送回管線2〇a等 設置泵等者為較佳。又’污泥分離槽16並未限制於沉降分 離，例如，亦可為膜分離等。 無氧生物處理槽10内，由於脱氮菌等之微生物、自污 泥分離槽16所供給的生物污泥，進行將無氧生物處理槽1〇 11 201223885 内之含氮物質變換為氮氣的脱氣 ίο内經由如前述之生物⑺尼 f ^生物處理糟 態。此時進行擾拌時，槽内污呼吸而成為無氧狀 又，無氧生物處理槽10之生物=度5為均—而為較佳。 自污泥分離槽16供給的生物，2▼留時間顯著短時， 生呼吸而被消耗，有無法維持==的氣不會藉由内 無氧生物處理槽1〇之生物污泥之滞留時間確伴為3二 以上。無氧狀態下所處理的生物污泥會自污 20c被連續地供給於第一生物處理槽12。 e、 =τ無氧生物處理槽_可為嫌氣狀態。 即，無氧生物處理槽Π)可為嫌氣槽。嫌氣槽係於嫌氣狀態 下進行·、Ψ㈣酵等。其巾職狀態係衫僅溶氧不 存在’來自亞賴或硝酸的氧亦不存在的條件。嫌氣槽之 場合，因反應過程中有機物成為必要，使排水之一部份流 入至嫌氣槽，有必要添加排水中之有機物。惟，使排水之 一部份流入時，嫌氣槽中排水之滞留時間會變短，而有必 要確保滯留時間。 如此，經由飽食狀態之第一生物處理槽12、飢锇狀態 之第一生物處理槽14、無氧狀態之無氧生物處理槽1〇而使 生物污泥進行循環時，會發生生物污泥之微粒化，可提高 生物污泥之沉降性。其結果，提高排水之處理速度成為可 能。又’活性污泥之管理上重要的污泥沉降性管理變容易。 以下’説明關於污泥之微粒化中的較佳條件等。 如第2圖所示，批次式活性污泥法之情形，反應步驟 12 201223885 中的反應初期，反應槽内之B〇D濃度成為高飽食狀態，但 BOD成分隨著分解的進行，反應槽内之b〇d濃度會降低， 而移行至飢餓狀態。於污泥之沉降性改善、污泥之微粒化 等，除了之後無氧狀態之步驟，此時飢餓狀態之時間相對 於飽食狀態為相當長者被認為是重要的。此比例之最適値 被認為依處理對象之BOD成分而異，但大多情形，叙餓狀 態者較飽食狀態更長時間為必要。於本實施形態，滿足前 述的MLSS負荷之範圍的第一生物處理槽12係成為飽食狀 態，第二生物處理槽14成為飢餓狀態。因此，以飽食狀態 相對於飢餓狀態的比例（飽食狀態/飢餓狀態）成為低於1 的方式，控制污泥送回量、及設計第一生物處理槽12及第 二生物處理槽14之容積為所冀望的。 批次式活性污泥法之情形係於同一反應槽内發生反 應，故飽食狀態及飢餓狀態之MLSS量為相同。因此，飽 食狀態相對於飢餓狀態的比例（飽食狀態/飢餓狀態）相 應飽食狀態的時間及凱餓狀態的時間為宜。另一方面，連 續式活性污泥法的情形，因飽食狀態及飢餓狀態的槽不 同，故保持的MLSS量各自相異。因此，飽食狀態相對於 飢餓狀態之比例以如下方式計算。 【數1】 第一生物處理槽之污泥保持量（容積xMLSS濃度） [g]x滯留時間[h] 第二生物處理槽之污泥保持量（容積xMLSS濃度） [g]x滯留時間[h] 13 201223885 又，於抵次式活性污泥法，已知飢餓狀態與飽食狀態 之循裱間隔亦為生物污泥之微粒化所必要的因+。一般而 5，已知飢餓狀態與飽食狀態之循環間隔越短，生物污泥 之微粒化會變困難。此於連續式之活性污泥法亦相同。本 實施形態中，以第一生物處理槽12及第二生物處理槽抖中 被處理水之滯留時間總計成為至少3小時以上的方式，設 疋第生物處理槽12與第二生物處理槽14中之容積、被處 理^流量、及送回污泥流量，作成飢餓狀態與飽食狀態之 循環間隔不為變短者為所冀望的。 於生物污泥中微粒化的觀點，將第一生物處理槽12、 第二生物處理槽14各自分割成複數個，使含BOD成分的排 水各自流入經分割的第一生物處理槽12,又，各自供給至 分割生物污泥的第二生物處理槽14者為較佳。使生物處理 槽分割的情形，彼等中之至少丨個之第—生物處理槽12及 第二生物處理槽14中之容積滿足前述生物污泥的微粒化 之較佳條件者為宜。 自污泥分離槽16排出的全體污泥流量及流入至無氧 生物處理槽10的污泥流量被設定為可確保第一生物處理 槽Π中之飽食狀態相對於前述第二生物處理槽Μ中之飢 餓狀態的比例（飽食狀態/飢餓狀態）為低於丨、無氧生物 處理槽之滞留時間為3G分鐘以上的方式為較佳。例如，使 流入無氧生物處理槽10的污泥流量增加時，無氧生物處理 槽10及第一生物處理槽12之滯留時間會持續減少，第一生 物處理槽12之MLSS濃度會降低。使流入無氧生物處理槽 201223885 10的污泥流量減少時，無氧生物處理槽10及第一生物處理 槽12之滯留時間會持續增加，第一生物處理槽12之MLSS 濃度會上升。全體之污泥流量增加時，無氧生物處理槽 10、第一生物處理槽12及第二生物處理槽14之滯留時間會 減少，第一生物處理槽12中MLSS濃度上升的同時，第二 生物處理槽14中MLSS濃度亦上升。全體之污泥流量減少 時，無氧生物處理槽10、第一生物處理槽12及第二生物處 理槽14之滯留時間會增加，第一生物處理槽12中MLSS濃 度增加的同時，第二生物處理槽14中MLSS濃度亦上升。 藉由如此送回流量之操作，可使無氧生物處理槽1〇、第一 生物處理槽12及第二生物處理槽14之滯留時間、第一生物 素處理槽12中MLSS濃度及第二生物處理槽丨斗中“^^濃 度專變化，故任意地控制飽食狀態相對於叙餓狀態的比例 成為可能。本實施形態之連續式之活性污泥法，與批次式 活性污泥法不同，生物污泥之微粒化上為重要因子的無氧 狀態、飽食狀態、飢餓狀態，可藉由送回流量之操作而任 意地控制為可能的點係有益的。 關於各生物處理槽内之pH並未特別規定，但與通常活 性污泥同樣地將各生物處理槽内之pH作成於6〜8之範圍者 為較佳。依據處理對象之刪成分的_，槽内之阳 動的情形’但於此情形’使用氫氧化納或鹽酸、硫酸等， 將槽内之pH控制於上述範圍内者為較佳。 通常之排水中含有 的必要，但於使核 一般於污泥之微粒化上核為必要。 成為如此核的微粒子，故並無特別添力 15 α 201223885 形成促進的觀點，添加Fe2+、 使氫氧化物形成者為較佳。X，e +、Ca2' Mg+等之離子 無氧生物處理槽Η)者為較佳杨Fe2、情形，添加於 外’可促進無氧狀態。 此’除了核之促進形成 較佳。據此，嫌氣性細菌的 ^，，、'氣生物處理槽1〇者為 變的容易增殖，而良好地保持I於無氧生物處 理槽ίο; 本實施形態對於增容的抑制：大二： 制，一般認為將環境作成使 .、'、有政。於增容之抑 擇性增殖的環境為有效的。的絲狀微生物難以選 之 狀態排除無耐受性的絲=生t為2基質濃度 .濃度梯度或叙餓狀態等的方法稱 導入基質： 將為了使絲狀微生物如攝 ，、無氧及嫌氣等之環境變化的方法將_代謝性= 子 u—selection)(參照非專利文獻ι)。本實施形態 因將生物>5泥作成無氧狀態或域狀態，成為動力學選揭 及代謝性選擇之作用容易作動的環境，故可抑制增容。 [實施例] s 以下’舉例實施例以更具體詳細地說明本發明，但本 發明並未限定於以下之實施例。 使用如第1圖所示的排水處理農置1 (無氧生物處理槽 10之容積10L、第一生物處理槽12之容積30L、第二生物處 理槽14之容積40L)，將工業水中有機性BOD成分進行以 BOD130〜300mg/L之任意濃度稀釋的被處理水之生物處 201223885 理。被處理水被連續地供給至第一生物處理槽12〇將標準 活性污泥法所使用的污泥作為種污泥來使用。馴養後， MLSS負荷之控制經由流量變化來進行。 無氧生物處理槽1〇係僅進行藉由攪拌機之攪拌，試驗 期間中，將D〇維持低於lmg/L·。第一生物處理槽12及第二 生物處理槽14係進行藉由散氣管的空氣曝氣，試驗期間 中’將D〇維持於5〜8mg/L之範圍。 水溫並未特別控制而於室溫下進行，試驗期間中，於 25〜28°C之範圍内推移。 將自污泥分離槽16所排出的全體污泥流量設定為供 給至第生物處理槽12被處理水之流量的相同量。又，將 供給於無氧生物處理槽1〇的污泥流量及供給於第二生物 處理槽14的污泥流量之比例調整為3 : 10。經由物質收支 而各槽之MLSS濃度比例被決定，因全體污泥流量係與被 處理水之流4成比例而以同樣之比例上升，故試驗期間中 飽食狀態相對於⑽狀態之關（飽食狀態/#1餓狀態之 比例）被固定於約0.34。 亏/匕刀離槽16水表面積負荷為〇 2m/h〜2.0m/h之範圍。 ^驗期㈤中，被處理水之BqD濃度及自污泥分離槽Μ 所獲得的最終處理水之BQD濃度、各敎MLss濃度、第 一生物處理槽12及第二生物處理槽14之MLSS負荷、成為 污泥沉降性指標之SVI3G(僅第二生物處理槽14)、第—生物 、無氧生_ 夺曰Η中央値）讀表1。又，於第3圖顯示各試驗期 17 201223885 間中的污泥粒徑分布。 [表1] MLS [m S濃度 g/L] BOD-MLSS 負荷 [kgBOD/kgMLSS/ d] 實際滯留時間[h] (包含送回流量） SVI30 [ml/g] 水質 [mgBOD/Ll 條件 期間 第一生 物處理 槽 第二生 物 處理槽 第一生 物處理 槽 第二生物 處理槽 第一 + 第二 生物處 理槽 無氧生物處 理槽 第二生 物 處理槽 被 處 理 水 污泥 分離 槽處 理水 種污 泥 一 _ 160 I 0-10 日 780 1100 0.35 0.04 17.9 6.0 120 130 未檢 測出 Π 10-20 日 760 1200 0.77 0.07 8.8 5.8 41 130 未檢 測出 m 20-30 日 1300 2200 1.84 0.18 2.5 1.5 36 180 未檢 測出 IV 30-40 曰 2800 5300 1.75 0.19 1.8 1.4 78 240 未檢 測出 V 40-50 日 2000 4700 1.94 0.14 3.2 4.1 48 310 未檢 測出 如表1所示’由試驗開始至第10日，將第一生物處理 槽12中MLSS負荷設定為〇.3kgBOD/kgMLSS/d，將第二生 物處理槽14 + MLSS負荷設定為〇 〇4kgB〇DkgMLSS/d。於 此試驗期間之SVI30，與種污泥作比較為降低，污泥之沉 降丨生提升。然而，如第3圖所示，於此試驗期間之粒度分 布與種污泥作比較並無大變化，無法認作微粒形成。以 MLSS負荷OJkgBOD/kgMLSS/d，係難以使第一生物處理 槽之生物污泥變成充分的飽食狀態，上述試驗期間（ 日間）中’認為生物污泥之微粒化不會發生。 減驗開始10日後〜20日，使被處理水之流入流量增加 18 201223885 而將第一生物處理槽12中MLSS負荷設定為 0.8kgBOD/kgMLSS/d。如表1所示，於此試驗期間之svi3〇 與種污泥作比較係大幅降低。又，如第3圖所示，於此試 驗期間之粒徑與種污泥作比較會變大，可謂生物污泥之微 粒化係進行中。 試驗開始20日後〜30日，使被處理水之流入水量、被 處理水之BOD濃度增加而設定第一生物處理槽12中MLSS 負荷為1.8kgBOD/kgMLSS/d。如表1所示，於此試驗期間 之SVI3 0係維持與試驗開始1 〇日後〜2〇日之試驗期間同樣 的低値。又，如第3圖所示，於此試驗期間，粒子徑進一 步變大。將此試驗期間之生物污泥以電子顯微鏡觀察的結 果，形成直徑約200μπι之微粒。The range below OkgBOD/kg MLSS/d~0.5kgBOD/kgMLSS/d is preferred. When there are many unreacted b〇d components flowing from the first biological treatment tank 12, the MLSS load in the second biological treatment tank 14 may exceed 0.5 kg BOD/kg MLSS/d. When the load of the second biological treatment tank 14*mlss exceeds 0.5 kg BOD/kg MLSS/d, the high MLSS load is continuously applied through the first biological treatment tank 12, so that the possibility of micromass-induced compatibilization from the biological sludge may occur. Sexual improvement situation. Next, the drain (also containing sludge) treated by the second biological treatment tank 14 is continuously introduced into the sludge separation tank 16 through the drain inflow line 18c. In the sludge separation tank 16, the sewage discharged from the second biological treatment tank 14 is sedimented and separated by the biological sludge. Further, the separated sludge of the biological sludge is discharged as treated water from the treated water discharge line 22. The biological sludge that has been centrifuged in the sludge separation tank 16 is supplied from the sludge return line 20a to the anaerobic biological treatment tank 10' and is supplied to the second biological treatment tank from the sludge return line 2〇b. 14. In the case of adjusting the amount of sludge returned, it is preferable to install a pump or the like in the sludge return line 2〇a or the like. Further, the sludge separation tank 16 is not limited to sedimentation separation, and may be, for example, membrane separation. In the anaerobic biological treatment tank 10, the microorganisms such as denitrifying bacteria and the biological sludge supplied from the sludge separation tank 16 are subjected to conversion of the nitrogen-containing substance in the anaerobic biological treatment tank 1〇11 201223885 into nitrogen gas. The gas ίο is treated by the organism as described above (7). At the time of the scramble, the inside of the tank is smeared and becomes anaerobic. Further, the anaerobic biological treatment tank 10 has a biological degree of 5, which is preferable. The organism supplied from the sludge separation tank 16 is consumed for a short period of time, and is consumed by the breathing, and the retention time of the biological sludge which cannot be maintained by == does not pass through the internal anaerobic biological treatment tank 1 Indeed accompanied by more than 3 two. The biological sludge treated in the anaerobic state is continuously supplied to the first biological treatment tank 12 from the stain 20c. e, =τ anaerobic biological treatment tank _ can be anaerobic. That is, the anaerobic biological treatment tank) may be