CN102515348B - Operating method for high-efficient anaerobic ammonium oxidation reactor - Google Patents
Operating method for high-efficient anaerobic ammonium oxidation reactor Download PDFInfo
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- CN102515348B CN102515348B CN2011104167575A CN201110416757A CN102515348B CN 102515348 B CN102515348 B CN 102515348B CN 2011104167575 A CN2011104167575 A CN 2011104167575A CN 201110416757 A CN201110416757 A CN 201110416757A CN 102515348 B CN102515348 B CN 102515348B
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- 230000003647 oxidation Effects 0.000 title claims abstract description 20
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 20
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 title claims abstract description 12
- 238000011017 operating method Methods 0.000 title abstract 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 88
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 72
- 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 abstract description 44
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 44
- 238000000034 method Methods 0.000 claims abstract description 35
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000010802 sludge Substances 0.000 claims abstract description 27
- 239000002351 wastewater Substances 0.000 claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 9
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000000758 substrate Substances 0.000 claims description 21
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 18
- 241001453382 Nitrosomonadales Species 0.000 claims description 14
- 238000006392 deoxygenation reaction Methods 0.000 claims description 12
- 238000005273 aeration Methods 0.000 claims description 11
- 229910021529 ammonia Inorganic materials 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims description 5
- 239000002245 particle Substances 0.000 claims description 5
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 4
- 150000003863 ammonium salts Chemical class 0.000 claims description 4
- 230000003203 everyday effect Effects 0.000 claims description 3
- 239000007789 gas Substances 0.000 claims description 3
- 239000011785 micronutrient Substances 0.000 claims description 3
- 235000013369 micronutrients Nutrition 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- 239000008399 tap water Substances 0.000 claims description 3
- 235000020679 tap water Nutrition 0.000 claims description 3
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 2
- 239000001110 calcium chloride Substances 0.000 claims description 2
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 2
- 235000019341 magnesium sulphate Nutrition 0.000 claims description 2
- 244000005700 microbiome Species 0.000 claims description 2
- 229940045641 monobasic sodium phosphate Drugs 0.000 claims description 2
- 238000004904 shortening Methods 0.000 claims description 2
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 claims description 2
- 241000894006 Bacteria Species 0.000 abstract description 6
- 239000011159 matrix material Substances 0.000 abstract description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 3
- 230000000452 restraining effect Effects 0.000 abstract 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 4
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 230000003321 amplification Effects 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000011081 inoculation Methods 0.000 description 2
- 238000003199 nucleic acid amplification method Methods 0.000 description 2
- 239000011573 trace mineral Substances 0.000 description 2
- 235000013619 trace mineral Nutrition 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000009629 microbiological culture Methods 0.000 description 1
- 230000002572 peristaltic effect Effects 0.000 description 1
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Abstract
The invention discloses an operating method for a high-efficient anaerobic ammonium oxidation reactor. The method comprises the steps of (1) inoculating anaerobic granular sludge in an anaerobic reactor, the wherein the anaerobic granular sludge accounts for 30-90% of total volume of the reactor; and (2) taking nitrogenous simulating wastewater as reaction inflowing water, wherein the temperatureof the reactor is controlled to be in 18-37 DEG C; and in a reactor starting stage, remaining hydraulic power for 12-48h, adjusting reaction operating conditions according to concentration of ammonianitrogen and/or nitrite nitrogen, operating the anaerobic reactor for 30-150d, and forming high-efficient anaerobic ammonium oxidation granular sludge enriched with anaerobic ammonium oxidation bacteria. The method improves total nitrogen load of the reactor in a way that the load is increased gradually by lower load so as to be beneficial to stable increasing of domestication enrichment and nitrogen removing rate of the anaerobic ammonium oxidation bacteria, can effectively avoid matrix restraining of anaerobic ammonium oxidation and is beneficial to reducing process operating cost when the reactor operates under a room temperature condition.
Description
(1) technical field
The present invention relates to the removal method of nitrogen in a kind of waste water, particularly a kind of operation method of efficient anaerobic ammoxidation reactor.
(2) background technology
Anaerobic ammonia oxidizing bacteria can under anaerobic be electron donor with ammonia, and nitrous acid is that electron acceptor(EA) generates the purpose that nitrogen is realized the green removal of nitrogen in the water.As a kind of new bio denitride technology, it is high to have a denitrogenation load based on the anaerobic ammonia oxidation process of anaerobic ammonia oxidizing bacteria, and working cost is low, takes up an area of advantages such as the space is little, and application prospect is very bright.
