TWI633067B - Method and device for treating organic drainage - Google Patents

Method and device for treating organic drainage Download PDF

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TWI633067B
TWI633067B TW103106258A TW103106258A TWI633067B TW I633067 B TWI633067 B TW I633067B TW 103106258 A TW103106258 A TW 103106258A TW 103106258 A TW103106258 A TW 103106258A TW I633067 B TWI633067 B TW I633067B
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小松和也
赤崎和
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栗田工業股份有限公司
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    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/346—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from semiconductor processing, e.g. waste water from polishing of wafers
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract

本發明目的在於對有機性排水，以厭氧性生物處理、好氧性生物處理、凝集處理及浮上或沉降分離、RO膜分離進行處理時，藉好氧性生物處理確實去除厭氧性生物處理中所生成的鹼度，減少凝集、固液分離所需之凝集劑用量，並且降低其後之RO膜的鹽類負載。透過以好氧性生物處理，在pH5.5~6.5之條件下，利用附著於載體的好氧性微生物，以貫流式進行處理，而藉好氧性生物處理確實去除厭氧性生物處理中所生成的鹼度。 The purpose of the present invention is to remove organic anaerobic biological treatment with anaerobic biological treatment, aerobic biological treatment, agglutination treatment, floating or sedimentation separation, and RO membrane separation when using organic aerobic biological treatment. The alkalinity generated in the process reduces the amount of coagulant required for agglomeration and solid-liquid separation, and reduces the salt load of the subsequent RO membrane. By aerobic biological treatment, under the condition of pH 5.5 ~ 6.5, the aerobic microorganisms attached to the carrier are used to perform the cross-flow treatment, and the aerobic biological treatment does remove the anaerobic biological treatment. The resulting alkalinity.

Description

有機性排水之處理方法及處理裝置 Method and device for treating organic drainage

本發明係有關於對有機性排水進行處理之方法及裝置，特別係有關於對有機性排水進行生物處理後，進一步進行逆滲透膜分離處理之方法及裝置。 The present invention relates to a method and a device for treating organic drainage, and more particularly to a method and a device for further performing reverse osmosis membrane separation treatment after biologically treating organic drainage.

近年來，水資源的回收再利用漸受重視，而積極進行排水的處理及回收。尤其是，由於超過濾(UF)膜或逆滲透(RO)膜所代表的具微細孔徑的膜分離裝置亦可去除高分子量之有機物質，可得高品質之處理水質，而經廣泛使用。此等膜分離裝置，因為膜的孔徑較小，當流入之有機物質濃度上升時，在膜面即易累積有機物質，致過濾阻力顯著上升，而不易注水。在此種情況下，在膜分離裝置的前段設置生物處理裝置，而於膜分離處理前先降低排水中的有機物質濃度，在穩定處理方面係屬有效。 In recent years, the recycling and reuse of water resources have been paid more and more attention, and the drainage treatment and recycling have been actively carried out. In particular, since a membrane separation device having a fine pore size represented by an ultrafiltration (UF) membrane or a reverse osmosis (RO) membrane can also remove high-molecular-weight organic substances and obtain high-quality treated water, it is widely used. In these membrane separation devices, because the pore diameter of the membrane is small, when the inflowing organic substance concentration rises, it is easy to accumulate organic substances on the membrane surface, resulting in a significant increase in filtration resistance, and it is not easy to inject water. In this case, a biological treatment device is provided in the front stage of the membrane separation device, and the concentration of organic substances in the drainage is reduced before the membrane separation treatment, which is effective in terms of stable treatment.

以往，對於在RO膜分離的前段進行生物處理而言，專利文獻1中提出一種對有機性排水，以厭氧性生物處理、好氧性生物處理、凝集處理及浮上或沉降分離、 RO膜分離依序進行處理的方法。 Conventionally, for the biological treatment in the first stage of RO membrane separation, Patent Document 1 proposes an organic drainage, an anaerobic biological treatment, aerobic biological treatment, agglutination treatment, and floating or sedimentation separation, RO membrane separation sequential processing method.

於此方法中，藉由將較少生成汙染RO膜之生物代謝產物的厭氧性生物處理應用於好氧性生物處理的前處理，RO膜汙染減少，可長期持續進行穩定的處理。 In this method, by applying an anaerobic biological treatment that generates less biological metabolites that pollute the RO membrane to the pretreatment of the aerobic biological treatment, the RO membrane pollution is reduced, and stable treatment can be continued for a long time.

專利文獻1之方法中，存有以下之不良情形。即，厭氧性生物處理過程中所生成的鹼度在經過好氧性生物處理後仍殘留，因該鹼度使凝集劑被消耗，以致凝集、固液分離所需之凝集劑添加量增大。其結果，過程中產生的汙泥量增加，同時RO膜的鹽類負載亦增加，使得透過水量降低。 The method of Patent Document 1 has the following disadvantages. That is, the alkalinity generated during the anaerobic biological treatment process still remains after the aerobic biological treatment. Because of this alkalinity, the agglutinating agent is consumed, so that the amount of the agglutinating agent required for agglutination and solid-liquid separation increases. . As a result, the amount of sludge generated in the process increases, and the salt load of the RO membrane also increases, which reduces the amount of permeated water.

