CN101113060A - A2/O+A/O technique wastewater biological denitrification phosphorous removal process and its device - Google Patents
A2/O+A/O technique wastewater biological denitrification phosphorous removal process and its device Download PDFInfo
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Abstract
The invention pertains to a field of the technique development of sewage treatment system. The invention is designed to solve the problem of instability and low standard-reaching rate of biological denitrification and phosphorus removal technic A2/O. The problem is caused by the competition of carbon source. The invention is based on the theory of dephosphorization and denitrification by denitrification and reasonably takes the advantage of the idea that intake carbon sources can be used instead of additional carbon sources to improve denitrification rate. The invention is designed to update the technic A2/O to the technic (A2/O+A/O) of anaerobia-anoxia 1-aerobic 2-anoxia 2-aerobic 2, and the invention can also optimize the nutrient removal ability of the technic (A2/O+A/O) by starting the switches of aeration and stirring and side-flow pump in anoxia 2 zone according to different quality and quantity of intake water. The invention can also fully exert the denitrification phosphorus removal performance and effectively use the intake carbon source within the technic (A2/O+A/O), can effectively improve water quality, evidently reduces operation cost and reforms operation status. The invention is applicable to urban sewage treatment which demands on a nutritive matter emission standard.
Description
Technical field
This technical field that the present invention belongs to is: sewage biological treatment system process exploitation aspect.
Background technology
(1) anaerobic-anoxic-aerobic process
Anaerobic-anoxic-aerobic process is called for short A
2(Anaerobic/Anoxic/Aerobic is abbreviated as A to O technology
2O), be widely used in extensive sewage work both at home and abroad as the simplest synchronous denitrogen dephosphorus technology in system, but this technology is with anaerobism, anoxic and aerobic three kinds of different envrionment conditions alternate runs and different types of microorganism species such as polyP bacteria, denitrifying bacteria, nitrifier coexists as in the same sludge system, certainly exist nitrifier, the different mud age of denitrifying bacteria and polyP bacteria and carbon source battle, the nitrate that carries in the returned sluge has also suppressed the release of phosphorus under the anaerobic condition simultaneously, this mutual restriction effect of result, cause the denitrogenation dephosphorizing efficient of this technology to be difficult to further to improve, finally cause the removal of nitrogen and phosphorus to become two aspects of opposition contradiction.
A
2/ O technology is made up of anaerobism-anoxic-aerobic three phases, the returned sluge that former water that intake pump 7 extracts and sludge reflux pump 9 extract from second pond 6 enters the head end of anaerobic zone 1 simultaneously, and mix with mixed solution in the anaerobic zone 1, stirrer 11 plays the mixing stirring action.Anaerobic zone 1 water outlet enters anoxic 2, inner circulating reflux pump 10 enters oxygen-starved area 2 from aerobic zone 3 ends through the mixed solution of lift pump 10 liftings of inner circulating reflux valve 22 simultaneously, oxygen-starved area 2 goes out water mixed liquid and enters aerobic zone 3, provide air to carry out aeration by airing system 12, aerobic zone 3 goes out water mixed liquid and enters second pond 6 through flowing water Valve 19, mud, is opened mud return valve 20 part mud is refluxed through post precipitation at second pond 6, and other mud are effluxed by excess sludge discharge valve 21.
(2) denitrification dephosphorization denitrification theory
Denitrification dephosphorization (Denitrifying phosphorus removal) (can be called anoxic and inhale phosphorus, Anoxic phosphorus uptake) is meant under the condition of anaerobic/anoxic (anaerobic/anoxic) alternate run, tames out a class with NO
3 --N is as the denitrification phosphorus-collecting bacterium superiority bacteria spp of final electron acceptor(EA), and they can be with nitrate NO
3 -As electron acceptor(EA), utilize internal carbon source (PHB) as electron donor, realize denitrification denitrogenation simultaneously and inhale the phosphorus effect by " carbon is dual-purpose " mode.Obviously, the denitrification dephosphorization theory has been broken the theory that denitrogenation dephosphorizing that traditional denitrogenation dephosphorizing mechanism thought must be finished by obligate denitrifying bacteria and obligate polyP bacteria respectively, make dephosphorization and denitrification denitrogenation process realize with same quasi-microorganism, this is an important breakthrough and leap to biological carbon and phosphorous removal mechanism, for new world has been opened up in the development of biological denitrification phosphorous removal technique.In this treating processes, NO
3 -No longer merely be considered as the damper of dephosphorization process, carry out the denitrifying phosphorus uptake reaction with it as final electron acceptor(EA), therefore, denitrification dephosphorization denitrification technology can be regarded as a kind of sustainable technology.
