CN106045030B - A2/o-uasb连续流城市生活污水深度脱氮除磷的装置与方法 - Google Patents
A2/o-uasb连续流城市生活污水深度脱氮除磷的装置与方法 Download PDFInfo
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- CN106045030B CN106045030B CN201610539158.5A CN201610539158A CN106045030B CN 106045030 B CN106045030 B CN 106045030B CN 201610539158 A CN201610539158 A CN 201610539158A CN 106045030 B CN106045030 B CN 106045030B
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- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 title claims abstract description 64
- 239000010865 sewage Substances 0.000 title claims abstract description 45
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 103
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- 230000003647 oxidation Effects 0.000 claims abstract description 16
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 16
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- 239000000523 sample Substances 0.000 claims description 32
- OAICVXFJPJFONN-UHFFFAOYSA-N phosphorus Chemical compound 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[P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 26
- 229910052698 phosphorus Inorganic materials 0.000 claims description 26
- 239000011574 phosphorus Substances 0.000 claims description 26
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- 210000003128 Head Anatomy 0.000 claims description 10
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[N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 claims description 6
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- 238000000034 method Methods 0.000 abstract description 26
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 22
- 229910052799 carbon Inorganic materials 0.000 abstract description 22
- 230000001580 bacterial Effects 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract 1
- 241000894006 Bacteria Species 0.000 description 7
