CN101759333A - Apparatus for stably maintaining sludge micro-bulking for saving energy in biological denitrification technology and method thereof - Google Patents
Apparatus for stably maintaining sludge micro-bulking for saving energy in biological denitrification technology and method thereof Download PDFInfo
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Abstract
The invention provides an apparatus for stably maintaining sludge micro-bulking for saving energy in biological denitrification technique, which is provided with a water inlet tank, a reactor, and a secondary sedimentation tank sequentially, the water inlet end of the reactor is provided with an anaerobic cellular chamber, the anoxia cellular chamber is provided with a stirrer inside, an aerobic cellular chamber or a passage is arranged behind the anoxia cellular chamber, the aerobic lattice chamber or the passage is provided with a dissolved oxygen probe and an aeration head, and each dissolved oxygen probe is connected to a PID control system, each aeration head is connected to an air compressor through an air-flow meter, each control switch is connected to the PID control system. By adopting reasonable regulating technology operation parameters, particularly, the technology is controlled to be carried out under the conditions of proper sludge burden and dissolved oxygen concentration, the invention improves inter-species balance between filamentous fungi and zoogloea bacterium, and controls the sludge bulking within a certain extent and avoids malignant sludge bulking, thereby stably maintaining sludge micro-bulking. The invention solves the technical problem of how to stably maintain sludge micro-bulking in sewage treatment, and saves aeration energy consumption and achieves sewage water high-efficiency treatment purpose while ensuring the process effect.
Description
Technical field
The present invention relates in a kind of bio-denitrifying sewage energy-efficient treatment apparatus and method, especially the Prepositive denitrification biological denitrificaion sewage treatment process stably maintaining sludge expands and realizes the method for sewage energy-efficient treatment.
Background technology
The Prepositive denitrification biological denitrification process is one of most widely used sewage treatment process of present China's municipal wastewater treatment plant, and this technology claims A/O(Anoxic/Oxic again) biological denitrification process is a kind of known sewage water denitrification treatment process.This technology has the technical process characteristic of simple owing to can utilize the denitrifying carbon source of carbonaceous organic material conduct under anoxic (Anoxic) condition in the water inlet.Yet this sewage treatment process need adopt bigger aeration rate to improve nitrification efficiency and prevent sludge bulking at aerobic zone usually, and existence can't prevent the generation of pernicious sludge bulking, and shortcoming such as the aeration operation energy consumption is big.
Summary of the invention
The purpose of this invention is to provide a kind of biological denitrification process stably maintaining sludge microdilatancy and realize energy-conservation apparatus and method, solution is how stably maintaining sludge microdilatancy and prevent the technical barrier of serious sludge bulking in sewage treatment process, and when guaranteeing nitrification effect, the purpose of utilizing less aeration energy consumption, realization wastewater efficient to handle.
For achieving the above object, patent of the present invention adopts following technical scheme: a kind of biological denitrification process stably maintaining sludge microdilatancy realizes energy-conservation device, according to order from former water feed-water end to the clear water water side, set gradually water tank inlet, reactor and second pond, it is characterized in that: described water tank inlet is through first peristaltic pump, water inlet pipe and valve are communicated with reactor, reactor) Shang Mian posticum is communicated with second pond through fresh water pipeline and valve, the middle part of reactor is through backflow nitrification liquid pipeline, second peristaltic pump and valve are communicated with the anoxia cell chamber, separator is set in the second pond, branch of the bottom sludge pipe of second pond is through mud return line, the 3rd peristaltic pump and valve are communicated with the anoxia cell chamber, another branch connects excess sludge pipe and valve, be provided with at least four road dividing plates in the reactor, the staggered flowing water communicating aperture that has of adjacent separator, the feed-water end of reactor is provided with at least one anoxia cell chamber, the indoor agitator that is provided with of anoxia cell, at least three aerobic lattice chambers are set after the anoxia cell chamber, and each aerobic lattice chamber all is provided with dissolved oxygen probe and the aeration head that can accurately control DO concentration, the signal wire of each dissolved oxygen probe is connected with the signal input part of PID Controlling System, each aeration head connects air compressor through air flowmeter, the trip switch of air compressor and each peristaltic pump is connected with the control signal output terminal of PID Controlling System, by the switching and the aperture of PID Controlling System control air compressor and each peristaltic pump.
