CN103708614B - Anaerobic ammonia oxidation and aerobic oxygen limited starting method based on MBBR (Moving Bed Biofilm Reactor) - Google Patents
Anaerobic ammonia oxidation and aerobic oxygen limited starting method based on MBBR (Moving Bed Biofilm Reactor) Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 37
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 17
- 239000001301 oxygen Substances 0.000 title claims abstract description 17
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 17
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title abstract description 16
- 230000003647 oxidation Effects 0.000 title abstract description 12
- 238000007254 oxidation reaction Methods 0.000 title abstract description 12
- 229910021529 ammonia Inorganic materials 0.000 title abstract description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 49
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 25
- 239000010802 sludge Substances 0.000 claims abstract description 18
- 239000010865 sewage Substances 0.000 claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 51
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 46
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 claims description 15
- AHEWZZJEDQVLOP-UHFFFAOYSA-N monobromobimane Chemical compound BrCC1=C(C)C(=O)N2N1C(C)=C(C)C2=O AHEWZZJEDQVLOP-UHFFFAOYSA-N 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 239000000945 filler Substances 0.000 claims description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 9
- 238000011081 inoculation Methods 0.000 claims description 9
- 238000005273 aeration Methods 0.000 claims description 8
- 239000000463 material Substances 0.000 claims description 8
- 238000012856 packing Methods 0.000 claims description 7
- 229910002651 NO3 Inorganic materials 0.000 claims description 5
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 5
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims description 5
- 238000012546 transfer Methods 0.000 claims description 3
- 230000008569 process Effects 0.000 abstract description 17
- 230000000694 effects Effects 0.000 abstract description 16
- 229910052799 carbon Inorganic materials 0.000 abstract description 10
- 244000005700 microbiome Species 0.000 abstract description 7
- 239000007789 gas Substances 0.000 abstract description 3
- 241001453382 Nitrosomonadales Species 0.000 description 10
- 241000894006 Bacteria Species 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 230000000813 microbial effect Effects 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 230000001546 nitrifying effect Effects 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 241000108664 Nitrobacteria Species 0.000 description 2
- 230000001351 cycling effect Effects 0.000 description 2
- 238000012851 eutrophication Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000001580 bacterial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000003653 coastal water Substances 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000035764 nutrition Effects 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
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- Y02W10/12—
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses an anaerobic ammonia oxidation and aerobic oxygen limited starting method based on an MBBR (Moving Bed Biofilm Reactor), belonging to the field of sewage treatment. By adopting an MBBR process for starting an anaerobic ammonia oxidation process, the starting method aiming at solving the problems that in the process of starting the anaerobic ammonia oxidation by using an activated sludge process in the prior art, sludge is easy to float upwards with generated gas and run away, a film is not easily hung on the microorganisms, the microorganisms are difficult to enrich and easy to jam after long-time running in the process of starting the anaerobic ammonia oxidation by using a biofilm method, and the previous methods are low in starting speed, and relatively difficult to realize engineering application. The technical scheme disclosed by the invention comprises nitrification starting, aerobic starting, and anaerobic ammonia oxidation running, only ordinary activated sludge is inoculated, a significant anaerobic ammonia oxidation effect can occur after 120-150d, and finally the total nitrogen film surface load reaches above 7.9gN/m<2>/d. The process disclosed by the invention is high in starting speed, high in biofilm activity, and reliable in running, and the total nitrogen removal is efficient, stable and low-carbon.
Description
Technical field
The invention belongs to sewage treatment area, be specifically related to a kind of Anammox based on MBBR aerobic limit oxygen starting method.
Background technology
There is Nitrogen Cycling in nature, and keeps balance.In recent years, due to artificially, Nitrogen Cycling has suffered destruction, result in intermediate accumulation, and cause the eutrophication of water body day by day serious, lake " wawter bloom " and coastal waters " red tide " happens occasionally, and becomes worse.Body eutrophication has jeopardized all conglomeraties such as agricultural, fishery, tourism, and forms grave danger to drinking water hygiene and food safety.Therefore, denitrogenation has become the important theme in sewage disposal.In eighties of last century, people act as basis with nitrification and denitrification, and the technical system of the wastewater biological denitrificaion of structure plays a role in denitrogenation of waste water, but there are problems, as: long flow path, nitric efficiency is low, and initial cost is high; Oxygen-supplying amount is large, and working cost is high; Denitrification process often needs additional carbon; And be present in dephosphorization process and there is the problems such as carbon source contention.Therefore, new biological denitrificaion theory and technology meets the tendency, and developed rapidly, as: simultaneous nitrification-denitrification technology, short-cut nitrification and denitrification technology, Anammox technology etc., the techniques such as SHRANON-ANAMOX, CANON, DENAMMOX of wherein setting up based on Anammox attract most attention.
