CN113697953A - Realization of A based on gradual reduction of suspended sludge concentration2Device and method for quickly starting anaerobic ammonium oxidation process in situ of/O part - Google Patents
Realization of A based on gradual reduction of suspended sludge concentration2Device and method for quickly starting anaerobic ammonium oxidation process in situ of/O part Download PDFInfo
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Abstract
Realization of A based on gradual reduction of suspended sludge concentration2An apparatus and a method for quick in-situ starting of an anaerobic ammonia oxidation process of an/O continuous flow part belong to the field of sewage treatment. 1) Adding suspended fillers without film hanging in an anaerobic/anoxic zone to provide a good environment for the retention and growth of anaerobic ammonium oxidation bacteria; 2) denitrifying bacteria gradually enriched on the anaerobic/anoxic biomembrane have short-range denitrification characteristics and can provide necessary substrate nitrite nitrogen for anaerobic ammonium oxidation bacteria; 3) and finally, the suspended sludge concentration is reduced to enable the denitrifying bacteria on the anaerobic/anoxic biomembrane to compete to more substrates, so that more substrate nitrite nitrogen is provided for the anaerobic ammonia oxidizing bacteria, the competitiveness of the whole course denitrifying bacteria in the suspended sludge to the nitrite nitrogen is weakened, and the anaerobic ammonia oxidizing bacteria are promoted to grow and be enriched together. And (3) adding suspended fillers which are not coated with membranes into the aerobic zone to enrich the nitrifying bacteria on the aerobic biomembrane. The invention realizes that2The quick in-situ start of the anaerobic ammonia oxidation process of the/O part saves energy and reduces consumption.
Description
Technical Field
The invention relates to a device and a method for deeply removing nitrogen and phosphorus from sewage, belongs to the technical field of sewage treatment by an activated sludge process, and is suitable for the technical fields of upgrading and modifying newly-built sewage plants and old sewage plants, treating municipal sewage and industrial wastewater and the like.
Background
At present, the municipal sewage treatment plant widely adopts the traditional nitrification and denitrification technology to carry out biological denitrification. Sufficient aeration is required in the nitrification process, which consumes a large amount of electric energy. The C/N ratio of urban sewage in China is low, so that a good denitrification effect can be achieved only by providing sufficient carbon sources in the denitrification process. In addition, in the traditional activated sludge nitrogen and phosphorus removal process, the nitrifying bacteria, the denitrifying bacteria and the phosphorus accumulating bacteria have contradiction and competition in the requirements of organic load, sludge age and carbon source, so that the nitrogen and phosphorus can not be efficiently removed in the same system at the same time, and the application of the biological phosphorus and phosphorus removal technology is prevented. Therefore, the seeking of a novel denitrification and dephosphorization process technology has great significance for energy conservation and consumption reduction of a sewage treatment plant.
As a novel denitrification technology, anaerobic ammonia oxidation has the advantages of saving aeration energy consumption and organic carbon source, low sludge yield and the like. At present, the anaerobic ammonia oxidation technology is mainly applied to the treatment of high-ammonia nitrogen and high-temperature wastewater such as sludge digestive juice, and if the anaerobic ammonia oxidation technology is applied to the treatment of urban main stream domestic sewage, the energy neutralization or output of a sewage treatment plant is hopeful to be realized. The major bottleneck of the application of the anammox technology in mainstream sewage treatment is the enrichment and retention of anammox bacteria, however, the realization of anammox by inoculating anammox mature sludge in an actual sewage treatment plant is impractical, so that the important significance of seeking a strategy for rapidly enriching the anammox bacteria in situ in mainstream municipal sewage is realized.
Research shows that the biomembrane in the anaerobic/anoxic zone can effectively retain anaerobic ammonia oxidizing bacteria, and denitrifying bacteria on the biomembrane can perform short-range denitrification to reduce nitrate nitrogen into nitrite nitrogen to provide substrate nitrite for anaerobic ammonia oxidation. Therefore, by adding the suspended filler in anaerobic/anoxic anaerobic treatment and adopting a certain strategy to quickly enrich the anammox bacteria in situ, the practical application of the anammox technology in urban main stream sewage treatment is expected to be promoted.
