WO2020015435A1 - 一种生活污水的处理方法 - Google Patents

一种生活污水的处理方法 Download PDF

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WO2020015435A1
WO2020015435A1 PCT/CN2019/085159 CN2019085159W WO2020015435A1 WO 2020015435 A1 WO2020015435 A1 WO 2020015435A1 CN 2019085159 W CN2019085159 W CN 2019085159W WO 2020015435 A1 WO2020015435 A1 WO 2020015435A1
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treatment
anaerobic
membrane
domestic sewage
aerobic
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PCT/CN2019/085159
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English (en)
French (fr)
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严滨
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厦门理工学院
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Priority to US16/769,924 priority Critical patent/US11352278B2/en
Priority to JP2020529254A priority patent/JP2021504118A/ja
Publication of WO2020015435A1 publication Critical patent/WO2020015435A1/zh

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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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
    • 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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/301—Aerobic and anaerobic treatment in the same reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/02—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor characterised by their properties
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/08—Hollow fibre membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/06—Organic material
    • 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
    • C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • 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
    • C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2688—Biological processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2315/00—Details relating to the membrane module operation
    • B01D2315/06—Submerged-type; Immersion type
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2325/00—Details relating to properties of membranes
    • B01D2325/02—Details relating to pores or porosity of the membranes
    • B01D2325/0283—Pore size
    • B01D2325/02834—Pore size more than 0.1 and up to 1 µm
    • 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
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • 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
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C02F2101/163—Nitrates
    • 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
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C02F2101/166—Nitrites
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/04—Oxidation reduction potential [ORP]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/20—Total organic carbon [TOC]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/44—Time
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C02F3/1273—Submerged membrane bioreactors
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the invention relates to the technical field of wastewater treatment, in particular to a method for treating domestic sewage.
  • Domestic sewage is the waste water discharged from the daily life of residents. It mainly comes from residential buildings and public buildings, such as houses, institutions, schools, hospitals, shops, public places, and industrial enterprises' toilets. Pollutants contained in domestic sewage are mainly organic matter (such as protein, carbohydrate, fat, urea, ammonia nitrogen, etc.) and a large number of pathogenic microorganisms (such as parasite eggs and intestinal infectious viruses).
  • the conventional biochemical treatment process can effectively reduce the COD, BOD, and SS of sewage, but generally only remove 10% to 20% of the N that is present in the sewage.
  • a large amount of nitrogen-containing sewage is discharged into the water body, which is an important source of water and rivers. , Lake pollution and eutrophication.
  • the microorganisms oxidized the nitrogen in the sewage into nitrite or nitrate, but did not discharge it.
  • denitrifying bacteria reduce nitrate and release molecular nitrogen (N 2 ) or nitrous oxide (N 2 O), which can remove nitrogen from water bodies. This process is called denitrification.
  • This process uses NO 2 - and NO 3 - are the ultimate electron acceptors for respiration, reducing nitric acid to nitrogen (N 2 ).
  • the present invention provides a method for treating domestic sewage with high nitrogen removal rate and simple operation.
  • a method for treating domestic sewage includes the following steps:
  • the domestic sewage after the preliminary treatment enters the membrane bioreactor for anaerobic-aerobic cycle treatment; the membrane bioreactor is filled with a hollow fiber membrane containing a quinone group.
  • the operating flux of the quinone-containing hollow fiber membrane in the membrane bioreactor is greater than or equal to 10 L / (m 2 ⁇ h), and the average pore diameter of the membrane is 0.1 micrometer.
  • the mass fraction of the quinone-based compound in the quinone-containing hollow fiber membrane is greater than 5%.
  • the sludge concentration in the membrane bioreactor is 4-6 g / L.
  • the time of a single anaerobic treatment during the anaerobic-aerobic cycle treatment is 50 to 70 minutes.
  • the redox potential of the anaerobic treatment is -50 to 0 mV.
  • the time of a single aerobic treatment during the anaerobic-aerobic cycle treatment is 20-40 minutes.
