TWI411584B - Method and apparatus for biologically treating organic matter-containing water - Google Patents

Method and apparatus for biologically treating organic matter-containing water Download PDF

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TWI411584B
TWI411584B TW97146987A TW97146987A TWI411584B TW I411584 B TWI411584 B TW I411584B TW 97146987 A TW97146987 A TW 97146987A TW 97146987 A TW97146987 A TW 97146987A TW I411584 B TWI411584 B TW I411584B
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biological treatment
water
membrane
anaerobic
organic
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TW97146987A
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TW200932688A (en
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Hidenari Yasui
Katsuhiko Momosaki
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Kurita Water Ind Ltd
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/28—Anaerobic digestion processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C02F2101/38—Organic compounds containing nitrogen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

A method and an apparatus for biological treatment of organic matter-containing water are provided to avoid an increase in the load with respect to a reverse osmosis membrane, prevent the contamination of the reverse osmosis membrane, and smoothly perform the water treatment using the reverse osmosis membrane. An apparatus(100) for biological treatment of organic matter-containing water comprises an anaerobic bioreactor(110), a membrane separation device(112), and a reverse osmosis membrane device(114). The anaerobic bioreactor performs methanogenesis by methanogenic bacteria when organic matter-containing water flows into the anaerobic bioreactor. The membrane separation device is connected to the anaerobic bioreactor. The membrane separation device separates treated liquid discharged from the anaerobic bioreactor. The reverse osmosis membrane device treats water separated by the membrane separation device.

Description

含有有機物的水的生物處理方法以及裝置Biological treatment method and device for water containing organic matter

本發明是有關於一種對含有有機物的水進行厭氧性處理(anaerobic treatment)之生物處理方法以及裝置，特別是有關於一種對排水(drainage)進行生物處理而將其用作純水製造用原水之生物處理方法以及裝置。The present invention relates to a biological treatment method and apparatus for anaerobic treatment of water containing organic matter, and more particularly to a biological treatment of drainage for use as raw water for pure water production. Biological treatment method and device.

一般認為，與厭氧性微生物群相比，需氧性(aerobic)微生物群具有多種多樣的有機物分解能力。因此，利用需氧性微生物群之需氧性生物處理，適用於處理含有複雜的高分子(聚合物)化合物的排水(例如食品排水)。另外，在厭氧性生物處理中高分子有機物的水解速度較慢，因此通常需要將水力停留時間(Hydraulic Retention Time)設為30天或30天以上。相對於此，需氧性生物處理的標準水力停留時間較短，為0.5天左右。It is believed that the aerobic microbiota has a wide variety of organic matter decomposition capabilities compared to anaerobic microbial populations. Therefore, aerobic biological treatment using an aerobic microbial population is suitable for treating drainage (for example, food drainage) containing a complex polymer (polymer) compound. Further, since the hydrolysis rate of the high molecular organic substance is slow in the anaerobic biological treatment, it is usually necessary to set the hydraulic retention time to 30 days or more. In contrast, the standard hydraulic retention time of aerobic biological treatment is relatively short, about 0.5 days.

近年來，如半導體製造工廠般在使用純水並排出其排水的設備等中進行水回收，即，對含有有機物的排水進行生物處理，將該處理水用作純水製造的原料。在進行如此水回收之含有有機物的水的生物處理中，先前是採用需氧性生物處理。當含有有機物的水中含有氮成分時，以需氧性條件將氮化合物氧化而生成硝酸或亞硝酸，再以無氧條件進行脫氮。另外，在進行需氧性生物處理時，亦大多藉由將需氧性微生物固定於載體上而增大生物處理槽的微生物保持量，從而提高處理速度(例如日本專利特開平9-187785號公報)。當使用載體時，例如可將每個生物處理槽中的有機物除去速度提高至1kg-COD/m3 /day~2kg-COD/m3 /day左右。In recent years, water is recovered in equipment such as a semiconductor manufacturing plant that uses pure water and discharges the water, that is, biological treatment of the organic-containing wastewater, and the treated water is used as a raw material for pure water production. In the biological treatment of organic water-containing water thus subjected to such water recovery, aerobic biological treatment was previously employed. When the organic substance-containing water contains a nitrogen component, the nitrogen compound is oxidized under aerobic conditions to form nitric acid or nitrous acid, and denitrification is carried out under anaerobic conditions. In addition, in the case of aerobic biological treatment, the amount of microorganisms retained in the biological treatment tank is increased by immobilizing the aerobic microorganisms on the carrier, thereby increasing the processing speed (for example, Japanese Patent Laid-Open Publication No. Hei 9-187785) ). When a carrier is used, for example, the removal rate of organic matter in each biological treatment tank can be increased to about 1 kg-COD/m 3 /day to 2 kg-COD/m 3 /day.

當將利用此種生物處理而獲得的處理液再利用於純水製造時，在將處理液以固液分離裝置進行處理而分離出微生物體之後，以逆滲透膜(RO膜)分離裝置等進行脫鹽處理(例如日本專利特開2007-175582號公報)。When the treatment liquid obtained by such biological treatment is reused in pure water production, the treatment liquid is treated by a solid-liquid separation device to separate the microorganisms, and then the reverse osmosis membrane (RO membrane) separation device or the like is used. Desalination treatment (for example, Japanese Patent Laid-Open Publication No. 2007-175582).

如上所述，在將排水作為純水製造的原水加以再利用時，通常進行使用膜分離裝置的處理。但是，分離膜由於運轉條件或被處理水的水質的原因而發生堵塞，特別是若對生物處理液進行膜分離，則存在微生物自身以及由微生物生成的黏性物質等附著於膜面上而發生堵塞之傾向。由微生物生成的黏性物質具有以高分子有機物為主體之難分解性，其生成量與生物處理槽中保持的微生物量大致成正比例地增大。因此，在使用增殖速度較大的需氧性微生物之需氧性生物處理中，高分子有機物的生成量亦較多。特別是當使用添加有載體的生物處理槽時，保有微生物量變多，因此高分子有機物的生成量變多。As described above, when the raw water produced by using the drainage water as pure water is reused, the treatment using the membrane separation apparatus is usually performed. However, the separation membrane is clogged due to the operating conditions or the quality of the water to be treated. In particular, when the membrane is separated from the biological treatment liquid, the microorganism itself and the viscous substance generated by the microorganism adhere to the membrane surface. The tendency to block. The viscous substance produced by the microorganism has a hardly decomposable property mainly composed of a polymer organic substance, and the amount of production thereof increases substantially in proportion to the amount of microorganisms held in the biological treatment tank. Therefore, in the aerobic biological treatment using an aerobic microorganism having a large proliferation rate, the amount of the polymer organic substance produced is also large. In particular, when a biological treatment tank to which a carrier is added is used, the amount of microorganisms retained is increased, so that the amount of production of high molecular organic substances is increased.

另一方面，厭氧性微生物的增殖速度比需氧性微生物慢，因此高分子有機物的生成量相對較少。但是，厭氧性生物處理原本對有機物的分解速度就較慢，因此容易產生被處理水(含有有機物的水)中含有的有機物不被分解，而是直接含有於或者其分解中間體含有於處理液中之現象。即，當進行需氧性生物處理時，有由於微生物的生成物而污染逆滲透膜之虞。另一方面，當進行厭氧性生物處理時，雖然由於微生物的生成物而造成膜污染的可能性較低，但由於處理液中殘存的有機物或分解中間體而造成膜污染的可能性變高。On the other hand, the rate of proliferation of anaerobic microorganisms is slower than that of aerobic microorganisms, so the amount of formation of high molecular organic substances is relatively small. However, the anaerobic biological treatment originally has a slow decomposition rate of the organic matter, so that the organic matter contained in the treated water (the organic-containing water) is not easily decomposed, but is directly contained in or the decomposition intermediate is contained in the treatment. The phenomenon in the liquid. That is, when the aerobic biological treatment is performed, there is a possibility that the reverse osmosis membrane is contaminated by the microorganism product. On the other hand, when anaerobic biological treatment is performed, although the possibility of membrane fouling due to the production of microorganisms is low, the possibility of membrane fouling due to residual organic substances or decomposition intermediates in the treatment liquid becomes high. .

另外，當在對排水進行生物處理後分離出處理液中含有的微生物體時，若採用凝聚沈澱(coagulation sedimentation)或加壓浮上方法，則分離並不充分，且分離水中含有微生物體等，會污染後段的逆滲透膜。特別是，當向生物處理槽中添加載體時，為了將載體進行固液分離必須使用篩等，但增大表面積而提高活性之載體的粒徑較小，因而容易使篩堵塞，為了避免此現象必需使用複雜構成的固液分離裝置或大的沈澱池。In addition, when the microorganisms contained in the treatment liquid are separated after biological treatment of the drainage, if the coagulation sedimentation or the pressurized floating method is used, the separation is not sufficient, and the separated water contains microorganisms, etc. Reverse osmosis membrane in the back stage of pollution. In particular, when a carrier is added to the biological treatment tank, it is necessary to use a sieve or the like in order to carry out solid-liquid separation of the carrier, but the particle size of the carrier which increases the surface area and increases the activity is small, so that the sieve is easily clogged, in order to avoid this phenomenon. It is necessary to use a solid-liquid separation device or a large sedimentation tank of a complicated structure.

對此，若利用設置於生物處理槽內的浸漬膜對經生物處理的處理液進行固液分離，則可良好地分離微生物體等，因此可防止後段的逆滲透膜污染。但是，存在浸漬膜自身發生堵塞之問題，特別是當進行需氧性處理時，存在由於微生物生成的高分子有機物而造成浸漬膜堵塞從而使滲透水量降低之問題。On the other hand, when the biologically treated treatment liquid is subjected to solid-liquid separation by the immersion membrane provided in the biological treatment tank, the microorganisms and the like can be well separated, and thus the reverse osmosis membrane contamination in the subsequent stage can be prevented. However, there is a problem that the immersion film itself is clogged, and in particular, when the aerobic treatment is performed, there is a problem that the immersion film is clogged by the polymer organic matter generated by the microorganism, and the amount of permeated water is lowered.

另外，當含有有機物的水中含有氮成分時，在除去氮成分的需氧性生物處理過程中，利用微生物使有機氮(organic nitrogen)無機化而生成氨，該氨被需氧性的硝化細菌(nitrifier)氧化而生成亞硝酸或硝酸，使得槽內液體的pH值降低，因此需要添加中和用的鹼。繼而，當於厭氧性條件下進行硝酸的脫氮處理時，硝酸或亞硝酸被無氧性的脫氮細菌還原成氮氣，在此過程中生成鹼而使pH值上升。因此，在脫氮步驟中必需添加中和用的酸。如此，在生物處理過程中為了中和而添加的酸或鹼，則成為後段的逆滲透膜(RO膜)的鹽類負荷。Further, when the organic substance-containing water contains a nitrogen component, in the aerobic biological treatment for removing the nitrogen component, the organic nitrogen is inorganicized by the microorganism to generate ammonia, which is aerobic nitrifying bacteria ( Nitrifier) oxidizes to form nitrous acid or nitric acid, which lowers the pH of the liquid in the tank, so it is necessary to add a base for neutralization. Then, when the denitrification treatment of nitric acid is carried out under anaerobic conditions, nitric acid or nitrous acid is reduced to nitrogen by an anaerobic denitrifying bacteria, and a base is formed in the process to raise the pH. Therefore, it is necessary to add an acid for neutralization in the denitrification step. As described above, the acid or base added for neutralization during the biological treatment is a salt load of the reverse osmosis membrane (RO membrane) in the subsequent stage.

如上所述，當進行反應至生成亞硝酸或硝酸再對其脫氮時，生成作為強酸之亞硝酸或硝酸、以及作為強鹼之OH- ，因此必需將強酸或強鹼中和。另一方面，於將氮化合物氧化的步驟中，若在生成氨的時間點使生物反應停止，則僅中和呈弱鹼性的氨即可，不必中和強酸或強鹼。為了使氮化合物的生物脫氮在生成氨的階段停止，則使增殖速度較慢的硝化細菌在生物反應槽內不增殖即可。具體而言，若縮短污泥在生物反應槽中的滯留時間，則硝化細菌會從生物反應槽流出(washout)而不保持於槽內，因此在生成氨的階段停止反應。As described above, when the reaction is carried out until nitrous acid or nitric acid is formed and then denitrified, nitrous acid or nitric acid as a strong acid and OH - as a strong base are formed, and therefore it is necessary to neutralize a strong acid or a strong base. On the other hand, in the step of oxidizing the nitrogen compound, if the biological reaction is stopped at the time of ammonia production, only the ammonia which is weakly alkaline can be neutralized, and it is not necessary to neutralize the strong acid or the strong base. In order to stop the biological denitrification of the nitrogen compound at the stage of ammonia production, the nitrifying bacteria having a slower proliferation rate may not be propagated in the biological reaction tank. Specifically, if the residence time of the sludge in the biological reaction tank is shortened, the nitrifying bacteria are washed out from the biological reaction tank without being held in the tank, so that the reaction is stopped at the stage of ammonia formation.

但是，為了使硝化細菌流出，必須將污泥在生物反應槽中的滯留時間設為4天或4天以下。若將污泥的滯留時間降低至4天或4天以下左右，則被處理水中所含有的有機物並不被充分分解。因此，在經生物處理的處理液中含有較多的殘存有機物，在逆滲透膜裝置中以殘存有機物作為基質而使得微生物易於增殖。增殖的微生物成為堵塞逆滲透膜的原因，從而使逆滲透膜的脫鹽性能降低。However, in order to allow the nitrifying bacteria to flow out, the residence time of the sludge in the biological reaction tank must be set to 4 days or less. When the residence time of the sludge is reduced to about 4 days or less, the organic matter contained in the water to be treated is not sufficiently decomposed. Therefore, the biologically treated treatment liquid contains a large amount of residual organic matter, and in the reverse osmosis membrane device, the residual organic matter is used as a matrix to allow the microorganism to easily proliferate. The proliferating microorganisms cause clogging of the reverse osmosis membrane, thereby degrading the desalination performance of the reverse osmosis membrane.

如上所述，當對含有有機物的水進行生物處理而將其再利用於純水製造時，排水處理製程會對使用逆滲透膜的處理造成不利影響。另外，以需氧性條件對含有有機物的水進行生物處理而進行硝化，則由於添加中和用試劑而導致對逆滲透膜裝置的負荷增大，另一方面，若為了抑制硝化的進行而縮短污泥滯留時間，則由於殘存有機物而導致逆滲透膜污染。本發明之目的在於，針對該課題，提供一種於含有有機物的水之生物處理中，在將處理水作為純水製造用水加以再利用時，避免對逆滲透膜之負荷的增大，並且亦防止逆滲透膜的污染，從而順利地進行使用逆滲透膜的處理之方法以及裝置。As described above, when the organic substance-containing water is biologically treated and reused in pure water production, the drainage treatment process adversely affects the treatment using the reverse osmosis membrane. In addition, when the organic material-containing water is biologically treated and subjected to nitrification under aerobic conditions, the load on the reverse osmosis membrane device is increased by the addition of the neutralizing reagent, and the nitrogenation is shortened in order to suppress the progress of nitrification. The sludge retention time causes contamination of the reverse osmosis membrane due to residual organic matter. An object of the present invention is to provide an object for preventing the increase in the load on the reverse osmosis membrane when the treated water is reused as pure water for manufacturing water in the biological treatment of water containing organic substances, and also to prevent the increase in the load on the reverse osmosis membrane. The method and apparatus for treating the reverse osmosis membrane are smoothly carried out by contamination of the reverse osmosis membrane.