an septic tank. The smoldering tank is carried out under the suffocating state, and the sputum (four) leaven. In the state of the towel, only the dissolved oxygen is not present. The condition that oxygen from Yalai or nitric acid does not exist. In the case of a gas tank, it is necessary to add a part of the drain to the gas tank because of the organic matter in the reaction process, and it is necessary to add the organic matter in the drain. However, when a part of the drainage water flows in, the residence time of the drainage in the septic tank becomes short, and it is necessary to ensure the residence time. In this manner, when the biological sludge is circulated through the first biological treatment tank 12 in the saturated state, the first biological treatment tank 14 in the hunger state, and the anaerobic biological treatment tank in the anaerobic state, biological sludge occurs. Micronization can improve the sedimentation of biological sludge. As a result, it is possible to increase the processing speed of the drainage. In addition, sludge sedimentation management, which is important in the management of activated sludge, is easy. The following describes the preferable conditions and the like in the microparticulation of sludge. As shown in Fig. 2, in the case of the batch type activated sludge method, in the initial stage of the reaction in the reaction step 12 201223885, the concentration of B〇D in the reaction tank becomes a high satiety state, but the BOD component proceeds with decomposition, and the reaction tank The concentration of b〇d inside will decrease and migrate to starvation. In the improvement of the sedimentation property of the sludge, the micronization of the sludge, and the like, in addition to the step of the anaerobic state after that, it is considered that the time of the hunger state is relatively long relative to the satiety state. The optimum ratio of this ratio is considered to vary depending on the BOD component of the subject, but in most cases, it is necessary that the hungry state is longer than the satiety state. In the present embodiment, the first biological treatment tank 12 that satisfies the range of the MLSS load described above is in a satiety state, and the second biological treatment tank 14 is in a starved state. Therefore, the ratio of the saturated state to the state of starvation (satisfying state/starvation state) is less than 1, the amount of sludge returned and the volume of the first biological treatment tank 12 and the second biological treatment tank 14 are designed to be Desperate. In the case of the batch type activated sludge method, the reaction occurs in the same reaction tank, so the amount of MLSS in the saturated state and the starvation state is the same. Therefore, the ratio of the satiety state to the hunger state (satisfaction state/starvation state) is corresponding to the time of the satiety state and the time of the starvation state. On the other hand, in the case of the continuous activated sludge method, since the tanks in the saturated state and the starved state are different, the amount of MLSS retained is different. Therefore, the ratio of the satiety state to the starvation state is calculated as follows. [Number 1] Sludge holding amount of the first biological treatment tank (volume xMLSS concentration) [g] x residence time [h] sludge holding amount of the second biological treatment tank (volume xMLSS concentration) [g] x residence time [ h] 13 201223885 In addition, in the secondary activated sludge process, it is known that the interval between the starvation state and the saturated state is also a necessary factor for the micronization of biological sludge. In general, it is known