CN204281406U - A kind of membrane bioreactor based on fouling membrane in-situ control - Google Patents
A kind of membrane bioreactor based on fouling membrane in-situ control Download PDFInfo
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- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 28
- 239000000701 coagulant Substances 0.000 claims description 27
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 12
- 239000011148 porous material Substances 0.000 claims description 6
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
技术领域 technical field
本实用新型涉及污水处理，尤其涉及污水处理中的一种基于膜污染原位控制的膜生物反应器。 The utility model relates to sewage treatment, in particular to a membrane bioreactor based on in-situ control of membrane pollution in sewage treatment.
背景技术 Background technique
膜生物反应器将生物处理与膜分离相结合，实现水力停留时间与污泥龄的分离控制，可大大提高反应器内微生物量，有利于特定功能菌的生长和污染物的去除。具有占地面积小，出水水质稳定，容易实现自动控制等优势，在水和废水处理领域的应用日益增多。膜作为膜生物反应器的核心部分，其所处环境十分恶劣。由于生物反应器内存在高浓度的悬浮物、有机物和微生物及胞外分泌物，导致膜的不可逆污染普遍存在，严重影响了膜生物反应器的应用。因此，如何在强化污染物去除效果的同时，控制膜污染成为膜生物反应器发展的关键瓶颈。 Membrane bioreactor combines biological treatment and membrane separation to realize the separation control of hydraulic retention time and sludge age, which can greatly increase the microbial biomass in the reactor, which is conducive to the growth of specific functional bacteria and the removal of pollutants. It has the advantages of small footprint, stable effluent quality, and easy automatic control. It is increasingly used in the field of water and wastewater treatment. Membrane is the core part of membrane bioreactor, and its environment is very harsh. Due to the high concentration of suspended solids, organic matter, microorganisms and extracellular secretions in the bioreactor, the irreversible fouling of the membrane is common, which seriously affects the application of the membrane bioreactor. Therefore, how to control membrane fouling while strengthening the pollutant removal effect has become a key bottleneck in the development of membrane bioreactors.
为强化膜生物反应器的处理效果和控制膜污染，可采用投加填料的方法增加微生物量，流化态的填料还可清洗膜表面的污染层，降低膜污染。国内相关的主要专利有：环流式膜生物反应器废水处理设备和废水处理方法（授权公告号CN 100429160C），主要通过固定填料上的工程菌或酶制剂去除污染物，同时利用膜进行固液分离；一种研究填料对膜污染改善的膜生物反应器系统和量化测试方法及应用（授权公告号CN 102642920B），主要通过三组平行运行的膜生物反应器来评价不同悬浮填料对膜污染的影响，为设计新型填料提供基础；投加填料的流化床型膜-生物反应器及水处理方法（授权公告号CN 1164507C），通过导流装置将反应池分隔为升流区和降流区，膜组件置于升流区内，通过曝气使填料流动，控制膜污染，强化处理效果；控制膜污染的一种膜生物反应器中混合液性质调控方法（公开号CN 1600705A），主要通过投加臭氧使反应器内混合液性质的改变从而控制膜污染；一种控制膜生物反应器中膜污染的新方法（公开号CN 102276055A），通过在反应器内投加填料作为生物膜的载体，优化曝气方式控制微生物代谢，从而减缓膜污染，一种平板陶瓷超滤膜生物反应器（公开号CN 103304021A），通过利用平板陶瓷膜和固定的FSB 生物载体对传统膜生物反应器改造，使微生物絮体附着在生物填料表面，有效缓解膜污染。 In order to enhance the treatment effect of the membrane bioreactor and control membrane fouling, the method of adding fillers can be used to increase the amount of microorganisms. The fluidized fillers can also clean the fouling layer on the membrane surface and reduce membrane fouling. The main domestic related patents are: circulation membrane bioreactor wastewater treatment equipment and wastewater treatment method (authorized announcement number CN 100429160C), which mainly removes pollutants through engineering bacteria or enzyme preparations on fixed packing, and at the same time uses membranes for solid-liquid separation ; A membrane bioreactor system and quantitative test method and application for research on the improvement of membrane fouling by fillers (authorized announcement number CN 102642920B), mainly through three sets of membrane bioreactors running in parallel to evaluate the impact of different suspended fillers on membrane fouling , to provide a basis for the design of new fillers; the fluidized bed membrane-bioreactor and water treatment method with fillers added (authorized announcement number CN 1164507C), the reaction pool is divided into an upflow zone and a downflow zone through a diversion device, The membrane module is placed in the upflow area, and the filler is flowed through aeration to control the membrane fouling and enhance the treatment effect; a method for controlling the properties of the mixed liquid in the membrane bioreactor (public number CN 1600705A) mainly through the injection Ozone is added to change the properties of the mixed liquid in the reactor to control membrane fouling; a new method for controlling membrane fouling in membrane bioreactors (publication number CN 102276055A), by adding fillers in the reactor as a biofilm carrier, Optimize the aeration mode to control microbial metabolism, thereby slowing down membrane fouling. A flat ceramic ultrafiltration membrane bioreactor (publication number CN 103304021A) transforms the traditional membrane bioreactor by using a flat ceramic membrane and a fixed FSB biological carrier. The microbial flocs are attached to the surface of the biofiller, which can effectively alleviate the membrane fouling.
