Double-aeration countercurrent mass transfer reaction device and method

Abstract

The invention relates to the technical field of aerobic granular sludge formation, in particular to a double-aeration countercurrent mass transfer reaction device and method. The device comprises a reactor body, a guide plate structure and an aeration head, wherein the guide plate structure divides the interior of the reactor body into a first fluid region and a plurality of second fluid regions; the aeration heads comprise 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 quantity of the nitrogen-rich gas is greater than that of the oxygen. According to the method, the flow field driving force of the reactor body is maintained through the nitrogen-rich gas; the dissolved oxygen amount is maintained in an oxygen countercurrent mass transfer mode, the retention time of bubbles in the reactor body is prolonged, the oxygen utilization rate is improved, and the problems that a traditional airlift reactor cannot maintain the flow field stability under the load change, and the contradiction exists between the requirement of high-load wastewater for aeration amount increase and sludge particle crushing are solved.

Description

Technical Field

[0001] The invention relates to the technical field of aerobic granular sludge formation, and in particular to a double aeration countercurrent mass transfer reaction device and method. Background Art

[0002] Aerobic granular sludge, the full name of which is Aerobic Granular Sludge, or AGS for short. In the field of environmental protection and wastewater treatment, AGS technology has attracted much attention due to its unique performance and broad application prospects. AGS is a microbial aggregate obtained by the self-immobilization and aggregation growth of microorganisms in flocculent sludge under a suitable environment, and has a compact and dense spherical structure. AGS has the advantages of good solid-liquid separation, high biomass concentration, strong tolerance, and short hydraulic retention time. It can effectively treat industrial sewage or wastewater such as high-concentration organic wastewater and high-salinity wastewater.

[0003] The success of AGS cultivation technology depends on efficient reactor design and optimization. Traditional AGS reactor types include SBR reactors, MBR reactors and airlift reactors. Among them, airlift reactors show certain potential in the cultivation of AGS due to their high shear force. The structure of the airlift reactor can generally be divided into a three-phase mixing zone and a separation zone. The sedimentation selection pressure and hydraulic shear force can be adjusted by adjusting the internal components and aeration volume, thereby achieving rapid sludge granulation. However, in the actual cultivation process, the influent load in the reactor is changing. The traditional airlift reactor cannot maintain the flow field stability under load changes for the cultivation of AGS, and the demand for increased aeration volume for high-load wastewater is in conflict with the crushing of sludge particles. In short, the contradiction between the maintenance of the flow field driving force of the traditional airlift reactor and the regulation of dissolved oxygen has limited the application of airlift reactors in AGS cultivation. Summary of the invention

[0004] In order to solve the problems that traditional airlift reactors cannot maintain flow field stability under load changes, and there is a contradiction between the demand for increased aeration volume in high-load wastewater and the crushing of sludge particles, the purpose of the present invention is to provide a double aeration countercurrent mass transfer reaction device and method for cultivating aerobic granular sludge. The device of the present invention can not only cope with changes in influent load, but also maintain flow field stability 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 the present invention provides a dual-aeration countercurrent mass flow reaction device, which is used for cultivating aerobic granular sludge. The device includes: a reactor body; a guide plate structure, which is arranged in the reactor body; the guide plate structure divides the interior of the reactor body into a first fluid zone and a plurality of second fluid zones; the plurality of second fluid zones are arranged outside the first fluid zone; an aeration head, including a first aeration head and a second aeration head, the first aeration head is arranged at the lower side of the first fluid zone; the second aeration head is arranged at the lower side of the second fluid zone corresponding thereto; 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 the aeration amount of oxygen; the aeration types of the first aeration head and the second aeration head change with the increase of the water inlet load of the reactor body to adjust the fluid direction of the first fluid zone and the second fluid zone; the aeration amount of the first aeration head and the second aeration head gradually increases with the increase of the particle size of the aerobic granular sludge in the reactor body.

[0007] The present invention independently controls the aeration type and aeration amount of the first aeration head and the second aeration head corresponding to the first fluid zone and the second fluid zone, thereby establishing a dual-aeration countercurrent mass transfer reaction device in which airlift and countercurrent oxygen supply are independently controlled. The dual-aeration countercurrent mass transfer reaction device of the present invention can change the aeration type and aeration amount of the first aeration head and the second aeration head according to the change of the influent load and the particle size of the aerobic granular sludge, and can maintain the stability of the flow field and the dissolved oxygen while coping with the change of the influent load, thereby solving the problem that the unified airlift reactor cannot maintain the stability of the flow field under load changes, and the contradiction between the demand for increased aeration amount of high-load wastewater and the crushing of sludge particles.

[0008] Preferably, the distance between the bottom of the guide plate 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 increases the flow rate of the fluid at the bottom of the reactor body by increasing the distance between the bottom of the guide plate structure and the bottom of the reactor body when the particle size of the aerobic granular sludge reaches >1.8 mm.

[0009] Preferably, the upper side of the guide plate structure is configured as a water outlet separation zone, and the water outlet separation zone is equipped with a plurality of three-phase separation tube assemblies, each of which has a connecting tube; the lower side of the guide plate 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 tube gradually deflects in the direction toward the water outlet separation zone. The purpose of changing the arrangement direction of the connecting tube is to ensure the reaction growth of the aerobic granular sludge in the reactor body when the particle size of the aerobic granular sludge is relatively small; as the particles increase, further changing the arrangement direction of the connecting tube helps to promote the aerobic granular sludge with a relatively large particle size to enter the descending zone, so as to achieve the particle size screening of the aerobic granular sludge, and when the particle size of the aerobic granular sludge reaches>1.8mm, the aerobic granular sludge with larger particles can enter the water outlet separation zone or increase the amount of aerobic granular sludge entering the water outlet separation zone to separate the aerobic granular sludge.

[0010] In the present 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 also includes: a water inlet detection unit, used for analyzing and detecting the water inlet load of the reactor body, and sending it to the processing unit; a particle size detection unit, used for analyzing and detecting the particle size of the aerobic granular sludge in the reactor body, and sending it to the processing unit; a processing unit, used for receiving the water inlet load detection data sent by the water inlet detection unit and the particle size detection data sent by the particle size detection unit, and comparing the water inlet load detection data with the set water inlet load data, and comparing the particle size detection data with the set particle size data, and adjusting the aeration type and aeration amount of the first aeration head and the second aeration head according to the comparison result.

