CN103613193A - A partitioned water-inflow type D-A2O sewage treatment method - Google Patents
A partitioned water-inflow type D-A2O sewage treatment method Download PDFInfo
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Abstract
本发明提供了一种分区进水式D-A2O污水处理方法，通过设计独立两相污泥/硝化液回流系统，其中一相正常进水并保持释磷和脱氮的同时，处于静歇的一相因过度缺氧而进行超量的释磷作用和充分的脱氮作用，确保系统厌氧段聚磷菌超量的释磷作用必然致使聚磷菌在好氧段的超量吸磷，最终以排放剩余污泥的形式而实现系统更为显著的除磷功效。本发明克服了A2O污水处理工艺中脱氮除磷效率难以进一步显著提升的问题，并且经过本发明处理后的出水水质稳定在一级A标至地表水环境质量Ⅴ类之间。
The invention provides a zonal water-inflow type DA 2 O sewage treatment method. By designing an independent two-phase sludge/nitrification liquid reflux system, one phase is in a static state while maintaining phosphorus release and nitrogen removal. In the first phase, excessive phosphorus release and sufficient denitrification are carried out due to excessive hypoxia, ensuring that the excessive phosphorus release by phosphorus accumulating bacteria in the anaerobic section of the system will inevitably lead to excessive phosphorus uptake by phosphorus accumulating bacteria in the aerobic section. Finally, the more significant phosphorus removal efficiency of the system is realized in the form of discharging excess sludge. The invention overcomes the problem that the efficiency of denitrification and phosphorus removal in the A2O sewage treatment process is difficult to be significantly improved further, and the quality of the effluent treated by the invention is stable between the first grade A standard and the surface water environmental quality grade V.
Description
技术领域technical field
本发明属于污水处理技术领域，尤其涉及一种分区进水式D-A2O污水处理方法。The invention belongs to the technical field of sewage treatment, and in particular relates to a zonal water-inflow type DA2O sewage treatment method.
背景技术Background technique
现有的A2/O污水处理方法为将污水经过厌氧池、缺氧池以及好氧池来进行处理，最后由沉淀池进行泥水分离，该方法不仅能有效去除污水中的有机物，亦可同步脱氮除磷。The existing A 2 /O sewage treatment method is to process sewage through anaerobic pool, anoxic pool and aerobic pool, and finally separate mud and water in sedimentation tank. This method can not only effectively remove organic matter in sewage, but also Simultaneous nitrogen and phosphorus removal.
但是，现有A2/O亦存在脱氮除磷效率难以进一步显著提升的问题，其主要原因是：（1）存在脱氮与除磷的碳源竞争问题；（2）存在微生物释磷和吸磷能力较低的问题。以往的研究成果表明，A2/O工艺中缺氧段的反硝化作用是除氮的主要途径，其关键在于缺氧段中是否有充足的碳源；同时，聚磷菌亦需摄取厌氧段中易降解有机物作释磷反应，方可在好氧段中过量吸磷而达到除磷之目的。当进水中的碳源缺乏，即进水为低C/N比时，A2/O工艺脱氮除磷碳源竞争问题尤为明显。从工艺流程来看，聚磷菌在厌氧段的释磷作用几乎消耗掉进水中的绝大部分易降解的有机物，故缺氧段仅剩的少量慢速或难降解的有机物难以满足反硝化脱氮作用而导致脱氮效果较差。从同一厌氧（缺氧）段来看，反硝化菌优先于聚磷菌利用有机碳源进行脱氮作用，从而导致聚磷菌释磷效果降低，其结果必然导致好氧段的吸磷效果不显著。因此，现有A2/O工艺的碳源竞争问题成为该工艺脱氮除磷的限制性因素。However, the existing A 2 /O also has the problem that it is difficult to further significantly improve the efficiency of nitrogen and phosphorus removal. The main reasons are: (1) the carbon source competition between nitrogen and phosphorus removal; (2) the existence of microbial phosphorus release and The problem of low phosphorus uptake capacity. Previous research results have shown that denitrification in the anoxic section of the A 2 /O process is the main way to remove nitrogen, and the key lies in whether there is sufficient carbon source in the anoxic section; The easy-to-degrade organic matter in the aerobic section can be used for phosphorus release reaction, so as to achieve the purpose of phosphorus removal in the aerobic section. When the carbon source in the influent water is short, that is, the influent water has a low C/N ratio, the competition problem of carbon source for nitrogen and phosphorus removal by A 2 /O process is particularly obvious. From the process point of view, the phosphorus-accumulating bacteria release phosphorus in the anaerobic section almost consumes most of the easily degradable organic matter in the water, so the only small amount of slow or refractory organic matter left in the anoxic section is difficult to meet the denitrification The denitrification effect leads to poor denitrification effect. From the perspective of the same anaerobic (anoxic) section, denitrifying bacteria use organic carbon sources to denitrify preferentially over phosphorus accumulating bacteria, which leads to a decrease in the phosphorus release effect of phosphorus accumulating bacteria, which will inevitably lead to the phosphorus uptake effect in the aerobic section Not obvious. Therefore, the competition of carbon sources in the existing A 2 /O process has become a limiting factor for the process of nitrogen and phosphorus removal.