基于上述讨论，可见现有方法和设备所存在的问题是：1）曝气和投加的填料仅能减缓膜表面的可逆污染，而对膜孔内的污染无能为力；2）采用的膜大部分为低机械强度的有机膜，无法忍受硬性填料的刮擦，而且大气量的曝气也会导致膜的抖动幅度增加，加速了膜的老化和损坏；3）反应器无污泥沉淀及排泥系统；4）无法去除水中的PPCPs和某些具有内分泌干扰作用的工业微量污染物。 Based on the above discussion, it can be seen that the problems existing in the existing methods and equipment are: 1) The aeration and the fillers added can only slow down the reversible pollution on the surface of the membrane, but can do nothing to the pollution in the membrane pores; 2) Most of the membranes used are It is an organic membrane with low mechanical strength, which cannot bear the scraping of hard fillers, and the large amount of aeration will also increase the shaking range of the membrane, which will accelerate the aging and damage of the membrane; 3) There is no sludge sedimentation and sludge discharge in the reactor system; 4) PPCPs and some industrial trace pollutants with endocrine disrupting effects cannot be removed from water.
发明内容 Contents of the invention
为了解决现有技术中的问题，本实用新型提供了一种基于膜污染原位控制的膜生物反应器。 In order to solve the problems in the prior art, the utility model provides a membrane bioreactor based on in-situ control of membrane fouling.
本实用新型提供了一种基于膜污染原位控制的膜生物反应器，包括反应池，所述反应池内设有膜组件、顶部导流板、侧部导流板和曝气装置，其中，所述顶部导流板设置在所述膜组件之上，所述侧部导流板设置在所述膜组件的外侧，所述曝气装置设置在所述膜组件之下，所述顶部导流板、侧部导流板之间设有供水流出的导流出口，所述侧部导流板、曝气装置之间设有供水流入的导流入口。 The utility model provides a membrane bioreactor based on in-situ control of membrane pollution, which includes a reaction pool in which a membrane module, a top deflector, a side deflector and an aeration device are arranged, wherein the The top deflector is arranged above the membrane module, the side deflector is arranged outside the membrane module, the aeration device is arranged under the membrane module, and the top deflector A diversion outlet for water outflow is provided between the side deflectors, and a diversion inlet for water inflow is provided between the side deflectors and the aeration device.
作为本实用新型的进一步改进，所述反应池内设有隔板，所述隔板沿水平面设置，所述隔板将所述反应池分隔成反应区和缓冲区，所述反应区位于所述隔板之上，所述缓冲区位于所述隔板之下，所述膜组件、顶部导流板、侧部导流板和曝气装置均设置在所述反应区内。 As a further improvement of the present utility model, a partition is arranged in the reaction pool, and the partition is arranged along the horizontal plane, and the partition divides the reaction pool into a reaction zone and a buffer zone, and the reaction zone is located in the partition above the plate, the buffer zone is located under the partition, and the membrane module, top deflector, side deflector and aeration device are all arranged in the reaction zone.
作为本实用新型的进一步改进，所述反应池的底部设有污泥区，所述污泥区位于所述缓冲区之下，所述污泥区的输出口设有排泥阀。 As a further improvement of the utility model, a sludge area is provided at the bottom of the reaction tank, the sludge area is located under the buffer zone, and a sludge discharge valve is provided at the output port of the sludge area.
作为本实用新型的进一步改进，所述侧部导流板绕所述膜组件的周向形成上下开口的侧部导流筒，所述侧部导流筒的底部设有扩口部，所述曝气装置设置在所述扩口部内。 As a further improvement of the present utility model, the side guide plate forms a side guide cylinder with upper and lower openings around the circumference of the membrane module, and the bottom of the side guide cylinder is provided with a flaring portion. The aeration device is arranged in the flared part.
作为本实用新型的进一步改进，所述顶部导流板为圆锥状，所述顶部导流板的顶点靠近所述膜组件，所述顶部导流板的底面靠近所述反应池的顶部。 As a further improvement of the present invention, the top deflector is conical, the apex of the top deflector is close to the membrane module, and the bottom surface of the top deflector is close to the top of the reaction pool.
作为本实用新型的进一步改进，所述反应池连接有进水装置，所述膜组件连接有出水装置，所述进水装置的进水口设置在所述反应池的侧壁、侧部导流板之间。 As a further improvement of the utility model, the reaction tank is connected with a water inlet device, the membrane module is connected with a water outlet device, and the water inlet of the water inlet device is arranged on the side wall and side guide plate of the reaction tank between.