Disclosure of Invention
The purpose of the invention is to solve the problem that the anammox bacteria are in practiceThe anaerobic ammonia oxidation technology is difficult to enrich and retain in a sewage treatment plant, so that the application of the anaerobic ammonia oxidation technology in actual main stream sewage is limited, and the method for realizing A based on gradually reducing the concentration of suspended sludge is provided2A device and a method for quickly starting an anaerobic ammonium oxidation process in situ of an O part. The method adds the suspended filler in the anaerobic/anoxic zone to provide a good environment for the retention and growth of the anaerobic ammonium oxidation bacteria. The denitrifying bacteria on the anaerobic/anoxic biomembrane have short-range denitrification characteristics, can reduce nitrate nitrogen into nitrite nitrogen, provide substrate nitrite for anaerobic ammonia oxidizing bacteria, and promote the growth of the anaerobic ammonia oxidizing bacteria on the anaerobic/anoxic biomembrane. In the process of reducing the suspended sludge, denitrifying bacteria on the anaerobic/anoxic biomembrane can compete to more substrates, so that more substrate nitrite nitrogen is provided for anaerobic ammonia oxidizing bacteria, the competitiveness of the whole-process denitrifying bacteria in the suspended sludge to the nitrite nitrogen is weakened, and the growth of the anaerobic ammonia oxidizing bacteria is promoted together to enrich the anaerobic ammonia oxidizing bacteria. Meanwhile, the suspended filler is added into the aerobic zone, so that enrichment of nitrifying bacteria on the aerobic biomembrane filler is promoted, and the nitrification performance of the aerobic zone is ensured to be kept stable in the process of reducing the concentration of the suspended sludge. And finally, under the condition of ensuring that the effluent of the bioreactor system is relatively stable, the rapid in-situ start of the anaerobic ammonia oxidation process of the continuous flow urban main stream sewage part is realized.
Realization of A based on gradual reduction of suspended sludge concentration2The device for quickly starting the anaerobic ammonia oxidation process of the/O part in situ mainly comprises a raw water tank (1) and an A2The reaction device (3) and the secondary sedimentation tank (11) are connected in sequence, A2the/O reaction device (3) sequentially comprises an anaerobic zone (4), an anoxic zone (5) and an aerobic zone (6); the raw water tank (1) is connected with the anaerobic zone (4) through a water inlet pump (2), the anaerobic zone (4) is connected with the anoxic zone (5), the anoxic zone (5) is connected with the aerobic zone (6), and overflowing holes are arranged in a vertically staggered mode according to the water flow direction to be connected with each grid chamber; the aerobic zone (6) is connected with the channel A2the/O overflow pipe (10) is connected with the secondary sedimentation tank (11); the bottom of the secondary sedimentation tank (11) is connected with the anaerobic zone (4) through a sludge reflux pump (17); a nitrifying liquid reflux pump (16) connects the last cell of the aerobic zone (6) with the first cell of the anoxic zone (5); a stirrer (7) is arranged in the anaerobic zone (4) and the anoxic zone (5) and is used for mixing the mixed liquid and fluidizing the suspended carrier (8);the aerobic zone (6) is provided with an aeration system of an air compressor (13), a gas flowmeter (14) and an aeration head (15) for aeration and fluidization of the aerobic zone suspension carrier (9); a polyethylene filler (8) with the specific surface area of 500m2/m3 and the diameter of 25 mm is placed in the anoxic zone (5), the filling ratio of the polyethylene filler is 10-30%, growth carriers are provided for anaerobic ammonium oxidation bacteria and denitrifying bacteria, and the anaerobic ammonium oxidation bacteria and the denitrifying bacteria are enriched; the aerobic zone (6) is internally provided with a polyethylene filler (9) with the diameter of 25 mm and the specific surface area of 500m2/m3, the filling ratio is 20-40 percent, and the polyethylene filler provides a growth carrier for nitrobacteria and enriches the nitrobacteria.
