CN103910432A - Energy-saving type nitrogen-phosphor efficient removing method for sequencing batch type domestic wastewater - Google Patents
Energy-saving type nitrogen-phosphor efficient removing method for sequencing batch type domestic wastewater Download PDFInfo
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Abstract
The invention discloses an energy-saving type nitrogen-phosphor efficient removing method for sequencing bath type domestic wastewater. The energy-saving type nitrogen-phosphor efficient removing method disclosed by the invention is characterized by adopting a sequencing batch type reactor to treat domestic wastewater, and comprises the following steps: (1) inputting domestic wastewater into the sequencing batch type reactor, and mechanically stirring for 2-3 hours under an anaerobic condition; (3) carrying out low-air rate aeration on the sequencing batch type reactor and controlling concentration of dissolved oxygen in the sequencing batch type reactor to 0.8mg/L-1.0mg/L, continuously reacting for 2.5-3.5 hours, and controlling a ratio of nitrate nitrogen concentration to phosphate concentration (in terms of phosphor) in the reactor to 1.9-2.2 after the reaction is ended; (3) stopping aeration for the sequencing batch type reactor, mechanically stirring and continuously reacting for 3-4 hours; (4) starting aeration for the sequencing batch type reactor, controlling concentration of the dissolved oxygen in the sequencing batch type reactor to 3mg/L-4mg/L, and continuously reacting for 1-2 hours; and (5) stopping aeration for the sequencing batch type reactor, stewing and precipitating, exhausting the treated domestic wastewater through a water draining tube, and exhausting residual sludge by a sludge exhausting tube, and the like.
Description
Technical field
The present invention relates to a kind of energy-saving efficient domestic sewage denitrification and dephosphorization method of realizing synchronous nitration and denitrification and denitrification dephosphorization coupling, belong to environmental wastewater processing technology field.
Background technology
At present in China's town domestic sewage, organic concentration is generally lower, and COD only has 100～200mg/L conventionally, makes the C/N value in town domestic sewage conventionally lower, and domestic sewage treatment process based on traditional denitrogenation dephosphorizing theory, as A
2/ O (Anaerobic/Anoxic/Oxic, A
2/ O), oxidation ditch and various SBR (Sequencing Batch Reactor, SBR) technique etc., there is many-sided unfavorable factor: the nitrate in competition, the mud of mud contradiction in age, anoxic denitrification and the anaerobic phosphorus release between nitrifier and polyP bacteria on carbon source is released the impact of phosphorus etc. on polyP bacteria, therefore dephosphorization and denitrification effect is unstable in actual applications.In the time that the C/N of sewage value is on the low side, can not meet denitrification and the demand of biological phosphate-eliminating to carbon source simultaneously, water outlet total nitrogen and total phosphorus concentration are always difficult to the limit value lower than 15mg/L and 0.5mg/L simultaneously.On the other hand, municipal sewage treatment is one of high energy consumption industry, and wherein aeration energy consumption accounts for the more than 40% of sewage disposal energy consumption, is unfavorable for the Sustainable development of sewage disposal.
Synchronous nitration and denitrification (Simultaneous Nitrification and Denitrification, SND) by restriction aeration, ammonia oxidation (nitrated) and denitrification are carried out simultaneously, compared with traditional biological denitride technology, SND has following advantage: (1) is little to DO concentration demand, saves aeration energy consumption; (2) nitration reaction consumes basicity, and anti-nitration reaction produces basicity, and this just makes the pH rangeability in reaction process little, is conducive to maintain the reaction environment in reactor.Denitrification dephosphorization is with the denitrogenation simultaneously of identical matrix and dephosphorization by Denitrifying Phosphate Accumulating Organisms, denitrifying bacteria and polyP bacteria are alleviated in traditional biological dephosphorization and denitrification process for the competition of carbon source and the contradiction of nitrifier and the best sludge age difference of polyP bacteria, the organism of energy saving approximately 50% and 30% oxygen-consumption, the surplus sludge volume of corresponding minimizing approximately 50%, processes significant for the denitrogenation dephosphorizing of low carbon source sanitary sewage.