[0012] Preferably, the condition for adjusting the aeration type of the first aeration head and the second aeration head according to the comparison result is: when the water inlet load detection data is less than 1.2 kg COD·m -3 ·d -1 When the aeration type of the second aeration head is adjusted to nitrogen-rich gas, the second fluid zone is configured as an ascending zone, and the aeration type of the first aeration head is adjusted to oxygen, so that the first fluid zone is configured as a descending zone; or, when the inlet load detection data is ≥1.2kg COD·m -3 ·d -1 When the aeration type of the first aeration head is adjusted to nitrogen-rich gas, the first fluid zone is configured as an ascending zone, and the aeration type of the second aeration head is adjusted to oxygen, so as to configure the second fluid zone as a descending zone.

[0013] Preferably, the condition for adjusting the aeration amount of the first aeration head and the second aeration head according to the comparison result is: when the water inlet load detection data is less than 1.2 kg COD·m -3 ·d -1 As the particle size of the aerobic granular sludge in the reactor body gradually increases, the aeration volume of the first aeration head increases from 4m 3 / h~6m 3 / h gradually increase to 8m 3 / h~10m 3 / h; the aeration volume of the second aeration head is 10m 3 / h~15m 3 / h gradually increase to 20m 3 / h~25m 3 / h; or, when the water inlet load test data is ≥1.2kgCOD·m -3 ·d -1 As the particle size of the aerobic granular sludge in the reactor body gradually increases, the aeration volume of the second aeration head increases from 10m 3 / h~12m 3 / h gradually increased to 14m 3 / h~18m 3 / h; the aeration volume of the first aeration head is 20m 3 / h~25m 3 / h gradually increase to 30m 3 / h~35m 3 / h.

[0014] Preferably, the condition for adjusting the aeration amount of the first aeration head and the second aeration head according to the comparison result is: the water inlet load detection data <1.2kg COD·m -3 ·d -1 At the same time, when the particle size of the aerobic granular sludge in the reactor body is less than 0.3 mm, the aeration volume of the first aeration head is 4 m 3 / h~6m 3 / h, the aeration volume of the second aeration head is 10m 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 volume of the first aeration head is 6m 3 / h~8m 3 / h, the aeration volume of the second aeration head is 15m 3 / h~20m 3 / h; when the particle size of aerobic granular sludge in the reactor body is >1.8mm, the aeration volume of the first aeration head is 8m 3 / h~10m 3 / h, the aeration volume of the second aeration head is 20m 3 / h~25m 3 / h; or, water inlet load test data ≥ 1.2kg COD·m -3 ·d -1 At the same time, when the particle size of the aerobic granular sludge in the reactor body is less than 0.3 mm, the aeration volume of the second aeration head is 10 m 3 / h~12m 3 / h, the aeration volume of the first aeration head is 20m 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 volume of the second aeration head is 12m 3 / h~14m 3 / h, the aeration volume of the first aeration head is 25m 3 / h~30m 3 / h; when the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the aeration volume of the second aeration head is 14m 3 / h~18m 3 / h, the aeration volume of the first aeration head is 30m 3 / h~35m 3 / h.

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

[0016] Preferably, four supporting parts are arranged around the bottom of the reactor body; the heights of the two supporting parts arranged opposite to each other are the same, and the two supporting parts arranged adjacent to each other have a height difference; the guide plate structure has two side notches, and the two side notches are respectively arranged on the two supporting parts arranged opposite to each other 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 tube and four guide plates; the four guide plates are respectively fixed on the side walls of the guide inner tube; the two side notches are arranged at the bottom of the two guide plates arranged opposite to each other, so that the two guide plates arranged opposite to each other are respectively overlapped and arranged on the supporting parts corresponding to them. Preferably, the height difference between the two supporting parts arranged adjacent to each other is 0.2m to 0.6m. By adjusting the distance between the bottom of the guide plate structure and the bottom of the reactor body within the set height difference range, it is helpful to accelerate the flow rate of the fluid at the bottom of the reactor body.

[0017] Preferably, the upper side of the guide plate structure is configured as a water outlet separation zone, and the water outlet separation zone is equipped with a plurality of three-phase separation tube assemblies, each of which has a connecting tube; the lower side of the guide plate structure is configured as a bottom gap zone; the processing unit can issue a prompt instruction for adjusting the arrangement direction of the connecting tube according to the comparison result; when the comparison result is that the particle size of the aerobic granular sludge in the reactor body is <0.3mm, the processing unit can issue a prompt instruction for adjusting the arrangement direction of the connecting tube to the direction toward the water outlet separation zone according to the comparison result; or, when the comparison result is that the particle size of the aerobic granular sludge in the reactor body is 0.3mm~1.8mm, the processing unit can issue a prompt instruction for adjusting the arrangement direction of the connecting tube to the direction perpendicular to the inner wall of the reactor body according to the comparison result; or, when the comparison result is that the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the processing unit can issue a prompt instruction for adjusting the arrangement direction of the connecting tube to the direction toward the bottom gap zone according to the comparison result.

[0018] The second aspect of the present invention provides a method for cultivating aerobic granular sludge, which is carried out using the double aeration countercurrent mass transfer reaction device of the first aspect, and the specific method comprises the following steps:

[0019] The water inlet load of the reactor body and the particle size of the aerobic granular sludge in the reactor body are obtained; according to the water inlet load of the reactor body, the aeration types of the first aeration head and the second aeration head are adjusted to determine the fluid directions of the first fluid zone and the second fluid zone; according to the particle size of the aerobic granular sludge in the reactor body, the aeration amounts of the first aeration head and the second aeration head are adjusted; and as the particle size of the aerobic granular sludge in the reactor body gradually increases, the aeration amounts of the first aeration head and the second aeration head gradually increase.