Anammox (Anaerobic Ammonium Oxidation is called for short ANAMMOX) is with NO
2 --N is electron acceptor(EA), CO
2for inorganic carbon source, under anaerobic, by NH
4 +-N is oxidized to N
2bioprocess.ANAMMOX technique traditional nitrification-denitrification technique of comparing has the advantage such as the aeration rate of saving 50% and the organic carbon source of 100%, so once finding the broad interest just causing numerous investigator.But ANAMMOX bacteria growing speed is low, and (the highest growth rate is 0.0027h
-1), the generation cycle long (11d), the first in the world seat ANAMMOX biological denitrificaion Engineering Projects reaches 3.5 years start time, and therefore start time, length was the limiting factor that restriction ANAMMOX technique is promoted.
Analyze reason, first, although anaerobic ammonia oxidizing bacteria (AAOB) extensively exists, floating mustiness bacterium, nitrifier, denitrifying bacteria all can be used as provenance, but because AAOB cell concn is low, do not express anaerobic ammoxidation activity, only have as cell concn >10
10-10
11individual/more than mL time just manifest anaerobic ammoxidation activity; Secondly, though a lot of bacterium has ANAMMOX activity, need specified conditions just can express, when condition is suitable for, its metabolic way changes ANAMMOX process into; Again, anaerobic ammonium oxidation process is gas generation process, initial start stage, and mud easily floats, loss, and cell concn is difficult to enrichment and increases, and has both added startup difficulty, and also substantially prolongs the startup cycle.Can find out, the key that Anammox starts is that holding of starting period mud is stayed and enrichment.
Activated sludge process mud-water separation weak effect, the startup for Anammox is unfavorable; Stay effect better although biological filter, catalytic oxidation etc. are held, easily block in longer start-up course, once need recoil, then totally unfavorable to startup process; MBBR (Moving Bed Biolfim Reactor, MBBR) be suspending carrier by adding some amount in reactor, improve the biomass in reactor and biological species, thus improve the processing efficiency of reactor, floating stuffing proportion is close to water, with water body similar density before and after biofilm, make it can suspend in water, Anammox can be met requirement is stayed for holding of startup, again can operation scheme flexible, prevent from blocking, but in actual procedure, find that the floating stuffing biofilm cycle is long, the problems such as toggle speed is undesirable.Once address these problems, the application of MBBR on Anammox must be strengthened, solve the problems such as Anammox not easily starts, the startup cycle is long, realize the low-carbon (LC) of sewage water denitrification, efficient.
Summary of the invention
In order to solve in prior art MBBR Anammox not easy to be filmed, not easily start, the problem such as the startup cycle is long, the present invention proposes a kind of Anammox anaerobism starting method based on MBBR, biofilm speed is fast, fluidizing performance good, the startup cycle is short, processing load advantages of higher to adopt this MBBR method for pretreating to have.