- 229920000903 Polyhydroxyalkanoate Polymers 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- NBIIXXVUZAFLBC-UHFFFAOYSA-K [O-]P([O-])([O-])=O Chemical compound 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[O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 239000010452 phosphate Substances 0.000 description 5
- ABLZXFCXXLZCGV-UHFFFAOYSA-N phosphorous acid Chemical compound 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OP(O)=O ABLZXFCXXLZCGV-UHFFFAOYSA-N 0.000 description 5
- 241000276438 Gadus morhua Species 0.000 description 4
- 230000001651 autotrophic Effects 0.000 description 4
- 235000019516 cod Nutrition 0.000 description 4
- 241000565118 Cordylophora caspia Species 0.000 description 3
- 206010061529 Polyp Diseases 0.000 description 3
- FGIUAXJPYTZDNR-UHFFFAOYSA-N Potassium nitrate Chemical compound 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[K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 3
- -1 nitrogen phosphorus Chemical compound 0.000 description 3
- 241001453382 Nitrosomonadales Species 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
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- NHNBFGGVMKEFGY-UHFFFAOYSA-N nitrate Chemical compound 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[O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 206010002660 Anoxia Diseases 0.000 description 1
- 241000976983 Anoxia Species 0.000 description 1
- 241000108664 Nitrobacteria Species 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000001419 dependent Effects 0.000 description 1
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- 239000003344 environmental pollutant Substances 0.000 description 1
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Classifications
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/28—Anaerobic digestion processes
- C02F3/2846—Anaerobic digestion processes using upflow anaerobic sludge blanket [UASB] reactors