that the shorter the cycle interval between the starved state and the saturated state, the more difficult it is to atomize the biological sludge. The same is true for the continuous activated sludge process. In the present embodiment, the first biological treatment tank 12 and the second biological treatment tank are provided in the biological treatment tank 12 and the second biological treatment tank 14 so that the total residence time of the water to be treated is at least three hours or more. The volume, the treated flow rate, and the return of the sludge flow rate are not expected to be shortened in the cycle of starvation and satiety. From the viewpoint of micronizing the biological sludge, the first biological treatment tank 12 and the second biological treatment tank 14 are each divided into a plurality of portions, and the wastewater containing the BOD component is caused to flow into the divided first biological treatment tank 12, respectively. It is preferred that each of the second biological treatment tanks 14 supplied to the divided biological sludge is supplied. In the case where the biological treatment tank is divided, it is preferable that the volume in the at least one of the biological treatment tank 12 and the second biological treatment tank 14 satisfies the preferable conditions for the atomization of the biological sludge. The flow rate of the entire sludge discharged from the sludge separation tank 16 and the flow rate of the sludge flowing into the anaerobic biological treatment tank 10 are set to ensure a saturated state in the first biological treatment tank relative to the aforementioned second biological treatment tank The ratio of the state of starvation (satisfying state/starvation state) is preferably a mode in which the residence time of the anaerobic biological treatment tank is less than 3 G minutes. For example, when the flow rate of the sludge flowing into the anaerobic biological treatment tank 10 is increased, the residence time of the anaerobic biological treatment tank 10 and the first biological treatment tank 12 is continuously decreased, and the MLSS concentration of the first biological treatment tank 12 is lowered. When the sludge flow rate to the anaerobic biological treatment tank 201223885 10 is reduced, the residence time of the anaerobic biological treatment tank 10 and the first biological treatment tank 12 continues to increase, and the MLSS concentration of the first biological treatment tank 12 rises. When the total sludge flow rate is increased, the residence time of the anaerobic biological treatment tank 10, the first biological treatment tank 12, and the second biological treatment tank 14 is reduced, and the MLSS concentration in the first biological treatment tank 12 is increased while the second organism The concentration of MLSS in the treatment tank 14 also rises. When the total sludge flow rate is reduced, the residence time of the anaerobic biological treatment tank 10, the first biological treatment tank 12, and the second biological treatment tank 14 is increased, and the concentration of MLSS in the first biological treatment tank 12 is increased while the second organism The concentration of MLSS in the treatment tank 14 also rises. By the operation of returning the flow rate in this way, the residence time of the anaerobic biological treatment tank 1 , the first biological treatment tank 12 and the second biological treatment tank 14 , the MLSS concentration in the first biotin treatment tank 12 , and the second organism can be made. In the treatment tank, the concentration of the ^^ is changed, so that it is possible to arbitrarily control the ratio of the saturated state to the state of the hungry