CN115571981A - Improved A 2 NSBR double-mud denitrification dephosphorization process method - Google Patents
Improved A 2 NSBR double-mud denitrification dephosphorization process method Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 109
- 230000008569 process Effects 0.000 title claims abstract description 92
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 218
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 109
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 109
- 239000011574 phosphorus Substances 0.000 claims abstract description 109
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- 238000005273 aeration Methods 0.000 claims abstract description 72
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 46
- 239000010865 sewage Substances 0.000 claims abstract description 27
- 229910002651 NO3 Inorganic materials 0.000 claims abstract description 12
- 238000001556 precipitation Methods 0.000 claims abstract description 12
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- 229910019142 PO4 Inorganic materials 0.000 claims abstract description 11
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 42
- 238000003756 stirring Methods 0.000 claims description 28
- 238000004062 sedimentation Methods 0.000 claims description 25
- 230000001546 nitrifying effect Effects 0.000 claims description 24
- 229910052757 nitrogen Inorganic materials 0.000 claims description 21
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- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 10
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
- C02F3/305—Nitrification and denitrification treatment characterised by the denitrification
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/38—Organic compounds containing nitrogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2203/00—Apparatus and plants for the biological treatment of water, waste water or sewage
- C02F2203/006—Apparatus and plants for the biological treatment of water, waste water or sewage details of construction, e.g. specially adapted seals, modules, connections
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/21—Dissolved organic carbon [DOC]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
Improved A 2 A NSBR double-mud denitrification dephosphorization process method belongs to the technical field of urban sewage treatment. The method comprises the following steps of A 2 NSBR Process A 2 The SBR tank is inserted into a low-oxygen phosphorus absorption process after anaerobic phosphorus release, so that the problem that the concentration of nitrate and phosphate in an anoxic section of the tank is not matched is solved; a is to be 2 The phosphorus removal liquid containing ammonia nitrogen after the anoxic denitrification phosphorus removal in the SBR tank is sent to the NSBR tank to undergo secondary nitrification operation, and then the secondary nitrification liquid after the precipitation is sent back to the A tank 2 The SBR tank is subjected to secondary denitrification dephosphorization operation, and finally, water is precipitated after aeration, thereby solving the problem of A 2 The NSBR technology has the problems of high concentration of effluent ammonia nitrogen and unstable operation in the process of treating urban sewage. MiningThe method combines fixed time with on-line parameters based on DO and pH to solve the problem A 2 The operation control problem of the NSBR process system. The process may be A 2 The actual application of the NSBR double-mud denitrifying phosphorus removal process provides technical support.
Description
Technical Field
The invention belongs to the technical field of biological sewage treatment, and particularly relates to an improved A 2 An NSBR double-mud denitrifying phosphorus removal process method. A. The 2 NSBR is anaerobic/anoxic (A) 2 ) Abbreviation of SBR-Nitrification (N) SBR.
Background
The concentration of organic matters in municipal sewage in China is generally low, and the requirement of synchronous nitrogen and phosphorus removal cannot be met, so that the effective removal of nitrogen and phosphorus becomes the bottleneck problem of standard discharge of municipal sewage plants. How to improve the dephosphorization and denitrification effect of the existing sewage treatment process, and research, develop a new economic and efficient dephosphorization and denitrification method and new technology are important problems to be solved urgently and are core problems for realizing the recycling of the advanced sewage treatment.
Denitrifying phosphorus accumulating bacteria can utilize NO 3 - As an electron acceptor, intracellular cohesive beta-hydroxybutyrate (PHB) is an electron donor, and synchronous nitrogen and phosphorus removal is realized in a one-carbon dual-purpose mode, so that two traditional independent processes of denitrification and phosphorus removal are organically combined into a whole, the problems of carbon source competition and sludge age contradiction in the synchronous nitrogen and phosphorus removal process are solved, and the saving of carbon source and oxygen consumption and the reduction of residual sludge are realized.
A 2 The NSBR technology is an earlier double-sludge denitrifying phosphorus and nitrogen removal intermittent flow technology developed by researchers, not only inherits the advantages of the SBR inherent flexibility in operation, lower operating cost and the like, but also introduces a denitrifying phosphorus and nitrogen removal mechanism and a double-sludge concept into the technology, thereby effectively overcoming the defects of urban sewage and industrial waste water in ChinaThe problem of carbon source shortage in the process of water dephosphorization and denitrification is a sewage treatment process with better application prospect.
Laboratory bench test results show that A 2 The NSBR process can obtain good dephosphorization and denitrification effects, but if the process is put into practical production operation, some defects still exist, which mainly show that the ammonia nitrogen concentration of effluent is higher, the stability of the process is easily influenced by water inlet conditions, the anoxic phosphorus uptake rate is not as high as the aerobic phosphorus uptake rate, the operation process control of the system is more complex and the like.
The higher ammonia nitrogen concentration of the effluent is mainly received by A 2 A of NSBR Process 2 The SBR tank is caused by ammonia nitrogen contained in mixed liquor at an anoxic section. Since the sludge index (SVI) of sewage plant activated sludge is generally 80-150mL/g, A 2 The volume exchange ratio of the SBR pool is generally only 50-70 percent, A 2 When the supernatant liquid after phosphorus release is sent to the NSBR tank by the SBR tank, the supernatant liquid is in the A state 2 30-50% of ammonia-containing nitrogen sludge water mixed liquor still remains in SBR pool, and an aeration stripping process is carried out after the pool, but A 2 The SBR tank almost does not contain nitrifying bacteria, and the residual ammonia nitrogen in the tank can only be removed a little through assimilation in the following processes of anoxic denitrification dephosphorization and aeration stripping, so that the concentration of the ammonia nitrogen in the effluent is higher.
Under a certain condition of the organic matter entering water, A 2 The stability of the operation of the NSBR process is mainly determined by A 2 And (4) whether the concentrations of nitrate and phosphate in the mixed liquor of the SBR pool in the anoxic section are matched or not. When the concentration of the nitrate is low, because of insufficient electron acceptors, the denitrification phosphorus absorption is limited, and even secondary ineffective phosphorus release is caused to influence the phosphorus removal effect; on the other hand, if the nitrate in the anoxic zone is excessive, the next period A is affected 2 Phosphorus release of the SBR pool in an anaerobic section and synthesis of PHB in phosphorus accumulating bacteria cells further influence the phosphorus and nitrogen removal effect of the system. It has been reported that the relationship between the consumption of nitrate nitrogen as an electron acceptor and the absorption of phosphate phosphorus in an anoxic environment is (phosphate phosphorus) Absorption of =0.89 (nitrate nitrogen) Consumption of +1.49, i.e. the consumption of nitrate nitrogen is slightly higher than the uptake of phosphate phosphorus in the anoxic zone; also, there are studies that show that the effect is not affectedUnder the condition of anaerobic phosphorus release in the next period, the nitrate nitrogen concentration of the anoxic section has positive correlation with the phosphorus absorption effect.
