CN115784439A - Vertical flow type device for realizing synchronous nitrogen and phosphorus removal of domestic sewage of villages and towns through granular sludge at low temperature - Google Patents
Vertical flow type device for realizing synchronous nitrogen and phosphorus removal of domestic sewage of villages and towns through granular sludge at low temperature Download PDFInfo
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- 239000010802 sludge Substances 0.000 title claims abstract description 141
- 239000010865 sewage Substances 0.000 title claims abstract description 45
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 38
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 20
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 20
- 239000011574 phosphorus Substances 0.000 title claims abstract description 20
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 19
- 230000001360 synchronised effect Effects 0.000 title claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 145
- 238000006243 chemical reaction Methods 0.000 claims abstract description 121
- 238000005273 aeration Methods 0.000 claims description 87
- 239000007788 liquid Substances 0.000 claims description 25
- 239000000523 sample Substances 0.000 claims description 22
- 238000004062 sedimentation Methods 0.000 claims description 19
- 230000001546 nitrifying effect Effects 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 13
- 229910052760 oxygen Inorganic materials 0.000 claims description 13
- 239000001301 oxygen Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 7
- 230000010485 coping Effects 0.000 abstract description 6
- 244000005700 microbiome Species 0.000 abstract description 5
- 239000002028 Biomass Substances 0.000 abstract description 4
- 230000014759 maintenance of location Effects 0.000 abstract description 4
- 230000002411 adverse Effects 0.000 abstract description 3
- 230000029058 respiratory gaseous exchange Effects 0.000 abstract description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 2
- 229910052799 carbon Inorganic materials 0.000 abstract description 2
- 238000005469 granulation Methods 0.000 abstract 1
- 230000003179 granulation Effects 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 238000010992 reflux Methods 0.000 description 47
- 238000000034 method Methods 0.000 description 11
- 239000002351 wastewater Substances 0.000 description 8
- 241000894006 Bacteria Species 0.000 description 7
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 7
- 239000003344 environmental pollutant Substances 0.000 description 4
- 238000012544 monitoring process Methods 0.000 description 4
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- 230000002159 abnormal effect Effects 0.000 description 3
- 230000001079 digestive effect Effects 0.000 description 3
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- 238000010008 shearing Methods 0.000 description 2
- 241000016680 Candidatus Accumulibacter Species 0.000 description 1
- 241000605008 Spirillum Species 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
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- 238000001914 filtration Methods 0.000 description 1
- 235000003642 hunger Nutrition 0.000 description 1
- 238000011081 inoculation Methods 0.000 description 1
- 230000009935 nitrosation Effects 0.000 description 1
- 238000007034 nitrosation reaction Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000036186 satiety Effects 0.000 description 1
- 235000019627 satiety Nutrition 0.000 description 1
- 238000001878 scanning electron micrograph Methods 0.000 description 1
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- 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
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The vertical flow type device for realizing synchronous nitrogen and phosphorus removal of domestic sewage in villages and small towns through granular sludge at low temperature utilizes hydraulic characteristics to enable the sludge to realize granulation so as to increase biomass, can realize efficient nitrogen and phosphorus removal and synchronous sludge treatment in the same device, is provided with a vertical guide plate in an anaerobic-anoxic reaction tank, structurally prolongs the hydraulic retention time of an anaerobic-anoxic zone, strengthens the utilization of the anaerobic-anoxic zone on a carbon source, simultaneously an aerobic zone can operate under low load, microorganisms in activated sludge are in an endogenous respiration period, and the sludge production amount of a system is low. The invention can treat the dispersive domestic sewage under the condition of low temperature, can eliminate the adverse effect of the return activated sludge on the anaerobic zone and the anoxic zone, improves the denitrification efficiency and is also used for removing phosphorus. The invention has the characteristics of high flexibility for coping with the change of inlet water quality and adjusting operation parameters and strong impact load resistance, has the characteristic of fast starting for coping with system damage caused by nonresistant factors such as power failure, cut-off and the like, and also has the foresight property of coping with the requirements of improving the effluent standard and the sludge discharge limitation.
Description
Technical Field
The invention relates to a vertical flow type device for realizing synchronous nitrogen and phosphorus removal of domestic sewage in villages and towns through granular sludge at a low temperature, belonging to the technical field of biological sewage treatment.
Background
The discharge amount of sewage in rural areas is increased year by year and is unstable, and the quality of the sewage is gradually complicated. The drainage system and the centralized sewage treatment system of the villages and towns in the north are not sound for a long time, and the problems of random discharge and substandard discharge of domestic sewage exist, so that the surface water environment is seriously influenced. Meanwhile, the domestic sewage of villages and towns has the problems of large water quality and water quantity fluctuation and high ammonia nitrogen concentration; in summer, due to dilution of rainwater and large water consumption, the concentration of pollutants is lower, the temperature in winter is greatly reduced, meanwhile, the sewage quantity is reduced, the concentration of pollutants is increased, and the water quality and water quantity change in day and night is more obvious; therefore, the development of a domestic sewage treatment technology which has strong impact load resistance and is suitable for a low-temperature environment is extremely urgent, and the effective treatment of sewage in villages and small towns is an important measure for improving the water environment quality of a drainage basin, and has important significance for guaranteeing the safety of the environment quality.