[先前技術文獻] [Prior technical literature] [專利文獻] [Patent Literature]

[專利文獻1]日本特開2007-175582號公報 [Patent Document 1] Japanese Patent Laid-Open No. 2007-175582

本發明係以解決上述專利文獻1之方法的問題，而提供一種可藉好氧性生物處理確實去除厭氧性生物處理中所生成的鹼度，減少凝集、固液分離所需之凝集劑用量，並且降低其後之RO膜的鹽類負載的有機性排水之處理方法及處理裝置為課題。 The present invention is to solve the problem of the method of the above patent document 1, and provides an aerobic biological treatment to reliably remove the alkalinity generated in the anaerobic biological treatment and reduce the amount of coagulant required for agglutination and solid-liquid separation. In addition, a method and a device for reducing the organic salt drainage of the subsequent RO film to support the organic wastewater are the subject.

本發明人等為解決上述課題而重複進行研究的結果發現，藉由在好氧性生物處理中使用載體，同時控制pH條件並以貫流式進行處理，可藉好氧性生物處理確實去除厭氧性生物處理中所生成的鹼度。 As a result of repeated studies by the present inventors in order to solve the above-mentioned problems, it was found that by using a carrier in aerobic biological treatment, while controlling the pH condition, and processing in a cross-flow manner, anaerobic biological treatment can be reliably removed by aerobic biological treatment. Alkalinity generated during sexual biological treatment.

本發明係基於此種見解而達成者，其要旨如下： The present invention has been achieved based on such insights, and the gist thereof is as follows:

[1]一種有機性排水之處理方法，其係具有：厭氧性生物處理步驟，對有機性排水在厭氧下進行生物處理；好氧性生物處理步驟，對從該厭氧性生物處理步驟流出的厭氧性生物處理水在好氧下進行生物處理；固液分離步驟，對從該好氧性生物處理步驟流出的好氧性生物處理水添加凝集劑使其凝集後進行固液分離；及逆滲透膜分離步驟，對該固液分離步驟中所分離的分離水進行處理的有機性排水之處理方法，其特徵為：該好氧性生物處理步驟係在pH5.5~6.5之條件下，利用附著於載體的好氧性微生物，以貫流式進行處理的步驟。 [1] An organic wastewater treatment method, which includes: an anaerobic biological treatment step, which performs biological treatment on organic wastewater under anaerobic conditions; an aerobic biological treatment step, which steps from the anaerobic biological treatment step The outflowing anaerobic biologically treated water is biologically treated under aerobic conditions; in the solid-liquid separation step, an aggregating agent is added to the aerobic biologically treated water flowing out of the aerobic biologically treating step to cause agglutination to perform solid-liquid separation; And a reverse osmosis membrane separation step, an organic drainage treatment method for treating the separated water separated in the solid-liquid separation step, characterized in that the aerobic biological treatment step is under the conditions of pH 5.5 to 6.5 , Using aerobic microorganisms attached to the carrier, the process of cross-flow processing.

[2]如[1]之有機性排水之處理方法，其中前述好氧性生物處理步驟中的pH條件為pH5.8~6.3。 [2] The method for treating organic wastewater according to [1], wherein the pH condition in the aerobic biological treatment step is pH 5.8 to 6.3.

[3]如[1]或[2]之有機性排水之處理方法，其係在前述好氧性生物處理步驟中，將前述厭氧性生物處理水裝入好氧性生物處理槽，在好氧下進行生物處理之方法，其中前述載體為海綿載體，該好氧性生物處理槽之載體填充率為10~50%。 [3] The treatment method of organic drainage as in [1] or [2], which is in the aforementioned aerobic biological treatment step, and the aforementioned anaerobic biological treatment water is charged into the aerobic biological treatment tank. In the method for biological treatment under oxygen, the aforementioned carrier is a sponge carrier, and the carrier filling rate of the aerobic biological treatment tank is 10-50%.

[4]如[1]至[3]中任一項之有機性排水之處理 方法，其中前述凝集劑為鐵系凝集劑。 [4] Treatment of organic drainage as in any of [1] to [3] The method, wherein the agglutinating agent is an iron-based agglutinating agent.

[5]如[4]之有機性排水之處理方法，其中前述鐵系凝集劑為氯化鐵，以FeCl3(38%)之添加量計，其添加量為30~80體積ppm。 [5] The method for treating organic wastewater according to [4], wherein the aforementioned iron-based coagulant is ferric chloride, and the added amount is 30 to 80 vol ppm based on the added amount of FeCl 3 (38%).

[6]如[1]至[5]中任一項之有機性排水之處理方法，其係對前述分離水經過膜過濾的過濾水，在前述逆滲透膜分離步驟中進行處理。 [6] The method for treating organic drainage according to any one of [1] to [5], wherein the filtered water obtained by filtering the separated water through a membrane is treated in the aforementioned reverse osmosis membrane separation step.