  • the amount of dissolved oxygen in the aerobic treatment is 1 to 3 mg / L.
  • the hydraulic retention time of the wastewater after the preliminary treatment in the membrane bioreactor is 4-6 hours.
  • the present invention has the following advantages:
  • the invention provides a method for treating domestic sewage.
  • the domestic sewage is initially treated through a grille and sediment, and large solid particles in the domestic sewage are removed.
  • the initially treated domestic sewage is carried out in a membrane bioreactor.
  • Anaerobic-aerobic cycle treatment during aerobic treatment, microorganisms oxidize nitrogen in sewage into nitrite or nitrate. Under anaerobic conditions, denitrifying bacteria in microorganisms reduce nitrate or nitrite.
  • Molecular nitrogen (N 2 ) or nitrous oxide (N 2 O) is released.
  • the membrane bioreactor of the present invention is filled with a hollow fiber membrane containing a quinone group.
  • the quinone group can be used as an electron in the process of microbial nitrogen removal.
  • the transfer carrier is involved in the denitrification process, participates in and promotes the reduction process of nitrate (nitrite), and increases the rate of denitrification under anaerobic conditions, so as to achieve the purpose of efficient denitrification and achieve the purpose of simultaneously removing COD and denitrification.
  • the results of the examples show that when the method provided by the present invention is used to treat domestic sewage, the COD content in the effluent is less than 20 mg / L, the total nitrogen content is less than 5 mg / L, and the total suspended particulates (SS) is 0.
  • FIG. 1 is a schematic diagram of a domestic sewage treatment process according to an embodiment of the present invention
  • Figure 1 1-grid; 2-settling tank; 3-membrane bioreactor; 4-hollow fiber membrane containing quinone group; 5-stirring device; 6-aeration device; 7-pump.
  • the invention provides a method for treating domestic sewage, including the following steps:
  • the domestic sewage after the preliminary treatment enters the membrane bioreactor for anaerobic-aerobic cycle treatment; the membrane bioreactor is filled with a hollow fiber membrane containing a quinone group.
  • the domestic sewage is initially processed through the grille and the sand in turn.
  • the invention has no special requirements on the source of domestic sewage.
  • the COD value of the domestic wastewater is preferably greater than 200 mg / L
  • the total nitrogen content is preferably greater than 30 mg / L
  • the total suspended solids (SS) content is preferably greater than 50 mg. / L.
  • the present invention has no special requirements for the specific methods of sand sedimentation and grill treatment, and the sand sedimentation and grill treatment can be performed by methods well known to those skilled in the art.
  • the present invention removes large particles of solids that can be removed by gravity in sewage through sedimentation treatment; intercepts large particles of solids suspended in sewage through grid treatment.
  • the present invention enters the treated sewage into the membrane bioreactor for anaerobic-aerobic cycle treatment; the membrane bioreactor is filled with a hollow fiber membrane containing quinone groups.
  • the membrane bioreactor according to the present invention is an anaerobic-aerobic integrated membrane bioreactor (AOMBR).
  • AOMBR is filled with a hollow fiber membrane containing a quinone group, and the central part of the AOMBR is equipped with a stirring device. Stirring during anaerobic treatment; aeration device at the bottom for aeration during aerobic treatment to provide oxygen.
  • the circulation of domestic sewage is preferably realized by a pump.
  • the membrane bioreactor is filled with a quinone group-containing hollow fiber membrane;
  • the running flux of the quinone group-containing hollow fiber membrane is preferably 10 L / (m 2 ⁇ h) or more, and more preferably 10 to 15 L / (m 2 ⁇ h);
  • the mass fraction of the quinone-based compound in the quinone-containing hollow fiber membrane is preferably greater than 5%, more preferably 10% to 15%;
  • the average pore diameter is preferably 0.1 ⁇ m.
  • the membrane filament having an area of 1 m 2 can filter at least 10 L of wastewater for 1 h.
  • the present invention preferably determines the total area of the hollow fiber membrane according to the treatment amount of domestic sewage; the present invention provides a quinone-based hollow fiber membrane
  • the hollow fiber membrane containing quinone group can be anthraquinone-functionalized polyvinylidene fluoride membrane.
