CN101891345A - Reinforced simultaneous nitrogen and phosphorus removal sewage treatment equipment and method for municipal sewage with low carbon source at low oxygen concentration - Google Patents
Reinforced simultaneous nitrogen and phosphorus removal sewage treatment equipment and method for municipal sewage with low carbon source at low oxygen concentration Download PDFInfo
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Abstract
The invention provides reinforced simultaneous nitrogen and phosphorus removal sewage treatment equipment and a method for municipal sewage with a low carbon source at low oxygen concentration. The equipment is composed of an SBR main reaction tank and two dephosphorizing tanks, wherein, the water inlet pipe of the SBR main reaction tank is led in from the upper part of the reaction tank, the water outlet pipe thereof is led out from the lower part of the reaction tank, and an external circulation sludge pipe is led out from the bottom of the SBR main reaction tank; the SBR main reaction tank is equipped with an aerating apparatus; and the SBR main reaction tank adopts an operation mode of water inflow in batches, and anaerobic-aerobic/anoxic alternation and sedimentation and drainage. The two dephosphorizing tanks have identical structure size and are respectively taken as an anaerobic phosphorus release tank and a chemical dephosphorizing tank in the same cycle for sewage treatment, and functions of the two tanks are exchanged in the next cycle. The invention can well realize reinforced simultaneous nitrogen and phosphorus removal treatment for the municipal sewage with a low carbon source under a low dissolved oxygen environment.
Description
Technical field
The invention belongs to technical field of sewage, the substep water-feeding SBR waste disposal plant and the method for particularly a kind of hypoxia condition reinforced low-carbon source sewage denitrification and dephosphorization are applicable to that cities and towns hang down the synchronous dephosphorization denitrogenation of carbon source sanitary sewage.
Background technology
Along with the aggravation of body eutrophication situation, how to guarantee that the dephosphorization denitrogenation removal effect that town sewage is handled has become inevitable problem.And the carbon source that synchronous biological denitrogenation dephosphorizing Sewage treatment systems exists is competed, mud contradiction in age, causes the municipal sewage plant to be difficult to obtain simultaneously excellent dephosphorization and denitrification effect.Especially in some southern cities, its sanitary sewage average COD concentration is lower than 200mg/L, and nitrogen, phosphorus concentration are higher relatively, COD/TN is usually below 5, COD/TP then is lower than 35, for this low carbon source city domestic sewage, guarantee simultaneously that dephosphorization and denitrification effect is just difficult more.How to realize the synchronous denitrification dephosphorizing of low carbon source urban sewage at low cost, become the technical barrier of having to face in this field.
At present more about the development research of effective denitride technology of low carbon source sewage, but the rare research report of seeing specially at the synchronous dephosphorization denitrogenation of reinforcement of low carbon source urban sewage.When handling low carbon source urban sewage, traditional treatment method mainly faces following several respects problem: the required aeration rate of (1) nitrifying process is than the shortage of big and denitrification organic carbon source.In traditional SBR technology, the disposable reactor that enters of sewage, organism and ammonia nitrogen all need to experience aerobic, the hypoxia response section in whole cycle, heterotrophic bacterium can preferentially utilize dissolved oxygen to carry out the oxidation operation decomposition when aeration began, nitrifier is not had an advantage in competition, thereby needs to strengthen aeration rate to guarantee nitrification effect; And in this higher dissolved oxygen environment, the organism in the system can excessively oxidatedly cause follow-up anoxic section to lack the required carbon source of denitrification again.Therefore when traditional technology is handled low carbon source sewage, often aerobic section needs aeration rate big and the anoxic stage needs to add in addition carbon source to satisfy de-nitrification requirements, causes power consumption and medicine to add the cost increase.(2) the sludge age contradiction between dephosphorization and the denitrogenation.Tradition dephosphorization mode is to remove phosphoric acid salt in the sewage by getting rid of rich phosphorus excess sludge, and the treatment system sludge age is short more to be beneficial to dephosphorization more; And the guaranteed prerequisite of Nitrogen removal effect is good nitrification effect, because the nitrobacteria rate of propagation is slow, this just requires the long sludge age of system held.Therefore, traditional technology is often handled the sludge age contradiction between bad denitrogenation and the dephosphorization, causes dephosphorization denitrogenation not take into account.(3) competition of the carbon source between the dephosphorization denitrogenation.Traditional biological dephosphorization mode need absorb low molecular organic material and release phosphorus simultaneously in the anaerobism section could be at aerobic section excess suction phosphorus.And heterotrophic denitrification also needs organism as electron donor.Therefore, unavoidably have the competition of carbon source between the denitrogenation dephosphorizing, this contradiction is more apparent outstanding under the lower situation of entering organic matter of water.
