WO2011160603A1 - 一种多级的生物脱氮除磷污水处理方法以及装置 - Google Patents

一种多级的生物脱氮除磷污水处理方法以及装置 Download PDF

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Publication number
WO2011160603A1
WO2011160603A1 PCT/CN2011/076358 CN2011076358W WO2011160603A1 WO 2011160603 A1 WO2011160603 A1 WO 2011160603A1 CN 2011076358 W CN2011076358 W CN 2011076358W WO 2011160603 A1 WO2011160603 A1 WO 2011160603A1
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tank
stage
aerobic
anoxic
anaerobic
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PCT/CN2011/076358
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English (en)
French (fr)
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杨企星
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可事托环保设备（上海）有限公司
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Publication of WO2011160603A1 publication Critical patent/WO2011160603A1/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
    • C02F3/308—Biological phosphorus removal

Definitions

  • Multi-stage biological nitrogen and phosphorus removal sewage treatment method and device Multi-stage biological nitrogen and phosphorus removal sewage treatment method and device
  • the invention relates to the technical field of environmental protection, in particular to a multi-stage biological nitrogen and phosphorus removal sewage treatment method and device.
  • A20 is the abbreviation of "anaerobic-anoxic-Oxic", and the A20 biological nitrogen and phosphorus removal process is a combination of traditional activated sludge process, biological digestion and anti-digestion process and biological phosphorus removal process. .
  • the structure of the device is shown in Fig. 1.
  • the sewage enters the anaerobic tank 1, the anoxic tank 2 and the aerobic tank 3 in sequence, and finally is discharged through the reflux tank 4, and the reflux tank 4 passes the sludge in the lower part of the sewage through the external return pipe. 5
  • an internal return pipe 6 is further disposed between the aerobic tank 3 and the anoxic tank 2.
  • the flora is mainly composed of nitrifying bacteria, denitrifying bacteria and polyphosphate bacteria.
  • the nitrifying bacteria converts the ammonia nitrogen and the organic nitrogen which are in the inflow into ammonia nitrogen, which is converted into nitrate by biological nitrification; in the anoxic tank 2, the denitrifying bacteria bring the internal reflux tube 6 into the Nitrate is converted into nitrogen by biological denitrification and escapes into the atmosphere to achieve the purpose of denitrification.
  • phosphorus accumulating bacteria release phosphorus and absorb easily degradable organic substances such as lower fatty acids.
  • oxygen pool 3 the phosphorus accumulating bacteria excessively absorb phosphorus, and the black matter is removed by discharging the excess sludge.
  • the advantage of the A20 process is that the three different environmental conditions of anaerobic, anoxic and aerobic and the organic combination of the microbial flora can simultaneously remove the organic matter and remove nitrogen and phosphorus; at the same time, the organic matter is removed by deoxidation and dephosphorization.
  • the process is the simplest, and the total hydraulic retention time is less than other similar processes; in the anaerobic-anoxic-aerobic alternate operation, the filamentous bacteria will not multiply, SVI is generally less than 100, will not 5 ⁇ The sludge is swelled;
  • the A20 process shown in Figure 1 can control the total phosphorus emission in the discharged sewage to be within l ⁇ 15mg/L, and the total nitrogen emission is controlled at 20 ⁇ 25mg/L.
  • the standards for total nitrogen and total phosphorus in wastewater are becoming more and more demanding. example For the mainland China, the total phosphorus emission is less than 0.5m g L and the total nitrogen emission is less than 15mg/L.
  • the prior art has not been able to meet this requirement.
  • the technical problem to be solved by the present invention is to provide a multi-stage biological nitrogen and phosphorus removal sewage treatment method and device, based on the reaction pool in the current A20 system, on the basis of not increasing the land occupation and chemical agents, More efficient filtration of total nitrogen and total phosphorus in wastewater.
  • the present invention provides a multi-stage biological nitrogen and phosphorus removal sewage treatment method, comprising: introducing sewage into an anaerobic tank; and then passing the anaerobic treated sewage into a lack-aerobic treatment unit
  • the lack-aerobic treatment unit is formed by a plurality of abundance-aerobic combination pools connected end to end, at least including from the first stage
  • the aerobic tank is refluxed to the return line of the anoxic tank of the same level; the sewage is completely discharged to the sedimentation tank through the last stage aerobic tank; the precipitated sludge is discharged into the return sludge concentration tank, in the sedimentation tank
  • the supernatant is used as a purified water discharge device; the supernatant in the return sludge concentration tank is discharged into the last stage aerobic tank; the sludge in the return sludge concentration tank is discharged into the last stage aerobic tank; the sludge in the return sludge concentration tank is discharge
  • the concentration of the nitrate is determined in the anoxic pool of each stage, and if the concentration of nitric acid in the pool is insufficient, The aerobic tank effluent of one or the following stage is returned to the anoxic tank for recycling to improve the denitrification capacity of the system.
  • the sewage is discharged from the anaerobic tank, it is only introduced into the first stage of the front stage of the lack-aerobic treatment unit or the continuous multi-stage anoxic tank from the first stage of the front stage, and according to the influent water Conditions and effluent requirements do not have to be directly passed to the last level or continuous two- or three-stage anoxic pool from the last level.
  • the invention further provides a multi-stage biological nitrogen and phosphorus removal sewage treatment device, comprising an anaerobic tank, a plurality of aerobic combined pool composed of an anoxic tank and an aerobic tank, a sedimentation tank, A return sludge concentration tank and a pre-anoxic tank, a plurality of aerobic combination pools are connected end to end to form a multi-stage lack-aerobic treatment unit, the sewage inlet pipe is connected to the anaerobic tank, and the anaerobic tank is directly connected to the anaerobic tank - the first stage of the front stage of the aerobic treatment unit or the continuous multi-stage anoxic tank from the first stage of the previous stage, the last aerobic tank of the multi-stage lack-aerobic treatment unit is connected to the sedimentation tank, the sedimentation tank connection device
  • the outlet pipe, the sedimentation tank is also connected to the anaerobic tank through the return sludge concentration tank and the pre-anoxic tank to form an external reflux pipeline, and the reflux s
  • the last stage of the multi-stage lack-aerobic treatment unit or the continuous two-stage or three-stage anoxic tank from the last stage is not connected to the anaerobic tank.
