CN102874980B - Method for processing wastewater by utilizing combination of granular sludge and dynamic film - Google Patents
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Abstract
Description
（一）技术领域 (1) Technical field
本发明涉及一种颗粒污泥与动态膜组合处理废水的方法，可去除有机物、氮等多种污染物，适用于处理工业废水和城市污水。The invention relates to a method for treating wastewater by combining granular sludge and a dynamic membrane, which can remove various pollutants such as organic matter and nitrogen, and is suitable for treating industrial wastewater and urban sewage.
（二）背景技术 (2) Background technology
动态膜生物反应器(Dynamic Membrane Bioreaetor，DMBR)是利用运行过程中在网膜表面形成的污泥层，将污泥截留在反应器内从而实现净化污水的一种工艺。该工艺具有膜生物反应器（MBR）的优点，无需常规污水生物处理工艺的沉淀池和污泥回流系统，同时大幅降低了膜组件的造价，膜污染更容易得到有效控制。动态膜制备简单，所使用的基膜一般为廉价易得的无纺布，筛网等，当微生物及其代谢产物在基膜上沉积成膜时就形成了动态膜。动态膜生物反应器具有设备简单、操作简便、处理效果较好、费用较低等优点，其缺点是膜阻力上升速度快，过滤周期短，膜污染物不易被清洗去除，且出水水质不够稳定。从结构上，动态膜可分为滤饼屡、凝胶层和膜基质。凝胶层与膜基质的结合比较强，有较好的截留能力；滤饼层主要由污泥絮团组成，结构松散，与底层的结合强度很弱。动态膜的形成及其性能受很多因素的影响，如曝气强度，错流流速，出水水头，污泥浓度以及进水水质等，所以动态膜的成膜时间长也是其缺点之一。Dynamic membrane bioreactor (Dynamic Membrane Bioreaetor, DMBR) is a process that uses the sludge layer formed on the surface of the omentum during operation to trap the sludge in the reactor to purify sewage. This process has the advantages of a membrane bioreactor (MBR), without the need for sedimentation tanks and sludge return systems in conventional sewage biological treatment processes, and at the same time greatly reduces the cost of membrane components, making it easier to effectively control membrane fouling. The preparation of the dynamic membrane is simple, and the base membrane used is generally cheap and easy-to-obtain non-woven fabrics, screens, etc., and the dynamic membrane is formed when microorganisms and their metabolites are deposited on the base membrane to form a film. The dynamic membrane bioreactor has the advantages of simple equipment, easy operation, good treatment effect, and low cost. Its disadvantages are that the membrane resistance rises quickly, the filtration cycle is short, the membrane pollutants are not easy to be cleaned and removed, and the effluent quality is not stable enough. Structurally, dynamic membranes can be divided into filter cake, gel layer and membrane matrix. The gel layer has a strong combination with the membrane matrix and has a good retention capacity; the filter cake layer is mainly composed of sludge flocs with a loose structure and a weak combination with the bottom layer. The formation and performance of dynamic membranes are affected by many factors, such as aeration intensity, cross-flow velocity, outlet head, sludge concentration, and influent water quality, so the long film-forming time of dynamic membranes is also one of its disadvantages.
在动态膜生物反应器中，生物污泥对污染物去除起主要作用。通过对国内外动态膜生物反应器的应用经验总结发现，出水水质不稳定是该技术发展受阻的重要因素。出水水质不稳定主要包括浊度的变化比较大，容易出现污泥流失的情况，而污泥的流失则会导致反应器内污泥浓度下降，处理性能降低。In dynamic membrane bioreactors, biological sludge plays a major role in pollutant removal. Through summarizing the application experience of dynamic membrane bioreactors at home and abroad, it is found that the unstable effluent quality is an important factor hindering the development of this technology. Unstable effluent quality mainly includes relatively large changes in turbidity, which is prone to sludge loss, and the loss of sludge will lead to a decrease in the sludge concentration in the reactor and a decrease in treatment performance.