本發明為了解決上述問題，藉由以厭氧性條件對含有有機物的水進行生物處理，而在不進行硝化反應的情況下除去被處理水中的有機物，將生物處理後的處理液中殘存的銨鹽在逆滲透膜裝置中進行濃縮後再另作處理。另外，有機物的厭氧性生物處理分為：利用酸生成菌群由有機物生成酸之步驟、利用甲烷生成菌群(methanogen)由酸生成甲烷之步驟。本發明人等發現，成為膜污染的原因物質的高分子有機物，主要是經由與酸生成步驟相關之酸生成菌群的代謝而生成。因此，本發明人等構思：藉由在不經過利用酸生成菌群之酸生成步驟的情況下生成甲烷而解決上述課題，從而完成本發明。具體而言，本發明提供以下之方法及裝置。In order to solve the above-mentioned problems, the present invention solves the above problems by biologically treating water containing an organic substance under anaerobic conditions, and removing the organic substance in the water to be treated without performing the nitrification reaction, and removing the ammonium remaining in the treatment liquid after the biological treatment. The salt is concentrated in a reverse osmosis membrane unit and then treated separately. Further, the anaerobic biological treatment of organic matter is a step of producing an acid from an organic substance by an acid-producing microbial group, and a step of generating methane from an acid by a methanogen. The present inventors have found that a polymer organic substance which is a cause of membrane fouling is mainly produced by metabolism of an acid-producing flora associated with an acid generating step. Therefore, the inventors of the present invention have conceived that the above problems can be solved by generating methane without undergoing an acid generating step using an acid generating microbial group, thereby completing the present invention. In particular, the present invention provides the following methods and apparatus.

(1)一種含有有機物的水的生物處理方法，其是以下列步驟進行處理：(1) A biological treatment method for water containing organic matter, which is treated in the following steps:

將含有有機物的水導入厭氧性生物處理槽中；Introducing water containing organic matter into an anaerobic biological treatment tank;

利用上述厭氧性生物處理槽內的甲烷生成菌群進行厭氧性生物處理；Anaerobic biological treatment using the methane-producing flora in the anaerobic biological treatment tank;

將利用上述厭氧性生物處理所獲得的處理液，在不進行需氧性生物處理的情況下進行膜分離；The treatment liquid obtained by the above anaerobic biological treatment is subjected to membrane separation without aerobic biological treatment;

以逆滲透膜處理利用上述膜分離所獲得的分離水。The separated water obtained by the above membrane separation was treated with a reverse osmosis membrane.

(2)如(1)所述之含有有機物的水的生物處理方法，其中上述含有有機物的水中，單體有機物相對於總有機碳的比例大於等於70%。(2) The biological treatment method of the organic substance-containing water according to (1), wherein the ratio of the monomer organic substance to the total organic carbon in the organic substance-containing water is 70% or more.

(3)如(1)或(2)所述之含有有機物的水的生物處理方法，其中將槽內的液體的溫度設為大於等於15℃小於等於40℃而進行上述厭氧性處理。(3) The biological treatment method of the organic-containing water according to (1) or (2), wherein the anaerobic treatment is performed by setting the temperature of the liquid in the tank to 15 ° C or more and 40 ° C or less.

(4)如(3)所述之含有有機物的水的生物處理方法，其中上述處理液於上述厭氧性處理的過程加溫，再將上述處理液進行膜分離以及逆滲透膜處理。(4) The biological treatment method of the organic substance-containing water according to (3), wherein the treatment liquid is heated in the anaerobic treatment process, and the treatment liquid is subjected to membrane separation and reverse osmosis membrane treatment.

(5)如(2)所述之含有有機物的水的生物處理方法，其中上述單體有機物是選自以氫氧化四甲銨、單乙醇胺、二乙二醇單丁醚、異丙醇、二甲基乙醯胺、二甲基甲醯胺、二甲基亞碸以及乙酸所組成之族群中的任一種以上。(5) The biological treatment method of the organic-containing water according to (2), wherein the monomer organic substance is selected from the group consisting of tetramethylammonium hydroxide, monoethanolamine, diethylene glycol monobutyl ether, isopropanol, and Any one or more of the group consisting of methyl acetamide, dimethylformamide, dimethyl hydrazine, and acetic acid.

(6)一種含有有機物的水的生物處理裝置，包括：(6) A biological treatment device for water containing organic matter, comprising:

厭氧性生物處理槽，導入含有有機物的水，利用甲烷生成菌群生成甲烷；An anaerobic biological treatment tank, introducing water containing organic matter, and generating methane by using a methane-producing flora;

膜分離裝置，與上述厭氧性生物處理槽相連接，對從上述厭氧性生物處理槽排出的處理液進行膜分離；a membrane separation device connected to the anaerobic biological treatment tank to perform membrane separation on the treatment liquid discharged from the anaerobic biological treatment tank;

逆滲透膜裝置，對上述膜分離裝置的分離水進行處理。The reverse osmosis membrane device processes the separated water of the membrane separation device.

(7)如(6)所述之含有有機物的水的生物處理裝置，其中上述含有有機物的水中，單體有機物相對於總有機碳的比例大於等於70%。(7) The biological treatment apparatus of the organic substance-containing water according to (6), wherein the ratio of the monomer organic substance to the total organic carbon in the organic substance-containing water is 70% or more.

(8)如(6)或(7)所述之含有有機物的水的生物處理裝置，其是以如下方式構成：(8) The biological treatment apparatus for organic-containing water according to (6) or (7), which is configured as follows:

上述厭氧性處理槽是將槽內液體的溫度設為大於等於15℃小於等於40℃而進行運轉，The anaerobic treatment tank is operated by setting the temperature of the liquid in the tank to 15 ° C or more and 40 ° C or less.

於上述厭氧性處理槽內在加溫狀態下將上述處理液供給至上述膜分離裝置以及上述逆滲透膜裝置。The treatment liquid is supplied to the membrane separation device and the reverse osmosis membrane device in a heated state in the anaerobic treatment tank.

(9)如(8)所述之含有有機物的水的生物處理裝置，更包括熱回收加熱裝置，用以熱回收前述上述逆滲透膜裝置的滲透水，並利用回收的熱量加溫上述厭氧性處理槽。(9) The biological treatment apparatus for organic-containing water according to (8), further comprising a heat recovery heating device for heat-recovering the permeated water of the reverse osmosis membrane device, and using the recovered heat to heat the anaerobic Sex processing tank.

(10)如(6)所述之含有有機物的水的生物處理裝置，其中上述膜分離裝置包括微量濾膜(microfiltration membrane)或者超濾膜(ultrafiltration membrane)。(10) The biological treatment apparatus of the organic substance-containing water according to (6), wherein the membrane separation apparatus comprises a microfiltration membrane or an ultrafiltration membrane.

(11)如(6)所述之含有有機物的水的生物處理裝置，更包括清洗裝置，用以供給在上述厭氧性生物處理槽中產生的生物生成氣(biogas，又稱生物沼氣)至上述膜分離裝置，以對上述膜分離裝置進行曝氣清洗。(11) The biological treatment apparatus for organic-containing water according to (6), further comprising a cleaning device for supplying bio-generated gas (biogas) generated in the anaerobic biological treatment tank to The membrane separation device performs aeration cleaning on the membrane separation device.

(12)一種含有有機物的水的生物處理裝置，包括：(12) A biological treatment device for water containing organic matter, comprising:

厭氧性生物處理槽，以導入含有有機物的水，並利用甲烷生成菌群生成甲烷；An anaerobic biological treatment tank for introducing water containing organic matter and generating methane by using a methane-producing flora;

膜分離裝置，與上述厭氧性生物處理槽相連接，用以對從上述厭氧性生物處理槽中排出的處理液進行膜分離；a membrane separation device connected to the anaerobic biological treatment tank for membrane separation of the treatment liquid discharged from the anaerobic biological treatment tank;

逆滲透膜裝置，用以處理上述膜分離裝置的分離水；a reverse osmosis membrane device for treating separated water of the membrane separation device;

濃縮水處理裝置，對上述逆滲透膜裝置的濃縮水進行處理。The concentrated water treatment device treats the concentrated water of the reverse osmosis membrane device.

(13)如(12)所述之含有有機物的水的生物處理裝置，其中上述濃縮水處理裝置包含與上述厭氧性生物處理槽不同的生物處理槽。(13) The biological treatment apparatus of the organic substance-containing water according to (12), wherein the concentrated water treatment apparatus includes a biological treatment tank different from the anaerobic biological treatment tank.

(14)如(12)或(13)所述之含有有機物的水的生物處理裝置，其中上述濃縮水處理裝置包含導入上述濃縮水並使其蒸發而取出蒸餾水之蒸發器。(14) The biological treatment apparatus of the organic-containing water according to (12) or (13), wherein the concentrated water treatment apparatus includes an evaporator that introduces the concentrated water and evaporates the distilled water.

(15)如(12)所述之含有有機物的水的生物處理裝置，其中上述濃縮水處理裝置包含反應柱(reactive column)，能將使上述濃縮水中的雜質不溶化的化學品添加至上述濃縮水中，並將固體物分離。(15) The biological treatment apparatus of the organic substance-containing water according to (12), wherein the concentrated water treatment apparatus includes a reaction column, and a chemical capable of insolubilizing impurities in the concentrated water is added to the concentrated water. And separate the solids.

(16)一種含有有機物的水的生物處理方法，包括：(16) A biological treatment method for water containing organic matter, comprising:

將含有有機物的水導入包含甲烷生成菌群的厭氧性生物處理槽中進行厭氧性生物處理，Anaerobic biological treatment is carried out by introducing water containing organic matter into an anaerobic biological treatment tank containing a methane-producing flora.

將利用上述厭氧性生物處理所獲得的處理液在不進行需氧性生物處理的情況下進行膜分離，The treatment liquid obtained by the above anaerobic biological treatment is subjected to membrane separation without aerobic biological treatment.

以逆滲透膜對利用上述膜分離所獲得的分離水進行處理，Treating the separated water obtained by the above membrane separation with a reverse osmosis membrane,

對利用上述逆滲透膜處理所獲得的濃縮水進行處理。The concentrated water obtained by the above reverse osmosis membrane treatment is treated.

(17)如(16)所述之含有有機物的水的生物處理方法，其中上述含有有機物的水中含有氮化合物。(17) The biological treatment method of the organic-containing water according to (16), wherein the organic substance-containing water contains a nitrogen compound.

(18)如(16)或(17)所述之含有有機物的水的生物處理方法，其中對上述濃縮水進行與上述厭氧性生物處理不同的生物處理；利用蒸發器對上述濃縮水進行蒸餾處理；以及/或者對上述濃縮水利用化學品使雜質不溶化後再進行處理。(18) The biological treatment method of the organic-containing water according to (16) or (17), wherein the concentrated water is subjected to biological treatment different from the anaerobic biological treatment; and the concentrated water is distilled by an evaporator Processing; and/or treating the concentrated water using chemicals to insolubilize the impurities.

於本說明書中，對於被處理水即含有有機物的水的特性(property)並無特別限定，不僅含有有機碳化合物亦可含有氮化合物。所謂「總有機碳」，是指水中所含各種有機碳化合物之總稱，不僅包含非揮發性有機物，亦包含不能以通常的TOC(總有機碳)儀測定的揮發性有機物。另外，有機碳化合物，較好的是微生物可直接吸收程度的低分子有機物(以下稱為「單體有機物」)的比例較多(例如相對於總有機碳大於等於70%)。所謂「單體有機物」，是排水中所含有的各種有機物中微生物可直接吸收程度的低分子有機物之總稱。單體有機物被甲烷生成菌群分解，因此若是以單體有機物為主體的含有有機物的水，則在厭氧性生物處理的步驟中酸生成菌群難以增殖。根據本發明者們的知識見解，若抑制酸生成菌群的增殖，則可抑制由該些微生物生成的高分子代謝物的生成，可防止由於代謝物所造成的逆滲透膜污染。In the present specification, the property of the water to be treated, that is, the water containing the organic substance is not particularly limited, and the organic carbon compound may contain not only the nitrogen compound. The term "total organic carbon" refers to a general term for various organic carbon compounds contained in water. It includes not only non-volatile organic substances, but also volatile organic compounds that cannot be measured by a conventional TOC (Total Organic Carbon) meter. Further, the organic carbon compound is preferably a ratio of a low molecular organic substance (hereinafter referred to as "monomer organic substance") which is directly absorbable by microorganisms (for example, 70% or more with respect to total organic carbon). The "monomer organic matter" is a general term for low molecular organic substances in which various microorganisms contained in the drainage are directly absorbed by microorganisms. Since the monomeric organic matter is decomposed by the methane-producing microflora, the organic acid-containing water mainly composed of the monomeric organic matter is difficult to proliferate in the step of anaerobic biological treatment. According to the knowledge of the inventors, when the proliferation of the acid-producing microbial group is inhibited, the formation of a polymer metabolite produced by the microorganisms can be suppressed, and the reverse osmosis membrane contamination by the metabolite can be prevented.

關於「單體有機物」，無法通過微生物細胞壁而被菌體外酵素分解之有機物，通常有機物彼此之間會發生聚合而使得分子量較大，於本說明書中，使用「單體有機物」是為表示除此種高分子有機物以外的有機物之用語。單體有機物之具體例，可舉出：用作甲烷生成菌群的基質之低分子有機物(例如甲酸、乙酸、甲醇、甲胺等)或氫氧化四甲銨、單乙醇胺、二乙二醇單丁醚、異丙醇、二甲基乙醯胺、二甲基甲醯胺、二甲基亞碸。於本發明中，特別是作為單體有機物之具有甲基的化合物(四甲基銨、二甲基乙醯胺、二甲基甲醯胺、二甲基亞碸)的含有比例較高之含有有機物的水，成為適宜的處理對象。The "monomer organic substance" is an organic substance that cannot be decomposed by the extracellular enzyme through the microbial cell wall. Usually, the organic substance is polymerized with each other to have a large molecular weight. In the present specification, the use of "monomer organic matter" means The term "organic matter other than polymer organic matter". Specific examples of the monomeric organic substance include low molecular organic substances (for example, formic acid, acetic acid, methanol, methylamine, etc.) used as a matrix of the methane-producing microbial group, or tetramethylammonium hydroxide, monoethanolamine, and diethylene glycol alone. Butyl ether, isopropanol, dimethylacetamide, dimethylformamide, dimethyl alum. In the present invention, in particular, a compound having a methyl group as a monomeric organic substance (tetramethylammonium, dimethylacetamide, dimethylformamide, dimethylammonium) has a high content ratio. Organic water is a suitable treatment target.

本發明中，利用甲烷生成菌群對被處理水中的有機物進行厭氧性生物處理。被處理水中的有機物組成，較好的是設定為以單體有機物為主。因單體有機物被甲烷生成菌群生物分解，故藉由將被處理水的特性設為單體有機物主體，可將被處理水中的有機物良好地生物分解而抑制有機物殘留於處理液中，且防止後段的分離膜污染。另外，本發明中，特別是藉由以作為單體有機物之具有甲基的化合物(四甲基銨、二甲基乙醯胺、二甲基甲醯胺、二甲基亞碸)的含有比例較高之含有有機物的水作為處理對象，而抑制酸生成菌群生成膜污染物質，藉此可防止由於高分子有機物所造成的膜污染。In the present invention, the organic matter in the water to be treated is subjected to anaerobic biological treatment using a methane-producing flora. The composition of the organic matter in the treated water is preferably set to be mainly monomeric organic matter. Since the monomeric organic matter is biodegraded by the methane-producing microbial group, the organic substance in the water to be treated can be biodegraded favorably by the characteristic of the water to be treated, and the organic substance can be prevented from remaining in the treatment liquid and prevented. The separation membrane in the latter stage is contaminated. Further, in the present invention, in particular, a content ratio of a compound having a methyl group (tetramethylammonium, dimethylacetamide, dimethylformamide, dimethylammonium) as a monomeric organic substance is contained. The higher organic matter-containing water is used as a treatment target, and the acid-producing microbial group is prevented from generating a film-contaminated substance, thereby preventing membrane contamination by the polymer organic substance.