  • each aerobic tank has an internal return conduit between the anoxic tank of the same stage and the anoxic tank of the above stages.
  • the type of the anaerobic tank is selected from one of a single cell or a plurality of series cells.
  • the invention has the advantages that only one backflow sludge concentration tank and a pre-anoxic tank connected thereto are added compared with the A20 process in the prior art, and the filtration is improved by adjusting the connection relationship between the respective filter tanks.
  • Efficiency specifically:
  • the sedimentation tank is connected to the original anaerobic tank through the return sludge concentration tank and the pre-anoxic tank to form an external reflux pipeline, which reduces the flow rate of the entire system, thereby reducing the dilution of the VFA and also controlling the negative of the nitrates.
  • the function optimizes the biological phosphorus removal environment, increases the sludge concentration and the actual residence time of all the front end regions except the final supernatant entering the section (the last stage of the aerobic tank), that is, strengthens the above biological phosphorus removal and denitrification
  • the total amount of nitrifying bacteria, the actual nitrification reaction time, and the reactant concentration in the front end region are enhanced, and the nitrification and denitrification reactions are enhanced to ensure the removal rate of the system organic nitrogen nitrogen ammonia and total ammonia.
  • the sludge concentration process greatly increases the sludge concentration and residence time of the pre-anoxic tank.
  • Pre-hypoxia The oxygen demand for endogenous degradation of the tank high sludge concentration and the increased actual residence time have fully met the requirement that the nitrate nitrogen entering the anaerobic tank is reduced to a sufficiently low level, which causes all the wastewater to enter the front anaerobic tank. It is feasible.
  • the limited carbon source is fully utilized, the required additional carbon source is reduced to a minimum, and the system is able to meet the total nitrogen emissions without increasing the pool capacity. need.
  • the anaerobic mixture is split into the first three anoxic tanks in the four-stage aerobic treatment unit.
  • the purpose is to ensure that all of the limited raw wastewater carbon sources are used for denitrification in the anoxic tank and through multiple stages of degradation.
  • Figure 1 is a schematic view showing the structure of an A20 device in the prior art.
  • FIG. 2 is a schematic structural view of the apparatus according to an embodiment of the present invention.
  • Figure 3 is a schematic illustration of the construction of the apparatus of another embodiment of the present invention with more flexibility.
  • Figure 4 is a schematic view showing the structure of an apparatus according to an embodiment of the present invention.
  • Figure 5 is a flow chart of the sewage treatment of the design shown in Figure 4.
  • 6 and 7 are schematic views showing the processing results of the above-described engineering examples.
  • FIG. 2 is a schematic view showing the structure of the apparatus of the present embodiment.
  • the apparatus shown includes: an anaerobic tank 110, a plurality of aerobic pools 130 formed by an anoxic tank 131 and an aerobic tank group 132, a sedimentation tank 150, a reflux sludge concentration tank 170, and a pre-anoxic tank 190, a plurality of lack-aerobic combination tanks 130 are connected end to end to form a multi-stage aerobic treatment unit 140, and a return line 133 from the first stage aerobic tank to the same level anoxic tank. .
  • the fourth embodiment of the present invention is a four-stage lack-aerobic combination unit composed of four groups of aerobic combination pools 130. 140 is explained as an example. In other embodiments, a suitable number of the aerobic combination pool forming processing unit can be flexibly selected according to the actual conditions of the project.
  • the type of anaerobic tank 110 is selected from one of a single cell or a plurality of series cells.
  • the inlet pipe of the sewage is connected to the anaerobic tank 110, and the anaerobic tank 110 is directly connected to the first stage of the front stage of the lack-aerobic treatment unit 140 or the continuous multi-stage anoxic tank 131 from the first stage of the front stage, wherein at least There is an in-stage return pipe 133 between the first stage aerobic tank 132 and the present stage anoxic tank 131, and the last aerobic tank 132 of the multi-stage lack-aerobic treatment unit is connected to the sedimentation tank 150, and the sedimentation tank 150 is connected.
  • the outlet pipe of the device, the sedimentation tank 150 is also connected to the initial anaerobic tank 110 through the return sludge concentration tank 170 and the pre-anoxic tank 190 to form an external return line, the return sludge concentration tank 170 further and the last stage aerobic tank A supernatant reflux conduit is formed between 132.
  • the method of treating sewage using the above device is as follows:
  • the sewage is passed to the anaerobic tank 110.
  • the sewage treated by the anaerobic tank 110 is introduced into the first stage of the front stage of the lack-aerobic treatment unit 140 or the continuous multi-stage anoxic tank 131 from the first stage of the preceding stage, the lack-aerobic treatment unit 140 is formed by connecting a plurality of lack-aerobic combination pools 130 end to end.
  • All of the sewage is discharged to the sedimentation tank 150 through the last stage aerobic tank 132.
  • the sludge precipitated in the sedimentation tank 150 is discharged to the return sludge concentration tank 170, and the supernatant in the sedimentation tank 150 is used as a purified water discharge device, and the remaining sludge of the system is discharged to the sludge disposal system of the sewage treatment plant.
  • the supernatant in the return sludge concentration tank 170 is discharged to the last stage aerobic tank 132.
  • the sludge in the return sludge concentration tank 170 is discharged into the initial anaerobic tank through the pre-anoxic tank 190 to carry out a sludge inoculation cycle reaction.
  • the characteristics of the sewage treated by the apparatus and method of the present embodiment are mainly that the reflux sludge concentration process is adopted, the total amount of liquid entering the front anaerobic zone and each reaction is greatly reduced, and the multi-stage anoxic-aerobic reaction is utilized.
  • the zone allows the mixture of anaerobic tanks to be split into multiple anoxic tanks.
  • a reflux sludge concentration process means that the sedimentation tank 150 is connected to the initial anaerobic tank 110 through the return sludge concentration tank 170 and the pre-anoxic tank 190 to form an external reflux line.
  • the function of the return sludge concentration tank 170 is to further separate the muddy water, and only a small amount of the liquid refluxed from the sedimentation tank 150 and most of the sludge are subjected to high-efficiency strengthening under the condition of high sludge concentration in the pre-anoxic tank 190.
  • Source drop After the denitrification process, the anaerobic pond 110 is entered, and after mixing with 100% of the original wastewater, a two-stage continuous anaerobic reaction is carried out.