For conventional municipal sewage, A 2 NSBR Process in A 2 It is difficult to achieve the above-mentioned conditions of matching the nitrogen and phosphorus concentrations during the anoxic period of the SBR tank, and it is common that the amount of nitrate as an electron acceptor is insufficient during the anoxic period. Taking domestic sewage with medium concentration as an example (TN =40mg/L and TP =8 mg/L), assuming sufficient carbon source, A 2 The volume exchange ratio of the SBR tank is 60%, and the nitrogen removal rate by the action of biological assimilation and the like in the reaction process is 12%, under the condition, the nitrogen balance is calculated, and A 2 The NSBR process can provide nitrate nitrogen concentration of only about 15mg/L at the beginning of the anoxic period, and the phosphate phosphorus concentration in the mixed liquor at the beginning of the anoxic period can be generally as high as more than 30 mg/L. Thus, A 2 The NSBR process is generally not able to provide the appropriate electron acceptor nitrate nitrogen for its anoxic period during the treatment of municipal sewage.
On the other hand, although A 2 The NSBR process can realize synchronous nitrogen and phosphorus removal in a one-carbon dual-purpose mode, but the operation management is complex, and the control problem of the operation process needs to be solved in the practical application of the process.
Disclosure of Invention
To give full play to A 2 The invention provides an improved A-type denitrifying phosphorus removal process based on full tests according to the characteristics of the water quality of municipal sewage and the flexible operation mode of an SBR process 2 An NSBR double-sludge denitrifying dephosphatation process method aims to provide technical support for the practical application of the process.
The basic idea of the invention (explained in connection with fig. 1)
(1) A is prepared from 2 A of NSBR Process 2 Anaerobic phosphorus release (A) in SBR pool 1 ) Post-insertion of a low oxygen aeration phosphorus uptake process (O) 1 ) In order to ensure subsequent hypoxia (A) 2 ) The concentration ratio of nitrate nitrogen to phosphate phosphorus in the time interval primary mixed liquid is 1.15-1.3, and the solution A is solved 2 SBR pool is in A 2 Mismatch of nitrate and phosphate concentrations during the time periodThe phosphorus absorption rate of the system can be improved integrally.
The test result shows that the method is in A 2 In the time-interval denitrifying phosphorus removal process, a good synchronous nitrogen and phosphorus removal effect can be obtained, and simultaneously, after phosphorus is removed, the residual small amount of nitrate nitrogen can be removed by denitrifying bacteria by using an internal carbon source in the continuous stirring process, so that the phenomenon of 'secondary ineffective phosphorus release' is avoided.
(2) A is prepared from 2 SBR pool warp A 2 The liquid containing ammonia nitrogen and phosphorus removed after the time-interval denitrification phosphorus removal and precipitation is transferred to an NSBR tank for secondary aeration nitrification operation (O) 3 ) Then the secondary nitrifying liquid is sent into the reactor A after precipitation 2 The SBR tank is operated for secondary denitrification dephosphorization (A) 3 ) Further removing residual nitrate and phosphate in the mixed solution by using the residual PHB in the polyphosphate accumulating bacteria cells in the pool, and finally aerating (O) 4 ) The COD, ammonia nitrogen, TN and TP of the effluent of the system reach the standard.
(3) The solution A is realized by combining fixed time with on-line parameters based on Dissolved Oxygen (DO) and pH 2 The operation control problem of the NSBR process system.
The improved type A of the invention 2 The NSBR double-mud denitrification dephosphorization process system has the following characteristics (with the description of the attached figure 2)
The system comprises an AOASBR pool 1, an NSBR pool 2, a raw water tank 3, an intermediate water tank 4, an intermediate water tank 5, an intermediate water tank 6, an intermediate water tank 7, a data processor 8 and a process controller 9;
the AOASBR tank 1 is connected with a raw water inlet pipe 10, an ammonia nitrogen and phosphorus-containing liquid outlet pipe 11, a phosphorus-containing nitrifying liquid return pipe 12, an ammonia nitrogen and phosphorus-containing liquid outlet pipe 13, a secondary nitrifying liquid return pipe 14, a drain pipe 15 and a sludge discharge pipe 16; a water inlet pump 17 and a valve 18 are arranged on the raw water inlet pipe 10, and the upstream end of the water inlet pump 17 is connected with the raw water tank 3; a valve 19 is arranged on the ammonia nitrogen and phosphorus containing liquid outlet pipe 11, and the downstream end of the ammonia nitrogen and phosphorus containing liquid outlet pipe 11 is connected with the intermediate water tank 4; the phosphorus-containing nitrifying liquid return pipe 12 is provided with a water inlet pump 20 and a valve 21, and the upstream end of the water inlet pump 20 is connected with the intermediate water tank 5; a valve 22 is arranged on the water outlet pipe 13 containing the ammonia nitrogen dephosphorization liquid, and the downstream end of the water outlet pipe 13 containing the ammonia nitrogen dephosphorization liquid is connected with the intermediate water tank 6; a water inlet pump 23 and a valve 24 are arranged on the secondary nitrification liquid return pipe 14, and the upstream end of the water inlet pump 23 is connected with the intermediate water tank 7; the drain pipe 15 and the sludge discharge pipe 16 are respectively provided with a valve 25 and a valve 26;
the NSBR tank 2 is connected with an ammonia nitrogen containing phosphorus release liquid inlet pipe 27, a phosphorus containing nitrifying liquid outlet pipe 28, an ammonia nitrogen containing phosphorus removal liquid inlet pipe 29, a secondary nitrifying liquid outlet pipe 30 and a sludge discharge pipe 31; a water inlet pump 32 and a valve 33 are arranged on the ammonia nitrogen and phosphorus releasing liquid inlet pipe 27, and the upstream end of the water inlet pump 32 is connected with the intermediate water tank 4; a valve 34 is arranged on the phosphorus-containing nitrifying liquid outlet pipe 28, and the downstream end of the phosphorus-containing nitrifying liquid outlet pipe 28 is connected with the middle water tank 5; a water inlet pump 35 and a valve 36 are arranged on the water inlet pipe 29 of the ammonia nitrogen phosphorus removal liquid, and the upstream end of the water inlet pump 35 is connected with the intermediate water tank 6; a valve 37 is arranged on the secondary nitrifying liquid outlet pipe 30, and the downstream end of the secondary nitrifying liquid outlet pipe 30 is connected with the intermediate water tank 7; a valve 38 is arranged on the sludge discharge pipe 31;
the data processor 8 is provided with a signal input end 39, a parameter setting and displaying end 40 and a signal output end 41; the signal output end 41 is connected with the process controller 9;
the AOASBR tank 1 and the NSBR tank 2 are respectively provided with aeration heads 42 and 43, pH sensors 44 and 45 and DO sensors 46 and 47, and the AOASBR tank 1 is also provided with a stirrer 48; the aeration heads 42 and 43 are respectively connected with air blowers 51 and 52 through valves 49 and 50, the pH sensors 44 and 45 and the DO sensors 46 and 47 are respectively connected with pH- DO instruments 53 and 54, and the pH- DO instruments 53 and 54 are respectively connected with a signal input end 39;
the process controller 9 is provided with all the water inlet pumps (17, 20, 23, 32, 35), all the valves (18, 19, 21, 22, 24, 25, 26, 33, 34, 36, 37, 38, 49, 50), the stirrer 48, all the relays 55 of the blowers (51, 52) and a control signal output end 56; the control signal output 56 is connected to all of the aforementioned water pumps (17, 20, 23, 32, 35), all of the aforementioned valves (18, 19, 21, 22, 24, 25, 26, 33, 34, 36, 37, 38, 49, 50), the agitator 48, and all of the aforementioned blowers (51, 52) via a control bus 57.