Realization of A based on gradual reduction of suspended sludge concentration2The device and the method for quickly starting the anaerobic ammonia oxidation process of the/O part in situ are characterized by comprising the following steps of:
stage one: the method is operated for 20-30 days under the condition that the concentration of suspended sludge is 3000-4000 mg/L according to the following operation adjusting and controlling strategy, so that part of activated sludge microorganisms are preliminarily attached and intercepted on the filler;
and a second stage: on the basis of the original excess sludge discharge, the discharge amount of the excess sludge is additionally increased by 5 to 10 percent every day, so that the sludge discharge amount A is increased2The concentration of the suspended sludge in the/O reaction device (3) is gradually reduced to 2000-3000 mg/L for 30-45 d; increasing the surplus sludge discharge and simultaneously increasing the aeration amount of each cell of the aerobic zone (6), and controlling the dissolved oxygen concentration in the last cell of the aerobic zone (6) to be 2-4 mg/L so that the ammonia nitrogen concentration of effluent water at the aerobic end is lower than 2 mg/L; then, the concentration of suspended sludge in the system is maintained to be 2000-3000 mg/L, and the system is operated for 30-60 d according to the following operation adjusting and controlling strategy;
and a third stage: on the basis of the stage two, the discharge amount of the residual sludge is additionally increased by 5 to 10 percent every day, so that the sludge is discharged from the stage A2The concentration of the suspended sludge in the/O reaction device (3) is gradually reduced to 1000-2000 mg/L for 30-45 d; increasing the surplus sludge discharge and simultaneously increasing the aeration amount of each cell of the aerobic zone (6), and controlling the dissolved oxygen concentration in the last cell of the aerobic zone (6) to be 2-4 mg/L so that the ammonia nitrogen concentration of effluent water at the aerobic end is lower than 2 mg/L; then, the concentration of suspended sludge in the system is maintained to be 1000-2000 mg/L, and the system is operated for 30-60 d according to the following operation adjusting and controlling strategy;
the runtime adjustment and control strategy is as follows:
A2the reflux ratio of the nitrifying liquid in the/O reaction device (3) is controlled to be 100-200%, and when the concentration of nitrate nitrogen or nitrite nitrogen in effluent of the anoxic zone (5) is higher than 3mg/L, the reflux ratio of the nitrifying liquid is reduced; when the concentration of nitrate nitrogen in the effluent of the aerobic zone (6) is higher than 10mg/L, the reflux ratio of the nitrifying liquid is increased;
the sludge reflux ratio is 50-100%, and the A is controlled by adjusting the discharge amount of the excess sludge2The sludge age of the floc sludge in the/O reaction device (3) is 15-20 days; the concentration of dissolved oxygen in the last cell of the aerobic zone (6) is 1-2 mg/L;
A2the hydraulic retention time of the/O reaction device (3) is 10-16 h, wherein the anaerobic hydraulic retention time is 1.5-3 h, so that the phosphorus release amount of the anaerobic zone (4) is more than 10 mg/L; the anoxic hydraulic retention time is 3-8 h;
when the average biomass of a single anaerobic/anoxic biomembrane is above 0.01g, the relative abundance of anaerobic ammonium oxidation bacteria is above 1%; a. the2the/O part anaerobic ammonia oxidation process is successfully started in situ quickly.
Realization of A based on gradual reduction of suspended sludge concentration2The device and the method for quickly starting the anaerobic ammonia oxidation process in situ of the/O part are characterized in that suspended fillers are added into an anaerobic/anoxic zone, so that a growth carrier can be provided for anaerobic ammonia oxidation bacteria, and the anaerobic ammonia oxidation bacteria can be effectively retained and enriched; the mutual supply and competition relationship of the biofilm and the functional microorganisms on the suspended sludge to the reaction substrates are regulated and controlled by regulating and controlling the concentration of the suspended sludge; in the process of gradually reducing the concentration of the suspended sludge, more nitrate nitrogen and organic matters are utilized by denitrifying bacteria with short-range denitrification characteristics on the anaerobic/anoxic biomembrane, so that more substrate nitrite nitrogen is provided for anaerobic ammonia oxidizing bacteria, the competitiveness of the whole-process denitrifying bacteria in the suspended sludge on the nitrite nitrogen is weakened, and the growth of the anaerobic ammonia oxidizing bacteria is promoted together to enrich the anaerobic ammonia oxidizing bacteria. The suspended filler added in the aerobic zone can continuously enrich nitrifying bacteria, and the nitrification performance of the aerobic zone is ensured to be kept stable in the process of reducing the concentration of suspended sludge.
