A dual aeration counter-current mass transfer reaction device and method

Abstract

The present application relates to the technical field of aerobic granular sludge formation, and specifically relates to a double-aeration countercurrent mass transfer reaction device and method. The device comprises a reactor body, a flow guide plate structure and an aeration head. The flow guide plate structure separates the interior of the reactor body into a first fluid zone and multiple second fluid zones. The aeration head comprises a first aeration head and a second aeration head, and the aeration types of the first aeration head and the second aeration head are different. The aeration types of the first aeration head and the second aeration head are respectively selected from oxygen or nitrogen-rich gas, and the aeration amount of the nitrogen-rich gas is greater than that of the oxygen. The method of the present application maintains the flow field driving force of the reactor body by using nitrogen-rich gas. The dissolved oxygen amount is maintained by using oxygen in a countercurrent mass transfer manner, the residence time of the gas bubbles in the reactor body is prolonged, the oxygen utilization rate is improved, and the problems that the traditional air-lift reactor cannot maintain the stability of the flow field under load changes, and that there is a contradiction between the increased demand for aeration amount of high-load wastewater and sludge particle crushing are solved.

Description

Technical Field

[0001] This invention relates to the field of aerobic granular sludge formation technology, specifically to a dual-aeration countercurrent mass transfer reaction device and method. Background Technology

[0002] Aerobic granular sludge, abbreviated as AGS, is a microbial aggregate formed by the self-immobilization and growth of flocculent sludge under suitable conditions. It possesses a compact, spherical structure and exhibits advantages such as excellent solid-liquid separation, high biomass concentration, strong tolerance, and short hydraulic retention time. AGS can effectively treat industrial wastewater or sewage, including high-concentration organic wastewater and high-salinity wastewater.

[0003] The success of AGS cultivation technology relies on efficient reactor design and optimization. Traditional AGS reactor types include SBR reactors, MBR reactors, and airlift reactors. Among them, airlift reactors have shown potential in AGS cultivation due to their high shear force. The structure of an airlift reactor generally consists of a three-phase mixing zone and a separation zone. Settling selectivity and hydraulic shear force can be adjusted by modifying internal components and aeration rates, thereby achieving rapid sludge granulation. However, in actual cultivation, the influent load within the reactor varies. Traditional airlift reactors cannot maintain flow field stability under varying loads, and the increased aeration demand from high-load wastewater contradicts the need for sludge particle breakage. In short, the contradiction between maintaining the flow field driving force and adjusting dissolved oxygen levels in traditional airlift reactors limits their application in AGS cultivation. Summary of the Invention

[0004] To address the challenges of maintaining flow field stability under varying loads in traditional airlift reactors, and the conflict between the increased aeration requirements of high-load wastewater and the need for sludge particle breakage, this invention aims to provide a dual-aeration countercurrent mass transfer reactor and method for cultivating aerobic granular sludge. This device can cope with changes in influent load while maintaining flow field and dissolved oxygen stability.

[0005] To achieve the above objectives, the technical solution of the present invention is as follows.

[0006] The first aspect of this invention provides a dual-aeration countercurrent mass transfer reactor for cultivating aerobic granular sludge. The reactor includes: a reactor body; a baffle structure disposed within the reactor body; the baffle structure dividing the interior of the reactor body into a first fluid zone and multiple second fluid zones; the multiple second fluid zones being disposed outside the first fluid zone; and aeration heads, including a first aeration head and a second aeration head, the first aeration head being disposed below the first fluid zone; the second aeration head being disposed below its corresponding second fluid zone; the first and second aeration heads having different aeration types; the aeration types of the first and second aeration heads being selected from oxygen or nitrogen-rich gas, respectively, with the aeration rate of nitrogen-rich gas being greater than that of oxygen; the aeration types of the first and second aeration heads changing with the increase of the influent load of the reactor body to adjust the fluid direction of the first and second fluid zones; and the aeration rates of the first and second aeration heads gradually increasing with the increase of the particle size of the aerobic granular sludge within the reactor body.

[0007] This invention establishes a dual-aeration countercurrent mass transfer reactor with independent control of the aeration type and aeration rate of the first and second aeration heads corresponding to the first and second fluid zones, respectively. The dual-aeration countercurrent mass transfer reactor of this invention can change the aeration type and aeration rate of the first and second aeration heads according to changes in influent load and aerobic granular sludge particle size. While coping with changes in influent load, it can maintain flow field stability and dissolved oxygen stability, solving the problems of traditional airlift reactors failing to maintain flow field stability under load changes, and the contradiction between the increased aeration rate demanded by high-load wastewater and sludge particle breakage.

[0008] Preferably, the distance between the bottom of the baffle structure and the bottom of the reactor body increases with the increase of the particle size of the aerobic granular sludge in the reactor body. The present invention mainly addresses the situation where the particle size of the aerobic granular sludge reaches >1.8 mm, by increasing the distance between the bottom of the baffle structure and the bottom of the reactor body to accelerate the fluid flow velocity at the bottom of the reactor body.

[0009] Preferably, the upper side of the baffle structure is configured as an effluent separation zone, which is equipped with multiple three-phase separation tube assemblies, each of which has a connecting pipe; the lower side of the baffle structure is configured as a bottom gap zone; as the particle size of the aerobic granular sludge in the reactor body increases, the arrangement direction of the connecting pipe gradually deflects from the direction towards the effluent separation zone to the direction towards the bottom gap zone. The purpose of changing the arrangement direction of the connecting pipe is to ensure the reaction and growth of aerobic granular sludge in the reactor body when the particle size of the aerobic granular sludge is relatively small; as the particle size increases, further changing the arrangement direction of the connecting pipe helps to promote the entry of relatively large aerobic granular sludge into the descending zone, so as to achieve particle size screening of aerobic granular sludge; when the particle size of aerobic granular sludge reaches >1.8mm, it can allow larger aerobic granular sludge particles to enter the effluent separation zone or increase the amount of aerobic granular sludge entering the effluent separation zone, so as to separate aerobic granular sludge.

[0010] In this invention, when the aeration type of the first aeration head is nitrogen-rich gas and the aeration type of the second aeration head is oxygen, the fluid direction of the first fluid zone corresponding to the first aeration head is from the bottom of the reactor body to the top of the reactor body; or, when the aeration type of the second aeration head is nitrogen-rich gas, the fluid direction of the second fluid zone corresponding to the second aeration head is from the bottom of the reactor body to the top of the reactor body.

[0011] Preferably, it further includes: an influent detection unit for analyzing and detecting the influent load of the reactor body and sending it to the processing unit; a particle size detection unit for analyzing and detecting the particle size of the aerobic granular sludge in the reactor body and sending it to the processing unit; and a processing unit for receiving the influent load detection data sent by the influent detection unit and the particle size detection data sent by the particle size detection unit, comparing the influent load detection data with the set influent load data, and comparing the particle size detection data with the set particle size data, and adjusting the aeration type and aeration rate of the first aeration head and the second aeration head according to the comparison results.

[0012] Preferably, the condition for adjusting the aeration type of the first and second aeration heads based on the comparison results is: when the influent load detection data is <1.2 kg COD·m³. -3 ·d -1 When the aeration type of the second aerator is adjusted to nitrogen-rich gas, the second fluid zone is configured as an ascending zone, and the aeration type of the first aerator is adjusted to oxygen, the first fluid zone is configured as a descending zone; or, when the influent load detection data is ≥1.2 kg COD·m³, -3 ·d -1 At that time, the aeration type of the first aeration head is adjusted to nitrogen-rich gas to configure the first fluid zone as an ascending zone, and the aeration type of the second aeration head is adjusted to oxygen to configure the second fluid zone as a descending zone.