Total lattice chamber of described reactor is divided at least 5 lattice chambers or many gallerys, at least 3 aerobic lattice chambers wherein are set, the water inlet pipe of described second pond is at the center, and effluent weir is discharged system in the peripheral overflow water outlet through rising pipe, and the volume of second pond is that 3-5h designs according to hydraulic detention time.
A kind of biological denitrification process stably maintaining sludge microdilatancy realizes method for saving energy, it is characterized in that: by the switching of PID Controlling System control air compressor and each peristaltic pump and the aperture of each valve, the flooding velocity of described water inlet pipe, the nitrification liquid quantity of reflux of backflow nitrification liquid pipeline and the returned sluge flow of mud return line are by changing the rotating speed of peristaltic pump, change valve opening or change the pump line caliber and regulate, the aeration rate of conditioned reaction device aerobic zone, the dissolved oxygen concentration of regulating aerobic zone is in 0.5-1.2mg/L optimal value scope, the control influent load, the sludge loading of regulating second pond is in 0.22-0.35kgCOD/kgMLSS/d.
The mud of described second pond in the SVI of at least 5 sludge ages value (sludge volume index) long-term control at 150-250mL/g.
Guarantee that technology moves at normal temperatures,, suitably increase aeration rate and keep the higher DO concentration of aerobic zone, exceed 0.5mg/L than the DO between normal epoch as low temperature environment.
Under the condition that N, P nutritive substance lack, in water inlet, add the corresponding water inlet COD/N/P ratio of regulating in normal value (100 ︰, 5 ︰ 1) scope.
When sludge loading is lower than 0.20kgCOD/kgMLSS/d, suitably improve sludge loading to the 0.25kgCOD/kgMLSS/d by the mode that increases sludge volume; When sludge loading is higher than 0.38kgCOD/kgMLSS/d, suitably reduce sludge loading to the 0.25kgCOD/kgMLSS/d by the mode that reduces sludge volume or prolong hydraulic detention time.
When mud SVI was higher than 250mL/g and thread fungus index continuously and surpasses 3 in 3 days, or the second pond mud height is when rising to 80% the highest mud position, can suitably increase aeration rate and keep the higher DO concentration of aerobic zone, exceed 0.5mg/L than the DO between normal epoch, and the mode of increase sludge volume suitably improves sludge loading.
When mud SVI was higher than 250mL/g and thread fungus index continuously and surpasses 3 in 3 days, or the second pond mud height is when rising to 80% the highest mud position, under the condition that does not increase the oxygen-starved area volume, can strengthen the effect of anoxic biological selector by increasing the anoxia cell chamber, suppress hyphomycetic further breeding.
When the water outlet ammonia nitrogen concentration surpasses discharge index, can suitably increase aeration rate and keep the higher DO concentration of aerobic zone, exceed 0.5mg/L than the DO between normal epoch.
The volume of the anoxia cell chamber that is provided with or hydraulic detention time foot have guaranteed that denitrification is back to the nitric nitrogen concentration that is contained the nitrification liquid of anoxia cell chamber from aerobic lattice chamber end.The volume of the aerobic lattice chamber that is provided with or hydraulic detention time foot have guaranteed that the ammonia nitrogen concentration of water outlet is lower than discharge index under low DO condition.
Patent compared with prior art of the present invention has following characteristics and beneficial effect: stably maintaining sludge microdilatancy of the present invention realizes that energy-conservation main method for by adjusting and control to parameters of technique process DO and influent load, causes the balanced growth of thread fungus and zoogloea bacterium.In stably maintaining sludge microdilatancy process, owing to adopted lower aeration rate, thus saved aeration energy consumption.