作为本实用新型的进一步改进，所述进水装置包括进水管，所述进水管连接有混凝剂投加装置。 As a further improvement of the utility model, the water inlet device includes a water inlet pipe connected to a coagulant dosing device.
作为本实用新型的进一步改进，所述出水装置与所述膜组件的顶部连接，所述曝气装置包括氧气源、与所述氧气源连接的臭氧发生器和与所述臭氧发生器连接的微孔曝气棒，所述微孔曝气棒设置在所述膜组件之下。 As a further improvement of the utility model, the water outlet device is connected to the top of the membrane module, and the aeration device includes an oxygen source, an ozone generator connected to the oxygen source, and a micrometer connected to the ozone generator. A porous aeration rod, the microporous aeration rod is arranged under the membrane module.
作为本实用新型的进一步改进，所述混凝剂投加装置包括混凝剂储存罐、与所述混凝剂储存罐连接的混凝剂投加泵和与所述混凝剂投加泵连接的投加管，所述投加管与所述进水管连接。 As a further improvement of the utility model, the coagulant dosing device includes a coagulant storage tank, a coagulant dosing pump connected to the coagulant storage tank, and a coagulant dosing pump connected to the coagulant dosing pump The dosing pipe, the dosing pipe is connected with the water inlet pipe.
作为本实用新型的进一步改进，所述反应池内填充有悬浮型填料，所述曝气装置为臭氧、纯氧混合的曝气装置。 As a further improvement of the utility model, the reaction tank is filled with suspended fillers, and the aeration device is an aeration device mixed with ozone and pure oxygen.
本实用新型还提供了一种基于膜污染原位控制的工艺，包括以下步骤： The utility model also provides a process based on in-situ control of membrane fouling, comprising the following steps:
S1、将膜组件设置在顶部导流板的下面、侧部导流板的内侧、曝气装置的上面，通过曝气装置进行曝气，使水流向上流，并且经过膜组件，通过侧部导流板将向上流的水导流在侧部导流板内侧，通过顶部导流板将向上流的水导流为向下流，通过顶部导流板、侧部导流板将向下流的水导流在侧部导流板外侧，在反应池内形成中心向上流、侧部向下流的循环水流； S1. Set the membrane module under the top deflector, inside the side deflector, and above the aeration device, aerate through the aeration device, make the water flow upward, pass through the membrane module, and pass through the side guide The deflector guides the upward-flowing water to the inner side of the side deflectors, guides the upward-flowing water to flow downward through the top deflector, and guides the downward-flowing water through the top deflector and side deflectors. It flows outside the side deflectors, forming a circulating water flow in the reaction tank with the center flowing upward and the side flowing downward;
S2、向反应池内投加混凝剂。 S2, adding a coagulant into the reaction tank.
作为本实用新型的进一步改进，步骤S1还包括：通过水平设置的隔板将反应池分隔为反应区、缓冲区，反应区位于隔板之上，缓冲区位于隔板之下，在缓冲区下设置污泥区，所述循环水流位于反应区内；步骤S2为：向进水装置投加混凝剂形成混凝水，将该混凝水注入到反应池侧壁、侧部导流板外侧之间，该混凝水的进水方向为垂直向下。 As a further improvement of the present utility model, step S1 also includes: separating the reaction pool into a reaction zone and a buffer zone through a horizontal partition, the reaction zone is located above the partition, the buffer zone is located under the partition, and the buffer zone is located under the buffer zone. A sludge area is set, and the circulating water flow is located in the reaction area; step S2 is: adding a coagulant to the water inlet device to form coagulation water, and injecting the coagulation water into the side wall of the reaction tank and the outside of the side deflector Between, the inflow direction of the coagulation water is vertically downward.
本实用新型的有益效果是：通过上述方案，可通过顶部导流板、侧部导流板和曝气装置在反应池内形成中心向上流、侧部向下流的循环水流，中心向上流的水流流经膜组件，可以有效控制膜表面的可逆污染。 The beneficial effects of the utility model are: through the above scheme, a circulating water flow with the center flowing upward and the side flowing downward can be formed in the reaction tank through the top deflector, the side deflector and the aeration device; Through the membrane module, the reversible fouling of the membrane surface can be effectively controlled.
附图说明 Description of drawings
图1是本实用新型一种基于膜污染原位控制的膜生物反应器的结构示意图； Fig. 1 is a structural representation of a membrane bioreactor based on in-situ control of membrane fouling of the present invention;
图2是图1的剖视图A-A； Fig. 2 is the sectional view A-A of Fig. 1;
图3是图1的剖视图B-B。 Fig. 3 is a sectional view B-B of Fig. 1 .
具体实施方式 Detailed ways
下面结合附图说明及具体实施方式对本实用新型进一步说明。 The utility model will be further described below in conjunction with the accompanying drawings and specific embodiments.