(3) segmental influent theory
Although can be by strengthening strategy at A
2Thereby a large amount of denitrifying phosphorus removing bacteria of enrichment improves the denitrogenation dephosphorizing effect of system in the/O technology, but owing to be subjected to the restriction of feature of technology own and influent quality, be difficult to further improve effluent quality, usually need to replenish the clearance that certain additional carbon improves nitrogen, and the additional of outer carbon source is not the sufficient and necessary condition that improves effluent quality, inevitably improves systematic running cost simultaneously yet and uses.If therefore energy properly distributed water-inlet carbon source is realized the efficient utilization of water-inlet carbon source, can improve the nutrient removal performance of system to a certain extent.
Summary of the invention
Unstable and the lower problem of compliance rate of single sludge organism denitrification dephosphorization technique treatment effect that the carbon source competition causes is that at present extensive biological nutrients is removed the difficult problem that sewage work faces jointly.The current nutrient removal effect that how effectively to improve traditional single sludge anaerobic-anoxic-aerobic process does not still have report, and all multi-states of optimizing the technology operational process are not provided clear and definite thresholding, and this all gives A
2O technology obtains good denitrogenation dephosphorizing effect and has brought practical difficulty, thereby has also just hindered the further raising of this technology operating performance and the minimizing of working cost.Present A
2O technology urgent problem is how to set up the stable denitrification dephosphorization performance and the optimal control problem of operation condition, to realize maximum denitrification dephosphorization and efficient denitrification under the prerequisite that guarantees effluent quality, the properly distributed water-inlet carbon source is to reduce the outer working cost that carbon source was increased of throwing simultaneously.Aerobic 2 (the A of the aerobic 1-anoxic of anaerobic-anoxic 1-2-
2/ O+A/O) the process spent water biological denitrification phosphorous removal technique just is based on the A that denitrification dephosphorization denitrification, the abundant outer carbon source denitrification of introducing segmental influent carbon source and relevant lot of experiments data such as zone of transition is set are developed
2Upgrading process-the A of/O technology
2/ O+A/O technology.A/O section in this technology is different with A/O technology, mainly is that the A/O section does not need inner circulating reflux, and A
2Contain the required a large amount of electron acceptor(EA) in oxygen-starved area in the A/O section in the water outlet of/O section, thereby effectively utilize water-inlet carbon source to realize the removal of nitrogen.
For adapting to the fluctuation of the influent quality and the water yield, optimize (A by the Open valve 18 of switch, aeration valve 23 and the by-pass flow pump 8 of stirrer 11 in the control reaction zone
2/ O+A/O) the operation of technology, make the nitrate load that enters anoxic 1 district 2 be enough to surpass the denitrification potentiality of common heterotrophic bacterium, the PHB that realizes the anaerobic zone storage in anoxic 1 district 2 is as electron donor, nitrate in the internal recycle mixed solution is as electron acceptor(EA), take place that traditional anaerobic-anoxic-aerobic process institute is irrealizable to be utilized same carbon source can finish denitrification and inhale the phosphorus effect, efficiently utilize simultaneously water-inlet carbon source, in anoxic 2 districts 4, intake by introducing part, and regulate segmental influent recently for outer carbon source denitrification provides reaction necessary competent outer carbon source, further improve A
2The nitrogen removal performance of O technology strengthens A
2The optimization and the control of the denitrogenation of O technique denitrification dephosphorization, and reasonably distribute water-inlet carbon source, thus realize A
2The low consumed high processing horizontal of O technology high-level efficiency.