The aerobic granular sludge has great application potential in the field of domestic sewage treatment. Compared with the traditional flocculent activated sludge, the granular sludge is a high-activity compact body formed by winding microorganisms, has higher biomass concentration and good sedimentation performance, and has good adaptability to impact load and adverse environmental conditions.
The invention relates to a vertical device for realizing synchronous nitrogen and phosphorus removal of domestic sewage in villages and towns through granular sludge at low temperature, which utilizes hydraulic characteristics to granulate the sludge so as to increase biomass, can realize high-efficiency nitrogen and phosphorus removal and synchronous sludge treatment in the same reactor, and is an environment-friendly process with high efficiency and low consumption. The process is characterized in that a vertical guide plate is arranged in an anaerobic-anoxic reaction tank, the hydraulic retention time of an anaerobic-anoxic zone is structurally prolonged, the utilization of a carbon source by the anaerobic-anoxic zone is enhanced, meanwhile, the aerobic zone can operate under low load, microorganisms in activated sludge are in an endogenous respiration period, and the sludge yield of a system is low. The system can treat the dispersive domestic sewage with complex water quality and water quantity conditions in villages and small towns under the low-temperature condition, can eliminate the adverse effect of the return activated sludge on the anaerobic zone and the anoxic zone, improves the denitrification efficiency and is used for removing phosphorus. In addition, the system has the characteristics of high flexibility for coping with the change of water inlet quality and adjusting operation parameters and high impact load resistance, has the characteristic of coping with system damage caused by nonresistant factors such as power failure, flow cutoff and the like to quickly start, and also has the foresight property of coping with the requirements of improving the water outlet standard and the sludge discharge limitation.
Disclosure of Invention
The invention aims to provide a vertical flow type device for realizing synchronous nitrogen and phosphorus removal of domestic sewage in villages and small towns through granular sludge at low temperature, and introduce stronger hydraulic shearing force, higher biomass concentration and a suspended biological bed to provide favorable conditions for the formation of the granular sludge, so as to solve the technical problems that a continuous flow sewage treatment process is difficult to normally operate in the aspect of treating the domestic sewage in the villages and small towns with large water quality and large water quantity fluctuation.
A vertical flow type device for realizing synchronous nitrogen and phosphorus removal of domestic sewage of villages and small towns through granular sludge at low temperature comprises an anaerobic-anoxic reaction tank, an aerobic reaction tank, a sedimentation tank, a water inlet pump, a guide baffle plate, an anaerobic return pipe, an anaerobic return ball valve, an anoxic return pipe, an anoxic return ball valve, a nitrifying liquid return pipe, a nitrifying liquid return ball valve, an aeration head, a gas flowmeter, an aeration pipe, an aeration pump, DO, PH, an ORP probe, an online water quality detector, a sludge return pipe, a sludge return ball valve, a sludge discharge ball valve, a temporary sludge storage tank, a water outlet weir, a water outlet valve, a water outlet pipe, a water outlet tank and an anoxic water outlet;
the anaerobic-anoxic reaction tank is formed by eighteen reaction compartments which are connected in series, an anoxic water outlet is formed between the anaerobic-anoxic reaction tank and the aerobic reaction tank and is communicated with the aerobic reaction tank, guide baffle plates are arranged between the reaction compartments in the transverse direction, the bottom end of the first guide baffle plate and the bottom of the anaerobic-anoxic reaction tank are provided with a flow channel, and the top of the first guide baffle plate is flush with the top of the anaerobic-anoxic reaction tank; the bottom end of the second guide baffle plate is tightly connected with the anaerobic-anoxic reaction tank, and the top end of the second guide baffle plate is lower than the top end of the anaerobic-anoxic reaction tank, and the second guide baffle plate and the aerobic reaction tank are continuously arranged in this way, so that the sludge-water mixed liquor enters the second row of reaction compartments from the bottom of the guide baffle plate of the first row of reaction compartments, then enters the third row of reaction compartments from the top of the guide baffle plate of the second row of reaction compartments, and finally flows into the aerobic reaction tank from the anoxic water outlet of the anaerobic-anoxic reaction tank; the height of the guide baffle plate is gradually reduced along the water flow direction;
an anaerobic backflow pipe and an anoxic backflow pipe are arranged in the anaerobic-anoxic reaction tank, an anaerobic backflow ball valve is arranged on the anaerobic backflow pipe, and an anoxic backflow ball valve is arranged on the anoxic backflow pipe;
a separation plate is arranged between the aerobic reaction tank and the sedimentation tank;