另外，在以甲烷生成菌群為主體的厭氧性處理中，實質上並不發生硝化反應。因此，當被處理水中含有氮化合物時，氮成分在生物處理步驟中在不發生脫氮的情況下被帶入逆滲透膜裝置中。因此，若被處理水中不含氮化合物，則可降低對逆滲透膜裝置的負荷。另一方面，本發明人等發現，當被處理水中含有氮化合物且供給至逆滲透膜裝置的液體中含有氮成分時，在逆滲透膜中經濃縮的氮成分具有抑制逆滲透膜裝置中的微生物增殖之可能性。因此，在逆滲透膜裝置中微生物容易增殖的條件(例如被處理水中含有10%~30%左右的高分子有機物之情形)下，可積極地使被處理水含有氮化合物。Further, in the anaerobic treatment mainly composed of the methane-producing microflora, the nitrification reaction does not substantially occur. Therefore, when the treated water contains a nitrogen compound, the nitrogen component is carried into the reverse osmosis membrane device in the biological treatment step without denitrification. Therefore, if the water to be treated does not contain a nitrogen compound, the load on the reverse osmosis membrane device can be reduced. On the other hand, the present inventors have found that when the nitrogen contained in the water to be treated and the liquid supplied to the reverse osmosis membrane device contain a nitrogen component, the concentrated nitrogen component in the reverse osmosis membrane has a function of suppressing the reverse osmosis membrane. The possibility of microbial proliferation. Therefore, in the reverse osmosis membrane apparatus, when the microorganisms are easily proliferated (for example, when the water to be treated contains 10% to 30% of a polymer organic substance), the water to be treated can be actively contained in the nitrogen compound.

在厭氧性生物處理槽內，為了將被處理水中的有機物良好地生物分解從而防止後段的膜污染，較好的是單體有機物在被處理水中的有機物中所佔比例較高。當被處理水中含有細菌或高分子有機物時，會引起以該些作為基質之酸生成菌群的生物分解，生成成為膜污染原因的可溶性高分子有機物。酸生成菌群的代謝物，若溫度小於15℃或超過40℃則僅有30%左右被分解，但若溫度大於等於15℃小於等於40℃則有90%左右被分解。因此，若將厭氧性生物處理槽的溫度設為大於等於15℃小於等於40℃，則即使除單體有機物以外之有機物的含量相對較高，亦可防止膜污染。In the anaerobic biological treatment tank, in order to biodegrade the organic matter in the water to be treated to prevent membrane fouling in the latter stage, it is preferred that the proportion of the monomeric organic matter in the organic matter in the water to be treated is high. When the water to be treated contains bacteria or a high molecular organic substance, biodegradation of the acid-producing bacteria group as the matrix is caused, and a soluble high-molecular organic substance which causes membrane foulion is formed. When the temperature of the metabolite of the acid-producing microbe is less than 15 ° C or exceeds 40 ° C, only about 30% is decomposed, but if the temperature is 15 ° C or more and 40 ° C or less, about 90% is decomposed. Therefore, when the temperature of the anaerobic biological treatment tank is set to 15 ° C or more and 40 ° C or less, even if the content of the organic substance other than the monomer organic substance is relatively high, membrane fouling can be prevented.

溫度條件特別好的是大於等於30℃小於等於40℃。如上所述，酸生成菌群的代謝物的分解效率因溫度條件而異，因此亦可根據溫度條件改變被處理水的特性。具體而言，若溫度條件為大於等於15℃且小於30℃，則較好的是使單體有機物在被處理水中的有機物中所佔比例大於等於75%。另外，當溫度條件為小於15℃或者超過40℃時，較好的是將單體有機物的比例設為大於等於90%。The temperature condition is particularly preferably 30 ° C or more and 40 ° C or less. As described above, the decomposition efficiency of the metabolite of the acid-producing flora differs depending on the temperature conditions, and therefore the characteristics of the water to be treated can be changed depending on the temperature conditions. Specifically, when the temperature condition is 15 ° C or more and less than 30 ° C, it is preferred that the proportion of the monomer organic matter in the organic matter in the water to be treated is 75% or more. Further, when the temperature condition is less than 15 ° C or more than 40 ° C, it is preferred to set the ratio of the monomer organic matter to 90% or more.

另外，若pH值大於等於6小於等於9，則可良好地分解酸生成菌群的代謝物，若pH值超出該範圍則其分解率會降低至30%左右。因此，較好的是將厭氧性生物處理槽之槽內液體的pH值調整為大於等於6小於等於9，但亦存在酸生成菌群的代謝物的生成較少之情形即單體有機物的比例充分高(實質上100%)之情形等亦可不調整pH值之情形。Further, when the pH is 6 or more and 9 or less, the metabolite of the acid-producing flora can be well decomposed, and if the pH exceeds this range, the decomposition rate is lowered to about 30%. Therefore, it is preferred to adjust the pH of the liquid in the tank of the anaerobic biological treatment tank to 6 or more and 9 or less, but there is also a case where the production of metabolites of the acid-producing microflora is small, that is, the monomer organic matter. The case where the ratio is sufficiently high (substantially 100%) or the like may not be adjusted.

厭氧性生物處理槽的槽內液體中，可含有被處理水中所含的銨鹽或/及被處理水中所含的有機氮化合物被分解而生成的銨鹽。此種銨鹽與厭氧性生物處理槽內伴隨有機物分解而生成的二氧化碳發生反應，生成碳酸氫銨。因此，當被處理水中含有氮化合物時，厭氧性生物處理槽之槽內液體的pH值亦可在不添加中和化學品的情況下維持在中性附近。The liquid in the tank of the anaerobic biological treatment tank may contain an ammonium salt contained in the water to be treated or an ammonium salt which is formed by decomposition of an organic nitrogen compound contained in the water to be treated. The ammonium salt reacts with carbon dioxide generated by decomposition of organic matter in the anaerobic biological treatment tank to form ammonium hydrogencarbonate. Therefore, when the treated water contains a nitrogen compound, the pH of the liquid in the tank of the anaerobic biological treatment tank can also be maintained in the vicinity of neutral without adding neutralizing chemicals.

從厭氧性生物處理槽中流出的處理液中含有微生物，因此在進行固液分離後，以逆滲透膜裝置對除去固體成分的水(分離水)進行脫鹽處理，而成為純水製造的原料。固液分離中可使用具備過濾膜的膜分離裝置。分離膜，亦可使用超濾膜(UF膜)或者微量濾膜(MF膜)，較好的是使用具有比通常的甲烷生成菌群的直徑更小的孔徑(例如小於等於100nm)之膜。Since the treatment liquid flowing out from the anaerobic biological treatment tank contains microorganisms, after the solid-liquid separation is performed, the water (separated water) from which the solid component is removed is desalted by a reverse osmosis membrane device to become a raw material for pure water production. . A membrane separation device equipped with a filtration membrane can be used for solid-liquid separation. As the separation membrane, an ultrafiltration membrane (UF membrane) or a microfiltration membrane (MF membrane) may be used, and it is preferred to use a membrane having a smaller pore diameter (for example, 100 nm or less) than the diameter of the usual methane-producing microflora.

另外，來自厭氧性生物處理槽的處理液中，含有在厭氧性生物處理槽中生成的碳酸氫銨或未經生物處理的有機物等。該些殘存物質的一部分在膜分離裝置中被除去，但其他部分在膜分離裝置中未被除去而被帶入逆滲透膜裝置中進行濃縮。因此，從逆滲透膜裝置排出的濃縮水(鹽水，brine)中，含有被濃縮大約10倍左右的碳酸氫銨等。因此，與被處理水不同，利用生物、化學或/及物理方法對鹽水進行處理。Further, the treatment liquid from the anaerobic biological treatment tank contains ammonium hydrogencarbonate or an organic material which has not been biologically treated, which is produced in the anaerobic biological treatment tank. A part of these residual substances were removed in the membrane separation apparatus, but the other parts were not removed in the membrane separation apparatus and brought into the reverse osmosis membrane apparatus to be concentrated. Therefore, the concentrated water (brine) discharged from the reverse osmosis membrane device contains ammonium hydrogencarbonate or the like which is concentrated about 10 times. Therefore, unlike the water to be treated, the brine is treated by biological, chemical or/and physical methods.

鹽水的處理方法可根據其特性進行選擇，例如生物處理，可舉出進行需氧性或無氧性生物脫氮的處理。生物脫氮中可使用異營性(heterotrophy)或者自營性(autotrophy)中的任一種脫氮微生物。The treatment method of the brine can be selected according to its characteristics, for example, biological treatment, and treatment for aerobic or anaerobic biological denitrification can be mentioned. Any one of heterotrophy or autotrophy may be used for biological nitrogen removal.

作為化學處理，可舉出：使pH值變化以使鹽水中所含的雜質不溶化之方法、添加與鹽水中的雜質形成化合物的化學品之方法等。化學處理中使用的化學品，可舉出：使pH值變化的酸或鹼、凝集劑、以及使鹽水中的雜質析出的種晶等。更具體而言，可舉出：與銨鹽反應而生成硫酸銨的硫酸、使蛋白質凝固的各種酸等。Examples of the chemical treatment include a method of changing the pH to insolubilize impurities contained in the brine, a method of adding a chemical which forms a compound with impurities in the brine, and the like. Examples of the chemical used in the chemical treatment include an acid or a base which changes a pH value, a coagulant, and a seed crystal which precipitates impurities in the brine. More specifically, sulfuric acid which reacts with an ammonium salt to form ammonium sulfate, various acids which solidify proteins, and the like can be given.

作為物理處理，可舉出蒸餾；亦可藉由曝氣使氨揮發。為了防止氨以氣體形式揮發，較好的是於酸性條件下進行蒸餾，亦可於減壓下進行加溫。另一方面，當藉由曝氣使氨揮發時，可設為鹼條件並利用大量的空氣進行曝氣。As the physical treatment, distillation may be mentioned; ammonia may be volatilized by aeration. In order to prevent ammonia from volatilizing in the form of a gas, it is preferred to carry out the distillation under acidic conditions or to carry out heating under reduced pressure. On the other hand, when ammonia is volatilized by aeration, it can be set as an alkali condition and a large amount of air is used for aeration.

亦可組合上述處理法對鹽水進行處理。例如可舉出：向鹽水中添加酸使氨(胺)不溶化後，利用蒸發器進行蒸餾處理，並回收水之方法。該方法具有可在降低含有氨的廢棄物的產生量的同時進行水回收之優點。The brine may also be treated in combination with the above treatment. For example, a method in which an acid is added to a brine to insolubilize ammonia (amine), and then distilled by an evaporator to recover water is mentioned. This method has an advantage that water can be recovered while reducing the amount of waste containing ammonia.

另外，本發明除應用於半導體以外亦應用於液晶顯示器等電子工業工廠的製造製程排水中，藉此可在不如食品工廠排水或汙水處理廠排水般含有高分子成分或各種各樣的化合物的情況下，利用厭氧性生物處理有效率地進行處理。除此之外，亦可將如化學工廠排水般水中含有的有機物及其濃度相對較為明確的排水作為應用對象。該些排水的組成明確，因此具有可利用實驗室實驗獲知處理能力之優點。In addition, the present invention is applied not only to semiconductors but also to the manufacturing process drainage of an electronic industrial factory such as a liquid crystal display, thereby being capable of containing a polymer component or various compounds in a manner not as good as that of a food factory drainage or a sewage treatment plant. In this case, the treatment is efficiently performed by anaerobic biological treatment. In addition to this, it is also possible to use organic substances contained in water such as chemical plant drainage and drainage with relatively clear concentration. The composition of these drainages is clear, and therefore has the advantage of being able to use laboratory experiments to know the processing capabilities.

[發明之效果][Effects of the Invention]

本發明中，藉由以厭氧條件對使有機物以單體有機物為主體之含有有機物的水進行生物處理，而抑制硝化反應，且抑制由於添加pH值調整用化學品所造成的鹽類濃度上升，可抑制酸生成菌群生成代謝物，藉此防止分離膜的污染，並利用甲烷生成菌群分解有機物。本發明中，在厭氧性生物處理之後，可在不進行需氧性生物處理的情況下，獲得有機物被充分分解的生物處理液。因此，可抑制酸生成菌群以及需氧性微生物群生成高分子有機物，同時可降低處理液中的殘存有機物量。因此，可防止在生物處理步驟後段進行膜分離時對分離膜的污染。另外，可將在厭氧性處理中未被除去的物質以逆滲透膜裝置進行濃縮，並進行其他處理，藉此可提高水回收率。In the present invention, the organic matter-containing water mainly composed of a monomeric organic substance is biologically treated under anaerobic conditions to suppress the nitrification reaction, and the salt concentration increase due to the addition of the pH adjusting chemical is suppressed. It can inhibit the formation of metabolites by the acid-producing microflora, thereby preventing the contamination of the separation membrane and decomposing the organic matter by the methane-producing microflora. In the present invention, after the anaerobic biological treatment, the biological treatment liquid in which the organic matter is sufficiently decomposed can be obtained without performing the aerobic biological treatment. Therefore, it is possible to suppress the formation of the polymer organic matter by the acid-producing microbial group and the aerobic microbial group, and to reduce the amount of residual organic matter in the treatment liquid. Therefore, contamination of the separation membrane at the time of membrane separation in the latter stage of the biological treatment step can be prevented. Further, the substance which has not been removed in the anaerobic treatment can be concentrated by a reverse osmosis membrane device and subjected to other treatments, whereby the water recovery rate can be improved.

為讓本發明之上述特徵和優點能更明顯易懂，下文特舉實施例，並配合所附圖式作詳細說明如下。The above described features and advantages of the present invention will be more apparent from the following description.

以下，利用圖式就本發明加以詳細說明。以下，對於同一構件附上同一符號，並省略或簡略其說明。Hereinafter, the present invention will be described in detail using the drawings. Hereinafter, the same members are denoted by the same reference numerals, and the description thereof will be omitted or simplified.

(實施形態一)(Embodiment 1)

圖1是本發明所使用之含有有機物的水的生物處理裝置(以下簡稱為「處理裝置」)100的模式圖。處理裝置100包括：厭氧性生物處理槽(以下稱為「反應器」)110、膜分離裝置112、逆滲透膜裝置114。在反應器110的入口處連接有原水管130。反應器110經由處理液管132與膜分離裝置112相連接，膜分離裝置112經由分離水管134與逆滲透膜裝置114相連接。在逆滲透膜裝置114的出口處連接有滲透水管136。Fig. 1 is a schematic view showing a biological treatment apparatus (hereinafter simply referred to as "processing apparatus") 100 for water containing organic substances used in the present invention. The processing apparatus 100 includes an anaerobic biological treatment tank (hereinafter referred to as "reactor") 110, a membrane separation device 112, and a reverse osmosis membrane device 114. A raw water pipe 130 is connected to the inlet of the reactor 110. The reactor 110 is connected to the membrane separation device 112 via a treatment liquid pipe 132, and the membrane separation device 112 is connected to the reverse osmosis membrane device 114 via a separation water pipe 134. A permeate water pipe 136 is connected to the outlet of the reverse osmosis membrane device 114.