Yet autotrophic type Anammox bacteria growing is very slow, and the doubling time reaches 11d, and extremely responsive and traditional microbial culture method is difficult to obtain the enrichment culture thing of anaerobic ammonia oxidizing bacteria to envrionment conditions.These characteristics of anaerobic ammonia oxidizing bacteria have determined that the enrichment culture of acquisition efficient anaerobic ammoxidation bacterium is very difficult, thereby it is also very difficult to make that also anaerobic ammonia oxidation reactor will obtain higher nitrogen removal performance.This has seriously restricted the theoretical investigation of anaerobic ammonia oxidizing bacteria and applying of this novel denitrification process.The present invention proposes a kind of operation method of efficient anaerobic ammoxidation reactor, and has important theory and realistic meaning.
(3) summary of the invention
The object of the invention provides a kind of operation method of efficient anaerobic ammoxidation reactor, this method is to improve the reactor operating load than the underload incremental manner, be conducive to the domestication enrichment of anaerobic ammonia oxidizing bacteria and the steady increase that nitrogen is removed speed, and can effectively avoid the matrix of Anammox to suppress, make it reach a higher operating load.
The technical solution used in the present invention is:
A kind of operation method of efficient anaerobic ammoxidation reactor, described method is:
(1) anaerobic grain sludge is inoculated in the anaerobic reactor, anaerobic grain sludge account for overall reactor long-pending 30～90%;
(2) serve as the reaction water inlet with nitrogenous simulated wastewater, regulate simulated wastewater pH value to 7.20～8.70 before the water inlet, and the feeding rare gas element is removed the dissolved oxygen in anaerobic reactor and the simulated wastewater, then simulated wastewater is continuously pumped into reactor, after reactor start-up, stop the reactor aeration is removed dissolved oxygen, only to the deoxygenation of reactor water inlet aeration, temperature of reactor is controlled in 18～37 ℃ and is not required homo(io)thermism, the reactor start-up stage, hydraulic detention time is 12～48h, every day, the monitoring reaction device was intake and the ammonia nitrogen of water outlet and the concentration of nitrite nitrogen, adjust the reactor operational conditions according to ammonia nitrogen and/or nitrite nitrogen concentration, when reactor satisfies following condition (A) or one of (B) time, adjusts water inlet substrate concn and/or hydraulic detention time to increase reactor total nitrogen load; So repeat to adjust, anaerobic reactor forms the anaerobic ammonium oxidation granular sludge of enrichment anaerobic ammonia oxidizing bacteria through the operation of 30～150d, and described substrate concn refers to ammonia nitrogen in the water into and the concentration of nitrite nitrogen; Ammonia nitrogen and the nitrite nitrogen concentration range of adjusting nitrogenous simulated wastewater when described water inlet is initial are 28～84mgL
-1Described condition (A) for water outlet nitrite nitrogen concentration less than 30mg/L, described condition (B) is that difference on the continuous three days water outlet ammonia nitrogen of reactor and the nitrite nitrogen concentration not statistically significant and water outlet nitrite nitrogen concentration are less than 60mg/L.
Described anaerobic ammonium oxidation granular sludge grain diameter 0.5～9mm, optimum particle diameter is 1～3mm, and described particle sphericity is 0.5～1.0, and proportion is greater than 1.
Described step (1) is washed mud with tap water before starting reactor, at hydraulic detention time is to wash 0.5～1d under the condition of 12～48h; The unloading phase hydraulic detention time be 12～48h, to wash out original matrix and impurity.
The method of the dissolved oxygen in the described removal anaerobic reactor of step (2) and the water inlet is: anaerobic reactor exposes to the sun nitrogen earlier to described anaerobic reactor and an aeration deoxygenation of simulated wastewater before starting, start after the reactor with nitrogen only to the deoxygenation of water inlet aeration, stop the deoxygenation of reactor aeration, only to the each aeration time 20min of reaction water inlet; Remove speed when the water inlet total nitrogen and surpass 2.0kg/ (m
3.d) need not the time again the water inlet nitrogen deoxygenation of exposing to the sun.
