CN117209062A - Circulation flow biochemical treatment reactor and method - Google Patents
Circulation flow biochemical treatment reactor and method Download PDFInfo
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- CN117209062A CN117209062A CN202311186250.4A CN202311186250A CN117209062A CN 117209062 A CN117209062 A CN 117209062A CN 202311186250 A CN202311186250 A CN 202311186250A CN 117209062 A CN117209062 A CN 117209062A
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Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention provides a circulating flow biochemical treatment reactor and a circulating flow biochemical treatment method, wherein the reactor comprises an anoxic zone, an aerobic zone and a sedimentation zone which are sequentially connected along a sewage flow method, and a sludge reflux zone for discharging sludge; the aerobic zone is provided with a nitrifying liquid return pipeline to the anoxic zone; the sludge reflux zone is provided with an anoxic reflux sludge pipeline to the anoxic zone. The circulation flow biochemical treatment method provided by the invention not only can realize the maximization of the nitrogen and phosphorus removal rate, but also can realize the stable and reliable treatment effect, flexible adjustment of process control, environmental friendliness, low energy consumption, convenient operation and maintenance management and relatively low construction cost, and fully exerts the maturity, high efficiency and economy of the circulation flow biochemical treatment method.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and relates to a sewage treatment device, in particular to a circulating flow biochemical treatment reactor and a circulating flow biochemical treatment method.
Background
Urban development and acceleration of industrial processes have led to increased attention to sewage treatment.
Traditional sewage treatment technologies include AAO technology, anaerobic ammonia oxidation technology, hydrolytic acidification technology, upflow anaerobic sludge blanket reactor technology and contact oxidation technology.
The AAO process mainly comprises the following treatment processes: the sewage sequentially passes through the anaerobic tank, the anoxic tank and the aerobic tank. Microorganisms capable of accumulating phosphorus in the activated sludge of the aerobic tank can absorb a large amount of soluble phosphorus, convert the soluble phosphorus into insoluble polyorthophosphate to be stored in a body, and finally discharge residual sludge through the secondary sedimentation tank to achieve the aim of system phosphorus removal. The AAO process has the advantages of general pollutant removal rate, stable effluent quality, high energy consumption, large equipment occupation and no contribution to wide popularization and application.
The anaerobic ammonia oxidation process is that under anaerobic or anoxic conditions, anaerobic ammonia oxidation microorganisms directly take NH as raw material 4+ As electron donor, with NO 3- Or NO 2- For electron acceptors, NH 4+ 、NO 3- Or NO 2- Conversion to N 2 Is a biological oxidation process of (a). Anaerobic ammoxidation utilizes a unique organism to oxidize ammonia nitrogen to N using nitrate as an electron donor 2 The anaerobic nitrification of nitrogen circulation is realized to the maximum extent, the coupling process has good prospect for denitrification from the anaerobic digested wastewater, and the process can save energy to a greater extent for the partial oxidation of high ammonia nitrogen low COD sewage due to nitrate. However, the method has harsh running conditions and long starting period; and the treatment degree is limited, and the treatment method needs to be combined with other processes.
The hydrolysis acidification technology controls anaerobic reaction in two stages of hydrolysis and acidification, and utilizes the action of anaerobic or facultative bacteria in the hydrolysis and acidification stages to hydrolyze suspended solids and macromolecular substances (including carbohydrate, fat, lipid and the like) difficult to biodegrade in sewage into soluble organic substances and micromolecular substances easy to biodegrade, and then the micromolecular organic substances are converted into volatile fatty acid under the action of acidizing bacteria. The method has limited sewage treatment degree and needs to be combined with other processes.
The upflow anaerobic sludge blanket reactor is a technology combining wastewater treatment with energy recycling. Which utilizes the metabolic processes of anaerobic microorganisms to convert organic matter, including a large amount of biogas and water, into inorganic matter, including small amounts of cellular material, without the need to provide oxygen. Sewage sequentially enters a sludge layer at the bottom and a sludge suspension layer at the middle and upper parts through a water distribution device, reacts with anaerobic microorganisms in the sewage to generate biogas, gas, liquid and solid mixed liquid are separated through an upper three-phase separator, the sludge falls back to a sludge suspension area, the separated sewage is discharged out of the system, and the biogas generated by the anaerobic reactor is recovered. The reactor is easy to adhere to sludge in the operation process, and the sedimentation of the sludge is affected.
The contact oxidation process fills the filler in the tank, the filler is immersed in aeration oxygenated sewage, the sewage flows through the filler which is fully covered with a biological film, and organic pollutants are removed under the metabolism of microorganisms. In summary, the traditional sewage treatment technology has the defects of poor performance, single process operation mode, serious secondary pollution, high energy consumption, complicated operation and management and high construction cost, and limits the sustainability and applicability of the traditional sewage treatment technology. Therefore, development of sewage treatment technology is necessary to be emphasized, and the level of sewage purification is continuously improved.
Disclosure of Invention
In view of the shortcomings of the prior art, the invention aims to provide a circulating flow biochemical treatment reactor and a circulating flow biochemical treatment method. The circulation flow biochemical treatment method provided by the invention not only can realize the maximization of the nitrogen and phosphorus removal rate, but also can realize the stable and reliable treatment effect, flexible adjustment of process control, environmental friendliness, low energy consumption, convenient operation and maintenance management and relatively low construction cost, and fully exerts the maturity, high efficiency and economy of the circulation flow biochemical treatment method.
To achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the present invention provides a circulating flow biochemical treatment reactor comprising an anoxic zone, an aerobic zone, and a settling zone, which are sequentially connected along a sewage flow process, and a sludge recirculation zone for discharging sludge;
The aerobic zone is provided with a nitrifying liquid return pipeline to the anoxic zone;
the sludge reflux zone is provided with an anoxic reflux sludge pipeline to the anoxic zone.
According to the reactor provided by the invention, the anoxic zone, the aerobic zone, the sedimentation zone and the sludge reflux zone are arranged, the outlet of the anoxic zone is connected with the aerobic zone, the outlet of the aerobic zone is connected with the sedimentation zone, and the sludge outlet of the sedimentation zone (namely the sludge circulation outlet of the sludge reflux zone) is connected with the anoxic zone, so that complete mixing and local plug flow of fluid in the reactor can be realized, and the problems of insufficient mixing of microorganisms and sewage and low treatment efficiency caused by overhigh concentration of inflow water can be effectively solved; the reactor is suitable for a large-flow circulation process, and has the advantages of low load, strong impact resistance, low energy consumption and occupation area saving.
As a preferable technical scheme of the invention, the material of the reactor comprises steel or steel concrete.
As a preferable technical scheme of the invention, the outlet of the anoxic zone is provided with a first water passing hole.
Preferably, a first water inlet area is arranged on one side of the anoxic area close to the inlet.