[0013] Preferably, the condition for adjusting the aeration rate of the first and second aeration heads based on the comparison results is: when the influent load detection data is <1.2 kg COD·m³. -3 ·d -1 At that time, as the particle size of the aerobic granular sludge within the reactor body gradually increased, the aeration rate of the first aeration head increased from 4m³ / h. 3 / h~6m 3 / h gradually increased to 8m 3 / h~10m 3 / h; the aeration rate of the second aeration head is 10m³ / h. 3 / h~15m 3 / h gradually increased to 20m 3 / h~25m 3 / h; or, when the influent load detection data is ≥1.2kgCOD·m -3 ·d -1 At that time, as the particle size of the aerobic granular sludge in the reactor body gradually increased, the aeration rate of the second aeration head increased from 10m³ / h. 3 / h~12m 3 / h gradually increased to 14m 3 / h~18m 3 / h; the aeration rate of the first aeration head is 20m³ / h. 3 / h~25m 3 / h gradually increased to 30m 3 / h~35m 3 / h.

[0014] Preferably, the condition for adjusting the aeration rate of the first and second aeration heads based on the comparison results is: influent load test data < 1.2 kg COD·m³ -3 ·d -1 Meanwhile, when the particle size of the aerobic granular sludge within the reactor body is <0.3mm, the aeration rate of the first aeration head is 4m³ / s. 3 / h~6m 3 / h, the aeration rate of the second aeration head is 10m³ / h. 3 / h~15m 3 / h; When the particle size of the aerobic granular sludge in the reactor body is 0.3mm~1.8mm, the aeration rate of the first aeration head is 6m³ / h. 3 / h~8m 3 / h, the aeration rate of the second aeration head is 15m³ / h. 3 / h~20m 3 / h; When the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the aeration rate of the first aeration head is 8m³ / h. 3 / h~10m 3 / h, the aeration rate of the second aeration head is 20m³ / h. 3 / h~25m 3 / h; or, influent load test data ≥1.2kg COD·m -3 ·d -1 Meanwhile, when the particle size of the aerobic granular sludge within the reactor body is <0.3mm, the aeration rate of the second aeration head is 10m³. 3 / h~12m 3 / h, the aeration rate of the first aeration head is 20m³ / h. 3 / h~25m 3 / h; When the particle size of the aerobic granular sludge in the reactor body is 0.3mm~1.8mm, the aeration rate of the second aeration head is 12m³ / h. 3 / h~14m 3 / h, the aeration rate of the first aeration head is 25m³ / h. 3 / h~30m 3 / h; When the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the aeration rate of the second aeration head is 14m³ / h. 3 / h~18m 3 / h, the aeration rate of the first aeration head is 30m³ / h. 3 / h~35m 3 / h.

[0015] Preferably, the processing unit can issue a prompting command to adjust the distance between the bottom of the guide plate structure and the bottom of the reactor body based on the comparison result; when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body is ≤1.8mm, the processing unit can issue a prompting command to adjust the distance between the bottom of the guide plate structure and the bottom of the reactor body to a first height based on the comparison result; or, when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the processing unit can issue a prompting command to adjust the distance between the bottom of the guide plate structure and the bottom of the reactor body to a second height based on the comparison result; the second height is greater than the first height.

[0016] Preferably, four support components are arranged around the bottom periphery of the reactor body; two opposite support components are at the same height, and two adjacent support components have a height difference; the guide plate structure has two side notches, and the two side notches are respectively arranged on the two opposite support components to adjust the distance between the bottom of the guide plate structure and the bottom of the reactor body. Preferably, the guide plate structure includes a guide inner cylinder and four guide plates; the four guide plates are respectively fixed to the side wall of the guide inner cylinder; the two side notches are arranged at the bottom of the two opposite guide plates, so that the two opposite guide plates overlap and are respectively arranged on their corresponding support components. Preferably, the height difference between two adjacent support components is 0.2m to 0.6m. By setting the height difference range, it is helpful to adjust the distance between the bottom of the guide plate structure and the bottom of the reactor body to accelerate the flow velocity of the fluid at the bottom of the reactor body.

[0017] Preferably, the upper side of the guide plate structure is configured as an effluent separation zone, which is equipped with multiple three-phase separation pipe assemblies, each of which has a connecting pipe; the lower side of the guide plate structure is configured as a bottom gap zone; the treatment unit can issue a prompt instruction to adjust the arrangement direction of the connecting pipe according to the comparison result; when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body is <0.3mm, the treatment unit can issue an instruction to adjust the arrangement direction of the connecting pipe to face the effluent separation zone; or, when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body is 0.3mm to 1.8mm, the treatment unit can issue an instruction to adjust the arrangement direction of the connecting pipe to face the inner wall of the reactor body; or, when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the treatment unit can issue an instruction to adjust the arrangement direction of the connecting pipe to face the bottom gap zone.

[0018] The second aspect of the present invention provides a method for cultivating aerobic granular sludge, which employs the dual-aeration countercurrent mass transfer reactor of the first aspect, and the specific method includes the following steps:

[0019] Obtain the influent load of the reactor body and the particle size of the aerobic granular sludge within the reactor body; adjust the aeration type of the first and second aeration heads according to the influent load of the reactor body to determine the fluid direction of the first and second fluid zones; adjust the aeration rate of the first and second aeration heads according to the particle size of the aerobic granular sludge within the reactor body; and gradually increase the aeration rate of the first and second aeration heads as the particle size of the aerobic granular sludge within the reactor body gradually increases.

[0020] Preferably, the method for adjusting the aeration type of the first and second aeration heads according to the influent load of the reactor body is as follows: when the influent load detection data is <1.2 kg COD·m-3 ·d -1 When the aeration type of the second aerator is adjusted to nitrogen-rich gas, the second fluid zone is configured as an ascending zone, and the aeration type of the first aerator is adjusted to oxygen, the first fluid zone is configured as a descending zone; or, when the influent load detection data is ≥1.2 kg COD·m³, -3 ·d -1 At that time, the aeration type of the first aeration head is adjusted to nitrogen-rich gas to configure the first fluid zone as an ascending zone, and the aeration type of the second aeration head is adjusted to oxygen to configure the second fluid zone as a descending zone.

[0021] Preferably, the method for adjusting the aeration rate of the first and second aeration heads based on the particle size of the aerobic granular sludge within the reactor body is as follows: when the influent load detection data is <1.2 kg COD·m³, -3 ·d -1 At that time, as the particle size of the aerobic granular sludge within the reactor body gradually increased, the aeration rate of the first aeration head increased from 4m³ / h. 3 / h~6m 3 / h gradually increased to 8m 3 / h~10m 3 / h; the aeration rate of the second aeration head is 10m³ / h. 3 / h~15m 3 / h gradually increased to 20m 3 / h~25m 3 / h; or, when the influent load test data is ≥1.2kg COD·m -3 ·d -1 At that time, as the particle size of the aerobic granular sludge in the reactor body gradually increased, the aeration rate of the second aeration head increased from 10m³ / h. 3 / h~12m 3 / h gradually increased to 14m 3 / h~18m 3 / h; the aeration rate of the first aeration head is 20m³ / h. 3 / h~25m 3 / h gradually increased to 30m 3 / h~35m 3 / h.