The modified form A 2 Starting and operating process of NSBR double-mud denitrification dephosphorization process system (with reference to figure 2)
1. Startup of system
Adding sludge with denitrification dephosphorization activity into the AOASBR tank 1, discharging sludge according to the actual operation condition of the AOASBR tank 1, and maintaining the sludge concentration of 3200-3600mg/L and the sludge age of 13-16d; adding sludge with nitrification activity into an NSBR tank 2, discharging sludge according to the actual operation condition of the NSBR tank 2, maintaining the sludge concentration of 3600-4200mg/L and the sludge age of 25-35d, and operating according to the following mode after a system is stable;
2. running operation process of one processing cycle of system
(1) Operational procedure for AOASBR pool 1
(1) Filling water: starting a water inlet pump 17, opening a valve 18, pumping domestic sewage from a raw water tank 3 into an AOASBR tank 1, taking the water filling ratio to be 0.6-0.7, and closing the valve 18 and the water inlet pump 17 after the water filling is finished;
②A 1 time interval anaerobic phosphorus release operation: starting the water inlet pump 17 and the valve 18, and simultaneously starting the stirrer 48 to carry out A 1 Performing anaerobic phosphorus release operation in a time period, taking the stirring time to be 60-120min according to the operation result, and closing the stirrer 48 after the stirring time is up;
③O 1 and (3) aeration operation in a time interval: after the stirrer 48 was turned off, the blower 51 was started, the valve 49 was opened, and O was performed 1 Performing aeration operation in a time interval, controlling the DO concentration in the AOASBR tank 1 to be 0.4-0.8mg/L, taking aeration time for 10-30min according to an operation result, and closing a valve 49 and an air blower 51 after aeration is finished;
(4) precipitating and transferring the ammonia nitrogen-containing phosphorus-releasing liquid: after the valve 49 and the blower 51 are closed, the AOASBR tank 1 enters a sludge-water separation settling state, the settling time is 30-60min, after the settling time is up, the valve 19 is opened, the ammonia nitrogen-containing phosphorus-releasing liquid is discharged into the intermediate water tank 4, the discharge ratio is 0.6-0.7, and after the discharge is finished, the valve 19 is closed;
⑤A 2 time-interval denitrification dephosphorization operation: after valve 19 is closed, intake pump 20 is started, valve 21 is opened, and NSBR tank 2 is drained in the previous cyclePumping phosphorus-containing nitrifying liquid in the intermediate water tank 5 into the AOASBR tank 1, taking the water filling ratio of 0.6-0.7, closing the valve 21 and the water inlet pump 20 after the water filling is finished, starting the stirrer 48 at the same time, and carrying out A 2 Denitrifying phosphorus removal operation is carried out in a time period;
⑥A 2 on-line control of the time interval running process: in A 2 In the stirring operation process of the time period, the change process of the pH parameter of the pH-DO instrument 53 is monitored on line, when the monitored pH parameter is changed from stable rising to stable falling, the first derivative of the pH value to the time is changed from stable being larger than zero to stable being smaller than zero, and the stirring time is not less than 80min, the stirrer 48 is closed;
the stable rising and the stable falling of the pH parameter mean that the continuous rising time of the pH is not less than 30min before the pH parameter is changed from rising to falling, and the continuous falling time of the pH is not less than 3min after the pH parameter is changed from rising to falling;
(7) precipitating and transferring the phosphorus removal liquid containing ammonia nitrogen: after the stirrer 48 is closed, the AOASBR tank 1 enters a sludge-water separation precipitation state, the precipitation time is 30-60min, after the precipitation time is up, the valve 22 is opened, the ammonia nitrogen-containing phosphorus removal liquid is discharged into the middle water tank 6, the water discharge ratio is 0.6-0.7, and after the water discharge is finished, the valve 22 is closed;
⑧A 3 and (3) performing secondary denitrification dephosphorization operation in a time period: after the valve 22 is closed, the water inlet pump 23 is started, the valve 24 is opened, the secondary nitrified liquid discharged into the intermediate water tank 7 from the NSBR tank 2 in the previous period is pumped into the AOASBR tank 1, the water filling ratio is 0.6-0.7, after the water filling is finished, the valve 24 and the water inlet pump 23 are closed, and the stirrer 48 is started at the same time to carry out A 3 Carrying out secondary denitrification dephosphorization operation in a time period, further removing residual nitrate and phosphate in the mixed liquor by utilizing the residual PHB in the phosphorus-accumulating bacteria cells, taking the stirring time for 20-40min, and closing the stirrer 48 after the stirring time is up;
⑨O 4 aeration operation in the period: after the stirrer 48 was turned off, the blower 51 was started, the valve 49 was opened, and O was performed 4 Performing aeration operation in a time interval, wherein the aeration time is 20-30min, blowing off nitrogen attached to sludge flocs and further removing residual phosphate in the AOASBR tank 1, and closing a valve 49 and an air blower 51 after the aeration is finished;
r deposits, drainage, mud discharging, the system is idle: after the valve 49 and the blower 51 are closed, the AOASBR tank 1 enters a sludge-water separation sedimentation state, the sedimentation time is 30-60min, after the sedimentation time is up, the valve 25 is opened to drain water, the water drainage ratio is 0.6-0.7, and the valve 26 is opened to drain sludge at the same time, so that the sludge age is controlled to be 13-16d; after the drainage and sludge discharge are completed, the valves 25 and 26 are closed, the AOASBR tank 1 enters an idle state, and after the idle time is up, the AOASBR tank 1 enters the next period for operation.
