Partitioned integrated aerobic granular sludge-membrane bioreactor coupling device and application

Abstract

The application discloses a partitioned integrated aerobic granular sludge-membrane bioreactor coupling device and application, the coupling device includes a water inlet system, a reactor main body, a water outlet system, a sludge discharge system, an automatic monitoring control system, the reactor main body is divided into multiple intervals by multiple baffles, including anoxic zone one, an aerobic zone, anoxic zone two, a sludge selection zone one, a sludge selection zone two, a membrane reaction zone and a sludge discharge and sedimentation zone.The application creates periodic satiation-starvation cycle conditions through anoxic-aerobic-anoxic (AOA) left and right alternating water feeding operation mode; good hydraulic shear force is created for the system by combining stirring and aeration; through the setting of the sludge selection zone, a good settling velocity selection pressure is created, necessary conditions for the formation of aerobic granular sludge under continuous flow conditions are created, and the technical problem that aerobic granular sludge is difficult to form under current continuous flow conditions is solved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of water treatment, in particular to a partitioned integrated aerobic granular sludge-membrane bioreactor coupling device and application. BACKGROUND

[0002] The urban sewage discharge standard in China is becoming increasingly stringent, and relevant policies have clearly pointed out that the discharge of pollutants should be comprehensively controlled, the precise upgrading of sewage treatment should be carried out, the water quality should be improved, and the utilization of reclaimed water should be promoted, so as to alleviate the pressure of water resource shortage, control water environmental pollution, and improve water ecological safety.

[0003] The aerobic granular sludge can significantly improve the degradation capacity of pollutants due to its regular shape, good settling performance, stable structure, high biomass and activity. At the same time, the aerobic granular sludge has an oxygen distribution gradient in the radial direction, forming an environment of external oxygen and internal anoxia, which has the function of simultaneously removing organic matter, nitrogen and phosphorus. This not only improves the efficiency of water treatment, but also makes the water treatment structure compact, reducing the land occupation. Compared with the traditional activated sludge method, the aerobic granular sludge has a small amount of sludge production, which can significantly reduce the cost of residual sludge treatment and disposal. The sequencing batch reactor is considered to be the most ideal reactor for promoting sludge granulation, and the settling velocity selection pressure, periodic satiation-starvation cycle and hydraulic shear force are the main factors driving the aerobic granulation of activated sludge in the sequencing batch system. However, compared with the traditional sequencing batch reactor, the continuous flow aerobic granular sludge technology has the advantages of low operation cost, easy operation and control, and matching the large water quantity and continuous flow of actual sewage plants, and has more research value and application potential. However, under the condition of continuous flow, it is a major challenge to create the above three driving forces to achieve rapid cultivation and stable operation of aerobic granular sludge.

[0004] The membrane bioreactor process can replace the secondary sedimentation tank of the traditional biological treatment technology, reduce the land occupation, improve the effluent water quality, and reduce the production of excess sludge, and is widely used in sewage / wastewater treatment. However, the membrane fouling problem of membrane bioreactor restricts the further popularization and application of membrane bioreactor. The aerobic granular sludge can effectively alleviate the membrane fouling problem, because of its dense granular structure, not only has good settling performance, but also produces less extracellular polymeric substance on its surface than flocculent sludge. Placing the membrane module in the aerobic granular sludge system can greatly reduce the blockage of the membrane holes. In addition, compared with organic membranes, inorganic ceramic membranes have better anti-pollution performance, so the combination of aerobic granular sludge and ceramic membrane bioreactor has the advantages of intensive land occupation, alleviation of membrane fouling, resistance to high pollutant load, and strong impact resistance.

[0005] However, the cultivation conditions of aerobic granular sludge are different from the operation conditions of membrane module. Large aeration scouring is needed in the membrane module area to alleviate membrane fouling, while excessive aeration in the sludge area can cause the disintegration of granular sludge. Meanwhile, the requirements for extracellular polymeric substances (EPS) are different in the two areas. Higher EPS is beneficial to the formation of granular sludge, while excessive EPS can accelerate membrane fouling. In addition, the direct contact between aerobic granular sludge and membrane module can cause the disintegration of aerobic granular sludge. Therefore, how to combine aerobic granular sludge with ceramic membrane bioreactor and create driving force for the formation of aerobic granular sludge under continuous flow conditions is a problem that needs to be solved.

[0006] Therefore, the present application is proposed. SUMMARY

[0007] To solve the above problems, the present application aims to provide a partitioned integrated aerobic granular sludge-membrane bioreactor coupling device and application. By designing the structure of the reactor and the hydraulic conditions, three necessary conditions for the formation of aerobic granular sludge are created under continuous flow conditions, i.e. settling velocity selection pressure, periodic satiation-starvation cycle, and hydraulic shear force, realizing the rapid formation and stable operation of aerobic granular sludge under continuous flow conditions. At the same time, the aerobic granular sludge and the membrane bioreactor are ingeniously operated in a partitioned integrated manner, avoiding the mutual influence of different operation conditions and coupling the advantages of the two, alleviating membrane fouling, improving the effluent water quality, reducing energy consumption, carbon emissions, land occupation, and sludge production. In addition, the device of the present application adopts a special operation mode of alternating anoxic-aerobic-anoxic (AOA) water inflow, which enhances the denitrification efficiency of the system based on two-stage anoxic denitrification. Moreover, the device avoids large height-diameter ratio in design, and the overall structure is consistent with the current continuous flow actual wastewater treatment plant structure, providing technical support for the upgrading and expansion of the mainstream continuous flow wastewater treatment plant process, and promoting the utilization of reclaimed water.

[0008] The present application is realized by the following technical solutions:

[0009] In a first aspect, the present application provides a partitioned integrated aerobic granular sludge-membrane bioreactor coupling device, which comprises a reactor body, wherein an aerobic zone, an anoxic zone, a sludge selection zone, and a membrane reaction zone are sequentially arranged in the reactor body along the horizontal direction.

[0010] A vertical baffle two is arranged in the anoxic zone, which divides the anoxic zone into two non-communicating anoxic zones one and two. An inlet one is arranged on the anoxic zone one, and an inlet two is arranged on the anoxic zone two. The bottom of the anoxic zone one and the bottom of the anoxic zone two are respectively connected to the bottom of the aerobic zone.

[0011] A vertical baffle six is arranged in the sludge selection zone, which divides the sludge selection zone into two non-communicating sludge selection zones one and two.

[0012] The bottom of the first sludge selection area is connected with the bottom of the first anoxic area, and the bottom of the second sludge selection area is connected with the bottom of the second anoxic area;

[0013] The two sides of the membrane reaction area are respectively provided with the first sedimentation area and the second sedimentation area, and the top of the first sedimentation area and the second sedimentation area is not connected with the top of the membrane reaction area;

[0014] The first sedimentation area and the first sludge selection area are connected through the electromagnetic valve one, and the second sedimentation area and the second sludge selection area are connected through the electromagnetic valve two.

[0015] In a specific embodiment, the first anoxic area is provided with a cantilever stirrer one, and the second anoxic area is provided with a cantilever stirrer two.

[0016] In a specific embodiment, the membrane reaction area is provided with a membrane assembly.

[0017] In a specific embodiment, the bottom of the aerobic area is provided with an aeration assembly one, and the bottom of the membrane reaction area is provided with an aeration assembly two.