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

[0021] Preferably, the method for adjusting the aeration amount of the first aeration head and the second aeration head according to the particle size of the aerobic granular sludge in the reactor body is as follows: when the inlet load detection data is less than 1.2 kg COD·m -3 ·d -1 As the particle size of the aerobic granular sludge in the reactor body gradually increases, the aeration volume of the first aeration head increases from 4m 3 / h~6m 3 / h gradually increase to 8m 3 / h~10m 3 / h; the aeration volume of the second aeration head is 10m 3 / h~15m 3 / h gradually increase to 20m 3 / h~25m 3 / h; or, when the inlet load test data is ≥1.2kg COD·m -3 ·d -1 As the particle size of the aerobic granular sludge in the reactor body gradually increases, the aeration volume of the second aeration head increases from 10m 3 / h~12m 3 / h gradually increased to 14m 3 / h~18m 3 / h; the aeration volume of the first aeration head is 20m 3 / h~25m 3 / h gradually increase to 30m 3 / h~35m 3 / h.

[0022] Preferably, the method for adjusting the aeration amount of the first aeration head and the second aeration head according to the particle size of the aerobic granular sludge in the reactor body is as follows: the inlet load detection data is less than 1.2 kg COD·m -3 ·d -1 At the same time, when the particle size of the aerobic granular sludge in the reactor body is less than 0.3 mm, the aeration volume of the first aeration head is 4 m 3 / h~6m 3 / h, the aeration volume of the second aeration head is 10m3 / h~15m 3 / h; when the particle size of the aerobic granular sludge in the reactor body is 0.3mm~1.8mm, the aeration volume of the first aeration head is 6m 3 / h~8m 3 / h, the aeration volume of the second aeration head is 15m 3 / h~20m 3 / h; when the particle size of aerobic granular sludge in the reactor body is >1.8mm, the aeration volume of the first aeration head is 8m 3 / h~10m 3 / h, the aeration volume of the second aeration head is 20m 3 / h~25m 3 / h; or, water inlet load test data ≥ 1.2kg COD·m -3 ·d -1 At the same time, when the particle size of the aerobic granular sludge in the reactor body is less than 0.3 mm, the aeration volume of the second aeration head is 10 m 3 / h~12m 3 / h, the aeration volume of the first aeration head is 20m 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 volume of the second aeration head is 12m 3 / h~14m 3 / h, the aeration volume of the first aeration head is 25m 3 / h~30m 3 / h; when the particle size of the aerobic granular sludge in the reactor body is >1.8mm, the aeration volume of the second aeration head is 14m 3 / h~18m 3 / h, the aeration volume of the first aeration head is 30m 3 / h~35m 3 / h.

[0023] Preferably, after obtaining the particle size of the aerobic granular sludge in 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 according to the particle size of the aerobic granular sludge in the reactor body; the method of 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 according to the particle size of the aerobic granular sludge in the reactor body is specifically: when the particle size of the aerobic granular sludge in 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 Towards the direction of 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~1.8mm, maintain the distance between the bottom of the guide plate structure and the bottom of the reactor body to a first height, and adjust the arrangement direction of the connecting pipe to be straight in the direction of the inner wall of the reactor body; or, when the particle size of the aerobic granular sludge in the reactor body is>1.8mm, adjust the distance between the bottom of the guide plate structure and the bottom of the reactor body to a second height, and adjust the arrangement direction of the connecting pipe to be towards the bottom gap area on the lower side of the guide plate structure; and the second height is greater than the first height.

[0024] Beneficial effects of the present invention:

[0025] 1. The present invention independently controls the aeration type and aeration amount of the first aeration head and the second aeration head corresponding to the first fluid zone and the second fluid zone to establish a dual-aeration countercurrent mass transfer reaction device with independent control of airlift and countercurrent oxygen supply. The dual-aeration countercurrent mass transfer reaction device of the present invention can change the aeration type and aeration amount of the first aeration head and the second aeration head according to the change of the influent load and the particle size of the aerobic granular sludge. While coping with the change of the influent load, it can maintain the stability of the flow field and the dissolved oxygen, thus solving the problem that the unified airlift reactor cannot maintain the stability of the flow field under load changes, and the contradiction between the demand for increased aeration amount of high-load wastewater and the crushing of sludge particles.

[0026] 2. The double aeration countercurrent mass transfer reaction device of the present invention mainly utilizes nitrogen-rich gas to provide the driving force for the fluid circulation of the reactor, and oxygen maintains the dissolved oxygen content of the reactor in a countercurrent mass transfer manner, so that the gas-liquid-solid three phases are separated at the top of the reactor body, the gas escapes from the liquid surface into the atmosphere, the liquid remains in the reactor body, and finally flows out of the reactor body, and the solid sludge is precipitated at the top of the reactor body and returns to the first fluid zone and the second fluid zone to continue the microbial reaction; the double aeration countercurrent mass transfer reaction device of the present invention can prolong the residence time of oxygen; improve the mass transfer efficiency; by forming a turbulent zone, the collision probability and movement trajectory of the granular sludge are increased, 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 nitrogen-rich gas; maintains the dissolved oxygen content by oxygen countercurrent mass transfer, prolongs the residence time of bubbles in the reactor, improves the utilization rate of gas materials, and solves the problem of flow field stability under load changes in existing airlift reactors. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] Figure 1 It is a side cutaway schematic diagram of a double aeration countercurrent mass transfer reaction device according to an embodiment of the present invention.

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

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

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

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

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

[0034] Figure 7 yes Figure 6 Schematic diagram of perspective A.

[0035] In the figure, 1. reactor body; 11. supporting component; 12. mud outlet; 13. water inlet pipe; 14. water outlet pipe; 2. guide plate structure; 21. guide inner tube; 22. guide plate; 221. side notch; 3. aeration head; 31. first aeration head; 32. second aeration head; 4. first fluid zone; 5. second fluid zone; 6. outlet separation zone; 7. bottom gap zone; 8. outlet 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 DESCRIPTION

[0036] In order to make the purpose, technical scheme and advantages of the present invention clearer, the present invention is further described in detail below in conjunction with the embodiments. It should be understood that the specific embodiments described herein are only used to explain the present invention and are not intended to limit the present invention. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in the field without making creative work are within the scope of protection of the present invention.