  • the preparation method is as follows Those skilled in the art can perform the method.
  • the filling method of the quinone group-containing hollow fiber membrane is not particularly required, and the filling method may be performed by a method well known to those skilled in the art.
  • the present invention has no special requirements on the water inlet rate of the preliminary treated domestic sewage in the membrane bioreactor. In specific embodiments of the present invention, specific details can be determined according to factors such as the amount of sewage treated and the cross-sectional area of the inlet pipe. Water inlet rate.
  • the sludge concentration in the membrane bioreactor is preferably 7 to 8 g / L, and more preferably 7.5 g / L.
  • the present invention has no special requirements on the type of the sludge, and the sludge for sewage treatment may be used as known to those skilled in the art.
  • the anaerobic treatment is performed first, and then the aerobic treatment is performed, and the circulation is sequentially performed.
  • the time of a single anaerobic treatment during the anaerobic-aerobic cycle treatment is preferably 50 to 70 minutes, more preferably 60 minutes; the oxidation-reduction potential of the anaerobic treatment is preferably -50 to 0 mV, More preferably, it is -40 to -30 mV.
  • anaerobic treatment is preferably performed under stirring conditions.
  • the rotation speed of the stirring is preferably 5 revolutions / min or less, and more preferably 3 to 4 revolutions / min.
  • a hydraulic stirrer is preferably provided in the membrane bioreactor.
  • a hollow fiber membrane is preferably packed around the membrane bioreactor, and a hydraulic stirrer is set in the center of the membrane bioreactor.
  • the hollow fiber membrane contains a quinone group, which can be used as an electron transfer carrier to participate in the denitrification process during the microbial denitrification process, participate in and promote the reduction process of nitrate (nitrite), and accelerate The rate of the denitrification process in the oxygen treatment process, so as to achieve the purpose of efficient denitrification.
  • the present invention efficiently reduces the nitrate nitrogen in domestic sewage to nitrogen through anaerobic treatment, and simultaneously degrades organic matter in domestic sewage to remove wastewater from wastewater. Decomposition of large molecular weight organic matter into smaller molecular weight organic matter, reducing the COD value of domestic sewage.
  • the time of a single aerobic treatment during the anaerobic-aerobic cycle treatment is preferably 20 to 40 minutes, more preferably 30 minutes; and the amount of dissolved oxygen in the aerobic treatment is preferably 1 to 3 mg / L. , More preferably 2 mg / L.
  • the present invention preferably provides oxygen for aerobic treatment by aeration.
  • the aeration process can agitate sewage, so aerobic treatment process does not need to be stirred.
  • the present invention preferably provides an aeration device at the bottom of the membrane bioreactor. There are no special requirements for the aeration device, and an aeration device well known to those skilled in the art can be used to provide oxygen for aerobic treatment.
  • ammonia nitrogen in domestic sewage is oxidized to nitrate nitrogen or nitrite nitrogen, and small molecular weight organics in domestic sewage are decomposed into inorganic substances, which further reduces the COD value of domestic sewage.
  • the hydraulic retention time of the domestic sewage after the preliminary treatment in the membrane bioreactor is preferably 4 to 6 hours, and more preferably 5 hours; within the hydraulic retention time, the anaerobic-aerobic cycle treatment The cycle is greater than 2 cycles.
  • the aeration device is turned off, the stirring device is turned on, and the anaerobic treatment is performed after 50 to 70 minutes.
  • Turn off the agitation device turn on the aeration device, perform aerobic treatment for 20-40 minutes, and then perform anaerobic treatment, and so on, and so on, until the preliminary treatment of domestic sewage in the membrane bioreactor's hydraulic retention time reaches 4-6 hours, then The treated sewage is discharged.
  • the effluent is preferably carried out in the aerobic treatment stage.
  • the aeration treatment in the aerobic treatment stage can agitate the membrane filaments.
