CN103723827A - Anaerobic ammonia oxidation anaerobic starting method based on MBBR - Google Patents
Anaerobic ammonia oxidation anaerobic starting method based on MBBR Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 39
- AHEWZZJEDQVLOP-UHFFFAOYSA-N monobromobimane Chemical compound BrCC1=C(C)C(=O)N2N1C(C)=C(C)C2=O AHEWZZJEDQVLOP-UHFFFAOYSA-N 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 13
- 238000007254 oxidation reaction Methods 0.000 title abstract description 13
- 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 40
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 21
- 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 58
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 51
- 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 27
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 239000000945 filler Substances 0.000 claims description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 10
- 238000005273 aeration Methods 0.000 claims description 10
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 238000011081 inoculation Methods 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 7
- 238000012856 packing Methods 0.000 claims description 7
- 238000004904 shortening Methods 0.000 claims description 6
- 238000012546 transfer Methods 0.000 claims description 4
- 230000000694 effects Effects 0.000 abstract description 13
- 229910052799 carbon Inorganic materials 0.000 abstract description 9
- 244000005700 microbiome Species 0.000 abstract description 7
- 239000007789 gas Substances 0.000 abstract description 3
- 238000006396 nitration reaction Methods 0.000 abstract description 2
- 238000007796 conventional method Methods 0.000 abstract 1
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 8
- 241001453382 Nitrosomonadales Species 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 230000000813 microbial effect Effects 0.000 description 7
- 241000894006 Bacteria Species 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 description 4
- 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 3
- 238000012545 processing Methods 0.000 description 3
- 241000108664 Nitrobacteria Species 0.000 description 2
- 241001148470 aerobic bacillus Species 0.000 description 2
- 238000013459 approach Methods 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
- 230000000903 blocking effect Effects 0.000 description 1
- 230000003197 catalytic effect 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
- 239000013067 intermediate product Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000000050 nutritive effect Effects 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
- 230000003068 static effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
The invention discloses an anaerobic ammonia oxidation anaerobic starting method based on MBBR, and belongs to the field of sewage treatment. By adopting MBBR process to start ammonia oxidation process, the method aims at solving the problems that sludge is easy to float and run away with produced gas during the process of starting ammonia oxidation through an activated sludge method, microorganism is not easy to form a film and enrich, and is easy to block during long-time operation during starting ammonia oxidation through a biofilm method, and conventional methods are slow in starting speed and difficult for engineering application. The invention adopts the technical scheme that nitration starting, anaerobic starting and anaerobic ammonia oxidation operation, and only common activated sludge is inoculated, so that an obvious anaerobic ammonia oxidation effect can occur after 160 to 190 d, and finally the total nitrogen film surface load reaches more than 7.4gN/m<2>/d. The method is high in process starting speed and biofilm activity, stable to operate, and efficient, stable and low-carbon in total nitrogen removal.
Description
Technical field
The invention belongs to sewage treatment area, be specifically related to a kind of Anammox anaerobism starting method based on MBBR.
Background technology
There is Nitrogen Cycling in nature, and keeps balance.In recent years, due to artificially, Nitrogen Cycling has been suffered destruction, has caused intermediate product accumulation, causes the eutrophication of water body day by day serious, and 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 drinking water hygiene and food safety are formed to grave danger.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 aspect denitrogenation of waste water, but have 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 have 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., wherein the technique such as the SHRANON-ANAMOX take Anammox as Foundation, CANON, DENAMMOX attracts 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 compare tradition nitrated-denitrification process has the advantages such as 50% the aeration rate of saving and 100% organic carbon source, so once the broad interest of finding just to have caused numerous investigators.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
11when individual/mL is above, just manifest anaerobic ammoxidation activity; Secondly, though a lot of bacterium has ANAMMOX activity, need specified conditions just can express, when condition is suitable, its metabolic way changes ANAMMOX process into; Again, anaerobic ammonium oxidation process is gas generation process, initial start stage, and mud easily floats, runs off, and cell concn is difficult to enrichment and increases, and has both increased startup difficulty, has also greatly extended start-up period.Can find out, the key that Anammox starts is that holding of starting period mud stay and enrichment.