[0037] Unless otherwise specified, the methods described in the following embodiments are all conventional methods; the reagents and materials described, unless otherwise specified, can all be purchased on the market. 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%. In the following embodiments of the present invention, nitrogen is used as the nitrogen-enriched gas for detailed description.

[0038] See also Figure 1 A double aeration countercurrent mass transfer reaction device is used to cultivate aerobic granular sludge. The device includes: a reactor body 1, a guide plate structure 2 and a plurality of aeration heads 3.

[0039] The reactor body 1 is mainly used to form a reaction chamber for cultivating aerobic granular sludge. Figure 1 , the longitudinal section of the reactor body 1 is funnel-shaped. Preferably, the cross section of the reactor body 1 is square, and the area of ​​the upper end of the reactor body 1 is larger than the area of ​​the lower end of the reactor body 1, that is, the reactor body 1 is of a size structure with a larger top and a smaller bottom. For example, the length of the lower end of the reactor body 1 is L, the width of the lower end of the reactor body 1 is W, the effective water depth is 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 43.1m 3 The material of the reactor body 1 is a steel concrete structure, which can of course be selected according to actual needs.

[0040] like Figures 3 to 5, the guide plate structure 2 is arranged in the reactor body 1; the guide plate 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 arranged outside the first fluid zone 4. Specifically, in order to facilitate the formation of a turbulent zone, increase the collision probability and movement trajectory of the granular sludge, and promote the formation of granular sludge, a guide plate structure 2 is installed in the reactor body 1, and the reaction chamber in the reactor body 1 is divided into a plurality of fluid zones by the guide plate structure 2. The guide plate structure 2 is arranged in the reactor body 1; the guide plate structure 2 divides the interior of the reactor body 1 into a first fluid zone 4, a water outlet separation zone 6, a second fluid zone 5 and a bottom gap zone 7. Among them, the first fluid zone 4 is located inside the second fluid zone 5. The water outlet separation zone 6 is located on the upper side of the first fluid zone 4, and the bottom gap zone 7 is located on the lower side of 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 of the first fluid zone 4 is from bottom to top, the fluid direction of the second fluid zone 5 is from top to bottom. When the fluid direction of the second fluid zone 5 is from bottom to top, the fluid direction of the first fluid zone 4 is from top to bottom. The first fluid zone 4 is arranged in the internal channel of the guide plate structure 2; the second fluid zone 5 is arranged in 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 gap zone 7 are respectively arranged at both 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 in the reactor body 1 to maintain the stability of the flow field and the dissolved oxygen, so as to cultivate aerobic granular sludge and realize the purpose of 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 arranged at the lower side of the first fluid zone 4; the second aeration head 32 is arranged at the lower side of the second fluid zone 5 corresponding thereto; 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 amount of the nitrogen-rich gas is greater than the aeration amount of the 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 amount 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. In order to maintain the stability of the flow field and the dissolved oxygen, a plurality of aeration heads are arranged in the reactor body 1, which are used for aeration of nitrogen-rich gas or oxygen respectively.

[0042] Specifically, the plurality of second aeration heads 32 are arranged around the outer sides of the plurality of first aeration heads 31. When the first aeration head 31 aerates nitrogen-rich gas and the second aeration head 32 aerates oxygen, the fluid direction of the first fluid zone 4 is from bottom to top, and the fluid direction of the second fluid zone 5 is from top to bottom. When the second aeration head 32 aerates nitrogen-rich gas and the first aeration head 31 aerates oxygen, the fluid direction of the second fluid zone 5 is from bottom to top, and the fluid direction of the first fluid zone 4 is from top to bottom. By adjusting the fluid direction of the first fluid zone 4 and the second fluid zone 5 and the aeration amount of the first aeration head 31 and the second aeration head 32, the flow field is maintained stable and the dissolved oxygen is stable, so as to cultivate aerobic granular sludge and realize rapid sludge granulation.

[0043] In order to facilitate the adjustment of the aeration height, an extension pipe is connected to the corresponding aeration head 3, such as Figure 1 , one end of the extension tube is connected to the bottom of the reactor body 1 by a thread. The extension tube is connected to the corresponding aeration head 3 as needed to change the height of the aeration head 3. The main function of the extension tube is to facilitate and flexibly adjust the height of the aeration head to adapt to different process requirements, for example, to adapt to different sludge characteristics, such as density, viscosity, solid content, etc. By adjusting the height of the aeration head, the aeration effect can also be optimized to ensure that the sludge mixture obtains a uniform oxygen supply to promote the uniform distribution and activity of microorganisms and improve the treatment efficiency of aerobic granular sludge. The appropriate aeration head height also helps to control the sedimentation of aerobic granular sludge. Thereby achieving efficient and economical sludge treatment.

[0044] On the basis of the above-mentioned embodiment, 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 with the increase of the particle size of the aerobic granular sludge in the reactor body 1. Preferably, the upper side of the guide plate structure 2 is configured as the effluent separation zone 6, and the effluent separation zone 6 is equipped with a plurality of 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 the 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 in the direction toward the effluent separation zone 6 and in the direction toward the bottom gap zone 7.

[0045] Specifically, the aeration gas of the first aeration head 31 and the second aeration head 32 is independently selected from oxygen or nitrogen-rich gas; and the ratio of the aeration amount of nitrogen-rich gas to the aeration amount of oxygen is 1.2 to 4:1, such as 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 aeration amount of nitrogen-rich gas is greater than the aeration amount of oxygen. The aeration amount of nitrogen-rich gas and the aeration amount of oxygen are adjusted according to the actual reaction conditions, such as the particle size of the aerobic granular sludge in the reaction system. Nitrogen-rich gas is used to provide power for the circulation of the reaction fluid; 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%. In order to ensure the normal operation of the device, a total of 5 microporous aeration heads are arranged at the bottom of the reactor body 1 to ensure that the superficial gas velocity during operation is greater than 1.2 cm / s. The five microporous aeration heads provide nitrogen-rich gas or oxygen respectively. Nitrogen mainly provides the driving force for the reaction fluid circulation, and oxygen maintains the dissolved oxygen content in the reaction fluid in a countercurrent mass transfer manner.