In addition, research report about the substep water-feeding SBR technology with strengthened denitrification effect is also arranged both at home and abroad much in recent years, but process object is generally the intermediate concentration municipal effluent, and main research is how to improve denitrification effect, rare seeing specially reported at the research of the synchronous dephosphorization and denitrification effect that how to improve low carbon source urban sewage, and also do not seen the research report of strengthening synchronous dephosphorization denitrogenation specially at low carbon source urban sewage under the low dissolved axygen condition as yet.
Summary of the invention
At above problem, the invention provides a kind of SBR waste disposal plant and method of using substep water intake mode synchronous dephosphorization denitrogenation of reinforced low-carbon source urban sewage under the low dissolved axygen environment.
Technical scheme of the present invention is as follows:
The waste disposal plant of the synchronous dephosphorization denitrogenation of a kind of reinforced low-carbon source urban sewage hypoxemia, it is made of SBR main reaction pond and two dephosphorization pond A and B.
The water inlet pipe in described SBR main reaction pond is inserted by top, rising pipe is picked out by the bottom, and bottom SBR main reaction pond, pick out the outer circulation sludge pipe, be provided with aerating apparatus in SBR main reaction pond, described SBR main reaction pond adopt water inlet in batches, anaerobic-aerobic/anoxic alternately-operation scheme of sedimentation and drawing.
Described dephosphorization pond A and dephosphorization pond B insert the anaerobic phosphorus releasing pool water inlet pipe respectively from top, the bottom picks out water shoot respectively, and the flow direction of water is two-way in the water shoot, and the sewage of promptly releasing behind the phosphorus both can flow to pond B from pond A, also can flow to pond A, decide on two pond functions from pond B.(sludge stream in the pipe is to also being two-way for the outer circulation sludge pipe that is picked out by SBR main reaction pond, when one-period finishes, part aerobic sludge in the SBR main reaction pond is for flowing out, but this part aerobic sludge release at pond A or pond B can flow back to SBR main reaction pond again after phosphorus finishes).Insert dephosphorization pond A and dephosphorization pond B respectively by sludge pipe respectively, dephosphorization pond A and dephosphorization pond B pick out waste pipe again respectively and insert SBR main reaction pond by the sewage backflow pipe from the bottom.Shore pipe is connected with sludge pipe, and pipe is to pass through valve closes always when not arranging chemical sludge, and only from pond A or pond B eliminating chemical sludge the time, just the valve open with shore pipe carries out spoil disposal.Be provided with agitator in dephosphorization pond A and the dephosphorization pond B.
Described dephosphorization pond A and dephosphorization pond B structure size are identical, and in the same one-period of sewage disposal, it is respectively as anaerobic phosphorus releasing pool and chemical dephosphorization pond, in the then function exchange in two ponds of next cycle.
The present invention has also further proposed to utilize said apparatus to carry out the method for sewage disposal, and its process is as follows:
Substep water inlet, (anaerobism) anoxic/aerobic alternative mode are adopted in SBR main reaction pond, be that SBR main reaction pond makes sewage distinguish the anoxic section of injecting reactor several times under anaerobic-aerobic/anoxic alternative operational mode, make SBR main reaction pond be in the low dissolved axygen environment by the control aeration rate simultaneously at aerobic stage; In SBR main reaction pond operation (after being actually each end cycle draining, part aerobic sludge in the SBR main reaction pond is arranged into anaerobic phosphorus releasing pool by the outer circulation sludge pipe in SBR main reaction pond and is carried out anaerobic phosphorus release, this part outer circulation mud is discharged SBR main reaction pond and is independently strengthened later on and release phosphorus, mud-water separation, processes such as backflow, and the SBR main reactor still moves according to time reaction time of oneself later at this part outer circulation mud of discharge, the reinforcement of circulating sludge is outside released the phosphorus process and is all over and can be back to the anaerobic stages of SBR main reaction pond next cycle after the draining, and all to release phosphorus independent and carry out simultaneously with the outer circulation sludge anaerobic of last one-period therefore can to think the reaction of SBR main reactor in each cycle).Outer circulation mud is arranged into anaerobic phosphorus releasing pool by the outer circulation sludge pipe in SBR main reaction pond and is carried out anaerobic phosphorus release, after releasing phosphorus end mud-water separation, rich phosphorus sewage enters the chemical dephosphorization pond through water shoot to carry out chemistry and consolidates phosphorus, Gu the sewage behind the phosphorus refluxes into SBR main reaction pond with further removal ammonia nitrogen and organic substance wherein through the sewage backflow pipe.