好氧颗粒污泥技术是在一定反应器内和操作条件下通过絮体污泥培养为一定粒径的污泥颗粒并实现处理污水的生物技术。该技术研究主要是在间歇式运行的序批式活性污泥反应器中进行，有时需要在培养过程中添加污泥载体。有研究指出，在间歇式运行的反应器中，较短的水力停留时间及较大的水流剪切作用有助于形成好氧颗粒污泥，沉淀时间是影响好氧颗粒菌落的主要因素。Aerobic granular sludge technology is a biological technology that cultivates sludge particles of a certain size through floc sludge in a certain reactor and operating conditions and realizes sewage treatment. The technical research is mainly carried out in the sequenced batch activated sludge reactor operated intermittently, and sometimes it is necessary to add sludge carrier during the cultivation process. Some studies have pointed out that in batch-run reactors, shorter hydraulic retention time and greater water flow shear are conducive to the formation of aerobic granular sludge, and settling time is the main factor affecting aerobic granular colonies.
好氧颗粒污泥反应器可采用不同接种污泥，包括絮状活性污泥和厌氧颗粒污泥。直接采用厌氧颗粒污泥进行驯化的方法简便且成功率高；而以普通絮状活性污泥为接种污泥，启动时间长，控制难度较大。有研究者以厌氧颗粒污泥为接种污泥在SBR反应器中培养出好氧颗粒污泥，而以普通活性污泥为接种污泥未获成功。显然，好氧颗粒污泥存在培养困难、启动速度慢的缺陷，而且一般应用于间歇式工艺中。The aerobic granular sludge reactor can use different seed sludge, including flocculent activated sludge and anaerobic granular sludge. The method of directly using anaerobic granular sludge for domestication is simple and has a high success rate; however, using ordinary flocculent activated sludge as inoculation sludge takes a long time to start and is difficult to control. Some researchers used anaerobic granular sludge as inoculation sludge to cultivate aerobic granular sludge in SBR reactor, but failed to use ordinary activated sludge as inoculation sludge. Obviously, aerobic granular sludge has the defects of difficult cultivation and slow start-up, and is generally used in batch processes.
为了能够解决颗粒污泥和动态膜各自的缺陷，并实现优势互补，本项目拟将动态膜技术引入颗粒污泥处理技术中，形成一种新型的动态膜与颗粒污泥的组合工艺技术。In order to solve the respective defects of granular sludge and dynamic membrane and realize complementary advantages, this project intends to introduce dynamic membrane technology into granular sludge treatment technology to form a new combined process technology of dynamic membrane and granular sludge.
动态膜技术与颗粒污泥组合技术，利用动态膜对颗粒物的截留作用，能够有效保证反应器中的生物量，并实现连续运行；利用颗粒污泥大的颗粒粒径更能有效地被截留在动态膜反应器内，避免污泥流失，实现稳定运行。此外，由于颗粒污泥具有较大的粒径，对氧的穿透具有适当的抵制作用，即使颗粒外部有一定的氧浓度，内部仍然会形成缺氧的微环境，颗粒污泥可以创造不同的环境，使硝化细菌和反硝化细菌具备各自适合的空间，能够同时发挥作用，有利于同时硝化和反硝化的进行。因而，颗粒污泥—动态膜组合工艺在去除废水中的有机物和硝化反硝脱氮方面具有巨大的潜力。The combination technology of dynamic membrane technology and granular sludge can effectively ensure the biomass in the reactor and realize continuous operation by using the interception effect of dynamic membrane on particulate matter; the large particle size of granular sludge can be more effectively trapped in the In the dynamic membrane reactor, sludge loss is avoided and stable operation is achieved. In addition, due to the large particle size of the granular sludge, it has an appropriate resistance to the penetration of oxygen. Even if there is a certain oxygen concentration outside the particle, an anoxic microenvironment will still be formed inside, and the granular sludge can create different Environment, so that nitrifying bacteria and denitrifying bacteria have their own suitable space, and can play a role at the same time, which is conducive to the simultaneous nitrification and denitrification. Therefore, the granular sludge-dynamic membrane combination process has great potential in the removal of organic matter and nitrification and denitrification in wastewater.