[0046] As a more preferred embodiment, the device further includes: a water inlet detection unit, a particle size detection unit and a processing unit. The water inlet detection unit is used to analyze and detect the water inlet 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 water inlet load detection data sent by the water inlet detection unit and the particle size detection data sent by the particle size detection unit, and compare the water inlet load detection data with the set water inlet load data, and compare the particle size detection data with the set particle size data, and adjust the aeration type and aeration amount of the first aeration head 31 and the second aeration head 32 according to the comparison result.

[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 result is: when the water inlet load detection data is less than 1.2 kg COD·m -3 ·d -1 When the aeration type of the second aeration head 32 is adjusted to nitrogen-rich gas, the second fluid zone 5 is configured as an ascending 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 a descending zone. Alternatively, when the inlet load detection data is ≥1.2 kg COD·m -3 ·d -1 When the aeration type of the first aeration head 31 is adjusted to nitrogen-rich gas, the first fluid zone 4 is configured as an ascending 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 a descending zone.

[0048] As a more preferred embodiment, the condition for adjusting the aeration amount of the first aeration head 31 and the second aeration head 32 according to the comparison result is: the water inlet load detection data < 1.2 kg COD·m -3 ·d -1 At the same time, when the particle size of the aerobic granular sludge in the reactor body 1 is less than 0.3 mm, the aeration volume of the first aeration head 31 is 4 m 3 / h~6m 3 / h, the aeration volume of the second aeration head 32 is 10m 3 / h~15m 3 / h; when the particle size of the aerobic granular sludge in the reactor body 1 is 0.3mm~1.8mm, the aeration volume of the first aeration head 31 is 6m 3 / h~8m 3 / h, the aeration volume of the second aeration head 32 is 15m 3 / h~20m 3 / h; when the particle size of the aerobic granular sludge in the reactor body 1 is> 1.8mm, the aeration volume of the first aeration head 31 is 8m 3 / h~10m 3 / h, the aeration volume of the second aeration head 32 is 20m 3 / h~25m 3 / h. Or, water inlet load test data ≥ 1.2kg COD·m -3 ·d -1 At the same time, when the particle size of the aerobic granular sludge in the reactor body 1 is less than 0.3 mm, the aeration volume of the second aeration head 32 is 10 m 3 / h~12m 3 / h, the aeration volume of the first aeration head 31 is 20m 3 / h~25m 3 / h; when the particle size of the aerobic granular sludge in the reactor body 1 is 0.3mm~1.8mm, the aeration volume of the second aeration head 32 is 12m 3 / h~14m 3 / h, the aeration volume of the first aeration head 31 is 25m 3 / h~30m 3 / h; when the particle size of the aerobic granular sludge in the reactor body 1 is >1.8mm, the aeration volume of the second aeration head 32 is 14m 3 / h~18m 3 / h, the aeration volume of the first aeration head 31 is 30m 3 / h~35m 3 / h.

[0049] As a more preferred embodiment, 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 according to the comparison result. When the comparison result is 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 is 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 second height h2 according to the comparison result.

[0050] Specifically, the second height h2 is greater than the first height h1. The prompt instruction is a combination of any one or more of a sound prompt, a light prompt, a vibration prompt, and a display prompt. For example, a combination of a sound prompt and a light prompt, etc. The display prompt can display the corresponding height data on an LED display screen. The light prompt can be a flashing or steady light of multiple colors, and the multiple colors of lights represent different heights. The sound prompt can be a voice prompt of the height to be adjusted, or a voice prompt of the particle size of the aerobic granular sludge. In the present invention, the processing unit issuing a prompt instruction belongs to the prior art.

[0051] As a more preferred embodiment, in order to facilitate the adjustment of the distance between the lower surface of the guide plate structure 2 and the bottom of the reactor body 1, as Figure 1 and Figure 3, four support members 11 are arranged around the bottom of the reactor body 1; the heights of the two support members 11 arranged opposite to each other are the same, and the two support members 11 arranged adjacent to each other have a height difference; for example, the height difference of the two support members 11 arranged adjacent to each other is 0.2m to 0.6m; for example, 0.2m, 0.3m, 0.4m, 0.5m, 0.6m, etc. The guide plate structure 2 has two side notches 221, and the two side notches 221 are respectively arranged on the two support members 11 arranged opposite to each other 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 members 11, and the support members 11 are support bars, and two are long and two are short. The support members 11 of the same length are distributed on the opposite sides of the bottom of the reactor body, and the guide plate 22 is also designed with side notches 221 arranged opposite to each other. 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; the guide plate is pulled out and 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, and 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 tube 21 and four guide plates 22; the four guide plates 22 are respectively fixed on the side walls of the guide inner tube 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 are respectively overlapped and arranged on the corresponding support components 11.

[0052] As a more preferred embodiment, the upper side of the guide plate structure 2 is configured as a water outlet separation zone 6, and the water outlet separation zone 6 is equipped with a plurality of 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; when the comparison result is that the particle size of the aerobic granular sludge in the reactor body 1 is <0.3mm, the processing unit can issue an adjustment according to the comparison result. The arrangement direction of the connecting pipe 921 is adjusted to the direction toward the water outlet separation zone 6. When the comparison result is that the particle size of the aerobic granular sludge in the reactor body 1 is 0.3mm~1.8mm, the processing unit can issue an adjustment according to the comparison result. The arrangement direction of the connecting pipe 921 is perpendicular to the inner wall of the reactor body 1. When the comparison result is that the particle size of the aerobic granular sludge in the reactor body 1 is >1.8mm, the processing unit can issue an adjustment according to the comparison result. The arrangement direction of the connecting pipe 921 is adjusted to the direction toward the bottom gap zone 7.

[0053] As a more preferred embodiment, Figure 1 and Figure 2, the effluent separation zone 6 is provided with an effluent weir 8 and a three-phase separation device 9, and the effluent weir 8 is fixedly connected to the top inner wall of the reactor body 1. Specifically, the area where the effluent weir 8 and the three-phase separation device 9 are located is the effluent separation zone. The effluent weir 8 is provided in the effluent separation zone 6 and is fixedly connected to the top inner wall of the reactor body 1. One end of the water outlet 14 is connected to the effluent weir 8 to discharge the sewage separated in the effluent weir 8. The sewage separated by the three-phase separation device 9 enters the effluent weir 8 and is discharged from the water outlet 14.