In aforesaid method, described SBR main reaction pond is in arbitrary reaction time, all having the mud outer circulation that accounts for total sludge quantity 15% to participate in anaerobism to pond A or pond B strengthens and releases phosphorus, the outer circulation mud of promptly going up one-period is back to the anaerobism section in SBR main reaction this cycle of pond and participates in the effect of follow-up suction phosphorus behind anaerobic phosphorus release, the outer circulation mud in this cycle then is back to the anaerobism section of SBR main reaction pond next cycle behind anaerobic phosphorus release.
Among the present invention, substep water inlet, (anaerobism) anoxic/aerobic alternative mode are adopted in SBR main reaction pond, be that SBR main reaction pond makes sewage distinguish the anoxic section of injecting reactor several times under anaerobic-aerobic/anoxic alternative operational mode, make SBR main reaction pond be in the low dissolved axygen environment by the control aeration rate simultaneously at aerobic stage.The operation scheme of substep water inlet has realized the limited more rational distribution of organic carbon source in the water inlet, the organism that reaction tank is brought in first water inlet into is fully adsorbed, absorbs and cause that organic concentration reduces rapidly in the system by microorganism in the anaerobism section, make the heterotrophic bacterium in the system not have competitive edge at the aerobic section that is right after, at the aerobic section that does not have the heterotrophic bacteria competition, keep lower dissolved oxygen concentration and just can guarantee that the autotrophy nitrifier given play to good nitrated usefulness, and can save aeration rate, reduce running cost.Substep water inlet and aerobic/anoxybiotic operation scheme make the heterotrophic denitrification bacterium carry out denitrification at the organic substance that the anoxic section of each water inlet makes full use of in the water into as carbon source, thus raising organism utilization ratio and denitrification effect.Thisly will substep water intake mode and low dissolved axygen control process combined and promptly can solve ammonia nitrogen halfway drawback of oxidation under the low dissolved axygen environment, can avoid organism excessively oxidated and can not be used as denitrifying carbon source under the high-solubility oxygen environment again.Simultaneously, utilize the excess suction phosphorus ability of polyP bacteria that low phosphorus hydrochlorate in the sewage is enriched in the polyP bacteria body, derive the rich phosphorus sludge of small part again and mixes the back reinforcement with sewage that COD concentration is about 300mg/L to the dephosphorization pond A (or B) and release phosphorus, and phosphorus is removed from system by getting rid of rich phosphorus sewage; Last rich phosphorus sewage carries out the solid phosphorus of chemistry in dephosphorization pond B (or A) handles.This dephosphorization mode is compared with getting rid of rich phosphorus sludge dephosphorization mode, needn't require the short sludge age of system held, can solve the sludge age contradiction between the denitrogenation dephosphorizing, again can more effective assurance sewage in the removal effect of TP.In addition, the dephosphorization mode that the rich phosphorus sewage of this row carries out chemical fixation helps to reduce consumption of chemical agent, reduces cost.
Advantage of the present invention
(1) at low carbon source urban sewage, the operation scheme of substep water inlet can realize the properly distributed to organic carbon source limited in the water inlet, carbon source is effectively absorbed in anaerobism section and anoxic section, make heterotrophic bacterium not have competitive edge at aerobic section, take low dissolved axygen control just can guarantee the good nitrated usefulness of autotrophy nitrifier performance at the aerobic section that does not have the heterotrophic bacteria competition, save aeration rate, reduced running cost.
(2) substep water inlet, anaerobic-aerobic/anoxic alternative operation scheme can improve system's nitrification and denitrification effect simultaneously, thereby improve denitrification effect.In traditional single step water-feeding SBR technology, sewage is disposable to be injected in the reactor, pass through aerobic in turn, the anoxic course, certainly will cause the waste of invalid oxidation of organism and aeration rate like this: because the disposable system that enters of sewage causes system to have the organic concentration gradient in time, it is higher and reaction later stage organism lacks promptly to begin organic concentration, therefore at the beginning aeration initial stage, heterotrophic bacterium has superiority in the system, at first utilizing oxygen in water to carry out oxidation operation decomposes, and nitrifier is in a disadvantageous position in competition and can not carries out nitration reaction immediately, cause organic oxidation waste in the sewage, just can carry out denitrification denitrogenation and often need additionally to add carbon source material, certainly will increase running cost like this to system in the anoxic section; Just because of this, traditional treatment method often by increasing aeration rate to exchange better nitrification effect for, causes the waste of organic faster decomposition and aeration rate.Limited carbon source in the more rational dispensing water of water intake mode of substep, organism is adsorbed fast in the anaerobism section in the first step water inlet, after the absorption, ammonia nitrogen can be oxidized to nitrate nitrogen rapidly at the aerobic section that is right after, utilize the organism in the second stepping water to carry out denitrification denitrogenation again, organism in the second stepping water carries out aeration to system after by denitrifying bacteria utilization fully again, owing to there is not more organic substance heterotrophic bacterium just can not utilize oxygen in the sewage prior to nitrobacteria, even under the very low condition of dissolved oxygen, still can obtain good nitrification effect, realize the low good denitrogenation of carbon source sewage under the low dissolved axygen environment.