[0022] Preferably, the method for adjusting the aeration rate of the first and second aeration heads based on the particle size of the aerobic granular sludge within the reactor body is as follows: Influent load detection data < 1.2 kg COD·m³ -3 ·d -1 Meanwhile, when the particle size of the aerobic granular sludge within the reactor body is <0.3mm, the aeration rate of the first aeration head is 4m³ / s. 3 / h~6m 3 / h, the aeration rate of the second aeration head is 10m³ / h.3 / h~15m 3 / h; When the particle size of the aerobic granular sludge in the reactor body is 0.3mm~1.8mm, the aeration rate of the first aeration head is 6m³ / h. 3 / h~8m 3 / h, the aeration rate of the second aeration head is 15m³ / h. 3 / h~20m 3 / h; When the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the aeration rate of the first aeration head is 8m³ / h. 3 / h~10m 3 / h, the aeration rate of the second aeration head is 20m³ / h. 3 / h~25m 3 / h; or, influent load test data ≥1.2kg COD·m -3 ·d -1 Meanwhile, when the particle size of the aerobic granular sludge within the reactor body is <0.3mm, the aeration rate of the second aeration head is 10m³. 3 / h~12m 3 / h, the aeration rate of the first aeration head is 20m³ / h. 3 / h~25m 3 / h; When the particle size of the aerobic granular sludge in the reactor body is 0.3mm~1.8mm, the aeration rate of the second aeration head is 12m³ / h. 3 / h~14m 3 / h, the aeration rate of the first aeration head is 25m³ / h. 3 / h~30m 3 / h; When the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the aeration rate of the second aeration head is 14m³ / h. 3 / h~18m 3 / h, the aeration rate of the first aeration head is 30m³ / h. 3 / h~35m 3 / h.

[0023] Preferably, after obtaining the particle size of the aerobic granular sludge within the reactor body, the method further includes: adjusting the distance between the bottom of the guide plate structure and the bottom of the reactor body, and the arrangement direction of the connecting pipe, based on the particle size of the aerobic granular sludge within the reactor body; specifically, when the particle size of the aerobic granular sludge within the reactor body is <0.3mm, adjusting the distance between the bottom of the guide plate structure and the bottom of the reactor body to a first height, and adjusting the arrangement direction of the connecting pipe to... The direction is towards the effluent separation zone on the upper side of the guide plate structure; or, when the particle size of the aerobic granular sludge in the reactor body is 0.3mm to 1.8mm, the distance between the bottom of the guide plate structure and the bottom of the reactor body is maintained at a first height, and the arrangement direction of the connecting pipe is adjusted to be straight against the inner wall of the reactor body; or, when the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the distance between the bottom of the guide plate structure and the bottom of the reactor body is adjusted to a second height, and the arrangement direction of the connecting pipe is adjusted to be towards the bottom gap zone on the lower side of the guide plate structure; and the second height is greater than the first height.

[0024] The beneficial effects of this invention are:

[0025] 1. This invention establishes a dual-aeration countercurrent mass transfer reactor with independent control of the aeration type and aeration rate of the first and second aeration heads corresponding to the first and second fluid zones, respectively. The dual-aeration countercurrent mass transfer reactor of this invention can change the aeration type and aeration rate of the first and second aeration heads according to changes in influent load and aerobic granular sludge particle size. While coping with changes in influent load, it can also maintain flow field stability and dissolved oxygen stability, solving the problems of traditional airlift reactors failing to maintain flow field stability under load changes, and the contradiction between the increased aeration rate demanded by high-load wastewater and sludge particle breakage.

[0026] 2. The dual-aeration countercurrent mass transfer reactor of the present invention mainly utilizes nitrogen-rich gas to provide the driving force for the reactor fluid circulation. Oxygen maintains the dissolved oxygen level in the reactor through countercurrent mass transfer, thereby separating the gas, liquid, and solid phases at the top of the reactor body. The gas escapes from the liquid surface and enters the atmosphere, while the liquid remains in the reactor body and eventually flows out of the reactor body. The solid sludge settles at the top of the reactor body and returns to the first and second fluid zones to continue the microbial reaction. The dual-aeration countercurrent mass transfer reactor of the present invention can prolong the oxygen residence time, improve the mass transfer efficiency, and increase the collision probability and movement trajectory of granular sludge by forming a turbulence zone, which is conducive to the formation of granular sludge.

[0027] 3. The method of the present invention maintains the flow field driving force of the airlift reactor by using nitrogen-rich gas; maintains the dissolved oxygen content by using oxygen countercurrent mass transfer, prolongs the residence time of bubbles in the reactor, improves the utilization rate of gas and feed, and solves the flow field stability problem of existing airlift reactors under load changes. Attached Figure Description

[0028] Figure 1 This is a side cross-sectional schematic diagram of the dual-aeration countercurrent mass transfer reaction device according to an embodiment of the present invention.

[0029] Figure 2 This is a top view schematic diagram of the dual-aeration countercurrent mass transfer reaction device provided in an embodiment of the present invention.

[0030] Figure 3 This is a schematic diagram of the flow guide plate structure provided in the embodiment of the present invention.

[0031] Figure 4 This is a top view schematic diagram of the guide plate structure provided in the embodiment of the present invention.

[0032] Figure 5 This is a schematic diagram of the structure of the guide plate provided in an embodiment of the present invention.

[0033] Figure 6 This is a schematic diagram of the three-phase separation device and guide plate structure provided in the embodiments of the present invention.

[0034] Figure 7 yes Figure 6 A schematic diagram from the perspective of A.

[0035] In the diagram, 1. Reactor body; 11. Supporting component; 12. Sludge discharge port; 13. Inlet pipe; 14. Outlet pipe; 2. Baffle structure; 21. Inner guide cylinder; 22. Baffle; 221. Side notch; 3. Aeration head; 31. First aeration head; 32. Second aeration head; 4. First fluid zone; 5. Second fluid zone; 6. Effluent separation zone; 7. Bottom clearance zone; 8. Effluent weir; 9. Three-phase separation device; 91. Separation zone partition; 92. Three-phase separation pipe assembly; 921. Connecting pipe; h1 is the first height; h2 is the second height. Detailed Implementation

[0036] To make the objectives, technical solutions, and advantages of this invention clearer, the invention will be further described in detail below with reference to embodiments. It should be understood that the specific embodiments described herein are merely illustrative and not intended to limit the invention. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without inventive effort are within the scope of protection of this invention.

[0037] Unless otherwise specified, the methods described in the following embodiments are conventional methods; the reagents and materials mentioned are commercially available unless otherwise specified. In the following embodiments, the nitrogen-enriched gas is nitrogen or nitrogen-enriched air; the nitrogen content of the nitrogen-enriched air is 50% to 95%. The following embodiments of the present invention use nitrogen as the nitrogen-enriched gas for detailed description.

[0038] Please see Figure 1 A dual-aeration countercurrent mass transfer reactor is used to cultivate aerobic granular sludge. The reactor includes: a reactor body 1, a guide plate structure 2, and multiple aeration heads 3.

[0039] Reactor body 1 is primarily used to form the reaction chamber for cultivating aerobic granular sludge. For example... Figure 1 The reactor body 1 has a funnel-shaped longitudinal section. Preferably, the reactor body 1 has a square cross-section, and the area of ​​the upper end of the reactor body 1 is larger than the area of ​​the lower end, that is, the reactor body 1 has a size structure that is larger at the top and smaller at the bottom. For example, let the length of the lower end of the reactor body 1 be L, the width of the lower end of the reactor body 1 be W, the effective water depth be H, and L = W = 2.1m, H = 5.55m; the length and width of the upper end of the reactor body 1 are both 5m; the effective volume of the reactor body 1 is 43.1m³. 3 The reactor body 1 is made of reinforced concrete, but this material can be chosen according to actual needs.