在原水管130的中途設置有第1熱交換器121，在滲透水管136的中途設置有第2熱交換器122。以流體管139將第1熱交換器121與第2熱交換器122相連接，使熱交換中所使用的流體在第1熱交換器121與第2熱交換器122之間循環。由第1熱交換器121、第2熱交換器122以及流體管139構成熱回收加熱裝置。The first heat exchanger 121 is provided in the middle of the raw water pipe 130, and the second heat exchanger 122 is provided in the middle of the permeate pipe 136. The first heat exchanger 121 and the second heat exchanger 122 are connected by the fluid pipe 139, and the fluid used for heat exchange is circulated between the first heat exchanger 121 and the second heat exchanger 122. The first heat exchanger 121, the second heat exchanger 122, and the fluid tube 139 constitute a heat recovery heating device.

反應器110上連接有排泥管135及排氣管131。從排泥管135中排出反應器110內的剩餘污泥，從排氣管131中排出反應器110內產生的氣體。排氣管131與膜分離裝置112相連接，以可曝氣清洗設置於膜分離裝置112內的分離膜(未圖示)之方式而構成，發揮作為清洗裝置的功能。另外，在膜分離裝置112上亦連接有返送管133，返送管133的出口端與反應器110相連接。逆滲透膜裝置114中，在濃縮側連接有鹽水管137。A drain pipe 135 and an exhaust pipe 131 are connected to the reactor 110. The excess sludge in the reactor 110 is discharged from the sludge discharge pipe 135, and the gas generated in the reactor 110 is discharged from the exhaust pipe 131. The exhaust pipe 131 is connected to the membrane separation device 112, and is configured to aerobically clean a separation membrane (not shown) provided in the membrane separation device 112, and functions as a cleaning device. Further, a return pipe 133 is also connected to the membrane separation device 112, and an outlet end of the return pipe 133 is connected to the reactor 110. In the reverse osmosis membrane device 114, a brine tube 137 is connected to the concentration side.

本發明中，將被處理水從原水管130供給至反應器110。較理想的是將單體有機物佔有機物全體70%以上的被處理水供給至反應器110。反應器110的適宜運轉條件是，如上所述，pH值為6~9，溫度為15℃~40℃尤其為30℃~40℃。若為如此條件，則當多少含有不成為甲烷生成菌群的基質之高分子有機物時，亦可防止由於酸生成菌群代謝物所造成的膜污染。In the present invention, the water to be treated is supplied from the raw water pipe 130 to the reactor 110. It is preferable to supply the treated water having 70% or more of the organic matter to the entire reactor 110 to the reactor 110. The suitable operating conditions for the reactor 110 are as described above, with a pH of 6 to 9, and a temperature of 15 to 40 ° C, especially 30 to 40 ° C. Under such a condition, when a polymer organic substance which does not become a matrix of the methane-producing microbial group is contained, it is possible to prevent membrane contamination by the acid-producing microbial metabolite.

反應器110內的甲烷生成菌群可為顆粒狀或者浮游性的任意狀態，甲烷生成菌群與酸生成菌群相比，較難生成黏性物質，因此難以形成顆粒狀污泥。因此，從反應器110排出的處理液中容易含有反應器110內的污泥。The methane-producing microbe in the reactor 110 may be in any form of granules or floating, and the methane-producing microbes are more difficult to form a viscous substance than the acid-producing bacterium, and thus it is difficult to form granulated sludge. Therefore, the sludge in the reactor 110 is easily contained in the treatment liquid discharged from the reactor 110.

本發明中，在反應器110後段設置有膜分離裝置112，因此可將處理液中含有的微生物體良好地進行固液分離。較好的是，如本實施形態所示，將膜分離裝置112與反應器110分開設置。作為膜，可使用超濾膜(UF膜)或者微量濾膜(MF膜)，較好的是孔徑小於通常的甲烷生成菌的直徑，具體而言較好的是孔徑為100nm或100nm以下左右。In the present invention, since the membrane separation device 112 is provided in the subsequent stage of the reactor 110, the microorganisms contained in the treatment liquid can be satisfactorily subjected to solid-liquid separation. Preferably, as shown in this embodiment, the membrane separation device 112 is provided separately from the reactor 110. As the membrane, an ultrafiltration membrane (UF membrane) or a microfiltration membrane (MF membrane) can be used, and it is preferred that the pore diameter is smaller than the diameter of a usual methane-producing bacterium, and specifically, the pore diameter is preferably about 100 nm or less.

膜分離裝置112的模組形式並無特別限定，但較好的是以從反應器110中送液的污泥在膜分離裝置112的內部難以堵塞或滯留之方式而構成，例如可適當地使用管狀形式或平板膜形式。另外，將處理液中的液體成分與固體成分加以分離之分離膜，如本實施形態所示，若設置於反應器110外成為所謂槽外型，則容易控制膜面流速，因此就防止膜面污染之觀點而言為較好。The module form of the membrane separation device 112 is not particularly limited. However, it is preferable that the sludge fed from the reactor 110 is not easily clogged or retained inside the membrane separation device 112, and can be suitably used, for example. In the form of a tube or a flat membrane. In addition, as shown in the present embodiment, the separation membrane which separates the liquid component and the solid component in the treatment liquid is a so-called tank type outside the reactor 110, and it is easy to control the membrane surface flow rate, thereby preventing the membrane surface. It is better from the point of view of pollution.

本實施態樣中，膜分離裝置112上連接有排氣管131，將處理液與生成氣體一同從反應器110送至膜分離裝置112。氣體一邊沿著膜分離裝置112內的被處理水流路移動一邊對分離膜進行曝氣清洗。對供給至膜分離裝置112的處理液在通過裝置內部期間進行固液分離，從透過側將除去固體成分的分離水排出至裝置外。另一方面，固體成分經濃縮的濃縮污泥液與氣體一同在膜分離裝置112的被處理液流路內移動，並從返送管133返送至反應器110。In the present embodiment, the membrane separation device 112 is connected to the exhaust pipe 131, and the treatment liquid is sent from the reactor 110 to the membrane separation device 112 together with the generated gas. The separation membrane is aerated and cleaned while moving along the water path to be treated in the membrane separation device 112. The treatment liquid supplied to the membrane separation device 112 is subjected to solid-liquid separation while passing through the inside of the apparatus, and the separated water from which the solid component is removed is discharged from the permeate side to the outside of the apparatus. On the other hand, the concentrated concentrated sludge liquid in which the solid component is concentrated is moved together with the gas in the liquid to be treated flow path of the membrane separation device 112, and is returned from the return pipe 133 to the reactor 110.

甲烷生成菌群與需氧性微生物相比增殖速度較慢，但若進行如此的污泥返送而將反應器110內的污泥濃度維持在4,000mg/L~10,000mg/L左右，則可獲得與進行需氧性活性污泥的需氧性生物處理時相同程度的分解速度。因此，若將污泥濃度設為上述範圍，則可使反應器110的水力停留時間成為0.5天~2天左右。從反應器110經由排泥管135適當地抽出剩餘污泥，調整反應器110內的污泥濃度。The methane-producing bacteria group has a slower growth rate than the aerobic microorganisms. However, if such a sludge is returned and the sludge concentration in the reactor 110 is maintained at about 4,000 mg/L to 10,000 mg/L, it is obtained. The rate of decomposition is the same as that in the aerobic biological treatment of aerobic activated sludge. Therefore, when the sludge concentration is in the above range, the hydraulic retention time of the reactor 110 can be made 0.5 to 2 days. The excess sludge is appropriately extracted from the reactor 110 via the drain pipe 135, and the sludge concentration in the reactor 110 is adjusted.

膜分離裝置112中分離出固體成分的分離水，在設置於膜分離裝置112後段的逆滲透膜裝置114中進行脫鹽而用作純水製造的原水。本實施形態中，反應器110是於30℃~40℃下運轉，處理液的溫度亦為30℃~40℃。其中，在不進行需氧性處理、亦不人為降低溫度的情況下，將從反應器110中排出的處理液送至膜分離裝置112以及逆滲透膜裝置114。30℃左右的液體容易進行逆滲透膜分離，因此藉由以溫熱狀態將來自反應器110的處理液送至逆滲透膜裝置114，可提高逆滲透膜裝置114的通量(flux)。The separated water of the solid component is separated from the membrane separation device 112, and is desalted in the reverse osmosis membrane device 114 installed in the subsequent stage of the membrane separation device 112 to be used as raw water for pure water production. In the present embodiment, the reactor 110 is operated at 30 ° C to 40 ° C, and the temperature of the treatment liquid is also 30 ° C to 40 ° C. In the case where the aerobic treatment is not performed and the temperature is not artificially lowered, the treatment liquid discharged from the reactor 110 is sent to the membrane separation device 112 and the reverse osmosis membrane device 114. The liquid at about 30 ° C is easily reversed. Since the permeable membrane is separated, the flux of the reverse osmosis membrane device 114 can be increased by sending the treatment liquid from the reactor 110 to the reverse osmosis membrane device 114 in a warm state.

從逆滲透膜裝置114中取出的液體依然溫熱。因此，於本實施態樣中，利用在排出滲透水的滲透水管136的中途所設置之第2熱交換器122，對滲透水進行熱交換而進行熱回收。利用第2熱交換器122中的熱交換被加溫的熱交換介質經由流體管139而送至第1熱交換器121。於第1熱交換器121中，以經加溫的熱交換介質將從原水管130中送來的原水進行加溫再送至反應器110。The liquid withdrawn from the reverse osmosis membrane unit 114 is still warm. Therefore, in the present embodiment, the second heat exchanger 122 provided in the middle of the permeate water pipe 136 that discharges the permeated water exchanges heat with the permeated water to perform heat recovery. The heat exchange medium heated by the heat exchange in the second heat exchanger 122 is sent to the first heat exchanger 121 via the fluid pipe 139. In the first heat exchanger 121, the raw water sent from the raw water pipe 130 is heated by the heated heat exchange medium and sent to the reactor 110.

在逆滲透膜裝置114中經處理而除去鹽類的滲透水，可用作純水製造用的原水。具體而言，在逆滲透膜裝置114的後段配置脫碳酸裝置或離子交換裝置、紫外線殺菌裝置等構成純水製造裝置之機器類，利用該些機器類對從逆滲透膜裝置114中排出的滲透水進行處理，藉此可製造純水。濃縮水若對其另外進行處理，則可與滲透水同樣地進行水回收。The permeated water of the salt is removed by treatment in the reverse osmosis membrane device 114, and can be used as raw water for producing pure water. Specifically, in the rear stage of the reverse osmosis membrane device 114, a device constituting a pure water producing device such as a decarbonation device, an ion exchange device, or an ultraviolet ray sterilizing device is disposed, and the osmosis discharged from the reverse osmosis membrane device 114 is performed by using these devices. The water is treated, whereby pure water can be produced. When the concentrated water is treated separately, water can be recovered in the same manner as the permeated water.

[實施例][Examples]

[實施例1][Example 1]

作為實施例1，使用模仿圖1所示之處理裝置100的實驗裝置進行實驗。實驗裝置的反應器110是以有效容積為1m3 、水力停留時間為0.5天的條件進行運轉。於反應器110內，將從處理甲醇的厭氧性反應器中排出的顆粒狀污泥，於後述的被處理液中進行培養而保持浮游性污泥。反應器110內之浮游性污泥的濃度為4,000mg/L，現存量(濕重比較)中的40%為甲烷生成菌群、60%為甲烷生成菌群的自我分解殘渣。As Example 1, an experiment was conducted using an experimental apparatus that mimics the processing apparatus 100 shown in Fig. 1. The reactor 110 of the experimental apparatus was operated under the conditions of an effective volume of 1 m 3 and a hydraulic retention time of 0.5 days. In the reactor 110, the granular sludge discharged from the anaerobic reactor for treating methanol is cultured in a liquid to be treated described later to maintain the floating sludge. The concentration of the floating sludge in the reactor 110 was 4,000 mg/L, and 40% of the existing amount (wet weight comparison) was a methane-producing flora and 60% was a self-decomposing residue of the methane-producing flora.

作為被處理水，使用總有機碳濃度為750mg/L、氮濃度為218mg/L、磷濃度為1.0mg-P/L的含有有機物的水。總有機物的組成是：氫氧化四甲銨濃度為250mg/L、單乙醇胺濃度為250mg/L、乙酸濃度為250mg/L，單體有機物相對於總有機碳的含有比例實質上為100%。As the water to be treated, organic-containing water having a total organic carbon concentration of 750 mg/L, a nitrogen concentration of 218 mg/L, and a phosphorus concentration of 1.0 mg-P/L was used. The composition of the total organic matter was: tetramethylammonium hydroxide concentration of 250 mg/L, monoethanolamine concentration of 250 mg/L, and acetic acid concentration of 250 mg/L, and the content ratio of the monomer organic matter to the total organic carbon was substantially 100%.

使被處理水加溫使反應器110內的槽內液體溫度達到35℃，並且將槽內液體的pH值調整為7.5。在膜分離裝置112內配置104根直徑為0.52cm的管狀UF膜(超濾膜，孔徑為30nm)，使從反應器110中排出的生物處理液與氣體一同流入管內，濃縮液與氣體返回至反應器110。膜分離裝置112的滲透水量(通量)為1.0m/day。The treated water was warmed so that the temperature of the liquid in the tank in the reactor 110 reached 35 ° C, and the pH of the liquid in the tank was adjusted to 7.5. 104 tubular UF membranes (ultrafiltration membranes having a pore diameter of 30 nm) having a diameter of 0.52 cm were disposed in the membrane separation device 112, and the biological treatment liquid discharged from the reactor 110 was flowed into the tube together with the gas, and the concentrated liquid and the gas were returned. To reactor 110. The permeate amount (flux) of the membrane separation device 112 was 1.0 m/day.

以上述條件繼續進行30日實驗，結果膜分離裝置112的通量可維持上述值，通水阻力最大為30kPa。從膜分離裝置112中獲得之分離水的TOC濃度在實驗期間為3mg/L~4mg/L的範圍，TOC除去率為99.5%。另外，利用逆滲透膜裝置114(具備全芳香族聚醯胺系超低壓膜作為逆滲透膜之螺旋式逆滲透膜裝置)以750kPa對該分離水進行脫鹽處理，經過20小時後的滲透水量維持在開始通水時的90%。The experiment was continued for 30 days under the above conditions, and as a result, the flux of the membrane separation device 112 was maintained at the above value, and the water flow resistance was at most 30 kPa. The TOC concentration of the separated water obtained from the membrane separation device 112 was in the range of 3 mg/L to 4 mg/L during the experiment, and the TOC removal rate was 99.5%. Further, the reverse osmosis membrane device 114 (a spiral reverse osmosis membrane device equipped with a wholly aromatic polyamine-based ultra-low pressure membrane as a reverse osmosis membrane) was desalted at 750 kPa, and the amount of permeated water was maintained after 20 hours. 90% at the beginning of watering.