图1至图3中的附图标号为：反应池1；顶部导流板11；侧部导流板12；填料13；进水管14；隔板15；排泥阀16；混凝剂投加泵2；混凝剂储存罐21；投加管22；臭氧发生器3；微孔曝气棒31；氧气源32；膜组件4；出水抽吸泵41；出水管42； The reference numerals in Fig. 1 to Fig. 3 are: reaction tank 1; top deflector 11; side deflector 12; filler 13; water inlet pipe 14; Pump 2; coagulant storage tank 21; dosing pipe 22; ozone generator 3; microporous aeration rod 31; oxygen source 32; membrane module 4; water outlet suction pump 41; water outlet pipe 42;
为解决当前膜生物反应器存在的问题，本实用新型提供一种可以原位控制膜污染的膜生物反应器及工艺，通过对进水投加混凝剂，在膜生物反应器内放置悬浮型填料，使用臭氧/纯氧曝气，在异形导流板的作用下实现膜表面和膜孔内污染的原位控制，同时利用臭氧/纯氧强化新兴污染物的去除效果。 In order to solve the problems existing in the current membrane bioreactor, the utility model provides a membrane bioreactor and a process that can control membrane fouling in situ. By adding coagulant to the influent, a suspended type The filler uses ozone/pure oxygen aeration to realize in-situ control of pollution on the membrane surface and inside the membrane pores under the action of special-shaped deflectors, and at the same time uses ozone/pure oxygen to enhance the removal effect of emerging pollutants.
如图1至图3所示，一种基于膜污染原位控制的膜生物反应器，包括反应池1，所述反应池1内设有膜组件4、顶部导流板11、侧部导流板12和曝气装置，其中，所述顶部导流板11竖直设置在所述膜组件4之上，所述侧部导流板12设置在所述膜组件4的外侧，所述曝气装置设置在所述膜组件4之下，所述顶部导流板11、侧部导流板12之间设有供水流出的导流出口，所述侧部导流板12、曝气装置之间设有供水流入的导流入口。 As shown in Figures 1 to 3, a membrane bioreactor based on in-situ control of membrane fouling includes a reaction tank 1, and the reaction tank 1 is provided with a membrane module 4, a top deflector 11, and a side deflector. Plate 12 and aeration device, wherein, the top deflector 11 is vertically arranged above the membrane module 4, the side deflector 12 is arranged outside the membrane module 4, and the aeration The device is arranged under the membrane module 4, and a flow guide outlet for water flow is provided between the top deflector 11 and the side deflector 12, and between the side deflector 12 and the aeration device There is a diversion inlet for water inflow.
如图1至图3所示，所述反应池1内设有填料13，所述填料13优选为悬浮型填料，优选在反应池内填充半悬浮型填料，所述半悬浮性填料的直径需要与导流出口、导流入口、相邻膜组件4的间隙相配合，所述填料13为耐氧化的柔性或刚性材料制成。 As shown in Fig. 1 to Fig. 3, described reaction tank 1 is provided with filler 13, and described filler 13 is preferably suspension type filler, preferably fills semi-suspension type filler in reaction tank, and the diameter of described semi-suspension filler needs and The diversion outlet, the diversion inlet, and the gaps between adjacent membrane modules 4 are matched, and the packing 13 is made of oxidation-resistant flexible or rigid material.
如图1至图3所示，所述曝气装置优选为臭氧、纯氧混合的曝气装置。 As shown in Figures 1 to 3, the aeration device is preferably an aeration device mixed with ozone and pure oxygen.
如图1至图3所示，所述膜组件4优选为耐氧化、高机械强度的陶瓷膜组件。 As shown in FIGS. 1 to 3 , the membrane module 4 is preferably an oxidation-resistant ceramic membrane module with high mechanical strength.
如图1至图3所示，所述反应池1内设有隔板15，所述隔板15优选为多孔隔板，所述隔板15沿水平面设置，所述隔板15将所述反应池1分隔成反应区和缓冲区，所述反应区位于所述隔板15之上，所述缓冲区位于所述隔板15之下，所述膜组件4、顶部导流板11、侧部导流板12和曝气装置均设置在所述反应区内。 As shown in Figures 1 to 3, a partition 15 is provided in the reaction tank 1, and the partition 15 is preferably a porous partition, and the partition 15 is arranged along a horizontal plane, and the partition 15 divides the reaction The pool 1 is divided into a reaction zone and a buffer zone, the reaction zone is above the partition 15, the buffer zone is below the partition 15, the membrane module 4, the top deflector 11, the side Both the deflector 12 and the aeration device are arranged in the reaction zone.
如图1至图3所示，所述反应池的底部设有污泥区，所述污泥区位于所述缓冲区之下，所述污泥区的输出口设有排泥阀16。 As shown in Figures 1 to 3, a sludge area is provided at the bottom of the reaction tank, the sludge area is located under the buffer zone, and a sludge discharge valve 16 is provided at the output port of the sludge area.
