Low-carbon biological treatment system

Abstract

The utility model relates to the technical field of wastewater treatment, in particular to a low-carbon biological treatment system which comprises a pretreatment module, a decarbonization module and a biological denitrification module, the pretreatment module comprises an adjusting tank and a pretreatment section, the adjusting tank is used for homogenizing and homogenizing wastewater entering the adjusting tank, and the pretreatment section is used for removing toxic and harmful pollutants which cannot be biologically degraded; the decarburization module comprises an aeration tank and a sedimentation tank and is used for removing organic matters in the wastewater. An MABR reaction zone and an anaerobic ammonia oxidation reaction zone are integrated into an up-flow reactor, an MABR reaction layer and an anaerobic ammonia oxidation reaction layer are formed in the reactor, multifunctional pollutant removal can be achieved, meanwhile, a pipeline for sludge dredging and discharging is arranged, it is guaranteed that the two processes can complement each other, partition reaction can be achieved, and the effect that the two processes can be recycled is achieved. And the function is not influenced by integrated design.

Description

Technical Field

[0001] This utility model relates to the field of wastewater treatment technology, and more specifically to a low-carbon biological treatment system. Background Technology

[0002] With the continuous development of the economy, more and more enterprises have emerged, and the large amount of pollution discharged by these enterprises has put enormous pressure on the ecological environment. Traditional sewage treatment technology relies on "energy consumption for water quality" and mostly adopts high-energy-consuming water treatment processes, which causes a large amount of energy loss and carbon emissions during the sewage treatment process, which is not conducive to the achievement of dual carbon goals.

[0003] In recent years, with the improvement of industrial levels and the continuous increase in the number of industrial enterprises, the types of wastewater have become increasingly complex. Compared with the past, nitrogenous pollutants in wastewater are constantly increasing, leading to a sustained increase in their impact on the natural environment, endangering the living space of aquatic plants and animals, and causing adverse consequences such as eutrophication of water bodies. Traditional water treatment technologies are gradually becoming inadequate for the new development trend. High-energy-consuming and low-efficiency treatment methods are gradually being replaced, and low-carbon and environmentally friendly biological treatment methods have become a new hotspot in the field of wastewater treatment.

[0004] To address the high power consumption and other issues associated with traditional water treatment methods, a new low-carbon biological treatment system is urgently needed. Utility Model Content

[0005] In view of the technical problems existing in the water treatment technology, this utility model proposes a low-carbon biological treatment system, including a pretreatment module, a decarbonization module and a biological denitrification module;

[0006] The pretreatment module includes an equalization tank and a pretreatment section. The equalization tank is used to homogenize and equalize the wastewater entering the equalization tank, and the pretreatment section is used to remove toxic and harmful pollutants that cannot be degraded by organisms.

[0007] The decarbonization module includes an aeration tank and a sedimentation tank, used to remove organic matter from wastewater;

[0008] The biological denitrification module includes a MABR reaction zone and an anaerobic ammonia oxidation reaction zone;

[0009] The MABR reaction zone and the anaerobic ammonia oxidation reaction zone are located in the upflow reactor. The MABR reaction zone is located below the anaerobic ammonia oxidation reaction zone. Wastewater discharged from the sedimentation tank enters the bottom of the upflow reactor and passes sequentially through the MABR reaction zone for removing COD from the wastewater and the anaerobic ammonia oxidation reaction zone for removing total nitrogen and ammonia nitrogen from the wastewater.

[0010] Preferably, the regulating tank is equipped with an aeration and stirring device or a mechanical stirring device.

[0011] Preferably, the pretreatment section includes one or more combinations of oil separator, flotation tank, sedimentation tank, and coagulation sedimentation tank, and the pretreatment section also includes a triple-effect evaporator and / or an advanced oxidation device.

[0012] Preferably, the MABR reaction zone is provided with a first oxygen-permeable membrane aeration structure and a second oxygen-permeable membrane aeration structure. The first and second oxygen-permeable membrane aeration structures are distributed vertically within the upflow reactor. The first oxygen-permeable membrane aeration structure is located below the second oxygen-permeable membrane aeration structure. Both the first and second oxygen-permeable membrane aeration structures are connected to an aeration fan, which is used to provide oxygen to the first and second oxygen-permeable membrane aeration structures.

[0013] Preferably, the aeration rate of the first oxygen-permeable membrane aeration structure is 0.5 to 1.5 times the COD concentration, and the aeration rate of the second oxygen-permeable membrane aeration structure is 0.25 to 0.5 times the ammonia nitrogen concentration.