Based on the gradual reduction of the suspended sludge concentrationDegree of achievement A2Compared with the prior art, the device and the method for quickly starting the/O partial anaerobic ammonia oxidation process in situ have the following advantages:
1) the key problem of anaerobic ammonia oxidation bacteria in-situ enrichment and retention in the application of the mainstream municipal sewage anaerobic ammonia oxidation technology is solved, and the method for realizing the rapid in-situ start of the anaerobic ammonia oxidation technology of the continuous flow mainstream municipal sewage part by gradually reducing the concentration of suspended sludge is firstly proposed;
2) in the implementation process, the effluent quality of the original bioreactor is kept relatively stable, the implementation without stopping production is realized, and the method can be widely applied to the upgrading and reconstruction of newly-built sewage plants and old sewage plants;
3) partial autotrophic nitrogen removal is realized based on short-cut denitrification coupling anaerobic ammonia oxidation, 50% of aeration quantity and 60% of carbon source adding quantity can be saved to the maximum theoretically, the sludge yield is low, and the sludge treatment cost is reduced;
drawings
FIG. 1 achievement of A based on stepwise reduction of suspended sludge concentration2The device for quickly starting the anaerobic ammonia oxidation process of the/O part in situ.
In fig. 1: 1-raw water tank; 2-a water inlet pump; 3-A2an/O reaction unit; 4-an anaerobic zone; 5-anoxic zone; 6-aerobic zone; 7-a stirrer; 8-diameter 25 mm specific surface area 500m2/m3The anaerobic/anoxic zone polyethylene filler of (a); 9-diameter 25 mm specific surface area 500m2/m3The aerobic zone polyethylene filler; 10-A2an/O overflow pipe; 11-a secondary sedimentation tank; 12-a water outlet; 13-a blower; 14-a rotameter; 15-a microporous aeration head; 16-nitrifying liquid reflux pump; 17-sludge reflux pump; 18-sludge return gate valve; 29-excess sludge gate valve.
Detailed Description
In order to make the implementation of the invention clearer, the invention is further explained in detail with reference to the attached drawings by combining specific embodiments. It should be noted that the following embodiments are only examples to help understand the core idea and technical solution of the present invention. The scope of the invention is not limited thereto.
1. Inoculating sludge
A2the/O reaction device (3) is inoculated with residual activated sludge of a secondary sedimentation tank of a traditional sewage treatment plant, and the activated sludge has basic nitrification, denitrification, carbon removal and phosphorus removal performances, MLSS>8000mg/L、MLVSS/MLSS>0.65、SV<45%, keeping the initial sludge concentration of the reactor to be 3000-4000 mg/L; high-density polyethylene suspension fillers (8) without film hanging are added into the anaerobic zone (4) and the anoxic zone (5) for enriching anaerobic ammonium oxidation bacteria and denitrifying bacteria, and the filling ratio is 10-30%; the aerobic zone (6) is added with high-density polyethylene suspended filler (9) without film hanging for enriching nitrobacteria, and the filling ratio is 20-40%;
2. gradually reducing the sludge concentration and enriching anaerobic ammonium oxidation bacteria on an anaerobic/anoxic biomembrane
1) Stage one: operating for 20-30 d according to the following operation adjusting and controlling strategy under the condition that the concentration of the suspended sludge is 3000-4000 mg/L, so that part of activated sludge microorganisms are preliminarily attached and intercepted on the filler; because the concentration of dissolved oxygen is low in the anaerobic/anoxic zone, functional microorganisms mainly attached and trapped on the packing of the anaerobic/anoxic zone are denitrifying bacteria and anaerobic ammonium oxidation bacteria; in the aerobic zone, due to a higher dissolved oxygen environment, the suspended filler mainly adheres to and entraps functional microorganisms which are nitrifying bacteria; the anaerobic ammonia oxidizing bacteria are difficult to effectively retain in the system due to low growth rate, the anaerobic/anoxic biomembrane can provide good growth conditions for the anaerobic ammonia oxidizing bacteria with low growth rate, and the biomembrane and floc sludge are separated in sludge age, so that the anaerobic ammonia oxidizing bacteria can be prevented from being elutriated by the system, and the purpose of effectively retaining and enriching the anaerobic ammonia oxidizing bacteria is achieved;