Adopt apparatus and method of the present invention, make mud that the thread fungus slight expansion take place, sludge volume index (SVI) long-term (being not less than 5 sludge ages) is controlled between 150 ~ 250mL/g.Regulate the process sludge load by influent load and be in 0.22-0.35kgCOD/kdMLSS/d, the aeration rate of control aerobic zone is regulated dissolved oxygen concentration in the optimal value scope of correspondence (0.5-1.2mg/L), adopt the mode of lattice or baffling to keep mixed solution in oxygen-starved area and aerobic zone plug-flow mode preferably, prevent and prevent underload other can bring out the condition and the factor of pernicious sludge bulking in conjunction with low dissolved axygen etc., realize the balanced growth of thread fungus and zoogloea bacterium, thus the stably maintaining sludge microdilatancy.
Description of drawings
Fig. 1 is a structural representation of the present invention.
Fig. 2 is the corresponding diagram of the present invention's required optimization dissolved oxygen concentration under different load.
Fig. 3 is the present invention's design sketch that sludge slight expansion is kept under different load, optimization DO.
Fig. 4 is the recovery effects figure of sludge slight expansion state of the present invention.
Fig. 5 is that structure of the present invention and inside are provided with the sex design sketch of sludge settling.
Reference numeral: 1-water tank inlet, 2-first peristaltic pump, the 3-valve, the 4-agitator, the 5-aeration head, the 6-under meter, the 7-air compressor, the 8-separator, 9-backflow nitrification liquid pipeline, the 10-water outlet, the 11-mud return line, the 12-excess sludge, the 13-reactor, 14-anoxia cell chamber, the aerobic lattice of 15-chamber, the 16-second pond, the 17-dissolved oxygen probe, the 18-posticum, 19-clear water pipe, the 20-water inlet pipe, the 21-dividing plate, 22-flowing water communicating aperture, the 23-PID Controlling System, 24-second peristaltic pump, 25-the 3rd peristaltic pump, the 26-effluent weir.
Embodiment
The present invention will be further described in detail below in conjunction with accompanying drawing.
Embodiment one is referring to shown in Figure 1, a kind of biological denitrification process stably maintaining sludge microdilatancy realizes energy-conservation device, according to order from former water feed-water end to the clear water water side, set gradually water tank inlet 1, reactor 13 and second pond 16, described water tank inlet 1 is through peristaltic pump 2, water inlet pipe 20 and valve 3 are communicated with reactor 13, posticum 18 above the reactor 13 is communicated with second pond 16 through fresh water pipeline 19 and valve, the middle part of reactor 13 is through backflow nitrification liquid pipeline 9, second peristaltic pump 24 and valve are communicated with anoxia cell chamber 14, separator 8 is set in the second pond 16, the water inlet pipe of described second pond is at the center, through rising pipe 10 discharge systems, the volume of second pond is that 3-5h designs according to hydraulic detention time to effluent weir 26 in the peripheral overflow water outlet.Branch of the bottom sludge pipe of second pond 16 is communicated with anoxia cell chamber 14 through mud return line 11, the 3rd peristaltic pump 25 and valve, and another branch connects excess sludge pipe 12 and valve.Total lattice chamber of reactor 13 is divided at least five lattice chambers or many gallerys, in be provided with at least four road dividing plates, the staggered flowing water communicating aperture 22 that has of adjacent separator, the feed-water end of reactor 13 is provided with at least one anoxia cell chamber 14, be provided with agitator 4 in the anoxia cell chamber 14, at least three aerobic lattice chambers 15 are set after the anoxia cell chamber, and each aerobic lattice chamber all is provided with dissolved oxygen probe 17 and the aeration head 5 that can accurately control DO concentration, the signal wire of each dissolved oxygen probe is connected with the signal input part of PID Controlling System 23, each aeration head 5 connects air compressor 7 through air flowmeter 6, the trip switch of air compressor and each peristaltic pump is connected with the control signal output terminal of PID Controlling System 23, by the switching of PID Controlling System control air compressor 7 and each peristaltic pump and the aperture of each valve 3.