(2) Operational procedure for NSBR pool 2
(1) Filling water: after the operation process (4) of the AOASBR tank 1 is finished, starting a water inlet pump 32, opening a valve 33, pumping the ammonia nitrogen-containing phosphorus-releasing liquid in the intermediate water tank 4 into the NSBR tank 2, wherein the water filling ratio is 0.6-0.7, and after the water filling is finished, closing the valve 33 and the water inlet pump 32;
②O 2 the interval aeration nitration operation and the on-line control thereof are as follows: after the valve 33 and the water inlet pump 32 are closed, the blower 52 is started, the valve 50 is opened, and O is carried out 2 And (3) aeration nitrification operation in a time interval, wherein in the operation process, the DO concentration in the NSBR pool 2 is controlled to be 1.5-2.5mg/L, the change process of pH and DO parameters of the pH-DO instrument 54 is monitored on line, when the monitored pH parameter is changed from stable decline to stable rise, the first derivative of the pH to the time is changed from stable less than zero to stable crossing zero to stable more than zero, the DO parameter is rapidly increased greatly, and when the aeration time is not less than 70min, the valve 50 and the blower 52 are closed, and the O is ended 2 Aeration and nitrification operation in time intervals;
the stable decrease and the stable increase of the pH parameter mean that the time for the pH to continuously decrease is not less than 30min before the pH parameter is changed from decrease to increase, and the time for the pH parameter to continuously increase is not less than 3min after the pH parameter is changed from decrease to increase;
(3) precipitating and transferring phosphorus-containing nitrifying liquid: after the valve 50 and the blower 52 are closed, the NSBR tank 2 enters a sludge-water separation sedimentation state, the sedimentation time is 30-60min, after the sedimentation time is up, the valve 34 is opened, the phosphorus-containing nitrifying liquid is discharged into the intermediate water tank 5, the water discharge ratio is 0.6-0.7, and after the water discharge is finished, the valve 34 is closed;
(4) water filling: after the valve 34 is closed, the water inlet pump 35 is started, the valve 36 is opened, the ammonia nitrogen and phosphorus removal liquid in the intermediate water tank 6 is pumped into the NSBR tank 2, the water filling ratio is 0.6-0.7, and after the water filling is finished, the valve 36 and the water inlet pump 35 are closed;
⑤O 3 and (3) time interval secondary aeration nitration operation: after the valve 36 and the water inlet pump 35 are closed, the blower 52 is started, the valve 50 is opened, and O is carried out 3 Performing secondary aeration and nitrification operation in a time interval, controlling the DO concentration in the NSBR pool 2 to be 1.5-2.5mg/L in the operation process, taking the aeration time to be 20-35min according to the operation result, and closing the valve 50 and the air blower 52 after the aeration is finished;
(6) deposit, drainage, row's mud, the system is idle: after the valve 50 and the blower 52 are closed, the NSBR tank 2 enters a sludge-water separation sedimentation state, the sedimentation time is 30-60min, after the sedimentation time is up, the valve 37 is opened, the secondary nitrified liquid is discharged into the intermediate water tank 7, the water discharge ratio is 0.6-0.7, meanwhile, the valve 38 is opened as required to discharge sludge, and the sludge age is controlled to be 25-35d; after the drainage and sludge discharge are completed, valves 37 and 38 are closed, the NSBR tank 2 enters an idle state, and after the idle time is up, the NSBR tank 2 enters the next cycle for operation.
Improved A 2 The NSBR double-sludge denitrification dephosphorization process system operates in a reciprocating mode in a period, and carbon, nitrogen and phosphorus in the domestic sewage are synchronously removed.
The AOASBR tank 1 and the NSBR tank 2 run each operation process, including the opening and closing of the water inlet pumps and valves, the opening and closing of the aeration and stirring processes, and the opening and closing of the water filling and draining processes, and are controlled in real time by sending instructions from the process controller 9 according to a control strategy; the water filling and draining ratio, the stirring time, the aeration time, and the change characteristic values of the stirring and aeration process control parameters DO and pH of the AOASBR tank 1 and the NSBR tank 2 are set and modified through a parameter setting and displaying end 40 of the data processor 8 according to the running condition of the system.
The invention has the advantages of
The invention provides an improved type A 2 The NSBR double-sludge denitrification dephosphorization process for treating the municipal sewage has the following advantages:
(1) Under the condition that the inlet water meets the requirement of a carbon source, the outlet water of the systemThe water quality can stably reach the first grade A standard of the discharge standard GB18918-2002 for pollutants of urban sewage treatment plants, and the problem of A is solved 2 The problem that the ammonia nitrogen content of the effluent of the NSBR process exceeds the standard is solved, and meanwhile, the dephosphorization rate of the system is integrally improved due to the fact that an aeration phosphorus absorption process exists in the AOASBR tank;
(2) Improves the stability of system operation and avoids A 2 In the anoxic denitrification dephosphorization stage, the NSBR process has the problems of affecting the phosphorus absorption effect and generating 'secondary ineffective phosphorus release' due to insufficient electron acceptor-nitrate;
(3) The method of combining fixed time with on-line parameters based on DO and pH solves the problem of operation control of the system.
(4) The modification A 2 The NSBR double-sludge denitrification dephosphorization process can realize the conventional A through simple operation mode change and the optimization of a control system 2 And upgrading and modifying the NSBR process system.
Drawings
FIG. 1 shows a modification A of the present invention 2 The NSBR double-sludge denitrifying dephosphatation process has an operation mode of one treatment period.