[0018] In a specific embodiment, the aeration assembly one includes a nano-aeration plate one and an aerator one arranged at the bottom of the aerobic area, the aerator one and the nano-aeration plate one are connected through a gas inlet pipe one, and the gas inlet pipe one is provided with a gas flow meter one and a check valve one;

[0019] The aeration assembly two includes a nano-aeration plate two and an aerator two arranged at the bottom of the membrane reaction area, the aerator two and the nano-aeration plate two are connected through a gas inlet pipe two, and the gas inlet pipe two is provided with a gas flow meter two and a check valve two.

[0020] In a specific embodiment, the coupling device further includes a water inlet system, the water inlet system includes a water inlet bucket, the water inlet bucket and the water inlet port one and the water inlet port two are connected through a water inlet pipe, and the water inlet pipe is provided with a water inlet pump.

[0021] In a specific embodiment, the coupling device further includes a water outlet system, the water outlet system includes a water outlet bucket, the water outlet bucket and the water inlet port one and the water inlet port two are connected through a water inlet pipe, and the water inlet pipe is provided with a water inlet pump.

[0022] In a specific embodiment, the coupling device further includes a sludge discharge system, the bottoms of the first sedimentation area and the second sedimentation area are connected to form a sludge discharge area, the sludge discharge area is located below the membrane reaction area, and the bottom of the membrane reaction area is connected with the sludge discharge area; the sludge discharge system includes a residual sludge collector, the residual sludge collector is connected with a sludge discharge port arranged at the bottom of the sludge discharge area through a sludge discharge pipe, and the sludge discharge pipe is provided with a sludge discharge pump.

[0023] In a specific embodiment, the coupling device further comprises an automatic monitoring control system, the automatic monitoring control system comprising a multi-parameter combined probe arranged in the anoxic zone and a dissolved oxygen probe arranged in the aerobic zone, the multi-parameter combined probe and the dissolved oxygen probe being electrically connected with a multi-parameter transmitter.

[0024] In a second aspect, the application further provides an application of the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device, which is applied to culturing aerobic granular sludge and sewage treatment.

[0025] Compared with the prior art, the application has the following advantages and beneficial effects:

[0026] 1. The partitioned integrated aerobic granular sludge-membrane bioreactor coupling device and the application provided by the embodiment of the application create periodic satiation-hunger cycle conditions through an anoxic-aerobic-anoxic (AOA) left-right alternating water feeding mode; create good hydraulic shear force for the system by combining stirring and aeration; create a good settling velocity selection pressure through the setting of the sludge selection zone, and create necessary conditions for the formation of aerobic granular sludge under continuous flow conditions, thereby solving the technical problem of difficulty in forming aerobic granular sludge under continuous flow conditions.

[0027] 2. The partitioned integrated aerobic granular sludge-membrane bioreactor coupling device and the application provided by the embodiment of the application create an anoxic-aerobic-anoxic (AOA) operation mode in time and space through a left-right alternating water feeding mode, and can realize deep denitrification and significantly improve the denitrification efficiency and impact load resistance of the system through the setting of two-stage anoxic zones.

[0028] 3. The partitioned integrated aerobic granular sludge-membrane bioreactor coupling device and the application provided by the embodiment of the application integrate the aerobic granular sludge and the ceramic membrane bioreactor process through a partitioned integrated design, can meet the differences in operation conditions of the two, can utilize the advantages of the two, can alleviate membrane pollution, can improve the effluent water quality, can reduce energy consumption and carbon emissions, can reduce the land occupation area and sludge production, and is a new green low-carbon sewage treatment technology, which can help improve the quality and efficiency of sewage treatment and promote the resource utilization of urban sewage.

[0029] 4. The partitioned integrated aerobic granular sludge-membrane bioreactor coupling device and the application provided by the embodiment of the application have simple structure and are easy to operate, avoid large height-diameter ratio in design, and are consistent with the current actual sewage treatment plant structure, and can provide a green, low-carbon and efficient solution for the upgrading and expansion modification of the current mainstream continuous flow sewage treatment process. BRIEF DESCRIPTION OF DRAWINGS

[0030] In order to more clearly illustrate the technical solutions of the exemplary embodiments of the present application, the following will briefly introduce the drawings needed to be used in the embodiments. It should be understood that the following drawings only show some of the embodiments of the present application, and therefore should not be regarded as a limitation on the scope, and for those skilled in the art, other related drawings can also be obtained without creative labor.

[0031] Figure 1 The planar structure diagram of the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device provided for the embodiments of the present application is shown in the figure.

[0032] Figure 2 The 3D structure diagram of the coupling device provided for the embodiments of the present application is shown in the figure.

[0033] Figure 3 The aerobic granular sludge cultivated by the coupling device provided for the embodiments of the present application is shown in the figure.

[0034] Figure 4 The treatment effect diagram of the coupling device provided for the embodiments of the present application on low-concentration sewage is shown in the figure.

[0035] Figure 5 The treatment effect diagram of the coupling device provided for the embodiments of the present application on high-concentration sewage is shown in the figure.

[0036] The drawings and component marks are as follows:

[0037] 1 - water inlet bucket, 2 - water inlet pump, 3 - water inlet pipe, 4 - water inlet port one, 5 - water inlet port two, 6 - baffle one, 7 - baffle two, 8 - baffle three, 9 - cantilever stirrer one, 10 - baffle four, 11 - aerator one, 12 - gas flow meter one, 13 - check valve one, 14 - air inlet pipe one, 15 - nano aeration plate one, 16 - cantilever stirrer two, 17 - baffle five, 18 - baffle six, 19 - baffle seven, 20 - baffle eight, 21 - baffle nine, 22 - baffle ten, 23 - baffle eleven, 24 - baffle twelve, 25 - hollow flat plate ceramic membrane assembly, 26 - aerator two, 27 - gas flow meter two, 28 - check valve two, 29 - air inlet pipe two, 30 - nano aeration plate two, 31 - electromagnetic valve one water inlet port, 32 - electromagnetic valve one, 33 - electromagnetic valve one water outlet, 34 - electromagnetic valve two water inlet port, 35 - electromagnetic valve two, 36 - electromagnetic valve two water outlet, 37 - water collecting port, 38 - paperless recorder, 39 - pressure sensor, 40 - bidirectional centrifugal pump, 41 - water outlet pipe, 42 - water outlet bucket, 43 - sludge discharge port, 44 - sludge discharge pipe, 45 - sludge discharge pump, 46 - residual sludge collector, 47 - dissolved oxygen probe, 48 - multi-parameter combined probe, 49 - multi-parameter transmitter. DETAILED DESCRIPTION

[0038] To make the objectives, technical solutions, and advantages of the present invention clearer, the present invention will be further described in detail below with reference to the embodiments and accompanying drawings. The illustrative embodiments and descriptions of the present invention are only used to explain the present invention and are not intended to limit the present invention.

[0039] In the following description, numerous specific details are set forth in order to provide a thorough understanding of the invention. However, it will be apparent to those skilled in the art that these specific details are not necessary to practice the invention. In other embodiments, well-known structures, materials, or methods have not been specifically described in order to avoid obscuring the invention.