[實施例2][Embodiment 2]

實施例2中，使用孔徑為400nm的MF膜來代替實施例1中使用的UF膜。其他以與實施例1同樣的條件進行實驗，結果來自安裝有MF膜的膜分離裝置之分離水的TOC濃度與實施例1同樣為3mg/L~4mg/L的範圍。另外，膜分離裝置112的通量維持在1.0m/day，以與實施例1同樣之方式利用逆滲透膜裝置114對分離水進行處理時的通量，即使自通水開始經過20小時後亦維持在最初的90%。另一方面，通水阻力最大達到40kPa，高於實施例1。反應器110內的污泥中之甲烷生成菌群的平均直徑為800nm，因此推測當使用MF膜時甲烷生成菌會堵塞分離膜的孔而導致膜堵塞。In Example 2, an MF film having a pore diameter of 400 nm was used instead of the UF film used in Example 1. The experiment was carried out under the same conditions as in Example 1. As a result, the TOC concentration of the separated water from the membrane separation apparatus equipped with the MF membrane was in the range of 3 mg/L to 4 mg/L in the same manner as in Example 1. Further, the flux of the membrane separation device 112 was maintained at 1.0 m/day, and the flux of the separated water was treated by the reverse osmosis membrane device 114 in the same manner as in Example 1, even after 20 hours from the start of the water passage. Maintained at the original 90%. On the other hand, the water resistance is up to 40 kPa, which is higher than that of the first embodiment. Since the average diameter of the methane-producing bacteria in the sludge in the reactor 110 is 800 nm, it is presumed that when the MF membrane is used, the methane-producing bacteria block the pores of the separation membrane and cause clogging of the membrane.

[比較例1][Comparative Example 1]

於比較例1中改變被處理水的特性。具體而言，於實施例1中使用的被處理水中，添加500mg-TOC/L的污水污泥，將單體有機物相對於總有機碳的比例調整為58%。另外，由於使用這樣的被處理水，故反應器110內的污泥組成亦發生變化。具體而言，比較例1中使用的反應器110中之浮游性污泥的污泥濃度為8,000mg/L，現存量(濕重比較)的20%為甲烷生成菌群，酸生成菌群為20%。剩餘的60%是來自污水污泥的細菌及自我分解殘渣。The characteristics of the water to be treated were changed in Comparative Example 1. Specifically, in the treated water used in Example 1, 500 mg-TOC/L of sewage sludge was added, and the ratio of the monomer organic matter to the total organic carbon was adjusted to 58%. Further, since such treated water is used, the sludge composition in the reactor 110 also changes. Specifically, the sludge concentration of the floating sludge in the reactor 110 used in Comparative Example 1 was 8,000 mg/L, and 20% of the existing amount (wet weight comparison) was a methane-producing flora, and the acid-producing flora was 20%. The remaining 60% are bacteria and self-decomposing residues from sewage sludge.

除了如此改變被處理水的特性、且改變反應器110內的微生物相之外，其餘以與實施例1同樣的條件進行實驗。其結果是膜分離裝置112的通量緩慢降低，並且自實驗開始20天後通水阻力超過30kPa。於比較例1中，膜分離裝置112之分離水的TOC濃度為18mg/L~43mg/L。The experiment was carried out under the same conditions as in Example 1 except that the characteristics of the water to be treated were changed and the microorganism phase in the reactor 110 was changed. As a result, the flux of the membrane separation device 112 was slowly lowered, and the water resistance exceeded 20 kPa after 20 days from the start of the experiment. In Comparative Example 1, the TOC concentration of the separated water of the membrane separation device 112 was from 18 mg/L to 43 mg/L.

[實施例3][Example 3]

實施例3中，將向被處理水中添加的污水污泥的量設為300mg-TOC/L(單體有機物的比例約為71%)。伴隨被處理水特性的改變，反應器110內的污泥成分亦發生變化。具體而言，實施例3中使用的反應器110中之浮游性污泥的污泥濃度為8,000mg/L，現存量(濕重比較)的30%為甲烷生成菌群，酸生成菌群為30%。In Example 3, the amount of sewage sludge added to the water to be treated was set to 300 mg-TOC/L (the ratio of the monomer organic matter was about 71%). The sludge composition in the reactor 110 also changes as the characteristics of the treated water change. Specifically, the sludge concentration of the floating sludge in the reactor 110 used in Example 3 was 8,000 mg/L, and 30% of the existing amount (wet weight comparison) was a methane-producing flora, and the acid-producing flora was 30%.

除了改變被處理水的特性及反應器110內的微生物相之外，其餘以與比較例1同樣的條件進行實驗。其結果，膜分離裝置112的通量表現出與實施例1同樣的行為，分離水的TOC濃度為3mg/L~5mg/L，處理分離水之逆滲透膜裝置114的通量維持在88%。The experiment was carried out under the same conditions as in Comparative Example 1, except that the characteristics of the water to be treated and the microorganism phase in the reactor 110 were changed. As a result, the flux of the membrane separation device 112 exhibited the same behavior as in Example 1, the TOC concentration of the separated water was 3 mg/L to 5 mg/L, and the flux of the reverse osmosis membrane device 114 for treating the separated water was maintained at 88%. .

由上述實驗顯示，若被處理水中的有機物的70%以上為單體有機物，並利用含有甲烷生成菌群的污泥進行厭氧性處理，則可防止生物處理的後段的分離膜堵塞。According to the above experiment, when 70% or more of the organic matter in the water to be treated is a monomeric organic substance and anaerobic treatment is carried out using sludge containing a methane-producing microbial flora, clogging of the separation membrane in the latter stage of biological treatment can be prevented.

[參考例1][Reference Example 1]

將實施例3中反應器110的槽內液體的溫度設為10℃。其結果，膜分離裝置112的通量下降，通水阻力於7天後超過30kPa。另外，與此分開地將反應器110的槽內液體的溫度設為50℃，結果同樣地，膜分離裝置112的通量下降，通水阻力於3天後超過30kPa。The temperature of the liquid in the tank of the reactor 110 in Example 3 was set to 10 °C. As a result, the flux of the membrane separation device 112 decreased, and the water passage resistance exceeded 30 kPa after 7 days. Further, the temperature of the liquid in the tank of the reactor 110 was set to 50 ° C separately from this, and as a result, the flux of the membrane separation device 112 was lowered, and the water-passing resistance exceeded 30 kPa after 3 days.

[參考例2][Reference Example 2]

將實施例3中反應器110的槽內液體的pH值設為5。其結果，膜分離裝置112的通水阻力急遽上升，通水阻力於10天後超過30kPa。另外，與此分開地將反應器110的槽內液體的pH值設為10，結果同樣地，膜分離裝置112的通水阻力急遽上升，通水阻力於8天後超過30kPa。The pH of the liquid in the tank of the reactor 110 in Example 3 was set to 5. As a result, the water passing resistance of the membrane separation device 112 increased rapidly, and the water passing resistance exceeded 30 kPa after 10 days. Further, the pH of the liquid in the tank of the reactor 110 was set to 10 separately from this, and as a result, the water flow resistance of the membrane separation device 112 was rapidly increased, and the water-passing resistance exceeded 30 kPa after 8 days.

[比較例2][Comparative Example 2]

比較例2中，在反應器內部設置吹入空氣的散氣裝置，藉此使反應器成為需氧性生物處理槽。除了將反應器改變成需氧性之外，其餘以與實施例1同樣的條件進行實驗，結果從需氧性生物處理槽流出之處理液的TOC濃度與實施例1同樣為3mg/L~4mg/L的範圍。但是，膜分離裝置112的通量，僅於20天內可維持預定的通量。另外，需氧性生物處理槽的槽內液體中，以200mg/L的濃度含有溶解性TOC。另一方面，實施例1之厭氧性反應器的槽內液體的溶解性TOC濃度為10mg/L左右。如上所述，比較例2中，槽內液體中的溶解性TOC濃度高於實施例1，構成溶解性TOC之高分子有機物的量與導入需氧性生物處理槽之被處理水相比，達到後者的約60倍。In Comparative Example 2, a diffusing device that blows air was provided inside the reactor, whereby the reactor became an aerobic biological treatment tank. Except that the reactor was changed to aerobicity, the experiment was carried out under the same conditions as in Example 1. As a result, the TOC concentration of the treatment liquid flowing out from the aerobic biological treatment tank was 3 mg/L to 4 mg as in Example 1. /L range. However, the flux of the membrane separation device 112 maintains a predetermined flux for only 20 days. Further, in the liquid in the tank of the aerobic biological treatment tank, the soluble TOC was contained at a concentration of 200 mg/L. On the other hand, the solubility TOC concentration of the liquid in the tank of the anaerobic reactor of Example 1 was about 10 mg/L. As described above, in Comparative Example 2, the solubility TOC concentration in the liquid in the tank was higher than that in Example 1, and the amount of the polymer organic matter constituting the soluble TOC was compared with the water to be treated introduced into the aerobic biological treatment tank. The latter is about 60 times.

污泥(細菌)相對於導入生物處理槽的被處理水中的有機物之轉換率，就需氧性微生物而言為0.3g/g，相對於此，就厭氧性微生物而言為0.04g/g。藉由最近的自我分解而生成高分子有機物，因此推斷轉換率越高則生成的高分子有機物越多。The conversion ratio of the sludge (bacteria) to the organic matter in the water to be treated introduced into the biological treatment tank is 0.3 g/g for the aerobic microorganism, and 0.04 g/g for the anaerobic microorganism. . Since the polymer organic matter is generated by the recent self-decomposition, it is estimated that the higher the conversion rate, the more polymer organic matter is produced.

另外，於比較例2中，以與實施例1同樣之方式，利用逆滲透膜對在膜分離裝置112中進行了膜分離的分離水進行處理，結果經過20小時後的滲透水量降低至開始通水時的60%。由該比較例2及實施例1顯示，藉由進行使用甲烷生成菌群的厭氧性生物處理來代替需氧性生物處理，可抑制污染分離膜的高分子有機物的生成。Further, in Comparative Example 2, in the same manner as in Example 1, the separated water subjected to membrane separation in the membrane separation device 112 was treated with a reverse osmosis membrane, and as a result, the amount of permeated water after 20 hours was lowered to start. 60% of water. According to Comparative Example 2 and Example 1, it was shown that anaerobic biological treatment using a methane-producing microbial group was carried out instead of aerobic biological treatment, whereby generation of a polymer organic substance in a contaminated separation membrane was suppressed.

進而，比較例2中，需氧性生物處理槽的微生物群中含有硝化細菌，原水中的氮成分被氧化成硝酸。因此，需氧性生物處理槽之槽內液體的pH值降低，且處理液的水質惡化。因此，在槽內液體的pH值低於5的時間點添加鹼將pH值調整為7。另外，在繼續保持需氧性條件一定時間後，停止向生物處理槽中供給空氣使其成為厭氧性條件，藉此進行脫氮。當以厭氧性條件進行脫氮時，添加無機酸，將pH值調整為7。進行如此的批次式脫氮處理並調整pH值之結果是，處理液中的鹽類濃度增高。因此，膜分離裝置後段之逆滲透膜裝置的滲透壓與實施例1相比增高100kPa~200kPa左右，逆滲透膜裝置之脫鹽效率降低，因此必需增加15%~20%左右的逆滲透膜裝置。Further, in Comparative Example 2, the microbial flora of the aerobic biological treatment tank contained nitrifying bacteria, and the nitrogen component in the raw water was oxidized to nitric acid. Therefore, the pH of the liquid in the tank of the aerobic biological treatment tank is lowered, and the water quality of the treatment liquid is deteriorated. Therefore, the pH was adjusted to 7 by adding a base at a time when the pH of the liquid in the tank was lower than 5. Further, after maintaining the aerobic condition for a certain period of time, the supply of air to the biological treatment tank is stopped to become an anaerobic condition, thereby performing denitrification. When denitrification was carried out under anaerobic conditions, a mineral acid was added to adjust the pH to 7. As a result of performing such a batch type denitrification treatment and adjusting the pH value, the salt concentration in the treatment liquid is increased. Therefore, the osmotic pressure of the reverse osmosis membrane device in the subsequent stage of the membrane separation device is increased by about 100 kPa to 200 kPa as compared with Example 1, and the desalination efficiency of the reverse osmosis membrane device is lowered. Therefore, it is necessary to increase the reverse osmosis membrane device by about 15% to 20%.

由以上實驗顯示，依照本發明，藉由使被處理水以單體有機物為主體並利用含有甲烷生成菌群的厭氧性污泥進行厭氧性生物處理，可減少處理液中含有之高分子有機物或未分解有機物的量，並防止對分離膜的污染。According to the above experiment, according to the present invention, the anaerobic biological treatment of the treated water with the monomeric organic matter and the anaerobic sludge containing the methane-producing microflora can reduce the polymer contained in the treatment liquid. The amount of organic matter or undecomposed organic matter, and prevents contamination of the separation membrane.

(實施形態二)(Embodiment 2)

圖2是本發明第二實施形態之含有有機物的水的生物處理裝置200的模式圖。處理裝置200包括：厭氧性生物處理槽(以下稱為「反應器」)210、膜分離裝置212、逆滲透膜裝置214、作為濃縮水處理裝置之Anammox槽241。在反應器210的入口處連接有原水管230。反應器210經由處理液管232與膜分離裝置212相連接，膜分離裝置212經由分離水管234與逆滲透膜裝置214相連接。在逆滲透膜裝置214的出口處連接有滲透水管236。Fig. 2 is a schematic view showing a biological treatment apparatus 200 containing water of an organic substance according to a second embodiment of the present invention. The processing apparatus 200 includes an anaerobic biological treatment tank (hereinafter referred to as "reactor") 210, a membrane separation device 212, a reverse osmosis membrane device 214, and an Anammox tank 241 as a concentrated water treatment device. A raw water pipe 230 is connected to the inlet of the reactor 210. The reactor 210 is connected to the membrane separation device 212 via a treatment liquid pipe 232, and the membrane separation device 212 is connected to the reverse osmosis membrane device 214 via a separation water pipe 234. A permeate pipe 236 is connected to the outlet of the reverse osmosis membrane unit 214.

在原水管230的中途設置有第1熱交換器221，在滲透水管236的中途設置有第2熱交換器222。以流體管239將第1熱交換器221與第2熱交換器222相連接，使熱交換中使用的流體在第1熱交換器221與第2熱交換器222之間循環。由第1熱交換器221、第2熱交換器222以及流體管239構成熱回收加熱裝置。The first heat exchanger 221 is provided in the middle of the raw water pipe 230, and the second heat exchanger 222 is provided in the middle of the permeate pipe 236. The first heat exchanger 221 and the second heat exchanger 222 are connected by the fluid pipe 239, and the fluid used for heat exchange is circulated between the first heat exchanger 221 and the second heat exchanger 222. The first heat exchanger 221, the second heat exchanger 222, and the fluid tube 239 constitute a heat recovery heating device.

反應器210上連接有排泥管235及排氣管231。從排泥管235中排出反應器210內的剩餘污泥，從排氣管231中排出反應器210內產生的氣體。排氣管231與膜分離裝置212連接，排氣管231是以可曝氣清洗設置於膜分離裝置212內的分離膜(未圖示)之方式而構成，發揮作為清洗裝置的功能。另外，膜分離裝置212上亦連接有返送管233，該返送管233的出口端與反應器210連接。逆滲透膜裝置214中，在濃縮側連接有鹽水管237。鹽水管237與Anammox槽241連接。A drain pipe 235 and an exhaust pipe 231 are connected to the reactor 210. The excess sludge in the reactor 210 is discharged from the sludge discharge pipe 235, and the gas generated in the reactor 210 is discharged from the exhaust pipe 231. The exhaust pipe 231 is connected to the membrane separation device 212, and the exhaust pipe 231 is configured to be capable of adiabatically cleaning a separation membrane (not shown) provided in the membrane separation device 212, and functions as a cleaning device. Further, a return pipe 233 is connected to the membrane separation device 212, and an outlet end of the return pipe 233 is connected to the reactor 210. In the reverse osmosis membrane device 214, a brine tube 237 is connected to the concentration side. The brine tube 237 is connected to the Anammox tank 241.