（三）发明内容 (3) Contents of the invention
本发明目的是提供一种将动态膜与活性污泥结合处理废水的方法，解决现有动态膜技术污泥流失、处理不稳定和颗粒污泥启动慢且一般只能间歇式运行的问题，实现高效处理污水的新生物处理技术。The purpose of the present invention is to provide a method for treating wastewater by combining dynamic membrane and activated sludge, so as to solve the problems of existing dynamic membrane technology, such as sludge loss, unstable treatment, and slow start-up of granular sludge, which generally can only be operated intermittently. New biological treatment technology for efficient treatment of sewage.
本发明采用的技术方案是：The technical scheme adopted in the present invention is:
一种利用颗粒污泥与动态膜结合处理废水的方法，所述方法采用动态膜生物反应系统进行，通过动态膜将污泥截留在动态膜生物反应器内高效降解污染物，同时在反应器内投加高分子有机物帮助反应器内的污泥颗粒化；透过动态膜的污泥经沉淀池沉淀后回流到反应器内，以维持反应器内稳定的颗粒污泥性能，所述动态膜生物反应系统由动态膜生物反应器和沉淀池串联构成，所述动态膜生物反应器两端分别设有进水口和出水口，所述动态膜生物反应器底部设有微孔曝气器和污泥回流入口，所述微孔曝气器通过管路与鼓风机连通，所述进水口通过进水泵与废水池连通，所述出水口处设有出水管，所述出水管靠近动态膜生物反应器一端设有动态膜，所述动态膜通过法兰固定于出水管壁上，所述出水管另一端与沉淀池连通，所述沉淀池顶部设有排水口、底部最低处设有污泥回流出口，所述污泥回流出口与污泥回流入口通过污泥回流泵连通；所述废水处理方法为：启动进水泵，将废水池中的废水泵入动态膜生物反应器内至废水量为反应器有效容积的1/2时停止进水，所述废水COD值为 600~5000mg/L、氨氮浓度为 30~1000 mg/L、pH 7.5~11.0，将污泥浓度为3.5g/L反应器容积的絮体污泥接种至动态膜生物反应器，开启鼓风机曝气，使污泥与废水混合液的溶解氧DO值不低于3mg/L；当反应器内废水COD值低于200mg/L时，开启进水泵，控制废水流量为0.21L/h、水力停留时间为2d；当沉淀池的排水口开始排水时，开启污泥回流泵并且控制污泥回流泵运行时间为每隔2h运行10min，流量为0.5L/h；所述动态膜生物反应器启动1~3天后投加一次高分子有机物a，然后每隔3~8天投加一次，每次投加的高分子有机物a与接种的絮体污泥质量比为0.01~ 0.05:1；每天监测排水口出水的COD值，调节进水流量和水力停留时间，使出水COD值小于100mg/L、氨氮浓度小于15 mg/L时，废水达标排放；所述高分子有机物a为聚丙烯酰胺、壳聚糖或有机胺盐，优选聚丙烯酰胺（PAM）。A method for treating wastewater by combining granular sludge and dynamic membranes. The method is carried out using a dynamic membrane bioreactor system, and the sludge is trapped in a dynamic membrane bioreactor through a dynamic membrane to efficiently degrade pollutants. Adding polymeric organic matter helps the sludge in the reactor to granulate; the sludge that passes through the dynamic membrane is sedimented in the sedimentation tank and then flows back into the reactor to maintain the stable performance of the granular sludge in the reactor. The dynamic membrane biological The reaction system consists of a dynamic membrane bioreactor and a sedimentation tank connected in series. The two ends of the dynamic membrane bioreactor are respectively provided with a water inlet and a water outlet. The bottom of the dynamic membrane bioreactor is provided with a microporous aerator and sludge The backflow inlet, the microporous aerator communicates with the blower through the pipeline, the water inlet communicates with the waste water tank through the water inlet pump, and the water outlet is provided with an outlet pipe, and the outlet pipe is close to one end of the dynamic membrane bioreactor A dynamic membrane is provided, and the dynamic membrane is fixed on the wall of the water outlet pipe through a flange. The other end of the