the water inlet tank is communicated with a first reaction grid of the anaerobic-anoxic reaction tank through a water inlet pump and a pipeline, and a nitrifying liquid reflux pipe is arranged between the anaerobic-anoxic reaction tank and the aerobic reaction tank and is provided with a nitrifying liquid reflux ball valve;
the bottom of the aerobic reaction tank is provided with an aeration device, the aeration fittings comprise an aeration head, an aeration valve, an aeration pipe and an aeration pump, one end of the aeration valve is connected with the aeration head at the bottom of the aerobic reaction tank, the other end of the aeration valve is connected with the aeration pump through the aeration pipe, and the aeration pipe is provided with a gas flow meter for detecting the aeration intensity;
the sedimentation tank is provided with an effluent weir, the top of the effluent weir is communicated with the effluent tank through an effluent valve and an effluent pipe, and the bottom of the effluent weir is communicated with the temporary sludge storage tank through a pipeline and a sludge discharge ball valve;
the bottom of the effluent weir is communicated with a sludge return pipe through a sludge return ball valve, and the sludge return pipe is communicated with the anaerobic-anoxic reaction tank and the aerobic reaction tank; the mixed liquid in the aerobic reaction tank enters the middle part of the sedimentation tank from a flow channel at the bottom and then flows from bottom to top, the flow velocity of the water flow is gradually reduced, the sludge is settled at the bottom, a sludge discharge port is arranged at the bottom, the sludge can be discharged into a sludge temporary storage tank under the control of a sludge discharge ball valve, water passes through a settled sludge layer and upwards, and the supernatant is discharged into a water outlet tank through a water outlet pipe under the control of a water outlet valve after being collected by a water outlet weir;
a DO probe, a PH probe and an ORP probe of the water quality online monitor are arranged on the upper part of the aerobic reaction tank, and the dissolved oxygen concentration, the PH probe and the OPR probe are online detected at any time.
The invention adopts a continuous flow vertical flow bioreactor (VBRs) with a guide baffle plate capable of controlling the water flow direction to culture aerobic granular sludge; the operation mode is as follows: the domestic sewage is pretreated by a sewage treatment plant and then enters a VBRs reaction device through a water inlet pump; dissolved oxygen is supplied to the VBRs reactor through an aeration pump and an aeration pipe to form an anaerobic tank and an anoxic tank, wherein the aeration amount is controlled through a gas flowmeter; the reflux system comprises sludge reflux, digestive juice reflux, anaerobic reflux and anoxic internal reflux; the effluent water flows into the effluent pool through the effluent weir. The reactor can be operated not only at normal temperature but also at 6-11 ℃.
Water inlet source: dispersing and collecting the actual domestic sewage after simple filtration and precipitation, wherein the C/N of the inlet water is within the range of 4-7;
sludge inoculation: activated sludge taken from an aerobic tank of a municipal domestic sewage treatment plant is directly added into wastewater of a VBRs reactor by a sludge lifting pump for stuffy explosion for 2 days, meanwhile, each group of backflow is started to disperse the sludge into each reaction tank, wastewater is introduced to the effective working volume of the reactor, the sludge concentration in the aerobic reaction tank is 3000-3500mg/L in the starting stage, and the sludge concentration in the anaerobic reaction tank is 4500-5000mg/L;
1) Starting a system: the method comprises the following steps of equipment debugging, sludge domestication and granular sludge formation, wherein the running time of a system starting stage at normal temperature is 15 days, and a VBRs reactor continuously feeds water and discharges water; the aeration and sludge reflux period is 30min, and the specific operation mode in each period is as follows: the reactor is operated under the condition of room temperature (the water inlet temperature is 18-25 ℃); the wastewater is pretreated by a domestic sewage treatment plant and then is conveyed into a VBRs reactor through a water inlet pump, pulse type water inlet is adopted for water inlet, so that in a grid area flowing upwards, sludge forms a suspended sludge bed due to the upward flow velocity of the wastewater, and granular sludge is formed; the anaerobic-anoxic reaction tank is provided with a guide baffle plate which divides the reactor into a plurality of reaction chambers connected in series, and water flow is guided by the guide baffle plate to flow upwards and downwards to enter the aerobic reaction tank. Starting an aeration pump for aerobic aeration, monitoring the Dissolved Oxygen (DO) concentration by a DO probe of the water quality online detector, controlling the dissolved oxygen concentration to be 3.0-5.0mg/L, continuously aerating for 22min, and then stopping aerating for 8min; starting sludge reflux and nitrification liquid reflux in the aeration process, and closing after the aeration is stopped; anaerobic reflux and anoxic internal reflux are always kept in an open state, so that the water inlet load is reduced. The bottom of the sedimentation tank is provided with a sludge discharge port, sludge is discharged to a temporary sludge storage tank once every 2 days, the sludge age is controlled to be 5 days, and the sludge concentration of an aerobic tank in the reactor is controlled to be 3000mg/L.
