CN100569669C - 厌氧-缺氧氧化沟工艺反硝化除磷装置及其方法 - Google Patents
厌氧-缺氧氧化沟工艺反硝化除磷装置及其方法 Download PDFInfo
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- CN100569669C CN100569669C CNB2007103039395A CN200710303939A CN100569669C CN 100569669 C CN100569669 C CN 100569669C CN B2007103039395 A CNB2007103039395 A CN B2007103039395A CN 200710303939 A CN200710303939 A CN 200710303939A CN 100569669 C CN100569669 C CN 100569669C
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- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 73
- 230000003647 oxidation Effects 0.000 title claims abstract description 71
- 238000000034 method Methods 0.000 title claims abstract description 33
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- 239000010802 sludge Substances 0.000 claims abstract description 47
- 241000894006 Bacteria Species 0.000 claims abstract description 45
- OAICVXFJPJFONN-UHFFFAOYSA-N phosphorus Chemical compound 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[P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 25
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 25
- 239000011574 phosphorus Substances 0.000 claims abstract description 25
- 241000565118 Cordylophora caspia Species 0.000 claims abstract description 19
- 206010061529 Polyp Diseases 0.000 claims abstract description 19
- 239000010865 sewage Substances 0.000 claims abstract description 16
- 238000005273 aeration Methods 0.000 claims description 44
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 28
- 229910052799 carbon Inorganic materials 0.000 claims description 25
- 238000007599 discharging Methods 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 230000000102 heterotrophic Effects 0.000 claims description 11