water outlet pipe is connected to the sedimentation tank. The top of the sedimentation tank is provided with a drain outlet, and the lowest part of the bottom is provided with a sludge return outlet. The sludge reflux outlet is connected to the sludge reflux inlet through the sludge reflux pump; the waste water treatment method is: start the water inlet pump, and pump the waste water in the waste water pool into the dynamic membrane bioreactor until the amount of waste water reaches the effective level of the reactor. When the volume is 1/2, the water intake is stopped, the COD value of the wastewater is 600~5000mg/L, the ammonia nitrogen concentration is 30~1000 mg/L, the pH is 7.5~11.0, and the sludge concentration is 3.5g/L. The floc sludge is inoculated into the dynamic membrane bioreactor, and the blower is turned on for aeration, so that the dissolved oxygen DO value of the sludge and wastewater mixture is not lower than 3mg/L; when the COD value of the wastewater in the reactor is lower than 200mg/L, Turn on the inlet pump, control the waste water flow rate to 0.21L/h, and the hydraulic retention time to 2d; when the outlet of the sedimentation tank starts to drain, turn on the sludge return pump and control the operation time of the sludge return pump to run for 10 minutes every 2 hours, and the flow rate 0.5L/h; the dynamic membrane bioreactor is added once 1-3 days after the start-up of high-molecular organic matter a, and then once every 3-8 days. The mass ratio of solid sludge is 0.01~0.05:1; the COD value of the outlet water is monitored every day, and the influent flow rate and hydraulic retention time are adjusted to make the effluent COD value less than 100mg/L and the ammonia nitrogen concentration less than 15 mg/L, the wastewater reaches the standard Emission; the polymeric organic compound a is polyacrylamide, chitosan or organic amine salt, preferably polyacrylamide (PAM).
进一步，所述动态膜为尼龙网，网孔孔径为40~200目，动态膜可以用网状材料构建而成，材质为有机高分子材料如尼龙等、无机材料如陶瓷等和金属材料如不锈钢等，筛网设置在装置中上部，采用柔性连接，便于更换筛网及维护。所述的动态膜的有效过水面积为0.01~0.05m2/(m3.d)。Further, the dynamic membrane is a nylon mesh with a mesh aperture of 40 to 200 meshes. The dynamic membrane can be constructed of a mesh material, and the material is an organic polymer material such as nylon, an inorganic material such as ceramics, and a metal material such as stainless steel. etc. The screen is set in the middle and upper part of the device, with flexible connection, which is convenient for screen replacement and maintenance. The effective water passing area of the dynamic membrane is 0.01-0.05m 2 /(m 3 .d).
进一步，所述沉淀池的上半部分为方形池，下半部分为倒锥形池，沉淀下来的污泥回流到反应器。Further, the upper half of the sedimentation tank is a square tank, and the lower part is an inverted conical tank, and the settled sludge is returned to the reactor.