(3) the effluent dephosphorization mode that effluxes the rich phosphorus sewage of anaerobism makes system can keep sludge quantity, solved the technical problem that denitrogenation dephosphorizing that low carbon source urban sewage denitrogenation and dephosphorization contradiction causes can not be taken into account, made system can be under long sludge age condition not only guarantee denitrification effect but also can keep the dephosphorization ability of good stable.
Description of drawings
Fig. 1 is a reinforced low-carbon source urban sewage hypoxemia synchronous denitrification dephosphorizing sewage treatment process apparatus structure synoptic diagram of the present invention.
Fig. 2 is a reinforced low-carbon source urban sewage hypoxemia synchronous denitrification dephosphorizing sewage treatment process device floor map of the present invention.
Fig. 3 is the process flow sheet of reinforced low-carbon source urban sewage hypoxemia synchronous denitrification dephosphorizing waste disposal plant operation of the present invention.
Among the figure, 1-SBR main reaction pond, 2-dephosphorization pond A, 3-dephosphorization pond B, 4-SBR pond water inlet pipe, 5-anaerobic phosphorus releasing pool water inlet pipe, the 6-aeration tube, 7-SBR pond rising pipe, the 8-micro porous aeration head, the 9-agitator, 10-outer circulation sludge pipe, 11-pond A sludge pipe, 12-pond B sludge pipe, 13-pond A waste pipe, 14-pond B waste pipe, the 15-water shoot, 16-sewage backflow pipe, the 17-shore pipe, 18-intake pump time controller, 19-air compressor machine time controller, 20-strains the hydrophone time controller, 21-agitator time controller, the 22-gas meter, 23-strains hydrophone, 24-anaerobic pond agitator, 25-chemical dephosphorization pond agitator.
Embodiment
The combination and the operation operation that further describe apparatus of the present invention below in conjunction with Fig. 1, Fig. 2 and Fig. 3 are elaborated:
This waste disposal plant is to be made of SBR main reaction pond 1 and dephosphorization pond A2 and dephosphorization pond B3, the water inlet pipe 4 in SBR main reaction pond is inserted by the top in SBR main reaction pond 1, rising pipe 7 is picked out by the bottom, and pick out the outer circulation sludge pipe 10 that can two-way circulate from the bottom in SBR main reaction pond 1, in SBR main reaction pond 1, aerating apparatus is set, SBR main reaction pond adopt water inlet in batches, anaerobic-aerobic/anoxic alternately-operation scheme of sedimentation and drawing.
Dephosphorization pond A2 and dephosphorization pond B3 have access to anaerobic phosphorus releasing pool water inlet pipe 5 respectively from top, and be connected to the water shoot 15 (pipe of this water shoot) that is interconnected for two-way circulating in the bottom in two ponds, and be connected with dephosphorization pond B3 with dephosphorization pond A2 respectively with 12 by sludge pipe 11 by the outer circulation sludge pipe 10 that SBR main reaction pond 1 picks out.Dephosphorization pond A2 and dephosphorization pond B3 pick out waste pipe 13 and 14 and insert SBR main reaction ponds 1 by sewage backflow pipe 16 again respectively from the bottom.Sludge pipe 11 also is connected with shore pipe 17 with 12, do not arrange chemical sludge the time, shore pipe 17 is by valve closes, only when dephosphorization pond A2 and dephosphorization pond B3 get rid of chemical sludge, just the valve open with shore pipe 17 carries out spoil disposal; Be provided with agitator 24 and 25 in described dephosphorization pond A2 and the dephosphorization pond B3.
Dephosphorization pond A2 and dephosphorization pond B3 structure size are identical, and in the same one-period of sewage disposal, it is respectively as anaerobic phosphorus releasing pool and chemical dephosphorization pond, in the then function exchange in two ponds of next cycle.
In this device, the water inlet pipe of SBR main reaction pond 1, dephosphorization pond A2 and dephosphorization pond B3 is controlled by a total intake pump time controller.The aerating apparatus in SBR main reaction pond 1 is equipped with gas meter 22 by 19 controls of an air compressor machine time controller on its supply air line.Agitator 24 among dephosphorization pond A2 and the dephosphorization pond B3 and 25 is by 21 controls of agitator time controller.Be provided with in the water inlet position of the rising pipe 7 in SBR main reaction pond and strain hydrophone 23, the described hydrophone 23 of straining is strained hydrophone time controller (20) control.