In fig. 1, the operation mode of the NSBR pool is inside the virtual frame, and the operation mode of the AOASBR pool is outside the virtual frame.
FIG. 2 shows a modification A of the present invention 2 The structure schematic diagram of the NSBR double-sludge denitrifying phosphorus removal process.
In fig. 2: 1-AOASBR pool, 2-NSBR pool, 3-raw water tank, 3-7 middle water tank, 8-data processor, 9-process controller, 10-raw water inlet pipe, 11-discharge pipe of phosphorus-containing nitrogen-releasing liquid, 12-return pipe of phosphorus-containing nitrifying liquid, 13-discharge pipe of phosphorus-releasing liquid containing nitrogen, 14-return pipe of secondary nitrifying liquid, 15-discharge pipe, 16-sludge discharge pipe, 17-inlet pump, 18-19-valve, 20-inlet pump, 21-22-valve, 23-inlet pump, 24-26-valve, 27-inlet pipe of phosphorus-releasing liquid containing nitrogen, 28-outlet pipe of phosphorus-containing nitrifying liquid, 29-inlet pipe of phosphorus-releasing liquid containing nitrogen, 30-outlet pipe of secondary nitrifying liquid, 31-sludge discharge pipe, 32-inlet pump, 33-34-valve, 35-inlet pump, 36-38-valve, 39-signal input end, 40-parameter setting and display end, 41-signal output end, 42-43-head, 44-45-pH sensor, 46-47-DO sensor, 48-DO-50-DO-54-relay, 49-53-55-aeration control relay, and aeration control relay.
Detailed Description
As shown in fig. 2, the modified form A 2 The NSBR double-mud denitrifying phosphorus removal process system consists of an AOASBR tank 1, an NSBR tank 2, a raw water tank 3, an intermediate water tank 4, an intermediate water tank 5, an intermediate water tank 6, an intermediate water tank 7, a data processor 8 and a process controller 9.
The connection of the units 1-9 is shown in fig. 2.
The modified form A 2 The working flow of one treatment period of the NSBR double-sludge denitrifying phosphorus removal process system is as follows:
pumping domestic sewage from a raw water tank 3 into an AOASBR tank 1, and treating the domestic sewage by a treatment process A 1 After the time interval anaerobic phosphorus release operation, O is carried out 1 The low-oxygen aeration operation in the time interval aims at absorbing and removing proper amount of phosphorus and realizing the follow-up A 2 The concentration ratio of nitrate nitrogen to phosphate phosphorus in the time period primary mixed liquid is 1.15-1.3, and O is determined according to the actual operation condition of the AOASBR tank 1 1 Aeration time of the session; after the aeration is stopped, discharging the ammonia nitrogen and phosphorus containing liquid into the intermediate water tank 4 through static sedimentation, simultaneously pumping the phosphorus containing nitrifying liquid discharged into the intermediate water tank 5 from the NSBR tank 2 in the previous period into the AOASBR tank 1, and carrying out A 2 The anoxic stirring denitrification dephosphorization operation is carried out in a time period; after stirring is stopped, the phosphorus removal liquid containing ammonia nitrogen is discharged into an intermediate water tank 6 through static sedimentation, and simultaneously, the secondary nitrifying liquid discharged into an intermediate water tank 7 in the previous period in the NSBR tank 2 is pumped into the AOASBR tank 1 for A 3 The secondary anoxic stirring denitrification dephosphorization operation in time interval utilizes the PHB remained in the polyphosphate accumulating bacteria cells in the pool to further remove the remained nitrate and phosphate in the mixed liquor, and finally passes through O 4 And (4) aeration operation is carried out at a time interval, so that COD, ammonia nitrogen, TN and TP of system effluent reach the standard.
For the NSBR pool 2, pumping the phosphorus release liquid containing ammonia nitrogen into the NSBR pool 2 from the intermediate water tank 4 for O 2 Aeration and nitrification operation in a time interval; after stopping the aeration and nitrification operation, discharging the phosphorus-containing nitrified liquid into the intermediate water tank 5 through static sedimentation, and then discharging the phosphorus-containing nitrified liquid into the intermediate water tankPumping the ammonia nitrogen-containing phosphorus removal liquid in the intermediate water tank 6 into an NSBR pool 2 for O 3 The secondary aeration nitration operation in the time interval realizes the oxidation of ammonia nitrogen in the phosphorus removal liquid containing ammonia nitrogen; o is 3 After the time-interval aeration nitrification operation is finished, the NSBR tank 2 discharges the secondary nitrification liquid into the intermediate water tank 7 after the static sedimentation, and the operation of one treatment period of the NSBR tank 2 is finished.
The following embodiments are described in connection with application examples:
the example was carried out under laboratory conditions using simulated domestic sewage based on NaAc and soluble starch as the main ingredients, plus a small amount of beef extract and nutrient salts, using NaHCO 3 Adjusting alkalinity and pH value, and adopting NH as ammonia nitrogen and phosphate phosphorus in water 4 Cl and KH 2 PO 4 The mixing is carried out, the organic matters of the simulated sewage are equivalent to the domestic sewage with medium and slightly low concentration, and the change range of the main water quality index during the test period is shown in the following table.
Simulating the water quality characteristics of domestic sewage
The test system is shown in figure 2, the AOASBR tank 1 and the NSBR tank 2 are the same and are made of organic glass, the height is 55cm, the inner diameter is 19cm, the bottom is in a circular truncated cone shape, and the total effective volume is 12L.
The system operation is described in conjunction with fig. 2:
1. startup of system
In the test process, the system is started according to the mode of the invention, and the sludge concentration of the AOASBR tank 1 is 3400mg/L, NSBR and the sludge concentration of the AOASBR tank 2 is 4000mg/L after the system runs stably.