[7]一種有機性排水之處理裝置，其係具有：厭氧性生物處理手段，對有機性排水在厭氧下進行生物處理；好氧性生物處理手段，對從該厭氧性生物處理手段流出的厭氧性生物處理水在好氧下進行生物處理；凝集劑添加手段，對從該好氧性生物處理手段流出的好氧性生物處理水添加凝集劑；固液分離手段，使添加有該凝集劑的水固液分離；及逆滲透膜分離手段，對該固液分離手段中所分離的分離水進行處理的有機性排水之處理裝置，其特徵為：該好氧性生物處理手段係在pH5.5~6.5之條件下，利用附著於載體的好氧性微生物，以貫流式進行處理的手段。 [7] An organic wastewater treatment device, which includes: anaerobic biological treatment means for biological treatment of organic drainage under anaerobic conditions; aerobic biological treatment means for the anaerobic biological treatment means The outflowing anaerobic biologically treated water is biologically treated under aerobic conditions; the agglutinating agent adding means adds an agglutinating agent to the aerobic biologically treated water flowing out of the aerobic biological treating means; the solid-liquid separation means The water-solid-liquid separation of the aggregating agent; and a reverse osmosis membrane separation means, an organic drainage treatment device for treating the separated water separated in the solid-liquid separation means, wherein the aerobic biological treatment means is Under the condition of pH 5.5 ~ 6.5, the method is used to process in a cross-flow manner by using aerobic microorganisms attached to the carrier.

[8]如[7]之有機性排水之處理裝置，其中前述好氧性生物處理手段中的pH條件為pH5.8~6.3。 [8] The organic wastewater treatment device according to [7], wherein the pH condition in the aforementioned aerobic biological treatment means is pH 5.8 to 6.3.

[9]如[7]或[8]之有機性排水之處理裝置，其中前述好氧性生物處理手段係盛裝前述厭氧性生物處理水並在好氧下進行生物處理的好氧性生物處理槽，前述載體為海綿載體，該好氧性生物處理槽之載體填充率為10~ 50%。 [9] The organic drainage treatment device according to [7] or [8], wherein the aerobic biological treatment means is an aerobic biological treatment that contains the aforementioned anaerobic biologically treated water and performs biological treatment under aerobic conditions The carrier is a sponge carrier, and the carrier filling rate of the aerobic biological treatment tank is 10 ~ 50%.

[10]如[7]至[9]中任一項之有機性排水之處理裝置，其中前述凝集劑為鐵系凝集劑。 [10] The organic wastewater treatment device according to any one of [7] to [9], wherein the agglutinating agent is an iron-based aggregating agent.

[11]如[10]之有機性排水之處理裝置，其中前述鐵系凝集劑為氯化鐵，以FeCl3(38%)之添加量計，其添加量為30~80體積ppm。 [11] The organic wastewater treatment device according to [10], wherein the aforementioned iron-based coagulant is ferric chloride, and the added amount is 30 to 80 vol ppm based on the added amount of FeCl 3 (38%).

[12]如[7]至[11]中任一項之有機性排水之處理裝置，其係具有對前述分離水進行膜過濾的膜過濾裝置，該膜過濾裝置之過濾水係在前述逆滲透膜分離手段中經處理。 [12] The organic drainage treatment device according to any one of [7] to [11], which is provided with a membrane filtration device for membrane filtration of the separated water, and the filtration water of the membrane filtration device is in the aforementioned reverse osmosis Processed in membrane separation means.

根據本發明，由於可藉在酸性條件下進行曝氣的好氧性生物處理確實去除厭氧性生物處理中所生成的鹼度，而能夠減少後段之凝集、固液分離所需之凝集劑添加量，其結果，可謀求產生汙泥量之減少、RO膜的鹽類負載之降低，得以進行有效的處理。 According to the present invention, since the aerobic biological treatment which can be aerated under acidic conditions can surely remove the alkalinity generated in the anaerobic biological treatment, it is possible to reduce the addition of agglutinating agent required for subsequent stage agglutination and solid-liquid separation. As a result, a reduction in the amount of sludge generated and a reduction in the salt load of the RO membrane can be achieved, and an effective treatment can be performed.

第1圖係表示本發明之有機性排水之處理裝置的實施形態的系統圖。 FIG. 1 is a system diagram showing an embodiment of an organic wastewater treatment device according to the present invention.

以下，就本發明之實施形態詳細加以說明。 Hereinafter, embodiments of the present invention will be described in detail.

本發明係如第1圖所示，以有機性排水為原水，在厭氧性生物處理槽1進行厭氧性生物處理後，在好氧性生物處理槽2進行好氧性生物處理，並對好氧性生物處理水添加凝集劑而在凝集槽3進行凝集處理後，使凝集處理水在固液分離槽3固液分離，再對分離水在RO膜分離裝置5進行RO膜分離處理的有機性排水之處理，其中在好氧性生物處理槽2設有載體，並利用附著於載體的好氧性微生物，在pH5.5~6.5之條件下以貫流式進行生物處理。 As shown in FIG. 1, the present invention uses organic drainage as raw water, performs anaerobic biological treatment in the anaerobic biological treatment tank 1, and performs aerobic biological treatment in the aerobic biological treatment tank 2. After agglutinating agent is added to the aerobic biological treatment water and the agglutination treatment is performed in the agglutination tank 3, the agglutination treatment water is subjected to solid-liquid separation in the solid-liquid separation tank 3, and the separated water is subjected to RO membrane separation treatment in the RO membrane separation device For the treatment of sexual drainage, a carrier is provided in the aerobic biological treatment tank 2 and the aerobic microorganisms attached to the carrier are used for biological treatment in a cross-flow manner under the conditions of pH 5.5 to 6.5.