Activated sludge process mud-water separation weak effect, unfavorable for the startup of Anammox; Although biological filter, catalytic oxidation etc. are held, stay effect better, in longer start-up course, easily stop up, once need recoil, totally unfavorable to startup process; MBBR (Moving Bed Biolfim Reactor, MBBR) be the suspending carrier by add some amount in reactor, improve biomass and biological species in reactor, thereby improve the processing efficiency of reactor, floating stuffing proportion approaches water, close with water body density before and after biofilm, it can be suspended in water, can meet Anammox and stay requirement for holding of startup, again can operation scheme flexible, prevent from blocking, but in actual procedure, find the problems such as the floating stuffing biofilm cycle is long, and toggle speed is undesirable.Once address these problems, must strengthen the application of MBBR on Anammox, solve the problems such as Anammox is difficult for starting, start-up period is long, realize the low-carbon (LC), efficient of sewage water denitrification.
Summary of the invention
For solve in prior art MBBR Anammox not easy to be filmed, be difficult for starting, the problem such as start-up period is long, the present invention proposes a kind of Anammox anaerobism starting method based on MBBR, adopt this MBBR method for pretreating to have that biofilm speed is fast, fluidizing performance good, start-up period is short, process load advantages of higher.
Technical solution of the present invention comprises:
An Anammox anaerobism starting method based on MBBR, 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, being cylindric, before biofilm, filler proportion is 0.93-0.97, porosity>=90%, the filling ratio of filler is 35-65%;
2) nitrated startup: this is nitrated carries out while being enabled in water temperature 12-35 ℃, inoculation sewage disposal plant aeration tank active sludge, sludge concentration>=2.0g/L in inoculation post-reactor, reactor ammonia nitrogen removal load>=0.05kgN/kgMLSS/d; After being dropped into reactor, fully mixes with biologic packing material seed sludge, the operation of employing intermittent mode, influent ammonium concentration is 100-300mg/L, water inlet total alkalinity is that 600-2000mg/L(is in calcium carbonate), control dissolved oxygen is 2.0-6.5mg/L, aeration operation is until the interior ammonia nitrogen consumption of reactor is greater than 90%, after reaction stops, water and mud are all discharged, enter next cycle, repeat this operation scheme, until ammonia nitrogen face load>=3.00gN/m
2/ d;
3) anaerobism starts: when this anaerobism is enabled in water temperature 25-35 ℃, carry out, adopt intermittent mode operation, influent ammonium concentration is 100-300mg/L, and total alkalinity is that 300-1500mg/L(is in calcium carbonate); According to aerobic, anaerobic sequence alternate, move several cycles, time aerobic, anaerobism in each cycle is 1-5h, anaerobism time and aerobic time ratio are 1.0-1.2:1, during aerobic operation, carrying out aeration and controlling dissolved oxygen is 1.0-2.5mg/L, dissolved oxygen <0.5mg/L is stirred and controls in anaerobism operation, and power of agitator is 5-15W/m
3, until ammonia nitrogen consumption is greater than 85% of influent ammonia nitrogen in reactor, after reaction stops, water is all discharged, enter next cycle, rerun according to this; 5 cycles of every operation, adjust anaerobism time and aerobic time ratio, each ratio increases 1.0-1.2, and all the other operational conditionss are constant, until anaerobism time and aerobic time ratio increase to more than 7.0; Transfer the operation of Continuous Flow anaerobism to, anaerobism power of agitator is 5-15W/m
3control influent ammonia nitrogen 50-200mg/L, water inlet nitrite nitrogen 50-200mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3:1, water inlet pH is 7.3-7.9, when water outlet ammonia nitrogen is less than 10mg/L, shorten the residence time, each shortening is no more than 1h, until nitrite nitrogen consumption/ammonia nitrogen consumption reaches more than 1.0 in reactor;
4) Anammox operation: this Anammox carries out while operating in water temperature 25-35 ℃, after nitrite nitrogen consumption/ammonia nitrogen consumption reaches more than 1.0 in reactor, continues to maintain anaerobism operation, and anaerobism power of agitator is 5-15W/m
3, control influent ammonia nitrogen 50-300mg/L, water inlet nitrite nitrogen 70-400mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3:1, and water inlet pH is 7.3-7.9, when water outlet ammonia nitrogen is less than 10mg/L, shortens the residence time, each shortening is no more than 1h, until total nitrogen face load reaches 7.4gN/m
2more than/d.