Technical solution of the present invention comprises:
Anammox based on a MBBR aerobic limit oxygen starting method, comprises the following steps:
1) select biologic packing material to fill, this biologic packing material specific surface area is greater than 500m
2/ m
3, in cylindric, before biofilm, filler proportion is 0.93-0.97, porosity of=90%, and the filling ratio of filler is 35-55%;
2) nitrated startup, this is nitrated carries out when being enabled in water temperature 12-35 DEG C, inoculation sewage disposal plant aeration tank active sludge, sludge concentration>=2.0g/L, reactor ammonia nitrogen removal load>=0.05kgN/kgMLSS/d in inoculation post-reactor; Fully mix with biologic packing material after seed sludge being dropped into reactor, employing intermittent mode runs, influent ammonium concentration is 100-300mg/L, water inlet total alkalinity is that 600-2000mg/L(is with calcium carbonate), control dissolved oxygen is 2.0-6.5mg/L, and aeration runs until ammonia nitrogen consumption is greater than 90% in reactor, water and mud are all discharged after stopping by reaction, enter next cycle, repeat this operation scheme, until ammonia nitrogen face load>=3.00gN/m
2/ d;
3) aerobic startup, this is aerobic carries out when being enabled in water temperature 25-35 DEG C, and adopt Continuous Flow mode to run, influent ammonium concentration is 100-300mg/L, and controlling pH in reactor is 7.5-8.2, and control dissolved oxygen is 0.3-1.4mg/L, and power of agitator is 2-4W/m
3, controlling residence time guarantee water outlet ammonia nitrogen is the 30-40% of influent ammonia nitrogen, until nitrite growing amount and nitrate growing amount sum/ammonia nitrogen consumption are down to less than 0.4 in reactor;
4) Anammox runs, this Anammox carries out when operating in water temperature 25-35 DEG C, when nitrite growing amount in reactor and nitrate growing amount sum/ammonia nitrogen consumption are down to after below 0.4, transfer Continuous Flow anaerobism to and run, carrying out anaerobism power of agitator is 5-15W/m
3control water temperature 25-35 DEG C, control influent ammonia nitrogen 50-80mg/L, water inlet nitrite nitrogen 60-110mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3, and inlet flow-patterm is 7.3-7.9, when water outlet ammonia nitrogen is less than 5mg/L, namely shorten the residence time, each shorter residence time is no more than 1h, until total nitrogen face load>=2.000gN/m
2/ d; Continue to maintain anaerobism to run, anaerobism power of agitator is 5-15W/m
3control water temperature 25-35 DEG C, control influent ammonia nitrogen 50-300mg/L, water inlet nitrite nitrogen 70-400mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3, and inlet flow-patterm is 7.3-7.9, namely shortens the residence time when water outlet ammonia nitrogen is less than 10mg/L, each shorter residence time is no more than 1h, until total nitrogen face load reaches 7.9gN/m
2/ more than d.
The Advantageous Effects that the present invention brings:
The present invention proposes a kind of Anammox based on MBBR aerobic limit oxygen starting method, compared with prior art, the present invention has the following advantages:
1) the present invention is by conjunction with MBBR and anaerobic ammonia oxidation process, effectively solves activated sludge process and is difficult to the problems such as enrichment anaerobic ammonia oxidizing bacteria and biomembrance process easily block;
2) by adopting the mode of first nitrated biofilm, rear aerobic limit oxygen Anammox biofilm, the anaerobic ammonia oxidizing bacteria not problem such as easy to be filmed can effectively be solved;
3) toggle speed is fast, without under any anaerobic ammonia oxidizing bacteria inoculation condition, adopts ordinary activated sludge to start, the whole process obvious Anammox effect that only needed namely occur for 120-150 days;
4) processing load is high, and when water temperature 25 DEG C, during 40% filling ratio, water inlet total nitrogen 200mg/L, the total nitrogen face load of filler can reach 9.5gN/m
2/ d, corresponding total nitrogen volumetric loading can reach 1.90kgN/m
3/ d, takes up an area little, simple to operate, reliable;
5) start-up course influent ammonia nitrogen scope is relatively large, can realize starting fast and steady running within the scope of 50-300mg/L, is applicable to most sewage situation;
6) give the media-filling rate started for Anammox anaerobism and specific surface area requirement, this filling ratio and specific surface area had both considered biological enrichment, considered again fluidisation that is aerobic, anaerobic condition.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, explanation clear, complete is further done to the present invention:
Fig. 1 is the Inlet and outlet water changing conditions figure of ammonia nitrogen in Anammox start-up course of the present invention;
Fig. 2 is the Inlet and outlet water changing conditions figure of Anammox start-up course Nitrite Nitrogen of the present invention;
Fig. 3 is the Inlet and outlet water changing conditions figure of nitrate nitrogen in Anammox start-up course of the present invention;
Fig. 4 is the changing conditions figure of feature stoichiometric coefficient in Anammox start-up course of the present invention;
Fig. 5 is in Anammox start-up course of the present invention, the hydraulic detention time of reactor, total nitrogen face load and total nitrogen volumetric loading changing conditions figure.