The described anaerobic reactor operational conditions of step (2) inflation method is one of following: a) reduction of the raising of Jin Shui substrate concn and hydraulic detention time is carried out respectively: the each 3.5～42mgL that improves synchronously of influent ammonia nitrogen and nitrite nitrogen
-1, but the influent concentration of nitrite nitrogen does not surpass 280mg/L; When adjusting hydraulic detention time, when if the hydraulic detention time when adjusting is 2～48h, each hydraulic detention time shortens 1～4h, if during less than 2h, shortening the water flow increasing amount that hydraulic detention time causes at every turn, the hydraulic detention time when adjusting to be equivalent to the flooding quantity that the water inlet of reactor day increases by 0.5～7 reactor effective volume; B) raising of water inlet substrate concn and the adjustment of hydraulic detention time hocket, namely improve described influent ammonia nitrogen and nitrite nitrogen concentration synchronously and hocket with the mode of adjusting hydraulic detention time, the raising of described water inlet substrate concn and the adjustment of hydraulic detention time are with method a); When c) adjusting water inlet substrate concn and hydraulic detention time simultaneously, the total nitrogen that increases load must not and be surpassed the maximum total nitrogen that increases when adjusting water inlet substrate concn and hydraulic detention time respectively and load, and the raising of the substrate concn of described water inlet and the adjustment of hydraulic detention time are with method a); In above inflation method any one method a)～c), if phenomenon appears suppressing in reactor, be that the mass concentration of water outlet nitrite nitrogen is when surpassing 100mg/L, reduce the water inlet substrate concn immediately or improve hydraulic detention time making reactor total nitrogen load reduce by 10～60%, adjust according to above-mentioned anaerobic reactor operational conditions inflation method again.
The component of being made up of following quality in the simulated wastewater of the present invention constitutes: ammonium salt (28～490mgL
-1), nitrite (28～490mgL
-1), SODIUM PHOSPHATE, MONOBASIC 9.0～11mg/L, bitter salt 57.74～64.46mg/L, saleratus 900～1100mg/L, calcium chloride 5.09～6.22mg/L, and micronutrient element Fe 2.07～2.53mg/L, the Zn 0.110～0.134mg/L, Co 0.067～0.082mg/L, B 0.002～0.004mg/L, Mn0.309～0.378mg/L, Cu 0.072～0.088mg/L, Ni 0.059～0.072mg/L and the Mo0.108～0.133mg/L that keep microorganism growth; The starting point concentration of ammonia nitrogen and nitrite nitrogen is 28～84mgL in the described waste water
-1, the mol ratio of ammonia nitrogen and nitrite nitrogen is 1: 0.9～1, described ammonia nitrogen and nitrite nitrogen provide with the form of ammonium salt and nitrite respectively.
Simulated wastewater of the present invention is adjusted ammonium salt and nitrite concentration in the simulated wastewater according to anaerobic ammonia oxidation reactor permission situation.
Micro-nutrients of the present invention adds with the form of EDTA chelating, with simulated wastewater volumeter, i.e. EDTA25.0mgL
-1, FeSO
47H
2O 11.43mgL
-1, H
3BO
40.018mgL
-1, MnCl
24H
2O 1.24mgL
-1, CuSO
45H
2O 0.31mgL
-1, ZnSO
47H
2O 0.54mgL
-1, NiCl
26H
2O 0.26mgL
-1, NaMoO
42H
2O 0.28mgL
-1, CoCl
26H
2O0.30mgL
-1
Described anaerobic reactor is upflow type anaerobic active sludge bed bioreactor (UASB), but is suitable for the anaerobic reactor of other kind equally.
Anaerobic grain sludge of the present invention can be any anaerobic grain sludge that contains anaerobic ammonia oxidizing bacteria, as the anaerobic digestion granule sludge.
Compared with prior art, beneficial effect of the present invention is mainly reflected in: the inoculation anaerobic grain sludge is conducive to the formation of holding back and accelerate brick-red anaerobic ammonium oxidation granular sludge of anaerobic ammonia oxidizing bacteria as bacterium source and the anaerobic ammonoxidation bacterium concentrating carrier of anaerobic ammonia oxidizing bacteria; Improve reactor total nitrogen load than the underload incremental manner and be conducive to the domestication enrichment of anaerobic ammonia oxidizing bacteria and the steady increase of nitrogen removal speed, and can effectively avoid the matrix of Anammox to suppress; High nitrogen is removed under the speed, and namely total nitrogen is removed speed above 2.0kg/ (m
3.d) operation under deoxygenation and the room temperature condition of needn't intaking the time is conducive to reduce the running cost of technology.