- 230000035683 MEAN RESIDENCE TIME Effects 0.000 claims description 9
- 238000006396 nitration reaction Methods 0.000 claims description 8
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OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- ABLZXFCXXLZCGV-UHFFFAOYSA-N phosphorous acid Chemical compound 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Abstract
厌氧-缺氧氧化沟工艺反硝化除磷装置及其方法属于污水处理技术领域。针对目前氧化沟工艺生物除磷效果较差的问题，将传统氧化沟进行改良，增强其除磷能力。在传统氧化沟处理装置的基础上，增设厌氧池和缺氧池A和缺氧池B，开发了具有反硝化除磷能力的新型氧化沟工艺。充分利用聚磷菌、反硝化菌和反硝化除磷菌的特点和它们之间的差异，使3种类型的微生物在一个系统中的三个选择器中占据不同的生态位，从而实现各自的功能。本发明通过合理分配回流污泥和进水，减缓了聚磷菌和反硝化菌之间的矛盾，使反硝化除磷菌在竞争中优势增强，达到高效脱氮除磷效果。本发明具有除磷效率高、运行相对稳定、不易发生污泥膨胀等优点。
Description
厌氧-缺氧氧化沟工艺反硝化除磷装置及其方法
技术领域
本发明一种厌氧-缺氧氧化沟工艺反硝化除磷装置及其方法，涉及的是生 活污水生物脱氮除磷的技术领域。 背景技术 氧化沟技术
氧化沟（oxidation ditch)又名连续循环曝气池（Continuous loop reactor)， 是活性污泥法的一种变形。氧化沟最初应用于荷兰，目前已成为一种重要污 水处理技术。近年来，采用氧化沟处理厂的速度有了'惊人的进展。目前在我 国氧化沟工艺的污水处理厂数量的增长更加迅速。氧化沟工艺运行稳定、操 作维护方便，出水水质优良。近年来改进的氧化沟工艺具有较好的脱氮除磷 能力使该工艺成为国内外最实用的工艺之一。氧化沟工艺为目前国内外新建 污水处理厂的首选工艺。
氧化沟具有特殊的水力学流态，既有完全混合式反应器的特点，又有推 流式反应器的特点，沟内存在宏观的溶解氧浓度梯度，另外在活性污泥絮体 中还存在微观的溶解氧梯度。氧化沟断面为矩形或梯形，平面形状多为椭圆 形。目前沟内水深一般为3〜5m,为防止活性污泥在沟中沉淀，氧化沟中平 均水流速度大于0.3m/s。氧化沟曝气混合设备有表面曝气机、曝气转刷或转 盘、射流曝气器、导管式曝气器和提升管式曝气机等，近年来配合使用的还 有水下推动器。
氧化沟工艺通常首先考虑生物脱氮，因此该工艺以高效的生物脱氮著 称，关于氧化沟工艺的生物除磷研究较少。因为氧化沟工艺水力停留时间较 长，污泥龄也较长，普遍认为这两方面限制氧化沟工艺的生物除磷能力。为 了提高氧化沟工艺的生物除磷能力，在传统的氧化沟工艺前端增设厌氧池和 缺氧池，将氧化沟工艺改进为A2/0氧化沟工艺。 生物除磷技术
生物除磷（EBPR)为一种经济和可持续性除磷方法，因为避免了投加化 学药剂而产生大量难以处理的化学污泥而成为近年来研究的热点。EBPR主要 通过聚磷菌(PAOs)在厌氧和好氧交替运行的环境中运行，PAOs在厌氧状态下吸收有机碳源，主要是挥发性有机酸(VFA)，来合成聚(3-羟基垸酸(PHA)并 将其储存于体内，消耗的能量主要来自于分解体内的聚il酸盐，同时将正磷 酸盐释放出微生物体外。在随后的好氧阶段，PAOs利用储蓄的PHA作为碳 源和能源生长繁殖，吸收水中的正磷酸盐，以聚磷酸盐的形式存储恢复体内 的聚磷酸盐水平。生物除磷就是将好氧阶段的富含磷的污泥作为剩余污泥排 出，达到生物除磷的目的。 反硝化除磷技术
在缺氧状态下也能进行磷的吸收。近年来，研究显示一些被称做反硝化 聚磷菌(DPAOs)的微生物能够以N(V或N02l乍为最终电子受体氧化体内的 PHA，提供吸收磷的能量。禾(J用N03'和N(V作为电子受体进行吸收磷反应被 称作反硝化除磷（DPR) 。 PHA在作为反硝化的碳源中起了重要的角色，反 硝化除磷使系统对碳源的需求量降低。