2. Running operation process of one processing cycle of system
(1) Operational procedure for AOASBR pool 1
(1) Filling water: starting a water inlet pump 17, opening a valve 18, pumping domestic sewage into the AOASBR tank 1 from the raw water tank 3, taking the water filling ratio to be 0.67, and closing the valve 18 and the water inlet pump 17 after the water filling is finished;
②A 1 time interval anaerobic phosphorus release operation: starting the water inlet pump 17 and the valve 18, and simultaneously starting the stirrer 48 to carry out A 1 Performing anaerobic phosphorus release operation in a time period, taking the stirring time to be 90min according to the operation result, and closing the stirrer 48 after the stirring time is up;
③O 1 and (3) time interval aeration operation: after the stirrer 48 was turned off, the blower 51 was started, the valve 49 was opened, and O was performed 1 Performing aeration operation in a time interval, controlling the DO concentration in the AOASBR tank 1 to be 0.4-0.8mg/L, taking the aeration time to be 10-30min according to the operation result, and closing a valve 49 and an air blower 51 after the aeration is finished;
(4) precipitating and transferring the ammonia nitrogen-containing phosphorus-releasing liquid: after the valve 49 and the blower 51 are closed, the AOASBR tank 1 enters a sludge-water separation settling state, the settling time is 40min, after the settling time is up, the valve 19 is opened, the ammonia nitrogen-containing phosphorus-releasing liquid is discharged into the intermediate water tank 4, the water discharge ratio is 0.67, and after the water discharge is finished, the valve 19 is closed;
⑤A 2 time-interval denitrification dephosphorization operation: after the valve 19 is closed, the water inlet pump 20 is started, the valve 21 is opened, the phosphorus-containing nitrified liquid discharged into the intermediate water tank 5 in the last period of the NSBR tank 2 is pumped into the AOASBR tank 1, the water filling ratio is 0.67, after the water filling is finished, the valve 21 and the water inlet pump 20 are closed, the stirrer 48 is started at the same time, and A is carried out 2 Denitrifying phosphorus removal operation is carried out in a time period;
⑥A 2 on-line control of the time interval running process: in A 2 In the stirring operation process of the time period, the change process of the pH parameter of the pH-DO instrument 53 is monitored on line, when the monitored pH parameter is changed from stable rising to stable falling, the first derivative of the pH to the time is changed from stable being larger than zero to crossing over the zero point to stable being smaller than zero, and the stirring time is not less than 80min, the stirrer 48 is closed;
the stable rising and the stable falling of the pH parameter mean that the continuous rising time of the pH is not less than 30min before the pH parameter is changed from rising to falling, and the continuous falling time of the pH is not less than 3min after the pH parameter is changed from rising to falling;
(7) precipitating and transferring the ammonia nitrogen-containing phosphorus removal liquid: after the stirrer 48 is closed, the AOASBR tank 1 enters a sludge-water separation precipitation state, the precipitation time is 40min, after the precipitation time is up, the valve 22 is opened, the ammonia nitrogen-containing phosphorus removal liquid is discharged into the intermediate water tank 6, the water discharge ratio is 0.67, and after the water discharge is finished, the valve 22 is closed;
⑧A 3 and (3) performing secondary denitrification dephosphorization operation in a time period: after the valve 22 is closed, the water inlet pump 23 is started, the valve 24 is opened, the secondary nitrified liquid discharged into the intermediate water tank 7 from the NSBR tank 2 in the previous period is pumped into the AOASBR tank 1, the water filling ratio is 0.67, after the water filling is finished, the valve 24 and the water inlet pump 23 are closed, the stirrer 48 is started at the same time, and A is carried out 3 Performing secondary denitrification dephosphorization operation in a time period, further removing residual nitrate and phosphate in the mixed liquor by utilizing the residual PHB in the polyphosphate accumulating bacteria cells, stirring for 35min, and closing a stirrer 48 after the stirring time is up;
⑨O 4 aeration operation in a time period: after the stirrer 48 was turned off, the blower 51 was started, the valve 49 was opened, and O was performed 4 Performing aeration operation in a time interval, wherein the aeration time is 25min, blowing off nitrogen attached to sludge flocs and further removing residual phosphate in the AOASBR tank 1, and closing a valve 49 and an air blower 51 after the aeration is finished;
r deposits, drainage, mud discharging, the system is idle: after the valve 49 and the blower 51 are closed, the AOASBR tank 1 enters a sludge-water separation sedimentation state, the sedimentation time is 40min, after the sedimentation time is up, the valve 25 is opened to drain water, the water drainage ratio is 0.67, and simultaneously the valve 26 is opened to drain sludge, so that the sludge age is controlled to be 13-16d; after the drainage and sludge discharge are completed, the valves 25 and 26 are closed, the AOASBR tank 1 enters an idle state, and after the idle time is up, the AOASBR tank 1 enters the next period for operation.
(2) Operational procedure for NSBR pool 2
(1) Filling water: after the operation process (4) of the AOASBR tank 1 is finished, starting the water inlet pump 32, opening the valve 33, pumping the ammonia nitrogen and phosphorus containing release liquid in the intermediate water tank 4 into the NSBR tank 2, taking the water filling ratio to be 0.67, and after the water filling is finished, closing the valve 33 and the water inlet pump 32;
②O 2 the time interval aeration nitration operation and the on-line control thereof are as follows: after the water filling is finished, the blower 52 is started, the valve 50 is opened, and O is carried out 2 Aeration and nitration operation in a time interval, and DO concentration in the NSBR tank 2 is controlled in the operation processThe temperature is 1.5-2.5mg/L, the change process of the pH and DO parameters of the pH-DO instrument 54 is monitored on line, when the monitored pH parameter is changed from stable decline to stable rise, the first derivative of the pH to the time is changed from stable less than zero to stable more than zero when crossing the zero point, the DO parameter is rapidly increased greatly, and the aeration time is not less than 70min, the valve 50 and the blower 52 are closed, and the O-flow is ended 2 Aeration and nitrification operation in a time interval;
the stable decrease and the stable increase of the pH parameter mean that the time for the pH to continuously decrease is not less than 30min before the pH parameter is changed from decrease to increase, and the time for the pH parameter to continuously increase is not less than 3min after the pH parameter is changed from decrease to increase;
(3) precipitating and transferring phosphorus-containing nitrifying liquid: after the valve 50 and the blower 52 are closed, the NSBR tank 2 enters a sludge-water separation sedimentation state, the sedimentation time is 40min, after the sedimentation time is up, the valve 34 is opened, the phosphorus-containing nitrifying liquid is discharged into the intermediate water tank 5, the water discharge ratio is 0.67, and after the water discharge is finished, the valve 34 is closed;
(4) filling water: after the valve 34 is closed, the water inlet pump 35 is started, the valve 36 is opened, the ammonia nitrogen and phosphorus removal liquid in the intermediate water tank 6 is pumped into the NSBR tank 2, the water filling ratio is 0.67, and after the water filling is finished, the valve 36 and the water inlet pump 35 are closed;
⑤O 3 and (3) time interval secondary aeration nitration operation: after the valve 36 and the water inlet pump 35 are closed, the blower 52 is started, the valve 50 is opened, and O is carried out 3 Performing secondary aeration and nitrification operation in a time interval, controlling the DO concentration in the NSBR pool 2 to be 1.5-2.5mg/L in the operation process, taking the aeration time for 30min according to the operation result, and closing the valve 50 and the air blower 52 after the aeration is finished;
(6) deposit, drainage, row's mud, the system is idle: after the valve 50 and the blower 52 are closed, the NSBR tank 2 enters a sludge-water separation sedimentation state, the sedimentation time is 40min, after the sedimentation time is up, the valve 37 is opened, the secondary nitrified liquid is discharged into the intermediate water tank 7, the water discharge ratio is 0.67, meanwhile, the valve 38 is opened as required to discharge sludge, and the sludge age is controlled to be 25-35d; after the drainage and sludge discharge are completed, valves 37 and 38 are closed, the NSBR tank 2 enters an idle state, and after the idle time is up, the NSBR tank 2 enters the next cycle for operation.