(4) description of drawings
Fig. 1 upflow type anaerobic active sludge bed bioreactor: 1-inlet chest; The 2-peristaltic pump of intaking; The 3-UASB reactor; The 4-water tank; The 5-fluid-tight; The 6-air outlet
(5) embodiment
The present invention is described further below in conjunction with specific embodiment, but protection scope of the present invention is not limited in this:
Reactor of the present invention is upflow type anaerobic active sludge bed bioreactor (UASB), and structure as shown in Figure 1.
Embodiment 1:
(1) inoculation anaerobic digestion granule sludge in upflow type anaerobic active sludge bed bioreactor, mud particle diameter 2～3mm, sphericity is about 0.9, and mean specific gravity is about 1.6 (much larger than 1), sludge settling forms Sludge Bed in reactor bottom, the mud bed volume account for overall reactor long-pending 60%.
(2) in the simulated wastewater ammonia nitrogen and nitrite nitrogen respectively with (NH
4)
2SO
4And NaNO
2Provide, mol ratio is 1: 1, and initial ammonia nitrogen and nitrite nitrogen concentration are 70mgL
-1, the component that described simulated wastewater is made up of following quality constitutes: (NH
4)
2SO
4(70～350mgL
-1), NaNO
2(70～350mgL
-1), KH
2PO
410mgL
-1, CaCl
22H
2O 5.6mgL
-1, MgSO
47H
2O 300mgL
-1, KHCO
31250mgL
-1, trace element is to add behind the EDTA chelating, and described trace element consists of EDTA 25.0mgL
-1, FeSO
47H
2O 11.43mgL
-1, H
3BO
40.018mgL
-1, MnCl
24H
2O 1.24mgL
-1, CuSO
45H
2O 0.31mgL
-1, ZnSO
47H
2O0.54mgL
-1, NiCl
26H
2O 0.26mgL
-1, NaMoO
42H
2O 0.28mgL
-1, CoCl
26H
2O 0.30mgL
-1
(3) beginning of reactor start-up, it is 12h that the reactor waterpower residence time is set, advance tap water to mud flushing after one day with nitrogen to reactor and the aeration deoxygenation of intaking, after the reactor start-up only to water inlet (nitrogen) gas that exposes to the sun, each aeration time 20min.Remove under the rate conditions at high nitrogen, namely total nitrogen is removed speed above 2.0kg/ (m
3.d) time, the nitrogen deoxygenation of no longer exposing to the sun of intaking.About 32 ℃ of control temperature of reactor, regulate with hydrochloric acid or sodium hydroxide that wastewater pH is 8.00 ± 0.25 in the inlet chest 1, simulated wastewater is intake continuously by peristaltic pump 2, waste water enters from UASB reactor 3 water-ins, enter water tank 4 through the operation back from the reactor water outlet, the nitrogen that produces enters liquid seal device 5, and 6 eliminatings from the air outlet.
Initial ammonia nitrogen and nitrite nitrogen concentration are 70mgL
-1, hydraulic detention time is 12h.Ammonia nitrogen and the nitrite nitrogen concentration of the every day water inlet of monitoring reaction device and water outlet, adjust the reactor operational conditions according to ammonia nitrogen and/or nitrite nitrogen concentration, when reactor satisfies condition (A): water outlet nitrite nitrogen concentration less than 30mg/L or (B): improve reactor total nitrogen load when the stable and water outlet nitrite nitrogen concentration of reactor water outlet data (ammonia nitrogen and nitrite nitrogen concentration) was less than 60mg/L in continuous three days.Reactor operation 1～93d influent ammonia nitrogen or nitrite nitrogen make into the amplification of 28mg/L synchronously, and water total nitrogen load is increased to 1.02kg/ (m3.d) by 0.42kg/ (m3.d), and anaerobic reactor forms the anaerobic ammonium oxidation granular sludge of enrichment anaerobic ammonia oxidizing bacteria through the operation of 60d.All increase to 182mg/L synchronously at 110d influent ammonia nitrogen and nitrite nitrogen concentration, adjust hydraulic detention time afterwards and progressively shorten to the 4h of 161d from initial 12h with the stride of 2h, total nitrogen is removed speed and is reached 2.09kg/ (m3.d).When influent ammonia nitrogen and nitrite nitrogen concentration all increase to after 210mg/L and hydraulic detention time foreshorten to 1.5h synchronously, no longer improve the water inlet substrate concn, only improve reactor total nitrogen load to reduce hydraulic detention time, the amount that the reduction of hydraulic detention time causes water flow to increase is equivalent to the flooding quantity that the water inlet of reactor day increases by 2 reactor effective volumes.Reactor moves to the 334th day, and total nitrogen is removed speed and reached 20.3kg/ (m
3.d), move to the 524th day total nitrogen and remove speed more up to 47.5kg/ (m
3.d).