Summary of the invention
Goal of the invention: the object of the invention is to overcome prior art deficiency, a kind of synchronous nitration and denitrification of suitable treatment low c/n value sanitary sewage and the high-efficient denitrification and dephosphorization technique of denitrification dephosphorization coupling are provided, and reduce energy consumption, minimizing sludge creation amount.
Technical scheme: energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method of the present invention, adopt sequencing batch reactor to process sanitary sewage, according to " water inlet anaerobism stirring → low-oxygen aeration → anoxia stirring → aerobic aeration → precipitation, draining, spoil disposal " 5 processes, periodic duty.Specifically comprise the following steps:
(1) sanitary sewage is inputted in sequencing batch reactor, and mechanical stirring 2～3 hours under anaerobic, make fully to mix with mud and water standing in reactor into water by mechanical stirring, Denitrifying Phosphate Accumulating Organisms absorbs low molecule organic matter synthetic PHA in vivo, carries out anaerobic phosphorus release reaction;
(2) the low tolerance aeration of sequencing batch reactor, and to control dissolved oxygen concentration in sequencing batch reactor be 0.8～1.0mg/L, sustained reaction 2.5～3.5 hours, carry out nitrated and Partial synchronization nitration denitrification reaction, mineralized nitrogen is nitric nitrogen and realizes part denitrogenation, and the ratio of the interior nitrate of control reaction end post-reactor and phosphate concn (take phosphorus) is 1.9～2.2;
(3) sequencing batch reactor is stopped to aeration, mechanical stirring, reactor is in anoxic condition, Denitrifying Phosphate Accumulating Organisms utilizes step B) in the nitric nitrogen that do not consume as electron acceptor(EA), stir section using anaerobism and store " internal carbon source "-PHA in vivo and carry out denitrification phosphorus-collecting reaction as electron donor, realize synchronous denitrification dephosphorizing, sustained reaction 3～4 hours;
(4) sequencing batch reactor starts aeration, and to control the concentration of dissolved oxygen in sequencing batch reactor be 3～4mg/L, sustained reaction 1～2 hour;
(5) sequencing batch reactor is stopped to aeration, staticly settle, then sanitary sewage after treatment is discharged through water shoot, and discharge excess sludge by shore pipe;
(6) repeating step (1)～(5) successively.
Further, described sequencing batch reactor is provided with pH sensor (2), redox potential sensor (3), dissolved oxygen sensor (4), pH/ redox potential detector (6), dissolved oxygen detector (7), PLC controller (16), intake pump (11), water inlet electrically operated valve, draining electrically operated valve (9), blower fan (14) and agitator (10); PH sensor (2) and redox potential sensor (3) wherein transmit signals to pH/ redox potential detector (6); Dissolved oxygen sensor (4) transmits signals to dissolved oxygen detector (7); PLC controller (16) is received from the signal that pH/ redox potential detector (6) and dissolved oxygen detector (7) are sent; PLC controller (16) sent control signal with the signal receiving and is sent to intake pump (11), water inlet electrically operated valve, draining electrically operated valve (9), blower fan (14) and agitator (10) according to the time of self clock.
Preferably, in step (1), what the ORP in sequencing batch reactor all reacted with anaerobic phosphorus release with pH carry out and decline, and in the time that reaction finishes, ORP no longer declines, pH transfers rising to, therefore when reaction proceed to dORP/dt and dpH/dt all from negative value become 0 or on the occasion of time, in practice, this condition occurs that required step (1) working time is 2～3 hours, end step (1), enters step (2).
Preferably, in step (2), pH in sequencing batch reactor carries out and declines with reaction, when reaction finish time, pH transfers rising to, therefore when react proceed to dpH/dt from negative value become 0 or on the occasion of time, in practice, this condition occurs that required step (2) working time is 2.5～3.5 hours, and end step (2), enters step (3).