如图1至图3所示，反应池1内的隔板15将反应区与污泥区分开，部分污泥絮体可在惯性力做用下进入网格下的污泥区，而填料13仍保留在反应区，填料13与隔板15的碰撞还可使填料13上老化的生物膜脱落进入污泥区，维持生物膜的高活性，污泥区的污泥可通过排泥阀16排除，反应池1的水力停留时间 0.5-1h。 As shown in Figures 1 to 3, the partition 15 in the reaction tank 1 separates the reaction zone from the sludge area, and part of the sludge flocs can enter the sludge area under the grid under the action of inertial force, while the filler 13 remains Retained in the reaction zone, the collision between the filler 13 and the partition 15 can also cause the aged biofilm on the filler 13 to fall off and enter the sludge zone, maintaining the high activity of the biofilm, and the sludge in the sludge zone can be discharged through the sludge discharge valve 16, The hydraulic retention time of reaction tank 1 is 0.5-1h.
如图1至图3所示，所述侧部导流板11绕所述膜组件4的周向形成上下开口的侧部导流筒，所述侧部导流筒的底部设有扩口部，所述扩口部类似喇叭状，所述曝气装置设置在所述扩口部内。 As shown in Figures 1 to 3, the side guide plate 11 forms a side guide tube with upper and lower openings around the circumference of the membrane module 4, and the bottom of the side guide tube is provided with a flared portion , the flared portion is similar to a trumpet shape, and the aeration device is arranged in the flared portion.
如图1至图3所示，所述顶部导流板11为圆锥状，所述顶部导流板11的顶点靠近所述膜组件4，所述顶部导流板11的底面靠近所述反应池1的顶部。 As shown in Figures 1 to 3, the top deflector 11 is conical, the apex of the top deflector 11 is close to the membrane module 4, and the bottom surface of the top deflector 11 is close to the reaction pool 1 top.
如图1至图3所示，所述反应池1连接有进水装置，所述膜组件4连接有出水装置，所述进水装置的进水口设置在所述反应池1的侧壁、侧部导流板12之间。 As shown in Figures 1 to 3, the reaction tank 1 is connected with a water inlet device, and the membrane module 4 is connected with a water outlet device, and the water inlet of the water inlet device is arranged on the side wall and side of the reaction tank 1. between the baffles 12.
如图1至图3所示，所述进水装置包括进水管14，所述进水管14连接有混凝剂投加装置。 As shown in FIGS. 1 to 3 , the water inlet device includes a water inlet pipe 14 connected to a coagulant dosing device.
如图1至图3所示，所述混凝剂投加装置包括混凝剂储存罐21、与所述混凝剂储存罐21连接的混凝剂投加泵2和与所述混凝剂投加泵2连接的投加管22，混凝剂通过投加管22直接进入进水管14，在进水管14内和反应池1内完成混凝过程。 As shown in Figures 1 to 3, the coagulant dosing device includes a coagulant storage tank 21, a coagulant dosing pump 2 connected to the coagulant storage tank 21 and a Dosing the dosing pipe 22 connected to the pump 2, the coagulant directly enters the water inlet pipe 14 through the dosing pipe 22, and completes the coagulation process in the water inlet pipe 14 and the reaction tank 1.
如图1至图3所示，所述出水装置与所述膜组件4的顶部连接。 As shown in FIGS. 1 to 3 , the water outlet device is connected to the top of the membrane module 4 .
如图1至图3所示，所述出水装置包括与所述膜组件4的顶部连接的出水抽吸泵41和与出水抽吸泵41连接的所述出水管42，出水抽吸泵41可提供-80kPa的抽吸压强和200kPa压强的扬程，出水抽吸泵41可同时作为产水泵和反冲洗泵使用。 As shown in Figures 1 to 3, the water outlet device includes an outlet suction pump 41 connected to the top of the membrane module 4 and an outlet pipe 42 connected to the outlet suction pump 41, the outlet suction pump 41 can Providing a suction pressure of -80kPa and a pressure lift of 200kPa, the discharge water suction pump 41 can be used as a production water pump and a backwash pump at the same time.
如图1至图3所示，所述曝气装置包括氧气源32、与所述氧气源32连接的臭氧发生器3和与所述臭氧发生器3连接的微孔曝气棒31，所述微孔曝气棒31设置在所述膜组件4之下，氧气源32可提供压力为40-100kPa的干燥纯氧，经过臭氧发生器3后可产生臭氧浓度在30-100mg/L的臭氧、纯氧混合气体，微孔曝气棒31可将臭氧均匀的分布于反应池1底部。 As shown in Figures 1 to 3, the aeration device includes an oxygen source 32, an ozone generator 3 connected to the oxygen source 32 and a microporous aeration rod 31 connected to the ozone generator 3, the Microporous aeration rod 31 is arranged under described membrane module 4, and oxygen source 32 can provide the dry pure oxygen that pressure is 40-100kPa, can produce the ozone of ozone concentration at 30-100mg/L after passing through ozone generator 3, The mixed gas of pure oxygen and the microporous aeration rod 31 can evenly distribute the ozone at the bottom of the reaction tank 1 .