[有機性排水] [Organic drainage]

在本發明中，作為處理對象物的有機性排水只要為一般待進行生物處理的含有機物之排水即可，不特別限定，可列舉例如電子產業排水、化學工廠排水、食品工廠排水等。舉例來說，在電子零件製程中，由於各種含有機物之排水會從顯影步驟、剝離步驟、蝕刻步驟、清洗步驟等當中大量產生，並且，較佳為將排水回收淨化成純水等級予以再使用，故而，此等排水係適用於作為本發明之處理對象排水。 In the present invention, the organic drainage to be treated is not particularly limited as long as it is organic-containing drainage to be subjected to biological treatment in general, and examples thereof include electronic industry drainage, chemical factory drainage, and food factory drainage. For example, in the manufacturing process of electronic parts, since various kinds of organic-containing drainages are generated in large quantities from the developing step, the peeling step, the etching step, the cleaning step, and the like, it is preferable to recycle the purified wastewater to a pure water level for reuse. Therefore, these drainage systems are suitable for drainage as the treatment object of the present invention.

作為此類有機性排水，可列舉例如含有異丙醇、乙醇等的有機性排水、含有單乙醇胺(MEA)、氫氧化四甲銨(TMAH)等有機態氮、氨態氮的有機性排水、含有二甲亞碸(DMSO)等有機硫化合物的有機性排水。 Examples of such organic waste water include organic waste water containing isopropyl alcohol, ethanol, and the like, organic waste water containing organic nitrogen such as monoethanolamine (MEA), tetramethylammonium hydroxide (TMAH), and ammonia nitrogen, Organic drainage containing organic sulfur compounds such as dimethyl sulfoxide (DMSO).

[厭氧性生物處理] [Anaerobic biological treatment]

作為用以對原水在厭氧下進行生物處理的厭氧性生物處理手段，只要為有機物分解效率優良者即可，可使用既知之厭氧性生物處理方式的生物反應槽。 As an anaerobic biological treatment means for biologically treating raw water under anaerobic conditions, as long as it is excellent in organic matter decomposition efficiency, a biological reaction tank of a known anaerobic biological treatment method can be used.

厭氧性生物處理手段可為在同一槽進行酸生成反應與甲烷生成反應的單相式、或在個別的槽進行各反應的兩相式。各反應槽可採浮遊方式(攪拌方式)、汙泥床方式(汙泥氈方式)等任意方式，又可為載體添加型、造粒汙泥型。 The anaerobic biological treatment means may be a single-phase system in which an acid generation reaction and a methane generation reaction are performed in the same tank, or a two-phase system in which each reaction is performed in a separate tank. Each reaction tank can adopt any method such as a floating method (stirring method), a sludge bed method (sludge felt method), and can also be a carrier addition type or a granulated sludge type.

作為厭氧性生物處理手段不特別限定，惟具備酸生成槽與UASB(上向流式厭氧性汙泥氈)方式的反應槽者，由於可進行高負載運作而較佳。 The anaerobic biological treatment method is not particularly limited, but those having an acid generation tank and a UASB (upward-flow anaerobic sludge blanket) reaction tank are preferred because they can perform high-load operation.

[好氧性生物處理] [Aerobic biological treatment]

在本發明中，好氧性生物處理係利用使活性汙泥附著於載體而保持的生物膜方式，以貫流式進行處理。此外，好氧性生物處理之貫流式處理由於不需要藉由汙泥之沉降分離或返送、抽除的濃度管理，而易於運作管理。再者，將後段產生的SS凝集去除時，亦可去除一部分生物處理中去除不盡的殘留有機物。 In the present invention, the aerobic biological treatment system is a cross-flow process using a biofilm system in which activated sludge is attached to a carrier and held. In addition, the aerobic biological treatment of the cross-flow treatment is easy to operate and manage because it does not require concentration management by sludge sedimentation separation, return, and extraction. In addition, when the SS agglomeration generated in the subsequent stage is removed, an endless amount of residual organic matter can be removed during biological treatment.

好氧性生物處理的方式可為固定床式、流化床式、展開床式等任意微生物床方式。作為在好氧性狀態下以微生物將有機物分解的好氧性生物處理槽，可使用設有用以對槽內供給氧氣(空氣)之散氣管、曝氣機等氧氣 供給手段的曝氣槽。 The aerobic biological treatment method can be any microbial bed method such as a fixed bed type, a fluidized bed type, and an expanded bed type. As an aerobic biological treatment tank that decomposes organic matter by microorganisms in an aerobic state, oxygen such as a diffuser and an aerator provided with oxygen (air) in the tank can be used. Aeration tank for supply means.

作為載體，活性炭、各類塑膠載體、海綿載體等均可使用。惟，若為海綿載體，則可將微生物維持於高濃度而較佳。作為海綿素材亦不特別限定，較佳為酯系聚胺甲酸酯。載體之投入量也無特別限制，一般而言，以相對於生物處理槽之槽容量的載體之視容量(以下，將此比率稱為「填充率」)計，較佳設為10~50%左右，特佳設為30~50%左右。 As the carrier, activated carbon, various plastic carriers, sponge carriers, etc. can be used. However, if it is a sponge carrier, microorganisms can be maintained at a high concentration. Although it does not specifically limit as a sponge material, Preferably it is an ester-type polyurethane. The amount of the carrier is also not particularly limited. Generally speaking, it is preferably 10 to 50% based on the apparent capacity of the carrier relative to the tank capacity of the biological treatment tank (hereinafter, this ratio is referred to as the "filling rate"). Right and left, the best setting is about 30-50%.