此外，现有A2/O工艺脱氮除磷与回流比密切相关。过低的回流比难有理想的脱氮除磷功效，但过高的回流比亦因造成厌（缺）氧段DO浓度过高而难有较高的脱氮效果和释磷能力。因此，现有A2/O工艺均控制污泥、泥水混合液回流比于较低值，其释磷和吸磷能力较小。In addition, the existing A 2 /O process for nitrogen and phosphorus removal is closely related to the reflux ratio. If the reflux ratio is too low, it is difficult to have ideal denitrification and phosphorus removal effects, but if the reflux ratio is too high, it is also difficult to have a high denitrification effect and phosphorus release capacity due to the high DO concentration in the anaerobic (anoxic) section. Therefore, the existing A 2 /O process controls the reflux ratio of sludge and mud-water mixture to a low value, and its phosphorus release and phosphorus absorption capacity is relatively small.
发明内容Contents of the invention
本发明的目的在于提供一种分区进水式D-A2O污水处理方法，旨在解决现有A2O污水处理方法中脱氮除磷效率有限的问题。The purpose of the present invention is to provide a zonal water-inflow type DA 2 O sewage treatment method, aiming to solve the problem of limited efficiency of nitrogen and phosphorus removal in the existing A 2 O sewage treatment method.
本发明是这样实现的，一种分区进水式D-A2O污水处理方法，包括以下步骤:The present invention is realized in this way, a kind of divisional water-inlet type DA 2 O sewage treatment method, comprises the following steps:
（1）将未处理污水分别注入到第一厌氧池、第一缺氧池、第二厌氧池以及第二缺氧池中，将所述第一厌氧池中与第一缺氧池连通，将第二厌氧池中与第二缺氧池连通，将第一缺氧池以及第二缺氧池与好氧池连通，将所述好氧池与二次沉淀池连通；(1) Inject untreated sewage into the first anaerobic pond, the first anoxic pond, the second anoxic pond and the second anoxic pond respectively, and combine the first anaerobic pond with the first anoxic pond Connecting, connecting the second anaerobic pond with the second anoxic pond, connecting the first anoxic pond and the second anoxic pond with the aerobic pond, and connecting the aerobic pond with the secondary sedimentation pond;
（2）当分区进水至第一厌氧池和第一缺氧池时，将所述好氧池中的部分污水回流到第一缺氧池中，将所述二次沉淀池中的部分污泥回流到第一厌氧池中；停止第二厌氧池和第二缺氧池进水，将所述第二厌氧池和第二缺氧池静置一段时间；(2) When water is divided into the first anaerobic tank and the first anoxic tank, part of the sewage in the aerobic tank is returned to the first anoxic tank, and part of the sewage in the secondary sedimentation tank is The sludge is returned to the first anaerobic pond; the second anaerobic pond and the second anoxic pond are stopped, and the second anaerobic pond and the second anoxic pond are left to stand for a period of time;
（3）当分区进水至第二厌氧池和第二缺氧池时，将所述好氧池中的部分污水回流到第二缺氧池中，将所述二次沉淀池中的部分污泥回流到第二厌氧池中；停止第一厌氧池和第一缺氧池进水，同时停止第一缺氧池以及第一厌氧池的回流操作；并在第一厌氧池和第一缺氧池静置一段时间后，停止对第二缺氧池以及第二厌氧池的进水及回流操作并进入步骤（2）。(3) When water is divided into the second anaerobic tank and the second anoxic tank, part of the sewage in the aerobic tank is returned to the second anoxic tank, and part of the secondary sedimentation tank is The sludge is returned to the second anaerobic tank; the first anaerobic tank and the first anoxic tank are stopped, and the return operation of the first anoxic tank and the first anaerobic tank is stopped; and in the first anaerobic tank After standing still with the first anoxic tank for a period of time, stop the water inflow and backflow operations to the second anoxic tank and the second anaerobic tank and enter step (2).