[0040] like Figures 3 to 5A flow guide structure 2 is disposed within the reactor body 1. The flow guide structure 2 divides the interior of the reactor body 1 into a first fluid zone 4 and multiple second fluid zones 5. The multiple second fluid zones 5 are disposed outside the first fluid zone 4. Specifically, in order to facilitate the formation of a turbulent flow zone, increase the collision probability and movement trajectory of granular sludge, and promote the formation of granular sludge, a flow guide structure 2 is installed within the reactor body 1. The flow guide structure 2 divides the reaction chamber within the reactor body 1 into multiple fluid zones. The flow guide structure 2 is disposed within the reactor body 1. The flow guide structure 2 divides the interior of the reactor body 1 into a first fluid zone 4, an effluent separation zone 6, second fluid zones 5, and a bottom gap zone 7. The first fluid zone 4 is located inside the second fluid zone 5. The effluent separation zone 6 is located above the first fluid zone 4, and the bottom gap zone 7 is located below the first fluid zone 4. In a preferred embodiment, the fluid direction of the first fluid zone 4 is opposite to the fluid direction of the second fluid zone 5. For example, when the fluid direction in the first fluid zone 4 is from bottom to top, the fluid direction in the second fluid zone 5 is from top to bottom. Conversely, when the fluid direction in the second fluid zone 5 is from bottom to top, the fluid direction in the first fluid zone 4 is from top to bottom. The first fluid zone 4 is located within the internal channel of the guide plate structure 2; the second fluid zone 5 is located within the channel between the outer wall of the guide plate structure 2 and the inner wall of the reactor body 1; the effluent separation zone 6 and the bottom clearance zone 7 are located at opposite ends of the reactor body 1. The fluid directions of the first fluid zone 4 and the second fluid zone 5 are adjusted according to the influent load within the reactor body 1 to maintain a stable flow field and dissolved oxygen levels, thereby cultivating aerobic granular sludge and achieving rapid sludge granulation.

[0041] like Figure 6 The aeration head 3 includes a first aeration head 31 and a second aeration head 32. The first aeration head 31 is located below the first fluid zone 4; the second aeration head 32 is located below its corresponding second fluid zone 5. The aeration types of the first aeration head 31 and the second aeration head 32 are different. The aeration types of the first aeration head 31 and the second aeration head 32 are respectively selected from oxygen or nitrogen-rich gas, and the aeration rate of nitrogen-rich gas is greater than that of oxygen. The aeration types of the first aeration head 31 and the second aeration head 32 change with the increase of the influent load of the reactor body 1 to adjust the fluid direction of the first fluid zone 4 and the second fluid zone 5. The aeration rates of the first aeration head 31 and the second aeration head 32 gradually increase with the increase of the particle size of the aerobic granular sludge in the reactor body 1. In order to maintain the stability of the flow field and dissolved oxygen, multiple aeration heads are configured in the reactor body 1 for aerating nitrogen-rich gas or oxygen, respectively.

[0042] Specifically, multiple second aeration heads 32 are arranged around the outside of multiple first aeration heads 31. When the first aeration heads 31 aerate nitrogen-rich gas and the second aeration heads 32 aerate oxygen, the fluid direction in the first fluid zone 4 is from bottom to top, and the fluid direction in the second fluid zone 5 is from top to bottom. When the second aeration heads 32 aerate nitrogen-rich gas and the first aeration heads 31 aerate oxygen, the fluid direction in the second fluid zone 5 is from bottom to top, and the fluid direction in the first fluid zone 4 is from top to bottom. By adjusting the fluid directions in the first fluid zone 4 and the second fluid zone 5, as well as the aeration rates of the first aeration heads 31 and the second aeration heads 32, the flow field and dissolved oxygen levels are maintained to cultivate aerobic granular sludge and achieve rapid sludge granulation.

[0043] To facilitate adjustment of the aeration height, an extension tube is connected to the corresponding aeration head 3, such as... Figure 1 One end of the extension pipe is threaded to the bottom of the reactor body 1. Extension pipes are connected to the corresponding aeration heads 3 as needed to change the height of the aeration heads 3. The main function of the extension pipe is to facilitate flexible adjustment of the aeration head height to adapt to different process requirements, such as different sludge characteristics, such as density, viscosity, and solids content. Adjusting the aeration head height also optimizes the aeration effect, ensuring a uniform oxygen supply to the sludge mixture, promoting the uniform distribution and activity of microorganisms, and improving the treatment efficiency of aerobic granular sludge. An appropriate aeration head height also helps control the settling properties of aerobic granular sludge, thus achieving efficient and economical sludge treatment.

[0044] Based on the above embodiments, as a more preferred embodiment, the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1 increases as the particle size of the aerobic granular sludge in the reactor body 1 increases. Preferably, the upper side of the guide plate structure 2 is configured as an effluent separation zone 6, which is equipped with multiple three-phase separation tube assemblies, each of which has a connecting pipe 921; the lower side of the guide plate structure 2 is configured as a bottom gap zone 7; as the particle size of the aerobic granular sludge in the reactor body 1 increases, the arrangement direction of the connecting pipe 921 gradually deflects from the direction toward the effluent separation zone 6 toward the direction toward the bottom gap zone 7.

[0045] Specifically, the aeration gases from the first aeration head 31 and the second aeration head 32 are independently selected from oxygen or nitrogen-rich gas; and the ratio of nitrogen-rich gas aeration volume to oxygen aeration volume is 1.2 to 4:1, for example, 1.2:1, 1.5:1, 2:1, 2.2:1, 2.5:1, 3:1, 3.2:1, 3.5:1, 4:1, etc. The nitrogen-rich gas aeration volume is greater than the oxygen aeration volume, and the nitrogen-rich gas aeration volume and oxygen aeration volume are adjusted according to the actual reaction conditions, such as the particle size of the aerobic granular sludge in the reaction system. The nitrogen-rich gas is used to provide the power for the circulation of the reaction fluid; the oxygen is used to maintain the dissolved oxygen content of the reaction fluid. Preferably, the nitrogen-rich gas is nitrogen or nitrogen-rich air; the nitrogen content of the nitrogen-rich air is 50% to 95%. To ensure the normal operation of the device, a total of 5 microporous aeration heads are configured at the bottom of the reactor body 1 to ensure that the apparent gas velocity during operation is greater than 1.2 cm / s. Five microporous aeration heads provide either nitrogen-rich gas or oxygen. Nitrogen primarily drives the circulation of the reaction fluid, while oxygen maintains the dissolved oxygen level in the reaction fluid through countercurrent mass transfer.

[0046] In a more preferred embodiment, the device further includes an influent detection unit, a particle size detection unit, and a treatment unit. The influent detection unit analyzes and detects the influent load of the reactor body 1 and sends the data to the treatment unit. The particle size detection unit analyzes and detects the particle size of the aerobic granular sludge within the reactor body 1 and sends the data to the treatment unit. The treatment unit receives the influent load detection data from the influent detection unit and the particle size detection data from the particle size detection unit, compares the influent load detection data with the set influent load data, and compares the particle size detection data with the set particle size data. Based on the comparison results, it adjusts the aeration type and aeration rate of the first aeration head 31 and the second aeration head 32.