[0040] Throughout this specification, references to "an embodiment," "an example," or "an example" mean that a particular feature, structure, or characteristic described in connection with that embodiment or example is included in at least one embodiment of the invention. Therefore, the phrases "an embodiment," "an example," "an example," or "an example" appearing in various places throughout the specification do not necessarily refer to the same embodiment or example. Furthermore, specific features, structures, or characteristics can be combined in one or more embodiments or examples in any suitable combination and / or sub-combination. Moreover, those skilled in the art will understand that the illustrations provided herein are for illustrative purposes and are not necessarily drawn to scale. The term "and / or" as used herein includes any and all combinations of one or more of the associated listed items.

[0041] In the description of this invention, the terms "front," "rear," "left," "right," "up," "down," "vertical," "horizontal," "high," "low," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limiting the scope of protection of this invention.

[0042] Example 1

[0043] like Figure 1 and Figure 2 As shown, this embodiment of the invention provides a partitioned integrated aerobic granular sludge-membrane bioreactor coupling device, including an influent system, a reactor body, an effluent system, a sludge discharge system, and an automatic monitoring and control system.

[0044] The water inlet system comprises a water inlet bucket 1, a water inlet pump 2 and a water inlet pipe 3, two water inlets are arranged on the reactor body, a first water inlet 4 and a second water inlet 5 are symmetrically arranged on the outer shell of the first anoxic zone and the second anoxic zone respectively and are 20 cm away from the bottom of the reactor in the longitudinal direction, the first water inlet 4 and the second water inlet 5 are connected with the water inlet pipe 3, the water inlet pump 2 is arranged on the water inlet pipe 3 and is controlled by a timer, and the device adopts a left-right alternating continuous water inlet mode of the first water inlet 4 and the second water inlet 5, and the alternating period is 2 hours.

[0045] The reactor body is internally provided with a plurality of baffles, so that the inner shell is divided into a plurality of zones, including a first anoxic zone, an aerobic zone, a second anoxic zone, a first sludge selection zone, a second sludge selection zone, a membrane reaction zone and a sludge sedimentation and discharge zone.

[0046] The first anoxic zone is composed of the reactor outer shell, a baffle 6, a baffle 7 and a baffle 8, and a cantilever stirrer 9 is arranged therein.

[0047] The baffle 6 is arranged between the first anoxic zone and the first sludge selection zone and is not connected with the bottom of the reactor, the longitudinal distance between the baffle 6 and the bottom of the reactor is 2 cm, and the bottom of the first anoxic zone and the first sludge selection zone are kept communicated.

[0048] The baffle 7 is connected with the bottom of the reactor and separates the first anoxic zone from the second anoxic zone.

[0049] The baffle 8 is arranged between the first anoxic zone and the aerobic zone and is not connected with the bottom of the reactor, the longitudinal distance between the baffle 8 and the bottom of the reactor is 2 cm, and the bottom of the first anoxic zone and the aerobic zone are kept communicated.

[0050] The arrangement of the cantilever stirrer 9 provides hydraulic mixing and stirring for the first anoxic zone and provides downward thrust for the sludge-water mixture, so that the sludge-water mixture in the first anoxic zone enters the aerobic zone through the bottom of the baffle 8 and realizes infinite vertical circular flow and large circulation of the sludge-water mixture between the first anoxic zone and the aerobic zone.

[0051] The aerobic zone is composed of an arc-shaped reactor outer shell, the baffle 8 and a baffle 10, and an aeration assembly 1 is arranged at the bottom of the aerobic zone.

[0052] The baffle 8 is arranged between the first anoxic zone and the aerobic zone and is not connected with the bottom of the reactor, the longitudinal distance between the baffle 8 and the bottom of the reactor is 2 cm, and the bottom of the first anoxic zone and the aerobic zone are kept communicated.

[0053] The baffle 10 is arranged between the aerobic zone and the second anoxic zone and is not connected with the bottom of the reactor, the longitudinal distance between the baffle 10 and the bottom of the reactor is 2 cm, and the bottom of the aerobic zone and the second anoxic zone are kept communicated.

[0054] The aeration assembly one is composed of an aeration machine 11, an air inlet pipe 14, a gas flow meter 12, a check valve 13 and a nano-aeration plate 15 inside the reactor. The aeration flow is adjusted based on the online dissolved oxygen concentration monitoring through the gas flow meter 12 to control the dissolved oxygen concentration to be 3-4 mg / L.

[0055] The aeration assembly one in the aerobic zone can provide stable and continuous aeration for the system, and mainly achieve the following three goals: 1) providing dissolved oxygen for microbial growth and metabolism to achieve degradation of pollutants; 2) the airflow generated by aeration can mix and agitate the sludge in the aerobic zone to make it uniformly mixed and avoid the generation of dead zones; 3) providing water power to push the sludge-water mixture in the aerobic zone to flow upward and enter the anoxic zone one and the anoxic zone two through the upper end of the baffle three 8 and the baffle four 10 to realize infinite vertical circulation of the sludge-water mixture between the aerobic zone and the anoxic zone one and the anoxic zone two.

[0056] The anoxic zone two is composed of a reactor shell, a baffle two 7, a baffle four 10, a baffle five 17, and a cantilever agitator two 16.

[0057] The baffle two 7 is connected to the bottom of the reactor to separate the anoxic zone two from the anoxic zone one.

[0058] The baffle four 10 is arranged between the anoxic zone two and the aerobic zone and is not connected to the bottom of the reactor, with a longitudinal distance of 2 cm, keeping the anoxic zone two communicated with the bottom of the aerobic zone.

[0059] The baffle five 17 is arranged between the anoxic zone two and the sludge selection zone two and is not connected to the bottom of the reactor, with a longitudinal distance of 2 cm, keeping the anoxic zone two communicated with the bottom of the sludge selection zone two.

[0060] The arrangement of the cantilever agitator provides hydraulic mixing and stirring for the anoxic zone two, and provides downward thrust for the sludge-water mixture to push the sludge-water mixture in the anoxic zone two to enter the aerobic zone through the bottom of the baffle four 10, realizing infinite vertical circulation of the sludge-water mixture between the anoxic zone two and the aerobic zone.

[0061] The sludge selection zone one is composed of a reactor shell, a baffle one 6, a baffle six 18 and a baffle seven 19. The baffle one 6 is not connected to the bottom of the reactor, with a longitudinal distance of 2 cm from the bottom of the reactor, keeping the sludge selection zone one communicated with the bottom of the anoxic zone one. The baffle six 18 and the baffle seven 19 are both connected to the bottom of the reactor.

[0062] The sludge selection zone two is composed of a reactor shell, a baffle five 17, a baffle six 18 and a baffle eight 20. The baffle five 17 is not connected to the bottom of the reactor, with a longitudinal distance of 2 cm from the bottom of the reactor, keeping the sludge selection zone two communicated with the bottom of the anoxic zone two. The baffle six 18 and the baffle eight 20 are both connected to the bottom of the reactor.

[0063] The membrane reaction zone is composed of the reactor shell, baffle 7 19, baffle 8 20, baffle 9 21, baffle 10 22, baffle 11 23, baffle 12 24, membrane module, and aeration assembly 2.

[0064] Baffle 7 19 and baffle 8 20 are connected to the reactor bottom; baffle 9 21 and baffle 10 22 are not connected to the reactor bottom, with a longitudinal spacing of 2 cm from the reactor bottom; baffle 11 23 is connected to the lower end of baffle 9 21 and is inclined at an angle of 70° longitudinally to baffle 9 21; baffle 12 24 is connected to the lower end of baffle 10 22 and is inclined at an angle of 70° longitudinally to baffle 10 22; baffle 11 23 and baffle 12 24 are not connected, with a horizontal spacing of 6 cm, forming a water flow channel.