2) and a second stage: on the basis of the original excess sludge discharge, the discharge amount of the excess sludge is additionally increased by 5 to 10 percent every day, so that the sludge discharge amount A is increased2The concentration of the suspended sludge in the/O reaction device (3) is gradually reduced to 2000-3000 mg/L for 30-45 d; increasing the surplus sludge discharge and simultaneously increasing the aeration amount of each cell of the aerobic zone (6), and controlling the dissolved oxygen concentration in the last cell of the aerobic zone (6) to be 2-4 mg/L so that the ammonia nitrogen concentration of effluent water at the aerobic end is lower than 2 mg/L; then, the concentration of suspended sludge in the system is maintained to be 2000-3000 mg/L, and the system is operated for 30-60 d according to the following operation adjusting and controlling strategy; due to suspensionAfter the sludge concentration is reduced, denitrifying bacteria on an anoxic biomembrane in the anoxic zone (5) compete for more substrates, so that more nitrate nitrogen is reduced into nitrite nitrogen, more substrate nitrite nitrogen is provided for anaerobic ammonia oxidizing bacteria, the growth of the anaerobic ammonia oxidizing bacteria is promoted to enrich the anaerobic ammonia oxidizing bacteria, nitrifying bacteria on a suspension filler in the aerobic zone (6) are enriched due to the fact that more substrates can be obtained, and the nitrification performance of the aerobic zone (6) in the process of reducing the concentration of the suspended sludge is guaranteed;
3) and a third stage: on the basis of the stage two, the discharge amount of the residual sludge is additionally increased by 5 to 10 percent every day, so that the sludge is discharged from the stage A2The concentration of the suspended sludge in the/O reaction device (3) is gradually reduced to 1000-2000 mg/L for 30-45 d; increasing the surplus sludge discharge and simultaneously increasing the aeration amount of each cell of the aerobic zone (6), and controlling the dissolved oxygen concentration in the last cell of the aerobic zone (6) to be 2-4 mg/L so that the ammonia nitrogen concentration of effluent water at the aerobic end is lower than 2 mg/L; then, the concentration of suspended sludge in the system is maintained to be 1000-2000 mg/L, and the system is operated for 30-60 d according to the following operation adjusting and controlling strategy; as the concentration of the suspended sludge is further reduced, the biological membrane in the anoxic zone (4) can obtain more substrates, the denitrifying bacteria and the anaerobic ammonium oxidation bacteria on the biological membrane in the anoxic zone (5) are further enriched, and the nitrifying bacteria on the biological membrane in the aerobic zone (6) are further enriched.
The runtime adjustment and control strategy is as follows:
A2the reflux ratio of the nitrifying liquid in the/O reaction device (3) is controlled to be 100-200%, and when the concentration of nitrate nitrogen or nitrite nitrogen in effluent of the anoxic zone (5) is higher than 3mg/L, the reflux ratio of the nitrifying liquid is reduced; when the concentration of nitrate nitrogen in the effluent of the aerobic zone (6) is higher than 10mg/L, the reflux ratio of the nitrifying liquid is increased;
the sludge reflux ratio is 50-100%, and the A is controlled by adjusting the discharge amount of the excess sludge2The sludge age of the floc sludge in the/O reaction device (3) is 15-20 days; the concentration of dissolved oxygen in the last cell of the aerobic zone (6) is 1-2 mg/L;
A2the hydraulic retention time of the/O reaction device (3) is 10-16 h, wherein the anaerobic hydraulic retention time is 1.5-3 h, so that the phosphorus release amount of the anaerobic zone (4) is more than 10 mg/L; the anoxic hydraulic retention time is 3-8 h;
when the average biomass of a single anaerobic/anoxic biomembrane is above 0.01g, the relative abundance of anaerobic ammonium oxidation bacteria is above 1%; a. the2the/O part anaerobic ammonia oxidation process is successfully started in situ quickly.
The experiment adopts domestic sewage of a certain community as raw water, and the specific water quality is as follows: NH (NH)4 +N is 45-60 mg/L, COD concentration is 140-250 mg/L, NO2 -N concentration of 0 to 0.5mg/L, NO3 --N concentration 0-1 mg/L;
the test result shows that: after 200 days of operation, the average biomass on a single anoxic biofilm was 0.023g, wherein the relative abundance of anammox bacteria was 1.8%; the experimental effluent quality was as follows: NH (NH)4 +N is 0 to 2mg/L, COD concentration is 20 to 35mg/L, NO2 --N concentration 0-0.5 mg/L, NO3 -The concentration of-N is 8-12 mg/L, and the concentration of TN is 9-12 mg/L.