[0047] As a more preferred embodiment, the condition for adjusting the aeration type of the first aeration head 31 and the second aeration head 32 according to the comparison results is: when the influent load detection data is <1.2 kg COD·m -3 ·d -1 At this time, adjust the aeration type of the second aeration head 32 to nitrogen-rich gas to configure the second fluid zone 5 as the rising zone, and adjust the aeration type of the first aeration head 31 to oxygen to configure the first fluid zone 4 as the falling zone. Alternatively, when the influent load detection data is ≥1.2 kg COD·m³... -3 ·d -1 At the same time, the aeration type of the first aeration head 31 is adjusted to nitrogen-rich gas so that the first fluid zone 4 is configured as the rising zone, and the aeration type of the second aeration head 32 is adjusted to oxygen so that the second fluid zone 5 is configured as the falling zone.

[0048] As a more preferred embodiment, the condition for adjusting the aeration rate of the first aeration head 31 and the second aeration head 32 based on the comparison results is: influent load detection data < 1.2 kg COD·m -3 ·d -1 Meanwhile, when the particle size of the aerobic granular sludge in reactor body 1 is <0.3mm, the aeration rate of the first aeration head 31 is 4m³ / s. 3 / h~6m 3 / h, the aeration rate of the second aeration head 32 is 10m³ / h. 3 / h~15m 3 / h; When the particle size of the aerobic granular sludge in reactor body 1 is 0.3mm to 1.8mm, the aeration rate of the first aeration head 31 is 6m³ / h. 3 / h~8m 3 / h, the aeration rate of the second aeration head 32 is 15m³ / h. 3 / h~20m 3 / h; When the particle size of the aerobic granular sludge in reactor body 1 is >1.8mm, the aeration rate of the first aeration head 31 is 8m³ / h. 3 / h~10m 3 / h, the aeration rate of the second aeration head 32 is 20m³ / h. 3 / h~25m 3 / h. Or, the influent load test data is ≥1.2kg COD·m³. -3 ·d -1 Meanwhile, when the particle size of the aerobic granular sludge in reactor body 1 is <0.3mm, the aeration rate of the second aeration head 32 is 10m³. 3 / h~12m 3 / h, the aeration rate of the first aeration head 31 is 20m³ / h. 3 / h~25m 3 / h; When the particle size of the aerobic granular sludge in reactor body 1 is 0.3mm to 1.8mm, the aeration rate of the second aeration head 32 is 12m³ / h. 3 / h~14m 3 / h, the aeration rate of the first aeration head 31 is 25m³ / h. 3 / h~30m 3 / h; When the particle size of the aerobic granular sludge in reactor body 1 is >1.8mm, the aeration rate of the second aeration head 32 is 14m³ / h. 3 / h~18m 3 / h, the aeration rate of the first aeration head 31 is 30m³ / h. 3 / h~35m 3 / h.

[0049] In a more preferred embodiment, the processing unit can issue a prompting command to adjust the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1 based on the comparison result. When the comparison result indicates that the particle size of the aerobic granular sludge in the reactor body 1 is ≤1.8mm, the processing unit can issue a prompting command to adjust the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1 to a first height h1. Alternatively, when the comparison result indicates that the particle size of the aerobic granular sludge in the reactor body 1 is >1.8mm, the processing unit can issue a prompting command to adjust the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1 to a second height h2.

[0050] Specifically, the second height h2 is greater than the first height h1. The prompting command can be any combination of one or more of the following: sound prompt, light prompt, vibration prompt, and display prompt. For example, a combination of sound and light prompts. The display prompt can show the corresponding height data on an LED display screen. The light prompt can be the flashing or steady illumination of multiple colors of light, with each color representing a different height. The sound prompt can be a voice prompt indicating the height to be adjusted, or a voice prompt indicating the particle size of the aerobic granular sludge. In this invention, the prompting command issued by the processing unit is existing technology.

[0051] As a more preferred embodiment, to facilitate adjustment of the distance between the lower surface of the guide vane structure 2 and the bottom of the reactor body 1, such as... Figure 1 and Figure 3Four support components 11 are arranged around the bottom periphery of the reactor body 1. Two opposite support components 11 have the same height, while two adjacent support components 11 have a height difference; for example, the height difference between two adjacent support components 11 is 0.2m to 0.6m; such as 0.2m, 0.3m, 0.4m, 0.5m, 0.6m, etc. The guide plate structure 2 has two side notches 221, which are respectively arranged on two opposite support components 11 to adjust the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1. For example, the reactor body 1 is designed with four support components 11, which are support bars, two long and two short. Support components 11 of the same length are distributed on opposite sides at the bottom of the reactor body, and the guide plate 22 is also designed with corresponding opposite side notches 221. When the side notch of the guide plate 22 is exactly located at the long support bar, the bottom of the guide plate 22 is 0.3m away from the bottom plate of the reactor body 1. After the guide plate is pulled out, rotated 90 degrees and then inserted into the reactor body 1, the side notch of the guide plate 22 corresponds to the position of the short support bar, and the side notch 221 does not contact the short support bar. At this time, the guide plate 22 without the side notch 221 contacts the long support bar and plays a supporting role. The bottom of the guide plate 22 is 0.6m away from the bottom of the reactor body 1. The guide plate structure 2 includes a guide inner cylinder 21 and four guide plates 22. The four guide plates 22 are respectively fixed on the side wall of the guide inner cylinder 21. Two side notches 221 are arranged at the bottom of two oppositely arranged guide plates 22 so that the two oppositely arranged guide plates 22 overlap and are respectively arranged on their corresponding support components 11.

[0052] In a more preferred embodiment, the upper side of the guide plate structure 2 is configured as an effluent separation zone 6, which is equipped with multiple three-phase separation pipe assemblies, each of which has a connecting pipe 921; the lower side of the guide plate structure 2 is configured as a bottom gap zone 7; when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body 1 is <0.3mm, the treatment unit can adjust the arrangement direction of the connecting pipe 921 to face the effluent separation zone 6 according to the comparison result. When the comparison result shows that the particle size of the aerobic granular sludge in the reactor body 1 is 0.3mm to 1.8mm, the treatment unit can adjust the arrangement direction of the connecting pipe 921 to be perpendicular to the inner wall of the reactor body 1 according to the comparison result. When the comparison result shows that the particle size of the aerobic granular sludge in the reactor body 1 is >1.8mm, the treatment unit can adjust the arrangement direction of the connecting pipe 921 to face the bottom gap zone 7 according to the comparison result.

[0053] As a more preferred implementation method, such as Figure 1 and Figure 2The effluent separation zone 6 is equipped with an effluent weir 8 and a three-phase separator 9. The effluent weir 8 is fixedly connected to the top inner wall of the reactor body 1. Specifically, the area containing the effluent weir 8 and the three-phase separator 9 is the effluent separation zone. The effluent weir 8 is located in the effluent separation zone 6 and is fixedly connected to the top inner wall of the reactor body 1. One end of the outlet 14 is connected to the effluent weir 8 to discharge the wastewater separated within the effluent weir 8. The wastewater separated by the three-phase separator 9 enters the effluent weir 8 and is discharged from the outlet 14.