It is as follows to utilize said apparatus to carry out the method for sewage disposal:
(1) SBR main reaction pond operation operation (is example to divide three stepping water):
1. water inlet for the first time: set flooding time according to setting flooding quantity, i.e. flooding quantity=flooding velocity * flooding time, flooding velocity is controlled by the liquid meter on the suction culvert; Intake pump is controlled by the time controller that is connected with water intaking valve, when the cycle begins intake pump under the control of time controller 18 with sewage through water inlet pipe 4 suction SBR main reaction ponds 1, when flooding quantity reached set(ting)value, intake pump was closed, and whole flooding time is controlled within the 10min.
2. anaerobism stirs: the agitator in the SBR main reaction pond is also by corresponding time controller control, after water inlet is finished for the first time, agitator 9 is opened to stir under the control of time controller 21 and is made into water and mud thorough mixing in the SBR main reaction pond, stops to stir when SBR main reaction pond begins to precipitate; This moment, air compressor machine was in closing condition, mixed solution in the whole SBR main reaction pond is in anaerobic state, organic substance in the denitrifying bacteria utilization water inlet carries out cycle residual nitric acid salt nitrogen in the denitrification removal system, and the VFA material in the polyP bacteria utilization water inlet carries out anaerobic phosphorus release.The anaerobism time is controlled at 1.0～1.5h, after anaerobism stirs beginning 30min, the mud of releasing among the pond A (2) behind the phosphorus is back to SBR main reaction pond 1 through outer circulation sludge pipe 10, utilization is released in polyP bacteria behind the phosphorus and the reaction tank and is gone up the effect of one-period residual nitric acid salt nitrogen generation denitrifying phosphorus uptake (promptly, reflux release mud behind the phosphorus can be immediately after being back to the anaerobism section with SBR main reaction pond on the effect of one-period residual nitric acid salt nitrogen generation denitrifying phosphorus uptake, and in SBR main reaction pond follow-up aerobic section also will participate in the effect of aerobic suction phosphorus).
3. aeration for the first time: after anaerobism finishes, aeration time controller 19 control air compressor machines begin aeration, air by aeration tube 6 by micro porous aeration head 8 to system's oxygenation, and, make SBR main reaction pond be in the hypoxemia good oxygen condition of DO concentration at 0.3～0.6mg/L by gas meter 22 control aeration rates; Under low DO environment, nitrococcus and nitrifier are with the ammonia nitrogen oxidation in the sewage, and polyP bacteria utilizes the phosphoric acid salt in the oxygen absorption sewage; When DO concentration in the SBR main reaction pond begins to rise to 1.0 when above, stop aeration.
4. water inlet for the second time: 1. with operation.
5. anoxia stirring: during water inlet beginning for the second time, air compressor machine is closed, and agitator 9 is still opened.After water inlet was finished, agitator continued to stir, and the main reaction pond is in anoxic condition at this moment, and the organic substance in the denitrifying bacteria utilization water inlet carries out the heterotrophic denitrification denitrogenation, removes the nitrate nitrogen that a last aeration phase produces.
6. aeration for the second time: 3. with operation.
7. water inlet for the third time: 1. with operation.
8. anoxia stirring: 5. with operation.
9. the back is aerobic: after three water inlets were finished and carried out anoxia stirring, aeration time controller 19 control air compressor machines began the final stage aeration, further to remove ammonia nitrogen residual in the system, organic substance and phosphoric acid salt.After DO concentration rises to 2.0mg/L in the SBR pond, stop aeration.
10. sedimentation and drawing: after last aeration phase was finished, air compressor machine, agitator 9 were closed, and mud-water separation is carried out in the sbr reactor pond.Treat that sludge settling to after SBR main reaction pond liquid level is below half, opens the valve of water shoot 7, strain hydrophone 23 and start under the control of time controller 20 and carry out draining that draining is closed the water shoot valve after finishing, system enters the next cycle circulation.
(2) effluent dephosphorization pond operation operation
A) inhaling the phosphorus sludge outer circulation strengthens and releases phosphorus: SBR main reaction pond finish operation 10. after, open the valve of outer circulation sludge pipe 10, make aerobic suction phosphorus sludge in the pond (account for total sludge quantity 15%) flow to pond A (pond A is as anaerobic phosphorus releasing pool) certainly herein, after treating that outer circulation mud enters pond A fully, close outer circulation sludge pipe valve, and in the pond, inject raw waste water (regulate COD be about 300mg/L) by waste pipe 5, the sludge quantity volume ratio among its amount of water and the pond A is 1: 1; After sewage injects and to finish, open agitator 24 in the anaerobic phosphorus releasing pool, carry out anaerobism stir (1.5～2.0h), make the phosphate concn that discharges in the pond reach 35～40mg/L; After releasing the phosphorus end, close agitator 24 and carry out mud-water separation; And SBR main reaction pond enters the next cycle circulation after discharging outer circulation mud.