[0014] Preferably, the anammox reaction zone is equipped with an anammox sludge hopper and an anammox inlet guide plate. The anammox inlet guide plate is positioned above the anammox sludge hopper. The bottom of the anammox sludge hopper is also connected to a pipe for discharging sludge from the bottom of the anammox sludge hopper and for backwashing the bottom of the anammox sludge hopper.

[0015] Preferably, the end of the pipe is connected to a first pipe and a second pipe. The first pipe is connected to a sludge tank, and the second pipe is connected to a backflushing gas source, which is an ammonia or inert gas source.

[0016] Preferably, the anammox sludge hopper is constructed as an upward-opening bucket-shaped structure, including a bottom surface and a side wall surface, wherein the angle between the side wall surface and the bottom surface is β, and β = 60 ± 5°.

[0017] Preferably, the anaerobic ammonia oxidation influent guide plate is configured to extend inward from the inner wall of the upflow reactor, and the included angle between the anaerobic ammonia oxidation influent guide plate and the inner wall of the upflow reactor is α, where α = 55 ± 5°.

[0018] Preferably, the lower end of the anammox influent guide plate extends below the upper edge of the anammox sludge hopper and is located inside the opening of the anammox sludge hopper.

[0019] Compared with the prior art, the advantages of this utility model are:

[0020] Convenient and flexible: This utility model sets up a pretreatment section before the decarbonization module, which can select the pretreatment process according to different water quality types. It is applicable to a variety of water quality types. The subsequent decarbonization module, MABR reaction zone and anaerobic ammonia oxidation reaction zone can effectively achieve the effects of denitrification and COD reduction.

[0021] Energy-saving and low-carbon: The MABR and anaerobic ammonia oxidation technologies are highly integrated into the upflow reactor. The oxygen-permeable membrane system provides high oxygen conversion efficiency, reducing aeration volume by 50-70% compared to traditional processes. Furthermore, no additional carbon source is required during the process to ensure high treatment efficiency, significantly reducing operating energy consumption. The entire system produces less sludge, reducing equipment investment and operating energy consumption for sludge treatment.

[0022] Smaller footprint: Because it integrates MABR and anaerobic ammonia oxidation processes, there is no need to add intermediate lifting units. The two processes complement each other. Through precise control of aeration, it provides a low dissolved oxygen and anaerobic environment to promote the smooth progress of nitrification and anaerobic ammonia oxidation reactions. Compared with traditional aerobic processes, it can save at least 3 to 4 times the tank volume.

[0023] Better results: In terms of COD removal and denitrification, multiple processes complement each other, achieving the removal of major pollutants without high energy consumption, thus truly realizing low-carbon treatment. Attached Figure Description

[0024] The accompanying drawings are not intended to be drawn to scale. In the drawings, each identical or nearly identical component shown in the various figures may be denoted by the same reference numeral. For clarity, not every component is labeled in each figure. Embodiments of various aspects of the present invention will now be described by way of example and with reference to the accompanying drawings, wherein:

[0025] Figure 1 This is a schematic diagram of the structure of the low-carbon biological treatment system shown in this utility model;

[0026] Figure 2 This is a schematic diagram of the upflow reactor shown in this utility model. Detailed Implementation

[0027] To better understand the technical content of this utility model, specific embodiments are provided below in conjunction with the accompanying drawings.

[0028] Combination Figure 1 and Figure 2 As shown, this utility model proposes a low-carbon biological treatment system, including a pretreatment module 10, a decarbonization module 20, and a biological denitrification module.

[0029] The pretreatment module 10 includes an equalization tank 11 and a pretreatment section 12. The equalization tank 11 is used to homogenize and equalize the wastewater entering the equalization tank 11.

[0030] The equalization tank 11 is located before the pretreatment section 12. The main function of the equalization tank 11 is to equalize the quality and quantity, so that the sewage entering the equalization tank 11 can be fully mixed and regulated, reducing the hydraulic impact on subsequent sections.

[0031] Optionally, the equalization tank 11 is equipped with an aeration and stirring device or a mechanical stirring device.

[0032] Specifically, wastewater is pumped up by a water pump or other means, flows through a screen to remove most of the suspended solids and fibrous impurities, and then enters the equalization tank 11. Optionally, the equalization tank 11 can be selectively equipped with aeration or mechanical stirring according to different water quality types to ensure good mixing effect and achieve homogeneity and uniformity.

[0033] The purpose of the pretreatment section 12 is to remove some toxic, harmful or difficult-to-biodegrade pollutants. This is a protective measure for the subsequent decarbonization module 20 and biological denitrification module, and also a necessary pretreatment measure to ensure that the effluent meets the standards.