Preferably, a first water outlet area is arranged on one side of the anoxic area close to the first water passing hole.
Preferably, a first diversion partition wall is arranged between the first water inlet area and the first water outlet area.
The first diversion partition wall is formed by combining partition plates or reinforced concrete partition walls.
Preferably, at least one second stirring device is respectively arranged in the first water inlet area and the first water outlet area.
Preferably, the anoxic zone is connected with the inlet of the aerobic zone through a first water passing hole.
It is noted that the anoxic zone of the present invention is also provided with an on-line monitoring instrument, including a pH detector and/or a DO detector, and those skilled in the art can set the on-line monitoring instrument as required.
The anoxic zone adopts a mode of combining a flow guide partition wall and a stirring device, and stirring is carried out while flow guide circulation is carried out, so that the full mixing of fluid can be effectively accelerated, and the problems of local siltation, short flow and dead water of the reactor are solved.
As a preferable technical scheme of the invention, at least two groups of supporting frames are arranged in the aerobic zone.
Preferably, the support frame is provided with biological filler.
Preferably, the biological filler accounts for 8-15% of the sewage volume in the aerobic zone, for example, 8%, 9%, 10%, 12%, 14% or 15%, but is not limited to the recited values, and other values not recited in the numerical range are equally applicable.
Preferably, the bio-filler comprises PP material and/or modified fiber material.
Preferably, at least one aeration device for oxygenating and stirring the mixed liquor is arranged in the aerobic zone.
The aeration device in the aerobic zone can be arranged between two groups of support frames and also can be arranged between the support frames and the reactor partition wall, so long as the purpose of accelerating the oxygenation of sewage can be realized.
Preferably, the aerobic zone is connected with the inlet of the sedimentation zone through a communicating pipe.
Preferably, a second diversion partition wall is arranged in the aerobic zone.
Preferably, the second guide partition wall includes a U-shaped partition wall and a partition wall.
Preferably, the partition wall is fixedly arranged at the middle position of the top of the aerobic zone.
Preferably, the U-shaped partition wall is fixedly arranged at the middle position of the bottom of the aerobic zone.
Preferably, at least two third stirring devices for stirring sewage are arranged in the aerobic zone.
It is noted that the aerobic zone of the present invention is further provided with an on-line monitoring instrument, including a pH detector and/or a DO detector, and those skilled in the art can set the on-line monitoring instrument as required.
According to the invention, the aerobic zone adopts the flow guide partition wall arranged according to the requirement to perform flow guide circulation, and adopts the aeration device to perform aeration, so that the aeration oxygenation capacity can be effectively reduced, the low-oxygen aeration is realized, the energy consumption of the reactor is reduced, and meanwhile, the treatment effect is good.
As a preferable technical scheme of the invention, the middle part of the sedimentation zone is provided with mud scraping equipment.
Preferably, the mud scraping device comprises a mud scraper, a central guide cylinder, a scum baffle and a slag discharge hopper.
Preferably, the inlet of the central guide cylinder of the mud scraping device is connected with the communicating pipe.
Notably, the mud scraper of the invention can select a center drive mud scraper or a peripheral drive mud scraper as required; wherein the mud scraper and the central guide cylinder are positioned on the same axis.
Preferably, the sludge of the sludge scraping device is connected with the sludge recirculation zone through a sludge discharge pipeline.
Preferably, the upper part of the sedimentation zone is provided with a water outlet weir plate.
Preferably, the water outlet weir plate is connected with a drain pipe.
The water outlet weir plate is formed by combining irregular toothed steel plates and fixed supports thereof.
As a preferred technical scheme of the invention, the circulating flow biochemical treatment reactor also comprises an anaerobic zone connected with the anoxic zone.
Preferably, the inlet of the anaerobic zone is provided with a water inlet pipe.
Preferably, the water outlet end of the water inlet pipe is connected with a uniform water distribution device;
preferably, an aeration device is arranged at the bottom of the anaerobic zone.
The aeration device is formed by combining a disc type aerator or a plurality of staggered perforated pipes and connecting pipes thereof.
Preferably, a mud-water separation device and a first stirring device are arranged in the anaerobic zone.
Preferably, the water outlet pipeline of the mud-water separation device is divided into two branches, one branch is connected with the water inlet pipe, and the other branch is connected with the inlet of the anoxic zone.
The mud-water separation device comprises a water outlet weir or a combination of the water outlet weir and a solid-liquid separator. The water outlet weir plate is formed by combining tooth-shaped steel plates with different specifications and fixing brackets thereof; the solid-liquid separator is formed by combining an equipment body, a filler and the solid-liquid separator.
Preferably, the anaerobic zone is provided with an anaerobic return sludge line to the sludge return zone.
Preferably, the anaerobic zone is provided with an anaerobic external sludge line to provide anaerobic sludge for the anaerobic zone.
The inside of the anaerobic zone is also provided with a diversion partition wall and an on-line detection instrument. The online detection instrument comprises a pH detector, a thermometer, an ORP/DO detector and NH 3 -N/nitrite detector, which can be set by the person skilled in the art as desired.
The outlet of the anaerobic zone is connected with the anoxic zone, and the sludge outlet of the sedimentation zone (namely the sludge circulation outlet of the sludge reflux zone) is connected with the anoxic zone and the anaerobic zone, so that the complete mixing and the local plug flow of fluid in the reactor are realized, and the problems of insufficient mixing of microorganisms and sewage and low treatment efficiency caused by overhigh concentration of inflow water are effectively solved.
As a preferable technical scheme of the invention, the sludge reflux zone is provided with a reflux sludge pipeline to an anaerobic zone.
Preferably, the sludge recirculation zone is provided with a sludge discharge pipe.
In a second aspect, the present invention provides a recycle stream biochemical treatment process carried out in a reactor as provided in the first aspect.
As a preferred embodiment of the present invention, the method comprises the steps of:
(1) The sewage enters an anoxic zone through an inlet to carry out denitrification to obtain a solution A, and part of organic matters are degraded;
(2) The solution A enters an aerobic zone to degrade organic matters, ammoniation and nitration of organic nitrogen and absorption of phosphorus to form a solution B, a part of the solution B enters a precipitation zone, and the rest of the solution B is recorded as nitration circulating liquid and enters an anoxic zone;
(3) And (3) performing mud-water separation on the solution B entering the precipitation zone to obtain a solution C and sludge, discharging the solution C from the reactor, and allowing the sludge to enter a sludge reflux zone.
The method provided by the invention not only can realize the maximization of the nitrogen and phosphorus removal rate, but also can realize the stable and reliable treatment effect, flexible adjustment of process control, environmental friendliness, low energy consumption, convenient operation and maintenance management and relatively low construction cost, and can fully exert the maturity, high efficiency and economy of the method.