B) releasing phosphorus sludge refluxes: after treating that the SBR pond enters anaerobism agitating procedure 30min, the last one-period among the B of pond has been released the outer circulation mud that phosphorus, draining finishes (account for total sludge quantity 15%) be back to SBR main reaction pond, the aerobic suction phosphorus of participation follow-up phase.
C) chemical dephosphorization: open between pond A and the pond B water shoot 15 valves, be rich in phosphatic supernatant liquor among the A of pond and enter pond B by water shoot 15, the rich phosphorus supernatant liquor water yield that enters pond B is identical with the flooding quantity of anaerobic phosphorus release; After draining is finished, close water shoot 15 valves, in the B of pond, add chemical dephosphorization agent (lime), and turn on agitator 25 stirs and phosphoric acid salt is fully contacted carry out coagulating sedimentation, by shore pipe 17 discharges of bottom, pond.And the mud among the A of pond will be back to the anaerobic stages (be pond A at next cycle with the pond B among the operation b) in SBR pond at next cycle;
D) sewage backflow: supernatant liquor among the B of pond is back to SBR main reaction pond 1 by sewage backflow pipe 16 aeration phase is with nitrogen and organism in the further removal sewage, and the pond B after the emptying will be at next cycle as anaerobic phosphorus releasing pool (be pond B at next cycle with the pond A among the operation a).
Concrete application example 1: the sanitary sewage with University Of Chongqing's campus discharging is a process object, a device day processing water yield is 200L, divide 2 stepping water (the water inlet ratio is 4: 3), operation condition is: aerobic 40min-sedimentation and drawing 2h behind the aerobic 40min-anoxic of aerobic 2.5h-water inlet 3L, the anoxic 50min-of water inlet 4L, the anaerobism 1h-20min-, the average C/N=3.9 of intaking, COD 86～186mg/L, NH
3-N 20～35mg/L, TN 21～38mg/L, TP 4-8mg/L, pH value 7-8, test temperature is 20-24 ℃.Test-results shows: aerobic section unit volume aeration rate is 3.57m when control SBR main reaction pond
3/ hm
3, the average DO concentration of aerobic section is about 0.16mg/L, and system sludge reaches under the situation of 80d age, system's effluent COD concentration is less than 30mg/L; The water outlet NH of system
3-N concentration is below 3.5mg/L, and average removal rate is 99%; System's water outlet TN concentration is lower than 14mg/L, and average removal rate reaches 63.3%; System's water outlet TP concentration is less than 0.5mg/L, and average removal rate surpasses 93%, and water outlet reaches " urban wastewater treatment firm pollutant emission standard " one-level category-A standard comprehensively.
Concrete application example 2: the sanitary sewage with University Of Chongqing's campus discharging is a process object, a device day processing water yield is 200L, divide 3 batches of water inlets (ratio is 2: 3: 2), operation condition is: the aerobic 60min-sedimentation and drawing of aerobic 60min-water inlet 2L, the anoxic 40min-of the aerobic 110min-water inlet of water inlet 2L, anaerobism 40min-3L, anoxic 50min-2h, the average C/N=2.9 of intaking, COD 45～127mg/L, NH
3-N 22～39mg/L, TN 23-40mg/L, TP 4-6mg/L, pH value 7-8, test temperature is 20-24 ℃.Test-results shows: aerobic section unit volume aeration rate is 3.57m when control SBR main reaction pond
3/ hm
3, the average DO concentration of aerobic section is about 0.18mg/L, and system sludge reaches under the situation of 80d age, system's effluent COD concentration is less than 31mg/L; The water outlet NH of system
3-N concentration is below 4mg/L, and average removal rate is 97%; System's water outlet TN concentration is lower than 13.5mg/L, and average removal rate is 65.1%; System's water outlet TP concentration is less than 0.5mg/L, and average removal rate is 93.7%, and water outlet reaches " urban wastewater treatment firm pollutant emission standard " one-level category-A standard comprehensively.