It is noted that in the drawings and in the description, implementation methods not shown or described are all forms known to those of ordinary skill in the art and are not described in detail. In addition, the above definitions of the respective elements are not limited to the specific structures, shapes or methods mentioned in the embodiments, and may not be simply modified or replaced. Any modification made within the spirit and principle of the present invention should be included within the scope of protection of the present invention.
Claims (3)
1. Realization of A based on gradual reduction of suspended sludge concentration2The device for quickly starting the anaerobic ammonia oxidation process in situ of the/O part is characterized in that: comprising a raw water tank (1) and A2the/O reaction device (3) and the secondary sedimentation tank (11) are connected in sequence; wherein A is2the/O reaction device (3) sequentially comprises an anaerobic zone (4), an anoxic zone (5) and an aerobic zone (6); the raw water tank (1) is connected with the anaerobic zone (4) through a water inlet pump (2), the anaerobic zone (4) is connected with the anoxic zone (5), the anoxic zone (5) is connected with the aerobic zone (6), and overflowing holes are arranged in a vertically staggered mode according to the water flow direction to be connected with each grid chamber; the aerobic zone (6) is connected with the channel A2the/O overflow pipe (10) is connected with the secondary sedimentation tank (11); two sinksThe bottom of the tank (11) is connected with the anaerobic zone (4) through a sludge reflux pump (17); a nitrifying liquid reflux pump (16) connects the last cell of the aerobic zone (6) with the first cell of the anoxic zone (5);
a stirrer (7) is arranged in the anaerobic zone (4) and the anoxic zone (5) and is used for mixing the mixed liquid and fluidizing the suspended filler (8); the aerobic zone (6) is provided with an aeration system of an air compressor (13), a gas flowmeter (14) and an aeration head (15) for aeration and fluidization of the suspended filler (9) in the aerobic zone.
2. The device according to claim 1, characterized in that polyethylene filler (8) is added into the anaerobic zone (4) and the anoxic zone (5) at a filling ratio of 10-30% to provide growth carriers for the anammox bacteria and the denitrifying bacteria so as to enrich the anammox bacteria and the denitrifying bacteria; the aerobic zone (6) is filled with 20-40 percent of the filler ratio to provide a growth carrier for the nitrobacteria so as to enrich the nitrobacteria.
3. The device of claim 1 is used for realizing A2The method for quickly starting the anaerobic ammonium oxidation process of the/O part in situ is characterized by comprising the following steps of:
(1) sludge inoculation: a. the2Inoculating residual activated sludge in a secondary sedimentation tank of a traditional sewage treatment plant by the aid of the/O reaction device (3), wherein the sludge concentration is 3000-4000 mg/L;
(2) the operation steps of gradually reducing the concentration of the suspended sludge are as follows:
stage one: the method is operated for 20-30 days under the condition that the concentration of suspended sludge is 3000-4000 mg/L according to the following operation adjusting and controlling strategy, so that part of activated sludge microorganisms are preliminarily attached and intercepted on the filler;
and a second stage: on the basis of the original excess sludge discharge, the discharge amount of the excess sludge is additionally increased by 5 to 10 percent every day, so that the sludge discharge amount A is increased2The concentration of the suspended sludge in the/O reaction device (3) is gradually reduced to 2000-3000 mg/L for 30-45 d; increasing the surplus sludge discharge and simultaneously increasing the aeration amount of each cell of the aerobic zone (6), and controlling the dissolved oxygen concentration in the last cell of the aerobic zone (6) to be 2-4 mg/L so that the ammonia nitrogen concentration of effluent water at the aerobic end is lower than 2 mg/L; suspension of the afterward maintenance systemThe concentration of the floating sludge is 2000-3000 mg/L, and the operation is carried out for 30-60 d according to the following operation adjusting and controlling strategy;