2) The system operates as follows when running:
2.1 System parameter optimization: urban domestic sewage enters the VBRs reactor, the inflow rate is controlled through a flow meter, and the Hydraulic Retention Time (HRT) of the system is changed; and adjusting aeration quantity, and monitoring the DO change of the dissolved oxygen concentration in water in real time through a DO probe of the water quality online detector.
2.2 Impact load resistance capacity): continuous water inflow is carried out under the optimized system operation parameters, the fluctuation of the sewage quality is large, and the short-time water inflow is abnormal (COD is greater than 1000mg/L, C/N is greater than 30 TN > -100mg/L, and C/N is less than 3). Operating the reactor under the condition of abnormal water quality water inflow; the water inflow is controlled by a flowmeter, and the reactor is continuously operated under the condition of lower/higher than normal water inflow.
2.3 System operation at low temperature and granular sludge cultivation: the reactor is continuously operated in winter, the inlet water is the actual domestic sewage treated by a domestic sewage treatment plant, and the water temperature is kept between 6 and 11 ℃. The aeration and reflux period of the reactor is 1h, and the specific operation mode in each period is as follows: aerating continuously for 52min, stopping aerating for 8min, starting sludge backflow and digestive juice backflow in the aeration process, and closing after the aeration is stopped; the anoxic internal reflux is always kept in an open state. Discharging sludge once every 4 days to a sludge temporary storage tank, controlling the sludge age to be 12 days, and controlling the sludge concentration of an aerobic tank in the reactor to be 5000mg/L.
2.4 Fast start after system failure: the system stops water inlet, aeration and backflow for 12-36h, and then normal operation and normal water outlet are recovered within three days by adjusting operation parameters.
Preferably, a guide baffle plate is arranged in the reactor to divide the reactor into 18 serial anoxic/anaerobic reaction chambers and 2 aerobic reaction chambers; each reaction chamber is a relatively independent up-and-down flow type sludge bed system.
Preferably, the dissolved oxygen concentrations of the anaerobic tank, the anoxic tank and the aerobic tank are respectively controlled to be 0.20 +/-0.05 mg/L, 0.40 +/-0.05 mg/L and 5 +/-0.25 mg/L.
The invention has the beneficial effects that:
the system is simple, the energy consumption is low, the daily workload is small, meanwhile, the impact load resistance is strong, the requirement on the operating environment is low, the system is suitable for the treatment of domestic sewage with large water quality and water quantity fluctuation and low temperature conditions, the degradation of organic matters is thorough, the denitrification and dephosphorization effects are excellent, and good conditions can be provided for the formation of granular sludge; the invention changes the water inlet mode, adjusts the water inlet flow and the aeration quantity, changes the reflux proportion and the reflux period, strengthens the nitrogen and phosphorus removal effect of the system and shortens the forming time of the granular sludge. The operation is stable and the water is discharged stably under the condition of no medicine.
Drawings
FIG. 1 is a schematic view of the structure of the present invention;
fig. 2 is a schematic structural view of the anaerobic-anoxic reaction tank of the present invention.
In the figure: a C1-anaerobic-anoxic reaction tank; c2-aerobic reaction tank; c3, a sedimentation tank; 1-a water inlet pool; 2-a water inlet pump; 3, guiding a baffle plate; 4-anaerobic reflux pipe; 5-anaerobic reflux ball valve; 6-anoxic reflux pipe; 7-an anoxic reflux ball valve; 8-nitrifying liquid reflux pipe; 9-nitrifying liquid reflux ball valve; 10-an aeration valve; 11-an aeration head; 12-a gas flow meter; 13-an aerator pipe; 14-an aeration pump; 15-DO; PH value; an ORP probe; 16-a water quality on-line detector; 17-a sludge return pipe; 18-sludge return ball valve; 19-a mud discharge ball valve; 20-a sludge temporary storage tank; 21-an effluent weir; 22-outlet valve; 23-a water outlet pipe; 24-a water outlet pool; 25-anoxic water outlet.