[0065] The membrane module material is preferably a hollow flat ceramic membrane module 25, but is not limited to a hollow flat ceramic membrane. The membrane pore size is <0.1 μm, the effective area of the membrane is 0.15 m 2 , and the membrane flux is 19.8 L / h / m 2 .

[0066] Aeration assembly 2 is composed of aeration machine 2 26, air inlet pipe 2 29, gas flow meter 2 27, check valve 2 28, and internal nano-aeration plate 2 30, which are arranged outside the reactor. Nano-aeration plate 2 30 is placed above baffle 11 23 and baffle 12 24. The aeration amount is adjusted by gas flow meter 2 27, and the aeration amount is 4 L / min. Nano-aeration plate 2 30 is placed at the lower end of the hollow flat ceramic membrane module 25, with a longitudinal spacing of 5 cm from the bottom of the hollow flat ceramic membrane module 25. Aeration assembly 2 is provided to provide continuous aeration to flush the membrane module and alleviate membrane fouling.

[0067] The sediment sludge discharge zone is composed of sedimentation zone 1, sedimentation zone 2, and the sludge discharge zone at the bottom.

[0068] Sedimentation zone 1 is composed of baffle 7 19, baffle 9 21, baffle 11 23, and the reactor shell, and is connected to the sludge selection zone 1 through electromagnetic valve 1 32. The water inlet of electromagnetic valve 1 31 is located in the sludge selection zone 1 reactor shell, with a longitudinal distance of 5 cm from the reactor top. The water outlet of electromagnetic valve 1 33 is located in the sedimentation zone 1 reactor shell, with a longitudinal distance of 5 cm from the reactor bottom. The sludge-water mixture enters the sedimentation zone 1 through electromagnetic valve 1 32 from the sludge selection zone 1 by gravity.

[0069] The second sedimentation zone is composed of baffle 8 20, baffle 10 22, baffle 12 24 and the reactor shell, and is connected with the second sludge selection zone through electromagnetic valve 2 35. The water inlet of electromagnetic valve 2 34 is located on the reactor shell of the second sludge selection zone, and is longitudinally 5 cm from the top of the reactor. The water outlet of electromagnetic valve 2 36 is located on the reactor shell of the second sedimentation zone, and is longitudinally 5 cm from the bottom of the reactor. The mixture of sludge and water flows into the second sedimentation zone from the second sludge selection zone through electromagnetic valve 2 35 by gravity. Electromagnetic valve 2 35 and the related water inlets and outlets are symmetrically distributed on the left and right sides of the reactor shell with electromagnetic valve 1 32 and the related water inlets and outlets.

[0070] The water inlet and electromagnetic valve 1 32 and electromagnetic valve 2 35 are controlled by a timer. When the water inlet is connected to the system through water inlet 1 4 in the first anoxic zone, electromagnetic valve 2 35 is opened; when the water inlet is connected to the system through water inlet 2 5 in the second anoxic zone, electromagnetic valve 1 32 is opened; the water inlet 1 4 and water inlet 2 5 alternate continuously for 2 hours. The unique water inlet mode makes the sewage / wastewater alternately run in two dynamic lines, dynamic line 1: water inlet 1 - first anoxic zone - aerobic zone - second anoxic zone - second sludge selection zone - second sedimentation zone - membrane reaction zone, dynamic line 2: water inlet 2 - second anoxic zone - aerobic zone - first anoxic zone - first sludge selection zone - first sedimentation zone - membrane reaction zone, with an alternating period of 2 hours.

[0071] The first sedimentation zone and the second sedimentation zone are connected at the bottom to form a sludge discharge zone. The sludge discharge zone is located at the lower end of the membrane reaction zone and is separated from the membrane reaction zone by baffle 11 23 and baffle 12 24. Baffle 11 23 and baffle 12 24 are not connected and are horizontally spaced 6 cm apart to form a water flow channel.

[0072] The water outlet system of the device is composed of hollow flat ceramic membrane assembly 25, water collection port 37, water outlet pipe 41, pressure sensor 39, paperless recorder 38, bidirectional centrifugal pump 40 and water outlet bucket 42. The water collection port 37 of the hollow flat ceramic membrane assembly 25 is connected with the water outlet pipe 41, and the water is pumped by the bidirectional centrifugal pump 40 to provide pressure for water production. One water production cycle is 10 minutes, and the pump's pumping and stopping ratio is 7:3 (minutes). During the operation of the device, the direction of rotation of the bidirectional centrifugal pump 40 is switched to suck water from the water outlet bucket 42 to perform online backwashing of the membrane assembly. The backwashing time is 1 minute in one water production cycle, and the backwashing flow rate is 5.95 L / h. When the transmembrane pressure difference displayed by the pressure sensor 39 reaches 30 KPa or more, it is considered that the membrane has been seriously polluted, and the operation cycle of the reactor is ended. The contaminated membrane assembly is taken out of the reactor, cleaned by physical cleaning and chemical agent immersion, and then put back into the reactor for reuse.

[0073] The sludge discharge system of the device is composed of sludge discharge port 43, sludge discharge pipe 44, sludge discharge pump 45 and residual sludge collector 46, and the sludge discharge port is arranged at the lower end of the sedimentation sludge discharge zone.

[0074] The automatic monitoring control system of the device comprises a multi-parameter combined probe 48 (including pH, ORP and temperature parameters) arranged in the anoxic zone, a dissolved oxygen probe 47, a pressure sensor 39, a paperless recorder 38 and a multi-parameter transmitter 49 arranged in the aerobic zone, and can realize online monitoring of multiple parameters such as pH, dissolved oxygen, ORP, temperature and pressure.

[0075] When the device is in use, sewage enters the anoxic zone I through the water inlet system, and is mixed with inoculated sludge uniformly under the action of the cantilever stirrer I 9 and does directional spiral motion. Under the downward thrust of the stirring paddle, the sludge-water mixture enters the bottom of the aerobic zone through the overflow port at the lower end of the baffle III 8. The regular and stable spiral ring motion provides good shear force for the sludge-water mixture, increases the collision opportunity of microorganisms, and is helpful to the agglomeration of microorganisms and the formation of granular sludge.

[0076] The sludge-water mixture entering the bottom of the aerobic zone obtains continuous power under the continuous aeration of the aeration assembly I, and does infinite rolling and falling ring motion in the vertical direction. The regular ring motion can provide stable hydraulic shear force for the fluid, promote the collision and agglomeration of flocculent sludge, and strengthen the granulation of flocculent sludge. In addition, the continuous aeration provides the sludge-water mixture with rising kinetic energy, pushes the sludge-water mixture to flow upwards to the horizontal surface, and disperses into the anoxic zone I and the anoxic zone II along the periphery. The setting of the aeration realizes the vertical infinite circulation of the sludge-water mixture between the aerobic zone and the anoxic zone I and the anoxic zone II.

[0077] The sludge-water mixture entering the anoxic zone II also does spiral ring motion under the action of the cantilever stirrer II 16, creates good shear force and hydraulic conditions, and is beneficial to the collision and granulation of flocculent sludge. Under the downward thrust of the stirring paddle, part of the sludge-water mixture flows back to the bottom of the aerobic zone through the overflow port at the lower end of the baffle IV 10, and part of the sludge-water mixture enters the sludge selection zone II through the overflow port at the lower end of the baffle V 17.