  • the advantage of the reflux sludge concentration process is that the sludge concentration in the anaerobic tank 110 at the front end of the system is increased by increasing the reflux sludge concentration tank 170, the actual residence time of the sewage in the anaerobic tank 110 is increased, and the backflow is reduced.
  • the oxygen zone and the reactants of the front reaction zone are controlled by the elimination of the supernatant in the reflux sludge concentration tank 170 and the denitrification in the pre-anoxic tank 190.
  • the total amount of nitrate in the oxygen pool 110 is controlled by the elimination of the supernatant in the reflux sludge concentration tank 170 and the denitrification in the pre-anoxic tank 190.
  • the return sludge concentration tank 170 controls the amount of the return liquid entering the anaerobic tank 110. Once the bottom flow rate of the sedimentation tank 150 which is separated by the mud water is fixed, the additional reflux will only increase the amount of the returned liquid, resulting in sludge concentration in the anaerobic zone. And dilution of organic matter. After the reflux mixture is subjected to slurry separation and concentration through the return sludge concentration tank 170, the pre-anoxic tank 190 continues to denitrify the remaining nitrate nitrogen (NO- X- N), and the apparatus relies on the internal carbon source.
  • NO- X- N nitrate nitrogen
  • the nitrate nitrogen concentration of the sludge can be controlled at 1 ⁇ 2 mg/L to ensure that the operation of the anaerobic tank 110 is not affected, and the carbon-free source adsorption release of phosphorus in the pre-anoxic tank 190 is prevented. .
  • the reduction in backflow to the anaerobic tank 110 further ensures that the effect of nitrate nitrogen on the anaerobic state is reduced to a minimum.
  • VFA volatile fatty acids
  • BCOD slowly degrading organic carbon
  • the increase in sludge concentration also increases the amount of polyphosphate bacteria.
  • the reflux liquid helium removes almost all organic carbon sources, and the increase in return flow will be thin.
  • the organic carbon source and VFA concentration in the anaerobic zone are released, thereby reducing the VFA adsorption effect of the polyphosphate bacteria.
  • the phosphorus release of phosphorus and the storage of PHB (poly- ⁇ -hydroxybutyric acid) are spontaneously high, thereby improving the phosphorus removal efficiency of the system, and the backflow to the anaerobic tank 110 is small.
  • the resulting large hydraulic retention time provides a longer reaction time for the polyphosphate bacteria in the anaerobic tank 110, thereby making more use of the VFA to convert to sputum.
  • the increase in sludge concentration and the actual hydraulic retention time in the anaerobic tank 110 also enhance the hydrolysis effect of the slow-degrading organic carbon source (SBCOD), and at the same time make it more easily degraded in the denitrification process of the anoxic tank 131 without being carried.
  • SBCOD slow-degrading organic carbon source
  • the limited carbon source is fully utilized, and the system energy consumption is also reduced.
  • the reduction in the return flow also increases the actual hydraulic retention time of each anoxic section, thereby enhancing the denitrification reaction of the anoxic tank 131.
  • the increase of sludge concentration in anoxic tank 131 not only ensures the strengthening of denitrification reaction, but also reduces the probability of SBCOD being entrained into the aeration tank, and also strengthens the rate of endogenous degradation denitrification, thus ensuring a limited carbon source. Make full use of the denitrification reaction.
  • the sludge return concentration tank 170 reduces the flow rate of the entire system, increasing the sludge concentration and the actual residence time of all front end regions except the final supernatant entering the section (the last stage of the aerobic tank 132), ie strengthening
  • the total amount of nitrifying bacteria, the actual nitrification reaction time, and the reactant concentration in the front end region are enhanced, and the nitrification reaction is enhanced to ensure the removal rate of organic nitrogen and ammonia nitrogen in the system. .
  • the strengthening of anaerobic conditions in the anaerobic tank 131 caused by less reflux dilution can also inhibit the growth of filamentous bacteria in the system, improve the sedimentation state of the sludge, and control the SVI of the system to be around 50, thereby ensuring contamination. Increased mud solubility.
  • the sludge concentration process reduces the total amount of pre-anoxic tank 190, which greatly increases the sludge concentration and residence time of the pre-anoxic tank 190.
  • the oxygen demand of the endogenous degradation of the high sludge concentration in the pre-anoxic tank 190 and the increased actual residence time have fully met the requirement that the nitrate nitrogen entering the anaerobic tank 110 is reduced to a sufficiently low level so that it is not necessary to divert the carbon source to the pre-deficient
  • the oxygen pool which makes it possible for all of the wastewater to enter the front anaerobic tank 110 becomes feasible. Setting the anaerobic tank 110 only at the front end and having only one inlet makes the system responsive. All of the wastewater entering the front increases the concentration of BOD5 and VFA in the anaerobic zone, which enhances the biological phosphorus removal effect.
  • SBCOD has a longer process of conversion to BCOD, so that it can be fully utilized in the denitrification process of the anoxic tank 131 without being carried to the aeration tank, thereby greatly reducing the denitrification reaction while greatly reducing
  • the aerobic to organic carbon source oxygen demand optimized the growth conditions of nitrifying bacteria in the aeration zone, and enhanced the system's nitrification efficiency.
  • the four-stage lack-aerobic treatment unit 140 is also one of the important features of the present embodiment.
  • the main role of the anoxic tanks in the first stage is to denitrify the nitrate nitrogen in the previous aerobic tank, thus forming a staged degradation of the total nitrogen of the system, eliminating the traditional large-flow internal reflux system.
  • the actual residence time in each reaction cell in the system is improved, the dilution of the organic carbon source in the anoxic zone caused by the reflux is reduced, the carbon source is fully utilized, and the denitrification reaction is enhanced.
  • the mixed liquid of the anaerobic tank 110 is branched into the first three anoxic tanks 131 in the four-stage aerobic treatment unit 140 for the purpose of ensuring that all of the raw waste water has a limited carbon source in the anoxic tank 131.
  • This arrangement can not only enhance the denitrification in the anoxic tank 131, but also cause the adsorption of phosphorus by the phosphorus accumulating bacteria in different environments by the anaerobic pool 110 to the diversion in the multi-stage anoxic tank 131, thereby making the biological phosphorus removal. Maximizes the growth of polyphosphate bacteria.