Claims (5)
1. the waste disposal plant of the synchronous dephosphorization denitrogenation of reinforced low-carbon source urban sewage hypoxemia, it is made of SBR main reaction pond (1) and two dephosphorization ponds, it is characterized in that:
The water inlet pipe (4) in described SBR main reaction pond is inserted by the top in SBR main reaction pond (1), rising pipe (7) is picked out by the bottom, and be connected to outer circulation sludge pipe (10) from the bottom in SBR main reaction pond (1), be provided with aerating apparatus in SBR main reaction pond (1), the alternately operation scheme of a sedimentation and drawing of water inlet in batches, anaerobism one aerobic/anoxic is adopted in described SBR main reaction pond;
Described dephosphorization pond A (2) and dephosphorization pond B (3) have access to anaerobic phosphorus releasing pool water inlet pipe (5) respectively from top, and being connected to the water shoot (15) that is communicated with two ponds in bottom, two ponds, the described outer circulation sludge pipe (10) that is picked out by SBR main reaction pond (1) is connected with dephosphorization pond B (3) with dephosphorization pond A (2) respectively by sludge pipe (11 and 12); Dephosphorization pond A (2) and dephosphorization pond B (3) pick out waste pipe (13 and 14) again respectively and insert SBR main reaction pond (1) by sewage backflow pipe (16) from the bottom; Described sludge pipe (11 and 12) also is connected with shore pipe (17), do not arrange chemical sludge the time, shore pipe (17) is by valve closes, and only from dephosphorization pond A (2) and dephosphorization pond B (3) eliminating chemical sludge the time, just the valve open with shore pipe (17) carries out spoil disposal; Be provided with agitator (24 and 25) in described dephosphorization pond A (2) and the dephosphorization pond B (3);
Described dephosphorization pond A (2) and dephosphorization pond B (3) structure size are identical, and in the same one-period of sewage disposal, it is respectively as anaerobic phosphorus releasing pool and chemical dephosphorization pond, in the then function exchange in two ponds of next cycle.
2. the waste disposal plant of the synchronous dephosphorization denitrogenation of reinforced low-carbon source urban sewage hypoxemia according to claim 1, the water inlet pipe of described SBR main reaction pond (1), dephosphorization pond A (2) and dephosphorization pond B (3) is controlled by a total intake pump time controller (18); The aerating apparatus in described SBR main reaction pond (1) is equipped with gas meter (22) by an air compressor machine time controller (19) control on its supply air line; Agitator (24 and 25) among described dephosphorization pond A (2) and the dephosphorization pond B (3) is by agitator time controller (21) control.
3. the waste disposal plant of the synchronous dephosphorization denitrogenation of reinforced low-carbon source urban sewage hypoxemia according to claim 1 and 2, be provided with in the water inlet position of the rising pipe (7) in described SBR main reaction pond and strain hydrophone (23), the described hydrophone (23) of straining is strained hydrophone time controller (20) control.
4. the method for utilizing the described device of claim 1 to carry out sewage disposal, its process is as follows:
Substep water inlet, (anaerobism) anoxic/aerobic alternative mode are adopted in SBR main reaction pond (1), be that SBR main reaction pond makes sewage distinguish the anoxic section of injecting reactor several times under anaerobic-aerobic/anoxic alternative operational mode, make SBR main reaction pond be in the low dissolved axygen environment by the control aeration rate simultaneously at aerobic stage; In the operation of SBR main reaction pond (1), outer circulation mud is arranged anaerobic phosphorus releasing pool by the outer circulation sludge pipe (10) in SBR main reaction pond and is carried out anaerobic phosphorus release, after releasing phosphorus end mud-water separation, rich phosphorus sewage enters the chemical dephosphorization pond through water shoot (15) and carries out the solid phosphorus of chemistry, Gu the sewage behind the phosphorus refluxes SBR main reaction pond (1) with further removal ammonia nitrogen and organic substance wherein through sewage backflow pipe (16);
In aforesaid method, described SBR main reaction pond (1) is in arbitrary reaction time, all having the mud outer circulation that accounts for total sludge quantity 15% to participate in anaerobism to dephosphorization pond A (2) or dephosphorization pond B (3) strengthens and releases phosphorus, the outer circulation mud of promptly going up one-period is back to the anaerobism section in SBR main reaction this cycle of pond and participates in the effect of follow-up suction phosphorus behind anaerobic phosphorus release, the outer circulation mud in this cycle then is back to the anaerobism section of SBR main reaction pond next cycle behind anaerobic phosphorus release.