Preferably, in step (3), pH in sequencing batch reactor carries out and rises with reaction, in the time that reaction finishes, pH transfers decline to, therefore proceeds to dpH/dt from the occasion of becoming 0 or when negative value when reacting, in practice, this condition occurs that required step (3) working time is 3～4 hours, and end step (3), enters step (4).
Preferably, in step (4), ORP in sequencing batch reactor carries out and rises with reaction, in the time that reaction finishes, it is stable that ORP maintains, therefore when reaction proceeds to dORP/dt from the time becoming 0, in practice, this condition occurs that required step (4) working time is 1～2 hour, and end step (4), enters step (5).
Preferably, in step (5), after staticly settling, water shoot is discharged the sanitary sewage after treatment of total Water massfraction 62～68% in reactor, and shore pipe is got rid of the mud of sludge quantity massfraction 5～6.7% in reactor.
Preferably guarantee the low-oxygen aeration stage while finishing in reactor the ratio of nitrate and phosphate concn (take phosphorus) under 1.9～2.2 prerequisite, improve the synchronous nitration and denitrification rate in low-oxygen aeration stage as far as possible, realize the efficient removal of nitrogen.
Compared with prior art, its beneficial effect is in the present invention: 1, realize synchronous nitration and denitrification effect by low-oxygen aeration and denitrogenate, reduced aeration energy consumption, reduced the reaction times simultaneously; 2, adopt Denitrifying Phosphorus Removal Technology, avoided the competition to carbon source of denitrification and biological phosphate-eliminating, for the processing of low c/n value sanitary sewage provides technical scheme; 3, phosphorus is mainly removed by the Denitrifying Phosphorus Removal in anoxia stirring stage, has reduced the required aeration energy consumption of traditional aerobic suction phosphorus process.
Accompanying drawing explanation
Fig. 1 is the step block diagram of a kind of energy-saving sequence batch (sanitary sewage nitrogen phosphorus removal method of the present invention;
Fig. 2 is a kind of sequencing batch reactor using in the embodiment of the present invention.
Embodiment
Below technical solution of the present invention is elaborated, but protection scope of the present invention is not limited to described embodiment.
In the middle of following examples, ORP represents that Oxidation-reduction Potential is redox potential.DO represents that Dissolved Oxygen is dissolved oxygen.
As shown in Figure 2, the sequencing batch reactor 1 that following examples adopt is provided with electric mixer 10 evenly to be mixed muddy water, and bottom is provided with aeration head 13, is connected with blower fan 14 by tracheae, and system is carried out to aeration, and charge flow rate is controlled by spinner-type flowmeter 12; This reactor is provided with water port, and water port is provided with electrically operated valve 9, is connected by water shoot 5, and the one-period reaction of system finishes rear unlatching electrically operated valve 9 and carries out draining; Water-in is connected with intake pump 11, open intake pump 11 can be from water tank 8 to sequencing batch reactor 1 water inlet, flooding velocity is controlled by spinner-type flowmeter 12; Be provided with pH sensor 2, ORP sensor 3 and be connected with pH/ORP detector 6 and be connected with DO detector 7 with DO sensor 4, the state parameters such as redox potential (ORP), pH value and DO to the whole process of system carry out on-line real time monitoring; Regularly discharge a certain amount of excess sludge by shore pipe 15.Adopt PLC controller 16 right intake pump 11, agitator 10, blower fan 14 and electrically operated valves 9 to open and close control, PLC controller 16 connects pH/ORP detector 6, DO detector 7 simultaneously, utilizes gained state parameter to control running situation.