Embodiment 2:
Reactor, seed sludge, deoxygenation and temperature condition and water inlet are all with embodiment 1.When reactor satisfies condition (A): the water outlet nitrite nitrogen less than 30mg/L or (B): improve the reactor operating load when the stable and water outlet nitrite nitrogen concentration of water outlet data (ammonia nitrogen or nitrite nitrogen concentration) was less than 60mg/L in continuous three days.Initial ammonia nitrogen and nitrite nitrogen concentration are 70mgL
-1, hydraulic detention time is 12h.Anaerobic reactor forms the anaerobic ammonium oxidation granular sludge of enrichment anaerobic ammonia oxidizing bacteria through the operation of 90d.Reactor operation 1～180d, hydraulic detention time progressively shortens to the 180th day 4h from initial 12h with the stride of 2h, and water inlet total nitrogen load is by 0.42kg/ (m
3.d) be increased to 0.89kg/ (m
3.d).Progressively increase water inlet substrate concn (ammonia nitrogen or nitrite nitrogen increase progressively with the amplification of 28mg/L synchronously) afterwards, 339～363d, the reactor waterpower residence time is 2h, the water inlet substrate concn is 350mg/L, the reactor operating performance reduces, nitrogen removal rate has dropped to 31% of 363d by 75% of 339d, and influent ammonia nitrogen and nitrite concentration reduce 70mg/L immediately synchronously, makes the total nitrogen load by 9.0kg/ (m
3.d) be reduced to 5.0kg/ (m
3.d), and adopt and progressively reduce hydraulic detention time raising reactor load, the amount that the water flow that the reduction of hydraulic detention time causes increases is equivalent to the flooding quantity of 4 reactor effective volumes of reactor day flooding quantity increase.At 479d, reactor total nitrogen load and total nitrogen are removed speed and have been reached 34.6 and 26.3kg/ (m respectively
3.d).
Claims (6)
1. the operation method of an efficient anaerobic ammoxidation reactor is characterized in that described method is:
(1) anaerobic grain sludge is inoculated in the anaerobic reactor, anaerobic grain sludge account for overall reactor long-pending 30～90%;
(2) serve as the reaction water inlet with nitrogenous simulated wastewater, regulate simulated wastewater pH value to 7.20～8.70 before the water inlet, and the feeding rare gas element is removed the dissolved oxygen of anaerobic reactor and simulated wastewater, then simulated wastewater is continuously pumped into reactor, behind reactor start-up, only reaction water inlet aeration is removed dissolved oxygen, temperature of reactor control is at 18～37 ℃, the reactor start-up stage, hydraulic detention time is 12～48h, ammonia nitrogen and the nitrite nitrogen concentration of the every day water inlet of monitoring reaction device and water outlet, adjust the reactor operational conditions according to ammonia nitrogen and/or nitrite nitrogen concentration, when reactor satisfies following condition (A) or one of (B) time, adjusts water inlet substrate concn and/or hydraulic detention time to increase reactor total nitrogen load; So repeat to adjust, anaerobic reactor forms the anaerobic ammonium oxidation granular sludge of enrichment anaerobic ammonia oxidizing bacteria through the operation of 30～150d, and described substrate concn refers to ammonia nitrogen and the nitrite nitrogen mass concentration separately in the water into; Ammonia nitrogen and the nitrite nitrogen concentration range of adjusting nitrogenous simulated wastewater when described water inlet is initial are 28～84mgL
-1Described condition (A) for water outlet nitrite nitrogen concentration less than 30mg/L, described condition (B) is that difference on the continuous three days water outlet ammonia nitrogen of reactor and the nitrite nitrogen concentration not statistically significant and water outlet nitrite nitrogen concentration are less than 60mg/L; Described anaerobic reactor operational conditions inflation method is one of following: a) raising of water inlet substrate concn and the adjustment of hydraulic detention time are carried out respectively: the each 3.5～42mgL that improves synchronously of influent ammonia nitrogen and nitrite nitrogen