As a preferred embodiment of the present invention, the hydraulic retention time of the anoxic zone in the step (1) is 1 to 40 hours, and may be, for example, 2 hours, 5 hours, 10 hours, 15 hours, 20 hours, 25 hours, 30 hours, 35 hours or 38 hours, but not limited to the recited values, and other values not recited in the numerical range are equally applicable.
Preferably, the stirring intensity of the anoxic zone in the step (1) is 4-12W/m 3 For example, it may be 5W/m 3 、7W/m 3 、9W/m 3 Or 11W/m 3 But are not limited to, the recited values, and other values not recited within the range of values are equally applicable.
Preferably, the denitrification load of the anoxic zone in the step (1) is in the range of 0.03 to 0.06kgNO 3 N/(kgMLSS. D), which may be, for example, 0.03kgNO 3 -N/(kgMLSS.d)、0.04kgNO 3 -N/(kgMLSS.d)、0.05kgNO 3 N/(kgMLSS. D) or 0.06kgNO 3 N/(kgMLSS. D), but not limited to the values recited, other values not recited within the range of values are equally applicable.
Preferably, the sludge load of the solution A and the solution B is 0.05-0.15 kgBOD 5 /(kgMLSS. D), for example, may be 0.07kgNO 3 -N/(kgMLSS.d)、0.09kgNO 3 -N/(kgMLSS.d)、0.11kgNO 3 N/(kgMLSS. D) or 0.13kgNO 3 N/(kgMLSS. D), but not limited to the values recited, other values not recited within the range of values are equally applicable.
Preferably, the sludge concentration of the solution A and the solution B is 4000 to 8000mg/L, for example, 4500mg/L, 5000mg/L, 6000mg/L, 7000mg/L or 7500mg/L, but not limited to the recited values, and other values not recited in the numerical range are equally applicable.
Preferably, the hydraulic retention time of the aerobic zone in the step (2) is 7 to 50 hours, for example, 8 hours, 10 hours, 20 hours, 30 hours, 40 hours or 45 hours, but the hydraulic retention time is not limited to the recited values, and other values not recited in the numerical range are equally applicable.
Preferably, the stirring intensity of the aerobic zone in the step (2) is 1-3W/m 3 For example, it may be 1.2W/m 3 、1.5W/m 3 、2W/m 3 、2.5W/m 3 Or 2.8W/m 3 But are not limited to, the recited values, and other values not recited within the range of values are equally applicable.
Preferably, the reflux ratio of the nitrifying cycle liquid in the step (2) is 100-1200%, for example, 150%, 200%, 400%, 600%, 800%, 1000% or 1150%, but not limited to the values listed, and other values not listed in the numerical range are equally applicable.
Preferably, the aeration intensity of the aerobic zone in the step (2) is 6-12 m 3 /m 2 H, for example, may be 7m 3 /m 2 .h、8m 3 /m 2 .h、9m 3 /m 2 .h、10m 3 /m 2 H or 11m 3 /m 2 H, but not limited to, the recited values, other values not recited in the range of values are equally applicable.
Preferably, the surface load of the precipitation zone of step (3) is from 0.4 to 1m 3 /m 2 H, for example, may be 0.5m 3 /m 2 .h、0.6m 3 /m 2 .h、0.7m 3 /m 2 .h、0.8m 3 /m 2 H or 0.9m 3 /m 2 H, but not limited to, the recited values, other values not recited in the range of values are equally applicable.
Preferably, the sludge recirculation ratio in the sludge recirculation zone in step (3) is 0 to 100%, for example 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80% or 90%, but not limited to the values recited, and other values not recited in the numerical range are equally applicable.
As a preferred embodiment of the present invention, the sewage in step (1) further includes, before entering the anoxic zone: the sewage is mixed with the sludge from the sludge recirculation zone in the anaerobic zone and phosphorus is released.
Preferably, the hydraulic retention time of the anaerobic zone is 0.5 to 45h, for example, 1h, 5h, 10h, 15h, 20h, 25h, 30h, 35h or 40h, but not limited to the recited values, other values not recited in the numerical range are equally applicable.
Preferably, the total nitrogen removal load of the anaerobic zone is in the range of 0.3-3 kgTN/m 3 D, for example, may be 0.5kg TN/m 3 .d、1kgTN/m 3 .d、1.5kgTN/m 3 .d、2kgTN/m 3 D or 2.5kg TN/m 3 D, but not limited to, the recited values, other values not recited in the range of values are equally applicable.
Preferably, the upward flow rate of the sewage in the anaerobic zone is 0.5 to 1.5m/h, for example, 0.7m/h, 0.9m/h, 1.1m/h or 1.3m/h, but not limited to the recited values, and other values not recited in the numerical range are equally applicable.
Preferably, the stirring intensity of the anaerobic zone is 4-12W/m 3 For example, it may be 5W/m 3 、7W/m 3 、9W/m 3 Or 11W/m 3 But are not limited to, the recited values, and other values not recited within the range of values are equally applicable.
As a preferred technical scheme of the invention, the circulating flow biochemical treatment method provided by the second aspect of the invention comprises the following steps:
(a) Mixing sewage and sludge from a sludge reflux zone in an anaerobic zone, and releasing phosphorus to obtain a mixed solution;
wherein the hydraulic retention time of the anaerobic zone is 0.5-45 h, and the total nitrogen removal load value range is 0.3-3 kgTN/m 3 D, the upward flow rate of the sewage is 0.5-1.5 m/h, and the stirring strength is 4-12W/m 3 ；
(b) The mixed solution obtained in the step (a) enters an anoxic zone through an inlet to carry out denitrification to obtain a solution A, and part of organic matters are degraded;
wherein the hydraulic retention time of the anoxic zone is 1-40 h, and the stirring strength is 4-12W/m 3 The denitrification load value range is 0.03-0.06 kgNO 3 -N/(kgmlss.d); the sludge load value of the solution A is 0.05-0.15 kgBOD 5 The sludge concentration of the solution A is 4000-8000 mg/L;
(c) The solution A enters an aerobic zone to degrade organic matters, ammoniation and nitration of organic nitrogen and absorption of phosphorus to form a solution B, a part of the solution B enters a precipitation zone, and the rest of the solution B is recorded as nitration circulating liquid and enters an anoxic zone;
Wherein the hydraulic retention time of the aerobic zone is 7-50 h, and the stirring strength is 1-3W/m 3 The aeration intensity is 6-12 m 3 /m 2 H; the reflux ratio of the nitrifying circulating liquid is 100-1200%; the sludge concentration of the solution B is 4000-8000 mg/L;
(d) Performing mud-water separation on the solution B entering the precipitation zone to obtain a solution C and sludge, discharging the solution C from the reactor, and allowing the sludge to enter a sludge reflux zone;
wherein the surface load of the sedimentation zone is 0.4-1 m 3 /m 2 H, the sludge reflux ratio is 0-100%.