state. The continuous activated sludge method of the present embodiment is different from the batch activated sludge method. The anaerobic state, the saturated state, and the starvation state, which are important factors in the micronization of the biological sludge, can be arbitrarily controlled to be possible points by the operation of returning the flow rate. About the pH in each biological treatment tank and Although it is not particularly specified, it is preferable to set the pH in each biological treatment tank to a range of 6 to 8 in the same manner as in the case of the usual activated sludge. Depending on the composition of the treatment target, the positive movement in the tank 'but In this case, it is preferred to use sodium hydroxide, hydrochloric acid, sulfuric acid, etc., to control the pH in the tank to the above range. Usually, the water is contained in the drainage, but the core is generally micronized on the sludge. As necessary. In order to be such a nuclear microparticle, there is no particular point of view on the formation of 15 α 201223885, and it is preferable to add Fe 2+ to form a hydroxide. The ion anaerobic biological treatment tank of X, e + , Ca 2 ' Mg + or the like is preferable. In the case of a better Yang Fe2, the addition of 'external' can promote an anaerobic state. This is better than the promotion of the nucleus. According to this, the qi of the anaerobic bacteria is one, In order to change easily, it is good to maintain I in the anaerobic biological treatment tank. In this embodiment, the suppression of compatibilization: the sophomore: system, it is generally considered that the environment is made to make ., ', have politics. The environment of selective proliferation is effective. The filamentous microorganisms are difficult to select and exclude the untolerant silk = raw t is 2 matrix concentration. The concentration gradient or the state of hunger is called the introduction matrix: The method of changing the environment such as taking in microorganisms, such as anaerobic and anaerobic, is _metabolism = sub-selection (see Non-Patent Document 1). In this embodiment, the biological > 5 mud is made into an anaerobic state or Domain state, becoming a dynamic selection and metabolic choice In the environment where it is easy to operate, the compatibilization can be suppressed. [Examples] s The following examples will be described in more detail, but the present invention is not limited to the following examples. The drainage treatment farm 1 (the volume of the anaerobic biological treatment tank 10 is 10 L, the volume of the first biological treatment tank 12 is 30 L, and the volume of the second biological treatment tank 14 is 40 L), and the organic BOD component in the industrial water is BOD 130 to 300 mg. The biological substance of the treated water diluted at any concentration of /L is 201223885. The treated water is continuously supplied to the first biological treatment tank 12, and the sludge used in the standard activated sludge method is used as the seed sludge. After that, the control of the MLSS load is performed by the flow rate change. The anaerobic biological treatment tank 1 was only stirred by a stirrer, and D〇 was maintained below 1 mg/L· during the test period. The first biological treatment tank 12 and the second biological treatment tank 14 perform air aeration by a diffusing pipe, and maintain D〇 in the range of 5 to 8 mg/L during the test period. The water temperature was carried out at room temperature without special control, and it was changed within the range of 25 to 28 °C during the test. The total sludge flow rate discharged from the sludge separation tank 16 is set to the same amount as the flow