[0034] Optionally, the pretreatment section 12 can select different pretreatment processes according to the type of water quality. For example, it can use processes such as oil separator, air flotation, grit chamber (sedimentation tank), coagulation sedimentation, triple-effect evaporation, etc. It can also use advanced oxidation processes, such as ozone advanced oxidation (including catalytic oxidation), Fenton, ultrasonic oxidation, photocatalytic oxidation, etc., or a combination of several processes. After the pretreatment section, the water meets the requirements for entering the decarbonization module 20.

[0035] Furthermore, if the wastewater requires phosphorus removal, chemical phosphorus removal can be implemented in the pretreatment stage.

[0036] Furthermore, the decarbonization module 20 includes an aeration tank 21 and a sedimentation tank 22 for removing organic matter from wastewater.

[0037] Among them, the decarbonization module 20 focuses on removing organic matter from wastewater. Specifically, the wastewater stays in the aeration tank 21 for 2 to 4 hours and in the sedimentation tank 22 for 1 to 1.5 hours. After adsorption and sedimentation, the COD removal rate reaches 50% to 70%, reducing the aeration volume and reducing operating energy consumption.

[0038] Optionally, the aeration tank 21 uses a blower for micro-aeration, with an aeration time of 0.5 to 1 hour per operating cycle and a sludge load of 1.5 to 2 kg BOD5 / (kg MLSS·d). The hydraulic retention time (HRT) of the sedimentation tank 22 is 1 to 1.5 hours.

[0039] In an optional embodiment, part of the sludge discharged from the sedimentation tank 22 is returned to the aeration tank 21, and part is discharged into the sludge tank 60.

[0040] Furthermore, the biological denitrification module includes a MABR reaction zone 30 and an anaerobic ammonia oxidation reaction zone 40.

[0041] The MABR reaction zone 30 and the anaerobic ammonia oxidation reaction zone 40 are located inside the upflow reactor 50, with the MABR reaction zone 30 located below the anaerobic ammonia oxidation reaction zone 40.

[0042] Thus, the wastewater discharged from the sedimentation tank 22 enters the bottom of the upflow reactor 50 and passes sequentially through the MABR reaction zone 30 for removing COD from the wastewater and the anaerobic ammonia oxidation reaction zone 40 for removing total nitrogen and ammonia nitrogen from the wastewater.

[0043] Among them, the MABR reaction zone 30 can degrade COD and convert 50% of the ammonia nitrogen in the wastewater into nitrite. The anaerobic ammonia oxidation reaction zone 40 does not require the addition of an additional carbon source. Anaerobic ammonia oxidation bacteria use ammonia as an electron donor and nitrite as an electron acceptor to oxidize ammonia into nitrogen gas, thereby achieving further denitrification of the system.

[0044] Furthermore, the wastewater from the upflow reactor 50, after being treated in the MABR reaction zone 30 and the anaerobic ammonia oxidation reaction zone 40, flows out from the top overflow tank 51.

[0045] Combination Figure 2 As shown, the MABR reaction zone 30 is provided with a first oxygen permeable membrane aeration structure 31 and a second oxygen permeable membrane aeration structure 32. The first oxygen permeable membrane aeration structure 31 and the second oxygen permeable membrane aeration structure 32 are distributed vertically within the upflow reactor 50, with the first oxygen permeable membrane aeration structure 31 located below the second oxygen permeable membrane aeration structure 32.

[0046] Optionally, the first oxygen-permeable membrane aeration structure 31 and the second oxygen-permeable membrane aeration structure 32 are MABR oxygen-permeable membrane aeration components.

[0047] Among them, the first oxygen-permeable membrane aeration structure 31 focuses on the removal of residual COD, while the second oxygen-permeable membrane aeration structure 32 focuses on the conversion of ammonia nitrogen, converting 50% of the ammonia nitrogen in the wastewater into nitrite.

[0048] Furthermore, both the first oxygen-permeable membrane aeration structure 31 and the second oxygen-permeable membrane aeration structure 32 are connected to an aeration blower, which is used to provide oxygen to the first oxygen-permeable membrane aeration structure 31 and the second oxygen-permeable membrane aeration structure 32.

[0049] The MABR reaction zone uses a blower for micro-aeration, which is a bubble-free aeration method that provides higher oxygen conversion efficiency and saves a lot of energy consumption.

[0050] In an optional embodiment, the aeration rate of the first oxygen-permeable membrane aeration structure 31 is 0.5 to 1.5 times the COD concentration, and the aeration rate of the second oxygen-permeable membrane aeration structure 32 is 0.25 to 0.5 times the ammonia nitrogen concentration.