於本發明中，經由原水管230將作為被處理水之含有氮化合物的含有有機物的水供給至反應器210。如上所述，反應器210的較佳運轉條件是，pH值為6~9、溫度為15~40℃尤其為30~40℃。若為此種條件，則於對含有不成為甲烷生成菌群的基質的高分子有機物之含有有機物的水進行處理之情形時，亦可防止由於酸生成菌群代謝物所造成的膜污染。In the present invention, the organic-containing water containing the nitrogen compound as the water to be treated is supplied to the reactor 210 via the raw water pipe 230. As described above, the preferred operating conditions of the reactor 210 are a pH of 6 to 9, a temperature of 15 to 40 ° C, especially 30 to 40 ° C. Under such a condition, when the organic substance-containing water containing the polymer organic substance which is not a matrix of the methane-producing microbial group is treated, it is possible to prevent membrane contamination by the acid-producing microbial metabolite.

反應器210內的甲烷生成菌群可為顆粒狀或者浮游性的任意狀態，甲烷生成菌群與酸生成菌群相比，較難以生成黏性物質，因此較難以形成顆粒狀污泥。因此，從反應器210排出的處理液中容易含有反應器210內的污泥。The methane-producing microbe in the reactor 210 may be in any form of granules or floating, and the methane-producing microbes are less likely to form a viscous substance than the acid-producing bacterium, and thus it is difficult to form granulated sludge. Therefore, the sludge in the reactor 210 is easily contained in the treatment liquid discharged from the reactor 210.

於本發明中，在反應器210後段設置有膜分離裝置212，因此可良好地將處理液中含有的微生物體進行固液分離。較好的是，如本實施形態所示將膜分離裝置212與反應器210分開設置。作為膜，可使用超濾膜(UF膜)或者微量濾膜(MF膜)，較好的是孔徑小於通常的甲烷生成菌的直徑，具體而言較好的是孔徑為100nm或100nm以下左右。In the present invention, since the membrane separation device 212 is provided in the subsequent stage of the reactor 210, the microorganisms contained in the treatment liquid can be satisfactorily separated into solid-liquid. Preferably, the membrane separation device 212 is provided separately from the reactor 210 as in the present embodiment. As the membrane, an ultrafiltration membrane (UF membrane) or a microfiltration membrane (MF membrane) can be used, and it is preferred that the pore diameter is smaller than the diameter of a usual methane-producing bacterium, and specifically, the pore diameter is preferably about 100 nm or less.

膜分離裝置212之模組形式並無特別限定，但較好的是以從反應器210中送液的污泥在膜分離裝置212內部難以堵塞或滯留之方式而構成，例如適宜使用管狀形式或平板膜形式。另外，將處理液中的液體成分與固體成分加以分離之分離膜，如本實施形態所示，若設置於反應器110外成為所謂槽外型，則容易控制膜面流速，因此就防止膜面污染之觀點而言是比較好的。The module form of the membrane separation device 212 is not particularly limited. However, it is preferred that the sludge fed from the reactor 210 is not easily clogged or retained inside the membrane separation device 212, and for example, a tubular form or In the form of a flat membrane. In addition, as shown in the present embodiment, the separation membrane which separates the liquid component and the solid component in the treatment liquid is a so-called tank type outside the reactor 110, and it is easy to control the membrane surface flow rate, thereby preventing the membrane surface. The point of view of pollution is better.

本實施態樣中，膜分離裝置212上連接有排氣管231，將處理液與生成氣體一同從反應器210送至膜分離裝置212。氣體一邊沿著膜分離裝置212內的被處理水流路移動一邊對分離膜進行曝氣清洗。供給至膜分離裝置212的處理液在通過裝置內部期間被固液分離，從透過側將除去固體成分的分離水排出至裝置外。另一方面，固體成分被濃縮的濃縮污泥液與氣體一同在膜分離裝置212的被處理液流路內移動，從返送管233返送至反應器210。In the present embodiment, the membrane separation device 212 is connected to the exhaust pipe 231, and the treatment liquid is sent from the reactor 210 to the membrane separation device 212 together with the generated gas. The separation membrane is aerated and cleaned while moving along the water path to be treated in the membrane separation device 212. The treatment liquid supplied to the membrane separation device 212 is solid-liquid separated while passing through the inside of the apparatus, and the separated water from which the solid component is removed is discharged from the permeate side to the outside of the apparatus. On the other hand, the concentrated sludge liquid in which the solid component is concentrated is moved together with the gas in the liquid to be treated flow path of the membrane separation device 212, and is returned from the return pipe 233 to the reactor 210.

甲烷生成菌群與需氧性微生物相比增殖速度較慢，但若進行如此的污泥返送並將反應器210內的污泥濃度維持在4,000mg/L~10,000mg/L左右，則可獲得與利用需氧性活性污泥進行需氧性生物處理之情形相同程度的分解速度。因此，若將污泥濃度設為上述範圍，則可使反應器210的水力停留時間成為0.5天~2天左右。將剩餘污泥從反應器210經由排泥管235適當地抽出，以調整反應器210內的污泥濃度。The methane-producing microbial group has a slower growth rate than the aerobic microorganism, but if such sludge is returned and the sludge concentration in the reactor 210 is maintained at about 4,000 mg/L to 10,000 mg/L, The rate of decomposition is the same as in the case of aerobic biological treatment using aerobic activated sludge. Therefore, when the sludge concentration is in the above range, the hydraulic retention time of the reactor 210 can be made 0.5 to 2 days. The excess sludge is appropriately withdrawn from the reactor 210 via the sludge discharge pipe 235 to adjust the sludge concentration in the reactor 210.

在膜分離裝置212中分離出固體成分的分離水，在設置於膜分離裝置212後段之逆滲透膜裝置214中進行脫鹽而用作純水製造的原水。於本實施形態中，反應器210是於30℃~40℃下運轉，處理液的溫度亦為30℃~40℃。在不進行需氧性處理、亦不人為降低溫度的情況下，將從反應器210中排出的處理液送至膜分離裝置212以及逆滲透膜裝置214。30℃左右的液體容易進行逆滲透膜分離，因此藉由以溫熱狀態將來自反應器210的處理液送至逆滲透膜裝置214，可提高逆滲透膜裝置214的通量。The separated water of the solid component is separated in the membrane separation device 212, and is desalted in the reverse osmosis membrane device 214 provided in the subsequent stage of the membrane separation device 212 to be used as raw water for pure water production. In the present embodiment, the reactor 210 is operated at 30 ° C to 40 ° C, and the temperature of the treatment liquid is also 30 ° C to 40 ° C. When the aerobic treatment is not performed and the temperature is not artificially lowered, the treatment liquid discharged from the reactor 210 is sent to the membrane separation device 212 and the reverse osmosis membrane device 214. The liquid at about 30 ° C is easily subjected to reverse osmosis membrane. Since it is separated, the flux of the reverse osmosis membrane device 214 can be increased by feeding the treatment liquid from the reactor 210 to the reverse osmosis membrane device 214 in a warm state.

從逆滲透膜裝置214排出的液體依然溫熱。因此，於本實施態樣中，利用在排出滲透水的滲透水管236的中途所設置之第2熱交換器222，對滲透水進行熱交換而進行熱回收。藉由第2熱交換器222中的熱交換而被加溫之熱交換介質，經由流體管239而送至第1熱交換器221。第1熱交換器221中，利用經加溫的熱交換介質將從原水管230送來的原水進行加溫後送至反應器210。The liquid discharged from the reverse osmosis membrane device 214 is still warm. Therefore, in the present embodiment, the second heat exchanger 222 provided in the middle of the permeate water pipe 236 that discharges the permeated water exchanges heat with the permeated water to perform heat recovery. The heat exchange medium heated by the heat exchange in the second heat exchanger 222 is sent to the first heat exchanger 221 via the fluid pipe 239. In the first heat exchanger 221, the raw water sent from the raw water pipe 230 is heated by the heated heat exchange medium, and then sent to the reactor 210.

在逆滲透膜裝置214中經處理而除去鹽類的滲透水，可用作純水製造用的原水。具體而言，在逆滲透膜裝置214的後段配置脫碳酸裝置或離子交換裝置、紫外線殺菌裝置等構成純水製造裝置之機器類，使用該些機器類對從逆滲透膜裝置214排出的滲透水進行處理，藉此可製造純水。從逆滲透膜裝置214中排出的鹽類被濃縮的濃縮水，從鹽水管237排出。The permeated water of the salt is removed by treatment in the reverse osmosis membrane device 214, and can be used as raw water for producing pure water. Specifically, in the latter stage of the reverse osmosis membrane device 214, a device constituting a pure water producing device such as a decarbonation device, an ion exchange device, or an ultraviolet ray sterilizing device is disposed, and the permeated water discharged from the reverse osmosis membrane device 214 is used using these devices. The treatment is carried out, whereby pure water can be produced. The concentrated concentrated water from which the salt discharged from the reverse osmosis membrane device 214 is concentrated is discharged from the brine tube 237.

第二實施形態之處理裝置200中，具有保持自營性脫氮微生物(Anammox微生物)的生物處理槽作為濃縮水處理裝置。在Anammox槽241中，從鹽水管237供給之濃縮水中的氨的一部分於微需氧性條件下被氧化成亞硝酸，於無氧條件下利用Anammox微生物的生物反應由氨與亞硝酸生成氮氣，並除去氮氣。The treatment apparatus 200 of the second embodiment has a biological treatment tank that holds a self-supporting nitrogen-removing microorganism (Anammox microorganism) as a concentrated water treatment device. In the Anammox tank 241, a portion of the ammonia in the concentrated water supplied from the brine tube 237 is oxidized to nitrous acid under microaerobic conditions, and nitrogen is generated from ammonia and nitrous acid by the biological reaction of the Anammox microorganism under anaerobic conditions. And remove nitrogen.

從配管242中排出來自Anammox槽241的流出液，視需要可進一步進行處理，用作純水製造的原水。或者，視需要亦可將流出液在固液分離裝置(未圖示)中進行固液分離，固體成分作為返送污泥形式而返送，將液體成分放出或者回收。The effluent from the Anammox tank 241 is discharged from the pipe 242, and may be further processed as needed to be used as raw water for pure water production. Alternatively, the effluent may be subjected to solid-liquid separation in a solid-liquid separation device (not shown) as needed, and the solid component may be returned as a return sludge, and the liquid component may be discharged or recovered.

(實施形態三)(Embodiment 3)

從逆滲透膜裝置214中排出的濃縮水，亦可利用除生物處理以外的方法對其進行處理。圖3是本發明第三實施形態之處理裝置300的模式圖。處理裝置300在具有反應柱343代替Anammox槽241作為濃縮水處理裝置之方面，與處理裝置200不同。在將濃縮水供給至反應柱343之鹽水管237的中途連接有未圖示的化學品注入裝置，以添加與濃縮水中的氨反應而生成固形物的化學品。向濃縮水中添加例如磷酸以及鎂鹽作為化學品，在反應柱343中生成磷酸銨鎂從而產生鳥糞石(struvite)結晶。可將鳥糞石結晶從反應柱343排出而用作肥料等，與結晶分離後除去氨之脫氨水，可作為純水製造的原水加以回收利用。The concentrated water discharged from the reverse osmosis membrane device 214 can also be treated by a method other than biological treatment. Fig. 3 is a schematic view showing a processing apparatus 300 according to a third embodiment of the present invention. The processing apparatus 300 is different from the processing apparatus 200 in that it has a reaction column 343 instead of the Anammox tank 241 as a concentrated water treatment apparatus. A chemical injection device (not shown) is connected to the middle of the brine pipe 237 in which the concentrated water is supplied to the reaction column 343, and a chemical which reacts with ammonia in the concentrated water to form a solid matter is added. To the concentrated water, for example, phosphoric acid and a magnesium salt are added as a chemical, and magnesium ammonium phosphate is formed in the reaction column 343 to produce struvite crystals. The struvite crystals can be discharged from the reaction column 343 to be used as a fertilizer or the like, and the deaminated water of ammonia can be removed after separation from the crystals, and can be recovered as raw water produced by pure water.

(實施形態四)(Embodiment 4)

圖4是本發明第四實施形態之處理裝置400的模式圖。處理裝置400具備蒸發器445作為濃縮水處理裝置。於處理裝置400中，將濃縮水導入蒸發器445中進行減壓蒸餾，從蒸餾水管446取出蒸餾水用作純水製造用原水。雖然圖中並未顯示，但亦可在蒸餾處理之前，向濃縮水中添加硫酸，使濃縮水的pH值成為4~6左右而使氨成為硫酸銨，從而回收氨。Fig. 4 is a schematic view showing a processing apparatus 400 according to a fourth embodiment of the present invention. The processing device 400 includes an evaporator 445 as a concentrated water treatment device. In the treatment apparatus 400, concentrated water is introduced into the evaporator 445 to perform vacuum distillation, and distilled water is taken out from the distillation water pipe 446 to be used as raw water for pure water production. Although not shown in the drawing, sulfuric acid may be added to the concentrated water before the distillation treatment, so that the pH of the concentrated water becomes about 4 to 6, and ammonia is made into ammonium sulfate, thereby recovering ammonia.

圖5表示以將生物處理、化學處理以及物理處理中的2種以上加以組合的方法對濃縮水進行處理的其他方法。於圖5的處理裝置500中，將生物處理槽(Anammox槽241)與蒸發器445組合而構成濃縮水處理裝置。於該處理裝置500中，藉由首先對濃縮水進行生物處理，可減少供給至蒸發器445的被處理水的pH值調整中所需酸的添加量。FIG. 5 shows another method of treating concentrated water by a method in which two or more of biological treatment, chemical treatment, and physical treatment are combined. In the processing apparatus 500 of FIG. 5, the biological treatment tank (Anammox tank 241) and the evaporator 445 are combined to form a concentrated water treatment apparatus. In the treatment apparatus 500, by first biologically treating the concentrated water, the amount of acid required for adjusting the pH of the water to be treated supplied to the evaporator 445 can be reduced.

[實施例][Examples]

[實施例4][Example 4]

實施例4中，利用模仿圖2所示之處理裝置200的實驗裝置進行實驗。實驗裝置的反應器210是以有效容積為1m3 、水力停留時間為0.5日之條件運轉。於反應器210內，將從處理甲醇的厭氧性反應器中排出的顆粒狀污泥，在後述之被處理液中進行培養而保持浮游性污泥。反應器210內的浮游性污泥的濃度為4,000mg/L，現存量(濕重比較)中的40%為甲烷生成菌群，60%為甲烷生成菌群的自我分解殘渣。In the fourth embodiment, the experiment was carried out using the experimental apparatus which imitated the processing apparatus 200 shown in FIG. The reactor 210 of the experimental apparatus was operated under the conditions of an effective volume of 1 m 3 and a hydraulic retention time of 0.5 day. In the reactor 210, the granular sludge discharged from the anaerobic reactor for treating methanol is cultured in a treatment liquid to be described later to maintain the floating sludge. The concentration of the floating sludge in the reactor 210 is 4,000 mg/L, and 40% of the existing amount (wet weight comparison) is a methane-producing flora, and 60% is a self-decomposing residue of the methane-producing flora.