The nitrification liquid quantity of reflux of the flooding velocity of water inlet pipe 20, backflow nitrification liquid pipeline 9 and the returned sluge flow of mud return line 11 are regulated by the rotating speed, change valve 3 apertures or the change pump line caliber that change peristaltic pump.The volume of the anoxia cell chamber 14 that is provided with or hydraulic detention time foot have guaranteed that denitrification is back to the nitric nitrogen concentration that is contained 14 nitrification liquids of anoxia cell chamber from aerobic lattice chamber 15 ends.The volume of the aerobic lattice chamber 15 that is provided with or hydraulic detention time foot have guaranteed that the ammonia nitrogen concentration of water outlet is lower than discharge index under low DO condition.The aeration rate of conditioned reaction device 13 aerobic zones, the dissolved oxygen concentration of regulating aerobic zone is in 0.5-1.2mg/L optimal value scope, the control influent load, regulate the process sludge load and be in 0.22-0.35kgCOD/kgMLSS/d, the control sludge volume index is not less than five sludge ages for a long time, is controlled between the 150-250mL/g.Regulate aeration rate in real time by DO concentration in the on-line monitoring reactor lattice chamber, so that keep required DO concentration.Under low temperature environment, suitably increase aeration rate and keep the higher DO concentration of aerobic zone, exceed 0.5mg/L than the DO between normal epoch.Under the condition that N, P nutritive substance lack, can suitably in water inlet, add respective substance and regulate water inlet COD/N/P ratio in normal value (100 ︰, 5 ︰ 1) scope.
Can be according to the test needs, by adjusting the position, water hole, conditioned reaction device working volume.Can be provided with 4-10 road active clapboard in the reactor, can dismantle flexibly, can adjust each the lattice chamber volume size and the reactor lattice number of chambers as required, the lattice number of chambers of reactor guarantees more than 5 in the test run, recommends to adopt 6 or 7.The anoxic operation of first lattice chamber, lattice chamber the 2nd can also can aerobicly be moved in the anoxic operation, from the aerobic operation in lattice chamber the 3rd.For fear of air-teturning mixed phenomenon, interleaved hole on dividing plate makes current present dirty fluidised form.The oxygen-starved area makes the active sludge in the reactor and intake substrate, returned sluge and backflow nitrification liquid thorough mixing by the stirring of mechanical stirrer.Aerobic zone adopts the sand burning head as micro-pore aeration by the air compressor air feed.Can regulate flooding velocity, nitrification liquid quantity of reflux and returned sluge flow by rotating speed or the change pump line caliber of regulating peristaltic pump.The water inlet pipe of second pond is at the center, and through rising pipe 10 discharge systems, the volume of second pond is that 3-5h designs according to hydraulic detention time to effluent weir 26 in the peripheral overflow water outlet.Set up the PID Controlling System, regulate aeration rate in real time by DO concentration in the on-line monitoring reactor lattice chamber, so that keep required DO concentration.
Referring to shown in Figure 2, shown corresponding diagram in order to be effective and required optimization dissolved oxygen concentration when keeping microdilatancy under different load, for A/O technology, come change of load to mean that then hydraulic detention time changes by changing flooding quantity.Under the situation that MLSS is constant substantially in influent ammonium concentration and system, the length of hydraulic detention time has tangible influence to the nitrification effect of system.When the sludge loading height be hydraulic detention time in short-term, reach identical nitrification effect, the carrying out that then needs higher dissolved oxygen concentration to accelerate nitration reaction.Otherwise, be hydraulic detention time when long when sludge loading is low, reach identical nitrification effect, then do not need higher dissolved oxygen concentration, otherwise will cause excessive aeration and waste energy.And the oxygen respiratory rate difference of different sludge loading correspondences is kept essentially identical SVI value or sludge slight expansion, and the DO value that then needs is different.When adopting this invention, the nitrification effect that at first need obtain to reach identical and under the prerequisite of the identical sludge slight expansion of stable maintenance, the required optimum dissolved oxygen concentration value of system.Draw the relation of COD-sludge loading and DO under the above-mentioned condition, constraint condition has two: (1) ammonia nitrogen removal frank maintains target value, guarantees that effluent quality is up to standard; (2) mud is in the microdilatancy state.Embodiment 1: A/O art breading sanitary sewage under the different load is guaranteeing that ammonia nitrogen removal reaches one-level B requirement, and is keeping under the prerequisite of stable sludge slight expansion, the optimization of DO concentration research.