PLC controller 16 is carried out following steps successively:
Step 1 realizes by following action: open intake pump 11, sanitary sewage is imported in sequencing batch reactor 1, intake after 5～10 minutes, close intake pump 11, start agitator 10, water inlet fully mixes with residue muddy water of upper cycle in reactor, and Denitrifying Phosphate Accumulating Organisms absorbs low molecule organic matter synthetic PHA in vivo, and anaerobic phosphorus release effect occurs.This stage is that anaerobism stirs section, carries out anaerobism and stirs 2～3 hours;
Step 2 realizes by following action: open blower fan 14, sequencing batch reactor 1 is carried out to low tolerance aeration, DO concentration maintains 0.8～1.0mg/L, carry out nitrated and Partial synchronization nitration denitrification reaction, mineralized nitrogen is nitric nitrogen and realizes part denitrogenation, and controlling reaction, to finish the ratio of nitrate and phosphate concn (take phosphorus) in post-reactor be 1.9～2.2.This stage is low-oxygen aeration section, and aeration continues, after 2.5～3.5 hours, to close blower fan 14;
Step 3 realizes by following action: close after blower fan 14, agitator is still working order, continue to stir, reactor is in anoxic condition, and Denitrifying Phosphate Accumulating Organisms utilizes the nitric nitrogen that do not consume in step B as electron acceptor(EA), carry out denitrification phosphorus-collecting reaction using the PHA storing in vivo in steps A as electron donor.This stage is anoxia stirring section, and reaction continues 3～4 hours;
Step 4 realizes by following action: open blower fan 14, sequencing batch reactor 1 is carried out to aeration, DO concentration maintains 3～4mg/L, and polyP bacteria carries out aerobic suction phosphorus.This stage is aerobic aeration section, and reaction is carried out 1～2 hour;
Step 5 realizes as follows: close blower fan 14 and agitator 10, staticly settle, then, by opening electrically operated valve 9 opening water discharge pipes 5, after processing, water (supernatant liquor) is discharged, and after a certain proportion of supernatant liquor is discharged, closes electrically operated valve 9; Open the valve on shore pipe 15, discharge a certain amount of excess sludge;
In each step, all adopt PLC controller 16 to open and close control to intake pump 11, agitator 10, blower fan 14 and electrically operated valve 9, system repeats above-mentioned 5 steps successively, the state parameters such as on-line real time monitoring redox potential ORP, pH value and DO, pH/ORP detector 6 is connected with PLC controller 16 with DO detector 7, automatically regulates 1 each elementary reaction time of sequencing batch reactor according to influent quality or reactor conditions.Whole system alternately experiences anaerobism, hypoxemia, anoxic, good oxygen condition, intermittent water inflow and water outlet, and by regularly a certain amount of excess sludge of discharge of shore pipe 15.
If influent COD increases, can the proper extension anaerobism section time, dORP/dt and dpH/dt by negative transfer to 0 or timing can be used as the state parameter that the anaerobism section time controls; If influent ammonium concentration increases, can be by low-oxygen aeration section time proper extension, when dpH/dt becomes 0 or timing from negative, can be used as the mark that in reactor, nitrification finishes; If water inlet phosphorus increases, can be by anoxic section time proper extension, the value of dpH/dt is by just transferring 0 or can be used as the mark of anoxic section denitrifying phosphorus uptake end of processing when negative to; The value of dORP/dt, by just transferring at 0 o'clock, illustrates nitration reaction and aerobic suction phosphorus end of processing in reactor.
In the time that the N/P of anoxic Duan Shuizhong value is 1.9～2.2, obtain good denitrification dephosphorization effect.
If desired further reduce water outlet concentration of nitrogen and phosphorus, improve removal efficiency of nitrogen and phosphorus, can consider suitably to intake in low-oxygen aeration section, utilize the denitrification that in water, carbon source improves denitrifying bacteria, suppress the consumption to PHA in body of common polyP bacteria and Denitrifying Phosphate Accumulating Organisms simultaneously, make Denitrifying Phosphate Accumulating Organisms have enough PHA to carry out denitrifying phosphorus uptake effect in anoxic section, thereby improve nitrogen phosphorus removal effect.