优选地，在步骤（1）中，所述未处理污水注入到第一厌氧池和第一缺氧池的量的比例为（7～9）：（1～3）；所述未处理污水注入到第二厌氧池和第二缺氧池的量的比例为（7～9）：（1～3）。Preferably, in step (1), the ratio of the amount of the untreated sewage injected into the first anaerobic tank and the first anoxic tank is (7-9): (1-3); the untreated sewage The ratio of the amount injected into the second anaerobic tank and the second anoxic tank is (7-9): (1-3).
优选地，所述好氧池中污水回流到第一缺氧池或第二缺氧池中的回流比为150～300%，且所述好氧池中污泥浓度MLSS为3500～4500mg/L。Preferably, the reflux ratio of sewage in the aerobic tank to the first anoxic tank or the second anoxic tank is 150-300%, and the sludge concentration MLSS in the aerobic tank is 3500-4500 mg/L .
优选地，所述二次沉淀池中污泥回流到第一厌氧池或第二厌氧池中的回流比为50～150%，且所述二次沉淀池中回流污泥浓度MLSS为4000～6800mg/L。Preferably, the return ratio of the sludge in the secondary sedimentation tank to the first anaerobic tank or the second anaerobic tank is 50-150%, and the return sludge concentration MLSS in the secondary sedimentation tank is 4000 ~6800mg/L.
优选地，所述二次沉淀池中的部分污泥回流到第一厌氧池或第二厌氧池中的同时对第一厌氧池或第二厌氧池进行持续搅拌。Preferably, while part of the sludge in the secondary sedimentation tank is returned to the first anaerobic tank or the second anaerobic tank, the first anaerobic tank or the second anaerobic tank is continuously stirred.
优选地，所述好氧池中的部分污水回流到第一缺氧池或第二缺氧池中的同时对第一缺氧池或第二缺氧池进行持续搅拌。Preferably, when part of the sewage in the aerobic tank is returned to the first anoxic tank or the second anoxic tank, the first anoxic tank or the second anoxic tank is continuously stirred.
优选地，在步骤（2）中所述第二厌氧池和第二缺氧池的静置时间以及步骤（3）中所述第一厌氧池和第一缺氧池的静置时间均为1～4h。Preferably, the resting time of the second anaerobic pond and the second anoxic pond in step (2) and the resting time of the first anaerobic pond and the first anoxic pond in step (3) are both For 1 ~ 4h.
本发明克服现有技术的不足，提供一种分区进水式D-A2O污水处理方法，通过设计独立两相污泥/硝化液回流系统，其中一相正常进水并保持释磷和脱氮的同时，处于静歇的一相因过度缺氧而进行超量的释磷作用和充分的脱氮作用，确保系统厌氧段聚磷菌超量的释磷作用必然致使聚磷菌在好氧段的超量吸磷，最终以排放剩余污泥的形式而实现系统更为显著的除磷功效。在本发明中，还确定出未处理污水注入到厌氧池和缺氧池之间的量的比例的控制，能够有效避免系统因碳源不足而导致的脱氮除磷效率不高问题。此外，在本发明中，二次沉淀池的污泥回流比以及好氧池的污水回流比对本发明的脱氮除磷效率有较大影响。The present invention overcomes the deficiencies of the prior art and provides a partitioned water-inflow type DA 2 O sewage treatment method. By designing an independent two-phase sludge/nitrification liquid return system, one phase normally enters water and maintains phosphorus release and nitrogen removal. At the same time, excessive phosphorus release and sufficient denitrification are carried out in the resting phase due to excessive hypoxia, ensuring that the excessive phosphorus release of phosphorus-accumulating bacteria in the anaerobic section of the system will inevitably lead to phosphorus-accumulating bacteria in the aerobic section. The excess phosphorus uptake by the system will eventually achieve a more significant phosphorus removal effect in the form of excess sludge discharge. In the present invention, the control of the ratio of the amount of untreated sewage injected into the anaerobic tank and the anoxic tank is also determined, which can effectively avoid the problem of low nitrogen and phosphorus removal efficiency caused by insufficient carbon sources in the system. In addition, in the present invention, the sludge reflux ratio of the secondary sedimentation tank and the sewage reflux ratio of the aerobic tank have a great influence on the denitrification and phosphorus removal efficiency of the present invention.