The useful technique effect that the present invention brings:
The present invention proposes a kind of Anammox anaerobism starting method based on MBBR, compared with prior art, the present invention has the following advantages:
1) the present invention, 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 the easy obstruction of biomembrance process;
2), by adopting the first mode of nitrated biofilm, rear Anammox biofilm, can effectively solve the not problem such as easy to be filmed of anaerobic ammonia oxidizing bacteria;
3) toggle speed is fast, under without any anaerobic ammonia oxidizing bacteria inoculation condition, adopts ordinary activated sludge to start, and whole process only needs to have occurred for 160-190 days obvious Anammox effect;
4) processing load is high, when water temperature is 25 ℃, and 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 within the scope of 50-300mg/L, realize and starting fast and steady running, is applicable to most sewage situations;
6) provided the media-filling rate and the specific surface area requirement that for Anammox anaerobism, start, this filling ratio and specific surface area had both been considered biological enrichment, considered again the fluidisation of anaerobic condition.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the present invention is done to further clear, complete explanation:
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 feature stoichiometric coefficient changing conditions figure 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, in conjunction with shown in Fig. 1 to Fig. 5, a kind of Anammox anaerobism starting method based on MBBR, 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%;
One of step 2: anaerobic ammonia oxidizing bacteria is difficult for biofilm on filler, and the easy biofilm of nitrobacteria, and the nitrifying bacteria community source that is anaerobic ammonia oxidizing bacteria, therefore first carry out nitrated startup.Nitrated startup, this is nitrated carries out while being enabled in water temperature 20.1-20.4 ℃, inoculation sewage disposal plant aeration tank active sludge, in inoculation post-reactor, sludge concentration is 3.82g/L, reactor ammonia nitrogen removal load is 0.056kgN/kgMLSS/d; After being dropped into reactor, fully mixes with biologic packing material seed sludge, the operation of employing intermittent mode, influent ammonium concentration is 150-160mg/L, and water inlet total alkalinity is that 800-900mg/L(is in calcium carbonate), control dissolved oxygen is 4.0-6.0mg/L, aeration operation is until the interior ammonia nitrogen consumption of reactor is greater than 90%, after reaction stops, water and mud are all discharged, enter next cycle, repeat this operation scheme, through 30 cycles (0-15d), ammonia nitrogen face load reaches 3.06gN/m
2/ d, now the microbial film entirety on filler is yellow, microbial film maturation;
Step 3: nitrobacteria is aerobic bacteria, for preventing in Anammox start-up course, the anaerobic environment of sudden change causes and the mortality of aerobic bacteria causes biofilm detachment, first carries out transitional anaerobism startup.Anaerobism starts, and when this anaerobism is enabled in water temperature 20.3-20.5 ℃, carries out, and adopts intermittent mode operation, and influent ammonium concentration is 140-150mg/L, and total alkalinity is that 700-800mg/L(is in calcium carbonate); According to aerobic, anaerobic sequence alternate, move several cycles, time aerobic, anaerobism in each cycle is 2.5h, anaerobism time and aerobic time ratio are 1.0, during aerobic operation, carrying out aeration and controlling dissolved oxygen is 1.5-2.0mg/L, dissolved oxygen <0.3mg/L is stirred and controls in anaerobism operation, and power of agitator is 9W/m
3, until ammonia nitrogen consumption is greater than 85% of influent ammonia nitrogen in reactor, after reaction stops, water is all discharged, enter next cycle, rerun according to this; 5 cycles of every operation, adjust anaerobism time and aerobic time ratio, increase by 1.0 at every turn, all the other operational conditionss are constant, and through 40 cycles (16-35d), aerobic/anaerobic time ratio increases to 8.0; By transitional anaerobism, start, microorganism adapts to anaerobic environment gradually, and 36d rises and transfers the operation of Continuous Flow anaerobism to, and anaerobism power of agitator is 9W/m