[0051] The first oxygen-permeable membrane aeration structure 31 focuses on the removal of residual COD, with an aeration rate of 0.5 to 1.5 times the COD equivalent. The second oxygen-permeable membrane aeration structure 32 focuses on the conversion of ammonia nitrogen, converting 50% of the ammonia nitrogen in the wastewater into nitrite, with an aeration rate of 0.25 to 0.5 times the ammonia nitrogen equivalent. The double-layer membrane aeration device is a bubble-free aeration system with an oxygen utilization rate of 50% to 90%. Through precise control of the aeration rate, after the reaction is completed, the COD in the wastewater has been basically removed. At this point, the ratio of ammonia nitrogen to nitrite in the wastewater is approximately 1:1.

[0052] In an optional embodiment, an online monitoring device is installed at a predetermined location within the upflow reactor 50 to detect COD equivalent and ammonia nitrogen equivalent, and the aforementioned data are obtained through measurement by the online monitoring device.

[0053] In this way, by adjusting the aeration rate, nitrite-producing bacteria can convert 50% of the ammonia nitrogen in the wastewater into nitrite. After the reaction is completed, the COD in the wastewater is basically removed, and the ratio of ammonia nitrogen to nitrite in the wastewater is about 1:1.

[0054] Combination Figure 2 As shown, the anaerobic ammonia oxidation reaction zone 40 is equipped with an anaerobic ammonia oxidation sludge hopper 41 and an anaerobic ammonia oxidation inlet guide plate 42. The anaerobic ammonia oxidation inlet guide plate 42 is positioned above the anaerobic ammonia oxidation sludge hopper 41. The bottom of the anaerobic ammonia oxidation sludge hopper 41 is also connected to a pipe 43, which is used to discharge the sludge from the bottom of the anaerobic ammonia oxidation sludge hopper 41 and to backwash the bottom of the anaerobic ammonia oxidation sludge hopper 41.

[0055] It should be understood that within the anaerobic ammonia oxidation reaction zone 40, under anaerobic or near-anaerobic conditions, anaerobic ammonia oxidizing bacteria use ammonia as an electron donor and nitrite as an electron acceptor to convert the remaining 50% of ammonia nitrogen into nitrogen gas, thus achieving the denitrification function.

[0056] Combination Figure 2 As shown, optionally, the anammox sludge hopper 41 is constructed as an upward-opening bucket-shaped structure, including a bottom surface and side walls, with the angle between the side walls and the bottom surface being β, where β = 60 ± 5°. The design of the anammox sludge hopper 41 ensures that the MABR reaction zone 30 and the anammox reaction zone 40 can complement each other and achieve zoned reaction, and its function is not affected by the integrated design.

[0057] Optionally, the anammox inlet guide plate 42 is configured to extend inward from the inner wall of the upflow reactor 50, and the included angle between the anammox inlet guide plate 42 and the inner wall of the upflow reactor 50 is α, where α = 55 ± 5°.

[0058] The lower end of the anammox influent guide plate 42 extends below the upper edge of the anammox sludge hopper 41 and is located inside the opening of the anammox sludge hopper 41.

[0059] Thus, through the guiding effect of the anammox influent guide plate 42, the wastewater treated in the MABR reaction zone 30 gradually enters the anammox sludge hopper 41, where the sludge deposited at the bottom can be discharged to the sludge tank 60 through the pipe 43.

[0060] Optionally, the end of pipe 43 is connected to a first pipe and a second pipe. The first pipe is connected to the sludge tank, and the second pipe is connected to a backflushing gas source, which is an ammonia or inert gas source.

[0061] Thus, pipe 43 serves the dual functions of sludge dredging and backwashing. Nitrogen or inert gas is selected as the aeration source to prevent the granular sludge in the upper anaerobic ammonia oxidation section from clogging the inlet channel after settling. Using nitrogen and inert gas for aeration will not increase the dissolved oxygen in the system, ensuring the smooth progress of the anaerobic ammonia oxidation reaction and ensuring that the effluent meets the standards.

[0062] In combination with the above, the MABR reaction zone 30 and the anaerobic ammonia oxidation reaction zone 40 are integrated into an upflow reactor 50, forming a MABR reaction layer and an anaerobic ammonia oxidation reaction layer within the reactor. This enables multifunctional pollutant removal. At the same time, pipes are installed to accommodate sludge dredging and discharge, ensuring that the two processes can complement each other and achieve zoned reactions, without being affected by the integrated design.

[0063] Although the present invention has been disclosed above with reference to preferred embodiments, it is not intended to limit the present invention. Those skilled in the art to which this invention pertains can make various modifications and refinements without departing from the spirit and scope of the present invention. Therefore, the scope of protection of this invention shall be determined by the claims.