[0078] In the sludge selection zone II, sludge with good settling performance precipitates at the bottom and returns to the anoxic zone II under the hydraulic action of the cantilever stirrer II in the anoxic zone II, and continues to circulate between the anoxic zone and the aerobic zone. Flocculent sludge with poor settling performance flows into the precipitation zone II with the effluent through the water inlet of the electromagnetic valve II 34. The sludge selection zone excludes sludge with poor settling performance and retains sludge with good settling performance according to the difference in sludge settling performance, and realizes the selection of sludge.

[0079] The sludge entering the precipitation zone II enters the bottom sludge discharge zone under the action of gravity and water power, and the effluent with less sludge enters the membrane reaction zone through the overflow surface between the baffle XI 23 and the baffle XII 24. The setting of the precipitation zone and the sludge discharge zone separates the residual sludge from the membrane reaction zone, realizes the concentration and discharge of sludge, and also reduces the content of microorganisms in the membrane reaction zone, slows down the membrane pollution.

[0080] The residual sludge entering the bottom sludge discharge area is discharged through the sludge discharge system, maintaining the metabolism and growth of the microorganisms in the system.

[0081] The effluent entering the membrane reaction area is removed of flocs by the filtration of the ceramic membrane assembly and is discharged through the effluent system. The membrane reaction area is provided with an aeration device, and the rising bubbles continuously scour the membrane assembly, causing the sludge deposited on the membrane assembly to fall off, reducing the concentration polarization phenomenon and slowing down the membrane pollution. Thus, the sewage / wastewater completes the route 1: water inlet one-anoxic area-oxygen area-anoxic area two-selective sludge area two-settling area two-membrane reaction area.

[0082] When the reactor is fed with water through the water inlet one for 2 hours, the sewage / wastewater enters the anoxic area two through the water inlet two. Under the action of the agitator, the sludge-water mixture is uniformly mixed and does directional spiral motion. Under the downward thrust of the stirring paddle, the sludge-water mixture enters the bottom of the oxygen area through the lower end overflow of the baffle four 10. The regular and stable spiral ring motion provides good shear force for the sludge-water mixture, increasing the collision opportunities of the microorganisms, which helps the agglomeration of the microorganisms and the formation of granular sludge.

[0083] The sludge-water mixture entering the bottom of the oxygen area obtains continuous power under continuous aeration and does infinite rolling and falling ring motion in the vertical direction. The regular ring motion can provide stable hydraulic shear force for the fluid, promoting the collision and agglomeration of the flocculent sludge and strengthening the granulation of the flocculent sludge. In addition, the continuous aeration provides the sludge-water mixture with rising kinetic energy, pushing the sludge-water mixture to flow upward to the horizontal surface and disperse into the anoxic area one and the anoxic area two along the periphery. The setting of the aeration realizes the vertical infinite circulation of the sludge-water mixture between the oxygen area and the anoxic area one and the anoxic area two.

[0084] The sludge-water mixture entering the anoxic area one also does spiral ring motion under the action of the agitator, creating good shear force and hydraulic conditions, which is beneficial to the collision and granulation of the flocculent sludge. Under the downward thrust of the stirring paddle, part of the sludge-water mixture flows back to the bottom of the oxygen area through the lower end overflow of the baffle three 8, and part of the sludge-water mixture enters the selective sludge area one through the lower end overflow of the baffle one 6.

[0085] In the selective sludge area one, the sludge with good settling performance precipitates at the bottom and returns to the anoxic area one under the hydraulic action of the agitator in the anoxic area one, continuing to circulate between the anoxic area and the oxygen area. The flocculent sludge with poor settling effect flows into the settling area one with the effluent through the water inlet 31 of the electromagnetic valve one. The selective sludge area excludes the sludge with poor settling performance and retains the sludge with good settling performance, realizing the selection of the sludge.

[0086] The sludge entering the sludge sedimentation zone one is under the action of gravity and water power, and enters the bottom sludge discharge zone, and the effluent with less sludge enters the membrane reaction zone through the flow surface between the baffle eleven 23 and the baffle twelve 24.

[0087] The residual sludge entering the bottom sludge discharge zone is discharged through the sludge discharge system, so as to maintain the metabolism and growth of microorganisms in the system.

[0088] The effluent entering the membrane reaction zone removes the floc under the filtration of the ceramic membrane assembly, and is discharged through the effluent system. At this time, the sewage / wastewater completes the operation of the line 2 (line 2: water inlet two-anoxic zone two-oxygen zone-anoxic zone one-sludge selection zone one-sludge sedimentation zone one-membrane reaction zone).

[0089] The currently generally recognized granulation theory of aerobic granular sludge is as follows: (1) mutual collision between cells to produce initial cell adhesion; (2) increase of cell surface hydrophobicity to enhance initial cohesion of cells, and self-cohesion of cells to produce micro-aggregates; (3) large amount of extracellular polymers produced by aggregated microorganisms to further promote irreversible aggregation and growth of microbial populations; and (4) under the action of flexible shear force formed by bubbles and water flow, the microbial populations continuously aggregate into granules. The formation process of the granules is affected by multiple fluid dynamics parameters, and the settling velocity selection pressure, periodic satiation-starvation cycle and hydraulic shear force are the main factors driving the aerobic granulation of activated sludge in the sequencing batch system.

[0090] The biological granules with larger density generally settle faster than the biological granules with smaller density. Under the settling velocity selection pressure, the biological mass with good settling performance is retained in the system, and the biological mass with poor settling performance is washed out of the reactor. Through this selection pressure, the granular sludge with good settling performance can be screened, and in addition, the cell hydrophobicity and synthesis of extracellular polymers are also improved under this selection pressure, which can promote the hydrophobic aggregation of microorganisms. Therefore, the settling velocity selection pressure is considered as a decisive factor for successful formation of aerobic granules.

[0091] The hydraulic shear force is considered as a key factor as important as the settling velocity selection pressure, and is the first driving force of the granulation process. In the granulation process, the hydraulic flow can make the microorganisms continuously collide and aggregate; at the same time, the shear force generated by aeration and stirring can induce the secretion of extracellular polymers, so as to enhance the cell surface hydrophobicity, and further promote the formation of granules; in addition, the shear force also has an important influence on the shape and size of the aerobic granules, and can strip the aging bacteria and filamentous bacteria on the surface of the mature granules, and plays a balancing role on the growth speed of the cells on the outer layer of the granules.

[0092] Studies have shown that periodic satiation-hunger cycle can promote the secretion of a large number of extracellular polymers by microorganisms, enhance the hydrophobicity of microbial cells, and be conducive to the adhesion and aggregation between microorganisms. In addition, the alternation of satiation-hunger conditions can inhibit the reproduction of filamentous microorganisms and be conducive to the growth of flocculating bacteria, thereby maintaining the stability of AGS. Therefore, the periodic satiation-hunger cycle is also considered as a main influencing factor for the formation of aerobic granules.