Further illustrate the present invention by specific embodiment below:
Embodiment 1
25～28 ℃ time, in reactor, mixed liquor suspended solid, MLSS concentration (mixed liquid suspended solids) MLSS is 3100mg/L～3300mg/L, sludge age is 20d, water-filling ratio is 62%, when sanitary sewage influent COD is 150mg/L, when COD/TN/TP is 25:5:1, coupling-SBR system anaerobism section (step 1), low-oxygen aeration section (step 2), anoxic section (step 3), be set to respectively 2h the working time of aerobic section (step 4) and precipitating phase (step 5), 3h, 3.5h, 1h, 1.5h, wherein in step 5, water shoot is discharged the sanitary sewage after treatment of total Water massfraction 62% in reactor, shore pipe is got rid of the mud of middle sludge quantity massfraction 5% in reactor, wherein the dissolved oxygen concentration of step 2 low-oxygen aeration section remains 0.95mg/L, wherein the dissolved oxygen concentration of step 4 aerobic section remains 3.5mg/L, water outlet COD, NH
4 +-N, TN and TP concentration are respectively 18.56mg/L, 0.03mg/L, 9.65mg/L and 0.51mg/L.TN and TP clearance are respectively 67.8% and 91.5%, and the TN wherein removing by SND and Denitrifying Phosphorus Removal is respectively 11.2% and 56.6%, and the TP that inhales phosphorus and the removal of aerobic suction phosphorus by anoxic denitrification after anaerobic phosphorus release is respectively 78.7% and 12.8%.
Embodiment 2
When water temperature is 20 ℃ of left and right, sludge age is 15d, and MLSS is 3497 ± 63mg/L, and SVI is 87 ± 1.6mL/g, and water-filling ratio is 66%, water inlet pH=7.50 ± 0.23, and sanitary sewage influent COD is 250mg/L, NH
4 +-N, TN and TP concentration are respectively 44mg/L, 50mg/L, 8.2mg/L time, coupling-SBR system anaerobism section (step 1), low-oxygen aeration section (step 2), anoxic section (step 3), be respectively 2h the working time of aerobic section (step 4) and precipitating phase (step 5), 3h, 3.5h, 1h, 1.5h, wherein in step 5, water shoot is discharged the sanitary sewage after treatment of total Water massfraction 66% in reactor, shore pipe is got rid of the mud of middle sludge quantity massfraction 6.7% in reactor, wherein the dissolved oxygen concentration of step 2 low-oxygen aeration section remains 1.0mg/L, wherein the dissolved oxygen concentration of step 4 aerobic section remains 4mg/L, obtain water outlet COD, NH
4 +-N, TN, TP concentration are respectively 30.42mg/L, 2.82mg/L, 9.71mg/L, 0.87mg/L, and system sludge overall performance is better, and ammonia nitrogen, TN and TP clearance are respectively 93.6%, 80.6% and 89.4%.
Embodiment 3
When water temperature is 18 ℃ of left and right, sludge age is 18d, and MLSS is 3412 ± 58mg/L, and water-filling ratio is 68%, water inlet pH=7.40 left and right, and sanitary sewage influent COD is 180mg/L, NH
4 +-N, TN and TP concentration are respectively 34mg/L, 42mg/L, when 7mg/L, coupling-SBR system anaerobism section (step 1), low-oxygen aeration section (step 2), anoxic section (step 3), aerobic section (step 4) and precipitating phase (step 5) moment out of service be respectively in step (1) when the dORP/dt in sequencing batch reactor and dpH/dt all from negative value become 0 or on the occasion of time, in step (2) when the dpH/dt in sequencing batch reactor from negative value become 0 or on the occasion of time, in step (3) when the dpH/dt in sequencing batch reactor is from the occasion of becoming 0 or when negative value, in step (4) when the dORP/dt in sequencing batch reactor is from the time becoming 0, when precipitation process reaches 2 hours, wherein in step 5, water shoot is discharged the sanitary sewage after treatment of total Water massfraction 68% in reactor, shore pipe is got rid of the mud of middle sludge quantity massfraction 5.6% in reactor, wherein the dissolved oxygen concentration of step 2 low-oxygen aeration section remains 0.8mg/L, wherein the dissolved oxygen concentration of step 4 aerobic section remains 3mg/L, obtains water outlet COD, NH
4 +-N, TN, TP concentration are respectively 17.8mg/L, 1.73mg/L, 9.88mg/L, 0.65mg/L, and TN and TP clearance are respectively 76.5% and 90.7%.