  • the phosphorus-accumulating bacteria can oxidize and release phosphorus in the body during the process of oxidizing and releasing phosphorus, that is, the concept of one carbon and two carbon, further utilizing a limited carbon source.
  • the liquid discharged from the anaerobic tank can also be diverted to more or less anoxic tanks, and the above technical effects can also be achieved.
  • the carbon source is not required to be high, and the endogenous degradation can be completely relied on for denitrification. Therefore, in a preferred embodiment
  • the last stage of the multi-stage lack-aerobic treatment unit 140 or the continuous two-stage or three-stage anoxic pool from the last stage is no longer connected to the anaerobic tank 110 to ensure the denitrification effect.
  • the effect of the last stage of the anoxic tank 131 not directly connected to the anaerobic tank 110 is also to prevent the organic nitrogen or ammonia nitrogen in the raw wastewater from entering the rear end of the reaction zone to ensure that the total nitrogen in the effluent reaches a minimum, and at the same time, the hypoxia can also be selected.
  • An additional carbon source facility (not shown) is set up in the pool 131 to ensure sufficient denitrification at this stage to ensure that the nitrate nitrogen in the mixture leaving the anoxic tank 131 is sufficiently low to ensure that the total nitrogen output can be Completely up to standard.
  • the last two or three stages of anoxic tanks may not be directly connected to the anaerobic tank according to the actual situation of the sewage, so as to ensure that the endogenous denitrification of the anoxic tank can be carried out more smoothly.
  • each aerobic tank 132 has an internal return pipeline between the anoxic tank 131 of the same stage and the anoxic pool 131 of the above stages, and the advantage is that the sewage passes through multiple stages. - During the aerobic treatment unit, the nitrate can be detected at the outlet of each stage of the anoxic tank 131.
  • the aerobic effluent is returned to the same level or above through the internal reflux line. Cycling in the anoxic tank, which stage of the anoxic tank can be returned to can be determined according to the actual water quality. In particular, a reflux line between the first stage aerobic tank and the first stage anoxic tank is necessary because the nitrates of the first stage anoxic tank are dependent on this reflux.
  • This embodiment is a secondary biological reaction scheme for a sewage plant.
  • this embodiment adopts a more typical process structure, namely, reflux concentration, anaerobic, and three-stage splitting.
  • Insufficient aerobic plus an endogenous deficiencies/aerobic degradation system to make full use of the limited carbon source to achieve the best phosphorus and nitrogen removal effect of the system.
  • the detailed process and distribution of each section of the system are shown in Figure 4.
  • the total system residence time is about 16 Hours, wherein the aerobic reaction time is 7.5 hours, the anoxic reaction time is 4.5 hours, the anaerobic reaction is 1 hour, and the total reaction time is 12.5 hours.
  • the SRT of the system design winter worst case condition (12 C) is 12 days.
  • the total volume of the sewage plant is 1 million tons, divided into 4 groups of 250,000 tons each, 2 sets per group, each 125,000 tons / grid / day.
  • Figure 2 shows the detailed design and system layout of the single cell reaction cell.
  • the system has a water depth of 6 meters, a length of 150 meters and a width of 740 meters.
  • an anaerobic water flow lifting pump and one stage of each aerobic reflux pump are respectively provided (2.5 KW). And 5.5 KW) are low lift over the wall to improve the pump, the pump has high efficiency and low energy consumption. Thanks to the segmentation technology, the total reflow/lift capacity of the system is significantly reduced compared to the existing A20 technology, which improves the processing capacity of the system and saves energy.
  • the flow distribution of each section of the split flow is completed by the frequency conversion control of the water pump and the opening degree of the rear-end area shunt gate. Microporous aeration in the 6 m water depth zone allows the fan and microporous aerator to work in their optimum working area.
  • the primary sedimentation tank of this embodiment adopts a 45-minute short-range, sediment removal design, mainly removes inorganic particles, removes 30% TSS, 15% COD, and 10% BOD5, and the secondary sedimentation tank can adopt the sedimentation tank of Zhoujin Zhouchu to improve
  • the clarification effect is that the concentration of the bottom sludge in the 1Q reflux is about 4000mg/l, and the concentration is up to 12000mg/l.
  • the 0.3Q is concentrated into the pre-anoxic tank for denitrification, and then enters the anaerobic zone and mixes with the incoming sewage. Begin the bioreactor degradation process.
  • Figure 5 is a plan view of the design shown in Figure 4, with the most unfavorable water temperature of 12 °C in winter. The age of the SRT designed under this condition is 12 days.
  • Figure 6 shows the distribution of mixed liquor sludge MLSS, showing that the majority of the MLSS can be controlled at 3300 mg/l, a reasonable range.
  • Figure 7 is a table showing the concentration distribution of each pollutant in each reaction zone.
  • the final line of effluent shows that the water quality is far superior to the national A-level emission standards, which fully reflects the reliability of the design.