The numerical ranges recited herein include not only the above-listed point values, but also any point values between the above-listed numerical ranges that are not listed, and are limited in space and for the sake of brevity, the present invention is not intended to be exhaustive of the specific point values that the stated ranges include.
Compared with the prior art, the invention has the following beneficial effects:
(1) The reactor provided by the invention has ideal mixing reaction effect and flexible operation mode: the hydraulic flow state is overall plug flow and zoned circulation mixing, and each zone reactor adopts the flow state of the circulation flow and simultaneously has the impact load resistance of the complete mixing type reactor and the matrix degradation driving force of the plug flow type reactor; the reactors in each zone adopt a circulating flow mode, the water inflow is uniformly distributed, the phenomena of rapid flow, vortex flow, short flow, dead water and mud accumulation are not easy to generate in the reactors, the head loss is small, the macro mixing uniformity is high, and the mixing reaction effect is ideal;
(2) The reactor provided by the invention has the advantages of impact load resistance and stable effluent quality: the reactor adopts hydrolysis acidification/anaerobic ammoxidation process with strong impact load resistance, and utilizes an external circulation system to quickly dilute the concentration of the original water pollutants, reduce the pollutant load and improve the impact resistance; the biological filler is arranged in the reactor, the organic matters in the wastewater are biochemically degraded by utilizing the enrichment effect of high-concentration microorganisms of the filler, the impact load resistance is improved, the treatment effect is operated, and the water quality safety of the effluent is ensured;
(3) The reactor provided by the invention has the advantages of small secondary pollution and environmental friendliness in biochemical treatment: by adopting a specific anaerobic process, the produced gas is a harmless compound, the sludge yield is low, and the secondary pollution is small; the specific microorganism carrier is adopted, so that the sludge sedimentation performance is enhanced, the output of residual sludge is small, and the consumable property is strong;
(4) The reactor provided by the invention has the advantages of low operation energy consumption and convenient operation management: the specific anaerobic technology is adopted, no or a small amount of additional organic matters are needed to be used as electron donors, the energy consumption is saved, the mud-water separation system is modularized, and the additional power consumption is not needed; the microporous aeration equipment is adopted, and the power energy consumption is far lower than that of a common perforation or mesoporous aeration system by combining a circulating flow hydraulic form; the aeration equipment for processing the finished product is adopted, so that the installation mode can be lifted, the disassembly and the assembly are convenient, and the operation and the maintenance are simple;
(5) The reactor provided by the invention has the advantages of small occupied area and low construction cost: the specific microorganism carrier is adopted, so that the effective pool capacity is reduced, and the occupied area is small; anaerobic, anoxic, aerobic and sedimentation are integrated, the volume utilization rate of the tank body is improved, and the construction cost is low.
Drawings
FIG. 1 is a schematic diagram of a circulating flow biochemical treatment reactor provided in one embodiment of the present invention;
FIG. 2 is a top view of a recirculating flow biochemical treatment reactor provided in one embodiment of the invention.
In fig. 1 and 2: 1 is an anaerobic zone, 2 is an anoxic zone, 3 is an aerobic zone, 4 is a sedimentation zone, 5 is a sludge reflux zone, 1a is a water inlet pipe, 1b is a mud-water separation device, 1c is a first stirring device, and 1d is an anaerobic reflux sludge pipeline; 1e is an anaerobic additional sludge pipeline, 2a is a first diversion partition wall, 2b is a first water passing hole, 2c is a second stirring device, 2d is an anoxic reflux sludge pipeline, 3a is a second diversion partition wall, 3b is a third stirring device, 3c is a nitrifying liquid reflux pipeline, 3d is a biological filler, 4a is a communicating pipe, 4b is a sludge scraping device, 4c is a water drain pipe, 4d is a sludge discharge pipeline, and 5a is a sludge discharge pipeline.
Detailed Description
The technical scheme of the invention is further described below by the specific embodiments with reference to the accompanying drawings. It will be apparent to those skilled in the art that the examples are merely to aid in understanding the invention and are not to be construed as a specific limitation thereof.
The technical scheme of the invention is further described by the following specific embodiments.
In one embodiment, the invention provides a circulating flow biochemical treatment reactor, which comprises an anaerobic zone 1, an anoxic zone 2, an aerobic zone 3 and a sedimentation zone 4 which are sequentially connected along a sewage flow method, and a sludge recirculation zone 5 for discharging sludge; the aerobic zone 1 is provided with a nitrifying liquid return pipeline 3c to the anoxic zone 2; the sludge recirculation zone 5 is provided with an anoxic recirculation sludge line 2d to the anoxic zone.
An inlet of the anaerobic zone 1 is provided with a water inlet pipe 1a; the water outlet end of the water inlet pipe 1a is connected with a uniform water distribution device; an aeration device is arranged at the bottom of the anaerobic zone 1; a mud-water separation device 1b and a first stirring device 1c are arranged in the anaerobic zone 1; the water outlet pipeline of the mud-water separation device 1b is divided into two branches, one branch is connected with the water inlet pipe, and the other branch is connected with the inlet of the anoxic zone 2; the anaerobic zone 1 is provided with an anaerobic return sludge pipeline 1d to the sludge return zone; the anaerobic zone is provided with an anaerobic external sludge pipeline 1e for providing anaerobic sludge for the anaerobic zone;
the outlet of the anoxic zone 1 is provided with a first water passing hole 2b; a first water inlet area is arranged at one side of the anoxic area 2 close to the inlet; a first water outlet area is arranged on one side of the anoxic area 2 close to the first water passing hole; a first diversion partition wall 2a is arranged between the first water inlet area and the first water outlet area; at least one second stirring device 2c is arranged in the first water inlet area and the first water outlet area respectively; the anoxic zone 2 is connected with the inlet of the aerobic zone through a first water passing hole 2 b.
At least two groups of support plates are arranged in the aerobic zone 3; the supporting plate is provided with biological filler 3d; the biological filler 3d accounts for 8-15% of the volume of sewage in the aerobic zone 3; the biological filler 3d comprises a PP material and/or a modified fiber material; at least one aeration device for accelerating the oxygenation of sewage is arranged in the aerobic zone 3; the aerobic zone 3 is connected with the inlet of the sedimentation zone 4 through a communicating pipe 4 a; a second diversion partition wall 3a is arranged in the aerobic zone; the second diversion partition wall 3a comprises a U-shaped partition wall and a partition wall; the partition wall is fixedly arranged at the middle position of the top of the aerobic zone; the U-shaped partition wall is fixedly arranged at the middle position of the bottom of the aerobic zone; at least two third stirring devices 3b for stirring sewage are arranged in the aerobic zone.