-
- 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
Abstract
A2/O‑UASB连续流城市生活污水深度脱氮除磷的装置与方法,属于污水生物处理领域。城市生活污水从进水箱泵入A2/O反应器的厌氧区,同时进入的还有二沉池回流的污泥。厌氧区的混合液进入缺氧区,同时将富含NO3 ‑‑N的UASB一体化厌氧氨氧化反应器的出水泵入A2/O反应器的缺氧区。A2/O好氧区的混合液进入二沉池,然后流入中间水箱,泵入一体化厌氧氨氧化UASB反应器中,其出水的一部分回流至连续流A2/O反应器中另一部分作为最终出水排出系统。本发明降低反硝化时碳源的消耗量,降低曝气量节省了能耗,同时解决了传统脱氮除磷工艺中除磷菌与脱氮菌在有机碳源、溶解氧等的竞争以及脱氮与除磷在污泥龄方面的矛盾问题。
Description
技术领域
本发明涉及的A2/O-UASB连续流城市生活污水深度脱氮除磷的装置与方法,属于污水生物处理技术领域,是一种强化低C/N的城市生活污水自养脱氮除磷的试验装置和方法。
背景技术
近年来,水体富营养化越来越严重,而氮和磷元素的过量排放是导致水体富营养化的重要因素,控制水体富营养化最主要的途径就是对水体进行深度的脱氮除磷。污水中的碳源是影响废水处理效果的重要因素,而我国目前城市生活污水最明显的特征就是 C/N(污水中碳元素与氮元素的质量浓度的比值)较低。为解决传统的生物脱氮除磷工艺在处理低C/N的城市生活污水时,无外加碳源的情况下无法进行深度脱氮除磷以及脱氮与除磷在污泥龄存在矛盾等问题,研究者们逐步开发了短程硝化反硝化、一体化厌氧氨氧化以及反硝化除磷等工艺。
一体化厌氧氨氧化工艺将短程硝化技术和厌氧氨氧化技术结合在一起,实现了污水的高效脱氮,且不需有机碳源。不仅能节省有机碳源,同时还能节省曝气量。然而一体化厌氧氨氧化工艺的出水带有大量的NO3 --N,不仅提高了出水总氮的含量,同时造成了NO3 --N资源的浪费。反硝化除磷工艺是目前污水生物脱氮除磷领域的最新理论和技术,反硝化聚磷菌利用体内的内碳源PHA作为电子受体,以“一碳两用”的方式同时实现污水反硝化脱氮和吸磷作用。反硝化除磷工艺的提出突破了传统生物脱氮除磷的理论,很好地解决传统工艺中存在的由碳源不足引起的脱氮菌和除磷菌对碳源的问题。在 A2/O工艺中实现反硝化除磷具有构造简单、设计运行经验成熟和控制复杂性小等一系列优点,并且A2/O工艺是目前国内外城镇污水厂的主体工艺。然而A2/O工艺为单污泥系统,无法解决脱氮菌与除磷菌在污泥龄上的矛盾问题。
A2/O-UASB连续流城市生活污水深度脱氮除磷工艺将反硝化除磷工艺与一体化厌氧氨氧化有机结合在一起,实现了污水脱氮和除磷的分离,有效的解决了脱氮菌与除磷菌在长短污泥龄的上的矛盾,同时反硝化除磷菌可以利用原水中的碳源进行反硝化除磷,不仅可以节省外碳源的投加,而且可以防止有机碳源对厌氧氨氧化的影响。厌氧氨氧化菌为自养菌,可以进一步节省在脱氮过程中有机碳源的需求量,同时一体化厌氧氨氧化所需的溶解氧较低,可以节省曝气量。而一体化厌氧氨氧化的出水中携带的NO3 --N 回流到A2/O反应器的缺氧区中可以作为反硝化除磷的电子供体进一步去除,降低了系统出水的总氮的含量,从而实现了城市生活污水的深度脱氮除磷。
发明内容
为解决低碳氮比城市生活污水在脱氮除磷过程中碳源不足以及脱氮菌和除磷菌在污泥龄上存在矛盾的问题,本发明提供了一种A2/O-UASB连续流城市生活污水深度脱氮除磷的装置与方法,是一种新型的结合了反硝化除磷技术和短程硝化厌氧氨氧化一体化技术的深度脱氮除磷技术。该工艺为双污泥系统,将生物脱氮和除磷分为两个污泥系统进行,可以有效的解决脱氮菌和除磷菌在长短污泥龄上的矛盾。A2/O连续流反应器负责除磷,反硝化除磷菌在厌氧环境先利用原水中的有机碳源进行释磷同时合成PHA 贮存在细胞体内,而后在缺氧区内反硝化聚磷菌利用体内贮存的PHA以及回流的厌氧氨氧化自养脱氮出水中的NO3 --N进行反硝化吸磷,为保证除磷效果,在A2/O连续流反应器的最后两格进行曝气,同时可以防止活性污泥在长期的厌缺氧条件下而发黑变臭。一体化厌氧氨氧化UASB反应器则负责脱氮,富含NH4 +-N的A2/O连续流反应器出水进入UASB反应器中,在微氧曝气的条件下通过短程硝化厌氧氨氧化反应进行自养脱氮,从而实现污水中氮磷的深度去除。