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Description

一种多级的生物脱氮除磷污水处理方法以及装置
【技术领域】
本发明涉及环保技术领域，尤其涉及一种多级的生物脱氮除磷污水处理方 法以及装置。
【背景技术】
A20是 "厌氧-缺氧-好氧"（ Anaerobic- Anoxic-Oxic) 的英文缩写， A20 生物脱氮除磷工艺是传统活性污泥工艺、生物消化及反消化工艺和生物除磷工 艺的综合。 其装置的结构示意图如附图 1所示， 污水依次进入厌氧池 1、 缺氧 池 2和好氧池 3， 最后经过回流池 4排出， 回流池 4将污水下部的污泥经过外 部回流管 5重新通入厌氧池 1进行循环处理，在好氧池 3和缺氧池 2之间还设 置一内部回流管 6。
在该装置内， BOD5、 SS和以各种形式存在的氮和磷将一一被去除。 A20 生物脱氮除磷系统的活性污泥中，菌群主要由硝化菌和反硝化菌、聚磷菌组成。 在好氧池 3中， 硝化细菌将入流中的氨氮及有机氮氨化成的氨氮， 通过生物硝 化作用， 转化成硝酸盐； 在缺氧池 2中， 反硝化细菌将内部回流管 6带入的硝 酸盐通过生物反硝化作用， 转化成氮气逸入到大气中， 从而达到脱氮的目的； 在厌氧池 1中， 聚磷菌释放磷， 并吸收低级脂肪酸等易降解的有机物， 而在好 氧池 3中， 聚磷菌则超量吸收磷， 并通过剩余污泥的排放， 将磯除去。
A20工艺的优点在于， 厌氧、缺氧、好氧三种不同的环境条件和种类微生 物菌群的有机配合， 能同时具有去除有机物、 脱氮除磷的功能； 在同时脱氧除 磷去除有机物的工艺中， 该工艺流程最为简单， 总的水力停留时间也少于同类 其他工艺； 在厌氧一缺氧一好氧交替运行下， 丝状菌不会大量繁殖， SVI—般 小于 100， 不会发生污泥膨胀； 污泥中磷含量高， 一般为 2. 5 %以上。
现有技术条件下， 图 1所示的 A20工艺能将排放污水中的总磷排放量控 制在 l〜15mg/L以内， 总氮排放量控制在 20〜25mg/L。 但是， 随着世界各地 对环境保护的日益重视， 对排放污水中的总氮和总磷含量标准越来越苛刻。例 如对于中国大陆地区而言， 要求总磷排放量小于 0.5mg L， 总氮排放量小于 15mg/L, 显然现有技术已经不能达到这一要求。
针对这一问题， 目前提出了很多解决方案， 例如 Roderick D. Reardon等人 在 2003 Water Environment Federation中提出的步进式给料 （STEP-FEED) 工 艺， 在与传统工艺达到相同的 lOmg/L总氮排放指标的情况下， 单位时间内处 理的污水量是传统工艺的两倍， 且节约成本。
日本的研究小组则将重点放在化学除磷上，改用化学药剂代替现有技术中 的聚磷菌生物除磯技术， 也取得了较好的效果， 但大量使用化学药剂所带来的 对环境的负面影响仍然处在研究阶段。
中国的研究小组也致力于对 A20 工艺的改进， 可以参考申请号为 200610119326.1 > 200710191174.0以及 200610117730.5等中国专利或者专利申 请中所披露的内容。
【发明内容】
本发明所要解决的技术问题是，提供一种多级的生物脱氮除磷污水处理方 法以及装置， 以现行 A20系统中的反应池作为基础， 在不大量增加占地和化 学药剂的基础上， 更有效的过滤污水中的总氮和总磷含量。
为了解决上述问题， 本发明提供了一种多级的生物脱氮除磷污水处理方 法， 包括： 将污水通入厌氧池； 再将厌氧池处理过的污水通入缺 -好氧处理单 元中前段的第一级或者自前段第一级起连续的多级缺氧池中， 所述缺-好氧处 理单元由多个缺-好氧组合池首尾相连形成， 其中至少包括从第一级的好氧池 回流至同级的缺氧池的回流管道；将污水全部通过最末一级好氧池排出至沉淀 池； 将沉淀后的污泥排入至回流污泥浓缩池， 沉淀池中的上清液作为净化水排 出装置； 将回流污泥浓缩池中的上清液排入最末一级好氧池； 将回流污泥浓缩 池中的污泥通过预缺氧池排入最初的厌氧池进行循环处理。
作为可选的技术方案， 在污水经过多级缺 -好氧处理单元的过程中， 在每 一级的缺氧池测定其硝酸盐类的浓度， 如该池中的硝酸浓度不够， 则将本级或 以下某一级的好氧池出水回流至此级缺氧池中循环处理， 以提高系统的反硝化 能力。 作为可选的技术方案， 污水从厌氧池排出后， 仅通入缺-好氧处理单元中 前段的第一级或者自前段第一级起连续的多级缺氧池中，而根据进水条件及出 水要求并不必须直接通入最后一级或者自最后一级起的连续两级或者三级缺 氧池中。
本发明进一步提供了一种多级的生物脱氮除磷污水处理装置，包括一厌氧 池、 多个由一缺氧池和一好氧池组成的缺-好氧组合池、 一沉淀池、 一回流污 泥浓缩池和一预缺氧池， 多个缺好氧组合池首尾相连形成多级缺 -好氧处理单 元， 污水的进水管连接至厌氧池， 厌氧池再直接连接至缺 -好氧处理单元中前 段的第一级或者自前段第一级起连续的多级缺氧池， 多级缺-好氧处理单元的 最末一个好氧池连接至沉淀池， 沉淀池连接装置的出水管， 沉淀池还通过回流 污泥浓缩池和预缺氧池连接至厌氧池形成外部回流管道， 回流污泥浓缩池进一 步和最末一级好氧池之间形成上清液回流管道。
作为可选的技术方案， 多级缺-好氧处理单元的最后一级或者自最后一级 起的连续两级或者三级缺氧池并不与厌氧池连接。
作为可选的技术方案，每个好氧池与同一级的缺氧池以及以上各级的缺氧 池之间具有内部回流管道。
作为可选的技术方案，所述厌氧池的类型选自于单池或者多个串联池中的 一种。
本发明的优点在于， 同现有技术中的 A20工艺相比， 仅增加了一回流污 泥浓缩池和与其连接的一预缺氧池，并且通过对各个过滤池之间连接关系的调 整提高了过滤效率， 具体在于：