5. method according to claim 4 is characterized in that: its concrete treatment step is as follows:
(1) water inlet: according to setting flooding quantity setting flooding time, promptly flooding quantity=flooding velocity * flooding time is controlled by time controller, and time controller control intake pump and water intaking valve were opened water inlet when the cycle began, and closes behind the arrival setting flooding time, and water inlet is finished; Whole water inlet process control is in 10min;
(2) anaerobism stirring: the agitator in the SBR main reaction pond is also by corresponding time controller control, and after water inlet was finished for the first time, time controller control agitator began stirring and continue to this reaction time to end when beginning to precipitate; This moment, the air compressor machine of aerating apparatus was in closing condition, and the mixed solution in the whole SBR main reaction pond is in anaerobic state, and polyP bacteria utilizes the VFA material in the former water to carry out anaerobic phosphorus release; The anaerobism time is controlled at 1.0～1.5h, after anaerobism stirs beginning 30min, the mud of releasing in the anaerobic phosphorus releasing pool behind the phosphorus is back to SBR main reaction pond, utilize in the polyP bacteria released behind the phosphorus and the reaction tank on the effect of one-period residual nitric acid salt nitrogen generation denitrifying phosphorus uptake;
(3) aeration/stopping exposing to the sun replaces: during beginning, open air compressor machine to SBR main reaction pond aeration by the air compressor machine time controller, and control the aeration rate of whole aeration phase, make DO in the main reaction pond maintain low dissolved axygen state between 0.3～0.6, microorganism utilizes DO and organic substance generation nitration reaction and anti-nitration reaction in the water under this low dissolved axygen state; Keep low DO concentration in the reaction tank by the control aeration rate, when DO is begun to rise by preset value under the constant aerating amount, close air compressor machine, aeration finishes; System carries out the water inlet second time, the same step of method (1); Utilize the organic substance in the water inlet to do carbon source after water inlet finishes for the second time, with residual nitric acid salt nitrogen generation denitrification denitrogenation effect in the system of last aeration phase end, under the stirring of agitator, the nitrogen of generation is overflowed from the water surface; When arriving default anoxic after the time, system carries out aeration once more, and method is with above-mentioned first time of aeration, water inlet for the third time after aeration finishes, the same step of method (1); Carry out above-mentioned anoxia stirring after water inlet is finished for the third time; Arrive default anoxic after the time, air compressor machine is opened, and system carries out last aeration phase;
(4) sedimentation and drawing: after last aeration phase is finished, air compressor machine, agitator are closed, system carries out mud-water separation, treat sludge settling to liquid level half when following, SBR main reaction pond draining;
(5) effluent dephosphorization: replace as reinforced anaerobic P releasing tank and chemical dephosphorization pond by dephosphorization pond A and dephosphorization pond B during the effluent dephosphorization, if promptly in one-period dephosphorization pond A as the reinforced anaerobic P releasing tank, then dephosphorization pond B is just as the chemical dephosphorization pond, and in the next cycle that is right after both exchange functions; Detailed process is as follows:
After finish in SBR main reaction pond, close water discharging valve, open the outer circulation sludge pipe valve in SBR main reaction pond, 15% of total sludge quantity in the pond is entered dephosphorization pond A as outer circulation mud, dephosphorization pond A is as the reinforced anaerobic P releasing tank herein, and B the inside in dephosphorization pond is equipped with one-period and has been finished the outer circulation mud of releasing after the phosphorus draining; After treating that outer circulation mud all enters dephosphorization pond A, close outer circulation sludge pipe valve, and Xiang Chizhong injection raw waste water, the raw waste water amount is 1: 1 with the sludge quantity volume ratio among the A of dephosphorization pond; After sewage injects and to finish, open agitator in the reinforced anaerobic P releasing tank, carry out anaerobic phosphorus release 2～3h, make that phosphate concn reaches 35～40mg/L in this pond; After releasing the phosphorus end, close agitator and carry out mud-water separation; When dephosphorization pond A carries out anaerobic phosphorus release, SBR main reaction pond enters the reaction of next cycle according to setting program, described according to step (2), after treating that SBR main reaction pond enters anaerobic stages 30min, release the suction phosphorus effect that anaerobism section that mud after the phosphorus draining is back to the SBR main reactor participates in follow-up phase with going up one-period among the B of dephosphorization pond, will be after the B emptying of dephosphorization pond as the chemical dephosphorization pond in this cycle; Treat to open after sludge settling is finished among the A of dephosphorization pond the water shoot of dephosphorization pond A, be rich in phosphatic supernatant liquor and enter dephosphorization pond B by water shoot, original mud has been back to main reactor among the dephosphorization this moment pond B, and the rich phosphorus supernatant liquor water yield that enters dephosphorization pond B should be identical with the flooding quantity of anaerobic phosphorus release; After draining is finished, in the B of dephosphorization pond, add chemical dephosphorization agent, and about turn on agitator stirring 30min, carry out the solid phosphorus of chemistry; Treat chemical sludge post precipitation among the B of dephosphorization pond, the aeration phase that supernatant liquor is back to SBR main reaction pond is with nitrogen and organism in the further removal sewage, and chemical sludge is discharged by the bottom shore pipe; To be back to the anaerobism section in SBR main reaction pond by the outer circulation sludge pipe in next reaction time and finished the mud of releasing the phosphorus draining this moment among the dephosphorization pond A, described in step (2), participate in the suction phosphorus effect of latter stage.
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