The present invention adopt technical scheme can be divided into following steps:
A
2/ O+A/O bio-denitrifying sewage dephosphorization process is characterized in that,
A
2/ O+A/O technology was made up of anaerobic stages, 1 stage of anoxic, aerobic 1 stage, 2 stages of anoxic and aerobic five stages of 2 stages:
At anaerobic stages, the raw waste water separated into two parts, the main flow part simultaneously enters anaerobic zone 1 through mud return valve 20 from the returned sluge that second pond 6 extracts by former water and the sludge reflux pump 9 that main flow pump 7 extracts, and mix with mixed solution in the anaerobic zone 1, in anaerobic zone 1, finish polyP bacteria under the stirring action of stirrer 11 and absorb biodegradable organic in the former water, form with internal carbon source PHB is stored in the polyP bacteria body, discharges the process of a large amount of phosphorus simultaneously; The by-pass flow part is by the denitrification of by-pass flow pump 8 carbon source outside the head end that by-pass flow valve 18 enters anoxic 2 districts from former water extraction by-pass flow is realized;
In 1 stage of anoxic: anaerobic zone 1 goes out water mixed liquid and inner circulating reflux pump 10 are mixed into anoxic 1 district 2 from the aerobic 1 district 3 terminal nitrification liquids that extract through inner circulating reflux valve 22 head end, nitrate in the inner circulating reflux liquid is as the denitrifying electron acceptor(EA) of polyP bacteria, the PHB that the anaerobic stages polyP bacteria stores finishes denitrification simultaneously and inhales the phosphorus effect as the electron donor of denitrifying phosphorus uptake, realizes the removal of most of phosphorus and nitrogen in anoxic 1 district 2;
In aerobic 1 stage: anoxic 1 district 2 goes out water mixed liquid and then enters aerobic 1 district 3, carries out aeration in aerobic 1 district 3 under the effect of airing system 12, and the major part of finishing organic pollutant is removed and the aerobic absorption of the nitrated and phosphorus of ammonia nitrogen;
In 2 stages of anoxic: aerobic 1 district 3 goes out water mixed liquid and by-pass flow pump 8 is mixed into anoxic 2 districts 4, the denitrification of carbon source outside anoxic 2 districts 4 mainly carry out from the by-pass flow that former water extracts under the effect of whipping appts 11.(COD concentration is 150～250mg/L, and influent ammonium concentration 70～100mg/L), and anoxic 2 districts 4 open air-supplying valve 23, close stirrer 11 and by-pass flow pump 8 and by-pass flow valve 18, carries out aerobic nitrification and react in anoxic 2 districts 4 when water inlet C/N is lower; As water inlet C/N (COD concentration 350～500mg/L when higher, and influent ammonium concentration is 45～60mg/L), anoxic 2 districts 4 close air-supplying valve 23, open stirrer 11 and by-pass flow pump 8 and by-pass flow valve 18, realize the anti-nitration reaction of outer carbon source in anoxic 2 districts 4, in anoxic 1 district 2, on the basis of denitrification dephosphorization, further improve the utilization ratio and the denitrification rate of outer carbon source, regulating by-pass flow this moment is 0.15 ± 0.01 than (by-pass flow pumping capacity and main flow pump and by-pass flow pumping capacity and ratio), A
2The denitrogenation dephosphorizing performance of/O+A/O technology reaches optimum.
In aerobic 2 stages: anoxic 2 districts 4 mixed solutions then enter aerobic 2 districts 5, further finish in the by-pass flow liquid sorption of nitrated and phosphorus of removal, the ammonia nitrogen of residue organic pollutant in aerobic 2 districts 5;
In the mud-water separation stage: aerobic 2 districts, 5 water outlets enter second pond 6, mixed solution supernatant liquor after the second pond mud-water separation effluxes, sludgd deposition is in the second pond bucket, the sedimentary part of bucket is promoted through mud return valve 20 by sludge reflux pump 9 and enters anaerobic zone 1, most of settled sludge then effluxes as excess sludge, and excess sludge discharge valve 21 is an open mode usually.
A
2/ O+A/O bio-denitrifying sewage dephosphorization apparatus is characterized in that:
Unstable and the lower problem of compliance rate of single sludge organism denitrification dephosphorization technique treatment effect that the carbon source competition causes is that at present extensive biological nutrients is removed the difficult problem that sewage work faces jointly.Based on the basic concept of denitrification dephosphorization denitrification theory and properly distributed water-inlet carbon source, at A
2Set up stable denitrification dephosphorization performance in the O technology, utilize the denitrification phosphorus-collecting bacterium, realize denitrogenation dephosphorizing synchronously, efficiently utilize water-inlet carbon source simultaneously, further improve A in " carbon is dual-purpose " mode
2The denitrogenation ability of O technology has not only solved the contradictory relation between denitrogenation and dephosphorization in traditional anaerobism-anoxic-aerobic process, and has saved operation energy consumption.
Compare not only the chemical oxygen demand COD consumption with traditional single mud denitrification dephosphorization technique and can save 50%, the oxygen consumption reduces by 30%, and sludge yield also is expected to reduce 50%.