作為被處理水，是使用總有機碳(TOC)濃度為500mg/L、氮濃度為152mg/L、無機鹽濃度為1,180mg/L的含有有機物的水。碳以及氮基本上是來自氫氧化四甲銨，其濃度是TOC為480mg/L、N為140mg/L。The water to be treated was an organic-containing water having a total organic carbon (TOC) concentration of 500 mg/L, a nitrogen concentration of 152 mg/L, and an inorganic salt concentration of 1,180 mg/L. Carbon and nitrogen are essentially derived from tetramethylammonium hydroxide at a concentration of 480 mg/L for TOC and 140 mg/L for N.

加溫被處理水，使反應器210內之槽內液體的溫度達到35℃。於膜分離裝置212內配置有104根直徑為0.52cm的管狀UF膜(孔徑為30nm)，使從反應器210排出的生物處理液與氣體一同流入管內，濃縮液與氣體返回至反應器210。將膜分離裝置212的滲透水量(通量)設為1.0m/day。利用逆滲透膜裝置214(具備全芳香族聚醯胺系超低壓膜作為逆滲透膜之螺旋式逆滲透膜裝置)於0.75MPa下將從膜分離裝置212中獲得的分離水濃縮10倍。The treated water was warmed so that the temperature of the liquid in the tank in the reactor 210 reached 35 °C. 104 tubular UF membranes (pore diameter: 30 nm) having a diameter of 0.52 cm were disposed in the membrane separation device 212, and the biological treatment liquid discharged from the reactor 210 was flowed into the tube together with the gas, and the concentrated liquid and the gas were returned to the reactor 210. . The permeate amount (flux) of the membrane separation device 212 was set to 1.0 m/day. The separated water obtained from the membrane separation device 212 was concentrated 10 times at 0.75 MPa by a reverse osmosis membrane device 214 (a spiral reverse osmosis membrane device having a wholly aromatic polyamine-based ultra-low pressure membrane as a reverse osmosis membrane).

以上述條件開始實驗30日後，氫氧化四甲銨被分解，來自膜分離裝置212之分離水的TOC濃度成為5mg/L，生成三甲胺與氨。分離水之TOC基本上是三甲胺，其濃度為4mg/L，剩餘的1mg/L是由微生物生成的高分子有機物。另外，分離水之氨濃度為135mg-N/L~140mg-N/L的範圍。該氨與反應器210內利用甲烷醱酵所產生的二氧化碳(濃度為120mg-C/L左右)反應，生成碳酸氫銨。因此，反應器210之槽內液體的pH值在不添加中和用試劑的情況下即可維持在pH7.0~pH7.5。After the experiment was started under the above conditions for 30 days, tetramethylammonium hydroxide was decomposed, and the TOC concentration of the separated water from the membrane separation device 212 was 5 mg/L to produce trimethylamine and ammonia. The TOC for separating water is basically trimethylamine at a concentration of 4 mg/L, and the remaining 1 mg/L is a high molecular organic substance produced by microorganisms. Further, the ammonia concentration of the separated water is in the range of 135 mg-N/L to 140 mg-N/L. The ammonia reacts with carbon dioxide (concentration of about 120 mg-C/L) produced by methane fermentation in the reactor 210 to form ammonium hydrogencarbonate. Therefore, the pH of the liquid in the tank of the reactor 210 can be maintained at pH 7.0 to pH 7.5 without adding a neutralizing reagent.

對分離水進行脫鹽處理之逆滲透膜裝置214，於實驗開始的60天間可於0.75MPa下、以0.95m/day的通量進行運轉。從逆滲透膜裝置214中獲得的濃縮水，其pH值大約為8.5、三甲胺濃度為40mg-C/L、碳酸氫銨濃度為1,400mg-N/L、高分子有機物濃度為10mg-C/L，鹽類(銨鹽)以及有機物的回收率大約為100%。The reverse osmosis membrane device 214 for desalting the separated water was operated at a flux of 0.95 m/day at 0.75 MPa for 60 days from the start of the experiment. The concentrated water obtained from the reverse osmosis membrane device 214 has a pH of about 8.5, a trimethylamine concentration of 40 mg-C/L, an ammonium hydrogencarbonate concentration of 1,400 mg-N/L, and a high molecular organic concentration of 10 mg-C/. The recovery of L, salts (ammonium salts) and organics is approximately 100%.

在Anammox槽241中以微好氧/無氧條件對濃縮水進行生物處理。對Anammox槽241的負荷為3kg-N/m3 /day。藉由在Anammox槽241中的處理，濃縮水中的三甲胺及氨的99%被生物分解，從Anammox槽241流出之處理液的BOD濃度為10mg/L以下、SS濃度亦為10mg/L以下、氮濃度為10mg-N/L。The concentrated water was biologically treated in the Anammox tank 241 under micro-aerobic/anaerobic conditions. The load on the Anammox tank 241 was 3 kg-N/m 3 /day. By the treatment in the Anammox tank 241, 99% of trimethylamine and ammonia in the concentrated water are biodegraded, and the BOD concentration of the treatment liquid flowing out from the Anammox tank 241 is 10 mg/L or less, and the SS concentration is also 10 mg/L or less. The nitrogen concentration is 10 mg-N/L.

[實施例5][Example 5]

於實施例5中使用模仿圖3之處理裝置300的實驗裝置，除此之外以與實施例4同樣的條件進行實驗。於實施例5中，在鹽水管237的中途以800mg/L的添加量添加作為鎂鹽之2%氯化鎂水溶液，並添加磷酸鉀溶液。另外，添加氫氧化鈉使pH值成為11，使碳酸氫銨發生解離而使銨離子游離。反應柱343的容量為20L，以200L/day的條件通入添加有上述化學品的濃縮水，結果銨離子與磷及鎂反應，生成直徑為2mm~3mm左右的鳥糞石結晶。經由配管344從反應柱343中取出之處理水的TOC濃度為50mg/L、氮濃度為140mg/L，可除去濃縮水中所含氨的90%。另外，從反應柱343中取出鳥糞石結晶，並進行分析，結果其主成分為氨、磷、鎂，幾乎不含重金屬，可用作肥料。The experiment was carried out under the same conditions as in Example 4 except that the experimental apparatus simulating the processing apparatus 300 of Fig. 3 was used in the fifth embodiment. In Example 5, a 2% magnesium chloride aqueous solution as a magnesium salt was added in an amount of 800 mg/L in the middle of the brine tube 237, and a potassium phosphate solution was added. Further, sodium hydroxide was added to bring the pH to 11, and the ammonium hydrogencarbonate was dissociated to release the ammonium ions. The capacity of the reaction column 343 was 20 L, and concentrated water to which the above chemical was added was passed under conditions of 200 L/day. As a result, ammonium ions reacted with phosphorus and magnesium to form struvite crystals having a diameter of about 2 mm to 3 mm. The treated water taken out from the reaction column 343 via the pipe 344 has a TOC concentration of 50 mg/L and a nitrogen concentration of 140 mg/L, and 90% of the ammonia contained in the concentrated water can be removed. Further, the struvite crystals were taken out from the reaction column 343 and analyzed, and as a result, the main components were ammonia, phosphorus, and magnesium, and almost no heavy metals were used, and they were used as fertilizers.

[實施例6][Embodiment 6]

於實施例6中使用模仿圖4之處理裝置400的實驗裝置，除此之外以與實施例4同樣的條件進行實驗。於實施例6中，從未圖示的化學品添加裝置在鹽水管337的中途添加硫酸，使供給至蒸發器445之濃縮水的鹼度成為0(pH 4.8)。蒸發器445是藉由進行減壓並將濃縮水加溫至40℃而進行蒸餾，從蒸餾水管446中取出蒸餾水。蒸餾水的TOC濃度為0.01mg-C/L、氮濃度為0.2mg-N/L。另外，回收殘留於蒸發器445內的硫酸銨漿料，結果可將濃縮水中之銨的98%以硫酸銨漿料形式加以回收。The experiment was carried out under the same conditions as in Example 4 except that the experimental apparatus simulating the processing apparatus 400 of Fig. 4 was used in the sixth embodiment. In Example 6, sulfuric acid was added to the middle of the brine tube 337 from a chemical addition device (not shown), and the alkalinity of the concentrated water supplied to the evaporator 445 was 0 (pH 4.8). The evaporator 445 is distilled by performing a reduced pressure and heating the concentrated water to 40 ° C, and distilled water is taken out from the distillation water pipe 446. The distilled water had a TOC concentration of 0.01 mg-C/L and a nitrogen concentration of 0.2 mg-N/L. Further, the ammonium sulfate slurry remaining in the evaporator 445 is recovered, and as a result, 98% of the ammonium in the concentrated water can be recovered as an ammonium sulfate slurry.

[實施例7][Embodiment 7]

於實施例7中使用模仿圖5之處理裝置500的實驗裝置，進一步以蒸發器445蒸餾利用實施例4的Anammox槽241中的生物處理所獲得的處理液。於實施例7中，供給至蒸發器445之液體的氨濃度為70mg-N/L，比實施例6低，因此為了使pH值降低所必需之酸的添加量成為實施例6的1/20。另外，從蒸發器445中排出之蒸餾水的水質是TOC濃度為0mg-C/L、氮濃度為0mg-N/L。In the seventh embodiment, the experimental apparatus which imitated the processing apparatus 500 of FIG. 5 was used, and the treatment liquid obtained by the biological treatment in the Anammox tank 241 of Example 4 was further distilled by the evaporator 445. In Example 7, the ammonia concentration of the liquid supplied to the evaporator 445 was 70 mg-N/L, which was lower than that of Example 6. Therefore, the amount of acid necessary for lowering the pH was 1/20 of that of Example 6. . Further, the water quality of the distilled water discharged from the evaporator 445 is a TOC concentration of 0 mg-C/L and a nitrogen concentration of 0 mg-N/L.

[比較例3][Comparative Example 3]

比較例3中，於反應器內部設置吹入空氣之散氣裝置，藉此使反應器成為需氧性生物處理槽。除了將反應器改變成需氧性之外，其餘以與實施例4同樣的條件進行實驗時，並未進行需氧性生物處理槽的pH值調整，因此自實驗開始1週後發現產生硝化反應，槽內液體的pH值降低至5.0~5.5左右。其結果，從需氧性生物處理槽流出之處理液的TOC濃度成為100mg/L~120mg/L左右，對從膜分離裝置中獲得的分離水進行脫鹽處理之逆滲透膜裝置的通量成為實施例4的一半。In Comparative Example 3, a diffusing device that blows air was provided inside the reactor, whereby the reactor became an aerobic biological treatment tank. Except that the reactor was changed to aerobicity, the pH adjustment of the aerobic biological treatment tank was not carried out under the same conditions as in Example 4, so that the nitrification reaction was found one week after the start of the experiment. The pH of the liquid in the tank is reduced to about 5.0 to 5.5. As a result, the TOC concentration of the treatment liquid flowing out from the aerobic biological treatment tank is about 100 mg/L to 120 mg/L, and the flux of the reverse osmosis membrane device for desalting the separated water obtained from the membrane separation device is implemented. Half of the example 4.

[比較例4][Comparative Example 4]

於比較例3中，向需氧性生物處理槽中添加氫氧化鈉而將槽內液體的pH值調整為6.5~7.5之範圍。其結果，可使從需氧性生物處理槽流出之處理液的TOC濃度降低至10mg/L。但是，處理液中以130mg/L~140mg/L左右的濃度含有硝酸，另外，由於用以調整pH值而添加的氫氧化鈉使得鹽濃度變高。因此，對從膜分離裝置中獲得的分離水進行脫鹽處理之逆滲透膜裝置的通量限於實施例4的60%。In Comparative Example 3, sodium hydroxide was added to the aerobic biological treatment tank to adjust the pH of the liquid in the tank to a range of 6.5 to 7.5. As a result, the TOC concentration of the treatment liquid flowing out of the aerobic biological treatment tank can be lowered to 10 mg/L. However, the treatment liquid contains nitric acid at a concentration of about 130 mg/L to 140 mg/L, and the sodium hydroxide added to adjust the pH value causes the salt concentration to increase. Therefore, the flux of the reverse osmosis membrane device for desalting the separated water obtained from the membrane separation device is limited to 60% of that of Example 4.

[比較例5][Comparative Example 5]

於比較例4中，在需氧性生物處理槽的後段設置脫氮槽，形成圖6所示構成的處理裝置600。處理裝置600具有需氧性生物處理槽(需氧性反應器610)來代替實施例中使用的厭氧性生物處理裝置(反應器210)，在需氧性反應器610的後段具有保持脫氮菌的脫氮槽613以及再曝氣槽611。向從需氧性反應器610流出的處理液中添加甲醇，向脫氮槽613中添加硫酸將pH值維持在6.5~7.5，進行脫氮處理。來自脫氮槽613的流出液，經由配管632B送至再曝氣槽611，在再曝氣槽611中進行再曝氣後，經由配管632C送至膜分離裝置612。其結果，自實驗開始後2週，對從膜分離裝置612中獲得的分離水進行脫鹽處理之逆滲透膜裝置614的通量成為實施例4的80%。但是，自實驗開始1個月後，逆滲透膜裝置614的通量降低至實施例4的50%。In Comparative Example 4, a denitrification tank was provided in the subsequent stage of the aerobic biological treatment tank to form a treatment apparatus 600 having the configuration shown in Fig. 6. The treatment device 600 has an aerobic biological treatment tank (aerobic reactor 610) instead of the anaerobic biological treatment unit (reactor 210) used in the embodiment, and has a denitrification in the latter stage of the aerobic reactor 610. The denitrification tank 613 and the re-aeration tank 611 of the bacteria. Methanol was added to the treatment liquid flowing out of the aerobic reactor 610, and sulfuric acid was added to the denitrification tank 613 to maintain the pH at 6.5 to 7.5, and the denitrification treatment was performed. The effluent from the denitrification tank 613 is sent to the re-aeration tank 611 via the pipe 632B, re-aerated in the re-aeration tank 611, and sent to the membrane separation device 612 via the pipe 632C. As a result, the flux of the reverse osmosis membrane device 614 for desalting the separated water obtained from the membrane separation device 612 was 80% of that of Example 4 two weeks after the start of the experiment. However, the flux of the reverse osmosis membrane device 614 was reduced to 50% of Example 4 one month after the start of the experiment.

因此，取出逆滲透膜對其進行顯微鏡觀察，結果有大量的生物膜附著於表面。實施例4中所使用之逆滲透膜裝置的逆滲透膜上幾乎未附著生物膜，因此可推斷比較例5中由於生物膜的附著而導致通量降低。於實施例中，在逆滲透膜上未附著生物膜的原因可認為是以下兩點。於逆滲透膜裝置中，濃縮鹽類使鹽水的pH值上升至8.5，因此從碳酸氫銨中解離出氨，由於氨的毒性而抑制微生物的增殖。另外，作為其他原因，可舉出：甲烷生成菌群與需氧性微生物相比增殖速度較慢，難以形成生物膜。Therefore, the reverse osmosis membrane was taken out and observed under a microscope, and as a result, a large amount of biofilm adhered to the surface. Since the biofilm was hardly adhered to the reverse osmosis membrane of the reverse osmosis membrane device used in Example 4, it was estimated that the flux was lowered due to the adhesion of the biofilm in Comparative Example 5. In the examples, the reason why the biofilm was not attached to the reverse osmosis membrane was considered to be the following two points. In the reverse osmosis membrane device, the concentration of the salt increases the pH of the brine to 8.5, so that ammonia is removed from the ammonium hydrogencarbonate, and the proliferation of the microorganism is inhibited by the toxicity of ammonia. Further, for other reasons, the methane-producing microbial group has a slower proliferation rate than the aerobic microorganism, and it is difficult to form a biofilm.