  • the sludge is not easy to adhere to the surface of the membrane filaments when the water is discharged. As a result, sludge adheres to the surface of the membrane filament, which causes pollution of the membrane filament and affects the water outlet rate.
  • FIG. 1 The schematic diagram of the water treatment process of the present invention is shown in FIG. 1.
  • Domestic sewage flows through the grit chamber 1 and the grille 2 for preliminary treatment.
  • the preliminary treated domestic sewage enters the membrane bioreactor (AOMBR) 3 for anaerobic-good.
  • AOMBR membrane bioreactor
  • the membrane bioreactor is filled with quinone-based hollow fiber membranes 4, the stirring device 5 is turned on during the anaerobic treatment, the aeration device 6 is turned off, and the aeration device 6 is turned off during the aerobic treatment, and the aeration device 6 is turned on During the treatment process, the pump 7 is used to realize the circulation of sewage, and the sewage that has reached the standard after the circulation treatment is introduced to the sewage treatment system discharge port through a suction pump for discharge.
  • the present invention has no special requirements for the treatment method of sludge in the membrane bioreactor. Those skilled in the art may perform the treatment. In specific embodiments of the present invention, it is preferable to regularly discharge sludge to ensure the water treatment effect.
  • the initial content of COD in domestic sewage is 400mg / L, the initial content of total nitrogen is 40mg / L, and the initial content of SS is 200mg / L;
  • the domestic sewage after the preliminary treatment enters the anaerobic-aerobic integrated membrane bioreactor (hereinafter referred to as AOMBR) for anaerobic-aerobic cycle treatment.
  • AOMBR anaerobic-aerobic integrated membrane bioreactor
  • the membrane filaments filled in the reactor are hollow fiber membranes containing quinone groups;
  • the sludge concentration in the AOMBR reactor is 4g / L;
  • AOMBR operates according to the following parameters: no aeration during anaerobic treatment, hydraulic stirring for 60min, and redox potential of -50mV; and then aerobic treatment for 30min, aerobic treatment exposure Gas, without stirring, the dissolved oxygen is controlled at 3mg / L, and the water is passed through the membrane filaments during the aerobic treatment; the hydraulic retention time HRT is 5h, and then the wastewater is discharged to the standard.
  • the COD, total nitrogen and SS content in the untreated domestic sewage are higher.
  • the COD content in the effluent is less than 20mg / L, and the total nitrogen content is less than 5mg / L
  • the denitrification rate of the domestic sewage treatment method provided by the present invention can reach about 87.5%, which achieves the purpose of efficient denitrification and achieves the effect of simultaneous removal of ammonia nitrogen and COD.
  • the initial content of COD in domestic sewage is 320mg / L
  • the initial content of ammonia nitrogen is 62mg / L
  • the initial content of SS is 85mg / L;
  • AOMBR anaerobic-aerobic integrated membrane bioreactor
  • the sludge concentration in the AOMBR reactor is 6g / L;
  • AOMBR operates according to the following parameters: no aeration during anaerobic treatment, hydraulic stirring for 60min, and redox potential of -20mV; and then aerobic treatment for 30min, aerobic treatment exposure Gas, without stirring, the dissolved oxygen is controlled at 2.5mg / L, and the water is discharged through the membrane filaments during the aerobic treatment; the hydraulic retention time HRT is 5.5h, and then the wastewater is discharged up to the standard.
  • the COD content in the treated sewage is less than 20mg / L and the total nitrogen content is less than 5mg / L, in which the SS is completely removed. It can be seen that the treatment of the sewage provided by the present invention The denitrification rate of the method can reach about 91.9%, which achieves the purpose of efficient denitrification and achieves the effect of simultaneous removal of ammonia nitrogen and COD.