进一步，所述的絮体污泥接种到生物反应器之前还包括混入高分子有机物如聚丙烯酰胺、壳聚糖、有机胺盐等，通过连续运行使得絮体污泥在该反应器内形成颗粒污泥，所述高分子有机物投加方式为：将絮体污泥与高分子有机物b混合，100rpm搅拌2min后接种至动态膜生物反应器，所述高分子有机物b与絮体污泥质量比为0.03:1，所述高分子有机物b为聚丙烯酰胺或壳聚糖，优选聚丙烯酰胺。Further, before the floc sludge is inoculated into the bioreactor, it also includes mixing high-molecular organic matter such as polyacrylamide, chitosan, organic amine salt, etc., through continuous operation, the floc sludge forms particles in the reactor Sludge, the way of adding the high molecular organic matter is: mixing the floc sludge with the high molecular organic matter b, stirring at 100rpm for 2min, and then inoculating it into the dynamic membrane bioreactor, the mass ratio of the high molecular organic matter b to the floc sludge is 0.03:1, and the polymeric organic compound b is polyacrylamide or chitosan, preferably polyacrylamide.
进一步，所述絮体污泥为纯菌种、活性污泥、厌氧污泥或剩余污泥中的一种或两种以上的混合，所述剩余污泥为城市污水处理厂或工业废水处理厂排出来的多余生物污泥。Further, the floc sludge is a mixture of one or more of pure bacteria, activated sludge, anaerobic sludge or excess sludge, and the excess sludge is treated by urban sewage treatment plants or industrial wastewater Excess biological sludge discharged from the factory.
进一步，优选所述动态膜生物反应器运行过程中间歇补充高分子有机物的方法为，动态膜生物反应器启动2天后投加一次高分子有机物a，然后每隔3~5天投加一次，每次投加的高分子有机物a与接种的絮体污泥质量比为0.01~0.05:1，所述高分子有机物a为聚丙烯酰胺或壳聚糖，优选聚丙烯酰胺。Further, it is preferred that the method of intermittently replenishing high-molecular organic matter during the operation of the dynamic membrane bioreactor is to add high-molecular organic matter a once 2 days after the dynamic membrane bioreactor starts, and then dosing once every 3 to 5 days. The mass ratio of the polymeric organic matter a to be added to the inoculated floc sludge is 0.01-0.05:1, and the polymeric organic matter a is polyacrylamide or chitosan, preferably polyacrylamide.
所述的动态膜生物反应器内部可设置导引水上下流的导流筒，所述导流筒外壁与反应器内壁构成回流腔，以强化污泥、水的流态，微孔曝气器设置在导流筒底部。The interior of the dynamic membrane bioreactor can be provided with a diversion cylinder to guide the water to flow up and down. The outer wall of the diversion cylinder and the inner wall of the reactor form a return cavity to strengthen the flow state of sludge and water. The microporous aerator is set at the bottom of the deflector.
所述的沉淀池根据水处理规模可采用斜板沉淀池、竖流式沉淀和辐流式沉淀池。According to the scale of water treatment, the sedimentation tank can adopt inclined plate sedimentation tank, vertical flow sedimentation and radial flow sedimentation tank.
所述高分子有机物a和高分子有机物b均为高分子有机物，为便于区分不同步骤所加入的高分子有机物量不同而命名，字母本身没有含义。The high-molecular organic matter a and the high-molecular organic matter b are both high-molecular organic matter, which are named for the convenience of distinguishing the different amounts of high-molecular organic matter added in different steps, and the letters themselves have no meaning.
本发明方法获得颗粒污泥浓度达到10g/L以上，而现有技术中关于活性污泥好氧生物处理的污泥浓度有：韩彪, 张萍, 张维维, 李骋,胡雅兰, 王启明, 鄢恒宇. 厌氧-好氧-物化工艺处理淀粉废水的工程实例. 环境科学与技术, 2010,33(12): 25-27；张立秋, 黄桂强, 石云峰, 肖桃生. 生化法处理变性淀粉废水工程实例. 工业用水与废水, 2005, 36(3): 71-72；廖鑫凯, 李清彪, 陈文谋,邓旭, 卢英华, 何宁. 多阶段曝气SBR法处理淀粉废水. 水处理技术, 2005,31(10):48-51，现有技术所获得的污泥浓度在2~5g/L。The concentration of granular sludge obtained by the method of the present invention reaches above 10g/L, while the sludge concentration of activated sludge aerobic biological treatment in the prior art includes: Han Biao, Zhang Ping, Zhang Weiwei, Li Cheng, Hu Yalan, Wang Qiming, Yan Hengyu. An engineering example of anaerobic-aerobic-physicochemical treatment of starch wastewater. Environmental Science and Technology, 2010,33(12): 25-27; Zhang Liqiu, Huang Guiqiang, Shi Yunfeng, Xiao Taosheng. Engineering examples of biochemical treatment of modified starch wastewater. Industrial Water and Wastewater, 2005, 36(3): 71-72; Liao Xinkai, Li Qingbiao, Chen Wenmou, Deng Xu, Lu Yinghua, He Ning. Multi-stage aeration SBR method for starch wastewater treatment. Water Treatment Technology, 2005,31(10) : 48-51, the obtained sludge concentration of prior art is at 2～5g/L.