Detailed Description
Referring to fig. 1 and 2, a vertical flow type device for realizing synchronous nitrogen and phosphorus removal of domestic sewage in villages and small towns through granular sludge at a low temperature comprises an anaerobic-anoxic reaction tank C1, an aerobic reaction tank C2, a sedimentation tank C3, a water inlet tank 1, a water inlet pump 2, a guide baffle plate 3, an anaerobic reflux pipe 4, an anaerobic reflux ball valve 5, an anoxic reflux pipe 6, an anoxic reflux ball valve 7, a nitrifying liquid reflux pipe 8, a nitrifying liquid reflux ball valve 9, an aeration valve 10, an aeration head 11, a gas flowmeter 12, an aeration pipe 13, an aeration pump 14, DO, PH, an ORP, a probe 15, an online water quality detector 16, a sludge reflux pipe 17, a sludge reflux ball valve 18, a sludge discharge ball valve 19, a temporary sludge storage tank 20, a water outlet weir 21, a water outlet valve 22, a water outlet pipe 23, a water outlet tank 24 and an anoxic water outlet 25;
the anaerobic-anoxic reaction tank C1, the aerobic reaction tank C2 and the sedimentation tank C3 are sequentially adjacent, the anaerobic-anoxic reaction tank C1 is composed of eighteen reaction compartments which are connected in series, an anoxic water outlet 25 is formed between the anaerobic-anoxic reaction tank C1 and the aerobic reaction tank C2 and is communicated with the aerobic reaction tank C2, guide baffle plates 3 are arranged between the reaction compartments in the transverse direction, the guide baffle plates 3 are arranged in a mode that a flow channel is formed between the bottom end of a first guide baffle plate 3 and the tank floor of the anaerobic-anoxic reaction tank C1, and the top of the first guide baffle plate 3 is flush with the tank top of the anaerobic-anoxic reaction tank C1; the bottom end of the second guide baffle plate 3 is closely connected with the anaerobic-anoxic reaction tank C1, the top end of the second guide baffle plate 3 is lower than the top end of the anaerobic-anoxic reaction tank C1, and the two guide baffle plates are continuously arranged in sequence, so that the muddy water mixed liquor enters the second row of reaction compartments from the bottom of the guide baffle plate 3 of the first row of reaction compartments, enters the third row of reaction compartments from the top of the guide baffle plate 3 of the second row of reaction compartments, and finally flows into the aerobic reaction tank C2 from the anoxic water outlet 25 of the anaerobic-anoxic reaction tank C1; the height of the guide baffle 3 is gradually reduced along the water flow direction;
an anaerobic return pipe 4 and an anoxic return pipe 6 are arranged in the anaerobic-anoxic reaction tank C1, an anaerobic return ball valve 5 is arranged on the anaerobic return pipe 4, and an anoxic return ball valve 7 is arranged on the anoxic return pipe 6;
a separation plate C21 is arranged between the aerobic reaction tank C2 and the sedimentation tank C3,
the water inlet tank 1 is communicated with a first reaction grid of the anaerobic-anoxic reaction tank C1 through a water inlet pump 2 and a pipeline, a nitrifying liquid return pipe 8 is arranged between the anaerobic-anoxic reaction tank C1 and the aerobic reaction tank C2, and a nitrifying liquid return ball valve 9 is arranged on the nitrifying liquid return pipe 8;
the bottom of the aerobic reaction tank C2 is provided with an aeration device, aeration accessories comprise an aeration head 11, an aeration valve 10, an aeration pipe 13 and an aeration pump 14, one end of the aeration valve 10 is connected with the aeration head 11 at the bottom of the aerobic reaction tank C2, the other end of the aeration valve 10 is connected with the aeration pump 14 through the aeration pipe 13, and the aeration pipe 13 is provided with a gas flow meter 12 for detecting the aeration intensity;
the sedimentation tank C3 is provided with an effluent weir 21, the top of the effluent weir 21 is communicated with an effluent tank 24 through an effluent valve 22 and an effluent pipe 23, and the bottom of the effluent weir 21 is communicated with a temporary sludge storage tank 20 through a pipeline and a sludge discharge ball valve 19;
the bottom of the effluent weir 21 is communicated with a sludge return pipe 17 through a sludge return ball valve 18, and the sludge return pipe 17 is communicated with the anaerobic-anoxic reaction tank C1 and the aerobic reaction tank C2; the mixed liquid in the aerobic reaction tank C2 enters the middle part of the sedimentation tank C3 from a flow channel at the bottom, then flows from bottom to top, the flow velocity of water flow is gradually slowed, sludge is settled at the bottom, a sludge discharge port is arranged at the bottom, the sludge can be discharged into the temporary sludge storage tank 20 under the control of the sludge discharge ball valve 19, water passes through a settled sludge layer and upwards, and supernatant liquid is discharged into a water outlet tank 24 through a water outlet pipe 23 under the control of a water outlet valve 22 after being collected by the water outlet weir 21;
a DO probe, a PH probe and an ORP probe 15 of a water quality on-line monitor 16 are arranged on the upper part of the aerobic reaction tank C2, and the dissolved oxygen concentration, the PH probe and the OPR probe are detected on line at any time.
The specific embodiment is as follows:
the sewage is taken from domestic sewage pretreated by a domestic sewage treatment plant in a certain village and a town of Changchun city, and the quality of raw water is as follows: COD concentration is 242-872mg/L, ammonia nitrogen concentration is 15.46-55.16mg/L, total nitrogen concentration is 20.31-91.44mg/L, and total phosphorus concentration is 1.04-4.66mg/L.