Abstract

一种生活污水的处理方法，其包括以下步骤：将生活污水依次经格栅（1）和沉沙进行初步处理；初步处理后的生活污水进入膜生物反应器（3）中进行厌氧-好氧循环处理；膜生物反应器（3）中装填有含有醌基的中空纤维膜（4）。

Description

一种生活污水的处理方法
本申请要求于2018年07月17日提交中国专利局、申请号为201810784970.3、发明名称为“一种生活污水的处理方法”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本发明涉及废水处理技术领域，特别涉及一种生活污水的处理方法。
背景技术
生活污水是居民日常生活中排出的废水，主要来源于居住建筑和公共建筑，如住宅、机关、学校、医院、商店、公共场所及工业企业卫生间等。生活污水所含的污染物主要是有机物(如蛋白质、碳水化合物、脂肪、尿素、氨氮等)和大量病原微生物(如寄生虫卵和肠道传染病毒等)。常规的生化处理工艺可以有效降低污水的COD、BOD和SS，但对污水中同时存在的N一般仅能去除10％～20％，大量含氮的污水排入水体，是许多重要水源地、江河、湖泊污染和富营养化的原因之一。
常规好氧处理工艺过程中，微生物将污水中的氮氧化成亚硝酸盐或硝酸盐，并未排出水体。在缺氧条件下，反硝化细菌还原硝酸盐，释放出分子态氮(N 2)或一氧化二氮(N 2O)，可脱除水体中的氮，称为反硝化过程，这个过程利用NO 2 -和NO 3 -为呼吸作用的最终电子受体，把硝酸还原成氮(N 2)。
基于以上原理，近年来国内外学者不断致力于生物法脱氮工艺的研究，典型代表有A/O，A2/O，UCT，五段Bardenpho，Phostrip等。这些工艺利用好氧-兼氧(缺氧)的联合运行方式，在缺氧过程中，利用反硝化细菌脱除氮，减少了污水中氮的排放，但现有工艺仍存在着诸多弊端，许多工艺的革新单从工程的角度改变参数，缺少对系统内生物因素的深入研究，未能从微生物的角度调控工艺，且上述工艺对污水中氮的脱除率仅能达到55～60％，脱氮率仍然较低。
发明内容
为了克服现有技术的上述缺点，本发明提供一种脱氮率高、操作简单的生活污水的处理方法。
为了解决上述技术问题，本发明采用的技术方案是：
一种生活污水的处理方法，包括以下步骤：
将生活污水依次经格栅和沉沙进行初步处理；
初步处理后的生活污水进入膜生物反应器中进行厌氧-好氧循环处理；所述膜生物反应器中装填有含有醌基的中空纤维膜。
优选的，所述含有醌基的中空纤维膜在膜生物反应器中的运行通量大于等于10L/(m 2·h)，膜平均孔径为0.1微米。
优选的，所述含有醌基的中空纤维膜中醌基化合物的质量分数大于5％。
优选的，所述膜生物反应器中的污泥浓度为4～6g/L。
优选的，所述厌氧-好氧循环处理过程中单次厌氧处理的时间为50～70min。
优选的，所述厌氧处理的氧化还原电位为-50～0mV。
优选的，所述厌氧-好氧循环处理过程中单次好氧处理的时间为20～40min。
优选的，所述好氧处理的溶氧量为1～3mg/L。
优选的，所述初步处理后的废水在膜生物反应器中的水力停留时间为4～6h。
本发明与现有技术相比，具有以下优点：
本发明提供了一种生活污水的处理方法，首先将生活污水经格栅和沉沙进行初步处理，将生活污水中的大颗粒固体物去除，初步处理后的生活污水进入膜生物反应器中进行厌氧-好氧循环处理；在好氧处理过程中，微生物将污水中的氮氧化成亚硝酸盐或硝酸盐，在厌氧条件下，微生物中的反硝化细菌还原硝酸盐或亚硝酸盐，释放出分子态氮(N 2)或一氧化二氮(N 2O)，本发明的膜生物反应器中装填有含有醌基的中空纤维膜，醌基在微生物脱氮过程中，可以作为电子转移载体介入反硝化过程，参与并促进硝酸盐(亚硝酸盐)的还原过程，提高厌氧条件下反硝化的速率，从而达到高效脱氮的目的，实现去除COD和脱氮同时完成的目的。实施例结果表明，使用本发明提供的方法对生活污水进行处理，出水中COD含量小于20mg/L，总氮含量小于5mg/L，悬浮物总颗粒(SS)为0。