[0054] like Figure 6 and Figure 7 , the three-phase separation device 9 includes a separation zone partition 91 and a plurality of three-phase separation pipe assemblies 92. The separation zone partition 91 is arranged in the outlet separation zone 6 and corresponds to the position of the first fluid zone 4; the separation zone partition 91 is fixedly connected or integrally connected to the outlet weir 8. There are a plurality of three-phase separation pipe assemblies 92, and they are installed on the separation zone partition 91; for example, the three-phase separation pipe assembly 92 is fixedly installed 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 tilted upward; when the angle θ is 0°, the connecting pipe 921 is horizontally arranged; when the angle θ is -45° or 135°, the connecting pipe 921 is tilted downward. The state where the angle θ is -45° is the state where the three-phase separation tube assembly 92 is rotated 180°.

[0055] As a more preferred embodiment, Figure 6 The bottom of the reactor body 1 has a mud discharge port 12, which is arranged between the first fluid zone 4 and the second fluid zone 5. The mud discharge port 12 is used to discharge the aerobic granular sludge formed. Figure 1 and Figure 2 The bottom side of the reactor body 1 is provided with an inlet pipe 13, and the top side of the reactor body 1 is provided with an outlet pipe 14. The inlet pipe 13 is arranged at one end of the second fluid area 5 close to the bottom gap area 7, and the outlet pipe 14 is installed on the side wall of the outlet weir 8. Specifically, domestic sewage and inoculated aerobic sludge are provided through the inlet pipe 13, and the separated sewage is discharged through the outlet pipe 14. For example, the inlet flow rate in the reactor body 1 is adjusted to 0.6m 3 / h~1.9m 3 / h, the sludge volume index is 22mg / L~38mg / L, and the suspended solid content of the mixed liquor is 4200mg / L~5000mg / L. The reaction device can flexibly adjust the internal components according to the operating conditions to change the flow field of the reaction device to achieve the purpose of cultivating aerobic granular sludge.

[0056] On the basis of the above-mentioned implementation mode, the embodiment of the present invention adopts a double-aeration countercurrent mass transfer reaction device to cultivate aerobic granular sludge. The method for cultivating aerobic granular sludge includes the following steps:

[0057] Step 1, obtaining the water inlet load of the reactor body 1 and the particle size of the aerobic granular sludge in the reactor body 1.

[0058] Step 2: According to the water inlet 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 flow direction of the first fluid zone 4 and the second fluid zone 5. The specific method is: when the water inlet load detection data is less than 1.2 kg COD·m -3 ·d -1 When the aeration type of the second aeration head 32 is adjusted to nitrogen-rich gas, the second fluid zone 5 is configured as an ascending 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 a descending zone. Alternatively, when the inlet load detection data is ≥1.2 kg COD·m -3 ·d -1 When the aeration type of the first aeration head 31 is adjusted to nitrogen-rich gas, the first fluid zone 4 is configured as an ascending 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 a descending zone. The aeration head 3 corresponding to the ascending zone is aerated with nitrogen-rich gas to provide a driving force for the circulation of the reaction fluid; the aeration head 3 corresponding to the descending zone is aerated with oxygen to maintain the dissolved oxygen content in the reaction fluid in a countercurrent mass transfer manner.

[0059] Step 3: According to the particle size of the aerobic granular sludge in the reactor body 1, the aeration amount of the first aeration head 31 and the second aeration head 32 is adjusted; and as the particle size of the aerobic granular sludge in the reactor body 1 gradually increases, the aeration amount of the first aeration head 31 and the second aeration head 32 gradually increases. The specific method is: the water inlet load detection data <1.2kg COD·m -3 ·d -1 At the same time, when the particle size of the aerobic granular sludge in the reactor body 1 is less than 0.3 mm, the aeration volume of the first aeration head 31 is 4 m 3 / h~6m 3 / h, the aeration volume of the second aeration head 32 is 10m 3 / h~15m 3 / h; when the particle size of the aerobic granular sludge in the reactor body 1 is 0.3mm~1.8mm, the aeration volume of the first aeration head 31 is 6m 3 / h~8m 3 / h, the aeration volume of the second aeration head 32 is 15m 3 / h~20m 3 / h; when the particle size of the aerobic granular sludge in the reactor body 1 is> 1.8mm, the aeration volume of the first aeration head 31 is 8m 3 / h~10m 3 / h, the aeration volume of the second aeration head 32 is 20m 3 / h~25m 3 / h. Or, water inlet load test data ≥ 1.2kg COD·m -3 ·d -1 At the same time, when the particle size of the aerobic granular sludge in the reactor body 1 is less than 0.3 mm, the aeration volume of the second aeration head 32 is 10 m 3 / h~12m 3 / h, the aeration volume of the first aeration head 31 is 20m 3 / h~25m 3 / h; when the particle size of the aerobic granular sludge in the reactor body 1 is 0.3mm~1.8mm, the aeration volume of the second aeration head 32 is 12m 3 / h~14m 3 / h, the aeration volume of the first aeration head 31 is 25m 3 / h~30m 3 / h; when the particle size of the aerobic granular sludge in the reactor body 1 is >1.8mm, the aeration volume of the second aeration head 32 is 14m 3 / h~18m 3 / h, the aeration volume of the first aeration head 31 is 30m 3 / h~35m 3 / h.

[0060] Step 4, 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 specific method is: 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 the first height h1, and adjust the arrangement direction of the connecting pipe 921 to the direction of the effluent separation zone 6 on the upper side of the guide plate structure 2. Specifically, 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, at this time, the distance between the bottom of the guide plate 22 and the bottom plate of the reactor body 1 is the minimum distance. For example, 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. The arrangement direction of the connecting pipe 921 is adjusted to be toward the water outlet 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 water outlet separation zone 6; that is, when the angle θ is +45°, the connecting pipe 921 is inclined upward.