The middle part of the sedimentation zone is provided with a mud scraping device 4b; the inlet of the mud scraping device 4b is connected with a communicating pipe 4 a; the mud scraping device 4b comprises a mud scraper, a central guide cylinder, a scum baffle and a slag discharge hopper; the sludge scraping device 4b is connected with the sludge reflux zone through a sludge discharge pipeline 4 d; the upper part of the sedimentation zone is provided with a water outlet weir plate; the water outlet weir plate is connected with a water discharge pipe 4 c.
The sludge recirculation zone is provided with a sludge discharge pipe 5a.
Example 1
The present example provides a circulating flow biochemical treatment reactor, based on the reactor described in one specific embodiment, the anaerobic zone, anoxic zone and aerobic zone have the following dimensions: l×b×h=61×28×8m, the size of the sludge recirculation zone being l×b×h=3×9×8m; the size of the precipitation zone is Φ21m, h=3.5m. No biological filler is arranged in the aerobic zone.
2 sludge pumps are arranged in the anaerobic zone, and Q=30m 3 H, h=18m, n=3kw; the mud-water separation device 1b is a water outlet overflow weir plate: b=200m, δ=3mm, 80m; 1 set of uniform water distribution system is configured, and each set of service area is 380m 2 ；
The configuration in the anoxic zone is as follows: the 4 second stirring devices 2c are submersible mixers, the impeller diameter of each submersible mixer is 620mm, the rotating speed of each blade is 480r/min, and N=5.5 kW; wherein, an on-line analyzer of dissolved oxygen is also arranged, 0-20 mg/L.
2 nitrifying liquid through-wall reflux pumps are arranged in the aerobic zone, and Q=370m 3 H, h=0.8m, n=2.5 kW;386 is provided with a sleeve-type microporous aerator,ventilation of 2-14 m 3 The aeration devices of each set can be independently closed for maintenance; 1 set of regulating weirs, l×b=1500×500mm;1 dissolved oxygen on-line analyzer, 0-20 mg/L;2 air suspension fans, q=60deg.m 3 /min，H＝8m，N＝90kW；
The sedimentation zone is configured with: 1 set of peripheral drive mud scrapers, Φ21m, h=5.5 m, n=0.55 kW;1 set of central guide cylinder, phi 2.5m, h=1.5m; 1 set of water outlet triangular weir, l×b×δ=62.2m× 300mm×3mm;1 set of scum baffles, l×b×δ=60 m×300mm×3mm;
the reflow zone configuration: 2 return sludge pumps, q=246 m 3 H, h=10m, n=11kw; 2 residual sludge pumps, q=50m 3 H, h=15m, n=2.2 kW;1 set of aeration stirring device, uniform aeration system and air consumption of 3m 3 /min。
The present example also provides a recycle stream biochemical treatment method, which is carried out in the above reactor, for treating 250m 3 Industrial sewage/h, said method comprising the steps of:
(a) Mixing sewage and sludge from a sludge reflux zone in an anaerobic zone, and releasing phosphorus to obtain a mixed solution;
wherein the hydraulic retention time of the anaerobic zone is 12h, the upward flow rate of sewage is 0.5m/h, and the stirring strength is 8W/m 3 ；
(b) The mixed solution obtained in the step (a) enters an anoxic zone through an inlet to carry out denitrification to obtain a solution A;
wherein the hydraulic retention time of the anoxic zone is 12h, and the stirring strength is 8W/m 3 The denitrification load takes on a value of 0.05kgNO 3 -N/(kgmlss.d); the sludge load value of the solution A is 0.08kgBOD 5 /(kg MLSS. D), the sludge concentration of solution A was 4500mg/L;
(c) The solution A enters an aerobic zone to degrade organic matters, ammoniation and nitration of organic nitrogen and absorption of phosphorus to form a solution B, a part of the solution B enters a precipitation zone, and the rest of the solution B is recorded as nitration circulating liquid and enters an anoxic zone;
wherein the hydraulic retention time of the aerobic zone is 25h, and the stirring strength is 2W/m 3 Aeration intensity of 6m 3 /m 2 H; the reflux ratio of the nitrifying circulating liquid is 200%; the sludge concentration of the solution B is 4500mg/L;
(d) The solution B entering the precipitation zone is subjected to cement separation to obtain a solution C and sludge, the solution C is discharged from the reactor, and the sludge enters the sludge reflux zone;
wherein the surface load of the precipitation zone is 0.7m 3 /m 2 H, the sludge reflux ratio is 100%.
The reactor and the method are used for treating sewage, and the water quality of inlet water and the water quality of outlet water of the sewage are shown in table 1. COD (chemical oxygen demand) Cr Represents chemical oxygen demand, B0D 5 Represents biochemical oxygen demand, TN represents total nitrogen, NH 3 -N represents ammonia nitrogen, TP represents total phosphorus, SS represents solid suspension concentration.
TABLE 1
Example 2
The present example provides a circulating flow biochemical treatment reactor, based on the reactor described in one specific embodiment, the anaerobic zone, anoxic zone and aerobic zone have the following dimensions: l×b×h=16.5×9×8.5m, and the size of the sludge recirculation zone is l×b×h=3×9×8m; the size of the precipitation zone is lxbxh=4.7x4.7x5.5 m. No biological filler is arranged in the aerobic zone.
Anaerobic zone configuration: 2 first agitating unit: submersible mixer with impeller diameter 320mm and blade rotationSpeed 960r/min, n=4kw; 148 sets of aeration systems, disc type aerators and ventilation capacity of 2-8 m 3 /h;1 set of mud-water separation device, each set of service area 48m 2 The method comprises the steps of carrying out a first treatment on the surface of the 1 set of uniform water distribution device, each set of service area is 48m 2 The method comprises the steps of carrying out a first treatment on the surface of the 1 online dissolved oxygen detector, 0-20 mg/L;1 online ammonia nitrogen detector, 0-2000 mg/L, output 4-20 mA signal; 1 on-line nitrite detector, 0-2000 mg/L;1 online PH meter, pH is 0-14; 1 on-line temperature detector, 0-100 ℃;1 ultrasonic liquid level meter, 0-6 m.
Configuration of anoxic zone: 2 second stirring devices: submersible mixer, impeller diameter 320mm, blade speed 960r/min, n=4kw.
And (3) configuration of an aerobic zone: mixed liquor reflux pump, Q= -100 m3/H, H=10m, N=5.5kw, 1 is prepared by 1; tubular microporous aerator, 100-hole aerator/hm and aeration rate of 12-24 m 3 /h/sleeve, 96 sleeves; 0-20 mg/L and 1 station of online dissolved oxygen detector; 0 to 14,1 PH meter on line; screw fan, q=20m3/min, h=10m, n=30kw, 3 stations;
and (3) configuration of a precipitation area: mud scraper, Φ=4.7m, h=5.5 m,0.75kw,1 station; center guide cylinder, d×h=1×2m,1 set; water outlet weir, lxbδ=15.6mx300mm×3mm,1 set; scum baffle, l×b×δ=10.4m× 300mm×3mm, with scum bucket, 1 set; sludge reflux pump, q=15m3/H, h=10m, n=1.1kw, 1 for 1.