本發明中，係將好氧性生物處理槽內的pH控制於5.5~6.5。為此，可對好氧性生物處理槽添加鹽酸、硫酸等酸來進行pH控制，但在原水中含有氮化合物時，因硝化使pH下降，從而添加氫氧化鈉、氫氧化鉀等鹼來加以調整。好氧性生物處理槽內的pH未達5.5時，好氧性生物處理所致之有機物分解不充分，有有機物殘留之虞；超過6.5時則無法充分去除厭氧性生物處理中所殘留的鹼度。從而，好氧性生物處理槽的pH係調整成5.5~6.5，較佳為5.8~6.3左右。 In the present invention, the pH in the aerobic biological treatment tank is controlled to 5.5 to 6.5. Therefore, pH can be controlled by adding acids such as hydrochloric acid and sulfuric acid to the aerobic biological treatment tank. However, when nitrogen compounds are contained in the raw water, the pH is lowered due to nitrification, and alkalis such as sodium hydroxide and potassium hydroxide are added for adjustment. . When the pH in the aerobic biological treatment tank is less than 5.5, the organic matter caused by the aerobic biological treatment is not sufficiently decomposed, and there is a risk of organic residues; when it exceeds 6.5, the alkali remaining in the anaerobic biological treatment cannot be fully removed. degree. Therefore, the pH of the aerobic biological treatment tank is adjusted to 5.5 to 6.5, preferably about 5.8 to 6.3.

好氧性生物處理槽可為單槽式或多槽式，且，若為單槽式時，可於槽內設置間壁。若為多槽式時，最後段之生物處理槽的pH係調整成5.5~6.5，較佳為pH5.8~6.3。而且，此時，前段側之好氧性生物處理槽的pH可為6.5~8.0程度。 The aerobic biological treatment tank may be a single tank type or a multi-tank type, and if it is a single tank type, a partition wall may be provided in the tank. In the case of a multi-tank type, the pH of the biological treatment tank at the last stage is adjusted to 5.5 to 6.5, preferably pH 5.8 to 6.3. Moreover, at this time, the pH of the aerobic biological treatment tank on the front side may be about 6.5 to 8.0.

[凝集處理] [Agglutination treatment]

對原水在厭氧下經生物處理後在好氧下進行生物處理所得之好氧性生物處理水，為利用後段的固液分離手段確實去除微生物體與高分子有機物質，係於固液分離前先經過凝集處理。好氧性生物處理水的凝集處理係使用一般的凝集處理裝置。該凝集處理裝置之凝集槽可僅為單槽，亦可以多層設置2槽以上。 The aerobic biologically treated water obtained by biologically treating the raw water under anaerobic and biologically under aerobic conditions is used for the solid-liquid separation method in the later stage to reliably remove microorganisms and high molecular organic substances. First go through agglutination. For agglutination treatment of aerobic biologically treated water, a general agglutination treatment device is used. The agglutination tank of the agglutination treatment device may be only a single tank, or two or more tanks may be provided in multiple layers.

作為凝集處理所使用的無機凝集劑，可列示氯化鐵、聚硫酸鐵等鐵系凝集劑、硫酸鋁、氯化鋁、聚氯化鋁等鋁系凝集劑，基於凝集效果方面較佳為鐵系凝集劑。此等無機凝集劑可單獨使用1種，亦可併用2種以上。 As the inorganic coagulant used in the agglutination treatment, iron-based coagulants such as ferric chloride and polyferric sulfate, aluminum-based coagulants such as aluminum sulfate, aluminum chloride, and polyaluminum chloride can be listed. Iron-based coagulant. These inorganic coagulants may be used singly or in combination of two or more kinds.

凝集處理時，係視需求添加pH調整劑予以調整成對使用之無機凝集劑屬合適的pH。舉例來說，若為鐵系凝集劑，在pH5.5以下使其反應係屬有效；若為鋁系凝集劑，在pH5.0以下使其反應後，予以調整成pH6.0以上則屬有效，因此，較佳為視需求添加鹽酸、硫酸等酸、或氫氧化鈉等鹼來進行pH調整。 During the agglutination treatment, a pH adjuster is added to adjust the inorganic aggregating agent to a suitable pH when needed. For example, if it is an iron-based agglutinating agent, its reaction system is effective at pH 5.5 or less; if it is an aluminum-based agglutinating agent, it is effective to adjust it to pH 6.0 or more after reacting it at pH 5.0 or less. Therefore, it is preferable to adjust the pH by adding an acid such as hydrochloric acid, sulfuric acid, or a base such as sodium hydroxide as needed.

凝集劑之添加量只要為如可得所需凝集效果的量即可，無特別限制，根據本發明，由可藉好氧性生物處理高程度去除厭氧性生物處理中所殘留的鹼度而言，若為例如氯化鐵等鐵系凝集劑，以FeCl3(38%)之添加量計為30~80ppm(體積)左右時，比起以往可大幅刪減，其結果，凝集處理水之固液分離中產生的汙泥量亦可大幅減少。 The addition amount of the coagulant is not particularly limited as long as the desired coagulation effect can be obtained. According to the present invention, the alkalinity remaining in the anaerobic biological treatment can be removed to a high degree by the aerobic biological treatment In other words, if it is an iron-based aggregating agent such as ferric chloride, when the amount of FeCl 3 (38%) is about 30 to 80 ppm (volume), it can be greatly reduced compared with the past. As a result, The amount of sludge produced in solid-liquid separation can also be greatly reduced.