[0054] like Figure 6 and Figure 7 The three-phase separation device 9 includes a separation zone partition 91 and multiple three-phase separation pipe assemblies 92. The separation zone partition 91 is disposed in the effluent separation zone 6 and corresponds to the position of the first fluid zone 4; the separation zone partition 91 is fixedly connected to the effluent weir 8 or integrally connected. Multiple three-phase separation pipe assemblies 92 are provided and mounted on the separation zone partition 91; for example, the three-phase separation pipe assemblies 92 are fixedly mounted on the separation zone partition 91 by bolts. Each three-phase separation pipe assembly 92 has a connecting pipe 921, and the angle between each connecting pipe 921 and the separation zone partition 91 is θ. Specifically, the angle θ is 0° or ±45°. For example, when the angle θ is +45°, the connecting pipe 921 is inclined upwards; when the angle θ is 0°, the connecting pipe 921 is horizontal; when the angle θ is -45° or 135°, the connecting pipe 921 is inclined downwards. The state with an included angle θ of -45° is the state after the three-phase separator assembly 92 has been rotated 180°.

[0055] As a more preferred implementation method, such as Figure 6 The reactor body 1 has a sludge discharge port 12 at its bottom, positioned between the first fluid zone 4 and the second fluid zone 5. The sludge discharge port 12 is used to discharge the formed aerobic granular sludge. Figure 1 and Figure 2 The reactor body 1 has an inlet pipe 13 on one side of its bottom and an outlet pipe 14 on one side of its top. The inlet pipe 13 is located at one end of the second fluid zone 5 near the bottom clearance zone 7, and the outlet pipe 14 is installed on the side wall of the effluent weir 8. Specifically, domestic sewage and aerobic sludge are supplied through the inlet pipe 13, and the separated sewage is discharged through the outlet pipe 14. For example, the influent flow rate in the reactor body 1 is adjusted to 0.6 m³ / s by the inlet pipe 13. 3 / h~1.9m 3 The sludge volume index is 22 mg / L to 38 mg / L, and the suspended solids content of the mixed liquor is 4200 mg / L to 5000 mg / L. This reactor allows for flexible adjustment of its internal components according to operating conditions to alter the flow field and achieve the goal of cultivating aerobic granular sludge.

[0056] Based on the above embodiments, this invention employs a dual-aeration countercurrent mass transfer reactor for the cultivation of aerobic granular sludge. The method for cultivating aerobic granular sludge includes the following steps:

[0057] Step 1: Obtain the influent load of reactor body 1 and the particle size of aerobic granular sludge inside reactor body 1.

[0058] Step 2: Based on the influent load of reactor body 1, adjust the aeration type of the first aeration head 31 and the second aeration head 32 to determine the fluid direction of the first fluid zone 4 and the second fluid zone 5. Specifically, when the influent load detection data is <1.2 kg COD·m³, -3 ·d -1 At this time, adjust the aeration type of the second aeration head 32 to nitrogen-rich gas to configure the second fluid zone 5 as the rising zone, and adjust the aeration type of the first aeration head 31 to oxygen to configure the first fluid zone 4 as the falling zone. Alternatively, when the influent load detection data is ≥1.2 kg COD·m³... -3 ·d -1 At the same time, the aeration type of the first aeration head 31 is adjusted to nitrogen-rich gas to configure the first fluid zone 4 as an ascending zone, and the aeration type of the second aeration head 32 is adjusted to oxygen to configure the second fluid zone 5 as a descending zone. Specifically, the aeration head 3 in the ascending zone aerates nitrogen-rich gas to provide the driving force for the circulation of the reaction fluid; the aeration head 3 in the descending zone aerates oxygen to maintain the dissolved oxygen level in the reaction fluid through countercurrent mass transfer.

[0059] Step 3: Adjust the aeration rate of the first aeration head 31 and the second aeration head 32 according to the particle size of the aerobic granular sludge in reactor body 1; and as the particle size of the aerobic granular sludge in reactor body 1 gradually increases, the aeration rate of the first aeration head 31 and the second aeration head 32 gradually increases. Specifically, the influent load detection data is <1.2 kg COD·m³. -3 ·d -1 Meanwhile, when the particle size of the aerobic granular sludge in reactor body 1 is <0.3mm, the aeration rate of the first aeration head 31 is 4m³ / s. 3 / h~6m 3 / h, the aeration rate of the second aeration head 32 is 10m³ / h. 3 / h~15m 3 / h; When the particle size of the aerobic granular sludge in reactor body 1 is 0.3mm to 1.8mm, the aeration rate of the first aeration head 31 is 6m³ / h. 3 / h~8m 3 / h, the aeration rate of the second aeration head 32 is 15m³ / h. 3 / h~20m 3 / h; When the particle size of the aerobic granular sludge in reactor body 1 is >1.8mm, the aeration rate of the first aeration head 31 is 8m³ / h. 3 / h~10m 3 / h, the aeration rate of the second aeration head 32 is 20m³ / h. 3 / h~25m 3 / h. Or, the influent load test data is ≥1.2kg COD·m³. -3 ·d -1 Meanwhile, when the particle size of the aerobic granular sludge in reactor body 1 is <0.3mm, the aeration rate of the second aeration head 32 is 10m³. 3 / h~12m 3 / h, the aeration rate of the first aeration head 31 is 20m³ / h. 3 / h~25m 3 / h; When the particle size of the aerobic granular sludge in reactor body 1 is 0.3mm to 1.8mm, the aeration rate of the second aeration head 32 is 12m³ / h. 3 / h~14m 3 / h, the aeration rate of the first aeration head 31 is 25m³ / h. 3 / h~30m 3 / h; When the particle size of the aerobic granular sludge in reactor body 1 is >1.8mm, the aeration rate of the second aeration head 32 is 14m³ / h. 3 / h~18m 3 / h, the aeration rate of the first aeration head 31 is 30m³ / h. 3 / h~35m 3 / h.

[0060] Step 4: Adjust the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1, as well as the arrangement direction of the connecting pipe 921, according to the particle size of the aerobic granular sludge in the reactor body 1. Specifically, when the particle size of the aerobic granular sludge in the reactor body 1 is <0.3mm, adjust the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1 to a first height h1, and adjust the arrangement direction of the connecting pipe 921 towards the effluent separation zone 6 on the upper side of the guide plate structure 2. Specifically, adjusting the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1 to the first height h1 results in the minimum distance between the bottom of the guide plate 22 and the bottom plate of the reactor body 1. For example, when the side notch of the guide plate 22 is located exactly at the long support bar, the bottom of the guide plate 22 is 0.3m from the bottom plate of the reactor body 1. Adjust the arrangement direction of the connecting pipe 921 to face the effluent separation zone 6 on the upper side of the guide plate structure 2. At this time, the arrangement direction of the connecting pipe 921 is upward to reduce the aerobic granular sludge entering the effluent separation zone 6; that is, when the included angle θ is +45°, the connecting pipe 921 is tilted upward.

[0061] When the particle size of the aerobic granular sludge in reactor body 1 is 0.3mm to 1.8mm, the distance between the bottom of the guide plate structure 2 and the bottom of reactor body 1 is maintained at a first height h1, and the arrangement direction of the connecting pipe 921 is adjusted to be straight against the inner wall of reactor body 1. At this time, the connecting pipe 921 of the three-phase separation pipe assembly 92 is adjusted to be arranged horizontally so that the relatively larger AGS particles enter the descending zone to achieve particle size screening of aerobic granular sludge. When the included angle θ is 0°, the connecting pipe 921 is set horizontally.