rate of the treated water to the biological treatment tank 12. Further, the ratio of the sludge flow rate supplied to the anaerobic biological treatment tank 1 and the sludge flow rate supplied to the second biological treatment tank 14 was adjusted to 3:10. The ratio of the MLSS concentration of each tank is determined by the material balance, and the total sludge flow rate is increased in the same proportion as the flow 4 of the treated water, so that the satiety state is relative to the (10) state during the test period (satisfaction) The ratio of the state / #1 hungry state is fixed at about 0.34. The water surface area load of the deficient/sickle from the tank 16 is in the range of 〇 2m/h to 2.0m/h. In the test period (5), the BqD concentration of the treated water and the BQD concentration of the final treated water obtained from the sludge separation tank, the concentration of each MLss, the MLSS load of the first biological treatment tank 12 and the second biological treatment tank 14 SVI3G (only the second biological treatment tank 14), the first biological, and the anaerobic raw _ 曰Η 曰Η 曰Η 成为 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 Further, in Fig. 3, the particle size distribution of the sludge in each test period 17 201223885 is shown. [Table 1] MLS [m S concentration g/L] BOD-MLSS Load [kgBOD/kgMLSS/d] Actual residence time [h] (including return flow) SVI30 [ml/g] Water quality [mgBOD/Ll condition period a biological treatment tank second biological treatment tank first biological treatment tank second biological treatment tank first + second biological treatment tank anoxic biological treatment tank second biological treatment tank treated water sludge separation tank treatment water sludge one _ 160 I 0-10 780 1100 0.35 0.04 17.9 6.0 120 130 Not detected Π 10-20 760 1200 0.77 0.07 8.8 5.8 41 130 Not detected m 20-30 Day 1300 2200 1.84 0.18 2.5 1.5 36 180 Not detected IV 30-40 曰2800 5300 1.75 0.19 1.8 1.4 78 240 Not detected V 40-50 Day 2000 4700 1.94 0.14 3.2 4.1 48 310 Not detected as shown in Table 1 'From the beginning of the test to the 10th day, the first creature will be The MLSS load in the treatment tank 12 was set to 〇3 kgBOD/kg MLSS/d, and the second biological treatment tank 14 + MLSS load was set to 〇〇4 kg B 〇 Dkg MLSS/d. During the test period, SVI30 was reduced compared with the sludge, and the sedimentation of the sludge was increased. However, as shown in Fig. 3, the particle size distribution during the test did not change much from the seed sludge and could not be considered as particle formation. With the MLSS load of OJkgBOD/kgMLSS/d, it is difficult to make the biological sludge of the first biological treatment tank into a sufficient saturated state, and in the above test period (daytime), it is considered that the micronization of the biological sludge does not occur. From the 10th to the 20th day after the start of the test, the inflow flow rate of the treated water is increased by 18 201223885 and the MLSS load in the first biological treatment tank 12 is set to 0.8 kg BOD/kg MLSS/d. As shown in Table 1, the comparison between svi3〇 and seed sludge during this test was greatly reduced. Further, as shown in Fig. 3, the particle size during the test period is increased as compared with the seed sludge, and the micronization system of the biological sludge is in progress. From the 20th to the 30th day after the start of the test, the inflow water amount of the water to be treated and the BOD concentration of the water to be treated are increased to set the MLSS load in the first biological treatment tank 12 to 1.8 kg BOD/kg MLSS/d. As shown in Table 1, the SVI3 0 during the test period was maintained at the same level as the test period of 1 to 2 days after the start of the test. Further, as shown in Fig. 3, during this test, the particle diameter further increased. The biological sludge during the test was observed by an electron microscope to form particles having a diameter of about 200 μm.