藉由凝集處理，生物處理水中的溶解性有機物或懸浮物即絮凝化。為使該凝集絮凝物生長，亦可在第1凝集槽予以添加無機凝集劑、在第2凝集槽予以添加高分子凝集劑。 By agglutination, dissolved organic matter or suspended matter in biologically treated water is flocculated. In order to grow the agglomerated floc, an inorganic coagulant may be added to the first agglutination tank, and a polymer coagulant may be added to the second agglutination tank.

[固液分離] [Solid-liquid separation]

作為對好氧性生物處理水進行凝集處理所得之凝集處理水的固液分離手段，有沉澱槽、浮上槽、離心分離機等，不特別限定，由生物處理水的凝集絮凝物容易發生浮上分離，且宜為面積較沉澱槽為小的裝置而言，特佳為將加壓浮上槽，尤為凝集加壓浮上槽作成小型。再者，好氧性生物處理水的固液分離亦可採用浸漬膜等的膜分離手段。 The solid-liquid separation means for the agglutinated treated water obtained by agglutinating the aerobic biologically treated water includes sedimentation tanks, floating tanks, centrifugal separators, and the like, which are not particularly limited, and flocculated flocs from biologically treated water are prone to floating separation In addition, it is preferable that the device has a smaller area than the sedimentation tank, and it is particularly preferable to make the pressure floating floating tank, especially the aggregation pressure floating floating tank into a small size. Furthermore, solid-liquid separation of aerobic biologically treated water can also be performed by membrane separation means such as a dipping membrane.

[RO膜分離處理] [RO membrane separation process]

藉固液分離得到的分離水，接著在RO膜分離裝置經處理，以此去除分離水中所殘留的溶存有機物與溶存鹽類。 The separated water obtained by solid-liquid separation is then processed in a RO membrane separation device to remove dissolved organic matter and dissolved salts remaining in the separated water.

較佳為在該RO膜分離裝置的前段設置過濾裝置來去除水中的SS。作為過濾裝置，可採用填充有砂、無煙煤等濾材的填充層型過濾裝置、使用精密過濾(MF)膜、超過濾(UF)膜等膜的膜過濾裝置等。 It is preferable to provide a filtering device at the front stage of the RO membrane separation device to remove SS in water. As the filter device, a packed-layer filter device filled with filter materials such as sand and anthracite, a membrane filter device using a membrane such as a precision filtration (MF) membrane, an ultrafiltration (UF) membrane, or the like can be used.

在本發明中，藉好氧性生物處理高程度去除厭氧性生物處理中所殘留的鹼度來減少凝集處理所需之凝 集劑量，由此可降低固液分離水中的鹽類濃度，而降低RO膜分離裝置的鹽類負載，其結果，可增加該RO膜分離裝置的透過水量。 In the present invention, the aerobic biological treatment is used to highly remove the alkalinity remaining in the anaerobic biological treatment to reduce the coagulation required for the agglutination treatment. By collecting the dose, the salt concentration in the solid-liquid separation water can be reduced, and the salt load of the RO membrane separation device can be reduced. As a result, the amount of permeated water of the RO membrane separation device can be increased.

[實施例] [Example]

以下舉出實施例及比較例對本發明更具體地加以說明。 The present invention will be described more specifically with reference to examples and comparative examples below.

在以下的實施例及比較例中，好氧性生物處理槽的pH調整及凝集處理時的pH調整係藉由對好氧性生物處理槽或待凝集處理的好氧性生物處理水添加氫氧化鈉或鹽酸來進行。 In the following examples and comparative examples, the pH adjustment of the aerobic biological treatment tank and the pH adjustment during the agglutination process are performed by adding hydroxide to the aerobic biological treatment tank or the aerobic biological treatment water to be agglomerated. Sodium or hydrochloric acid.

[實施例1] [Example 1]

以下述水質之液晶工廠的有機性排水為原水，以1.6L/d之處理水量進行處理。 The organic wastewater from the liquid crystal plant with the following water quality was used as raw water, and treated with a treated water volume of 1.6 L / d.

<原水水質> <Raw water quality>

pH：10 pH: 10

TOC：100mg/L TOC: 100mg / L

T-N：20mg-N/L T-N: 20mg-N / L

PO4-P：0.5mg-P/L PO 4 -P: 0.5mg-P / L

(添加其他微量金屬、礦物質作為營養劑) (Adding other trace metals and minerals as nutrients)

將原水首先以上向流注入至下述規格的厭氧 性生物處理槽後，再注入至下述規格的好氧性生物處理槽。 The raw water is first injected upward to the following anaerobic specifications After the biological treatment tank, it is injected into the aerobic biological treatment tank of the following specifications.

<厭氧性生物處理槽> <Anaerobic biological treatment tank>

槽容量：4L(直徑10cm×高度50cm之圓筒狀) Tank capacity: 4L (cylindrical shape with a diameter of 10cm x a height of 50cm)

溫度：30℃ Temperature: 30 ℃

以啤酒工廠排水處理設施的厭氧顆粒為植種汙泥取0.8L，投入1.6L聚丙烯製圓筒狀載體( 3mm×5mm)並培養2個月者。 Take 0.8L of anaerobic granules from the wastewater treatment facilities of beer factory as seed sludge, and put 1.6L of polypropylene cylindrical carrier ( 3mm × 5mm) and cultured for 2 months.