Embodiment
In order to make object of the present invention, technical scheme and advantage clearer, clear and definite, below with reference to specific embodiment, the present invention is described in more detail.
The present invention, shown in composition graphs 1 to Fig. 5, a kind of Anammox based on MBBR aerobic limit oxygen starting method, comprises the following steps:
Embodiment 1:
Step 1:MBBR technique floating stuffing specific surface area>=500m used
2/ m
3, proportion is 0.95, diameter 25cm, thick 10cm, reactor volume 5m
3, add floating stuffing 2.50m
3, filling ratio 50%;
Step 2: anaerobic ammonia oxidizing bacteria is biofilm on filler not easily, and the easy biofilm of nitrobacteria, and nitrifying bacteria community is one of Anammox flora source, therefore first carry out nitrated startup.Nitrated startup, this is nitrated carries out when being enabled in water temperature 20.1-20.4 DEG C, inoculation sewage disposal plant aeration tank active sludge, and in inoculation post-reactor, sludge concentration is 3.88g/L, and reactor ammonia nitrogen removal load is 0.056kgN/kgMLSS/d; Fully mix with biologic packing material after seed sludge being dropped into reactor, employing intermittent mode runs, influent ammonium concentration is 150-160mg/L, and water inlet total alkalinity is 800.5-820.3mg/L, and control dissolved oxygen is 4.0-6.0mg/L, aeration runs until ammonia nitrogen consumption is greater than 90% in reactor, water and mud are all discharged after stopping by reaction, enter next cycle, repeat this operation scheme, through 30 cycles (0-15d), ammonia nitrogen face load reaches 3.12gN/m
2/ d, now filler entirety is in deep yellow, and microbial film is ripe;
Step 3: nitrobacteria is the important sources of Anammox bacterial classification, by keeping aerobic condition, allowing it keep active, can improve bacterium source activity, ensure its transformation efficiency; Simultaneously, anaerobic ammonia oxidizing bacteria is anerobe, need growth under anaerobic, when carrying out limit oxygen aeration, because nitrifying bacteria community activity is high, Dissolved Oxygen in Water can be consumed rapidly, create the microenvironment of anaerobism, meanwhile, due to the reservation of nitrifying bacteria community activity, it is transformed advantageously to anaerobic ammonia oxidizing bacteria.Aerobic startup, this is aerobic carries out when being enabled in water temperature 30-32 DEG C, and adopt Continuous Flow mode to run, influent ammonium concentration is 155-170mg/L, and controlling pH in reactor is 7.7-8.1, and control dissolved oxygen is 0.7-1.1mg/L, and power of agitator is 3.5W/m
3, the control residence time is 8h, and for ensureing that water outlet ammonia nitrogen is the 30-40% of influent ammonia nitrogen, progressively shorten the residence time, during to 127d, in reactor, nitrite and nitrate growing amount sum/ammonia nitrogen consumption are down to 0.381; In tradition denitrogenation path, the removal of total nitrogen cannot be realized under the condition not having organic carbon source, the consumption of ammonia nitrogen should be suitable with the nitrite nitrogen generated and nitrate nitrogen sum, only has Anammox approach, could realize not having the total nitrogen removal under organic carbon source condition.When this ratio is down to less than 0.4, think that Anammox phenomenon is obvious, Anammox starts successfully.Can obviously find out from observation, the microbial film of reactor transforms from yellow to incarnadine gradually;
Step 4: Anammox runs, from 128d, transfer Continuous Flow anaerobism to run, anaerobism power of agitator is 12W/m
3, control influent ammonia nitrogen 70-75mg/L, water inlet nitrite nitrogen 85-95mg/L, inlet flow-patterm 7.3-7.9, the residence time is 6.31h, progressively shortens residence time guarantee water outlet ammonia nitrogen and is greater than 5mg/L, reach 2.03gN/m to 163d total nitrogen face load
2/ d, has now had obvious Anammox to react in reactor, aerogenesis is obvious, and redness is brighter, and to 214d, total nitrogen face load reaches 7.98gN/m
2/ d, volumetric loading reaches 1.99kgN/m
3/ d; System is mature and stable.The nitrate nitrogen of the nitrite nitrogen consumed in reaction process and the ratio of ammonia nitrogen, generation and the ratio of ammonia nitrogen after stabilization mean value are respectively 1.15 and 0.20, with 1.31 of Anammox theoretical value, 0.26 close.