The present example also provides a recycle stream biochemical treatment method, which is carried out in the above reactor for treating 200m 3 Industrial waste water of/d, said method comprising the steps of:
(a) Mixing sewage and sludge from a sludge reflux zone in an anaerobic zone, and releasing phosphorus to obtain a mixed solution;
wherein the hydraulic retention time of the anaerobic zone is 45h, the upward flow rate of sewage is 0.5m/h, and the stirring strength is 12W/m 3 ；
(b) The mixed solution obtained in the step (a) enters an anoxic zone through an inlet to carry out denitrification to obtain a solution A;
wherein the hydraulic retention time of the anoxic zone is 38h, and the stirring strength is12W/m 3 The denitrification load takes on a value of 0.03kgNO 3 -N/(kgmlss.d); the sludge load of the solution A takes a value of 0.05kgBOD 5 /(kg MLSS. D), the sludge concentration of solution A was 4500mg/L;
(c) The solution A enters an aerobic zone to degrade organic matters, ammoniation and nitration of organic nitrogen and absorption of phosphorus to form a solution B, a part of the solution B enters a precipitation zone, and the rest of the solution B is recorded as nitration circulating liquid and enters an anoxic zone;
wherein the hydraulic retention time of the aerobic zone is 50h, and the stirring strength is 2W/m 3 Aeration intensity is 12m 3 /m 2 H; the reflux ratio of the nitrifying circulating liquid is 700%; the sludge concentration of the solution B is 4500mg/L;
(d) The solution B entering the precipitation zone is subjected to cement separation to obtain a solution C and sludge, the solution C is discharged from the reactor, and the sludge enters the sludge reflux zone;
wherein the surface load of the precipitation zone is 0.4m 3 /m 2 H, the sludge reflux ratio is 100%.
The reactor and the method are used for treating sewage, and the water quality of inlet water and the water quality of outlet water of the sewage are shown in table 2. COD (chemical oxygen demand) Cr Represents chemical oxygen demand, B0D 5 Represents biochemical oxygen demand, TN represents total nitrogen, NH 3 -N represents ammonia nitrogen, TP represents total phosphorus, SS represents solid suspension concentration.
TABLE 2
Example 3
The present example provides a recirculating flow biochemical reactor, based on the reactor described in one embodiment, the anoxic zone and the aerobic zone are sized as follows: l×b×h=14×19×6.5m, and the size of the sludge recirculation zone is l×b×h=10×3×3.7m; the size of the settling zone was l×b×h=9×9×3.7m. The reactor provided in this example does not contain an anaerobic zone inside.
Configuration of anoxic zone: submersible mixer, impeller diameter 620mm, blade rotation speed 480r/min, n=5.5 kw, 4; 0-20 mg/L and 2 stations of online dissolved oxygen detectors; 0 to 14,2 PH meters on line;
and (3) configuration of an aerobic zone: nitrifying liquid through-wall reflux pump, Q=180m3/H, H=0.8m, N=2.5kw, 2 stations; a pipe-type microporous aerator, Ventilation of 2-20 m 3 Each aerator can be independently closed for maintenance, and 160 sets of aerators can be independently closed for maintenance; regulating a weir gate, l×b=1500×500mm,2 sets; the unit diameter phi of the biological filler and the bracket is 150mm, the spacing is 150mm, the filling ratio of the biological filler is 10 percent, and 1 batch; 0-20 mg/L and 2 stations of online dissolved oxygen detectors; on-line PH meter: 0 to 14,2 stations; air suspension fan: q= 80m 3 Min, h=10m, n=110kw, variable frequency, 2 stations;
and (3) configuring a sludge recirculation zone: sludge reflux pump, q=30m 3 H, h=18m, n=3kw, 2 with 2 preparations; residual sludge pump, q=30m 3 H, h=18m, n=3kw, 1 with 1 preparation; aeration stirring device, perforated aeration system and air consumption of 3m 3 1 set of the medicine is per minute;
and (3) configuration of a precipitation area: a secondary sedimentation tank mud scraper, d×h=9×3.5m, n=0.55 kw,2 stations; center guide cylinder, dxh=1.5×1.5m,2 sets; water outlet weir, l×b×δ=32m×300mm×3mm,2 sets; a scum baffle, L×B×delta=23m×300mm×3mm, a scum bucket and 2 sets;
the present example also provides a recycle stream biochemical treatment method, which is carried out in the above reactor for treating 65m 3 Industrial sewage/h, said method comprising the steps of:
(1) Sewage enters an anoxic zone through an inlet to carry out denitrification to obtain a solution A;
Wherein the hydraulic retention time of the anoxic zone is 26 hours, and the stirring strength is 7W/m 3 The denitrification load takes on a value of 0.03kgNO 3 -N/(kgmlss.d); the sludge load of the solution A takes a value of 0.05kgBOD 5 /(kg MLSS. D), the sludge concentration of the solution A was 6000mg/L;
(2) The solution A enters an aerobic zone to degrade organic matters, ammoniation and nitration of organic nitrogen and absorption of phosphorus to form a solution B, a part of the solution B enters a precipitation zone, and the rest of the solution B is recorded as nitration circulating liquid and enters an anoxic zone;
wherein the hydraulic retention time of the aerobic zone is 18h, and the aeration intensity is 8m 3 /m 2 H; the reflux ratio of the nitrifying circulating liquid is 600%; the sludge concentration of the solution B is 6000mg/L;
(3) The solution B entering the precipitation zone is subjected to cement separation to obtain a solution C and sludge, the solution C is discharged from the reactor, and the sludge enters the sludge reflux zone;
wherein the surface load of the precipitation zone is 0.4m 3 /m 2 H, the sludge reflux ratio is 100%.
The reactor and the method are used for treating sewage, and the water quality of inlet water and the water quality of outlet water of the sewage are shown in table 3. COD (chemical oxygen demand) Cr Represents chemical oxygen demand, B0D 5 Represents biochemical oxygen demand, TN represents total nitrogen, NH 3 -N represents ammonia nitrogen, TP represents total phosphorus, SS represents solid suspension concentration.
TABLE 3 Table 3
Example 4
The present example provides a recirculating flow biochemical reactor, based on the reactor described in one embodiment, the anoxic zone and the aerobic zone are sized as follows: l×b×h=15×20×7.5m, the size of the sludge recirculation zone is l×b×h=8×2.5×3.8m m; the size of the settling zone was l×b×h=7×7×3.8m. The reactor provided in this example does not contain an anaerobic zone inside.