<好氧性生物處理槽> <Aerobic biological treatment tank>

槽容量：4L Tank capacity: 4L

以40%之填充率添加聚胺甲酸酯海綿(3mm見方)，投入工廠排水處理設施的活性汙泥(MLSS約6,000mg/L)作為植種汙泥並培養3週者。 Polyurethane sponge (3mm square) was added at a filling rate of 40%, and activated sludge (MLSS, about 6,000 mg / L) was put into the plant sewage treatment facility as planting sludge and cultured for 3 weeks.

pH5.8~6.0 pH5.8 ~ 6.0

對好氧性生物處理槽的處理水，添加以FeCl3(38%)添加量計如表1，2所示的量的38重量%氯化鐵(FeCl3)水溶液，將pH調整成5.5進行凝集處理，並針對靜置30分鐘經沉降分離後的上澄液，調查MFF值。又，針對將該上澄液以孔徑0.45μm濾紙過濾後的過濾水測定TOC濃度。 To the treated water of the aerobic biological treatment tank, an aqueous solution of 38% by weight of iron chloride (FeCl 3 ) in an amount shown in Tables 1 and 2 based on the FeCl 3 (38%) addition amount was added, and the pH was adjusted to 5.5. Aggregation treatment was performed, and the MFF value was investigated with respect to the supernatant liquid which was left to stand for 30 minutes and separated by sedimentation. In addition, the TOC concentration was measured with respect to filtered water obtained by filtering the supernatant liquid through a filter paper having a pore diameter of 0.45 μm.

將此等結果示於表1，2。 The results are shown in Tables 1 and 2.

[比較例1] [Comparative Example 1]

除將實施例1中好氧性生物處理槽的pH調整成6.8~7.0以外係同樣地進行，調查MFF值及TOC濃度，將結果示於表1，2。 The same procedure was performed except that the pH of the aerobic biological treatment tank in Example 1 was adjusted to 6.8 to 7.0. The MFF value and the TOC concentration were investigated, and the results are shown in Tables 1 and 2.

[比較例2] [Comparative Example 2]

除將實施例1中好氧性生物處理槽的pH調整成4.8~5.0以外係同樣地進行，調查MFF值及TOC濃度，將結果示於表1，2。 The same procedure was performed except that the pH of the aerobic biological treatment tank in Example 1 was adjusted to 4.8 to 5.0. The MFF value and the TOC concentration were investigated, and the results are shown in Tables 1 and 2.

由表1，2可明瞭以下所述者。 Tables 1 and 2 show the following.

於實施例1中，藉由添加30mg/L的FeCl3，MFF值為1.1、TOC為1.5mg/L，均為較低值，對於供給至RO膜，可得良好的水質。另一方面，於比較例1中，TOC與實施例雖無大的差異，但對於MFF值，則須添加FeCl3至75mg/L，才會下降至1.1。茲認為此係因好氧性生物處理水中所殘留的鹼度使FeCl3被消耗，在30mg/L凝集不充分所致。此外，在比較例2中，即使添加100mg/L的FeCl3，TOC仍殘留5mg/L左右，未藉由凝集而減少。茲認為此係好氧性生物處理槽的pH較低，有機物去除不充分，使液晶工廠排水所含的低分子有機物殘留所致。 In Example 1, by adding 30 mg / L of FeCl 3 , the MFF value is 1.1 and the TOC is 1.5 mg / L, which are both low values. Good water quality can be obtained for supplying to the RO membrane. On the other hand, in Comparative Example 1, although TOC is not much different from the Examples, for MFF value, FeCl 3 must be added to 75 mg / L before it will drop to 1.1. It is believed that this is due to the consumption of FeCl 3 due to the alkalinity remaining in the aerobic biologically treated water, resulting in insufficient agglutination at 30 mg / L. Moreover, in Comparative Example 2, even when 100 mg / L of FeCl 3 was added , TOC remained at about 5 mg / L, which was not reduced by agglutination. It is believed that the pH of this aerobic biological treatment tank is low, the organic matter is not removed sufficiently, and the low-molecular-weight organic matter contained in the wastewater of the liquid crystal factory is caused.

業已採用特定形態對本發明詳細加以說明，惟本領域具有通常知識者應理解，在不悖離本發明意圖暨範圍下可實施種種變更。 The present invention has been described in detail using specific forms, but those with ordinary knowledge in the art should understand that various changes can be implemented without departing from the intention and scope of the present invention.

本申請案係基於2013年3月29日所申請之日本專利申請2013-074167，茲援用其全體以供引用。 This application is based on Japanese Patent Application No. 2013-074167 filed on March 29, 2013, the entirety of which is hereby incorporated by reference.