Adopt A/O art breading campus life sewage, mixed liquor suspended solid, MLSS concentration (MLSS) maintains between 2500 ~ 3500mg/L in the aeration tank, and average reactor temperature is 25 ℃, nitrate recirculation ratio 150%, and mud refluxes 100%.Oxygen-starved area and aerobic zone volume ratio are 1 ︰ 5, come change of load by the change flooding velocity, and after each load beginning adopted high-solubility oxygen stable earlier, the aeration rate of the every lattice of re-adjustment aerobic zone chamber was kept the interior average DO of reactor in different levels.Find that will reach ammonia nitrogen removal frank more than 70% under different influent load conditions, and keep SVI between 150 ~ 250mL/g, the relation of required optimum dissolved oxygen and sludge loading is shown in figure accompanying drawing 2 after summing up the conclusion testing data.The dissolved oxygen of high loading correspondence wants high with respect to the dissolved oxygen of underload correspondence.When the COD-sludge loading was 0.40kgCOD/kgMLSS/d, corresponding optimum dissolved oxygen concentration was 1.2mg/L; And when the COD-sludge loading was 0.30kgCOD/kgMLSS/d, corresponding optimum dissolved oxygen concentration was 0.8mg/L; When the COD-sludge loading was reduced to 0.25kgCOD/kgMLSS/d, corresponding optimum dissolved oxygen concentration was 0.6mg/L.
Embodiment two has shown at different load, has optimized the design sketch that sludge slight expansion is kept under the DO referring to shown in Figure 3, under the DO condition of optimizing, and the change curve of SVI and thread fungus index (FI) in the stably maintaining sludge microdilatancy state runtime system.The energy-conservation device (as shown in Figure 1) of stably maintaining sludge microdilatancy realization is kept sludge slight expansion in the employing sewage disposal under the DO concentration of optimizing.Former water is campus life sewage, and mixed liquor suspended solid, MLSS dense (MLSS) maintains between 2500 ~ 3500mg/L in the aeration tank, and average reactor temperature is 25 ℃, nitrate recirculation ratio 150%, return sludge ratio 100%.Oxygen-starved area and aerobic zone volume ratio are 1 ︰ 5, come change of load by changing flooding velocity, and it is 170 ~ 320L/d that duration of test is handled the water yield.
When the COD-of system sludge loading (Ns) when being lower than 0.20kgCOD/kgMLSS/d, the SVI value has surpassed 250mL/g, and microscopy finds that thread fungus quantity is more, and thread fungus index (FI) mostly is more than 3 or 3.When the COD-of system sludge loading (Ns) when being higher than 0.38kgCOD/kgMLSS/d, the SVI value is also higher relatively, has surpassed 250mL/g, and microscopy finds that thread fungus quantity is more, and FI mostly is 3.And when COD-sludge loading (Ns) was 0.22 ~ 0.35kgCOD/kgMLSS/d, the energy stable maintenance was between 150 ~ 250mL/g substantially for the SVI value of mud in the A/O technology, and FI mostly is greatly below 2 or 2.Therefore, the load that suits to keep the microdilatancy state in A/O technology is between 0.22 ~ 0.35kgCOD/kgMLSS/d, and system moves under the DO condition of optimizing in this scope, and system can maintain sludge slight expansion state preferably.