The tank body of the reactor is rectangular, the whole size is 3m multiplied by 2m multiplied by 4m, and the total effective volume is 21m 3 Effective volume of C1 of anaerobic-anoxic reaction tank is 5m 3 The reaction chamber is divided into 18 reaction chambers connected in series by a guide plate; the aerobic reaction tank C2 is divided into 2 grids, and the effective volume of each grid is 6m 3 (ii) a Effective volume of sedimentation tank C3 is 2m 3 And the effective volume of the sludge temporary storage tank is 2m 3 . By dividing a plurality of reaction chambers, the substrate in the inlet water is fully contacted with the microorganisms to be degraded and removed, and simultaneouslyThe reactor is promoted to form an organic matter concentration gradient along the flow path, the length of an endogenous respiration segment is prolonged, and the satiety and hunger ratio is reduced, so that the formation of granular sludge is promoted.
The device of the VBRs bioreactor comprises an aeration pump 14, a gas flowmeter 12, an aeration head (11), a water quality online detection device 16, a PH probe, a DO probe and an ORP probe 15. The reactor was run as follows: municipal sewage enters a VBRs reactor through a water inlet pump after being pretreated by a sewage treatment plant; dissolved oxygen is connected with a micropore aeration pipe through an aeration pump 14 to provide oxygen for the VBRs, and the aeration amount is controlled through a gas flowmeter 12; the reflux system comprises an anaerobic reflux ball valve 5, an anoxic reflux pipe 6, an anoxic reflux ball valve 7, a nitrifying liquid reflux pipe 8, a nitrifying liquid reflux ball valve 9 and a sludge reflux ball valve 18; effluent automatically flows into the effluent pool through the effluent weir 21, and in the running process of the reactor, the temperature of 18-25 ℃ is a normal temperature running stage, and the temperature of 6-11 ℃ is a low temperature running stage.
The specific operation is as follows:
directly adding activated sludge taken from an aerobic tank of a domestic sewage treatment plant into wastewater of a VBRs reactor by a sludge lifting pump, and performing smoldering explosion for 2 days; simultaneously starting each group of reflux to disperse the sludge into each reaction tank, wherein the reflux ratio of the sludge is 240 percent, and then introducing wastewater to the effective working volume of the reactor, wherein the inoculated sludge is flocculent sludge, the sludge concentration is 5500mg/L, the sludge concentration in the aerobic reaction tank at the starting stage is 3000-3500mg/L, and the sludge concentration in the anaerobic reaction tank is 4500-5000mg/L;
1) And (3) starting a system: equipment debugging, sludge acclimation and granular sludge formation. The running time of the system at normal temperature is 15 days, and the VBRs reactor continuously feeds water and discharges water; the aeration and sludge reflux period is 30min, and the specific operation mode in each period is as follows: the reactor is operated under the condition of room temperature (the water inlet temperature is 18-25 ℃); the wastewater is pretreated by a domestic sewage treatment plant and then is conveyed into the VBRs reactor through a water inlet pump, pulse type water inlet is adopted for water inlet, so that in the grid area flowing upwards, sludge forms a suspended sludge bed due to the upward flow velocity of the wastewater, and the formation of granular sludge is facilitated. The anaerobic zone and the anoxic zone are provided with guide baffle plates, the reactor is divided into 18 reaction chambers connected in series, and water flow is guided by the guide baffle plates to flow upwards and downwards to enter the aerobic zone; the aeration pump is started to carry out aerobic aeration, the longitudinal water flow and the ascending aeration provide stronger and more three-dimensional hydraulic shearing force for the sludge-water mixed liquid together, the collision friction among the sludge is enhanced, the secretion of extracellular polymers is promoted, and the formation of aerobic granular sludge is promoted. Monitoring the dissolved oxygen concentration DO by a DO probe of the water quality on-line detector, controlling the dissolved oxygen concentration DO to be between 3.0 and 5.0mg/L, and stopping aeration for 8min after continuous aeration for 22 min; starting sludge reflux and nitrification liquid reflux in the aeration process, and closing after the aeration is stopped; anaerobic reflux and anoxic reflux are always kept in an open state, so that the water inlet load is reduced. A sludge discharge port is arranged at the bottom of the sedimentation tank, sludge is discharged to a temporary sludge storage tank once every 2 days, the sludge age is controlled to be 5 days, and the sludge concentration of an aerobic tank in the reactor is controlled to be 3000mg/L; the COD concentration of the effluent of the reactor at the starting stage of the system is 12mg/L, the removal rate is more than 90 percent, the ammonia nitrogen concentration is 0.446mg/L, the removal rate is more than 90 percent, the total phosphorus concentration is 0.1mg/L, the removal rate is more than 90 percent, the total nitrogen concentration is 12mg/L, and the removal rate is more than 60 percent.