Under ordinary activated sludge inoculation condition, Anammox startup lasts 127d, and total nitrogen face load reaches 7.98gN/m
2/ d lasts 214d.
Embodiment 2:
For the running condition of checking MBBR-ANAMMOX under high ammonia-nitrogen condition, proceed to 214 days in embodiment 1, total nitrogen face load reaches 7.98gN/m
2/ d, now volumetric loading is 1.99kgN/m
3/ d, after system is mature and stable, continue anaerobism and run, anaerobism power of agitator is 13W/m
3, control influent ammonia nitrogen 270-275mg/L, water inlet nitrite nitrogen 315-330mg/L, inlet flow-patterm 7.3-7.9, tends towards stability through 90d reactor operating mode, and total nitrogen face load reaches 20.83gN/m
2/ d, now volumetric loading is 5.21kgN/m
3/ d, the raising of load is more conducive to Anammox due to high ammonia nitrogen.
Can find out from Fig. 1, Fig. 2, Fig. 3: the changing conditions of nitrogen whole Anammox start-up course;
Fig. 4: the feature stoichiometric coefficient of Anammox reaction refers to, the ratio (R of the ammonia nitrogen of the nitrite nitrogen that reaction consumes and consumption
1), the ratio (R of ammonia nitrogen of nitrate nitrogen that reaction generates and consumption
2), these two ratios are typical stoichiometric coefficients of Anammox reaction, and theoretical value is respectively 1.31,0.26, are to judge that whether reaction is the major criterion of Anammox, and along with the startup of Anammox, this ratio more and more levels off to theoretical value; Feature stoichiometric coefficient (R
3) refer to the ratio of ammonia nitrogen of nitrite nitrogen and nitrate nitrogen sum and the consumption generated in reacting, be mainly used in the degree of closeness of nitrogen change and Anammox feature stoichiometric number in Indicator Reaction process, for judging the enrichment condition of anaerobic ammonia oxidizing bacteria in reactor, in tradition denitrogenation path, when should not nitrogen loss be produced without when organic carbon source, this ratio should close to 1, but Anammox is without the need to organic carbon source, when this ratio is down to less than 0.4, think that Anammox phenomenon is comparatively obvious.
Fig. 5: the face load in whole Anammox start-up course and volumetric loading.
The principal feature of MBBR-ANAMMOX is as follows:
1) microorganism hold stay effective: floating stuffing is by adopting the frame mode of boring, and arrange multiple tracks groove and rack, considerably increase the specific surface area of filler, the present invention selects the specific surface area of floating stuffing at 500m
2/ m
3above, the microbial film quantity that filling surface is adhered to and concentration also greatly increase, and microorganism is held and stays effective, is more conducive to the startup of Anammox;
2) there is the effect of microorganism active selector switch: due to the fluidisation of floating stuffing, facilitate biomembranous renewal, aging and active poor microbial film can come off in time, and discharge system, intrasystem microorganism is allowed to be in higher activity, compare anaerobic ammonium oxidation granular sludge, microorganism active is higher, affects treatment effect without the need to worrying that particle is excessive;
3) form is reacted good: floating stuffing is in fluidized state in reactor, its reaction form is similar to complete, filler and gas, water contact gear ratio are more abundant, improve the effect of mass transmitting of microbial film on filler and water Middle nutrition material, compared with other fixed bed fillers, floating stuffing layer does not have head loss substantially, is conducive to the homogeneity of water distribution, effectively can prevent the stopping state of static bed biomembrane method;
4) start the cycle short: under ordinary activated sludge inoculation condition, Anammox startup lasts 127d, and total nitrogen face load reaches 7.62gN/m
2/ d lasts 214d;
5) processing load is high: the highest total nitrogen face load can reach 20.83gN/m
2/ d, volumetric loading is 5.21kgN/m
3/ d;
6) applied widely: start-up course influent ammonia nitrogen scope is relatively large, can realize starting fast and steady running within the scope of 50-300mg/L, be applicable to most sewage situation.