Claims (8)

一種有機性排水之處理方法，其係具有：厭氧性生物處理步驟，對有機性排水在厭氧下進行生物處理；好氧性生物處理步驟，對從該厭氧性生物處理步驟流出的厭氧性生物處理水在好氧下進行生物處理；固液分離步驟，對從該好氧性生物處理步驟流出的好氧性生物處理水添加鐵系凝集劑在pH5.5以下使其反應並進行凝集後進行固液分離；及逆滲透膜分離步驟，對該固液分離步驟中所分離的分離水進行處理的有機性排水之處理方法，其特徵為：該好氧性生物處理步驟係在pH5.8~6.3之條件下，利用附著於載體的好氧性微生物，以貫流式進行處理的步驟。An organic wastewater treatment method includes: an anaerobic biological treatment step for biologically treating organic wastewater under anaerobic conditions; an aerobic biological treatment step for anaerobic organisms flowing out of the anaerobic biological treatment step The aerobic biologically treated water is biologically treated under aerobic conditions; in the solid-liquid separation step, iron-based agglutinating agent is added to the aerobic biologically treated water flowing out of the aerobic biologically treating step to make it react at pH 5.5 or less and proceed. Solid-liquid separation after agglomeration; and a reverse osmosis membrane separation step, a method for treating organic wastewater by treating the separated water separated in the solid-liquid separation step, characterized in that the aerobic biological treatment step is at pH 5 .8 ~ 6.3, the process of using aerobic microorganisms attached to the carrier in a cross-flow process. 如請求項1之有機性排水之處理方法，其係在該好氧性生物處理步驟中，將該厭氧性生物處理水裝入好氧性生物處理槽，在好氧下進行生物處理之方法，其中該載體為海綿載體，該好氧性生物處理槽之載體填充率為10~50%。For example, the organic wastewater treatment method of claim 1 is a method of loading the anaerobic biological treatment water into the aerobic biological treatment tank in the aerobic biological treatment step, and performing the biological treatment under aerobic conditions. The carrier is a sponge carrier, and the carrier filling rate of the aerobic biological treatment tank is 10-50%. 如請求項1之有機性排水之處理方法，其中該鐵系凝集劑為氯化鐵，以FeCl3(38%)之添加量計，其添加量為30~80體積ppm。For example, the method for treating organic wastewater according to claim 1, wherein the iron-based aggregating agent is ferric chloride, and the added amount is 30 to 80 vol ppm based on the added amount of FeCl 3 (38%). 如請求項1至3中任一項之有機性排水之處理方法，其係對該分離水經過膜過濾的過濾水，在該逆滲透膜分離步驟中進行處理。The treatment method of organic drainage according to any one of claims 1 to 3, which is a process of filtering the separated water through membrane filtration in the reverse osmosis membrane separation step. 一種有機性排水之處理裝置，其係具有：厭氧性生物處理手段，對有機性排水在厭氧下進行生物處理；好氧性生物處理手段，對從該厭氧性生物處理手段流出的厭氧性生物處理水在好氧下進行生物處理；凝集劑添加手段，對從該好氧性生物處理手段流出的好氧性生物處理水添加鐵系凝集劑在pH5.5以下使其反應；固液分離手段，使添加有該鐵系凝集劑的水固液分離；及逆滲透膜分離手段，對該固液分離步驟中所分離的分離水進行處理的有機性排水之處理裝置，其特徵為：該好氧性生物處理手段係在pH5.8~6.3之條件下，利用附著於載體的好氧性微生物，以貫流式進行處理的手段。An organic wastewater treatment device includes: an anaerobic biological treatment means for biologically treating organic drainage under anaerobic conditions; an aerobic biological treatment means for anaerobes flowing out of the anaerobic biological treatment means The aerobic biologically treated water is biologically treated under aerobic conditions; the agglutinating agent adding means adds iron-based aggregating agent to the aerobic biologically treated water flowing out of the aerobic biologically treating means to react at a pH of 5.5 or less; The liquid separation means separates water, solid and liquid by adding the iron-based coagulant; and the reverse osmosis membrane separation means, an organic drainage treatment device for treating the separated water separated in the solid-liquid separation step, is characterized in that: : The aerobic biological treatment means is a means for treating in a cross-flow manner by using aerobic microorganisms attached to a carrier at a pH of 5.8 to 6.3. 如請求項5之有機性排水之處理裝置，其中該好氧性生物處理手段係盛裝該厭氧性生物處理水並在好氧下進行生物處理的好氧性生物處理槽，該載體為海綿載體，該好氧性生物處理槽之載體填充率為10~50%。For example, the organic drainage treatment device of claim 5, wherein the aerobic biological treatment means is an aerobic biological treatment tank containing the anaerobic biologically treated water and performing biological treatment under aerobic conditions, and the carrier is a sponge carrier. The carrier filling rate of the aerobic biological treatment tank is 10-50%. 如請求項5之有機性排水之處理裝置，其中該鐵系凝集劑為氯化鐵，以FeCl3(38%)之添加量計，其添加量為30~80體積ppm。For example, the organic wastewater treatment device of claim 5, wherein the iron-based aggregating agent is ferric chloride, and the added amount is 30 to 80 vol ppm based on the added amount of FeCl 3 (38%). 如請求項5至7中任一項之有機性排水之處理裝置，其具有對該分離水進行膜過濾的膜過濾裝置，該膜過濾裝置之過濾水係在該逆滲透膜分離手段中經處理。The organic drainage treatment device according to any one of claims 5 to 7, comprising a membrane filtration device for membrane filtration of the separated water, and the filtered water of the membrane filtration device is treated in the reverse osmosis membrane separation means. .
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