Description of drawings
Fig. 1: anaerobism-anoxic-aerobic (A
2/ O) process structure synoptic diagram
1 anaerobic zone; 2 oxygen-starved areas; 3 aerobic zones; 6 second ponds; 7 intake pumps; 9 sludge reflux pumps; 10 inner circulating reflux pumps; 11 stirrers; 12 airing systems; 19 flowing water Valves; 20 mud return valves; 21 excess sludge discharge valves; 22 inner circulating reflux valves;
Fig. 2: the aerobic 2 (A of the aerobic 1-anoxic of anaerobic-anoxic 1-2-
2/ O+A/O) process structure synoptic diagram
1 anaerobic zone; 2 anoxics, 1 district; 3 aerobic 1 districts; 4 anoxics, 2 districts; 5 aerobic 2 districts; 6 second ponds; 7 main flow pumps; 8 by-pass flow pumps; 9 sludge reflux pumps; 10 inner circulating reflux pumps; 11 stirrers; 12 airing systems; 13 computers; The 14PLC housing; DO in 15 reactors, pH and ORP on-line sensor; DO in 16 second ponds, pH and ORP on-line sensor; 17 mud liquidometers; 18 inlet valves; 19 flowing water Valves; 20 mud return valves; 21 excess sludge discharge valves; 22 inner circulating reflux valves; 23 aeration valves; 24 aeration heads;
Embodiment
Describe patent of the present invention in detail below in conjunction with drawings and Examples:
Testing selected trial model is two gallery pulling flow type rectangular reactor, and test is divided into 9 compartment operations, and preceding two compartments are anaerobic zone 1, and next a compartment is anoxic 1 district 2, and four compartments in back are aerobic 1 district 4, are anoxic 2 districts 4 and aerobic 2 districts 5 then.In anaerobic zone 1 and anoxic 1 district) and anoxic 2 districts 4 in stirrer 11 be installed respectively be in suspended state to keep mud, air feeder 12 arrives pressurized air in each reaction zone tapping point through supply air line, bloat micro bubble by aeration head and satisfy microorganism growth, the size of tolerance serves as the test set(ting)value by the control of the valve on the supply air line with the DO concentration in the realization response district.Water inlet, returned sluge, internal recycle nitrification liquid are respectively by main flow pump 7 and by-pass flow pump 8, return sludge pump 9, inner circulating reflux pump 10 promotes, measures, and regulates rotating speed according to the test needs and reaches required flow, advances to avoid the back mixing phenomenon by promoting current communicating pipe between each dividing plate of reactor.
In the process of the test, the raw waste water separated into two parts, former water that main flow pump 7 extracts and sludge reflux pump 9 enter anaerobic zone 1 simultaneously from the returned sluge that second pond 6 extracts, and mix with mixed solution in the anaerobic zone 1, under the stirring action of anaerobic zone 1 stirrer 11, polyP bacteria absorbs the biodegradable organic in the former water, is stored in the polyP bacteria body with the form of internal carbon source PHB, discharges a large amount of phosphorus simultaneously; Anaerobic zone 1 water outlet and inner circulating reflux pump 10 are mixed into anoxic 1 district 2 from the aerobic 1 district 3 terminal nitrification liquids that extract, nitrate in the inner circulating reflux liquid is as the denitrifying electron acceptor(EA) of polyP bacteria, the PHB that the anaerobic stages polyP bacteria stores finishes denitrification simultaneously and inhales the phosphorus effect as the electron donor of denitrifying phosphorus uptake, and anoxic in 1 district 2 removal that the denitrifying phosphorus uptake reaction realizes most of phosphorus and nitrogen takes place; Anoxic 1 district 2 goes out water mixed liquid and then enters aerobic 1 district 3, and the aerobic absorption of the nitrated and phosphorus of ammonia nitrogen is removed and realized to the major part of finishing organic pollutant by aeration in aerobic 1 district 3; Aerobic 1 district 3 goes out water mixed liquid and by-pass flow pump 8 is mixed into anoxic 2 districts 4, the denitrification of carbon source outside anoxic 2 districts 4 mainly carry out from the by-pass flow that former water extracts under the effect of whipping appts 11; Anoxic 2 districts 4 mixed solutions then enter aerobic 2 districts 5, removal, aerobic 2 districts, 5 water outlets of further finishing residue organic pollutant in the by-pass flow liquid in aerobic 2 districts enter second pond 6, mixed solution supernatant liquor after the second pond mud-water separation effluxes, sludgd deposition is in the second pond bucket, the sedimentary part of bucket is risen to by sludge reflux pump 20 and enters anaerobic zone 1, most of settled sludge then effluxes as excess sludge, and excess sludge discharge valve 21 is an open mode usually;
Example 1
Adopt A in the process of the test
2/ O process using synthetic beer waste water (COD=25 1-406mg/L, total nitrogen TN=44.6-65.4mg/L and total phosphorus TP=7.1-11.5mg/L, C/N=6.5-7.4, C/P=40.1-57.2), hydraulic detention time 9h, sludge age 10-12d, sludge concentration 3500 ± 100mg/L, return sludge ratio 0.5, control water inlet pH is stabilized in 7.2～7.6, and temperature is controlled at 20-23 ℃ by heating rod.Test-results shows that the denitrifying phosphorus uptake amount is 15% with the ratio of aerobic suction phosphorus amount, COD clearance 85%, and the clearance of TN and TP is respectively 69% and 75%.