由以上所述顯示，利用甲烷生成菌群對含有有機物的水進行厭氧性處理，藉此可在不添加pH值調整劑的情況下將有機物生物分解，且可抑制污染分離膜之高分子有機物的生成量。As described above, the methane-producing microbial group is subjected to anaerobic treatment of the organic-containing water, whereby the organic substance can be biodegraded without adding a pH adjusting agent, and the polymer organic substance contaminating the separation membrane can be suppressed. The amount of production.

另外，在利用甲烷生成菌群的厭氧性處理步驟中，由氨與二氧化碳生成碳酸氫銨，在不對其進行需氧性處理的情況下在逆滲透膜裝置中進行濃縮，藉此可抑制在逆滲透膜裝置中形成生物膜。即，可防止將以厭氧性處理步驟無法除去的物質在逆滲透膜裝置中進行濃縮時對逆滲透膜的污染。Further, in the anaerobic treatment step using the methane-producing microflora, ammonium bicarbonate is formed from ammonia and carbon dioxide, and is concentrated in the reverse osmosis membrane device without aerobic treatment, thereby suppressing A biofilm is formed in the reverse osmosis membrane device. That is, it is possible to prevent contamination of the reverse osmosis membrane when the substance which cannot be removed by the anaerobic treatment step is concentrated in the reverse osmosis membrane apparatus.

[產業上的可利用性][Industrial availability]

本發明可用於對含有有機物的水進行生物處理而再利用於純水製造。The present invention can be used for biological treatment of water containing organic matter and reuse in pure water production.

雖然本發明已以實施例揭露如上，然其並非用以限定本發明，任何所屬技術領域中具有通常知識者，在不脫離本發明之精神和範圍內，當可作些許之更動與潤飾，故本發明之保護範圍當視後附之申請專利範圍所界定者為準。Although the present invention has been disclosed in the above embodiments, it is not intended to limit the invention, and any one of ordinary skill in the art can make some modifications and refinements without departing from the spirit and scope of the invention. The scope of the invention is defined by the scope of the appended claims.

100、200、300、400、500．．．生物處理裝置100, 200, 300, 400, 500. . . Biological treatment device

110．．．厭氧性生物處理槽110. . . Anaerobic biological treatment tank

112、212．．．膜分離裝置112, 212. . . Membrane separation device

114、214、614．．．逆滲透膜裝置114, 214, 614. . . Reverse osmosis membrane device

121、221、621．．．第1熱交換器(熱回收加熱裝置)121, 221, 621. . . First heat exchanger (heat recovery heating device)

122、222、622．．．第2熱交換器(熱回收加熱裝置)122, 222, 622. . . Second heat exchanger (heat recovery heating device)

130、230．．．原水管130, 230. . . Raw water pipe

131、231．．．排氣管131, 231. . . exhaust pipe

132、232．．．處理液管132, 232. . . Treatment liquid tube

133、233．．．返送管133, 233. . . Return tube

134、234．．．分離水管134, 234. . . Separation water pipe

135、235．．．排泥管135, 235. . . Drain pipe

136、236．．．滲透水管136, 236. . . Permeate pipe

137、237．．．鹽水管137, 237. . . Brine tube

138、238、242、344、446、630、631、632、632B、632C、633、634、635、636、637、638、639、642．．．配管138, 238, 242, 344, 446, 630, 631, 632, 632B, 632C, 633, 634, 635, 636, 637, 638, 639, 642. . . Piping

139、239．．．流體管139, 239. . . Fluid tube

210．．．厭氧性生物處理槽(反應器)210. . . Anaerobic biological treatment tank (reactor)

241、641．．．Anammox槽(濃縮水處理裝置)241, 641. . . Anammox tank (concentrated water treatment unit)

343．．．反應柱343. . . Reaction column

445．．．蒸發器445. . . Evaporator

600．．．比較例的生物處理裝置600. . . Comparative biological treatment device

610．．．需氧性生物處理槽(需氧性反應器)610. . . Aerobic biological treatment tank (aerobic reactor)

611．．．再曝氣層611. . . Re-aeration layer

612．．．膜分離裝置612. . . Membrane separation device

613．．．脫氮槽613. . . Nitrogen removal tank

圖1是本發明第一實施形態之生物處理裝置的模式圖。Fig. 1 is a schematic view showing a biological treatment apparatus according to a first embodiment of the present invention.

圖2是本發明第二實施形態之生物處理裝置的模式圖。Fig. 2 is a schematic view showing a biological treatment apparatus according to a second embodiment of the present invention.

圖3是本發明第三實施形態之生物處理裝置的模式圖。Fig. 3 is a schematic view showing a biological treatment apparatus according to a third embodiment of the present invention.

圖4是本發明第四實施形態之生物處理裝置的模式圖。Fig. 4 is a schematic view showing a biological treatment apparatus according to a fourth embodiment of the present invention.

圖5是本發明第五實施形態之生物處理裝置的模式圖。Fig. 5 is a schematic view showing a biological treatment apparatus according to a fifth embodiment of the present invention.

圖6是比較例5中所使用實驗裝置的模式圖。Fig. 6 is a schematic view showing an experimental apparatus used in Comparative Example 5.

100．．．生物處理裝置100. . . Biological treatment device

110．．．厭氧性生物處理槽(反應器)110. . . Anaerobic biological treatment tank (reactor)

112．．．膜分離裝置112. . . Membrane separation device

114．．．逆滲透膜裝置114. . . Reverse osmosis membrane device

121．．．第1熱交換器(熱回收加熱裝置)121. . . First heat exchanger (heat recovery heating device)

122．．．第2熱交換器(熱回收加熱裝置)122. . . Second heat exchanger (heat recovery heating device)

130．．．原水管130. . . Raw water pipe

131．．．排氣管131. . . exhaust pipe

132．．．處理液管132. . . Treatment liquid tube

133．．．返送管133. . . Return pipe

134．．．分離水管134. . . Separation water pipe

135．．．排泥管135. . . Drain pipe

136．．．滲透水管136. . . Permeate pipe

137．．．鹽水管137. . . Brine tube

138．．．配管138. . . Piping

139．．．流體管139. . . Fluid tube

Claims (18)

一種含有有機物的水的生物處理方法，包括：將含有有機物的水導入厭氧性生物處理槽中；利用該厭氧性生物處理槽內的甲烷生成菌群進行厭氧性生物處理；將利用該厭氧性生物處理所獲得的處理液在不進行需氧性生物處理的情況下，進行膜分離；以逆滲透膜對利用該膜分離所獲得的分離水進行處理。A biological treatment method for water containing organic matter, comprising: introducing water containing organic matter into an anaerobic biological treatment tank; performing anaerobic biological treatment using the methane-producing microflora in the anaerobic biological treatment tank; The treatment liquid obtained by the anaerobic biological treatment is subjected to membrane separation without aerobic biological treatment, and the separated water obtained by the membrane separation is treated with a reverse osmosis membrane. 如申請專利範圍第1項所述之含有有機物的水的生物處理方法，其中該含有有機物的水中，單體有機物相對於總有機碳的比例大於等於70%。The biological treatment method of the organic-containing water according to claim 1, wherein the ratio of the monomer organic matter to the total organic carbon in the organic-containing water is 70% or more. 如申請專利範圍第1項或第2項所述之含有有機物的水的生物處理方法，其中將該厭氧性生物處理槽內的液體的溫度設為大於等於15℃小於等於40℃而進行該厭氧性處理。The biological treatment method of the organic-containing water according to the first or second aspect of the invention, wherein the temperature of the liquid in the anaerobic biological treatment tank is 15 ° C or more and 40 ° C or less Anaerobic treatment. 如申請專利範圍第3項所述之含有有機物的水的生物處理方法，其中該處理液於該厭氧性處理的過程加溫，再進行該膜分離以及該逆滲透膜處理。The biological treatment method of the organic-containing water according to claim 3, wherein the treatment liquid is heated in the anaerobic treatment process, and the membrane separation and the reverse osmosis membrane treatment are performed. 如申請專利範圍第2項所述之含有有機物的水的生物處理方法，其中該單體有機物是選自以氫氧化四甲銨、單乙醇胺、二乙二醇單丁醚、異丙醇、二甲基乙醯胺、二甲基甲醯胺、二甲基亞碸以及乙酸所組成之族群中的任意一種以上。The biological treatment method of the organic substance-containing water according to claim 2, wherein the monomer organic substance is selected from the group consisting of tetramethylammonium hydroxide, monoethanolamine, diethylene glycol monobutyl ether, isopropanol, and Any one or more of the group consisting of methyl acetamide, dimethylformamide, dimethyl hydrazine, and acetic acid. 一種含有有機物的水的生物處理裝置，包括：厭氧性生物處理槽，用以導入含有有機物的水並利用甲烷生成菌群生成甲烷；膜分離裝置，與該厭氧性生物處理槽相連接，用以對從該厭氧性生物處理槽中排出的處理液進行膜分離；逆滲透膜裝置，用以處理該膜分離裝置的分離水。A biological treatment device for water containing organic matter, comprising: an anaerobic biological treatment tank for introducing water containing organic matter and generating methane by using a methane-producing flora; and a membrane separation device connected to the anaerobic biological treatment tank, It is used for membrane separation of the treatment liquid discharged from the anaerobic biological treatment tank; and a reverse osmosis membrane device for treating the separated water of the membrane separation device. 如申請專利範圍第6項所述之含有有機物的水的生物處理裝置，其中該含有有機物的水中，單體有機物相對於總有機碳的包含比例大於等於70%。The biological treatment apparatus of the organic substance-containing water according to claim 6, wherein the content of the monomeric organic matter to the total organic carbon in the organic-containing water is 70% or more. 如申請專利範圍第6項或第7項所述之含有有機物的水的生物處理裝置，其構成包括：該厭氧性處理槽，是將槽內液體的溫度設為大於等於15℃小於等於40℃而進行運轉，該處理液於該厭氧性處理槽中在加溫狀態下供給至該膜分離裝置以及該逆滲透膜裝置。The biological treatment device for water containing organic matter according to claim 6 or 7, wherein the anaerobic treatment tank has a temperature of the liquid in the tank of 15 ° C or more and 40 or less. The operation is carried out at ° C, and the treatment liquid is supplied to the membrane separation device and the reverse osmosis membrane device in a heated state in the anaerobic treatment tank. 如申請專利範圍第8項所述之含有有機物的水的生物處理裝置，更包括熱回收加熱裝置，用以熱回收該逆滲透膜裝置的滲透水，並利用所回收的熱來加溫該厭氧性處理槽。The biological treatment device for the organic substance-containing water according to claim 8 further includes a heat recovery heating device for heat recovery of the permeated water of the reverse osmosis membrane device, and using the recovered heat to warm the anaerobic Oxygen treatment tank. 如申請專利範圍第6項所述之含有有機物的水的生物處理裝置，其中該膜分離裝置包括微量濾膜或者超濾膜。The biological treatment device for organic-containing water according to claim 6, wherein the membrane separation device comprises a microfiltration membrane or an ultrafiltration membrane. 如申請專利範圍第6項所述之含有有機物的水的生物處理裝置，更包括清洗裝置，用以供給在該厭氧性生物處理槽中所產生的生物生成氣至該膜分離裝置，以對該膜分離裝置進行曝氣清洗。The biological treatment device for the organic substance-containing water according to claim 6, further comprising a cleaning device for supplying the bio-generated gas generated in the anaerobic biological treatment tank to the membrane separation device, The membrane separation device performs aeration cleaning. 一種含有有機物的水的生物處理裝置，包括：厭氧性生物處理槽，用以導入含有有機物的水並利用甲烷生成菌群生成甲烷；膜分離裝置，與該厭氧性生物處理槽相連接，用以對從該厭氧性生物處理槽排出的處理液進行膜分離；逆滲透膜裝置，用以處理該膜分離裝置的分離水理；濃縮水處理裝置，用以處理該逆滲透膜裝置的濃縮水。A biological treatment device for water containing organic matter, comprising: an anaerobic biological treatment tank for introducing water containing organic matter and generating methane by using a methane-producing flora; and a membrane separation device connected to the anaerobic biological treatment tank, a membrane separation for treating the treatment liquid discharged from the anaerobic biological treatment tank; a reverse osmosis membrane device for treating the separation water treatment of the membrane separation device; and a concentrated water treatment device for treating the reverse osmosis membrane device Concentrated water. 如申請專利範圍第12項所述之含有有機物的水的生物處理裝置，其中該濃縮水處理裝置包括與該厭氧性生物處理槽不同的生物處理槽。The biological treatment apparatus of the organic-containing water according to claim 12, wherein the concentrated water treatment apparatus comprises a biological treatment tank different from the anaerobic biological treatment tank. 如申請專利範圍第12項或第13項所述之含有有機物的水的生物處理裝置，其中該濃縮水處理裝置包括蒸發器，導入該濃縮水使其蒸發而取出蒸餾水。The biological treatment apparatus of the organic substance-containing water according to claim 12 or 13, wherein the concentrated water treatment apparatus includes an evaporator, and the concentrated water is introduced to evaporate to take out distilled water. 如申請專利範圍第12項所述之含有有機物的水的生物處理裝置，其中該濃縮水處理裝置包括反應柱，將使該濃縮水中的雜質不溶化的化學品添加至該濃縮水中，並分離出固形物。The biological treatment apparatus of the organic substance-containing water according to claim 12, wherein the concentrated water treatment apparatus includes a reaction column, and a chemical that insoluates impurities in the concentrated water is added to the concentrated water, and the solid is separated. Things. 一種含有有機物的水的生物處理方法，包括：將含有有機物的水導入包含甲烷生成菌群的厭氧性生物處理槽中進行厭氧性生物處理；將利用該厭氧性生物處理所獲得的處理液在不進行需氧性生物處理的情況下進行膜分離；以逆滲透膜處理利用該膜分離所獲得的分離水；對利用該逆滲透膜處理所獲得的濃縮水進行處理。A biological treatment method for water containing organic matter, comprising: introducing water containing organic matter into an anaerobic biological treatment tank containing a group of methane-producing bacteria for anaerobic biological treatment; and treating by using the anaerobic biological treatment The liquid is subjected to membrane separation without aerobic biological treatment; the separated water obtained by the membrane separation is treated with a reverse osmosis membrane; and the concentrated water obtained by the reverse osmosis membrane treatment is treated. 如申請專利範圍第16項所述之含有有機物的水的生物處理方法，其中該含有有機物的水中含有氮化合物。The biological treatment method of the organic-containing water according to claim 16, wherein the organic-containing water contains a nitrogen compound. 如申請專利範圍第16項或第17項所述之含有有機物的水的生物處理方法，其中對該濃縮水進行與該厭氧性生物處理不同的生物處理；利用蒸發器對該濃縮水進行蒸餾處理；以及/或者對該濃縮水利用化學品使雜質不溶化再進行處理。The biological treatment method of the organic substance-containing water according to claim 16 or 17, wherein the concentrated water is subjected to biological treatment different from the anaerobic biological treatment; and the concentrated water is distilled by an evaporator. Processing; and/or treating the concentrated water with chemicals to render the impurities insoluble.
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