说明书附图
图1为本发明实施例提供的生活污水处理流程示意图；
图1中：1-格栅；2-沉砂池；3-膜生物反应器；4-含有醌基的中空纤维膜；5-搅拌装置；6-曝气装置；7-泵。
具体实施方式
下面结合实施例和附图对本发明进一步说明。
本发明提供了一种生活污水的处理方法，包括以下步骤：
将生活污水依次经格栅和沉沙进行初步处理；
初步处理后的生活污水进入膜生物反应器中进行厌氧-好氧循环处理；所述膜生物反应器中装填有含有醌基的中空纤维膜。
本发明将生活污水依次经格栅和沉沙进行初步处理。本发明对生活污水的来源没有特殊要求，日常生活中排出的、来源于居住建筑和公共建筑，如住宅、机关、学校、医院、商店、公共场所及工业企业卫生间等的废水都可以使用本发明的方法进行处理；在本发明的具体实施例中，所述生活废水的COD值优选为大于200mg/L，总氮含量优选为大于30mg/L，悬浮物总颗粒(SS)含量优选为大于50mg/L。
本发明对沉沙和格栅处理的具体方法没有特殊要求，使用本领域技术人员熟知的方法进行沉沙和格栅处理即可。本发明通过沉沙处理将污水中可以用重力去除的大颗粒固体去除；通过格栅处理将悬浮在污水中的大颗粒固体拦截。
初步处理完成后，本发明将初步处理后的生活污水进入膜生物反应器中进行厌氧-好氧循环处理；所述膜生物反应器中装填有含有醌基的中空纤维膜。本发明所述的膜生物反应器为厌氧-好氧一体化膜生物反应器(AOMBR)，所述AOMBR中装填有含有醌基的中空纤维膜，且AOMBR中央装有搅拌装置，用于在厌氧处理过程中进行搅拌；底部有曝气装置，用于在好氧处理过程中进行曝气以提供氧气。本发明优选通过泵实现生活污水的流通。
在本发明中，所述膜生物反应器中装填有含有醌基的中空纤维膜；所述含有醌基的中空纤维膜的运行通量优选大于等于10L/(m 2·h)，更优选为10～15L/(m 2·h)；所述含有醌基的中空纤维膜中醌基化合物的质量分 数优选大于5％，更优选为10％～15％；所述含有醌基的中空纤维膜的平均孔径优选为0.1微米。在本发明的具体实施例中，面积为1m 2的膜丝1h能够过滤至少10L废水，本发明优选根据生活污水的处理量确定中空纤维膜的总面积；本发明对含有醌基的中空纤维膜的来源没有特殊要求，直接购买使用或自行制备均可，在本发明的具体实施例中，所述含有醌基的中空纤维膜具体可以为蒽醌功能化聚偏氟乙烯膜，其制备方法按照本领域技术人员熟知的方法进行即可。本发明对所述含有醌基的中空纤维膜的装填方法没有特殊要求，使用本领域技术人员熟知的方法进行装填即可。
本发明对所述初步处理后的生活污水的在膜生物反应器中的进水速率没有特殊要求，在本发明的具体实施例中，可根据污水处理量及进水管截面积等因素确定具体的进水速率。
在本发明中，所述膜生物反应器中的污泥浓度优选为7～8g/L，更优选为7.5g/L。本发明对所述污泥的种类没有特殊要求，使用本领域技术人员熟知的污水处理用污泥即可。
在本发明中，所述初步处理后的生活污水进入膜生物反应器后先进行厌氧处理再进行好氧处理，依次循环。在本发明中，所述厌氧-好氧循环处理过程中单次厌氧处理的时间优选为50～70min，更优选为60min；所述厌氧处理的氧化还原电位优选为-50～0mV，更优选为-40～-30mV；本发明优选在搅拌条件下进行厌氧处理，所述搅拌的转速优选小于等于5转/min，更优选为3～4转/min，本发明通过搅拌使污泥悬浮在水中，与带有醌基的中空纤维膜充分接触，避免污泥沉积造成反应效率降低，本发明优选在膜生物反应器中设置水力搅拌器，为避免搅拌过程碰触到中空纤维膜，本发明优选将中空纤维膜装填在膜生物反应器的四周，将水力搅拌器设置在膜生物反应器中央。