試驗開始30日後〜40日，將第一生物處理槽12之MLSS 負荷設定為1.8kgBOD/kgMLSS/d，配合MLSS漢度之上 昇，使被處理水之流入水量增加下，將第一生物處理槽12 與第二生物處理槽14之滞留時間總計設定為丨，8 h。其結果 如表1所示，於此試驗期間之SVI30，與試驗開始後日後 〜30日試驗期間作比較為上升的。試驗開始3〇日後〜4〇曰試 驗期間之生物污泥以電子顯微鏡觀察的結果，雖試驗開始 20曰後〜30日試驗期間所形成的微粒被維持，但其周圍會 附著集團。此附著的集團被認為是生物污泥之沉降性惡;匕 的原因。 忒驗開始40日後〜5〇日’將被處理水之濃度之稀 釋比例變更為30Gmg/L，使被處理水之流人水量減少，將 201223885 第一生物處理槽12之MLSS負荷設定為 1.9kgBOD/kgMLSS/d ’將第一生物處理槽12與第二生物處 理槽14之滯留時間之總計設定為3.2h。其結果，如表1所 示，試驗開始30日後〜40日之試驗期間中，上昇的SVI30 於此試驗期間會降低，可見生物污泥沉降性的改善傾向。 試驗開始40日後〜50日試驗期間之生物污泥以電子顯微鏡 觀察的結果’試驗開始30日後〜40日試驗期間中附著微粒 的集團會減少。 如以上所述，將第一生物處理槽12中MLSS負荷設定 為0.31<:名3〇〇/1^1^88/4’將第二生物處理槽14中]^1^8負 荷設定為0.04kgBODkgMLSS/d的情形，雖然污泥之沉降性 提升，但10日間之試驗期間中，不會發生生物污泥之微粒 化。而且，使第一生物處理槽12中]VILSS負荷上升至 0.8kgBOD/kgMLSS/d以上時，發生所謂1〇日間的短期間的 生物污泥之微粒化。又，第一生物處理槽12與第二生物處 理槽14滯留時間之總計為低時，微粒之周圍附著集團，有 生物污泥之沉降性降低的情形。 其次’使用新的相同之種污泥，基於省略第1圖之無 氧生物處理槽10，啟動至第一生物處理槽12中MLS S負荷 成為l.4kgBOD/kgMLSS/d、第二生物處理槽14中MLSS負 荷成為0.1kgBODkgMLSS/d，此負荷下進行2〇曰間之運 轉。此時污泥之狀況以電子顯微鏡觀察的結果，因應啟動 而可見污泥之微粒化，但20日間之運轉中可見多量的微小 動物增殖，由此，微粒會被破壞。20日間運轉後之結果整 201223885 理於表2。如表2所示，SVI30與微粒化的條件比較 南的値。 之後’附加無氧生物處理槽1〇,未變更負荷條件下進 行10日間之運轉。10日間運轉後之結果整理於表2'。如表2 所示’ 10日間之運轉後之SVI3G，與省略無氧生物處理槽 10的情_比，會大幅降低。此時污泥之狀況以電子顯微 鏡觀察的結果，可見微小動物之減少，又形成直經約 200μηι之微粒。由此結果，認為無氧生物處理槽丨^對微粒 化有大的貢獻。 )” [表2] MLSS [m& 濃度 BOD-MI [kgBOD/1 d AS負荷 cgMLSS/ ] 實際滞留時間[h] (含送回流詈） —-— SVI30 [ml/g] 水質[mgBOD/U 條件 第一生物 處理槽 第二生 物 處理槽 第一生 物處理 槽 第二生 物 處理槽 第一+第 生物處理 槽 無氧生物 處理槽 第二生物 處理槽 被處 理水 ~~------- 污泥分離 去岳由IfR 種污泥 - - - - - - 160 1—----- 200 — 200 T苜处埋水 没有無 氧槽 1800 4400 1.4 0.1 3.9 ------ 62 未檢測^ 未檢測出 有無氧 槽 1800 4400 1.4 0.1 3.9 4.4 36 〜 」 【圖式簡單説明】 [第1圖]為顯示本實施形態有關之排水處理裝置之一 例的概略構成圖。 [第2圖]為顯示批次式活性污泥法中的i批次之Β 〇 D遭 度與時間之關係圖。 [第3圖]為顯示實施例之各試驗期間中的污泥粒徑分 21 201223885 布。 【主要元件符號説明】 1 排水處理裝置 10 無氧生物處理槽 12 第一生物處理槽 14 第二生物處理槽 16 污泥分離槽 18a〜18c 排水流入管線 20a~20c 污泥送回管線 22 處理水排出管線 2230 days after the start of the test, the MLSS load of the first biological treatment tank 12 is set to 1.8 kg BOD/kg MLSS/d, and the MLSS Han degree is increased to increase the inflow water volume of the treated water, and the first biological treatment tank is added. The total residence time of 12 and the second biological treatment tank 14 is set to 丨, 8 h. The results are shown in Table 1. The SVI30 during the test period was increased in comparison with the test period after the start of the test and the 30-day test period. As a result of observing the biological sludge from the start of the test for 3 days to 4 weeks after the test, the particles formed during the test period from 20 pm to 30 days after the start of the test were maintained, but the group was attached around it. This attached group is considered to be the cause of sedimentation of biological sludge; After 40 days from the start of the test, the dilution ratio of the concentration of the treated water is changed to 30 Gmg/L, and the amount of water in the treated water is reduced. The MLSS load of the first biological treatment tank 12 of 201223885 is set to 1.9 kg BOD. /kgMLSS/d 'The total of the residence time of the first biological treatment tank 12 and the second biological treatment tank 14 is set to 3.2 h. As a result, as shown in Table 1, in the test period from 30 days to 40 days after the start of the test, the rising SVI30 was lowered during the test period, and the sedimentation property of the biological sludge tends to be improved. The results of observing the biological sludge by electron microscopy from the 40th day to the 50th day after the start of the test were reduced