[0061] When the particle size of the aerobic granular sludge in the reactor body 1 is 0.3 mm to 1.8 mm, 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 in the direction of the inner wall of the 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 AGS with a relatively large particle size enters the descending area to achieve the particle size screening of the aerobic granular sludge. When the angle θ is 0°, the connecting pipe 921 is arranged 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 the second height h2, and the second height h2 is greater than the first height h1; to accelerate the flow rate of the fluid at the bottom of the reactor body 1, and the aerobic granular sludge formed is deposited and discharged in the bottom gap area 7. 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, plays 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 be in the direction of the bottom gap area 7 on the lower side of the guide plate structure 2. At this time, the guide plate structure 2 is rotated to arrange the connecting pipe 921 of the three-phase separation pipe assembly 92 downward, so that the aerobic granular sludge with larger particles enters the effluent separation zone 6 or increases the amount of aerobic granular sludge entering the effluent separation zone 6. That is, when the angle θ is -45° or 135°, the connecting pipe 921 is tilted downward. The state where the angle θ is -45° is the state where the three-phase separation pipe assembly 92 is 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 water load is low, which is <1.2 kg COD·m -3 ·d -1 When the AGS particle size is small, that is, the particle size is less than 0.3mm, the oxygen aeration volume is 4m 3 / h~6m 3 / h, nitrogen-rich gas aeration volume 10m 3 / h~15m 3 / h, the height of the guide plate from the bottom plate is set to 0.3m, at this time the height of the guide plate and the liquid surface is 0.5m, the near-surface velocity of the fluid is low, and the connecting pipe of the three-phase separation pipe is arranged at 45° upward to reduce the amount of sludge entering the separation zone. When the particle size increases, that is, 0.3mm≤particle size≤1.8mm, a horizontal connecting pipe is selected to increase the amount of sludge entering the separation zone. Light sludge with small particle size is more likely to enter the three-phase separation connecting pipe with sewage and then enter the separation zone, and heavy sludge with large particle size directly enters the descending zone to achieve particle size screening of the sludge. Oxygen aeration volume 6m 3 / h~8m 3 / h, nitrogen-rich gas aeration volume 15m 3 / h~20m 3 / h. When the particle size increases further, that is, the particle size is greater than 1.8mm, the height of the guide plate from the bottom plate is adjusted to 0.6m. At this time, the height between the guide plate and the liquid surface is 0.2m. The flow velocity of the fluid near the liquid surface is relatively high. A 45° downward connecting pipe is selected and the aeration volume is increased, that is, the oxygen aeration volume is 8m 3 / h~10m 3 / h, nitrogen-rich gas aeration volume 20m 3 / h~25m 3 / h.

[0065] Implementation method 2: When the influent load is high, >1.2kg COD·m -3 ·d -1 When the AGS particle size is small, that is, the particle size is less than 0.3mm, and the oxygen aeration volume is 10m 3 / h~12m 3 / h, nitrogen-rich gas aeration volume 20m 3 / h~25m 3 / h, the height of the guide plate from the bottom plate is set to 0.3m, at this time the height of the guide plate and the liquid surface is 0.5m, the near-surface velocity of the fluid is low, and the connecting pipe of the three-phase separation pipe is arranged downward at 45° to reduce the amount of sludge entering the separation zone. When the particle size increases, that is, 0.3mm≤particle size≤1.8mm, a horizontal connecting pipe is selected to increase the amount of sludge entering the separation zone. Light sludge with small particle size is more likely to enter the three-phase separation connecting pipe with sewage and then enter the separation zone, and heavy sludge with large particle size directly enters the descending zone, thereby achieving particle size screening of the sludge. Oxygen aeration volume 12m 3 / h~14m 3 / h, nitrogen-rich gas aeration volume 25m 3 / h~30m 3 / h. When the particle size increases further, that is, the particle size is greater than 1.8mm, the height of the guide plate from the bottom plate is adjusted to 0.6m. At this time, the height between the guide plate and the liquid surface is 0.2m. The near-liquid surface velocity of the fluid is relatively high. Select a 45° upward connecting pipe and increase the aeration volume, that is, the oxygen aeration volume is 14m 3 / h~18m 3 / h, aeration volume of nitrogen-rich gas 30m 3 / h~35m 3 / h.

[0066] The dual-aeration airlift reactor with separated driving force and dissolved oxygen designed in one embodiment of the present invention mainly separates driving force control from dissolved oxygen control through innovation of reactor structure, makes parameters such as sedimentation selection pressure and hydraulic shear force adjustable, and further explores the potential of airlift reactor in cultivating granular sludge. In pursuit of flow field stability and dissolved oxygen stability under changes in influent load, the water quality conditions, fluid mechanics conditions and stable operating range for cultivating AGS are analyzed, and a mathematical model between organic load-oxygen supply-fluid mechanics characteristics-pollution degradation is established, providing a theoretical basis and working conditions for the promotion of AGS technology and the scale-up of reactors.

[0067] It is only 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 principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A double aeration countercurrent mass transfer reaction device, characterized in that: Applied to the cultivation of aerobic granular sludge, the device comprises: Reactor body (1); a guide plate structure (2) arranged in the reactor body (1); the guide plate 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 arranged outside the first fluid zone (4); an aeration head (3), comprising a first aeration head (31) and a second aeration head (32), wherein the first aeration head (31) is arranged at the lower side of the first fluid zone (4); the second aeration head (32) is arranged at the lower side of a second fluid zone (5) corresponding thereto; the first aeration head (31) and the second aeration head (32) have different aeration types; 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 amount of the nitrogen-rich gas is greater than the aeration amount of the oxygen; The aeration types of the first aeration head (31) and the second aeration head (32) are changed as the water inlet load of the reactor body (1) increases, so as to adjust the fluid direction of the first fluid zone (4) and the second fluid zone (5); The aeration amounts of the first aeration head (31) and the second aeration head (32) gradually increase as the particle size of the aerobic granular sludge in the reactor body (1) increases.