Embodiment three is referring to shown in Figure 4, shown the influence that the aeration tank fluidised form is kept sludge slight expansion and the variation effect figure of reactor sludge settling under different total number of divisions.Stably maintaining sludge microdilatancy realization method for saving energy (as shown in Figure 1) is kept sludge slight expansion in the employing sewage disposal under the DO concentration of optimizing, former water is campus life sewage, mixed liquor suspended solid, MLSS dense (MLSS) maintains between 2500 ~ 3500mg/L in the aeration tank, average reactor temperature is 25 ℃, nitrate recirculation ratio 150%, return sludge ratio 100%.Oxygen-starved area and aerobic zone volume ratio are 1 ︰ 5.When system during in the steady running of low dissolved axygen sludge slight expansion, lay down two plates, aerobic zone is become 3 lattice from 5 lattice, destroyed plug-flow fluidised form good in the aeration tank, strengthen mud simultaneously and reflux, reflux ratio is transferred to 300%.Under the DO=0.5mg/L condition, the SVI value begins to rise, and has found hyphomycetic propagation after 6 days, and SVI reaches 200mL/g after 20 days, and has the trend that continues rising, and the thread fungus reproduction speed is very fast.At this moment turn back to dividing plate, recover reflux ratio to 150%, DO transfers to 0.5mg/L, and sludge bulking is under control immediately, and SVI is reduced to 150mL/g.
Embodiment four has further shown reactor structure and inner the setting the influence to sludge settling referring to shown in Figure 5.Stably maintaining sludge microdilatancy realization method for saving energy (as shown in Figure 1) is kept sludge slight expansion in the employing sewage disposal under the DO concentration of optimizing, former water is campus life sewage, mixed liquor suspended solid, MLSS dense (MLSS) maintains between 2500 ~ 3500mg/L in the aeration tank, average reactor temperature is 25 ℃, nitrate recirculation ratio 150%, return sludge ratio 100%.Be divided into 7 forms in the reactor, preceding two forms are the oxygen-starved area, and back 5 lattice chambers are set to aerobic zone, and the aerobic zone volume ratio is 2 ︰ 5.After system is stable under normal operation, lay down plate and remove two oxygen-starved areas of leading portion, change reactor the aerobic operation of into two lattice chambers, destroyed plug-flow fluidised form good in the aeration tank.Under the DO=0.5-0.8mg/L condition, the SVI value begins to rise fast, and SVI reaches 709mL/g after 30 days, occurs tangible sludge loss in the second pond.Pernicious sludge bulking taking place after 70 days, turn back to dividing plate again, and recover the oxygen-starved area, strengthen the effect of anaerobic selector, it is constant to keep DO concentration, and sludge bulking is under control immediately, and SVI is reduced between the 150-250mL/g.
Claims (10)
1. a biological denitrification process stably maintaining sludge microdilatancy realizes energy-conservation device, according to order from former water feed-water end to the clear water water side, set gradually water tank inlet (1), reactor (13) and second pond (16), it is characterized in that: described water tank inlet (1) is through first peristaltic pump (2), water inlet pipe (20) and valve (3) are communicated with reactor (13), posticum (18) above the reactor (13) is communicated with second pond (16) through fresh water pipeline (19) and valve, the middle part of reactor (13) is through backflow nitrification liquid pipeline (9), second peristaltic pump (24) and valve are communicated with anoxia cell chamber (14), separator (8) is set in the second pond (16), branch of the bottom sludge pipe of second pond (16) is through mud return line (11), the 3rd peristaltic pump (25) and valve are communicated with anoxia cell chamber (14), another branch connects excess sludge pipe (12) and valve, be provided with at least four road dividing plates in the reactor (13), the staggered flowing water communicating aperture (22) that has of adjacent separator, the feed-water end of reactor (13) is provided with at least one anoxia cell chamber (14), be provided with agitator (4) in the anoxia cell chamber (14), at least three aerobic lattice chambers (15) are set after the anoxia cell chamber, and each aerobic lattice chamber all is provided with dissolved oxygen probe (17) and the aeration head (5) that can accurately control DO concentration, the signal wire of each dissolved oxygen probe is connected with the signal input part of PID Controlling System (23), each aeration head (5) connects air compressor (7) through air flowmeter (6), the trip switch of air compressor and each peristaltic pump is connected with the control signal output terminal of PID Controlling System (23), by the switching and the aperture of PID Controlling System control air compressor (7) and each peristaltic pump.
2. biological denitrification process stably maintaining sludge microdilatancy according to claim 1 realizes energy-conservation device, it is characterized in that: total lattice chamber of described reactor (13) is divided at least 5 lattice chambers or many gallerys, at least 3 aerobic lattice chambers wherein are set, the water inlet pipe of described second pond is at the center, through rising pipe (10) discharge system, the volume of second pond is that 3-5h designs according to hydraulic detention time to effluent weir (26) in the peripheral overflow water outlet.