[0093] The device of the present application creates good necessary conditions for the formation of granular sludge under continuous flow conditions through special structure and operation mode. The sewage / wastewater is alternately operated through two dynamic lines (dynamic line 1: water inlet one-anoxic zone-aerobic zone-anoxic zone two-sludge selection zone two-settling zone two-membrane reaction zone, dynamic line 2: water inlet two-anoxic zone two-aerobic zone-anoxic zone one-sludge selection zone one-settling zone one-membrane reaction zone), which creates a periodic satiation-hunger cycle and promotes the formation of granular sludge. The setting of the anoxic zone agitator and the aerobic zone aeration device creates numerous circumferential water flow patterns in the system, realizes the infinite vertical circulation between the aerobic zone and the anoxic zone one and the anoxic zone two, provides sufficient shear force for the system, and promotes the collision of flocculent sludge and the formation of granular sludge. The setting of the sludge selection zone fully utilizes the difference in sludge settling performance, retains sludge with good settling performance, and excludes sludge with poor settling performance, thereby better achieving sludge selection. Based on the special structure and operation mode of the device, settling velocity selection pressure, periodic satiation-hunger cycle and hydraulic shear force are created under continuous flow conditions, which can realize the rapid formation and stable operation of aerobic granular sludge under continuous flow conditions.

[0094] Example 2

[0095] The present application provides a method for culturing aerobic granular sludge by using the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device of example 1.

[0096] The activated sludge at the end of the biochemical tank of a municipal wastewater treatment plant is used as the inoculated sludge of the device, the initial sludge concentration is 4 g / L, MLVSS / MLSS = 0.57, and 90% of the sludge particle size is <165 μm.

[0097] The sludge is cultured by using artificial synthetic wastewater as the influent, and the influent quality is shown in Table 1. Sodium acetate and glucose are used as carbon sources, NH4Cl is used as nitrogen source, and K2HPO4·3H2O and KH2PO4 are used as phosphorus sources. The influent COD is about 350 mg / L, NH4 + -N is 30 mg / L, TN is 30 mg / L, and TP is 5 mg / L. At the same time, in order to meet the needs of the growth process of microorganisms, Fe, Cu, Mn, Zn and other trace elements are also added to the synthetic wastewater.

[0098] The effective height of the device liquid level is controlled to be 25 cm, the hydraulic retention time is set to be 8 h, the pH of the inlet water is about 7.0, the temperature is about 25℃, the dissolved oxygen in the aerobic zone is 3-4 mg / L. The effluent water is produced by hollow flat ceramic membrane, the effective area of the ceramic membrane is 0.15 m 2 , the membrane pore size is 0.1 μm, the effluent water is produced by constant current mode, the peristaltic pump pumping stop ratio (minute 7:3), the effluent membrane flux is 19.8 L / (m 2 *h).

[0099] Table 1

[0100]

[0101]

[0102] The wastewater is introduced into the device through the inlet system, and the alternating water inlet of inlet one and inlet two is realized by the timer control, and the alternating period is 2 hours. Thus, the wastewater is alternately operated in two dynamic lines (dynamic line 1: inlet one-anoxic zone-one-aerobic zone-two-anoxic zone-two-sedimentation zone two-membrane reaction zone, dynamic line 2: inlet two-two-anoxic zone-aerobic zone-one-anoxic zone-one-sedimentation zone one-membrane reaction zone). The special water inlet mode of the embodiment of the application creates a periodic satiation-hunger cycle condition for the system, which can induce the secretion of extracellular polymers and enhance the hydrophobicity of the microbial cell surface, so as to promote the formation of cell aggregates. In addition, the filamentous bacteria rapidly expand outward during the satiation period, and the filamentous structure shrinks during the hunger period, and the satiation-hunger alternation can significantly improve the settling performance of the sludge and maintain the stability of the aerobic granular sludge. Therefore, the left-right alternating water inlet operation mode creates one of the necessary conditions for the system granular sludge formation, that is, the periodic satiation-hunger cycle.

[0103] The sewage entering the anoxic zone is mixed quickly under the action of the agitator and does directional spiral movement. Under the downward thrust of the agitating paddle, the sludge-water mixture passes through the flow port at the lower end of the anoxic zone and enters the bottom of the aerobic zone. In the aerobic zone, the continuous aeration provides the sludge-water mixture with constant power, which pushes the sludge-water mixture to rise and do infinite vertical rolling and circular movement. The sludge-water mixture reaching the horizontal plane of the aerobic zone disperses along the periphery, and a small part of the sludge returns to the primary anoxic zone to continue the circulation, and most of the sludge enters the secondary anoxic zone under the hydraulic drive. The sludge entering the secondary anoxic zone also does directional spiral movement under the action of the agitator, and under the downward thrust, part of the sludge enters the sludge selection zone, and part of the sludge returns to the aerobic zone to enter a new round of circulation. The combination of agitation and aeration provides sufficient hydraulic conditions for the system and realizes the vertical infinite circulation of the sludge-water mixture between the aerobic zone and the anoxic zone. The regular and stable spiral movement and circular movement provide stable hydraulic shear force for the fluid. The hydraulic shear force has an important influence on the formation and structure of the aerobic granular sludge. High hydraulic shear force helps the collision and coagulation of the flocculent sludge, promotes the granulation of the flocculent sludge, and at the same time helps to remove the rapidly growing filamentous bacteria accumulated on the surface of the granules, shearing the aerobic granules into regular and compact spherical shapes. In addition, the shear force has been proved to induce the secretion of extracellular polymeric substances and enhance the hydrophobicity of the cell surface. Therefore, the device combines agitation and aeration to create the necessary conditions for granular sludge formation, namely hydraulic shear force.

[0104] The sludge entering the sludge selection zone is settled according to the difference in sludge settling velocity, and the sludge with good settling performance is precipitated at the bottom of the device and taken back to the anoxic zone by the hydraulic circulation of the anoxic zone to continue the circulation movement between the anoxic zone and the aerobic zone. The flocculent sludge with poor settling effect is discharged with the effluent through the electromagnetic valve into the sedimentation zone. The selection pressure based on the settling velocity is the determining factor for the granulation of the sludge in the sequencing batch reactor. The settling velocity of the granular sludge is greater than that of the flocculent sludge. The setting of the sludge selection zone fully utilizes the difference in the settling performance of the sludge, selects the aggregates with good settling performance, and eliminates the flocculent sludge with poor settling performance. At the same time, the settling velocity selection pressure can also promote the production of extracellular polymeric substances, improve the hydrophobicity of the cell surface, and enhance the hydrophobicity of the microorganisms. Therefore, the setting of the sludge selection zone of the device creates the necessary conditions for the formation of granular sludge under continuous flow conditions, namely the settling velocity selection pressure.

[0105] The sludge-water mixture entering the sedimentation and sludge discharge zone enters the bottom sludge discharge zone under the action of gravity and hydraulic drive, and the effluent with less sludge enters the membrane reaction zone through the flow surface between the baffle eleven 23 and the baffle twelve 24. The setting of the sedimentation and sludge discharge zone separates the residual sludge from the effluent, realizes the concentration and discharge of the sludge, and also reduces the content of suspended solids in the membrane reaction zone, slowing down the membrane pollution.

[0106] The device of the present application creates three necessary conditions (sedimentation velocity selection pressure, periodic satiation-hunger cycle and hydraulic shear force) for the formation of aerobic granular sludge under continuous flow conditions through special structure and operation mode, solves the technical problem that aerobic granular sludge is difficult to form under the current continuous flow conditions, and realizes the rapid start-up and stable operation of aerobic granular sludge.