相比与现有技术的缺点和不足，本发明具有以下有益效果：本发明克服了A2O污水处理工艺中脱氮除磷效率难以进一步显著提升的问题，并且经过本发明处理后的出水水质稳定在一级A标至地表水环境质量Ⅴ类之间。Compared with the shortcomings and deficiencies of the prior art, the present invention has the following beneficial effects: the present invention overcomes the problem that it is difficult to significantly improve the efficiency of nitrogen and phosphorus removal in the A2O sewage treatment process, and the quality of the effluent treated by the present invention is It is stable between the first grade A standard and the surface water environmental quality grade V.
附图说明Description of drawings
图1是本发明分区进水式D-A2O污水处理方法一实施例的工艺流程图；其中，1为第一厌氧池，2为第一缺氧池，3为第二厌氧池，4为第二缺氧池，5为好氧池，6为二次沉淀池；A1和A2为未处理污水的输入流路，B1和B2为硝化水回流流路，C1和C2为污泥回流流路，D为二次沉淀池的出水流路，F为二次沉淀池的污泥排放流路。Fig. 1 is a process flow chart of an embodiment of the partition water-inflow type DA2O sewage treatment method of the present invention; wherein, 1 is the first anaerobic tank, 2 is the first anoxic tank, 3 is the second anaerobic tank, 4 is the second anoxic tank, 5 is the aerobic tank, and 6 is the secondary sedimentation tank; A1 and A2 are the input flow path of untreated sewage, B1 and B2 are the return flow path of nitrification water, and C1 and C2 are the sludge return flow D is the effluent flow path of the secondary sedimentation tank, and F is the sludge discharge flow path of the secondary sedimentation tank.
具体实施方式Detailed ways
为了使本发明的目的、技术方案及优点更加清楚明白，以下结合附图及实施例，对本发明进行进一步详细说明。应当理解，此处所描述的具体实施例仅仅用以解释本发明，并不用于限定本发明。In order to make the object, technical solution and advantages of the present invention clearer, the present invention will be further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described here are only used to explain the present invention, not to limit the present invention.
在本发明实施例中，一种分区进水式D-A2O污水处理方法，包括以下步骤：In an embodiment of the present invention, a zonal water-inflow DA 2 O sewage treatment method includes the following steps:
（1）将未处理污水分别注入到第一厌氧池1、第一缺氧池2、第二厌氧池3以及第二缺氧池4中，将所述第一厌氧池1中与第一缺氧池2连通，将第二厌氧池3中与第二缺氧池4连通，将第一缺氧池2以及第二缺氧池4与好氧池5连通，将所述好氧池5与二次沉淀池连通；(1) Inject untreated sewage into the first anaerobic pool 1, the first anoxic pool 2, the second anaerobic pool 3, and the second anoxic pool 4, and combine the first anaerobic pool 1 with The first anoxic pool 2 is communicated, the second anoxic pool 3 is communicated with the second anoxic pool 4, the first anoxic pool 2 and the second anoxic pool 4 are communicated with the aerobic pool 5, and the well Oxygen tank 5 is communicated with secondary sedimentation tank;
（2）当分区进水至第一厌氧池和第一缺氧池时，将所述好氧池5中的部分污水回流到第一缺氧池2中，将所述二次沉淀池中的部分污泥回流到第一厌氧池1中；停止第二厌氧池和第二缺氧池进水，将所述第二厌氧池3和第二缺氧池4静置一段时间；(2) When water is divided into the first anaerobic tank and the first anoxic tank, part of the sewage in the aerobic tank 5 is returned to the first anoxic tank 2, and the secondary sedimentation tank Part of the sludge is returned to the first anaerobic pond 1; stop the second anaerobic pond and the second anoxic pond water intake, the second anaerobic pond 3 and the second anoxic pond 4 are left to stand for a period of time;
（3）当分区进水至第二厌氧池和第二缺氧池时，将所述好氧池5中的部分污水回流到第二缺氧池4中，将所述二次沉淀池中的部分污泥回流到第二厌氧池3中；停止第一厌氧池和第一缺氧池进水，同时停止对第一缺氧池2、第一厌氧池1的进水与回流操作，并在第一厌氧池1和第一缺氧池2静置一段时间后，停止对第二缺氧池4以及第二厌氧池3的进水与回流操作并进入步骤（2）。(3) When the water is divided into the second anaerobic tank and the second anoxic tank, part of the sewage in the aerobic tank 5 is returned to the second anoxic tank 4, and the secondary sedimentation tank part of the sludge back to the second anaerobic tank 3; stop the first anaerobic tank and the first anoxic tank inflow, while stopping the first anoxic tank 2, the first anaerobic tank 1 inflow and backflow operation, and after the first anaerobic pool 1 and the first anoxic pool 2 have been left to stand for a period of time, stop the water inflow and return operations to the second anoxic pool 4 and the second anaerobic pool 3 and enter step (2) .