3, control influent ammonia nitrogen 50-55mg/L, water inlet nitrite nitrogen 50-55mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3:1, and water inlet pH is 7.3-7.9, and the control residence time is 23h, when being less than 10mg/L, water outlet ammonia nitrogen shortens the residence time, each shortening is no more than 1h, to 101d, starts to occur the obvious consumption of nitrite nitrogen in reactor, microbial film color transfers redness to gradually by Huang, to 166d, the residence time is 12h, and nitrite nitrogen consumption/ammonia nitrogen consumption reaches 1.01.Under the anaerobic conditions without organic carbon source, nitrite nitrogen can not carry out anti-nitration reaction, and the significantly sacrificing of nitrite nitrogen has proved to have occurred anaerobic ammonium oxidation process.From nitrite nitrogen consumption/ammonia nitrogen consumption, reaching 1.01 can assert, had obvious Anammox reaction, and aerogenesis is obvious in reactor, and microbial film is changed to redness gradually by yellow, and Anammox starts successfully;
Step 4: Anammox operation, after nitrite nitrogen consumption/ammonia nitrogen consumption reaches 1.01 in reactor, continue to maintain anaerobism operation, anaerobism power of agitator is 13W/m
3control influent ammonia nitrogen 70-75mg/L, water inlet nitrite nitrogen 75-85mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3:1, water inlet pH is 7.3-7.9, when being less than 10mg/L, water outlet ammonia nitrogen shortens the residence time, each shortening is no more than 1h, and operation in this way, to 246d, the residence time is only 1.714h, and total nitrogen face load reaches 7.71gN/m
2/ d, now volumetric loading is 1.92kgN/m
3/ d, system is mature and stable.The nitrite nitrogen consuming in reaction process and the ratio of ammonia nitrogen, the nitrate nitrogen of generation and the ratio of ammonia nitrogen are respectively 1.19 and 0.21 at stable rear mean value, approach with 1.31,0.26 of Anammox theoretical value.
Under ordinary activated sludge inoculation condition, Anammox startup lasts 166d, and total nitrogen face load reaches 7.62gN/m
2/ d lasts 246d.
Embodiment 2:
For the running condition of checking MBBR-ANAMMOX under high ammonia nitrogen condition, at embodiment 1, proceed to 246 days, total nitrogen face load reaches 7.71gN/m
2/ d, now volumetric loading is 1.92kgN/m
3/ d, after system is mature and stable, continues anaerobism operation, and anaerobism power of agitator is 13W/m
3, control influent ammonia nitrogen 270-275mg/L, water inlet nitrite nitrogen 315-330mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3:1, and water inlet pH7.3-7.9 tends towards stability through 95d reactor operating mode, and total nitrogen face load reaches 20.83gN/m
2/ d, now volumetric loading is 5.21kgN/m
3/ d, compares embodiment 1, and what total nitrogen was loaded increases substantially mainly due to the carrying out that is more conducive to Anammox under high ammonia nitrogen condition.
From Fig. 1, Fig. 2, Fig. 3, can find out: the changing conditions of nitrogen whole Anammox start-up course, should not there is the loss of sub-nitrogen in tradition denitrogenation path, only have Anammox path just can under the anaerobic condition without organic carbon source, realize the removal of total nitrogen under the anaerobic condition without organic carbon source;
Fig. 4: the feature stoichiometric coefficient of Anammox reaction refers to, the ratio (R of the nitrite nitrogen that reaction consumes and the ammonia nitrogen of consumption
1), the nitrate nitrogen that generates of reaction and the ratio (R of the ammonia nitrogen of consumption
2), these two ratios are typical stoichiometric coefficients of Anammox reaction, and theoretical value is respectively 1.31,0.26, is judge whether react is the major criterion of Anammox, and along with the startup of Anammox, this ratio more and more levels off to theoretical value.
Fig. 5: face load and volumetric loading in whole Anammox start-up course.