与现有技术相比，本发明的有益效果主要体现在：本发明动态膜生物处理反应系统的结构简单，易操作管理，利用本发明处理废水的方法可以获得10g/L以上的污泥浓度（现有活性污泥好氧生物处理技术的污泥浓度一般在2~5g/L），处理负荷高，克服颗粒污泥和动态膜单独技术的缺陷，污泥不流失，并连续运行，出水COD和氨氮分别小于100mg/L和15mg/L，COD和氨氮去除率分别达到了85%和90%以上，能够实现去除有机物和脱氮功能。Compared with the prior art, the beneficial effects of the present invention are mainly reflected in: the structure of the dynamic membrane biological treatment reaction system of the present invention is simple, easy to operate and manage, and the sludge concentration above 10g/L can be obtained by using the method for treating wastewater of the present invention ( The sludge concentration of the existing activated sludge aerobic biological treatment technology is generally 2~5g/L), the treatment load is high, and the defects of the separate technology of granular sludge and dynamic membrane are overcome, the sludge is not lost, and it runs continuously, and the effluent COD and ammonia nitrogen are less than 100mg/L and 15mg/L respectively, and the COD and ammonia nitrogen removal rates have reached 85% and 90% respectively, which can realize the functions of removing organic matter and denitrification.
（四）附图说明 (4) Description of drawings
图1 动态膜生物反应系统结构示意图：1-动态膜生物反应器，2-沉淀池，3-进水口，4-出水口，5-微孔曝气器，6-鼓风机，7-进水泵，8-废水池，9-动态膜，10-排水口，11-污泥回流出口，12-污泥回流入口，13-污泥回流泵。Figure 1 Schematic diagram of the dynamic membrane bioreaction system structure: 1-dynamic membrane bioreactor, 2-sedimentation tank, 3-water inlet, 4-water outlet, 5-microporous aerator, 6-blower, 7-inlet pump, 8-Wastewater pool, 9-Dynamic membrane, 10-Outlet, 11-Sludge return outlet, 12-Sludge return inlet, 13-Sludge return pump.