反硝化除磷因为PAO利用内碳源进行反硝化反应从而具有如下两个优 点：①节省碳源，因为反硝化过程通常需要原水中易降解碳源，反硝化除磷 过程使碳源在PAO释磷过程利用之后还能够应用于作为反硝化的碳源，碳源 使用了两次，提髙了碳源的利用效率。②PAO体内的碳源在反硝化过程被N03' 氧化，相当于降低了好氧过程的需氧量，从而具有节能的优点。
发明内容
本发明的目的是提供一种厌氧-缺氧氧化沟工艺反硝化除磷装置和方法， 以解决氧化沟工艺在进水碳氮比较低时生物脱氮和除磷效率较低的问题，从 而促进生物脱氮除磷的稳定性和高效率。
本发明提供的一种厌氧-缺氧氧化沟工艺反硝化除磷装置，包括水箱1、 包括曝气池8的氧化沟主体，和二沉池16 ，其特征在于，在所述的氧化沟主 体前端增设三个选择器：厌氧池4、缺氧池A5和缺氧池B6。
应用所述厌氧-缺氧氧化沟工艺反硝化除磷装置的方法，其特征在于，包 括以下步骤：
1)将含有聚磷菌、反硝化菌和硝化菌的活性污泥添加到氧化沟主体和二 沉池16内，将生活污水投加入水箱i中，启动进水泵A2和进水泵B3，同时 开启回流污泥泵Ai8和回流污泥泵B19，通过连续处理生活污水使活性污泥在氧化沟系统中经过1〜2个月的驯化和培养；使氧化沟内的活性污泥浓度维
持在3000mg/L〜4500mg/L;
2) 70%〜80%的原污水和25%~50%的回流污泥在厌氧池4中经搅拌器7 混合，回流污泥中的少量N(V决速被异养菌反硝化去除，随后聚磷菌吸收挥 发性有机酸，并进行磷的释放；在厌氧池4平均停留时间为40〜60分钟；
3) 上述厌氧池4中排出的泥水进入缺氧池A5后，和污泥回流泵B19泵 入的50°/。~75%回流污泥混合，释磷后的聚磷菌部分具有反硝化除磷功能，称 为反硝化聚磷菌，该类微生物在缺氧池A5中利用回流污泥中带入的N(V作 为电子受体进行反硝化吸收磷；在缺氧池A5中平均停留时间为60〜80分钟；
4) 上述缺氧池A5中排出的泥水进入缺氧池B6后，和进水泵3泵入的 20%〜30%原水混合，异养菌利用原水中的易降解碳源将缺氧池A5中未反应 的N(V还原为N2;在缺氧池B6中平均停留时间为20〜40分钟；
5) 上述缺氧池B6排出的泥水进入氧化沟曝气池8中后，鼓风机12对进 水进行鼓风曝气，曝气系统由鼓风机12、转子流量计13空气管14和曝气头 15组成，曝气量的大小根据运行状态进出水情况运用转子流量计13进行调整， 控制出水NH/在1〜4mg/L，若出水NH4+超出该范围，就要对曝气量进行调整， 出水NH4、4mg/L时，增大曝气量，出水NH4、lmg/L时，减小曝气量；处理 水在氧化沟曝气池8中平均水力停留时间14-20小时后经溢流堰9自流进入二 沉池16中，在氧化沟出水处设置DO仪lO和pH计ll,根据DO仪的在线示 数控制溶解氧在1.0〜2.0mg/L， pH通常在7.0〜8.0之间；
在氧化沟曝气池8中进行以下四种反应：异氧菌利用有机物进行的碳氧 化反应、硝化菌硝化反应、聚磷菌包括反硝化聚磷菌的吸收磷反应；
6) 从氧化沟曝气池8中溢流出的处理水进入二沉池16进行泥水分离， 上清液溢流经出水管17排出系统，回流污泥分别经回流污泥泵A18和回流污 泥泵B19分别回流至厌氧池4和缺氧池A5;
7) 剩余污泥通过剩余污泥泵20排出系统，通过排出剩余污泥来控制污 泥龄，污泥龄控制在10~15d。
发明的有益效果本发明涉及的厌氧-缺氧-氧化沟反硝化除磷工艺与传统的氧化沟工艺相 比具有如下优点：
1、 在生物脱氮基础上实现了稳定的生物除磷，TP的去除率能够达到80% 以上；
2、 将原水和回流污泥根据生物脱氮和生物除磷的原理进行优化分配，使 大部分原水中的碳源优先满足生物除磷的需求，使聚磷菌充分释放磷，然后 利用聚磷菌的内碳源进行反硝化，达到一碳两用的效果，缓和了生物脱氮和 生物除磷对碳源竞争的矛盾。同时反硝化除磷过程还节省了随后在氧化沟曝 气池中的曝气能耗；
3、 缺氧池6中的迸水作用为：避免进水中碳源过量，使厌氧池过量的碳 源进入缺氧池5中，发生传统的反硝化反应从而影响反硝化吸磷；为缺氧池6 中进行的反硝化提供碳源；