沉淀池通过回流污泥浓缩池和预缺氧池连接至最初的厌氧池形成了外部 回流管道， 减少了整个系统的流量， 从而减小了 VFA的稀释， 同时也控制了 硝酸盐类的负面作用优化了生物除磷环境，增加了污泥浓度及除最后上清液进 入段（最后一级的好氧池）外所有前端区域的实际停留时间， 即强化了上述的 生物除磷及反硝化反应之外， 也增加了硝化菌的总量， 实际硝化反应时间， 以 及前端区域的反应物浓度， 强化了硝化及反硝化反应， 保证了系统有机氮氮氨 以及总氨的去除率。
污泥浓缩工艺使得预缺氧池的污泥浓度及停留时间都大大提高了。预缺氧 池高污泥浓度内源降解的需氧量及加大的实际停留时间己经充分满足了进入 厌氧池的硝态氮降至足够低的要求， 这使得全部废水进入前部厌氧池变得可 行。
通过采用多级的缺-好氧处理单元， 充分利用了有限的碳源， 将需要的外 加碳源降低到了最低的限度，同时也在不增加池容的基础上使系统能够满足总 氮排放的需要。
厌氧池的混合液分流至四级缺-好氧处理单元中的前三个缺氧池中， 其目 的在于确保所有有限原废水碳源在缺氧池中用于反硝化，同时通过多段降解的 方式提高了总反应速率， 特别是前段的反应速率， 强化了硝化及反硝化反应， 从而使得系统出水总氮能降至最低水平。
【附图说明】
附图 1是现有技术中的 A20装置的结构示意图。
附图 2是本发明一个具体实施方式所述装置的结构示意图。
附图 3是本发明另一个具更多灵活性的具体实施方式所述装置的结构示意 图。
附图 4是本发明所对应的一个工程实施例的装置结构示意图。
附图 5为附图 4所示的设计方案的污水处理流程图。
附图 6与附图 7是上述工程实施例的处理结果示意图。
【具体实施方式】
接下来结合附图对本发明所述的一种多级的生物脱氮除磷污水处理方法 以及装置的具体实施方式做出详细说明。
附图 2所示是本具体实施方式所述装置的结构示意图。 所示的装置包括： 一厌氧池 110、多个由一缺氧池 131和一好氧池组 132成的缺 -好氧组合池 130、 一沉淀池 150、 一回流污泥浓缩池 170和一预缺氧池 190， 多个缺 -好氧组合池 130首尾相连形成多级缺-好氧处理单元 140， 以及从第一级的好氧池回流至同 级的缺氧池的回流管道 133。
本具体实施方式以四组缺 -好氧组合池 130组成的四级缺-好氧组合单元 140作为例子进行说明， 在其他的实施方式中， 可以根据工程的实际情况灵活 选择合适数目的缺-好氧组合池形成处理单元。
所述厌氧池 110的类型选自于单池或者多个串联池中的一种。
污水的进水管连接至厌氧池 110，厌氧池 110再直接连接至缺 -好氧处理单 元 140中前段的第一级或者自前段第一级起连续的多级缺氧池 131， 其中至少 第一级好氧池 132和本级缺氧池 131之间具有级内的回流管道 133， 多级缺- 好氧处理单元的最末一个好氧池 132连接至沉淀池 150， 沉淀池 150连接装置 的出水管，沉淀池 150还通过回流污泥浓缩池 170和预缺氧池 190连接至最初 的厌氧池 110形成外部回流管道， 回流污泥浓缩池 170进一步和最末一级好氧 池 132之间形成上清液回流管道。
采用上述装置处理污水的方法如下：
将污水通入厌氧池 110。
再将厌氧池 110处理过的污水通入缺-好氧处理单元 140中前段的第一级 或者自前段第一级起连续的多级缺氧池 131中， 所述缺-好氧处理单元 140由 多个缺 -好氧组合池 130首尾相连形成。
将污水全部通过最末一级好氧池 132排出至沉淀池 150。
将沉淀池 150中沉淀的污泥排入至回流污泥浓缩池 170， 沉淀池 150中的 上清液作为净化水排出装置， 而系统剩余的污泥则排至污水厂的污泥处置系 统。
将回流污泥浓缩池 170中的上清液排入最末一级好氧池 132。
将回流污泥浓缩池 170中的污泥通过过预缺氧池 190排入最初的厌氧池进 行污泥接种循环反应。
采用本实施方式所述装置和方法处理污水的特点主要在于采用了回流污 泥浓缩工艺， 使进入前部厌氧区及各反应的液体总量大大减少， 并利用多级缺 氧-好氧反应区使厌氧池的混合液可以分流到多个缺氧池中。
具体的说，采用了回流污泥浓缩工艺是指沉淀池 150通过回流污泥浓缩池 170和预缺氧池 190连接至最初的厌氧池 110形成了外部回流管道。 回流污泥 浓缩池 170的作用是将泥水进一步分离，仅将少量从沉淀池 150中回流的液体 与大部分的污泥，在预缺氧池 190中经过高污泥浓度条件下的高效强化内源降 解的反硝化过程后进入厌氧池 110， 与 100%的原废水混合后进行二段连续的 厌氧反应。实验表明，小于 30%的从沉淀池 150中回流的液体与 90%以上的污 泥能够回流到预缺氧池 190中， 由此回流污泥浓缩池 170对污泥的浓缩效果可 见一斑。
回流污泥浓缩工艺的优点在于通过增加回流污泥浓缩池 170增加系统前端 厌氧池 110中的污泥浓度， 增加了污水在厌氧池 110中的实际停留时间， 减小 了回流对系统厌氧区以及前部反应区的反应物特别是碳源有机物浓度的稀释， 并通过对回流污泥浓缩池 170中的上清液的排除以及在预缺氧池 190中的反硝 化， 控制进入厌氧池 110的硝酸盐总量。
回流污泥浓缩池 170控制了回流液进入厌氧池 110的量，一旦起泥水分离 作用的沉淀池 150底部回流量固定， 附加的回流只会增加回流的液体量， 造成 厌氧区污泥浓度及有机物的稀释。在回流混合液经过回流污泥浓縮池 170进行 泥水分离浓缩之后，预缺氧池 190对剩下的硝态氮（NO— X-N)继续进行反硝化， 所述装置依靠内碳源进行反硝化， 由于经过污泥浓缩后的混合液悬浮固体浓度 (MLSS : mixed liquor suspended solids)能达到 lOOOOmg/L以上，高浓度 MLSS 的内源呼吸作用对氧源产生巨大需求，从而强化了预缺氧池 190的反硝化和降 低硝态氮浓度的效果。在较高微生物浓度下， 内源反硝化的程度有时是非常可 观的（请参考 Kiuru & Rautiainen, 1998)。经过预缺氧池 190之后污泥的硝态氮 浓度可以控制在 l〜2mg/L， 以保证不影响厌氧池 110的运行， 同时防止磷在 预缺氧池 190中的无碳源吸附释放。至厌氧池 110的回流量的减少更确保了将 硝态氮对厌氧状态的影响降低到了最低点。