如图1至图3所示，一种基于膜污染原位控制的工艺，包括以下步骤： As shown in Figures 1 to 3, a process based on in-situ control of membrane fouling includes the following steps:
S1、将膜组件4设置在顶部导流板11的下面、侧部导流板12的内侧、曝气装置的上面，通过曝气装置进行曝气，使水流向上流，并且经过膜组件4，通过侧部导流板12将向上流的水导流在侧部导流板12的内侧，通过顶部导流板11将向上流的水导流为向下流，通过顶部导流板11、侧部导流板12将向下流的水导流在侧部导流板12的外侧，在反应池1内形成中心向上流、侧部向下流的循环水流； S1. The membrane module 4 is arranged under the top deflector 11, inside the side deflector 12, and above the aeration device, and the aeration device is used for aeration to make the water flow upward and pass through the membrane module 4, By the side deflectors 12, the upwardly flowing water is diverted to the inner side of the side deflectors 12, by the top deflectors 11, the upwardly flowing water is guided to flow downward, by the top deflectors 11, the side The deflector 12 guides the water flowing downward to the outside of the side deflector 12, forming a circulating water flow with the center flowing upward and the side flowing downward in the reaction tank 1;
S2、向反应池1内投加混凝剂。 S2. Add coagulant into the reaction tank 1 .
如图1至图3所示，步骤S1还包括：通过水平设置的隔板15将反应池1分隔为反应区、缓冲区，反应区位于隔板之上，缓冲区位于隔板之下，在缓冲区下设置污泥区，所述循环水流位于反应区内；步骤S2为：向进水装置投加混凝剂形成混凝水，将该混凝水注入到反应池1的侧壁、侧部导流板12的外侧之间，该混凝水的进水方向为垂直向下。 As shown in Figures 1 to 3, step S1 also includes: dividing the reaction pool 1 into a reaction zone and a buffer zone by a partition plate 15 arranged horizontally, the reaction zone is located above the partition plate, and the buffer zone is located below the partition plate, A sludge zone is set under the buffer zone, and the circulating water flow is located in the reaction zone; step S2 is: adding a coagulant to the water inlet device to form coagulation water, and injecting the coagulation water into the side wall and side wall of the reaction tank 1 Between the outer sides of the upper deflectors 12, the water inflow direction of the coagulated water is vertically downward.
本实用新型提供的一种基于膜污染原位控制的膜生物反应器及其工艺具有以下优点： A membrane bioreactor based on in-situ control of membrane pollution and its technology provided by the utility model have the following advantages:
1、投加混凝剂后的混凝水直接进入反应池1，在反应池1内实现微絮凝过程，膜过滤可截留绝大部分混凝水中的颗粒物，并可在反应池1内形成一定浓度的絮体，絮体可停留较长时间，其本身就是一种“填料”，附着于絮体上的微生物可对污染物进行降解； 1. The coagulation water after adding the coagulant directly enters the reaction tank 1, and the micro-flocculation process is realized in the reaction tank 1. Membrane filtration can intercept most of the particles in the coagulation water, and can form a certain amount in the reaction tank 1. Concentration of flocs, the flocs can stay for a long time, which itself is a kind of "filler", and the microorganisms attached to the flocs can degrade the pollutants;
2、膜组件4过滤同时对反应池1中的混凝水进行臭氧、纯氧曝气，气体带动水体和填料13运行，在顶部导流板11、侧部导流板12的共同作用下形成在反应池1内形成中心向上流、侧部向下流的循环水流，完成混凝过程，填料13为固着态微生物提供载体的同时可降低膜表面的可逆污染阻力，臭氧可氧化水中有机物，去除色度和臭味，并且可控制膜组件4的孔内的有机物污染，因此，可实现污染物去除和控制膜污染的双重效果； 2. The membrane module 4 filters and aerates the coagulation water in the reaction tank 1 with ozone and pure oxygen at the same time, the gas drives the water body and the filler 13 to run, and is formed under the joint action of the top deflector 11 and the side deflector 12 In the reaction tank 1, a circulating water flow with the center flowing upward and the side flowing downward is formed to complete the coagulation process. The filler 13 provides a carrier for the fixed microorganisms and can reduce the reversible pollution resistance of the membrane surface. Ozone can oxidize organic matter in water and remove color. degree and odor, and can control the organic pollution in the pores of the membrane module 4, therefore, the dual effects of pollutant removal and membrane fouling control can be achieved;
3、通过臭氧、纯氧曝气，投加的臭氧量为1-5mg/L，反应区的溶解氧浓度可维持在10-15mg/L左右；在隔板15的分离作用下，填料13始终位于反应池1的反应区；在惯性力和重力作用下，部分絮体可通过隔板15在污泥区形成污泥，减少排泥水量，提高产水率。 3. Through ozone and pure oxygen aeration, the amount of ozone added is 1-5mg/L, and the dissolved oxygen concentration in the reaction zone can be maintained at about 10-15mg/L; Located in the reaction zone of the reaction tank 1; under the action of inertial force and gravity, some flocs can form sludge in the sludge zone through the partition 15, reducing the amount of sludge discharge water and increasing the water production rate.