The principal feature of MBBR-ANAMMOX is as follows:
1) microorganism hold stay effective: floating stuffing, by adopting the frame mode of boring, arranges multiple tracks groove and rack, has greatly increased the specific surface area of filler, and the present invention selects the specific surface area of floating stuffing at 500m
2/ m
3above, microbial film quantity and concentration that filling surface adheres to are also greatly increased, microorganism is held and stays effectively, 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, promoted biomembranous renewal, aging and active poor microbial film can come off in time, and discharge system, allow intrasystem microorganism in higher activity, compare anaerobic ammonium oxidation granular sludge, microorganism active is higher, without worrying the excessive treatment effect that affects of particle;
3) reaction form good: floating stuffing in reactor in fluidized state, its reaction form is similar to complete, filler and gas, water contact gear ratio are more abundant, improved the effect of mass transmitting of nutritive substance in microbial film on filler and water, compared with other fixed bed fillers, floating stuffing layer does not have head loss substantially, is conducive to the homogeneity of water distribution, can effectively prevent the stopping state of static bed biomembrane method;
4) start-up period is short: under ordinary activated sludge inoculation condition, Anammox startup lasts 166d, and total nitrogen face load reaches 7.62gN/m
2/ d lasts 246d;
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 within the scope of 50-300mg/L, realize and starting fast and steady running, be applicable to most sewage situations.
The part of not addressing in aforesaid way is taked or is used for reference prior art and can 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 be in protection scope of the present invention.
Claims (1)
1. the Anammox anaerobism starting method based on MBBR, 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, being cylindric, before biofilm, filler proportion is 0.93-0.97, porosity>=90%, the filling ratio of filler is 35-65%;
2) nitrated startup: this is nitrated carries out while being enabled in water temperature 12-35 ℃, inoculation sewage disposal plant aeration tank active sludge, sludge concentration>=2.0g/L in inoculation post-reactor, reactor ammonia nitrogen removal load>=0.05kgN/kgMLSS/d; After being dropped into reactor, fully mixes with biologic packing material seed sludge, the operation of employing intermittent mode, 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 operation is until the interior ammonia nitrogen consumption of reactor is greater than 90%, after reaction stops, water and mud are all discharged, enter next cycle, repeat this operation scheme, until ammonia nitrogen face load>=3.00gN/m
2/ d;
3) anaerobism starts: when this anaerobism is enabled in water temperature 25-35 ℃, carry out, adopt intermittent mode operation, influent ammonium concentration is 100-300mg/L, and total alkalinity is 300-1500mg/L; According to aerobic, anaerobic sequence alternate, move several cycles, time aerobic, anaerobism in each cycle is 1-5h, anaerobism time and aerobic time ratio are 1.0-1.2:1, during aerobic operation, carrying out aeration and controlling dissolved oxygen is 1.0-2.5mg/L, dissolved oxygen <0.5mg/L is stirred and controls in anaerobism operation, and power of agitator is 5-15W/m
3, until ammonia nitrogen consumption is greater than 85% of influent ammonia nitrogen in reactor, after reaction stops, water is all discharged, enter next cycle, rerun according to this; 5 cycles of every operation, adjust anaerobism time and aerobic time ratio, each ratio increases 1.0-1.2, and all the other operational conditionss are constant, until anaerobism time and aerobic time ratio increase to more than 7.0; Transfer the operation of Continuous Flow anaerobism to, anaerobism power of agitator is 5-15W/m
3control influent ammonia nitrogen 50-200mg/L, water inlet nitrite nitrogen 50-200mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3:1, water inlet pH is 7.3-7.9, when water outlet ammonia nitrogen is less than 10mg/L, shorten the residence time, each shortening is no more than 1h, until nitrite nitrogen consumption/ammonia nitrogen consumption reaches more than 1.0 in reactor;
4) Anammox operation: this Anammox carries out while operating in water temperature 25-35 ℃, after nitrite nitrogen consumption/ammonia nitrogen consumption reaches more than 1.0 in reactor, continues to maintain anaerobism operation, and anaerobism power of agitator is 5-15W/m
3, control influent ammonia nitrogen 50-300mg/L, water inlet nitrite nitrogen 70-400mg/L, water inlet nitrite nitrogen/ammonia nitrogen is 1.0-1.3:1, and water inlet pH is 7.3-7.9, when water outlet ammonia nitrogen is less than 10mg/L, shortens the residence time, each shortening is no more than 1h, until total nitrogen face load reaches 7.4gN/m
2more than/d.
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