本发明的A2/O-UASB连续流城市生活污水深度脱氮除磷的装置,其特征在于:包括顺序连接的城市污水原水箱(1)、A2/O反应器厌氧区(4)、缺氧区(5)、好氧区(6)、二沉池(7)、中间水箱(19)、一体化厌氧氨氧化UASB反应器(22)、出水水箱(26)。 A2/O连续流反应器内分别设有第一进水管(2)、进水泵(3)、搅拌器(8)、第一空气压缩机(12)、转子流量计(13)、粘土曝气头(14)、第一DO探头(16)、第一pH探头(17)、第一WTW溶氧仪(15)、第一排泥管(9)、污泥回流管(10)以及污泥回流泵(11)。一体化厌氧氨氧化UASB反应器(22)主要设有第二进水管(20)、第二进水泵(21)、三相分离器(23)、取样口(24)、第二出水管(25)、第二排泥管(33)、加热带(34)、第二DO探头(37)、第二pH探头(36)、第二WTW溶氧仪(35)第二空气压缩机(30)、第二转子流量计(32)、第二粘土曝气盘(31)。
A2/O-UASB连续流城市生活污水深度脱氮除磷的装置,其特征在于:城市生活污水原水箱(1)通过进水管(2)和第一进水泵(3)与A2/O反应器的厌氧区(4)相连, A2/O反应器的厌氧区以及缺氧区内都设有搅拌器(8),第一空气压缩机(12)经第一转子流量计(13)以及砂土曝气头(14)为A2/O反应器的好氧区(6)提供曝气;好氧区(6)内设有第一DO探头(16)以及第一pH探头(17),DO探头与pH探头分别与第一WTW溶氧仪(15)相连;中间水箱(19)与A2/O反应器的二沉池相连,同时通过第二进水管(20)和第二进水泵(21)与一体化厌氧氨氧化UASB反应器相连;第二空气压缩机(30)经第二转子流量计(32)以及砂土曝气盘(31)为UASB反应器(22)提供曝气;UASB反应器(22)内设有第二DO探头(37)以及第二pH探头 (36),DO探头与pH探头分别与第二WTW溶氧仪(35)相连。出水水箱(26)通过硝化液回流管(28)以及硝化液回流泵(29)与A2/O反应器的缺氧区(5)相连。
本发明提供的A2/O-UASB连续流城市生活污水深度脱氮除磷的方法,其特征在于:包括以下两个阶段的内容:
阶段一:系统的启动。在A2/O反应器中接种反硝化除磷污泥,使A2/O反应器内的污泥浓度达到3000~3500mg/L;在一体化厌氧氨氧化反应器中按2:1的比例同时接种短程硝化絮体污泥和厌氧氨氧化颗粒污泥(其污泥浓度分别为3000~3500mg/L、 3000~4000mg/L)。使UASB反应器中的污泥浓度达到3000~4000mg/L。在此阶段,A2/O 反应器开启四格曝气,生活污水首先进入A2/O反应器进行有机物的降解、厌氧吸磷和好氧吸磷,其去除有机物和磷并富含氨氮的出水作为一体化厌氧氨氧化UASB反应器的进水,进行短程硝化和厌氧氨氧化,将氨氮转化为氮气从废水中排出。当A2/O反应器的磷去除率达到95%以上,UASB反应器的总氮去除率达到85%以上,即认为 A2/O-UASB连续流城市生活污水深度脱氮除磷系统启动成功。
阶段二:系统的稳定运行。待系统启动成功后,将A2/O反应器好氧区的前两格改为缺氧区,同时将部分一体化厌氧氨氧化UASB反应器的出水回流至A2/O反应器的缺氧区,为反硝化除磷提供电子受体。系统的运行包括以下几个步骤:
1)第一进水泵(3)经第一进水管(2)将原水箱(1)中的城市生活污水泵入A2/O 反应器的厌氧区(4),同时污泥回流泵(11)将二沉池中的污泥回流至厌氧区,与厌氧区的污泥混合后,聚磷菌吸收原水中约85~88%的有机物,并以PHAs的形式贮存于其生物体内,同时释放出体内的磷酸盐。
2)厌氧区的混合液进入A2/O反应器的缺氧区(5),同时回流泵(29)将富含NO3 --N的一体化厌氧氨氧化UASB反应器的出水泵入至A2/O反应器的缺氧区。反硝化聚磷菌以回流的硝态氮作为电子受体,以厌氧区贮存的PHA为电子供体,进行缺氧反硝化吸磷反应。
3)缺氧区的混合液随后进入A2/O反应器的好氧区(6),第一空气压缩机(12)为好氧区提供曝气。通过转子流量计调节空气流量控制好氧区的DO浓度为1.0~1.5mg/L。
4)来自A2/O反应器的混合液进入二沉池(7),实现混合液的泥水分离,混合液从二沉池流入到中间水箱(19)富含氨氮的上清液经第二进水泵(21)由中间水箱泵入至 UASB反应器(22)中。二沉池(7)泥斗中的污泥重新回流到A2/O反应器的厌氧区,同时每天从第一排泥口(9)进行排泥,使A2/O反应器的SRT为10~15d,反应器中的污泥浓度维持在3000~4000mg/L;