（五）具体实施方式(5) Specific implementation methods
下面结合具体实施例对本发明进行进一步描述，但本发明的保护范围并不仅限于此：The present invention is further described below in conjunction with specific embodiment, but protection scope of the present invention is not limited thereto:
实施例1：Example 1:
所述动态膜生物反应系统由动态膜生物反应器1（有效容积为10L（200 mm×50mm×1200mm））和沉淀池2串联构成，所述动态膜生物反应器1两端设有进水口3和出水口4，底部设有微孔曝气器5和污泥回流入口12，所述微孔曝气器5通过管路与鼓风机6连通，所述进水口3通过进水泵7与废水池8连通，所述出水口4处设有出水管，所述出水管靠近动态膜生物反应器1一端设有动态膜9，所述动态膜9通过法兰固定于出水管壁上，所述出水管另一端与沉淀池2连通，所述沉淀池2顶部设有排水口10、底部设有污泥回流出口11，所述污泥回流出口11与污泥回流入口12通过污泥回流泵13连通；所述微孔曝气器为陶瓷微孔曝气器，所述沉淀池的上半部分为方形池，下半部分为倒锥形池。The dynamic membrane bioreactor system is composed of a dynamic membrane bioreactor 1 (with an effective volume of 10L (200mm×50mm×1200mm)) and a sedimentation tank 2 connected in series, and the two ends of the dynamic membrane bioreactor 1 are provided with water inlets 3 and water outlet 4, the bottom is provided with a microporous aerator 5 and a sludge return inlet 12, the microporous aerator 5 is communicated with the blower 6 through a pipeline, and the water inlet 3 is connected to the waste water tank 8 through a water inlet pump 7 Connected, the water outlet 4 is provided with an outlet pipe, and the end of the outlet pipe near the dynamic membrane bioreactor 1 is provided with a dynamic membrane 9, and the dynamic membrane 9 is fixed on the wall of the outlet pipe through a flange, and the outlet pipe The other end is communicated with the sedimentation tank 2, the top of the sedimentation tank 2 is provided with a drain outlet 10, and the bottom is provided with a sludge return outlet 11, and the sludge return outlet 11 is communicated with the sludge return inlet 12 through a sludge return pump 13; The microporous aerator is a ceramic microporous aerator, the upper half of the sedimentation tank is a square tank, and the lower part is an inverted conical tank.
动态膜反应器有效容积为10L（200 mm×50mm×1200mm），动态膜采用了120目尼龙网固定在2块100 mm×100mm的方形法兰之间，尼龙网过水尺寸为50 mm×50mm，尼龙网将颗粒污泥拦截在反应器内，水由尼龙网一面透过后从另一面流出，动态膜上端距离出水口20mm，出水口设置在反应器内液面下30mm；陶瓷微孔曝气器距离动态膜生物反应器底部20mm，主要功能是供给反应器空气；反应器出水流入后续设置的平流沉淀池，沉淀池尺寸为200 mm×50mm×600mm，沉淀池上设置排水口，排水口距离沉淀池顶端为200mm。The effective volume of the dynamic membrane reactor is 10L (200mm×50mm×1200mm). The dynamic membrane is fixed between two 100mm×100mm square flanges with a 120-mesh nylon mesh. The size of the nylon mesh is 50mm×50mm. , the nylon net intercepts the granular sludge in the reactor, and the water flows out from the other side after passing through one side of the nylon net. The upper end of the dynamic membrane is 20mm away from the water outlet, and the water outlet is set 30mm below the liquid level in the reactor; ceramic microporous aeration The device is 20mm away from the bottom of the dynamic membrane bioreactor, and its main function is to supply air to the reactor; the effluent from the reactor flows into the subsequent advection sedimentation tank. The size of the sedimentation tank is 200mm×50mm×600mm. The top of the pool is 200mm.