Example 2
Adopt A/O process using synthetic beer waste water (COD=25 1-406 mg/L, total nitrogen TN=44.6-65.4mg/L and total phosphorus TP=7.1-11.5mg/L in the process of the test, C/N=6.5-7.4, C/P=40.1-57.2), hydraulic detention time 9h, sludge age 10-12d, sludge concentration 3500 ± 100mg/L, return sludge ratio 0.5, control water inlet pH is stabilized in 7.2～7.6, and temperature is controlled at 20-23 ℃ by heating rod.Test-results shows that the denitrifying phosphorus uptake amount is 0% with the ratio of aerobic suction phosphorus amount, and the COD clearance is higher than 86%, and the clearance of TN and TP is respectively 76% and 15%.
Example 3
Adopt A in the process of the test
2/ O+A/O technology synthetic beer waste water (COD=222-256 mg/L, total nitrogen TN=67-73mg/L and total phosphorus TP=6.3-6.8mg/L, C/N=3.4-3.9, C/P=35.2-38.5), hydraulic detention time 9h, sludge age 10-12d, sludge concentration 3500 ± 100mg/L, return sludge ratio 0.5, control water inlet pH is stabilized in 7.2～7.6, and temperature is controlled at 20-23 ℃ by heating rod, investigate low C/N than the time aeration opened, close stirrer and by-pass flow pump.From A
2The test-results of/O+A/O technology shows (Fig. 1,2 and 3), and the denitrifying phosphorus uptake amount is 45% with the ratio of aerobic suction phosphorus amount, and the COD clearance is higher than 80%, and the clearance of TN and TP is respectively 71% and 83%.
Example 4
Adopt A in the process of the test
2/ O+A/O process using synthetic beer waste water (COD=251-406mg/L, total nitrogen TN=44.6-65.4mg/L and total phosphorus TP=7.1-11.5mg/L, C/N=6.5-7.4, C/P=40.1-57.2), hydraulic detention time 9h, sludge age 10-12d, sludge concentration 3500 ± 100mg/L, return sludge ratio 0.5, control water inlet pH is stabilized in 7.2～7.6, and temperature is controlled at 20-23 ℃ by heating rod, when the by-pass flow ratio is controlled at 0.15.Test-results shows that the denitrifying phosphorus uptake amount is optimum value (being higher than 70%) with the ratio of aerobic suction phosphorus amount, and the COD clearance is higher than 90%, and the clearance of TN and TP is respectively 86% and 95%.