[0062] When the particle size of the aerobic granular sludge in the reactor body 1 is >1.8mm, the distance between the bottom of the guide plate structure 2 and the bottom of the reactor body 1 is adjusted to a second height h2, and the second height h2 is greater than the first height h1; this accelerates the flow velocity of the fluid at the bottom of the reactor body 1, and the formed aerobic granular sludge is deposited in the bottom gap region 7 and discharged. For example, the second height h2 = 0.6m. At this time, the distance between the bottom of the guide plate 22 and the bottom plate of the reactor body 1 is the maximum distance. For example, when the side notch of the guide plate 22 corresponds to the position of the short support bar, and the side notch 221 does not contact the short support bar; at this time, the guide plate 22 without the side notch 221 contacts the long support bar, playing a supporting role, and the bottom of the guide plate 22 is 0.6m away from the bottom of the reactor body 1. And the arrangement direction of the connecting pipe 921 is adjusted to face the bottom gap region 7 below the guide plate structure 2. At this time, the rotating guide plate structure 2 causes the connecting pipe 921 of the three-phase separation pipe assembly 92 to be arranged downwards; this allows larger aerobic granular sludge particles to enter the effluent separation zone 6 or increases the amount of aerobic granular sludge entering the effluent separation zone 6. That is, when the included angle θ is -45° or 135°, the connecting pipe 921 is tilted downwards. The state with included angle θ of -45° is the state after the three-phase separation pipe assembly 92 has been rotated 180°.

[0063] The specific operation method is as follows:

[0064] Implementation Method 1: When AGS is still in the early stage of cultivation, the influent load is low, <1.2 kg COD·m³. -3 ·d -1 At this stage, only a small amount of oxygen is needed to maintain the system. The aerator in the center aerates oxygen, while the four aerators around the perimeter aerate nitrogen-rich gas. When the AGS particle size is small (<0.3mm), the oxygen aeration rate is 4m³ / s. 3 / h~6m 3 / h, nitrogen-rich gas aeration rate 10m³ 3 / h~15m 3The flow rate is set at 0.3m above the bottom plate, and 0.5m above the liquid surface. The near-liquid surface velocity is low, and the connecting pipe of the three-phase separation pipe is arranged at an upward 45° angle to reduce the amount of sludge entering the separation zone. When the particle size increases (0.3mm ≤ particle size ≤ 1.8mm), a horizontal connecting pipe is used to increase the amount of sludge entering the separation zone. Smaller light sludge particles more easily enter the three-phase separation connecting pipe and thus the separation zone with the wastewater, while larger heavy sludge particles directly enter the descending zone, achieving particle size screening of the sludge. Oxygen aeration rate is 6m³ / h. 3 / h~8m 3 / h, nitrogen-rich gas aeration rate 15m³ 3 / h~20m 3 / h. When the particle size further increases, i.e., the particle size > 1.8 mm, the height of the guide plate from the bottom plate is adjusted to 0.6 m. At this time, the height of the guide plate from the liquid surface is 0.2 m, and the fluid near the liquid surface has a higher velocity. A downward 45° connecting pipe is selected and the aeration rate is increased, i.e., the oxygen aeration rate is 8 m³ / h. 3 / h~10m 3 / h, nitrogen-rich gas aeration rate 20m³ 3 / h~25m 3 / h.

[0065] Implementation Method 2: When the influent load is high, >1.2 kg COD·m -3 ·d -1 At this time, a large amount of oxygen is required. The aerator head at the center aerates nitrogen-rich gas, while the four aerator heads around the perimeter aerate oxygen. That is, the center of the reactor body is the rising zone, and the perimeter is the falling zone. When the AGS particle size is small, i.e., <0.3mm, the oxygen aeration rate is 10m³ / h. 3 / h~12m 3 / h, nitrogen-rich gas aeration rate 20m³ 3 / h~25m 3 With a flow rate of / h, the height of the guide plate from the bottom plate is set to 0.3m. At this point, the height of the guide plate from the liquid surface is 0.5m, resulting in a lower near-liquid surface velocity. The connecting pipe of the three-phase separation pipe is arranged downwards at 45° to reduce the amount of sludge entering the separation zone. When the particle size increases (0.3mm ≤ particle size ≤ 1.8mm), a horizontal connecting pipe is used to increase the amount of sludge entering the separation zone. Smaller light sludge particles are more likely to enter the three-phase separation connecting pipe with the wastewater and thus enter the separation zone, while larger heavy sludge particles directly enter the descending zone. This allows for particle size screening of the sludge. Oxygen aeration rate is 12m³ / h. 3 / h~14m 3 / h, nitrogen-rich gas aeration rate 25m³ / h 3 / h~30m 3 / h. When the particle size further increases, i.e., the particle size > 1.8 mm, the height of the guide plate from the bottom plate is adjusted to 0.6 m. At this time, the height of the guide plate from the liquid surface is 0.2 m, and the fluid near the liquid surface has a higher velocity. A connecting pipe at an upward 45° angle is selected, and the aeration rate is increased to 14 m³ / h. 3 / h~18m 3 / h, nitrogen-rich gas aeration rate 30m³ 3 / h~35m 3 / h.

[0066] This invention presents a dual-aeration airlift reactor with separate driving force and dissolved oxygen control, designed according to one embodiment. The main innovation lies in the reactor structure, which separates driving force control from dissolved oxygen control, making parameters such as settling selectivity and hydraulic shear force adjustable, thus further exploring the potential of airlift reactors in cultivating granular sludge. In pursuit of stable flow field and dissolved oxygen levels under varying influent loads, the invention analyzes the water quality conditions, fluid dynamics, and stable operating range for AGS cultivation, establishing a mathematical model relating organic load, oxygen supply, fluid dynamics characteristics, and pollutant degradation. This provides a theoretical basis and operating conditions for the promotion of AGS technology and reactor scale-up.

[0067] This is merely a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A dual-aeration countercurrent mass transfer reaction device, characterized in that, The device, used for cultivating aerobic granular sludge, includes: Reactor body (1); A flow guide structure (2) is disposed inside the reactor body (1); the flow guide structure (2) divides the interior of the reactor body (1) into a first fluid zone (4) and a plurality of second fluid zones (5); the plurality of second fluid zones (5) are disposed outside the first fluid zone (4); The aeration head (3) includes a first aeration head (31) and a second aeration head (32). The first aeration head (31) is disposed on the lower side of the first fluid zone (4); the second aeration head (32) is disposed on the lower side of the corresponding second fluid zone (5); the aeration types of the first aeration head (31) and the second aeration head (32) are different. The aeration type of the first aeration head (31) and the second aeration head (32) is selected from oxygen or nitrogen-rich gas, respectively, and the aeration volume of nitrogen-rich gas is greater than that of oxygen. The aeration type of the first aeration head (31) and the second aeration head (32) changes with the increase of the influent load of the reactor body (1) to adjust the fluid direction of the first fluid zone (4) and the second fluid zone (5); The aeration rate of the first aeration head (31) and the second aeration head (32) gradually increases with the increase of the particle size of the aerobic granular sludge in the reactor body (1); Also includes: The inlet water detection unit is used to analyze and detect the inlet water load of the reactor body (1) and send it to the processing unit; The particle size detection unit is used to analyze and detect the particle size of the aerobic granular sludge in the reactor body (1) and send it to the processing unit; The processing unit is used to receive the influent load detection data sent by the influent detection unit and the particle size detection data sent by the particle size detection unit, compare the influent load detection data with the set influent load data, compare the particle size detection data with the set particle size data, and adjust the aeration type and aeration volume of the first aeration head (31) and the second aeration head (32) according to the comparison result. The conditions for adjusting the aeration type of the first aeration head (31) and the second aeration head (32) based on the comparison results are as follows: When the influent load test data is <1.2kg COD·m -3 ·d -1 At the same time, the aeration type of the second aeration head (32) is adjusted to nitrogen-rich gas so that the second fluid zone (5) is configured as the rising zone, and the aeration type of the first aeration head (31) is adjusted to oxygen so that the first fluid zone (4) is configured as the falling zone. Alternatively, when the influent load test data is ≥1.2 kg COD·m -3 ·d -1 At the same time, the aeration type of the first aeration head (31) is adjusted to nitrogen-rich gas so that the first fluid zone (4) is configured as the rising zone, and the aeration type of the second aeration head (32) is adjusted to oxygen so that the second fluid zone (5) is configured as the falling zone.