[0107] Through 30 days of cultivation, aerobic granular sludge is successfully cultivated in the coupling device described in Example 1 of the present application, Figure 3 Microscope pictures and real photos of the inoculated sludge and the sludge after 30 days of cultivation are presented. Laser particle size analyzer test results show that 50% of the inoculated sludge particle size is less than 77.5 μm, 90% of the inoculated sludge particle size is less than 165 μm, and after 30 days of cultivation, 50% of the sludge particle size in the system is greater than 342 μm, and 10% of the sludge particle size is greater than 1000 μm. This shows that under the special structure and operation mode of the device of the present application, the system can realize the rapid formation of aerobic granular sludge under continuous flow conditions, and the formation of granular sludge significantly reduces the rate of membrane fouling.

[0108] Example 3

[0109] The present application provides a kind of aerobic granular sludge cultivated by example 2 and the coupling device described in example 1 for treating low concentration sewage.

[0110] To further verify the application and efficiency of the device for treating low concentration sewage, the aerobic granular sludge system cultivated by example 2 is used to treat low concentration artificial synthetic sewage. The water quality of low concentration artificial synthetic sewage is shown in Table 2. Sodium acetate and glucose are used as carbon source, NH4Cl is used as nitrogen source, K2HPO4·3H2O and KH2PO4 are used as phosphorus source, and Fe, Cu, Mn, Zn and other trace elements are also added to meet the needs of microbial growth during the synthesis of sewage. The influent COD is 150 mg / L, NH4 + N is 30 mg / L, TN is 30 mg / L, TP is 5 mg / L, and COD:N:P is 30:6:1.

[0111] The sewage is introduced into the device through the anoxic zone of the influent system, and the timer control is used to realize the alternate water inlet of inlet one and inlet two with an alternate period of 2 hours. The effective height of the liquid surface of the device is controlled to be 25 cm, the hydraulic retention time is set to be 8 h, the influent pH is about 7.0, the temperature is about 25℃, and the dissolved oxygen in the aerobic zone is 3-4 mg / L. The effluent is produced by hollow flat ceramic membrane, the effective area of the ceramic membrane is 0.15 m 2 , the membrane pore size is 0.1 μm, the effluent is produced by constant flow mode, the peristaltic pump pumping stop ratio (minute 7:3), and the effluent membrane flux is 19.8 L / (m 2 *h).

[0112] Table 2

[0113]

[0114]

[0115] The coupling device of the present application, after the reactor is started by using the above-mentioned process to cultivate aerobic granular sludge, the specific process of wastewater treatment is as follows:

[0116] The target wastewater is continuously introduced into the device through the water inlet system, and the water inlet pump is controlled by the timer to ensure that the water can be alternately and continuously introduced on both sides, so that the wastewater can be alternately operated in two dynamic lines, dynamic line 1: water inlet one-anoxic zone-oxygen zone-anoxic zone two-selective sludge zone two-settling zone two-membrane reaction zone, dynamic line 2: water inlet two-anoxic zone two-oxygen zone-anoxic zone one-selective sludge zone one-settling zone one-membrane reaction zone, and the alternate cycle is 2 hours.

[0117] When dynamic line 1 is operated, the wastewater first enters the anoxic zone one, and under the action of the stirring paddle, the sludge-water mixture is quickly mixed, and the microorganisms fully utilize the carbon source in the wastewater for denitrification, so as to realize the removal of NO3 - -N and NO2 - -N. With the wastewater entering the oxygen zone, under the action of dissolved oxygen, the microorganisms fully oxidize and decompose organic matter, and at the same time, the ammonia-oxidizing bacteria convert NH4 + -N in the wastewater into NO3 - -N and NO2 - -N under the aerobic condition. In the continuous aeration upflow, the wastewater containing NO3 - -N and NO2 - -N quickly rises with the bubbles and flows horizontally into the anoxic zone one and the anoxic zone two at the top of the oxygen zone. The sludge returned to the anoxic zone one starts a new cycle, and the sludge-water mixture entering the anoxic zone two further carries out denitrification reaction under the second-stage anoxic condition. At the same time, the sludge fully absorbing phosphorus enters the selective sludge zone two from the lower end of the baffle five 17, and the sludge with good settling performance is precipitated at the bottom of the selective sludge zone two and returns to the main reaction zone under the hydrodynamic action of the stirring paddle in the anoxic zone two, and participates in the cycle again, while the sludge with poor settling performance enters the sludge settling and discharging zone through the electromagnetic valve two and is discharged by the sludge discharging system. The effluent enters the membrane reaction zone through the overflow surface between the baffle eleven 23 and the baffle twelve 24, is filtered by the ceramic membrane assembly, and the water quality is further improved and discharged.

[0118] When the device is operated in the mode of flow line 2, the sewage undergoes the same treatment process, only the flow direction is changed. The sewage first enters the second anoxic zone. Under the action of the stirring paddle, the sludge-water mixture is quickly mixed, and the microorganisms fully utilize the carbon source in the sewage for denitrification, so that NO3 - -N and NO2 - -N is removed. With the sewage entering the aerobic zone, the microorganisms fully oxidize and decompose the organic matter under the action of dissolved oxygen, and the ammonia-oxidizing bacteria convert NH4 + -N in the sewage into NO3 - -N and NO2 - -N under the aerobic condition. In the continuous aeration upflow, the sewage containing NO3 - -N and NO2 - -N is quickly lifted by the bubbles and flows horizontally into the first anoxic zone and the second anoxic zone at the top of the aerobic zone. The sludge returned to the second anoxic zone starts a new cycle, and the sludge-water mixture entering the first anoxic zone further undergoes denitrification under the second anoxic condition. Meanwhile, the sludge fully absorbing phosphorus enters the first sludge selection zone from the lower end of the baffle 6, and the sludge with good settling performance is precipitated at the bottom of the first sludge selection zone and returns to the main reaction zone under the action of the water power generated by the stirring paddle in the first anoxic zone to participate in the cycle again, while the sludge with poor settling performance enters the sludge precipitation and discharge zone through the electromagnetic valve 32 and is discharged by the sludge discharge system. The effluent enters the membrane reaction zone through the overflow surface between the baffle 11 23 and the baffle 12 24, is filtered by the ceramic membrane assembly, and is further discharged to improve the effluent quality.

[0119] The multiple chambers of the device create different habitat conditions such as aerobic, anoxic and anaerobic, and create a good growth and enrichment environment for the C, N and P efficient removal bacterial flora. The cyclic operation of the multiple chambers realizes the synergistic and efficient removal of C, N and P, and the AOA operation mode created in time and space, and the setting of the second anoxic zone can realize the deep denitrification of the sewage / wastewater. Combined with the efficient filtering effect of the ceramic membrane assembly, the suspended solids and colloidal substances in the sewage / wastewater are intercepted, and the effluent quality is significantly improved. Under the special structure and operation mode of the device, the rich functional microbial flora collide, agglomerate and granulate, forming aerobic granular sludge with external aerobic, middle anoxic and internal anaerobic, which further shortens the nitrification, denitrification and phosphorus removal process, strengthens the synergistic removal of C, N and P, and improves the treatment load and impact load capacity of the system.

[0120] The system is stably operated under this condition for 25 days, and the operation effect is shown in Table 1 Figure 4 , the average removal rate of COD is 92.7%, the average removal rate of TN is 77.6%, and the average removal rate of TP is 63.8%, the effluent COD is stably below 15 mg / L, and NH4 +-N is lower than 1 mg / L, TN is lower than 8 mg / L, and TP is lower than 3 mg / L, and the effluent can reach the surface water IV class standard except TP and TN. The results show that the device has high sewage treatment capacity, and can also achieve good denitrification for low carbon-nitrogen ratio sewage.