在本发明中，所述中空纤维膜中含有醌基，醌基在微生物脱氮过程中，可以作为电子转移载体介入反硝化过程，参与并促进硝酸盐(亚硝酸盐)的还原过程，加速厌氧处理过程中反硝化过程的速率，从而达到高效脱氮的目的，本发明通过厌氧处理将生活污水中的硝态氮高效还原为氮气，同时对生活污水中的有机物进行降解，将废水中的大分子量的有机物分解成较小分子量的有机物，降低生活污水的COD值。
在本发明中，所述厌氧-好氧循环处理过程中单次好氧处理的时间优选为20～40min，更优选为30min；所述好氧处理的溶氧量优选为1～3mg/L，更优选为2mg/L。本发明优选通过曝气对好氧处理提供氧气，曝气过程可以使污水发生搅动，因而好氧处理过程无需进行搅拌，本发明优选在膜生物反应器底部设置曝气装置，本发明对所述曝气装置没有特殊要求，使用本领域技术人员熟知的曝气装置，能够为好氧处理提供氧气即可。在好氧处理过程中，生活污水中的氨态氮被氧化为硝态氮或亚硝态氮，同时将生活污水中的小分子量有机物分解为无机物，进一步降低生活污水的COD值。
在本发明中，所述初步处理后的生活污水在膜生物反应器中的水力停留时间优选为4～6h，更优选为5h；在该水力停留时间内，所述厌氧-好氧循环处理循环大于2个周期。
在本发明的具体实施例中，优选首先将初步处理后的生活污水进入膜生物反应器中进行厌氧处理，厌氧处理过程中关闭曝气装置，开启搅拌装置，厌氧处理50～70min后关闭搅拌装置，开启曝气装置，进行好氧处理20～40min，然后再进行厌氧处理，依次类推，直至初步处理后的生活污水在膜生物反应器中的水力停留时间达到4～6h后将处理后的污水排出。本发明优选在好氧处理阶段进行出水，好氧处理阶段的曝气处理可以搅动膜丝，出水时污泥不易粘附在膜丝表面，厌氧处理阶段膜丝的搅动力度不足，出水时会造成污泥粘附在膜丝表面，造成膜丝的污染，影响出水速率。
本发明的水处理过程示意图如图1所示，生活污水流经沉砂池1和格栅2进行初步处理，初步处理后的生活污水进入膜生物反应器(AOMBR)3中进行厌氧-好氧循环处理，膜生物反应器中装填含有醌基的中空纤维膜4，厌氧处理过程中开启搅拌装置5，关闭曝气装置6，好氧处理过程中关闭搅拌装置5，开启曝气装置6，处理过程中利用泵7实现污水的流通，循环处理后达标的污水通过抽吸泵引到污水处理系统排放口进行排放，本发明对膜生物反应器中污泥的处理方法没有特殊要求，使用本领域技术人员熟知的方法进行处理即可，在本发明的具体实施例中，优选定时排泥以确保水处理效果。
下面结合实施例对本发明提供的方案进行详细的描述，但不能将它们理解为对本发明保护范围的限定。
实施例1
生活污水中COD的初始含量为400mg/L，总氮初始含量为40mg/L，SS初始含量为200mg/L；
生活污水经格栅和沉沙进行初步处理；
初步处理后的生活污水进入厌氧-好氧一体化膜生物反应器(以下简称AOMBR)中进行厌氧-好氧循环处理，反应器内装填的膜丝为含有醌基的中空纤维膜；
AOMBR反应器中的污泥浓度为4g/L；AOMBR按以下参数运行：厌氧处理过程不曝气、水力搅拌60min，氧化还原电位为-50mV；然后进行好氧处理30min，好氧处理过程曝气，不搅拌，溶氧控制在3mg/L，好氧处理过程通过膜丝出水；水力停留时间HRT为5h，然后废水达标排放。
对处理后的生活污水中的COD值、总氮含量和SS含量进行检测，所得结果见表1；