5)启动第二进水泵(21)将二沉池(7)分离的上清液从中间水箱(19)泵入一体化厌氧氨氧化UASB反应器(22)中,开启第二空气压缩机(30),通过第二转子流量计(32)调节空气流量,控制一体化厌氧氨氧化UASB反应器(22)内的DO浓度为 0.3~0.8mg/L。
6)一体化厌氧氨氧化UASB反应器的出水排入出水水箱(26),启动硝化液回流泵(29)将出水水箱的硝化液回流至A2/O反应器的缺氧区,为反硝化除磷提供电子受体。最终出水经排水管(27)从出水水箱(26)排出系统。
本发明提供的A2/O-UASB连续流城市生活污水深度脱氮除磷的装置与方法,与传统的生物脱氮除磷工艺相比具有以下优点:
1)传统的生物脱氮除磷工艺将脱氮和除磷置于同一个系统中,这样不可避免的存在污泥龄的矛盾问题,而该工艺将脱氮和除磷置于两个系统中进行,可以有效的解决脱氮和除磷对污泥龄要求不同的矛盾。
2)传统的生物脱氮除磷工艺在处理低碳氮比的城市生活污水时想要达到污水的深度脱氮除磷则必须外加碳源,而该工艺利用自养的厌氧氨氧化菌进行脱氮以及利用原水中的碳源进行除磷,从而节省了外碳源的投加,降低了工艺的运行成本。
3)由于硝化细菌的世代时间较长,传统的生物脱氮除磷工艺的好氧段较长,不仅耗氧量较大,而且产泥量大。该工艺将脱氮作用放在一体化厌氧氨氧化UASB反应器中进行,可以缩短A2/O反应器的好氧段,而且一体化厌氧氨氧化只需微氧曝气,因此可以减少曝气量。A2/O反应器短暂的好氧段主要的目的在于对缺氧段剩余的磷进一步去除,同时防止活性污泥由于长期的厌缺氧环境导致发黑变臭,而不是用于硝化作用。
4)由于A2/O反应器不进行硝化作用,所以A2/O反应器的出水中只含有很少量的亚硝酸盐和硝酸盐,二沉池中不易发生因反硝化而导致的污泥上浮,回流污泥回流到厌氧段后,没有氧的释放过程,从而更容易形成厌氧条件,提高聚磷菌在厌氧段的释磷效率。
附图说明
图1是A2/O-UASB连续流城市生活污水深度脱氮除磷的装置与方法的示意图。
图1中:1-进水水箱,2-第一进水管,3-第一进水泵,4-厌氧区,5-缺氧区,6-好氧区,7-二沉池,8-搅拌器,9-第一排泥管,10-污泥回流管,11-污泥回流泵,12-第一空气压缩机,13-第一转子流量计,14第一曝气头,15-第一WTW溶氧仪,16-第一DO 探头,17-第一pH探头,18-A2/O出水管,19-中间水箱,20-第二进水管,21-第二进水泵,22-UASB反应器,23-三相分离器,24-取样口,25-UASB出水管,26-出水水箱, 27-最终出水管,28-硝化液回流管,29-硝化液回流泵,30-第二空气压缩机,31-第二曝气盘,32-第二转子流量计,33-第二排泥管,34-加热带,35-第二WTW溶氧仪,36-第二pH探头,37-第二DO探头。
具体实施方式
下面结合附图和实施案例对本发明做进一步说明。
本发明中的A2/O-UASB连续流城市生活污水深度脱氮除磷系统如图1所示。装置主要包括:顺序连接的城市污水原水箱(1)、A2/O反应器厌氧区(4)、缺氧区(5)、好氧区(6)、二沉池(7)、中间水箱(19)、一体化厌氧氨氧化UASB反应器(22)、出水水箱(26)、。A2/O连续流反应器内分别设有第一进水管(2)、进水泵(3)、搅拌器(8)、第一空气压缩机(12)、转子流量计(13)、粘土曝气头(14)、第一 DO探头(16)、第一pH探头(17)、第一WTW溶氧仪(15)、第一排泥管(9)、污泥回流管(10)以及污泥回流泵(11)。一体化厌氧氨氧化UASB反应器(22)主要设有第二进水管(20)、第二进水泵(21)、三相分离器(23)、取样口(24)、第二出水管(25)、第二排泥管(33)、加热带(34)、第二DO探头(37)、第二pH 探头(36)、第二WTW溶氧仪(35)第二空气压缩机(30)、第二转子流量计(32)、第二粘土曝气盘(31)。
A2/O-UASB连续流城市生活污水深度脱氮除磷的装置与方法的具体操作运行步骤和工艺参数如下:
阶段一:系统的启动。在A2/O反应器中接种反硝化除磷污泥,使A2/O反应器内的污泥浓度达到3000~3500mg/L;在一体化厌氧氨氧化反应器中按2:1的比例同时接种短程硝化絮体污泥和厌氧氨氧化颗粒污泥(其污泥浓度分别为3000~3500mg/L、 3000~4000mg/L)。使UASB反应器中的污泥浓度达到4000~4500mg/L。在此阶段,A2/O 反应器开启四格曝气,生活污水首先进入A2/O反应器进行有机物的降解、厌氧吸磷和好氧吸磷,其去除有机物和磷并富含氨氮的出水作为一体化厌氧氨氧化UASB反应器的进水,进行短程硝化和厌氧氨氧化,将氨氮转化为氮气从废水中排出。当A2/O反应器的磷去除率达到95%以上,UASB反应器的总氮去除率达到85%以上,即认为 A2/O-UASB连续流城市生活污水深度脱氮除磷系统启动成功。
阶段二:系统的稳定运行。待系统启动成功后,将A2/O反应器好氧区的前两格改为缺氧区,同时将部分一体化厌氧氨氧化UASB反应器的出水回流至A2/O反应器的缺氧区,为反硝化除磷提供电子受体。系统的运行包括以下几个步骤:
1)第一进水泵(3)经第一进水管(2)将原水箱(1)中的城市生活污水泵入A2/O 反应器的厌氧区(4),同时污泥回流泵(11)将二沉池中的污泥回流至厌氧区,与厌氧区的污泥混合后,聚磷菌吸收原水中约85~88%的有机物,并以PHAs的形式贮存于其生物体内,同时释放出体内的磷酸盐。
2)厌氧区的混合液进入A2/O反应器的缺氧区(5),同时回流泵(29)将富含NO3 --N的一体化厌氧氨氧化UASB反应器的出水泵入至A2/O反应器的缺氧区。反硝化聚磷菌以回流的硝态氮作为电子受体,以厌氧区贮存的PHA为电子供体,进行缺氧反硝化吸磷反应。
3)缺氧区的混合液随后进入A2/O反应器的好氧区(6),第一空气压缩机(12)为好氧区提供曝气。通过转子流量计调节空气流量控制好氧区的DO浓度为1.0~1.5mg/L。
4)来自A2/O反应器的混合液进入二沉池(7),实现混合液的泥水分离,混合液从二沉池流入到中间水箱(19)富含氨氮的上清液经第二进水泵(21)由中间水箱泵入至 UASB反应器(22)中。二沉池(7)泥斗中的污泥重新回流到A2/O反应器的厌氧区,同时每天从第一排泥口(9)进行排泥,使A2/O反应器的SRT为10~15d,反应器中的污泥浓度维持在3000~4000mg/L;
5)启动第二进水泵(21)将二沉池(7)分离的上清液从中间水箱(19)泵入一体化厌氧氨氧化UASB反应器(22)中,开启第二空气压缩机(30),通过第二转子流量计(32)调节空气流量,控制一体化厌氧氨氧化UASB反应器(22)内的DO浓度为 0.3~0.8mg/L。
6)一体化厌氧氨氧化UASB反应器的出水排入出水水箱(26),启动硝化液回流泵(29)将出水水箱的硝化液回流至A2/O反应器的缺氧区,为反硝化除磷提供电子受体。最终出水经排水管(27)从出水水箱(26)排出系统。
试验期间以北京某高校家属区实际生活污水为处理对象。A2/O反应器由8个格室构成,总有效体积为24.8L,第一格式为厌氧区,随后的5个是缺氧区,剩余两个为好氧区,即厌氧区、缺氧区和好氧区的容积比是1∶5∶2。A2/O反应器的进水流量为3.1L/h,即HRT为8h,SRT控制在15d,硝化液回流比为300%,污泥回流比为100%。UASB 反应器的容积为6L,污泥浓度维持在4000~4500mg/L。试验期间的平均进出水水质如表1所示:
表1试验期间的平均进出水水质
污染物 | COD | NH<sub>4</sub><sup>+</sup>-N | TN | TP |
进水水质(mg/L) | 285.9 | 62.7 | 71.5 | 6.31 |
出水水质(mg/L) | 41.24 | 0.58 | 9.32 | 0.21 |
去除率(%) | 85.6 | 99.1 | 87 | 96.6 |
由表1可知,最终出水的COD小于50mg/L,NH4 +-N小于1mg/L,TN小于10mg/L,总磷小于0.5mg/L,COD、NH4 +-N、TN、TP的平均去除率分别达到85.6%、99.1%、 87%、96.6%,稳定运行后,出水COD、NH4 +-N、TN、TP浓度均稳定达到国家一级A 标准。
Claims (2)