The test result shows that: after the operation is stable, COD of the final effluent of the system is less than 20mg/L, ammonia nitrogen is less than 4mg/L, nitrate nitrogen is less than 2mg/L, TN is less than 6mg/L, and TP is less than 0.5mg/L, thereby achieving the first-class A emission standard of the pollutant emission standard GB18918-2002 of urban sewage treatment plants.
The foregoing is a further description of the invention with reference to specific test embodiments for the purpose of facilitating a person skilled in the art to better understand and apply the invention, and the detailed description of the invention should not be considered as being limited to these descriptions, so that simple modifications made by a person skilled in the art are within the scope of the invention.
Claims (1)
1. Improved generation A 2 The NSBR double-mud denitrification dephosphorization process method is characterized by comprising the following steps:
the process method is performed with a system comprising an AOASBR tank (1), an NSBR tank (2), a raw water tank (3), a first intermediate water tank (4), a second intermediate water tank (5), a third intermediate water tank (6), a fourth intermediate water tank (7), a data processor (8) and a process controller (9);
the starting of the system:
adding sludge with denitrifying phosphorus removal activity into the AOASBR tank (1), discharging sludge according to the actual operation condition of the AOASBR tank (1), maintaining the sludge concentration to be 3200-3600mg/L and the sludge age to be 13-16d, adding sludge with denitrifying activity into the NSBR tank (2), discharging sludge according to the actual operation condition of the NSBR tank (2), maintaining the sludge concentration to be 3600-4200mg/L and the sludge age to be 25-35d, and operating according to the following mode after the system is stabilized;
the running operation process of the system in one processing cycle comprises the following steps:
1) Operational process of the AOASBR pool (1)
(1) Filling water: starting a first water inlet pump (17) of the system, opening a first valve (18) of the system, pumping domestic sewage from the raw water tank (3) into the AOASBR tank (1), wherein the water filling ratio is 0.6-0.7, and closing the first valve (18) and the first water inlet pump (17) after the water filling is finished;
②A 1 time interval anaerobic phosphorus release operation: starting the stirrer (48) of the system to carry out A while starting the first water inlet pump (17) and opening the first valve (18) 1 Anaerobic phosphorus release operation in a time interval, taking the stirring time to be 60-120min according to the operation result, and closing the stirrer (48) after the stirring time is up;
③O 1 and (3) time interval aeration operation: after the stirrer (48) is closed, a first air blower (51) of the system is started, a second valve (49) of the system is opened, and O is carried out 1 Performing time interval aeration operation, controlling the DO concentration in the AOASBR tank (1) to be 0.4-0.8mg/L, taking the aeration time to be 10-30min according to the operation result, and closing the second valve (49) and the first air blower (51) after the aeration is finished;
(4) precipitating and transferring the ammonia nitrogen-containing phosphorus-releasing liquid: after the second valve (49) and the first air blower (51) are closed, the AOASBR tank (1) enters a sludge-water separation settling state, the settling time is 30-60min, after the settling time is up, a third valve (19) of the system is opened, the ammonia nitrogen-containing phosphorus-releasing liquid is discharged into the first intermediate water tank (4), the discharge water ratio is 0.6-0.7, and after the discharge water is finished, the third valve (19) is closed;
⑤A 2 time-interval denitrification dephosphorization operation: after the third valve (19) is closed, a second water inlet pump (20) of the system is started, a fourth valve (21) of the system is opened, the phosphorus-containing nitrified liquid discharged into the second intermediate water tank (5) in the last period of the NSBR tank (2) is pumped into the AOASBR tank (1), the water filling ratio is 0.6-0.7, after the water filling is finished, the fourth valve (21) and the second water inlet pump (20) are closed, the stirrer (48) is started at the same time, and A is carried out 2 Denitrifying phosphorus removal operation is carried out in a time period;
⑥A 2 on-line control of the time-interval running process: in A 2 During the stirring operation of the time interval, monitoring the change process of the pH parameter of a first pH-DO instrument (53) of the system on line, and when the monitored pH parameter is changed from stable rising to stable falling, the first derivative of the pH value to the time is changed from stable being larger than zero to stable crossing zero to stable being smaller than zero, and the stirring time is not less than 80min, closing the stirrer (48);
the stable rising and the stable falling of the pH parameter mean that the continuous rising time of the pH is not less than 30min before the pH parameter is changed from rising to falling, and the continuous falling time of the pH is not less than 3min after the pH parameter is changed from rising to falling;
(7) precipitating and transferring the ammonia nitrogen-containing phosphorus removal liquid: after the stirrer (48) is closed, the AOASBR tank 1 enters a sludge-water separation precipitation state, the precipitation time is 30-60min, after the precipitation time is up, a fifth valve (22) of the system is opened, the ammonia nitrogen-containing phosphorus removal liquid is discharged into the third intermediate water tank (6), the water discharge ratio is 0.6-0.7, and after the water discharge is finished, the fifth valve (22) is closed;
⑧A 3 and (3) performing secondary denitrification dephosphorization operation in a time period: after the fifth valve (22) is closed, a third water inlet pump (23) of the system is started, a sixth valve (24) of the system is opened, secondary nitrified liquid discharged into an intermediate water tank 7 in the last period of the NSBR tank 2 is pumped into the AOASBR tank 1, the water filling ratio is 0.6-0.7, after the water filling is finished, the sixth valve (24) and the third water inlet pump (23) are closed, the stirrer (48) is started at the same time, and A is carried out 3 Performing secondary denitrification dephosphorization operation in time intervals, further removing residual nitrate and phosphate in the mixed liquor by utilizing the residual PHB in the phosphorus-accumulating bacteria cells, taking the stirring time for 20-40min, and closing the stirrer (48) after the stirring time is up;