4、 缺氧池A5和缺氧池B6中进行的反硝化反应回收了碱度，提升了pH 值，避免了由于碱度不足影响曝气池中进行的硝化反应；
5、 前置厌氧池4、缺氧池A5和缺氧池B6起了生物选择器的功能，抑制 了丝状菌的生长，从而在一定程度上降低了发生丝状菌污泥膨胀的概率。
附图说明
图1厌氧-缺氧氧化沟工艺反硝化除磷装置示意图
其中1一水箱、2—进水泵A， 3—进水泵B、 4一厌氧池、5—缺氧池A, 6—缺氧池B、 7—搅拌器、8—曝气池、9一溢流堰、10—DO仪、11—pH计、 12—鼓风机、13—转子流量计、14一空气管、15—曝气头、16~二沉池、17— 出水管、18—回流污泥泵A， 19一回流污泥泵B， 20—剩余污泥泵。
具体实施方式
下面结合附图及实施例对本发明进行详细说明： 具体实施例一
接种污泥来自北京市酒仙桥污水处理厂的回流污泥，试验用水取自北京
市酒仙桥污水处理厂曝气沉砂池。试验阶段主要水质指标为：COD为
232〜621mg/L，NH/为42.1〜64.5mg/L,P043陽为5.2~9.1mg/L，TP为5.9~9.7mg/L, TN为56.4~73.5mg/LpH为7.2-7.8。试验中所采用的分析方法均按照国家环境 保护局发布的标准方法.试验步骤为将接种污泥添加到曝气池8内，将生活污水投加入水箱l中, 启动进水泵A2和进水泵B3， 70〜80%的原污水和25~50%的回流污泥在厌氧 池4中经搅拌器7混合，回流污泥中的少量N(V快速被异养菌反硝化去除， 聚磷菌吸收挥发性有机酸，并进行磷的释放。在厌氧池4平均停留时间为40〜 60分钟。厌氧池4中排出的泥水进入缺氧池A5后，和污泥回流泵B19泵入 的50〜75%回流污泥混合，释磷后的聚磷菌部分具有反硝化除磷功能，称为反 硝化聚磷菌，该类微生物在缺氧池5中利用回流污泥中带入的N(V作为电子 受体进行反硝化吸收磷。在缺氧池5中平均停留时间为60〜80分钟；缺氧池 5A中排出的泥水进入缺氧池6B后，和进水泵B3泵入20〜30%的原水混合， 异养菌利用原水中的易降解碳源将缺氧池A5中未反应的NCV还原为N2。在 缺氧池B6中平均停留时间为20〜40分钟。缺氧池B6排出的泥水进入氧化沟 曝气池8中后，鼓风机12为位于曝气池8中的曝气头15提供氧气，对处理 水进行鼓风曝气，曝气量的大小根据运行状态进出水情况进行调整，控制出 水NH/在l~4mg/L，若出水NH4+超出该范围，就要对曝气量进行调整，出水 NH4+〉4mg/L时，增大曝气量，出水NH4+〈lmg/L时，减小曝气量。处理水在 氧化沟曝气池8中平均水力停留时间14-20小时后排水进入二沉池16中。在 氧化沟曝气池8中进行以下四种反应：异氧菌利用有机物进行的碳氧化反应、 硝化菌硝化反应、聚磷菌包括反硝化聚磷菌的吸收磷反应。从氧化沟曝气池8 中溢流出的处理水进入二沉池16进行泥水分离，上清液排出系统，回流污泥 分别回流至厌氧池A5和缺氧池B6。
按照以上实施步骤进行，活性污泥在氧化沟系统中经过3个月的驯化和 培养后，出水中COD、 NH/、 TP和TN的浓度分别为35.7〜60.5mg/L， 0~6.4mg/L， 0.11〜2.41mg/L和13.7~25.4mg/L,平均值分别为45.8mg/L， 3.4mg/L， 0.58mg/L和16.5mg/L， COD、 NH/、 TP和TN的平均去除率分别 为狄7、 93.4%、 92.1%和74.6%。
具体实施例二
接种污泥来自北京市酒仙桥污水处理厂的回流污泥，试验用水取自北京 工业大学家属池市政管道生活污水。主要水质指标为：COD为201〜532mg/L， NH/为47.5/61.9 mg/L， P(V—为3.4/8.6mg/L, TN为52.4/68.3 mg/L， pH为 7.2/7.8。试验中所采用的分析方法均按照国家环境保护局发布的标准方法.试验步骤为将接种污泥添加到曝气池8内，将生活污水投加入水箱1中， 启动进水泵A2和进水泵B3，进水泵A2和B3的进水比例为4: 1，同时开启 回流污泥泵A18和B19，回流污泥泵A18和B19的流量比为1: 3，通过连续 处理生活污水使活性污泥在氧化沟系统中经过2个月的驯化和培养，使氧化 沟系统内的活性污泥浓度维持在3000mg/L〜4500mg/L。 