表1生活污水处理前后的水质变化
Figure PCTCN2019085159-appb-000001
根据表1中的数据可以看出，未经处理的生活污水中COD、总氮和SS含量都较高，经AOMBR处理后，出水中的COD含量小于20mg/L，总氮含量小于5mg/L，其中SS完全被去除，可以看出，本发明提供的生活污水的处理方法脱氮率能够达到87.5％左右，达到了高效脱氮的目的，取得了氨氮和COD同时去除的效果。
实施例2
生活污水中COD的初始含量为320mg/L，氨氮初始含量为62mg/L，SS初始含量为85mg/L；
生活污水经格栅和沉沙进行初步处理；
初步处理后的生活污水进入厌氧-好氧一体化膜生物反应器(以下简称AOMBR)，反应器内装填的膜丝为含有醌基的中空纤维膜；
AOMBR反应器中的污泥浓度为6g/L；AOMBR按以下参数运行：厌氧处理过程不曝气、水力搅拌60min，氧化还原电位为-20mV；然后进行好氧处理30min，好氧处理过程曝气，不搅拌，溶氧控制在2.5mg/L，好氧处理过程通过膜丝出水；水力停留时间HRT为5.5h，然后废水达标排放。
对处理后的生活污水中的COD值、总氮含量和SS含量进行检测，所得结果见表2；
表2生活污水处理前后的水质变化
Figure PCTCN2019085159-appb-000002
根据表2中的数据可以看出，处理后的生活污水中的COD含量小于20mg/L，总氮含量小于5mg/L，其中SS完全被去除，可以看出，本发明提供的生活污水的处理方法脱氮率能够达到91.9％左右，达到了高效脱氮的目的，取得了氨氮和COD同时去除的效果。
以上实施例的说明只是用于帮助理解本发明的方法及其核心思想。应当指出，对于本技术领域的普通技术人员来说，在不脱离本发明原理的前提下，还可以对本发明进行若干改进和修饰，这些改进和修饰也落入本发明权利要求的保护范围内。对这些实施例的多种修改对本领域的专业技术人员来说是显而易见的，本文中所定义的一般原理可以在不脱离本发明的精神或范围的情况下在其它实施例中实现。因此，本发明将不会被限制于本文所示的这些实施例，而是要符合与本文所公开的原理和新颖特点相一致的最宽的范围。

Claims (9)

  1. 一种生活污水的处理方法，包括以下步骤：
    将生活污水依次经格栅和沉沙进行初步处理；
    初步处理后的生活污水进入膜生物反应器中进行厌氧-好氧循环处理；所述膜生物反应器中装填有含有醌基的中空纤维膜。
  2. 根据权利要求1所述的处理方法，其特征在于，所述含有醌基的中空纤维膜在膜生物反应器中的运行通量大于等于10L/(m 2·h)，膜平均孔径为0.1微米。
  3. 根据权利要求1或2所述的处理方法，其特征在于，所述含有醌基的中空纤维膜中醌基化合物的质量分数大于5％。
  4. 根据权利要求1所述的处理方法，其特征在于，所述膜生物反应器中的污泥浓度为4～6g/L。
  5. 根据权利要求1所述的处理方法，其特征在于，所述厌氧-好氧循环处理过程中单次厌氧处理的时间为50～70min。
  6. 根据权利要求5所述的处理方法，其特征在于，所述厌氧处理的氧化还原电位为-50～0mV。
  7. 根据权利要求1所述的处理方法，其特征在于，所述厌氧-好氧循环处理过程中单次好氧处理的时间为20～40min。
  8. 根据权利要求7所述的处理方法，其特征在于，所述好氧处理的溶氧量为1～3mg/L。
  9. 根据权利要求1所述的处理方法，其特征在于，所述初步处理后的废水在膜生物反应器中的水力停留时间为4～6h。
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