Claims (2)
1. A
2/ O+A/O bio-denitrifying sewage dephosphorization process is characterized in that, is made up of anaerobic stages, 1 stage of anoxic, aerobic 1 stage, 2 stages of anoxic and aerobic five stages of 2 stages:
At anaerobic stages, the raw waste water separated into two parts, the main flow part enters anaerobic zone (1) by former water and the sludge reflux pump (9) that main flow pump (7) extracts simultaneously from the returned sluge that second pond (6) extracts, and with anaerobic zone (1) in mixed solution mix, in anaerobic zone (1), finish polyP bacteria under the stirring action of stirrer (11) and absorb biodegradable organic in the former water, form with internal carbon source PHB is stored in the polyP bacteria body, discharges the process of a large amount of phosphorus simultaneously; The denitrification of carbon source outside the head end that the by-pass flow part enters anoxic 2 districts by by-pass flow pump (8) from former water extraction by-pass flow is realized;
In 1 stage of anoxic: the nitrification liquid that anaerobic zone (1) goes out water mixed liquid and inner circulating reflux pump (10) terminal extraction from aerobic 1 district (3) is mixed into anoxic 1 district (2), nitrate in the inner circulating reflux liquid is as the denitrifying electron acceptor(EA) of polyP bacteria, the PHB that the anaerobic stages polyP bacteria stores finishes denitrification simultaneously and inhales the phosphorus effect as the electron donor of denitrifying phosphorus uptake, realizes the removal of most of phosphorus and nitrogen in anoxic 1 district (2);
In aerobic 1 stage: anoxic 1 district (2) goes out water mixed liquid and then enters aerobic 1 district (3), carries out aeration under the effect of the inherent airing system in aerobic 1 district (3) (12), and the major part of finishing organic pollutant is removed and the aerobic absorption of the nitrated and phosphorus of ammonia nitrogen;
In 2 stages of anoxic: aerobic 1 district (3) goes out water mixed liquid and by-pass flow pump (8) is mixed into anoxic 2 districts (4), the denitrification of carbon source outside anoxic 2 districts (4) mainly carry out from the by-pass flow that former water extracts under the effect of whipping appts (11); When water inlet COD concentration is 150～250mg/L, and influent ammonium concentration 70～100mg/L, anoxic 2 districts (4) open air-supplying valve (23), close stirrer (11) and by-pass flow pump (8), carry out aerobic nitrification to react in anoxic 2 districts (4); As water inlet COD concentration 350～500mg/L, and influent ammonium concentration is 45～60mg/L, anoxic 2 districts (4) close air-supplying valve (23), open stirrer (11) and by-pass flow pump (8), realize the anti-nitration reaction of outer carbon source in anoxic 2 districts (4), in anoxic 1 district, on the basis of denitrification dephosphorization, further improve the utilization ratio and the denitrification rate of outer carbon source, regulate the by-pass flow ratio this moment is 0.15 ± 0.01, A
2The denitrogenation dephosphorizing performance of/O+A/O technology reaches optimum;
In aerobic 2 stages: anoxic 2 districts (4) mixed solution then enters aerobic 2 districts (5), further finishes in the by-pass flow liquid sorption of nitrated and phosphorus of removal, the ammonia nitrogen of residue organic pollutant in aerobic 2 districts;
In the mud-water separation stage: aerobic 2 districts (5) water outlet enters second pond (6), mixed solution supernatant liquor after the second pond mud-water separation effluxes, sludgd deposition is in the second pond bucket, the sedimentary part of bucket is promoted by sludge reflux pump (9) and enters anaerobic zone (1), most of settled sludge then effluxes as excess sludge, and excess sludge discharge valve (21) is an open mode usually.
2. according to the used A of the technology of claim 1
2/ O+A/O bio-denitrifying sewage dephosphorization apparatus is characterized in that:
Main flow pump (7) links to each other with the water inlet pipe of anaerobic zone (1) head end, and return sludge pump (9) carries the second pond returned sluge and the main flow water inlet enters anaerobic zone (1) simultaneously; Anaerobic zone (1) links to each other with anoxic 1 district (2), the water side in anoxic 1 district (2) links to each other with aerobic 1 district (3) feed-water end, the terminal rising pipe in aerobic 1 district (3) links to each other with inner circulating reflux valve (22), inner circulating reflux valve (22) water side links to each other with inner circulating reflux pump (10), and the water side of inner circulating reflux pump (10) links to each other with the water inlet pipe of the head end in anoxic 1 district (2); Water side, aerobic 1 district (3) links to each other with anoxic 2 districts (4); By-pass flow pump (8) links to each other with the water inlet pipe of anoxic 2 districts (4) head end, and the water outlet that by-pass flow pump (10) water outlet and aerobic 1 district (3) end contain a large amount of nitrate mixes and enters anoxic 2 districts (4) head end water inlet pipe simultaneously; Anoxic 2 districts (4) link to each other with aerobic 2 districts (5), and aerobic 2 districts (5) link to each other with second pond (6) water inlet pipe; Airing system (12) links to each other with aerobic 2 districts (5) district with aerobic 1 district (3), and the air-supplying valve (23) in anoxic 2 districts (4) links to each other with aeration head (24); (DO) of dissolved oxygen is installed in main reactor and the second pond, pH and redox potential (ORP) on-line sensor (15) and (16), on-line sensor (15) and (16), mud liquidometer (17), PLC housing (14) and computer (13) constitute the PLC on-line monitoring system.
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