Configuration of anoxic zone: submersible mixer, impeller diameter 620mm, blade rotation speed 480r/min, n=5.5 kw,2 stations; 0-20 mg/L and 2 stations of online dissolved oxygen detectors; 0 to 14,1 PH meter on line;
and (3) configuration of an aerobic zone: nitrifying liquid through-wall reflux pump, Q=180m 3 H, h=0.8m, n=2.5kw, 2 stations; a pipe-type microporous aerator,ventilation of 2-14 m 3 Each set of aerator can be independently closed for maintenance, and 107 sets of aerators can be independently closed for maintenance; regulating a weir gate, l×b=1500×500mm,1 set; the unit diameter phi of the biological filler and the bracket is 150mm, the spacing is 150mm, the filling ratio of the biological filler is 10 percent, and 1 batch; on-line dissolved oxygen detector, 0-20 mg/L,4-20mA signal output, 1 station; on-line PH meter: 0 to 14,2 stations; air suspension fan: q=50m 3 /min, h=10m, n=100kw, 2 stations;
And (3) configuring a sludge recirculation zone: sludge reflux pump, q=15m 3 H, h=15m, n=2.2kw, 1 with 1 preparation; residual sludge pump, q=15m 3 H, h=15m, n=2.2kw, 1 stage; aeration stirring device, and air consumption is 3m 3 1 set of the medicine is per minute;
and (3) configuration of a precipitation area: a mud scraper, d×h=7×3.8m, n=0.55 kw,1 station; center guide cylinder, d×h=1.5×1.5m,1 set; water outlet weir, lxbδ=23.6mx300mm×3mm,2 jackets; scum baffle, l×b×δ=16.7m× 300mm×3mm, with scum bucket, 1 set;
the present example also provides a recycle stream biochemical treatment method, which is carried out in the above reactor for treating 50m 3 Industrial sewage/h, said method comprising the steps of:
(1) Sewage enters an anoxic zone through an inlet to carry out denitrification to obtain a solution A;
wherein the hydraulic retention time of the anoxic zone is 21h, and the stirring strength is 6W/m 3 The denitrification load takes on a value of 0.03kgNO 3 -N/(kgmlss.d); the sludge load of the solution A takes a value of 0.05kgBOD 5 /(kg MLSS. D), the sludge concentration of the solution A was 6000mg/L;
(2) The solution A enters an aerobic zone to degrade organic matters, ammoniation and nitration of organic nitrogen and absorption of phosphorus to form a solution B, a part of the solution B enters a precipitation zone, and the rest of the solution B is recorded as nitration circulating liquid and enters an anoxic zone;
Wherein the hydraulic retention time of the aerobic zone is 15h, and the aeration intensity is 10m 3 /m 2 H; the reflux ratio of the nitrifying circulating liquid is 700%; the sludge concentration of the solution B is 6000mg/L;
(3) The solution B entering the precipitation zone is subjected to cement separation to obtain a solution C and sludge, the solution C is discharged from the reactor, and the sludge enters the sludge reflux zone;
wherein the surface load of the precipitation zone is 1m 3 /m 2 H, the sludge reflux ratio is 100%.
The reactor and the method are used for treating sewage, and the water quality of inlet water and the water quality of outlet water of the sewage are shown in table 4. COD (chemical oxygen demand) Cr Represents chemical oxygen demand, B0D 5 Represents biochemical oxygen demand, TN represents total nitrogen, NH 3 -N represents ammonia nitrogen, TP represents total phosphorus, SS represents solid suspension concentration.
TABLE 4 Table 4
Example 5
This example provides a recirculating flow biochemical treatment reactor which differs from example 3 only in that:
the first water inlet area, the first water outlet area and the first diversion partition wall in the anoxic area are not arranged in the embodiment.
The circulating flow biochemical treatment method provided in this example is the same as that in example 3.
Example 6
This example provides a recirculating flow biochemical treatment reactor which differs from example 3 only in that:
The present embodiment does not provide a second deflector wall in the aerobic zone.
The circulating flow biochemical treatment method provided in this example is the same as that in example 3.
Example 7
This example provides a recirculating flow biochemical treatment reactor which is the same as example 3.
The biochemical treatment method of the recycle stream provided in this embodiment is different from that of embodiment 3 only in that:
in the embodiment, the hydraulic retention time of the anoxic zone is modified to be 0.5h, the hydraulic retention time of the aerobic zone is modified to be 6h, and the surface load of the sedimentation zone is modified to be 0.3m 3 /m 2 .h。
Example 8
This example provides a recirculating flow biochemical treatment reactor which is the same as example 3.
The biochemical treatment method of the recycle stream provided in this embodiment is different from that of embodiment 3 only in that:
in the embodiment, the reflux ratio of the nitrifying circulating liquid in the aerobic zone is modified to be 50%; the sludge reflux ratio was modified to 0%.
Comparative example 1
This comparative example provides a recirculating flow biochemical treatment reactor which differs from example 3 only in that:
in the embodiment, a nitrifying liquid return pipeline is not arranged in the aerobic zone.
The biochemical treatment method of the recycle stream provided in this comparative example was the same as that of example 3.
Comparative example 2
This comparative example provides a recirculating flow biochemical treatment reactor which differs from example 3 only in that:
In the embodiment, an anoxic return sludge pipeline is not arranged in the sludge return area.
The biochemical treatment method of the recycle stream provided in this comparative example was the same as that of example 3.
The reactors of examples 5-8 and comparative examples 1-2 were used to treat 65m 3 Industrial wastewater (identical to example 3) of/h, the influent water quality and the effluent water quality of which are shown in Table 5.
TABLE 5
From tables 1-5, the following points can be seen:
(1) From the data of examples 1-4, it can be seen that the reactor and the method provided by the invention can enable the effluent quality to reach or better than the direct discharge standard of the battery industry pollutant discharge standard (GB 30844-2013) and the electronic industry water pollutant discharge standard (GB 39031-2020);
(2) From the data of comparative examples 3 and 1-2, it can be seen that the comparative example 1 is different from example 3 in that no nitrifying liquid return line is provided in the aerobic zone, and the comparative example 2 is different from example 3 in that no anoxic return sludge line is provided in the sludge return zone, and from Table 5, the effluent quality of comparative examples 1-2 is deteriorated compared with example 3, so that the reactor and the method provided by the present invention have excellent treatment effects.
In conclusion, the circulating flow biochemical treatment method provided by the invention not only can realize the maximization of the nitrogen and phosphorus removal rate, but also can realize the stable and reliable treatment effect, flexible adjustment of process control, environmental friendliness, low energy consumption and convenient management of operation and maintenance.
The applicant states that the detailed structural features of the present invention are described by the above embodiments, but the present invention is not limited to the above detailed structural features, i.e. it does not mean that the present invention must be implemented depending on the above detailed structural features. It should be apparent to those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, addition of auxiliary components, selection of specific modes, etc., are within the scope of the present invention and the scope of the disclosure.