所述废水处理方法为：启动进水泵，将废水池中的废水泵入动态膜生物反应器内至废水量为5L时停止进水，所述废水COD值为 800mg/L、TP 6.8 mg/L、氨氮浓度为 90 mg/L、pH 8.5，将活性污泥与聚丙烯酰胺以质量比1:0.03混合后100rpm搅拌2min后，将活性污泥浓度3.5g/L反应器容积的活性污泥与聚丙烯酰胺混合物接种至动态膜生物反应器，开启微孔曝气器使污泥与废水混合液的DO值不低于3mg/L，一直曝气，当反应器内废水COD值低于200mg/L时，开启进水泵，废水流量为0.21L/h，水力停留时间为2d，当沉淀池的排水口开始排水时，开启污泥回流泵间歇运行，并控制污泥回流泵运行时间为每隔2h运行10min，流量为0.5L/h；动态膜生物反应器运行过程中间歇补充聚丙烯酰胺，动态膜生物反应器启动2天后投加一次聚丙烯酰胺，然后每隔3天投加一次，每次投加的聚丙烯酰胺与接种的活性污泥质量比为0.015:1，每天监测排水口出水的COD值，调整进水流量和水力停留时间，使出水COD值小于100mg/L、氨氮浓度小于15 mg/L时，废水达标排放。The waste water treatment method is as follows: start the water inlet pump, pump the waste water in the waste water pool into the dynamic membrane bioreactor until the waste water volume is 5L, stop the water inflow, the waste water COD value is 800 mg/L, TP 6.8 mg/L , the concentration of ammonia nitrogen is 90 mg/L, and the pH is 8.5. After mixing the activated sludge and polyacrylamide at a mass ratio of 1:0.03 and stirring at 100 rpm for 2 minutes, the activated sludge with an activated sludge concentration of 3.5g/L and a reactor volume of Inoculate the polyacrylamide mixture into the dynamic membrane bioreactor, turn on the microporous aerator to make the DO value of the sludge and wastewater mixture not less than 3mg/L, and keep aerating, when the COD value of the wastewater in the reactor is lower than 200mg/L When L, turn on the inlet pump, the waste water flow rate is 0.21L/h, and the hydraulic retention time is 2d. When the outlet of the sedimentation tank starts to discharge water, start the sludge return pump to run intermittently, and control the operation time of the sludge return pump to be every 2h running 10min, the flow rate is 0.5L/h; polyacrylamide is intermittently supplemented during the operation of the dynamic membrane bioreactor, polyacrylamide is added once 2 days after the dynamic membrane bioreactor is started, and then once every 3 days, every The mass ratio of the polyacrylamide to the inoculated activated sludge is 0.015:1, and the COD value of the outlet water is monitored every day, and the influent flow and hydraulic retention time are adjusted so that the COD value of the effluent is less than 100mg/L and the concentration of ammonia nitrogen is less than When the concentration is 15 mg/L, the wastewater reaches the standard discharge.
动态膜反应器运行过程中，根据COD处理效率的提高进水流量、缩小水力停留时间，当COD去除率达到85%时，流量提高50%；当COD处理负荷大于1.5kg/(m3.d) 时，流量提高30%。During the operation of the dynamic membrane reactor, according to the improvement of the COD treatment efficiency to increase the influent flow rate and reduce the hydraulic retention time, when the COD removal rate reaches 85%, the flow rate increases by 50%; when the COD treatment load is greater than 1.5kg/(m 3 .d ), flow increases by 30%.
经过4个月的启动及运行，污泥浓度达到了11.2g/L，污泥颗粒平均粒径达到了0.65 mm；当COD的处理负荷达到3.6kgCOD/(m3.d)时，出水COD和氨氮分别小于100mg/L和15mg/L，COD和氨氮去除率分别达到了85%和90%以上。After 4 months of start-up and operation, the sludge concentration reached 11.2g/L, and the average particle size of sludge particles reached 0.65 mm; when the COD treatment load reached 3.6kgCOD/(m 3 .d), the effluent COD and The ammonia nitrogen is less than 100mg/L and 15mg/L respectively, and the removal rates of COD and ammonia nitrogen are over 85% and 90% respectively.
然而，没有形成好氧颗粒污泥的普通活性污泥工艺处理相同的废水时，污泥浓度只能维持在6.5g/L以下，否则出水浑浊、污泥流失。正常运行时，当COD的处理负荷达到1.5kgCOD/(m3.d)时，出水COD和氨氮分别小于150mg/L和25mg/L，COD和氨氮去除率分别达到了85%和90%以上。However, when the ordinary activated sludge process that does not form aerobic granular sludge treats the same wastewater, the sludge concentration can only be maintained below 6.5g/L, otherwise the effluent will be turbid and the sludge will be lost. During normal operation, when the COD treatment load reaches 1.5kgCOD/(m 3 .d), the effluent COD and ammonia nitrogen are less than 150mg/L and 25mg/L respectively, and the COD and ammonia nitrogen removal rates reach 85% and 90% respectively.
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