The part do not addressed in aforesaid way is taked or uses for reference prior art to realize.
It should be noted that, any equivalent way that those skilled in the art make under the instruction of this specification sheets, or obviously variant all should in protection scope of the present invention.
Claims (1)
1., based on an Anammox aerobic limit oxygen starting method of MBBR, it is characterized in that comprising the following steps:
1) select biologic packing material to fill, this biologic packing material specific surface area is greater than 500m
2/ m
3, in cylindric, before biofilm, filler proportion is 0.93-0.97, porosity of=90%, and the filling ratio of filler is 35-55%;
2) nitrated startup: this is nitrated carries out when being enabled in water temperature 12-35 DEG C, inoculation sewage disposal plant aeration tank active sludge, sludge concentration>=2.0g/L, reactor ammonia nitrogen removal load>=0.05kgN/kgMLSS/d in inoculation post-reactor; Fully mix with biologic packing material after seed sludge being dropped into reactor, employing intermittent mode runs, influent ammonium concentration is 100-300mg/L, water inlet total alkalinity is 600-2000mg/L, and control dissolved oxygen is 2.0-6.5mg/L, and aeration runs until ammonia nitrogen consumption is greater than 90% in reactor, water and mud are all discharged after stopping by reaction, enter next cycle, repeat this operation scheme, until ammonia nitrogen face load>=3.00gN/m
2/ d;
3) aerobic startup: this is aerobic carries out when being enabled in water temperature 25-35 DEG C, and adopt Continuous Flow mode to run, influent ammonium concentration is 100-300mg/L, and controlling pH in reactor is 7.5-8.2, and control dissolved oxygen is 0.3-1.4mg/L, and power of agitator is 2-4W/m
3, controlling residence time guarantee water outlet ammonia nitrogen is the 30-40% of influent ammonia nitrogen, until nitrite growing amount and nitrate growing amount sum/ammonia nitrogen consumption are down to less than 0.4 in reactor;
4) Anammox runs: carry out when this Anammox operates in water temperature 25-35 DEG C, when nitrite growing amount in reactor and nitrate growing amount sum/ammonia nitrogen consumption are down to after below 0.4, transfer Continuous Flow anaerobism to run, carrying out anaerobism power of agitator is 5-15W/m
3control water temperature 25-35 DEG C, control influent ammonia nitrogen 50-80mg/L, water inlet nitrite nitrogen 60-110mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3, and inlet flow-patterm is 7.3-7.9, when water outlet ammonia nitrogen is less than 5mg/L, namely shorten the residence time, each shorter residence time is no more than 1h, until total nitrogen face load>=2.000gN/m
2/ d; Continue to maintain anaerobism to run, anaerobism power of agitator is 5-15W/m
3control water temperature 25-35 DEG C, control influent ammonia nitrogen 50-300mg/L, water inlet nitrite nitrogen 70-400mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3, and inlet flow-patterm is 7.3-7.9, namely shortens the residence time when water outlet ammonia nitrogen is less than 10mg/L, each shorter residence time is no more than 1h, until total nitrogen face load reaches 7.9gN/m
2/ more than d.
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| KR100430578B1 (en) * | 2002-02-20 | 2004-05-10 | 송영채 | The organic material and nitrogen removal system using the three phase fluidized bed biofilm reactors |
| JP4948648B2 (en) * | 2007-08-08 | 2012-06-06 | 彭光浩 | Method for removing carbon and nitrogen contaminants in contaminated water using heterotrophic ammonia oxidizing bacteria |
| RU2438997C2 (en) * | 2007-08-08 | 2012-01-10 | Гуаньхао ПЕНГ | Method of removing c and n contaminant compounds using heterotrophic ammonia-oxidising bacteria |
| CN103226366B (en) * | 2013-05-09 | 2017-10-03 | 中国科学院生态环境研究中心 | The control method of short distance nitration Anammox integral type denitrification process |
| CN103408140B (en) * | 2013-08-14 | 2014-12-10 | 哈尔滨工业大学 | Control method realizing CANON process high-efficiency stable operation |
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