3. one kind is utilized the biological denitrification process stably maintaining sludge microdilatancy of the described device of claim 1-2 to realize method for saving energy, it is characterized in that: by the switching of PID Controlling System (23) control air compressor (7) and each peristaltic pump and the aperture of each valve (3), the flooding velocity of described water inlet pipe (20), the returned sluge flow of the nitrification liquid quantity of reflux of backflow nitrification liquid pipeline (9) and mud return line (11) is by changing the rotating speed of peristaltic pump, change valve opening or change the pump line caliber and regulate, the aeration rate of conditioned reaction device (13) aerobic zone, the dissolved oxygen concentration of regulating aerobic zone is in 0.5-1.2mg/L optimal value scope, the control influent load, the sludge loading of regulating second pond (16) is in 0.22-0.35kgCOD/kgMLSS/d.
4. biological denitrification process stably maintaining sludge microdilatancy according to claim 3 realizes method for saving energy, it is characterized in that: the mud of described second pond (16) in the sludge volume index long-term control of at least 5 sludge ages at 150-250mL/g.
5. biological denitrification process stably maintaining sludge microdilatancy according to claim 3 realizes method for saving energy, it is characterized in that: assurance technology is moved at normal temperatures, as low temperature environment, suitably increase aeration rate and keep the higher DO concentration of aerobic zone, exceed 0.5mg/L than the DO between normal epoch.
6. biological denitrification process stably maintaining sludge microdilatancy according to claim 3 realizes method for saving energy, it is characterized in that: under the condition that N, P nutritive substance lack, in water inlet, add the corresponding water inlet COD/N/P ratio of regulating in 100: 5: 1 scopes of normal value.
7. biological denitrification process stably maintaining sludge microdilatancy according to claim 3 realizes method for saving energy, it is characterized in that: when sludge loading is lower than 0.20kgCOD/kgMLSS/d, suitably improve sludge loading to the 0.25kgCOD/kgMLSS/d by the mode that increases sludge volume; When sludge loading is higher than 0.38kgCOD/kgMLSS/d, suitably reduce sludge loading to the 0.25kgCOD/kgMLSS/d by the mode that reduces sludge volume or prolong hydraulic detention time.
8. biological denitrification process stably maintaining sludge microdilatancy according to claim 3 realizes method for saving energy, it is characterized in that: when mud SVI was higher than 250mL/g and thread fungus index continuously and surpasses 3 in 3 days, or the second pond mud height is when rising to 80% the highest mud position, can suitably increase aeration rate and keep the higher DO concentration of aerobic zone, exceed 0.5mg/L than the DO between normal epoch, and the mode of increase sludge volume suitably improves sludge loading.
9. biological denitrification process stably maintaining sludge microdilatancy according to claim 3 realizes method for saving energy, it is characterized in that: when mud SVI was higher than 250mL/g and thread fungus index continuously and surpasses 3 in 3 days, or the second pond mud height is when rising to 80% the highest mud position, under the condition that does not increase the oxygen-starved area volume, can strengthen the effect of anoxic biological selector by increasing the anoxia cell chamber, suppress hyphomycetic further breeding.
10. biological denitrification process stably maintaining sludge microdilatancy according to claim 3 realizes method for saving energy, it is characterized in that: when the water outlet ammonia nitrogen concentration surpasses discharge index, can suitably increase aeration rate and keep the higher DO concentration of aerobic zone, exceed 0.5mg/L than the DO between normal epoch; The volume of the anoxia cell chamber (14) that is provided with or hydraulic detention time foot have guaranteed that denitrification is back to the nitric nitrogen concentration that is contained the nitrification liquid of anoxia cell chamber (14) from aerobic lattice chamber (15) end; The volume of the aerobic lattice chamber (15) that is provided with or hydraulic detention time foot have guaranteed that the ammonia nitrogen concentration of water outlet is lower than discharge index under low DO condition.
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