The applicant states that the detailed process flow of the present invention is illustrated by the above examples, but the present invention is not limited to the above detailed process flow, i.e. it does not mean that the present invention must be implemented depending on the above detailed process flow. It should be apparent to those skilled in the art that any modification of the present invention, equivalent substitution of raw materials for the product of the present invention, addition of auxiliary components, selection of specific modes, etc., falls within the scope of the present invention and the scope of disclosure.
Claims (10)
1. A circulating flow biochemical treatment reactor, which is characterized by comprising an anoxic zone, an aerobic zone and a sedimentation zone which are sequentially connected along a sewage flow method, and a sludge reflux zone for discharging sludge;
The aerobic zone is provided with a nitrifying liquid return pipeline to the anoxic zone;
the sludge reflux zone is provided with an anoxic reflux sludge pipeline to the anoxic zone.
2. The circulation flow biochemical treatment reactor according to claim 1, wherein the material of the reactor comprises steel or steel concrete;
preferably, the outlet of the anoxic zone is provided with a first water passing hole;
preferably, a first water inlet area is arranged on one side of the anoxic area close to the inlet;
preferably, a first water outlet area is arranged on one side of the anoxic area close to the first water passing hole;
preferably, a first diversion partition wall is arranged between the first water inlet area and the first water outlet area;
preferably, at least one second stirring device is respectively arranged in the first water inlet area and the first water outlet area;
preferably, the anoxic zone is connected with the inlet of the aerobic zone through a first water passing hole.
3. The circulating flow biochemical treatment reactor according to claim 1 or 2, wherein at least two sets of support frames are provided inside the aerobic zone;
preferably, the support frame is provided with biological filler;
preferably, the biological filler accounts for 8-15% of the volume of sewage in the aerobic zone;
Preferably, the biological filler comprises PP material and/or modified fiber material;
preferably, at least one aeration device for oxygenating and stirring the mixed liquor is arranged in the aerobic zone;
preferably, the aerobic zone is connected with the inlet of the sedimentation zone through a communicating pipe;
preferably, a second diversion partition wall is arranged in the aerobic zone;
preferably, the second guide partition wall comprises a U-shaped partition wall and a partition wall;
preferably, the partition wall is fixedly arranged at the middle position of the top of the aerobic zone;
preferably, the U-shaped partition wall is fixedly arranged at the middle position of the bottom of the aerobic zone;
preferably, at least two third stirring devices for stirring sewage are arranged in the aerobic zone.
4. A recirculating flow biochemical treatment reactor according to any one of claims 1-3, characterized in that the middle part of the sedimentation zone is provided with a sludge scraping device;
preferably, the mud scraping device comprises a mud scraper, a central guide cylinder, a scum baffle and a slag discharge hopper;
preferably, the inlet of the central guide cylinder of the mud scraping device is connected with the communicating pipe;
preferably, the sludge of the sludge scraping device is connected with the sludge reflux zone through a sludge discharge pipeline;
Preferably, the upper part of the sedimentation zone is provided with a water outlet weir plate;
preferably, the water outlet weir plate is connected with a drain pipe.
5. The circulating flow biochemical treatment reactor of any one of claims 1-4, further comprising an anaerobic zone connected to the anoxic zone within the circulating flow biochemical treatment reactor;
preferably, the inlet of the anaerobic zone is provided with a water inlet pipe;
preferably, the water outlet end of the water inlet pipe is connected with a uniform water distribution device;
preferably, an aeration device is arranged at the bottom of the anaerobic zone;
preferably, a mud-water separation device and a first stirring device are arranged in the anaerobic zone;
preferably, the water outlet pipeline of the mud-water separation device is divided into two branches, one branch is connected with the water inlet pipe, and the other branch is connected with the inlet of the anoxic zone;
preferably, the anaerobic zone is provided with an anaerobic return sludge pipeline to the sludge return zone;
preferably, the anaerobic zone is provided with an anaerobic external sludge line to provide anaerobic sludge for the anaerobic zone.
6. The circulating flow biochemical treatment reactor according to any one of claims 1 to 5, wherein the sludge recirculation zone is provided with a recirculation sludge line to an anaerobic zone;
Preferably, the sludge recirculation zone is provided with a sludge discharge pipe.
7. A method for biochemical treatment of a recycle stream, characterized in that the method is carried out in a reactor according to any one of claims 1 to 6.
8. The method according to claim 7, characterized in that it comprises the steps of:
(1) The sewage enters an anoxic zone through an inlet to carry out denitrification to obtain a solution A, and part of organic matters are degraded;
(2) The solution A enters an aerobic zone to degrade organic matters, ammoniation and nitration of organic nitrogen and absorption of phosphorus to form a solution B, a part of the solution B enters a precipitation zone, and the rest of the solution B is recorded as nitration circulating liquid and enters an anoxic zone;
(3) And (3) performing mud-water separation on the solution B entering the precipitation zone to obtain a solution C and sludge, discharging the solution C from the reactor, and allowing the sludge to enter a sludge reflux zone.
9. The method of claim 8, wherein the hydraulic retention time of the anoxic zone of step (1) is 1 to 40 hours;
preferably, the stirring intensity of the anoxic zone in the step (1) is 4-12W/m 3 ；
Preferably, the denitrification load of the anoxic zone in the step (1) is in the range of 0.03 to 0.06kgNO 3 -N/(kgMLSS.d)；
Preferably, the sludge load of the solution A and the solution B is 0.05-0.15 kgBOD 5 /(kgMLSS.d)；
Preferably, the sludge concentration of the solution A and the solution B is 4000-8000 mg/L;
preferably, the hydraulic retention time of the aerobic zone in the step (2) is 7-50 h;
preferably, the stirring intensity of the aerobic zone in the step (2) is 1-3W/m 3 ；
Preferably, the reflux ratio of the nitrifying circulating liquid in the step (2) is 100-1200%;
preferably, the aeration intensity of the aerobic zone in the step (2) is 6-12 m 3 /m 2 .h；
Preferably, the surface load of the precipitation zone of step (3) is from 0.4 to 1m 3 /m 2 .h；
Preferably, the sludge reflux ratio of the sludge reflux zone in the step (3) is 0-100%.
10. The method of claim 8 or 9, wherein the wastewater of step (1) further comprises, prior to entering the anoxic zone: mixing sewage and sludge from a sludge reflux zone in an anaerobic zone and releasing phosphorus;
preferably, the hydraulic retention time of the anaerobic zone is 0.5-45 h;
preferably, the total nitrogen removal load of the anaerobic zone is in the range of 0.3-3 kgTN/m 3 .d；
Preferably, the upward flow rate of the sewage in the anaerobic zone is 0.5-1.5 m/h;
preferably, the stirring intensity of the anaerobic zone is 4-12W/m 3 。
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