-1, but the influent concentration of nitrite nitrogen is no more than 280mg/L; When adjusting hydraulic detention time, when if the hydraulic detention time when adjusting is 2～48h, each hydraulic detention time shortens 1～4h, if during less than 2h, shortening the water flow increasing amount that hydraulic detention time causes at every turn, the hydraulic detention time when adjusting to be equivalent to the flooding quantity that the water inlet of reactor day increases by 0.5～7 reactor effective volume; B) raising of water inlet substrate concn and the adjustment of hydraulic detention time hocket: namely improve described influent ammonia nitrogen and nitrite nitrogen concentration synchronously and hocket with the mode of adjusting hydraulic detention time, the raising of the substrate concn of described water inlet and the adjustment of hydraulic detention time are with method a); C) total nitrogen of adjusting water inlet substrate concn and hydraulic detention time simultaneously and increasing load must not and be surpassed the maximum total nitrogen that increases when adjusting water inlet substrate concn and hydraulic detention time respectively and load, and the raising of described water inlet substrate concn and the adjustment of hydraulic detention time are with method a); In above inflation method any one method a)～c), if phenomenon appears suppressing in reactor, be that the mass concentration of water outlet nitrite nitrogen is when surpassing 100mg/L, reduce the water inlet substrate concn immediately or improve hydraulic detention time making reactor total nitrogen load reduce by 10～60%, adjust according to above-mentioned anaerobic reactor operational conditions inflation method again.
2. the operation method of anaerobic ammonia oxidation reactor as claimed in claim 1 is characterized in that described anaerobic grain sludge particle diameter 0.5～9mm, and described particle sphericity is 0.5～1.0, and proportion is greater than 1.
3. the operation method of anaerobic ammonia oxidation reactor as claimed in claim 1 is characterized in that described step (1) washes mud with tap water before starting reactor, at hydraulic detention time is to wash 0.5～1d under the condition of 12～48h; The unloading phase hydraulic detention time be 12～48h.
4. the operation method of anaerobic ammonia oxidation reactor as claimed in claim 1, the method that it is characterized in that the dissolved oxygen in the described removal anaerobic reactor of step (2) and the water inlet is: anaerobic reactor exposes to the sun nitrogen earlier to described anaerobic reactor and the deoxygenation of simulated wastewater aeration before starting, start after the reactor, only to the reactor water inlet nitrogen deoxygenation of exposing to the sun, each aeration time is 20min, removes speed when the total nitrogen of water inlet and surpasses 2.0kg/ (m
3D) time, stop the water inlet nitrogen deoxygenation of exposing to the sun.
5. the operation method of anaerobic ammonia oxidation reactor as claimed in claim 1 is characterized in that the component that described simulated wastewater is made up of following quality constitutes: ammonium salt 28～490mgL
-1, nitrite 28～490mgL
-1, SODIUM PHOSPHATE, MONOBASIC 9.0～11mg/L, bitter salt 57.74～64.46mg/L, saleratus 900～1100mg/L, calcium chloride 5.09～6.22mg/L, and micronutrient element Fe2.07～2.53mg/L, the Zn0.110～0.134mg/L, Co0.067～0.082mg/L, B0.002～0.004mg/L, Mn0.309～0.378mg/L, Cu0.072～0.088mg/L, Ni0.059～0.072mg/L and the Mo0.108～0.133mg/L that keep microorganism growth; The starting point concentration of ammonia nitrogen and nitrite nitrogen is 28～84mgL in the described waste water
-1, the mol ratio of ammonia nitrogen and nitrite nitrogen is 1:0.9～1.4.
6. the operation method of anaerobic ammonia oxidation reactor as claimed in claim 1 is characterized in that described anaerobic reactor is upflow type anaerobic active sludge bed bioreactor.
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| CN102730922A (en) * | 2012-06-28 | 2012-10-17 | 杭州师范大学 | Preservation device of anaerobic ammonium oxidation granular sludge |
| CN102951733A (en) * | 2012-11-20 | 2013-03-06 | 杭州师范大学 | Uniformly distributed feeding upflow type anaerobic ammonia oxidation reactor |
| CN103663687B (en) * | 2013-12-02 | 2015-03-04 | 北京工业大学 | Cultivation method of anaerobic ammonium oxidation bacteria capable of degrading nitrate nitrogen |
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