2) The system operates as follows when running:
2.1 System parameter optimization: urban domestic sewage enters the VBRs reactor, inflow is controlled through a flow meter, the Hydraulic Retention Time (HRT) of the system is changed, the system continuously operates for 15 days under the conditions that the HRT is 169h, 20h and 24h, and the effluent quality and the removal rate are as follows:
the aeration quantity is adjusted to be 0.8,1.2,1.6m 3 And respectively operating for 15 days under the condition of/h, and monitoring the DO change of the dissolved oxygen concentration in the water in real time through a DO probe of the water quality online detector. Finally, the optimal HRT of the reaction is determined to be 20h, and the water inlet flow is 1m 3 H, aeration rate of 1.2m 3 /h。
2.2 Stable operation at normal temperature): continuously feeding water at 18-25 ℃ under the optimized system operation parameters, and controlling the water quality of the fed water to ensure that the COD concentration is 180-242mg/L, the ammonia nitrogen concentration is 15.52-28.11mg/L, the total nitrogen concentration is 22.90-46.23mg/L, and the total phosphorus concentration is 1.55-5.03mg/L. The system has stable effluent, can realize ultralow discharge of effluent, and has COD concentration less than 15mg/L, removal rate of over 92 percent, ammonia nitrogen concentration less than 0.2mg/L, removal rate of over 98 percent, total nitrogen concentration less than 8mg/L, removal rate of over 75 percent, total phosphorus concentration less than 0.1mg/L and removal rate of over 99 percent.
2.3 Impact load resistance capacity): continuous water inflow is carried out under the optimized system operation parameters, the fluctuation of the sewage quality is large, and the short-time water inflow is abnormal (COD)>1000mg/L，C/N>30；TN>100mg/L，C/N<3) Does not influence the water outlet of the reactor and is in continuous C/N<After the operation is carried out for 12 hours under the condition of 3, the total nitrogen removal rate of the effluent is reduced to below 60 percent; controlling the water inflow by a flowmeter, and continuously operating the reactor below the normal water inflow condition when the water inflow rises to 1.4m 3 Continuously operating for 12 h/h, increasing the ammonia nitrogen concentration of the effluent to 3-5mg/L, the total nitrogen concentration to be below 12mg/L, the total phosphorus concentration to be below 0.2mg/L and the COD concentration to be below 30 mg/L.
2.4 System operation at low temperature and granular sludge culture: the reactor is continuously operated in winter, the inlet water is the actual domestic sewage treated by a domestic sewage treatment plant, and the water temperature is kept between 6 and 11 ℃. The aeration and reflux period of the reactor is 1h, and the specific operation mode in each period is as follows: aerating continuously for 52min, stopping aerating for 8min, starting sludge backflow and digestive juice backflow in the aeration process, and closing after the aeration is stopped; the anoxic internal reflux is always kept in an open state. Discharging sludge once every 4 days to a temporary sludge storage tank, controlling the sludge age to be 12 days, and controlling the sludge concentration of an aerobic tank in the reactor to be 5000mg/L. During the low-temperature stable operation, the COD concentration of the effluent of the reactor is less than 30mg/L, the removal rate is more than 93%, the ammonia nitrogen concentration is less than 0.5mg/L, the removal rate is more than 90%, the total nitrogen concentration is less than 15mg/L, the removal rate is more than 60%, the total phosphorus concentration is less than 0.1mg/L, and the removal rate is more than 99%. The water quality indexes of the effluent are all superior to GB18918 first-grade A discharge standard.
2.5 Fast start after system failure: the system stops water feeding, aeration and backflow for 12-36h, and then continuously feeds water and keeps 1m by adjusting the operation parameters 3 The flow per hour is increased, the sludge reflux ratio is increased to 300%, aeration is recovered, the sludge concentration in the aerobic reaction tank is controlled to be 5000mg/L through continuous sludge discharge after 24 hours, and the system can recover normal operation and normal water discharge after three days.
The reactor is operated according to the method, and the aerobic granular sludge in the system is analyzed as follows: in a granular sludge SEM image, the surfaces of granules are covered by filamentous bacteria, some short-rod bacteria are tightly wrapped, and meanwhile, a pore structure appears, so that the degradation and removal of pollutants are realized through the synergistic effect of different bacteria; the concentration of Extracellular Polymeric Substances (EPS) is kept at 32 mg/(g.MLSS) during stable operation, and the aggregation of microorganisms is effectively promoted; the analysis result of the functional flora shows that the aerobic sludge contains most varied bacteria, the nitrosation spirillum is a dominant bacterium on the level, and the functional bacteria such as Candidatus-Accumulibacter and the like are also available. Practice proves that the coexistence of various functional bacteria can achieve the effect of removing various pollutants at the same time; the result proves that the invention can well form aerobic granular sludge in the process of treating domestic sewage in a continuous flow mode and has excellent denitrification and dephosphorization effects.