Ekama曾提出的生物除磷关键在于挥发性脂肪酸（VFA) 的获得、 普通异 养菌和聚磷菌的数量、及剩余的氧源（以上观点请参考 Ekama and Marais, 1984, Comeau et al., 1987)。 VFA的量取决于原水中的 VFA和异养菌转化为缓慢降解 有机碳 （BCOD) 产生的 VFA, 原水中的 VFA由水质而定， 而由 BCOD转化 获得的 VFA则决定于异氧微生物的数量和水力停留时间， 实际的水力停留时 间决定于原水流量和通过外部回流管道的回流量的总和。 回流量越小， 则实际 水力停留时间越长 VAF转化效应就越高。 污泥浓度的提高， 还增加了聚磷菌 的量， 与此同时， 回流的液巳去除了几乎所有的有机碳源， 回流量的增加将稀 释厌氧区的有机碳源及 VFA的浓度， 从而降低聚磷菌的 VFA吸附效应。 在大 量 VFA存在的前提下， 聚磷菌释放磷和存储 PHB (聚 -β-羟基丁酸） 效率奇迹 般的高， 从而改善了系统的除磷效率， 而且至厌氧池 110的回流量小也造成的 较大水力停留时间给厌氧池 110中的聚磷菌提供了更长的反应时间，从而更多 的利用 VFA转化为 ΡΗΒ的机会。
厌氧池 110中污泥浓度的上升和实际水力停留时间加长也强化了缓慢降解 有机碳源 （SBCOD) 水解效应， 同时使得其更易在缺氧池 131 的反硝化过程 中被降解而不被携带到好氧池 132中， 充分利用了有限碳源， 也降低了系统能 耗。回流量的减小同时也增加了各缺氧段的实际水力停留时间从而强化了缺氧 池 131的反硝化反应。缺氧池 131污泥浓度的增加不但确保了反硝化反应的强 化， 减小了 SBCOD被夹带到曝气池的几率， 也强化了内源降解反硝化反应的 速率， 从而保证了有限碳源在反硝化反应中的充分利用。
总之， 污泥回流浓縮池 170减少了整个系统的流量， 增加了污泥浓度及除 最后上清液进入段（最后一级的好氧池 132)外所有前端区域的实际停留时间， 即强化了上述的生物除磷及反硝化反应之外， 也增加了硝化菌的总量， 实际硝 化反应时间， 以及前端区域的反应物浓度， 强化了硝化反应， 保证了系统有机 氮以及氨氮的去除率。并且， 回流稀释较少带来的厌氧池 131中厌氧条件的强 化还可以抑制系统内丝状菌的生长， 改善了污泥的沉淀状态， 可控制系统的 SVI在 50左右， 保证了污泥溶度的提高。
污泥浓缩工艺减少了经过预缺氧池 190的总量，使得预缺氧池 190的污泥 浓度及停留时间都大大提高了。预缺氧池 190高污泥浓度内源降解的需氧量及 加大的实际停留时间已经充分满足了进入厌氧池 110的硝态氮降至足够低的要 求从而不必分流碳源至预缺氧池，这使得全部废水进入前部厌氧池 110变得可 行。 只将厌氧池 110设立在前端且只有一个进水口使得系统响应简单了。全部 废水进入前部增加了厌氧区 BOD5及 VFA的浓度， 强化了生物除磷效果。
并且， SBCOD有了更长的向 BCOD转化的过程， 使得其能在缺氧池 131 的反硝化过程中被充分利用而不被携带到曝气池，从而在强化了反硝化反应同 时也大大降低了好氧去有机碳源的需氧量， 优化了曝气区硝化菌的生长条件， 强化了系统的硝化反应效率。 四级缺-好氧处理单元 140也是本实施方式的重要特点之一。 第一级以外 各级的缺氧池主要作用在于将前一级好氧池硝化的硝态氮反硝化，从而形成了 系统总氮的阶段性降解， 省去了传统的大流量内回流系统， 提高了系统内各个 反应池中的实际停留时间， 降低了回流造成的缺氧区有机碳源的稀释， 充分利 用了碳源， 强化了反硝化反应。
本实施方式中， 厌氧池 110的混合液分流至四级缺-好氧处理单元 140中 的前三个缺氧池 131中，其目的在于确保所有原废水有限碳源在缺氧池 131中 用于反硝化， 而不是过早的进入好氧池 132中。这一设置不仅可以强化缺氧池 131中的反硝化作用， 而且可以通过厌氧池 110向多级缺氧池 131中的分流造 成不同环境下聚磷菌对磷的吸附， 从而使生物除磷最大化， 可促进聚磷菌的生 长。利用硝态氮作为电子受体， 聚磷菌可氧化释磷期间存储在体内的 PHB， 即 一碳二用的概念， 进一步充分利用了有限的碳源。
在其他的实施方式中， 根据进出水水质条件的不同， 厌氧池排出的液体也 可以分流至更多或者更少的缺氧池中， 同样可以达到上述的技术效果。
在多级缺-好氧处理单元 140最末几级由于的已经接近硝化 /反硝化处理的 末尾， 因此碳源要求不高， 可完全依赖内源降解进行反硝化， 因此在较佳的实 施方式中， 多级缺-好氧处理单元 140的最后一级或者自最后一级起的连续两 级或者三级缺氧池并不再与厌氧池 110连接， 以保证脱氮效果。
最末一级的缺氧池 131不与厌氧池 110直接连接的效果还在于避免原废水 中有机氮或氨氮进入反应区后端以确保出水总氮达到最低， 同时还可以选择在 该缺氧池 131中设立外加碳源设施（图中未示出）， 保证在该级的充分反硝化， 以确保离开该缺氧池 131的混合液中的硝态氮足够低，从而保证出水总氮能够 完全达标。在其他的实施方式中， 也可以根据污水的实际情况选择最末两级或 者三级的缺氧池都不直接和厌氧池连接， 以保证缺氧池的内源反硝化能够更顺 利的进行。