1.A2/O-UASB连续流城市生活污水深度脱氮除磷的装置,其特征在于:包括顺序连接的城市污水原水箱(1)、A2/O反应器厌氧区(4)、缺氧区(5)、好氧区(6)、二沉池(7)、中间水箱(19)、一体化厌氧氨氧化UASB反应器(22)、出水水箱(26);A2/O连续流反应器内分别设有第一进水管(2)、进水泵(3)、搅拌器(8)、第一空气压缩机(12)、转子流量计(13)、粘土曝气头(14)、第一DO探头(16)、第一pH探头(17)、第一WTW溶氧仪(15)、第一排泥管(9)、污泥回流管(10)以及污泥回流泵(11);一体化厌氧氨氧化UASB反应器(22)主要设有第二进水管(20)、第二进水泵(21)、三相分离器(23)、取样口(24)、第二出水管(25)、第二排泥管(33)、加热带(34)、第二DO探头(37)、第二pH探头(36)、第二WTW溶氧仪(35)第二空气压缩机(30)、第二转子流量计(32)、第二粘土曝气盘(31);城市生活污水原水箱(1)通过进水管(2)和第一进水泵(3)与A2/O反应器的厌氧区(4)相连,A2/O反应器的厌氧区以及缺氧区内都设有搅拌器(8),第一空气压缩机(12)经第一转子流量计(13)以及砂土曝气头(14)为A2/O反应器的好氧区(6)提供曝气;好氧区(6)内设有第一DO探头(16)以及第一pH探头(17),DO探头与pH探头分别与第一WTW溶氧仪(15)相连;中间水箱(19)与A2/O反应器的二沉池相连,同时通过第二进水管(20)和第二进水泵(21)与一体化厌氧氨氧化UASB反应器相连;第二空气压缩机(30)经第二转子流量计(32)以及砂土曝气盘(31)为UASB反应器(22)提供曝气;UASB反应器(22)内设有第二DO探头(37)以及第二pH探头(36),DO探头与pH探头分别与第二WTW溶氧仪(35)相连;出水水箱(26)通过硝化液回流管(28)以及硝化液回流泵(29)与A2/O反应器的缺氧区(5)相连。
2.应用如权利要求1所述装置的方法,其特征在于,包括以下两个阶段:
阶段一:系统的启动;在A2/O反应器中接种反硝化除磷污泥,使A2/O反应器内的污泥浓度达到3000~3500mg/L;在一体化厌氧氨氧化反应器中按体积比为2:1的比例同时接种短程硝化絮体污泥和厌氧氨氧化颗粒污泥,短程硝化絮体污泥和厌氧氨氧化颗粒污泥浓度分别为3000~3500mg/L、3000~4000mg/L;使UASB反应器中的污泥浓度达到3000~4000mg/L;在此阶段,A2/O反应器开启四格曝气,生活污水首先进入A2/O反应器进行有机物的降解、厌氧吸磷和好氧吸磷,其去除有机物和磷并富含氨氮的出水作为一体化厌氧氨氧化UASB反应器的进水,进行短程硝化和厌氧氨氧化,将氨氮转化为氮气从废水中排出;当A2/O反应器的磷去除率达到95%以上,UASB反应器的总氮去除率达到85%以上,即认为A2/O-UASB连续流城市生活污水深度脱氮除磷系统启动成功;
阶段二:系统的稳定运行;待系统启动成功后,将A2/O反应器好氧区的前两格改为缺氧区,同时将部分一体化厌氧氨氧化UASB反应器的出水回流至A2/O反应器的缺氧区,为反硝化除磷提供电子受体;系统的运行包括以下几个步骤:
1)第一进水泵(3)经第一进水管(2)将原水箱(1)中的城市生活污水泵入A2/O反应器的厌氧区(4),同时污泥回流泵(11)将二沉池中的污泥回流至厌氧区;
2)厌氧区的混合液进入A2/O反应器的缺氧区(5),同时回流泵(29)将富含NO3 --N的一体化厌氧氨氧化UASB反应器的出水泵入至A2/O反应器的缺氧区;
3)缺氧区的混合液随后进入A2/O反应器的好氧区(6),第一空气压缩机(12)为好氧区提供曝气;通过转子流量计调节空气流量控制好氧区的DO浓度为1.0~1.5mg/L;
4)来自A2/O反应器的混合液进入二沉池(7),实现混合液的泥水分离,混合液从二沉池流入到中间水箱(19)富含氨氮的上清液经第二进水泵(21)由中间水箱泵入至UASB反应器(22)中;二沉池(7)泥斗中的污泥重新回流到A2/O反应器的厌氧区,同时每天从第一排泥口(9)进行排泥,使A2/O反应器的SRT为10~15d,反应器中的污泥浓度维持在3000~4000mg/L;
5)启动第二进水泵(21)将二沉池(7)分离的上清液从中间水箱(19)泵入一体化厌氧氨氧化UASB反应器(22)中,开启第二空气压缩机(30),通过第二转子流量计(32)调节空气流量控制一体化厌氧氨氧化UASB反应器(22)内的DO浓度为0.3~0.8mg/L;
6)一体化厌氧氨氧化UASB反应器的出水排入出水水箱(26),启动硝化液回流泵(29)将出水水箱的硝化液回流至A2/O反应器的缺氧区,为反硝化除磷提供电子受体;最终出水经排水管(27)从出水水箱(26)排出系统。
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