2. The double aeration countercurrent mass transfer reaction device according to claim 1, characterized in that: Also includes: A water inlet detection unit, used for analyzing and detecting the water inlet load of the reactor body (1), and sending the water inlet load to a processing unit; A particle size detection unit, used to analyze and detect the particle size of the aerobic granular sludge in the reactor body (1), and send it to a processing unit; A processing unit is used to receive the water inlet load detection data sent by the water inlet detection unit and the particle size detection data sent by the particle size detection unit, and compare the water inlet load detection data with the set water inlet load data, and compare the particle size detection data with the set particle size data, and adjust the aeration type and aeration amount of the first aeration head (31) and the second aeration head (32) according to the comparison result.

3. The double aeration countercurrent mass transfer reaction device according to claim 2, characterized in that: The conditions for adjusting the aeration types of the first aeration head (31) and the second aeration head (32) according to the comparison result are: When the inlet load test data is less than 1.2 kg COD·m -3 ·d -1 When the second aeration head (32) is used for aeration, the aeration type is adjusted to nitrogen-rich gas, so that the second fluid zone (5) is configured as an ascending 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 a descending zone; Or, when the inlet load test data is ≥1.2kg COD·m -3 ·d -1 When the aeration type of the first aeration head (31) is adjusted to nitrogen-rich gas, the first fluid zone (4) is configured as an ascending zone, and the aeration type of the second aeration head (32) is adjusted to oxygen, so as to configure the second fluid zone (5) as a descending zone.

4. The double aeration countercurrent mass transfer reaction device according to claim 3, characterized in that: The conditions for adjusting the aeration amounts of the first aeration head (31) and the second aeration head (32) according to the comparison result are: When the inlet load test data is less than 1.2 kg COD·m -3 ·d -1 When 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 4m 3 / h~6m 3 / h gradually increase to 8m 3 / h~10m 3 / h; the aeration volume of the second aeration head (32) is 10m 3 / h~15m 3 / h gradually increase to 20m 3 / h~25m 3 / h; Or, when the inlet load test data is ≥1.2kg COD·m -3 ·d -1 When 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 10m 3 / h~12m 3 / h gradually increased to 14m 3 / h~18m 3 / h; the aeration volume of the first aeration head (31) is 20m 3 / h~25m 3 / h gradually increase to 30m 3 / h~35m 3 / h.

5. The double aeration countercurrent mass transfer reaction device according to claim 2, characterized in that: The processing unit can issue a prompt instruction for adjusting the distance between the bottom of the guide plate structure (2) and the bottom 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 ≤1.8 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 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 greater than 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) based on the comparison result; the second height (h2) is greater than the first height (h1).

6. The double aeration countercurrent mass transfer reaction device according to claim 2, characterized in that: The upper side of the guide plate structure (2) is configured as a water outlet separation zone (6), and the water outlet separation zone (6) is equipped with a plurality of 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 area (7); The processing unit can issue a prompt instruction for adjusting the arrangement direction of the connecting pipe (921) 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 less than 0.3 mm, the processing unit can adjust the arrangement direction of the connecting pipe (921) to be toward 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 issue an adjustment, based on the comparison result, to arrange the connecting pipe (921) in a direction perpendicular to the inner wall of the reactor body (1); Alternatively, when the comparison result shows that the particle size of the aerobic granular sludge in the reactor body (1) is greater than 1.8 mm, the processing unit can adjust the arrangement direction of the connecting pipe (921) to be toward the bottom gap area (7) according to the comparison result.

7. A method for cultivating aerobic granular sludge, characterized in that: The double aeration countercurrent mass transfer reaction device according to claim 6 is used, and the specific method comprises the following steps: Obtaining the water inlet load of the reactor body (1) and the particle size of the aerobic granular sludge in the reactor body (1); According to the water inlet 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 amounts of the first aeration head (31) and the second aeration head (32) are 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 amounts of the first aeration head (31) and the second aeration head (32) gradually increase.

8. The method for cultivating aerobic granular sludge according to claim 7, 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 water inlet load of the reactor body (1) is specifically: When the inlet load test data is less than 1.2 kg COD·m -3 ·d -1 When the second aeration head (32) is used for aeration, the aeration type is adjusted to nitrogen-rich gas, so that the second fluid zone (5) is configured as an ascending 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 a descending zone; Or, when the inlet load test data is ≥1.2kg COD·m -3 ·d -1 When the aeration type of the first aeration head (31) is adjusted to nitrogen-rich gas, the first fluid zone (4) is configured as an ascending zone, and the aeration type of the second aeration head (32) is adjusted to oxygen, so as to configure the second fluid zone (5) as a descending zone.

9. The method for cultivating aerobic granular sludge according to claim 7, characterized in that: The method for adjusting the aeration amount of the first aeration head (31) and the second aeration head (32) according to the particle size of the aerobic granular sludge in the reactor body (1) is specifically: When the inlet load test data is less than 1.2 kg COD·m -3 ·d -1 When 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 4m 3 / h~6m 3 / h gradually increase to 8m 3 / h~10m 3 / h; the aeration volume of the second aeration head (32) is 10m 3 / h~15m 3 / h gradually increase to 20m 3 / h~25m 3 / h; Or, when the inlet load test data is ≥1.2kg COD·m -3 ·d -1 When 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 10m 3 / h~12m 3 / h gradually increased to 14m 3 / h~18m 3 / h; the aeration volume of the first aeration head (31) is 20m 3 / h~25m 3 / h gradually increase to 30m 3 / h~35m 3 / h.

10. The method for cultivating aerobic granular sludge according to claim 7, characterized in that: After obtaining the particle size of the aerobic granular sludge in the reactor body (1), the method further comprises: According to the particle size of the aerobic granular sludge in the reactor body (1), 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) are adjusted; The method of 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 specifically as follows: When the particle size of the aerobic granular sludge in the reactor body (1) is less than 0.3 mm, the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) is adjusted to a first height (h1), and the arrangement direction of the connecting pipe (921) is adjusted to be in the direction of 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 0.3 mm to 1.8 mm, the distance between the bottom of the guide plate structure (2) and the bottom of the reactor body (1) is maintained at a first height (h1), and the arrangement direction of the connecting pipe (921) is adjusted to be in the direction of the inner wall of the reactor body (1); When the particle size of the aerobic granular sludge in the reactor body (1) is greater than 1.8 mm, 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 arrangement direction of the connecting pipe (921) is adjusted to be in the direction of 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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