因此， 本装置通过采用厌氧分流加多级的缺-好氧处理单元 140， 充分利用 了有限的碳源， 将需要的外加碳源降低到了最低的限度， 同时也在不增加池容 的基础上使系统能够满足总氮排放的需要， 同时也使本系统与其系统相比， 更 为简单。 附图 3所示是本发明的另一具体实施方式。 同前一实施方式不同的是， 此 实施方式中每个好氧池 132与同一级的缺氧池 131以及以上各级缺氧池 131之 间具有内部回流管道， 其优点在于污水经过多级缺 -好氧处理单元的过程中， 可以在每一级缺氧池 131的出水处检测硝酸盐， 如果硝酸盐太低， 则通过上述 内部回流管道回流好氧出水至同一级或者以上某一级的缺氧池中循环处理， 回 流至哪一级缺氧池可以根据实际水质情况决定。尤其是第一级的好氧池和第一 级的缺氧池之间的回流管道是必须的，因为第一级缺氧池的硝酸盐类依赖于此 回流取得。
接下来给出本发明的一个工程实施例 。
本实施例是针对一个污水厂的二级生物反应方案
污水厂的进水水质条件及出水要求详见以下的表一和表二。
表一 设计进水水质 单位： mg/L
Figure imgf000011_0001
根据上述表格， 本实施例采用一种较为典型的工艺结构， 即回流浓缩、 厌 氧、 三段分流。 缺好氧外加一段内源缺 /好氧降解系统以充分利用有限碳源从 而达到系统最佳的除磷脱氮效应， 系统各段详细流程及分布见附图 4， 系统总 停留时间约为 16小时， 其中好氧反应时间 7.5小时， 缺氧反应时间 4.5小时， 厌氧反应 1小时， 总反应时为 12.5小时， 系统设计冬季最不利条件（12 C )下 的 SRT为 12天。 污水厂总厂量 100万吨， 分为 4组， 每组 25万吨， 每组 2 格， 每个 12.5万吨 /格 /天。 图二为单格反应池的详细设计及系统格局。 系统水 深为 6米， 长 150米， 宽 740米。 系统表面搅拌机 6台 (每组五台 35马力， 一 台 20马力)， 用于厌氧及缺氧反应池的污泥混合。
本实施例同时设厌氧出水分流提升泵及各一段好氧回流泵各一台（2.5 KW 及 5.5 KW) 均为低扬程过墙提高泵， 水泵的效率高， 能耗低。 由于采用了分 段处理的技术， 系统的总回流 /提升水量比现有的 A20技术大大降低了， 改善 了系统的处理能力也节省了能耗。分流各段的流量分配通过水泵的变频控制及 后端区域分流闸门的开启度来完成。采用在 6米水深区域进行微孔曝气使风机 及微孔曝气器均在其最佳工作区域工作。
本实施例的初沉池采用 45分钟短程， 沉淀去除设计， 主要去除无机颗粒 为主， 去除 30%TSS， 15%COD, 10%BOD5, 二沉池可采用周进周初之沉淀池 以便提高澄清效果， 底部污泥在 1Q 回流的浓度约为 4000mg/l， 位浓縮可达 12000mg/l， 此 0.3Q的浓缩进预缺氧池进行反硝化， 然后进入厌氧区与进来的 污水混合开始生物反应降解过程。
附图 5为附图 4所示的设计方案工程图，条件为冬季最不利水温 12°C。在 此条件下设计之泥龄 SRT为 12天。
附图 6为混合液污泥浓度 MLSS之分布，显示绝大部分区域的 MLSS可控 制在 3300mg/l， 一个合理的进行范围内。
附图 7为各污染物在各反应区域的浓度分布表。最后一行出水状态显示出 水水质远远优于国家一级 A排放标准之要求， 充分体现了本设计方案的可靠 性。
以上所述仅是本发明的优选实施方式， 应当指出， 对于本技术领域的普通 技术人员， 在不脱离本发明原理的前提下， 还可以做出若干改进和润饰， 这些 改进和润饰也应视为本发明的保护范围。

Claims

权 利 要 求 书
1. 一种多级的生物脱氮除磷污水处理方法， 包括：
将污水通入厌氧池；
再将厌氧池处理过的污水通入缺 -好氧处理单元中前段的第一级或者自前 段第一级起连续的多级缺氧池中，所述缺-好氧处理单元由多个缺-好氧组合 池首尾相连形成， 其中至少包括从第一级的好氧池回流至同级的缺氧池的 回流管道；
将污水全部通过最末一级好氧池排出至沉淀池；
将沉淀后的污泥排入至回流污泥浓缩池， 沉淀池中的上清液作为净化水排 出装置；
将回流污泥浓縮池中的上清液排入最末一级好氧池；
将回流污泥浓縮池中的污泥通过过预缺氧池排入最初的厌氧池进行循环处 理。
2. 根据权利要求 1所述的多级的生物脱氮除磷污水处理方法， 其特征在于， 在污水经过多级缺 -好氧处理单元的过程中， 在每一级的缺氧池测定其硝酸 盐类的浓度， 如该池中的硝酸浓度不够， 则将本级或以下某一级的好氧池 出水回流至此级缺氧池中循环处理， 以强化系统的反硝化能力。
3. 根据权利要求 1所述的多级的生物脱氮除磷污水处理方法， 其特征在于， 污水从厌氧池排出后， 仅通入缺-好氧处理单元中前段的第一级或者自前段 第一级起连续的多级缺氧池中， 而并不通入最后一级或者自最后一级起的 连续两级或者三级缺氧池中。
4. 一种多级的生物脱氮除磷污水处理装置， 其特征在于， 包括一厌氧池、 多 个由一缺氧池和一好氧池组成的缺-好氧组合池、 一沉淀池、 一回流污泥浓 缩池和一预缺氧池， 多个缺好氧组合池首尾相连形成多级缺 -好氧处理单 元， 污水的进水管连接至厌氧池， 厌氧池再直接连接至缺-好氧处理单元中 前段的第一级或者自前段第一级起连续的多级缺氧池， 多级缺 -好氧处理单 元的最末一个好氧池连接至沉淀池， 沉淀池连接装置的出水管， 沉淀池还 通过回流污泥浓縮池和预缺氧池连接至厌氧池形成外部回流管道， 回流污 泥浓缩池进一步和最末一级好氧池之间形成上清液回流管道。
5. 根据权利要求 4所述的多级的生物脱氮除磷污水处理装置， 其特征在于， 多级缺-好氧处理单元的最后一级或者自最后一级起的连续两级或者三级 缺氧池并不与厌氧池连接。
6. 根据权利要求 4所述的多级的生物脱氮除磷污水处理装置， 其特征在于， 每个好氧池与同一级的缺氧池以及以上各级的缺氧池之间具有内部回流管 道。
7. 根据权利要求 4所述的多级的生物脱氮除磷污水处理装置， 其特征在于， 所述厌氧池的类型选自于单池或者多个串联池中的一种。
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