80°/。的原污水和25% 的回流污泥在厌氧池4中经搅拌器混合，回流污泥中的少量N(V快速被异养 菌反硝化去除，随后聚磷菌吸收挥发性有机酸，并进行磷的释放。在厌氧池 平均停留时间为40〜60分钟。厌氧池4中排出的泥水进入缺氧池A5后，和 污泥回流泵B19泵入的75%回流污泥混合，释磷后的聚磷菌部分具有反硝化 除磷功能，称为反硝化聚磷菌，该类微生物在缺氧池A5中利用回流污泥中带 入的N03—作为电子受体进行反硝化吸收磷。在缺氧池A5中平均停留时间为 60〜80分钟；缺氧池5A中排出的泥水进入缺氧池6B后，和进水泵B3泵入 的20°/。原水混合，异养菌利用原水中的易降解碳源将缺氧池A5中未反应的 NCV还原为N2。在缺氧池B6中平均停留时间为20〜40分钟。缺氧池B6排 出的泥水进入氧化沟曝气池8中后，鼓风机12为位于曝气池8中的曝气头15 提供氧气，对处理水进行鼓风曝气。处理水在氧化沟曝气池8中平均水力停 留时间14-20小时后排水进入二沉池16中。在氧化沟曝气池8中进行以下四 种反应：异氧菌利用有机物进行的碳氧化反应、硝化菌硝化反应、聚磷菌包 括反硝化聚磷菌的吸收磷反应。从氧化沟曝气池8中溢流出的处理水进入二 沉池16进行泥水分离，上清液排出系统，回流污泥分别回流至厌氧池A5和 缺氧池B6。
按照以上实施步骤进行，活性污泥在氧化沟系统中经过2个月的驯化和 培养后，出水中COD、NH4+、P043， TN的平均浓度分别为40.2mg/L，2.4mg/L， 0.41mg/L和15.4mg/L， COD、 NH/、 PO,和TN的平均去除率分别为86.4、 95.6%、 92.7%和73.5%。
Claims (1)
1、一种反硝化除磷的方法，应用一种厌氧-缺氧氧化沟工艺反硝化除磷装置，该装置包括水箱(1)、包括曝气池(8)的氧化沟主体和二沉池(16)，在所述的氧化沟主体前端增设三个选择器：厌氧池(4)、缺氧池A(5)和缺氧池B(6)，其特征在于，该方法包括以下步骤： 1)将含有聚磷菌、反硝化菌和硝化菌的活性污泥添加到氧化沟主体和二沉池(16)内，将生活污水投加入水箱(1)中，启动进水泵A(2)和进水泵B(3)，同时开启回流污泥泵A(18)和回流污泥泵B(19)，通过连续处理生活污水使活性污泥在氧化沟系统中经过1～2个月的驯化和培养；使氧化沟内的活性污泥浓度维持在3000mg/L～4500mg/L； 2)25～50％的回流污泥和70％～80％的原水在厌氧池(4)混合，回流污泥中的聚磷菌在厌氧状态下吸收易降解有机碳源释放磷，在厌氧池平均停留时间为40～60分钟； 3)上述厌氧池(4)中排出的泥水和其余的50％～75％回流污泥进入缺氧池A(5)后，因回流污泥中含有NO3-和NO2-，聚磷菌中的一部分菌称为反硝化聚磷菌，其在缺氧池A(5)进行以NO3-或NO2-作为最终电子受体的吸磷反应，在缺氧池(5)中平均停留时间为60～80分钟； 4)上述缺氧池A(5)中排出的泥水和其余的20％～30％原水进入缺氧池B(6)混合，异养菌利用原水中的有机物进行反硝化反应，还原缺氧池A(5)剩余的NO3-，在缺氧池B(6)中平均停留时间为20～40分钟； 5)上述缺氧池B(6)中排出的泥水进入曝气池(8)，在氧化沟中曝气系统提供氧气；在好氧状态下，异养菌氧化COD，硝化菌将NH4+氧化为NO2-和NO3-，聚磷菌吸收磷，在曝气池(8)中平均水力停留时间14-20小时，氧化沟中污泥浓度控制在3000～4500mg/L； 6)上述曝气池(8)中排出的泥水经溢流管溢流进入二沉池进行泥水分离，浓缩后的污泥经回流污泥泵A(18)送回上述厌氧池(4)，浓缩后的污泥经回流污泥泵B(19)送回上述缺氧池A(5)，上清液溢流排出系统； 7)剩余污泥通过剩余污泥泵(20)排出系统，通过排出剩余污泥来控制污泥龄，污泥龄控制在10～15d。
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