更具体的，二次沉淀池中的部分污泥回流到第一厌氧池1或第二厌氧池3中的同时对第一厌氧池1或第二厌氧池3进行持续搅拌。好氧池5中的部分污水回流到第一缺氧池2或第二缺氧池4中的同时对第一缺氧池2或第二缺氧池4进行持续搅拌。搅拌使污水或者泥水混合均匀，更有利于聚磷菌以及反硝化菌的生长，提高除磷脱氮的效果。More specifically, part of the sludge in the secondary sedimentation tank is returned to the first anaerobic tank 1 or the second anaerobic tank 3 while continuously stirring the first anaerobic tank 1 or the second anaerobic tank 3 . Part of the sewage in the aerobic tank 5 flows back into the first anoxic tank 2 or the second anoxic tank 4 while continuously stirring the first anoxic tank 2 or the second anoxic tank 4 . Stirring makes the sewage or muddy water mix evenly, which is more conducive to the growth of phosphorus accumulating bacteria and denitrifying bacteria, and improves the effect of phosphorus and nitrogen removal.
在本发明的实际应用过程中，主要通过设计了独立两相污泥/硝化液回流系统，其中，在步骤（2）中，第一厌氧池1、第一缺氧池2、好氧池5以及二次沉淀池6为第一相污泥/硝化液回流系统，控制未处理污水的输入流路A1为第一厌氧池1和第一缺氧池2注入未处理污水，控制硝化水回流流路B1给第一缺氧池2回流硝化液，控制污泥回流流路C1给第一厌氧池1回流污泥，而第二相污泥/硝化液回流系统处于静置状态；而在步骤（3）中，第二厌氧池3和第二缺氧池4、好氧池5以及二次沉淀池又构成又第二相污泥/硝化液回流系统，控制未处理污水的输入流路A2为第一厌氧池3和第一缺氧池4注入未处理污水，控制硝化水回流流路B2给第一缺氧池4回流硝化液，控制污泥回流流路C2给第一厌氧池3回流污泥此时，第二厌氧池3和第二缺氧池4处于静置状态。In the actual application process of the present invention, mainly by designing an independent two-phase sludge/nitrification liquid return system, wherein, in step (2), the first anaerobic tank 1, the first anoxic tank 2, the aerobic tank 5 and the secondary sedimentation tank 6 are the first phase sludge/nitrification liquid return system, controlling the input flow path A1 of untreated sewage to inject untreated sewage into the first anaerobic tank 1 and the first anoxic tank 2, and controlling the nitrification water The return flow path B1 returns the nitrifying liquid to the first anoxic tank 2, and the control sludge return flow path C1 returns the sludge to the first anaerobic pool 1, while the second-phase sludge/nitrifying liquid return system is in a static state; and In step (3), the second anaerobic tank 3, the second anoxic tank 4, the aerobic tank 5 and the secondary sedimentation tank constitute a second-phase sludge/nitrifying liquid return system to control the input of untreated sewage The flow path A2 injects untreated sewage into the first anaerobic pool 3 and the first anoxic pool 4, controls the nitrification water return flow path B2 to return the nitrification liquid to the first anoxic pool 4, and controls the sludge return flow path C2 to the first anoxic pool. At this time, the anaerobic tank 3 returns the sludge, and the second anaerobic tank 3 and the second anoxic tank 4 are in a static state.