Claims (1)
1. The utility model provides a vertical-flow type realizes device of synchronous nitrogen and phosphorus removal of villages and small towns domestic sewage through granular sludge at low temperature which characterized in that: the device comprises an anaerobic-anoxic reaction tank (C1), an aerobic reaction tank (C2), a sedimentation tank (C3), a water inlet tank (1), a water inlet pump (2), a guide baffle plate (3), an anaerobic return pipe (4), an anaerobic return ball valve (5), an anoxic return pipe (6), an anoxic return ball valve (7), a nitrified liquid return pipe (8), a nitrified liquid return ball valve (9), an aeration valve (10), an aeration head (11), a gas flowmeter (12), an aeration pipe (13), an aeration pump (14), DO, PH, an ORP probe (15), a water quality online detector (16), a sludge return pipe (17), a sludge return ball valve (18), a sludge discharge ball valve (19), a sludge temporary storage tank (20), a water outlet weir (21), a water outlet valve (22), a water outlet pipe (23), a water outlet tank (24) and an anoxic water outlet (25);
the anaerobic-anoxic reaction tank (C1), the aerobic reaction tank (C2) and the sedimentation tank (C3) are sequentially adjacent, the anaerobic-anoxic reaction tank (C1) is composed of eighteen reaction compartments connected in series, an anoxic water outlet (25) is formed between the anaerobic-anoxic reaction tank (C1) and the aerobic reaction tank (C2) and is communicated with the aerobic reaction tank (C2), guide baffle plates (3) are arranged between the reaction compartments in the transverse direction, the guide baffle plates (3) are arranged in a mode that a flow channel is formed between the bottom end of the first guide baffle plate (3) and the tank floor of the anaerobic-anoxic reaction tank (C1), and the top of the first guide baffle plate (3) is flush with the tank top of the anaerobic-anoxic reaction tank (C1); the bottom end of the second guide baffle plate (3) is tightly connected with the anaerobic-anoxic reaction tank (C1), the top end of the second guide baffle plate (3) is lower than the top end of the anaerobic-anoxic reaction tank (C1), and the second guide baffle plate and the top end are arranged in succession, so that the muddy water mixed liquor enters the second row of reaction chambers from the bottom of the guide baffle plate (3) of the first row of reaction chambers, then enters the third row of reaction chambers from the top of the guide baffle plate (3) of the second row of reaction chambers, and finally flows into the aerobic reaction tank (C2) from the anoxic water outlet (25) of the anaerobic-anoxic reaction tank (C1); the height of the guide baffle plate (3) is gradually reduced along the water flow direction;
an anaerobic return pipe (4) and an anoxic return pipe (6) are arranged in the anaerobic-anoxic reaction tank (C1), an anaerobic return ball valve (5) is arranged on the anaerobic return pipe (4), and an anoxic return ball valve (7) is arranged on the anoxic return pipe (6);
a separation plate (C21) is arranged between the aerobic reaction tank (C2) and the sedimentation tank (C3);
the water inlet tank (1) is communicated with a first reaction grid of the anaerobic-anoxic reaction tank (C1) through a water inlet pump (2) and a pipeline, a nitrifying liquid return pipe (8) is arranged between the anaerobic-anoxic reaction tank (C1) and the aerobic reaction tank (C2), and a nitrifying liquid return ball valve (9) is arranged on the nitrifying liquid return pipe (8);
an aeration device is arranged at the bottom of the aerobic reaction tank (C2), the aeration accessories comprise an aeration head (11), an aeration valve (10), an aeration pipe (13) and an aeration pump (14), one end of the aeration valve (10) is connected with the aeration head (11) at the bottom of the aerobic reaction tank (C2), the other end of the aeration valve (10) is connected with the aeration pump (14) through the aeration pipe (13), and a gas flow meter (12) for detecting the aeration intensity is arranged on the aeration pipe (13);
the sedimentation tank (C3) is provided with an effluent weir (21), the top of the effluent weir (21) is communicated with an effluent tank (24) through an effluent valve (22) and an effluent pipe (23), and the bottom of the effluent weir (21) is communicated with a temporary sludge storage tank (20) through a pipeline and a sludge discharge ball valve (19);
the bottom of the effluent weir (21) is communicated with a sludge return pipe (17) through a sludge return ball valve (18), and the sludge return pipe (17) is communicated with an anaerobic-anoxic reaction tank (C1) and an aerobic reaction tank (C2); the mixed liquid in the aerobic reaction tank (C2) enters the middle part of the sedimentation tank (C3) from a flow channel at the bottom, then flows from bottom to top, the flow velocity of water flow is gradually slowed down, sludge is settled at the bottom, a sludge discharge port is arranged at the bottom, the sludge can be discharged into a temporary sludge storage tank (20) under the control of a sludge discharge ball valve (19), water passes through a settled sludge layer to go upwards, and supernatant is discharged into a water outlet tank (24) through a water outlet pipe (23) under the control of a water outlet valve (22) after being collected by a water outlet weir (21);
DO, PH and ORP probes (15) of the water quality on-line monitor (16) are arranged on the upper part of the aerobic reaction tank (C2) to detect the dissolved oxygen concentration, PH and OPR values on line at any time.
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