[0121] Example 4

[0122] The embodiment of the application provides a high-concentration sewage treatment device using the aerobic granular sludge cultured in the embodiment 2 and the coupling device in the embodiment 1.

[0123] In order to further verify the application and efficiency of the device in treating high-concentration sewage, the aerobic granular sludge system cultured in the embodiment 2 is used to treat high-concentration artificial synthetic sewage. The quality of the high-concentration artificial synthetic sewage is shown in Table 3, sodium acetate and glucose are used as carbon sources, NH4Cl is used as a nitrogen source, K2HPO4·3H2O and KH2PO4 are used as phosphorus sources, and Fe, Cu, Mn, Zn and other trace elements are also added in the synthetic sewage to meet the needs of microbial growth. The influent COD is 750 mg / L, the influent NH4 + -N is 40 mg / L, TN is 40 mg / L, TP is 10 mg / L, and COD:N:P is 75:4:1.

[0124] The sewage is introduced into the anoxic zone of the device through the influent system, and the influent of the influent port 1 and the influent port 2 is realized alternately by the timer control, and the alternating period is 2 hours. The effective height of the device liquid surface is controlled to be 25 cm, the hydraulic retention time is set to be 8 h, the influent pH is about 7.0, the temperature is about 25℃, and the dissolved oxygen in the aerobic zone is 3-4 mg / L. The effluent is produced by the hollow flat ceramic membrane, the effective area of the ceramic membrane is 0.15 m 2 , the membrane pore size is 0.1 μm, the effluent is obtained by using the constant current mode, the peristaltic pump pumping stop ratio (minute 7:3), and the effluent membrane flux is 19.8 L / (m 2 *h).

[0125] Table 3

[0126]

[0127]

[0128] The system is stably operated for 25 days under the condition, and the operation effect is shown in Figure 5 , the average removal rate of COD is 95.7%, the average removal rate of TN is 90.8%, the average removal rate of TP is 85.5%, the effluent COD is stably lower than 40 mg / L, the effluent NH4 +The effluent can reach the surface water IV class standard except TP and TN, and the effluent can stably reach the surface water IV class standard except TP and TN. The results show that the device has good treatment effect on high-concentration sewage and has strong impact load capacity.

[0129] The above-described specific embodiments explain the purpose, technical solutions and beneficial effects of the present application in further detail. It should be understood that the above-described specific embodiments are merely specific embodiments of the present application and are not used to limit the protection scope of the present application. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims

1. The application of a partitioned integrated aerobic granular sludge-membrane bioreactor coupling device, characterized in that, Cultivation of aerobic granular sludge and sewage treatment The coupling device comprises a reactor body, and an aerobic zone, an anoxic zone, a sludge selection zone and a membrane reaction zone are sequentially arranged in the reactor body along a horizontal direction; The anoxic zone is provided with a vertical baffle two (7), the baffle two (7) separates the anoxic zone into two non-communicating anoxic zone one and anoxic zone two, the anoxic zone one is provided with a water inlet one (4), the anoxic zone two is provided with a water inlet two (5), the bottom of the anoxic zone one and the bottom of the anoxic zone two are respectively communicated with the bottom of the aerobic zone; The sludge selection zone is provided with a vertical baffle six (18), the baffle six (18) separates the sludge selection zone into two non-communicating sludge selection zone one and sludge selection zone two; The bottom of the sludge selection zone one is communicated with the bottom of the anoxic zone one, and the bottom of the sludge selection zone two is communicated with the bottom of the anoxic zone two; The two sides of the membrane reaction zone are respectively provided with a sedimentation zone one and a sedimentation zone two, and the top of the sedimentation zone one and the sedimentation zone two is not communicated with the top of the membrane reaction zone; The sedimentation zone one and the sludge selection zone one are communicated through a solenoid valve one (32), and the sedimentation zone two and the sludge selection zone two are communicated through a solenoid valve two (35); The anoxic zone one is provided with a cantilever stirrer one (9), and the anoxic zone two is provided with a cantilever stirrer two (16); The bottom of the aerobic zone is provided with an aeration assembly one, and the bottom of the membrane reaction zone is provided with an aeration assembly two; When the sewage is introduced into the device through the water inlet one (4) in the anoxic zone one, the solenoid valve two (35) is opened, and the sewage dynamic circuit one is: water inlet one-anoxic zone one-aerobic zone-anoxic zone two-sludge selection zone two-sedimentation zone two-membrane reaction zone; When the sewage is introduced into the device through the water inlet two (5) in the anoxic zone two, the solenoid valve one (32) is opened, and the sewage dynamic circuit two is: water inlet two-anoxic zone two-aerobic zone-anoxic zone one-sludge selection zone one-sedimentation zone one-membrane reaction zone; The sewage is alternately and continuously introduced into the device from the water inlet one (4) and the water inlet two (5) for 2 hours.

2. The use of the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device according to claim 1, characterized in that, The membrane reaction zone is provided with a membrane assembly (25).

3. The use of the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device according to claim 1, characterized in that, The aeration assembly one comprises a nano aeration plate one (15) and an aerator one (11) arranged at the bottom of the aerobic zone, the aerator one (11) and the nano aeration plate one (15) are connected through an air inlet pipe one (14), and the air inlet pipe one (14) is provided with a gas flow meter one (12) and a check valve one (13); The aeration assembly two comprises a nano aeration plate two (30) and an aerator two (26) arranged at the bottom of the membrane reaction zone, the aerator two (26) and the nano aeration plate two (30) are connected through an air inlet pipe two (29), and the air inlet pipe two (29) is provided with a gas flow meter two (27) and a check valve two (28).

4. The use of the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device according to claim 1, characterized in that, The coupling device further comprises a water inlet system, the water inlet system comprises a water inlet bucket (1), the water inlet bucket (1) and the water inlet one (4) and the water inlet two (5) are communicated through a water inlet pipe (3), and the water inlet pipe (3) is provided with a water inlet pump (2).

5. The use of the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device according to claim 2, characterized in that, The coupling device further comprises a water outlet system, which comprises a water outlet barrel (42) connected with the water collecting port (37) of the membrane assembly (25) through a water outlet pipe (41), and a two-way centrifugal pump (40) is installed on the water outlet pipe (41).

6. The use of the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device according to claim 1, characterized in that, The coupling device further comprises a sludge discharge system, the bottoms of the first and second sedimentation zones are communicated to form a sludge discharge zone, the sludge discharge zone is located below the membrane reaction zone, and the bottom of the membrane reaction zone is communicated with the sludge discharge zone; the sludge discharge system comprises a residual sludge collector (46) connected with a sludge discharge port (43) arranged at the bottom of the sludge discharge zone through a sludge discharge pipe (44), and a sludge discharge pump (45) is arranged on the sludge discharge pipe (44).

7. The use of the partitioned integrated aerobic granular sludge-membrane bioreactor coupling device according to claim 1, characterized in that, The coupling device further comprises an automatic monitoring and control system, which comprises a multi-parameter combined probe (48) arranged in the anoxic zone and a dissolved oxygen probe (47) arranged in the aerobic zone, and the multi-parameter combined probe (48) and the dissolved oxygen probe (47) are electrically connected with a multi-parameter transmitter (49).

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