2. The dual-aeration countercurrent mass transfer reactor according to claim 1, characterized in that, The conditions for adjusting the aeration rate of the first aeration head (31) and the second aeration head (32) based on the comparison results are as follows: When the influent load test data is <1.2kg COD·m -3 ·d -1 As the particle size of the aerobic granular sludge in the reactor body (1) gradually increases, the aeration rate of the first aeration head (31) increases from 4 m³ / s. 3 / h~6m 3 / h gradually increased to 8m 3 / h~10m 3 / h; the aeration rate of the second aeration head (32) is 10m 3 / h~15m 3 / h gradually increased to 20m 3 / h~25m 3 / h; Alternatively, when the influent load test data is ≥1.2 kg COD·m -3 ·d -1 As the particle size of the aerobic granular sludge in the reactor body (1) gradually increases, the aeration rate of the second aeration head (32) increases from 10 m³ / s. 3 / h~12m 3 / h gradually increased to 14m 3 / h~18m 3 / h; the aeration rate of the first aeration head (31) is 20m 3 / h~25m 3 / h gradually increased to 30m 3 / h~35m 3 / h.

3. The dual-aeration countercurrent mass transfer reaction device according to claim 1, characterized in that, The processing unit can issue a prompting command to adjust the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) based on the comparison results. When the comparison result shows that the particle size of the aerobic granular sludge in the reactor body (1) is ≤1.8mm, the processing unit can issue a prompt instruction to adjust the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) to the first height (h1) according to the comparison result. Alternatively, when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body (1) is >1.8 mm, the processing unit can issue a prompt instruction to adjust the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) to a second height (h2) according to the comparison result; the second height (h2) is greater than the first height (h1).

4. The dual-aeration countercurrent mass transfer reactor according to claim 1, characterized in that, The upper side of the guide plate structure (2) is configured as a water separation zone (6), and the water separation zone (6) is equipped with multiple three-phase separation pipe assemblies, each of which has a connecting pipe (921). The lower side of the guide vane structure (2) is configured as a bottom gap area (7); The processing unit can issue a prompting command to adjust the arrangement direction of the connecting pipe (921) based on the comparison result; When the comparison result shows that the particle size of the aerobic granular sludge in the reactor body (1) is <0.3mm, the treatment unit can adjust the arrangement direction of the connecting pipe (921) to face the effluent separation zone (6) according to the comparison result. Alternatively, when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body (1) is 0.3 mm to 1.8 mm, the processing unit can adjust the arrangement direction of the connecting pipe (921) to be perpendicular to the inner wall of the reactor body (1) according to the comparison result. Alternatively, when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body (1) is >1.8 mm, the treatment unit can adjust the arrangement direction of the connecting pipe (921) to face the bottom gap area (7) according to the comparison result.

5. A method for cultivating aerobic granular sludge, characterized in that, The reaction is carried out using the dual-aeration countercurrent mass transfer apparatus as described in claim 4, and the specific method includes the following steps: Obtain the influent load of the reactor body (1) and the particle size of the aerobic granular sludge inside the reactor body (1); According to the influent load of the reactor body (1), the aeration type of the first aeration head (31) and the second aeration head (32) is adjusted to determine the fluid direction of the first fluid zone (4) and the second fluid zone (5); The aeration rate of the first aeration head (31) and the second aeration head (32) is adjusted according to the particle size of the aerobic granular sludge in the reactor body (1); and as the particle size of the aerobic granular sludge in the reactor body (1) gradually increases, the aeration rate of the first aeration head (31) and the second aeration head (32) gradually increases.

6. The method for cultivating aerobic granular sludge according to claim 5, characterized in that, The method for adjusting the aeration type of the first aeration head (31) and the second aeration head (32) according to the influent load of the reactor body (1) is as follows: When the influent load test data is <1.2kg COD·m -3 ·d -1 At the same time, the aeration type of the second aeration head (32) is adjusted to nitrogen-rich gas so that the second fluid zone (5) is configured as the rising zone, and the aeration type of the first aeration head (31) is adjusted to oxygen so that the first fluid zone (4) is configured as the falling zone. Alternatively, when the influent load test data is ≥1.2 kg COD·m -3 ·d -1 At the same time, the aeration type of the first aeration head (31) is adjusted to nitrogen-rich gas so that the first fluid zone (4) is configured as the rising zone, and the aeration type of the second aeration head (32) is adjusted to oxygen so that the second fluid zone (5) is configured as the falling zone.

7. The method for cultivating aerobic granular sludge according to claim 5, characterized in that, The method for adjusting the aeration rate of the first aeration head (31) and the second aeration head (32) based on the particle size of the aerobic granular sludge in the reactor body (1) is as follows: When the influent load test data is <1.2kg COD·m -3 ·d -1 As the particle size of the aerobic granular sludge in the reactor body (1) gradually increases, the aeration rate of the first aeration head (31) increases from 4 m³ / s. 3 / h~6m 3 / h gradually increased to 8m 3 / h~10m 3 / h; the aeration rate of the second aeration head (32) is 10m 3 / h~15m 3 / h gradually increased to 20m 3 / h~25m 3 / h; Alternatively, when the influent load test data is ≥1.2 kg COD·m -3 ·d -1 As the particle size of the aerobic granular sludge in the reactor body (1) gradually increases, the aeration rate of the second aeration head (32) increases from 10 m³ / s. 3 / h~12m 3 / h gradually increased to 14m 3 / h~18m 3 / h; the aeration rate of the first aeration head (31) is 20m 3 / h~25m 3 / h gradually increased to 30m 3 / h~35m 3 / h.

8. The method for cultivating aerobic granular sludge according to claim 5, characterized in that, After obtaining the particle size of the aerobic granular sludge in the reactor body (1), the method further includes: According to the particle size of the aerobic granular sludge in the reactor body (1), adjust the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) and the arrangement direction of the connecting pipe (921). The method for adjusting the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) and the arrangement direction of the connecting pipe (921) according to the particle size of the aerobic granular sludge in the reactor body (1) is as follows: When the particle size of the aerobic granular sludge in the reactor body (1) is <0.3mm, the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) is adjusted to the first height (h1), and the arrangement direction of the connecting pipe (921) is adjusted to face the effluent separation zone (6) on the upper side of the guide plate structure (2). When the particle size of the aerobic granular sludge in the reactor body (1) is 0.3mm to 1.8mm, the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) is maintained to the first height (h1), and the arrangement direction of the connecting pipe (921) is adjusted to be straight to the inner wall of the reactor body (1). When the particle size of the aerobic granular sludge in the reactor body (1) is >1.8mm, the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) is adjusted to the second height (h2), and the arrangement direction of the connecting pipe (921) is adjusted to face the bottom gap area (7) on the lower side of the guide plate structure (2); and the second height (h2) is greater than the first height (h1).

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