and a third stage: on the basis of the stage two, the discharge amount of the residual sludge is additionally increased by 5 to 10 percent every day, so that the sludge is discharged from the stage A2The concentration of the suspended sludge in the/O reaction device (3) is gradually reduced to 1000-2000 mg/L for 30-45 d; increasing the surplus sludge discharge and simultaneously increasing the aeration amount of each cell of the aerobic zone (6), and controlling the dissolved oxygen concentration in the last cell of the aerobic zone (6) to be 2-4 mg/L so that the ammonia nitrogen concentration of effluent water at the aerobic end is lower than 2 mg/L; then, the concentration of suspended sludge in the system is maintained to be 1000-2000 mg/L, and the system is operated for 30-60 d according to the following operation adjusting and controlling strategy;
the runtime adjustment and control strategy is as follows:
A2the reflux ratio of the nitrifying liquid in the/O reaction device (3) is controlled to be 100-200%, and when the concentration of nitrate nitrogen or nitrite nitrogen in effluent of the anoxic zone (5) is higher than 3/L, the reflux ratio of the nitrifying liquid is reduced; when the concentration of nitrate nitrogen in the effluent of the aerobic zone (6) is higher than 10mg/L, the reflux ratio of the nitrifying liquid is increased;
the sludge reflux ratio is 50-100%, and the A is controlled by adjusting the discharge amount of the excess sludge2The sludge age of the floc sludge in the/O reaction device (3) is 15-20 days; the concentration of dissolved oxygen in the last cell of the aerobic zone (6) is 1-2 mg/L;
A2the hydraulic retention time of the/O reaction device (3) is 10-16 h, wherein the anaerobic hydraulic retention time is 1.5-3 h, so that the phosphorus release amount of the anaerobic zone (4) is more than 10 mg/L; the anoxic hydraulic retention time is 3-8 h;
when the average biomass of a single anaerobic/anoxic biomembrane is above 0.01g, the relative abundance of anaerobic ammonium oxidation bacteria is above 1%; a. the2the/O part anaerobic ammonia oxidation process is successfully started in situ quickly.
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| CN115745161A (en) * | 2022-11-05 | 2023-03-07 | 北京工业大学 | Device and method for transforming traditional municipal sewage denitrification process based on suspended sludge into pure biomembrane PDA denitrification process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007275833A (en) * | 2006-04-11 | 2007-10-25 | Souwa Eng:Kk | Microorganism treatment method and device for waste water |
| CN102718314A (en) * | 2012-05-24 | 2012-10-10 | 北京工业大学 | Method for quick starting of anaerobic ammonium oxidation technology at room temperature in low matrix |
| CN104556376A (en) * | 2014-11-29 | 2015-04-29 | 北京工业大学 | Autotrophic nitrogen removal method for biological phosphorus removal of urban sewage based on short-cut denitrification for providing nitrite |
| CN106477812A (en) * | 2016-10-28 | 2017-03-08 | 重庆渝桑环保科技有限公司 | Saprobia multiplication denitrifying method |
| CN110615531A (en) * | 2019-09-16 | 2019-12-27 | 北京工业大学 | DEAMOX sludge double-reflux AOAO sewage-based deep nitrogen and phosphorus removal device and method |
-
2021
- 2021-08-11 CN CN202110919734.XA patent/CN113697953B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007275833A (en) * | 2006-04-11 | 2007-10-25 | Souwa Eng:Kk | Microorganism treatment method and device for waste water |
| CN102718314A (en) * | 2012-05-24 | 2012-10-10 | 北京工业大学 | Method for quick starting of anaerobic ammonium oxidation technology at room temperature in low matrix |
| CN104556376A (en) * | 2014-11-29 | 2015-04-29 | 北京工业大学 | Autotrophic nitrogen removal method for biological phosphorus removal of urban sewage based on short-cut denitrification for providing nitrite |
| CN106477812A (en) * | 2016-10-28 | 2017-03-08 | 重庆渝桑环保科技有限公司 | Saprobia multiplication denitrifying method |
| CN110615531A (en) * | 2019-09-16 | 2019-12-27 | 北京工业大学 | DEAMOX sludge double-reflux AOAO sewage-based deep nitrogen and phosphorus removal device and method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115745161A (en) * | 2022-11-05 | 2023-03-07 | 北京工业大学 | Device and method for transforming traditional municipal sewage denitrification process based on suspended sludge into pure biomembrane PDA denitrification process |
| CN115745161B (en) * | 2022-11-05 | 2024-04-26 | 北京工业大学 | Device and method for modifying urban sewage denitrification traditional process based on suspended sludge into pure biological membrane PDA denitrification process |
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