⑨O 4 aeration operation in the period: after the stirrer (48) is closed, the first air blower (51) is started, the second valve (49) is opened, and O is carried out 4 Performing aeration operation in a time interval, wherein the aeration time is 20-30min, blowing off nitrogen attached to sludge flocs and further removing residual phosphate in the AOASBR tank (1), and closing the second valve (49) and the first air blower (51) after the aeration is finished;
r deposits, drainage, mud discharging, the system is idle: after the second valve (49) and the first air blower (51) are closed, the AOASBR tank (1) enters a sludge-water separation sedimentation state, the sedimentation time is 30-60min, after the sedimentation time is up, a seventh valve (25) of the system is opened to drain water, the water drainage ratio is 0.6-0.7, an eighth valve (26) of the system is opened to drain sludge, and the sludge age is controlled to be 13-16d; after the water and mud discharging is finished, the seventh valve (25) and the eighth valve (26) are closed, the AOASBR tank (1) enters an idle state, and after the idle time is up, the AOASBR tank (1) enters the next period for operation;
2) The operation process of the NSBR pool (2)
(1) Filling water: after the operation process (4) of the AOASBR tank (1) is finished, starting a fourth water inlet pump (32) of the system, opening a ninth valve (33) of the system, pumping the ammonia nitrogen-containing phosphorus-releasing liquid in the first intermediate water tank (4) into the NSBR tank (2), taking the water filling ratio of 0.6-0.7, and closing the ninth valve (33) and the fourth water inlet pump (32) after the water filling is finished;
②O 2 the time interval aeration nitration operation and the on-line control thereof are as follows: after the ninth valve (33) and the fourth water inlet pump (32) are closed, a second air blower (52) of the system is started, a tenth valve (50) of the system is opened, and O is carried out 2 And (2) performing aeration nitrification operation in a time interval, controlling the DO concentration in the NSBR pool (2) to be 1.5-2.5mg/L in the operation process, simultaneously monitoring the change process of pH and DO parameters of a second pH-DO instrument (54) of the system on line, when the pH parameter is monitored to be changed from stable reduction to stable rise, the first derivative of the pH to the time is changed from stable less than zero to stable more than zero when crossing a zero point, simultaneously the DO parameter is greatly and rapidly increased, and the aeration time is not less than 70min, closing the tenth valve (50) and the second air blower (52), and ending the O 2 Aeration and nitrification operation in time intervals;
the stable decrease and the stable increase of the pH parameter mean that the time for the pH to continuously decrease is not less than 30min before the pH parameter is changed from decrease to increase, and the time for the pH parameter to continuously increase is not less than 3min after the pH parameter is changed from decrease to increase;
(3) precipitating and transferring phosphorus-containing nitrifying liquid: after the tenth valve (50) and the second air blower (52) are closed, the NSBR tank (2) enters a sludge-water separation settling state, the settling time is 30-60min, after the settling time is up, an eleventh valve (34) of the system is opened, the phosphorus-containing nitrifying liquid is discharged into the second intermediate water tank (5), the water discharge ratio is 0.6-0.7, and after the water discharge is finished, the eleventh valve (34) is closed;
(4) filling water: after the eleventh valve (34) is closed, a fifth water inlet pump (35) of the system is started, a twelfth valve (36) of the system is opened, the ammonia nitrogen-containing phosphorus removal liquid in the third intermediate water tank (6) is pumped into the NSBR tank (2), the water filling ratio is 0.6-0.7, and after the water filling is finished, the twelfth valve (36) and the fifth water inlet pump (35) are closed;
⑤O 3 and (3) time interval secondary aeration nitration operation: after the twelfth valve (36) and the fifth water inlet pump (35) are closed, the second blower (52) is started, the tenth valve (50) is opened, and O is carried out 3 Performing secondary aeration and nitrification operation in a time interval, controlling the DO concentration in the NSBR tank (2) to be 1.5-2.5mg/L in the operation process, taking aeration time for 20-35min according to an operation result, and closing the tenth valve (50) and the second air blower (52) after aeration is finished;
(6) deposit, drainage, row's mud, the system is idle: after the tenth valve (50) and the second air blower (52) are closed, the NSBR tank (2) enters a sludge-water separation settling state, the settling time is 30-60min, after the settling time is up, a thirteenth valve (37) of the system is opened, secondary nitrified liquid is discharged into the fourth intermediate water tank 7, the water discharge ratio is 0.6-0.7, and simultaneously a fourteenth valve (38) of the system is opened as required to discharge sludge, so that the sludge age is controlled to be 25-35d; after the water and mud discharging is finished, the thirteenth valve (37) and the fourteenth valve (38) are closed, the NSBR tank (2) enters an idle state, and after the idle time is up, the NSBR tank (2) enters the next period for operation;
the AOASBR pool (1) and the NSBR pool (2) run each operation process, which comprises the opening and closing of each water inlet pump and each valve, the opening and closing of the aeration and stirring processes, and the opening and closing of the water filling and draining processes, instructions are sent by the process controller (9) according to a control strategy, and the real-time control is completed, and the change characteristic values of the water filling and draining ratio, the stirring time, the aeration time, the stirring and aeration process control parameters DO and the pH of the AOASBR pool (1) and the NSBR pool (2) are set and modified through the parameter setting and display end (40) of the data processor (8) according to the operation condition of the system.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211204863.1A CN115571981A (en) | 2022-09-29 | 2022-09-29 | Improved A 2 NSBR double-mud denitrification dephosphorization process method |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202211204863.1A CN115571981A (en) | 2022-09-29 | 2022-09-29 | Improved A 2 NSBR double-mud denitrification dephosphorization process method |
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| Publication Number | Publication Date |
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| CN115571981A true CN115571981A (en) | 2023-01-06 |
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| WO2022062615A1 (en) * | 2020-09-24 | 2022-03-31 | 北京工业大学 | Device and method for implementing deep denitrogenation of domestic sewage by half shortcut nitrification-anaerobic ammonium oxidation coupled sulfur autotrophic denitrification |
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