by 30 days after the start of the test and 40 minutes after the test. As described above, the MLSS load in the first biological treatment tank 12 is set to 0.31 <:name 3〇〇/1^1^88/4', and the load in the second biological treatment tank 14 is set to In the case of 0.04 kg of BODkg MLSS/d, although the sedimentation property of the sludge was improved, the micronization of the biological sludge did not occur during the test period of 10 days. Further, when the VILSS load in the first biological treatment tank 12 is increased to 0.8 kgBOD/kg MLSS/d or more, the so-called microbialization of the biological sludge in a short period of time is caused. When the total amount of residence time of the first biological treatment tank 12 and the second biological treatment tank 14 is low, the group is adhered to the periphery of the fine particles, and the sedimentation property of the biological sludge is lowered. Next, 'using the new same type of sludge, based on the anaerobic biological treatment tank 10 omitted in Fig. 1, the MLS S load to the first biological treatment tank 12 is changed to 1.4 kg BOD/kg MLSS/d, and the second biological treatment tank The MLSS load in 14 is 0.1 kg BODkg MLSS/d, and the operation is performed at 2 Torr under this load. At this time, the state of the sludge was observed by an electron microscope, and the sludge was micronized in response to the start-up. However, during the 20-day operation, a large amount of microscopic animals were observed to proliferate, and the particles were destroyed. The result of the operation after the 20th day is 201223885. As shown in Table 2, SVI30 is compared with the conditions of micronization. Thereafter, the anaerobic biological treatment tank was attached 1 Torr, and the operation was carried out for 10 days without changing the load. The results after 10 days of operation are summarized in Table 2'. As shown in Table 2, the SVI3G after the operation of the 10th day is greatly reduced compared with the case where the anaerobic biological treatment tank 10 is omitted. At this time, the state of the sludge was observed by electron microscopy, and it was found that the microscopic animals were reduced, and the particles of about 200 μm were formed. As a result, it is considered that the anaerobic biological treatment tank has a large contribution to the micronization. ) [Table 2] MLSS [m& Concentration BOD-MI [kgBOD/1 d AS load cgMLSS/] Actual residence time [h] (including return reflux) —-— SVI30 [ml/g] Water quality [mgBOD/U Condition first biological treatment tank second biological treatment tank first biological treatment tank second biological treatment tank first + biological treatment tank anaerobic biological treatment tank second biological treatment tank treated water ~~------- Sludge separation to Yue by IfR seed sludge - - - - - - 160 1—----- 200 — 200 T苜 buried water without anaerobic tank 1800 4400 1.4 0.1 3.9 ------ 62 Not detected ^ The anaerobic tank is not detected. 1800 4400 1.4 0.1 3.9 4.4 36 〜 ” [Brief Description] [Fig. 1] is a schematic configuration diagram showing an example of the wastewater treatment apparatus according to the present embodiment. [Fig. 2] is a graph showing the relationship between the degree of Β D and the time of the i batch in the batch type activated sludge method. [Fig. 3] is a graph showing the sludge particle size in each test period of the example 21 201223885. [Description of main components] 1 Drainage treatment device 10 Oxygen-free biological treatment tank 12 First biological treatment tank 14 Second biological treatment tank 16 Sludge separation tanks 18a to 18c Drainage inflow lines 20a to 20c Sludge return line 22 Treatment of water Discharge line 22