在本发明中，例如，当第一相污泥/硝化液回流系统工作时，未处理污水经恒流泵以一定比例分别流至第一相污泥/硝化液回流系统的第一厌氧池1和第一缺氧池2中，新注入污水会同来自二次沉淀池的回流污泥进入第一厌氧池1，第一厌氧池1中的出流污水再会同部分新注入污水以及来自好氧池5的回流污水进入第一缺氧池2中；此外，二次沉淀池中回流到第一厌氧池1的污泥经第一厌氧池1以及第一缺氧池2搅拌充分混合生化反应后，泥水混合液流至好氧池5；好氧池5一部分混合液回流至第一缺氧池2，另一部分由好氧池5的溢流堰出流至二次沉淀池6中进行泥水分离，上清液由二次沉淀池6的出水堰流出，污泥部分回流至第一厌氧池1，剩余污泥排出系统外。与好氧池5、二次沉淀池6回流的硝化液、污泥在搅拌机连搅拌使活性污泥微生物与污水中的污染物基质充分接触而发生有机物降解、脱氮和释磷反应，第一缺氧池2的泥水混合液流至好氧池5进行吸磷反应。当系统一相以上述运行状态运行时，另一相则处于静歇状态，整个试验过程，第一、第二相污泥/硝化液回流系统的交替运行实现了污染物的处理及污水的净化。更具体的，在本发明中第一、第二相污泥/硝化液回流系统每间隔1～4h交替一次。第一、第二相污泥/硝化液回流系统交替运行方式的结果是必然确保系统其中一相正常进水并保持释磷和脱氮的同时，处于静歇的一相因过度缺氧而进行超量的释磷作用和充分的脱氮作用。厌氧段聚磷菌超量的释磷作用必然致使聚磷菌在好氧段的超量吸磷，最终以排放剩余污泥的形式而实现系统更为显著的除磷功效。In the present invention, for example, when the first-phase sludge/nitrating liquid return system works, the untreated sewage flows to the first anaerobic tank of the first-phase sludge/nitrifying liquid return system in a certain proportion through the constant flow pump 1 and the first anoxic tank 2, the newly injected sewage enters the first anaerobic tank 1 together with the return sludge from the secondary sedimentation tank, and the outflow sewage in the first anaerobic tank 1 is combined with part of the newly injected sewage and the sludge from the The return sewage from the aerobic tank 5 enters the first anoxic tank 2; in addition, the sludge returned to the first anaerobic tank 1 in the secondary sedimentation tank is fully stirred by the first anaerobic tank 1 and the first anoxic tank 2 After the mixed biochemical reaction, the mud-water mixture flows to the aerobic tank 5; part of the mixed solution in the aerobic tank 5 flows back to the first anoxic tank 2, and the other part flows out from the overflow weir of the aerobic tank 5 to the secondary sedimentation tank 6 The mud-water separation is carried out in the middle, the supernatant liquid flows out from the outlet weir of the secondary sedimentation tank 6, and part of the sludge flows back to the first anaerobic tank 1, and the remaining sludge is discharged out of the system. The nitrification liquid and sludge returned to the aerobic tank 5 and the secondary sedimentation tank 6 are continuously stirred in the mixer to make the activated sludge microorganisms fully contact with the pollutant matrix in the sewage to cause organic matter degradation, denitrification and phosphorus release reactions. The mud-water mixture in the anoxic tank 2 flows to the aerobic tank 5 for phosphorus absorption reaction. When one phase of the system operates in the above-mentioned operating state, the other phase is in a static state. During the entire test process, the alternate operation of the first and second phase sludge/nitrating liquid return systems has realized the treatment of pollutants and the purification of sewage . More specifically, in the present invention, the first and second phase sludge/nitration liquid reflux systems are alternated every 1-4 hours. As a result of the alternating operation of the first and second phase sludge/nitrification liquid return systems, it is necessary to ensure that one phase of the system is normally influent and maintains phosphorus release and denitrification, while the resting phase is depleted due to excessive hypoxia. Excessive phosphorus release and sufficient denitrification. Excessive phosphorus release by phosphorus accumulating bacteria in the anaerobic stage will inevitably lead to excessive phosphorus uptake by phosphorus accumulating bacteria in the aerobic stage, and finally achieve a more significant phosphorus removal effect in the form of excess sludge discharge.