Claims

1. A low-carbon biological treatment system, characterized by, It includes a pretreatment module (10), a decarbonization module (20), and a biological denitrification module; The pretreatment module (10) includes an equalization tank (11) and a pretreatment section (12). The equalization tank (11) is used to homogenize and equalize the wastewater entering the equalization tank (11). The pretreatment section (12) is used to remove toxic and harmful pollutants that cannot be degraded by organisms. The decarbonization module (20) includes an aeration tank (21) and a sedimentation tank (22) for removing organic matter from wastewater; The biological denitrification module includes a MABR reaction zone (30) and an anaerobic ammonia oxidation reaction zone (40); The MABR reaction zone (30) and the anaerobic ammonia oxidation reaction zone (40) are located in the upflow reactor (50). The MABR reaction zone (30) is located below the anaerobic ammonia oxidation reaction zone (40). Wastewater discharged from the sedimentation tank (22) enters the bottom of the upflow reactor (50) and passes sequentially through the MABR reaction zone (30) for removing COD from the wastewater and the anaerobic ammonia oxidation reaction zone (40) for removing total nitrogen and ammonia nitrogen from the wastewater.

2. The low-carbon biological treatment system according to claim 1, characterized by, The regulating tank (11) is equipped with an aeration and stirring device or a mechanical stirring device.

3. The low-carbon biological treatment system according to claim 1, characterized by, The pretreatment section (12) includes one or more combinations of oil separator, flotation tank, sedimentation tank, and coagulation sedimentation tank. The pretreatment section (12) also includes a triple-effect evaporator and / or an advanced oxidation device.

4. The low-carbon biological treatment system according to claim 1, characterized by, The MABR reaction zone (30) is provided with a first oxygen permeable membrane aeration structure (31) and a second oxygen permeable membrane aeration structure (32). The first oxygen permeable membrane aeration structure (31) and the second oxygen permeable membrane aeration structure (32) are distributed vertically within the upflow reactor (50). The first oxygen permeable membrane aeration structure (31) is located below the second oxygen permeable membrane aeration structure (32). Both the first oxygen permeable membrane aeration structure (31) and the second oxygen permeable membrane aeration structure (32) are connected to an aeration fan. The aeration fan is used to provide oxygen to the first oxygen permeable membrane aeration structure (31) and the second oxygen permeable membrane aeration structure (32).

5. The low-carbon biological treatment system according to claim 4, characterized by The aeration rate of the first oxygen-permeable membrane aeration structure (31) is 0.5 to 1.5 times the COD concentration, and the aeration rate of the second oxygen-permeable membrane aeration structure (32) is 0.25 to 0.5 times the ammonia nitrogen concentration.

6. The low-carbon biological treatment system according to claim 1, characterized by The anaerobic ammonia oxidation reaction zone (40) is equipped with an anaerobic ammonia oxidation sludge hopper (41) and an anaerobic ammonia oxidation inlet guide plate (42). The anaerobic ammonia oxidation inlet guide plate (42) is located above the anaerobic ammonia oxidation sludge hopper (41). The bottom of the anaerobic ammonia oxidation sludge hopper (41) is also connected to a pipe (43). The pipe (43) is used to discharge the sludge at the bottom of the anaerobic ammonia oxidation sludge hopper (41) and to backwash the bottom of the anaerobic ammonia oxidation sludge hopper (41).

7. The low-carbon biological treatment system according to claim 6, characterized by The end of the pipe (43) is connected to a first pipe and a second pipe. The first pipe is connected to a sludge tank, and the second pipe is connected to a backflushing gas source, which is an ammonia or inert gas source.

8. The low-carbon biological treatment system according to claim 6, characterized by The anaerobic ammonia oxidation sludge hopper (41) is constructed as an upward-opening bucket-shaped structure, including a bottom surface and a side wall surface, wherein the angle between the side wall surface and the bottom surface is β, β = 60 ± 5°.

9. The low-carbon biological treatment system according to claim 6, characterized by The anaerobic ammonia oxidation inlet guide plate (42) is configured to extend inward from the inner wall of the upflow reactor (50), and the included angle between the anaerobic ammonia oxidation inlet guide plate (42) and the inner wall of the upflow reactor (50) is α, where α = 55 ± 5°.

10. The low-carbon biological treatment system according to claim 6, characterized in that, The lower end of the anammox influent guide plate (42) extends below the upper edge of the anammox sludge hopper (41) and is located inside the opening of the anammox sludge hopper (41).

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