本实用新型提供的一种基于膜污染原位控制的膜生物反应器在正式运行之前，需经过一定时间的微生物培养，培养时间视环境温度和水质条件而定。 The membrane bioreactor based on in-situ control of membrane pollution provided by the utility model needs to undergo a certain period of microbial cultivation before the official operation, and the cultivation time depends on the ambient temperature and water quality conditions.
本实用新型解决的关键问题之一是：如何有效地控制膜污染。其原理是：1）曝气使填料13呈流化态，填料13和水流分别具有较高的摩擦力和剪切力，结合填料13直径与相邻膜组件4间隙的调节，絮体和填料13在循环水流带动下，可有效控制膜表面的可逆污染；2）臭氧可分解大分子有机物，增加有机物的亲水性，一方面有利于膜池内污染物的降解，一方面溶解态臭氧可进入膜孔，与膜组件4孔内的有机物反应，从而制膜孔内的物理不可逆有机物污染，延长膜的化学清洗周期；3）反应池1设置了缓冲区和污泥区，有利于控制反应区内的絮体浓度，避免在反应过程中絮体浓度持续增加而加重膜的污染。 One of the key problems solved by the utility model is: how to effectively control membrane fouling. The principle is: 1) Aeration makes the filler 13 in a fluidized state, the filler 13 and the water flow have high friction and shear force respectively, combined with the adjustment of the diameter of the filler 13 and the gap between the adjacent membrane module 4, the floc and filler 13 Driven by the circulating water flow, the reversible pollution on the membrane surface can be effectively controlled; 2) Ozone can decompose macromolecular organic matter and increase the hydrophilicity of organic matter. On the one hand, it is beneficial to the degradation of pollutants in the membrane pool. On the other hand, dissolved ozone can enter Membrane holes react with the organic matter in the 4 holes of the membrane module, thereby preventing physical irreversible organic matter pollution in the membrane hole and prolonging the chemical cleaning cycle of the membrane; 3) The reaction pool 1 is equipped with a buffer zone and a sludge area, which is beneficial to control the reaction area The concentration of flocs in the reaction process can avoid the continuous increase of the concentration of flocs in the reaction process and aggravate the fouling of the membrane.
与现有技术相比，本实用新型的显著优点是填料13和混凝剂形成的絮体均可作为微生物的载体，且絮体的比表面积远高于填料，增加了微生物量，同时臭氧、纯氧曝气过程比传统的空气曝气具有更高的氧分压，提高了氧的传质效率。高生物量和氧的高传质效率保证了污染物的降解速率，提高了反应器的有机物容积负荷。 Compared with the prior art, the remarkable advantage of the utility model is that the flocs formed by the filler 13 and the coagulant can be used as the carrier of microorganisms, and the specific surface area of the flocs is much higher than that of the fillers, which increases the microbial load, and at the same time, ozone, The pure oxygen aeration process has a higher oxygen partial pressure than the traditional air aeration, which improves the oxygen mass transfer efficiency. The high mass transfer efficiency of high biomass and oxygen ensures the degradation rate of pollutants and increases the organic volume loading of the reactor.
利用本实用新型处理微污染原水或低浓度有机物废水时，具有如下优点：1）采用混凝工艺后，反应池1内形成一定浓度絮体，絮体和填料13可同时为微生物生长提供载体，有利于世代时间长的微生物如硝化细菌的繁殖，絮体还可以吸附部分进水的污染物，絮体和填料13在循环水流带动下，降低膜组件4的污染物负荷；2）采用臭氧、纯氧曝气，使填料13处于流化态可以分别控制膜组件4的可逆污染和膜组件4孔内的物理不可逆有机物污染，实现膜污染的原位控制；3）臭氧可分解不利于微生物分解的大分子有机物，强化有机物的去除效果；4）臭氧、纯氧曝气的使用加快了氧的传质，降低能耗；5）反应池1分区为反应区、缓冲区、污泥区，可使反应区内污泥浓度不至太高而加重膜污染。 When the utility model is used to treat slightly polluted raw water or low-concentration organic waste water, it has the following advantages: 1) After adopting the coagulation process, a certain concentration of flocs is formed in the reaction tank 1, and the flocs and fillers 13 can simultaneously provide carriers for the growth of microorganisms, It is beneficial to the reproduction of microorganisms with a long generation time such as nitrifying bacteria, and the flocs can also absorb some pollutants in the influent. Driven by the circulating water flow, the flocs and filler 13 reduce the pollutant load of the membrane module 4; 2) use ozone, Pure oxygen aeration, so that the filler 13 is in a fluidized state, can respectively control the reversible pollution of the membrane module 4 and the physical irreversible organic pollution in the pores of the membrane module 4, and realize the in-situ control of membrane pollution; 3) Ozone can be decomposed and is not conducive to microbial decomposition 4) The use of ozone and pure oxygen aeration speeds up the mass transfer of oxygen and reduces energy consumption; 5) The reaction pool 1 is divided into reaction area, buffer zone, and sludge area, which can Make the sludge concentration in the reaction zone not too high and aggravate the membrane fouling.