更具体的，为了进一步提高对污水中脱磷除氮的效果，在本发明实施例中，在上述步骤（1）中，所述未处理污水注入到第一厌氧池1和第一缺氧池2的量的比例为（7～9）：（1～3）；所述未处理污水注入到第二厌氧池3和第二缺氧池4的量的比例为（7～9）：（1～3）。More specifically, in order to further improve the effect of dephosphorization and nitrogen removal in sewage, in the embodiment of the present invention, in the above step (1), the untreated sewage is injected into the first anaerobic tank 1 and the first anoxic The ratio of the amount of pool 2 is (7-9): (1-3); the ratio of the amount of the untreated sewage injected into the second anaerobic pool 3 and the second anoxic pool 4 is (7-9): (1~3).
在本发明的实际应用过程中，采用从A2/O的厌氧池和缺氧池按一定比例分别进水，能够有效避免系统因碳源不足而导致的脱氮除磷效率不高问题。In the actual application process of the present invention, water is fed from the A 2 /O anaerobic tank and the anoxic tank at a certain ratio, which can effectively avoid the problem of low nitrogen and phosphorus removal efficiency caused by insufficient carbon sources in the system.
更具体的，为了能更好对污水中脱磷除氮效果的控制，在本发明实施例中，所述好氧池5中污水回流到第一缺氧池2或第二缺氧池4中的回流比为150～300%，且好氧池5中污泥浓度MLSS为3500～4500mg/L；所述二次沉淀池6中污泥回流到第一厌氧池1或第二厌氧池3中的回流比为50～150%，且回流污泥浓度MLSS为4000～6800mg/L。More specifically, in order to better control the effect of dephosphorization and nitrogen removal in sewage, in the embodiment of the present invention, the sewage in the aerobic pool 5 is returned to the first anoxic pool 2 or the second anoxic pool 4 The reflux ratio is 150-300%, and the sludge concentration MLSS in the aerobic tank 5 is 3500-4500 mg/L; the sludge in the secondary sedimentation tank 6 is returned to the first anaerobic tank 1 or the second anaerobic tank The reflux ratio in 3 is 50-150%, and the return sludge concentration MLSS is 4000-6800mg/L.
为了更好的证明本发明对污水处理过程中所具有的脱磷除氮的效果，本发明进行以下试验：In order to prove better that the present invention has the effect of dephosphorization and nitrogen removal in the sewage treatment process, the present invention carries out following test:
小试试验用水采用葡萄糖、蛋白胨、无水乙酸钠、磷酸二氢钾、氯化氨、碳酸氢纳等与自来水人工配置而成，用以模拟生活污水。The test water of the small test is artificially prepared by using glucose, peptone, anhydrous sodium acetate, potassium dihydrogen phosphate, ammonium chloride, sodium bicarbonate, etc. and tap water to simulate domestic sewage.
试验条件：水温=15～22℃；厌氧池进水比例=70～90%，缺氧池进水比例=10～30%；水力停留时间HRT=8～11h；混合液回流比R=150～300%（好氧池5污泥浓度MLSS=3500～4500mg/L）；污泥回流比r=50～150%（回流污泥浓度MLSS=4000～6800mg/L）；两相交替运行时间T=1～4h。Test conditions: water temperature = 15 ~ 22 ℃; anaerobic pool inlet ratio = 70 ~ 90%, anoxic pool inlet ratio = 10 ~ 30%; hydraulic retention time HRT = 8 ~ 11h; mixed liquid reflux ratio R = 150 ～300% (Aerobic pool 5 sludge concentration MLSS=3500～4500mg/L); sludge return ratio r=50～150% (reflux sludge concentration MLSS=4000～6800mg/L); Two-phase alternate operation time T =1～4h.
小试试验结果详见表1：The results of the small test are shown in Table 1:
表1试验结果Table 1 Test results
由表1可知，通过本发明的方法处理后的出水水质稳定在一级A标至地表水环境质量Ⅴ类之间。As can be seen from Table 1, the quality of the effluent treated by the method of the present invention is stable between the first grade A standard and the surface water environmental quality grade V.
以上所述仅为本发明的较佳实施例而已，并不用以限制本发明，凡在本发明的精神和原则之内所作的任何修改、等同替换和改进等，均应包含在本发明的保护范围之内。The above descriptions are only preferred embodiments of the present invention, and are not intended to limit the present invention. Any modifications, equivalent replacements and improvements made within the spirit and principles of the present invention should be included in the protection of the present invention. within range.
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