Embodiment 4
When water temperature is 22 ℃ of left and right, sludge age is 15d, and MLSS is 3300 ± 70mg/L, and water-filling ratio is 66%, water inlet pH=7.35 left and right, and sanitary sewage influent COD is 210mg/L, NH
4 +-N, TN and TP concentration are respectively 38mg/L, 44mg/L, when 6mg/L, coupling-SBR system anaerobism section (step 1), low-oxygen aeration section (step 2), anoxic section (step 3), be respectively 3h the working time of aerobic section (step 4) and precipitating phase (step 5), 2.5h, 3h, 2h, 1h, wherein in step 5, water shoot is discharged the sanitary sewage after treatment of total Water massfraction 66% in reactor, shore pipe is got rid of the mud of middle sludge quantity massfraction 6.7% in reactor, wherein the dissolved oxygen concentration of step 2 low-oxygen aeration section remains 0.9mg/L, wherein the dissolved oxygen concentration of step 4 aerobic section remains 3.5mg/L, obtain water outlet COD, NH
4 +-N, TN, TP concentration are respectively 22.6mg/L, 1.75mg/L, 9.50mg/L, 0.57mg/L, and TN and TP clearance are respectively 78.4% and 90.5%.
Embodiment 5
Adopt traditional anaerobic/anoxic/aerobic process (A
2/ O technique) processing sanitary sewage.When water temperature is 20 ℃ of left and right, sludge age is 15d, and MLSS is 3300mg/L left and right, flooding velocity Q=4.22L/h, and influent COD is 185mg/L, NH
4 +when-N, TN and TP concentration are respectively 35mg/L, 45mg/L, 5mg/L, traditional A
2be respectively 2.5h, 3h, 8h the working time of/O technique anaerobism section, anoxic section, aerobic section, and wherein the dissolved oxygen concentration of aerobic aeration section remains 3.5mg/L, and mixed solution internal reflux amount is 8.6L/h, and sludge reflux amount is 2.2L/h, obtains water outlet COD, NH
4 +-N, TN, TP concentration are respectively 17.56mg/L, 2.07mg/L, 15.59mg/L, 0.92mg/L, and TN and TP clearance are respectively 65.36% and 81.6%.
More each embodiment data are known, and energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method of the present invention is fast with respect to the prior art reaction times, and removal efficiency of nitrogen and phosphorus is high, possesses significant progress.
As mentioned above, although represented and explained the present invention with reference to specific preferred embodiment, it shall not be construed as the restriction to the present invention self.Not departing under the spirit and scope of the present invention prerequisite of claims definition, can make in the form and details various variations to it.
Claims (8)
1. an energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method, is characterized in that, adopts sequencing batch reactor to process sanitary sewage, and comprises the following steps:
(1) sanitary sewage is inputted in sequencing batch reactor, and mechanical stirring 2～3 hours under anaerobic;
(2) the low tolerance aeration of sequencing batch reactor, and to control dissolved oxygen concentration in sequencing batch reactor be 0.8～1.0mg/L, sustained reaction 2.5～3.5 hours, and by adjusting the degree of Dissolved Oxygen concentration Control synchronous nitration and denitrification, make reaction finish in post-reactor nitric nitrogen mass concentration with the ratio of the phosphoric acid salt mass concentration take phosphorus as 1.9～2.2;
(3) sequencing batch reactor is stopped to aeration, mechanical stirring, sustained reaction 3～4 hours;
(4) sequencing batch reactor starts aeration, and to control the concentration of dissolved oxygen in sequencing batch reactor be 3～4mg/L, sustained reaction 1～2 hour;
(5) sequencing batch reactor is stopped to aeration, staticly settle, sanitary sewage after treatment is discharged through water shoot, and discharge excess sludge by shore pipe;
(6) repeating step (1)～(5) successively.
2. energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method according to claim 1, it is characterized in that, described sequencing batch reactor is provided with pH sensor (2), redox potential sensor (3), dissolved oxygen sensor (4), pH/ redox potential detector (6), dissolved oxygen detector (7), PLC controller (16), intake pump (11), water inlet electrically operated valve, draining electrically operated valve (9), blower fan (14) and agitator (10); PH sensor (2) and redox potential sensor (3) wherein transmit signals to pH/ redox potential detector (6); Dissolved oxygen sensor (4) transmits signals to dissolved oxygen detector (7); PLC controller (16) is received from the signal that pH/ redox potential detector (6) and dissolved oxygen detector (7) are sent; PLC controller (16) sent control signal with the signal receiving and is sent to intake pump (11), water inlet electrically operated valve, draining electrically operated valve (9), blower fan (14) and agitator (10) according to the time of self clock.
3. energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method according to claim 1, it is characterized in that: in step (1) when the dORP/dt in sequencing batch reactor and dpH/dt all from negative value become 0 or on the occasion of time, end step (1), enters step (2).
4. energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method according to claim 1, it is characterized in that: in step (2) when the dpH/dt in sequencing batch reactor from negative value become 0 or on the occasion of time, end step (2), enters step (3).
5. energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method according to claim 1, it is characterized in that: in step (3) when the dpH/dt in sequencing batch reactor is from the occasion of becoming 0 or when negative value, end step (3), enters step (4).
6. energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method according to claim 1, it is characterized in that: in step (4) when the dORP/dt in sequencing batch reactor is from the time becoming 0, end step (4), enters step (5).
7. energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method according to claim 1, it is characterized in that: in step (5), water shoot is discharged the sanitary sewage after treatment of total Water massfraction 62～68% in reactor, and shore pipe is got rid of the mud of middle sludge quantity massfraction 5～6.7% in reactor.
8. energy-saving sequence batch (sanitary sewage nitrogen phosphorus efficiency removal method according to claim 1, is characterized in that: the dissolved oxygen solubility in step (2) sequencing batch reactor is 0.8mg/L.
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| CN104944584B (en) * | 2015-07-12 | 2017-03-22 | 北京工业大学 | Process control method for achieving interior source storage and interior source denitrification nitrogen and phosphorus removal strengthening of SNDPR system through delaying anaerobism |
| CN105293699A (en) * | 2015-10-25 | 2016-02-03 | 北京工业大学 | Method for performing denitrifying phosphorus removal through anaerobism-nitration-oxygen deprivation-nitration technology |
| CN105776758A (en) * | 2016-04-20 | 2016-07-20 | 安徽国祯环保节能科技股份有限公司 | Improved SBR wastewater treatment process for obtaining standard IV-class surface water |
| CN105776758B (en) * | 2016-04-20 | 2018-09-28 | 安徽国祯环保节能科技股份有限公司 | A kind of Modified SBR sewage treatment process of IV class of surface water up to standard |
| CN105800777A (en) * | 2016-05-16 | 2016-07-27 | 沈阳环境科学研究院 | Energy-saving sewage treatment system based on SBR process |
| CN107082492A (en) * | 2017-04-27 | 2017-08-22 | 东南大学 | A kind of low consumption continuous stream domestic sewage treatment reactor and nitrogen phosphorus efficiency minimizing technology |
| CN107082492B (en) * | 2017-04-27 | 2020-09-11 | 东南大学 | Low-consumption continuous flow domestic sewage treatment reactor and nitrogen and phosphorus efficient removal method |
| CN110156163A (en) * | 2019-06-15 | 2019-08-23 | 北京中科宇清环保有限公司 | Handle the integrated reactor of sanitary sewage |
| CN111153495A (en) * | 2020-01-19 | 2020-05-15 | 武汉德同宜环境科技有限公司 | Sequencing batch reaction process and device for single-step denitrification without moving part |
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| CN103910432B (en) | 2016-06-08 |
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