以下提供两项实验，进一步说明本实用新型。 Two experiments are provided below to further illustrate the utility model.
实验1 Experiment 1
测试本实用新型对膜污染的控制效果，在曝气量为400L/h，臭氧投加量为2mg/L，膜通量为100L/m2h，水力停留时间0.5h的工况下处理微污染原水，与未投加臭氧和填料的膜生物反应器相比，膜的化学清洗周期可由7天延长至20天。 To test the control effect of the utility model on membrane fouling, the microbiological treatment was carried out under the working condition that the aeration rate was 400L/h, the dosage of ozone was 2mg/L, the membrane flux was 100L/m 2 h, and the hydraulic retention time was 0.5h. Contaminated raw water, compared with membrane bioreactors without ozone and fillers, the chemical cleaning cycle of the membrane can be extended from 7 days to 20 days.
实验2 Experiment 2
测试本实用新型对有机物、氨氮、PPCPs和嗅味物质的去除效果，在曝气量为400L/h，臭氧投加量为2mg/L，膜通量为100L/m2h，水力停留时间0.5h的工况下，反应池1水中的溶解氧可由4mg/L提高至15-20mg/L，PPCPs和嗅味物质的去除率为95%以上，有机物的去除率约为50%，对氨氮的绝对去除量可达3-4mg/L而无亚硝酸盐的积累。 Test the removal effect of the utility model on organic matter, ammonia nitrogen, PPCPs and odor substances, when the aeration rate is 400L/h, the ozone dosage is 2mg/L, the membrane flux is 100L/m 2 h, and the hydraulic retention time is 0.5 Under the working condition of h, the dissolved oxygen in the water of reaction tank 1 can be increased from 4mg/L to 15-20mg/L, the removal rate of PPCPs and odor substances is more than 95%, the removal rate of organic matter is about 50%, and the removal rate of ammonia nitrogen The absolute removal amount can reach 3-4mg/L without the accumulation of nitrite.
以上内容是结合具体的优选实施方式对本实用新型所作的进一步详细说明，不能认定本实用新型的具体实施只局限于这些说明。对于本实用新型所属技术领域的普通技术人员来说，在不脱离本实用新型构思的前提下，还可以做出若干简单推演或替换，都应当视为属于本实用新型的保护范围。 The above content is a further detailed description of the utility model in combination with specific preferred embodiments, and it cannot be assumed that the specific implementation of the utility model is only limited to these descriptions. For a person of ordinary skill in the technical field to which the utility model belongs, without departing from the concept of the utility model, some simple deduction or substitutions can also be made, which should be regarded as belonging to the protection scope of the utility model.
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| CN201420738968.XU CN204281406U (en) | 2014-11-28 | 2014-11-28 | A kind of membrane bioreactor based on fouling membrane in-situ control |
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| CN201420738968.XU CN204281406U (en) | 2014-11-28 | 2014-11-28 | A kind of membrane bioreactor based on fouling membrane in-situ control |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445600A (en) * | 2014-11-28 | 2015-03-25 | 深圳中清环境科技有限公司 | Membrane pollution in-situ control based membrane bioreactor and technology thereof |
| CN112387118A (en) * | 2019-08-19 | 2021-02-23 | 北京奥博水处理有限责任公司 | Online self-cleaning ceramic membrane filter |
| CN114506965A (en) * | 2020-11-17 | 2022-05-17 | 湖南盛世丰花生物科技有限公司 | Three-phase biological fluidized bed for treating high-concentration organic wastewater |
-
2014
- 2014-11-28 CN CN201420738968.XU patent/CN204281406U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445600A (en) * | 2014-11-28 | 2015-03-25 | 深圳中清环境科技有限公司 | Membrane pollution in-situ control based membrane bioreactor and technology thereof |
| CN112387118A (en) * | 2019-08-19 | 2021-02-23 | 北京奥博水处理有限责任公司 | Online self-cleaning ceramic membrane filter |
| CN114506965A (en) * | 2020-11-17 | 2022-05-17 | 湖南盛世丰花生物科技有限公司 | Three-phase biological fluidized bed for treating high-concentration organic wastewater |
| CN114506965B (en) * | 2020-11-17 | 2023-12-19 | 湖南盛世丰花生物科技股份有限公司 | Three-phase biological fluidized bed for treating high-concentration organic wastewater |
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