CN112142202A - Method for denitrifying sewage by integrated semi-nitrification-anaerobic ammonia oxidation reactor - Google Patents
Method for denitrifying sewage by integrated semi-nitrification-anaerobic ammonia oxidation reactor Download PDFInfo
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 53
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 32
- 230000003647 oxidation Effects 0.000 title claims abstract description 31
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 30
- 239000010865 sewage Substances 0.000 title claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 91
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 87
- 238000005273 aeration Methods 0.000 claims abstract description 35
- 230000001965 increasing effect Effects 0.000 claims abstract description 27
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000004021 humic acid Substances 0.000 claims abstract description 16
- 238000004062 sedimentation Methods 0.000 claims abstract description 11
- 239000003513 alkali Substances 0.000 claims abstract description 10
- 238000010438 heat treatment Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims abstract description 6
- 230000002572 peristaltic effect Effects 0.000 claims abstract description 6
- 230000008569 process Effects 0.000 claims description 29
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 235000013619 trace mineral Nutrition 0.000 claims description 16
- 239000011573 trace mineral Substances 0.000 claims description 16
- 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
- 239000010802 sludge Substances 0.000 claims description 13
- 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 claims description 12
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 11
- 229910052760 oxygen Inorganic materials 0.000 claims description 11
- 239000001301 oxygen Substances 0.000 claims description 11
- 230000014759 maintenance of location Effects 0.000 claims description 10
- 239000002351 wastewater Substances 0.000 claims description 10
- 239000011159 matrix material Substances 0.000 claims description 9
- 239000002366 mineral element Substances 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 241000894006 Bacteria Species 0.000 claims description 8
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 8
- 239000001110 calcium chloride Substances 0.000 claims description 8
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 8
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 7
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 7
- 230000003203 everyday effect Effects 0.000 claims description 6
- 238000012544 monitoring process Methods 0.000 claims description 6
- 235000015097 nutrients Nutrition 0.000 claims description 6
- 230000001276 controlling effect Effects 0.000 claims description 5
- 230000000813 microbial effect Effects 0.000 claims description 5
- UIIMBOGNXHQVGW-UHFFFAOYSA-M sodium bicarbonate Substances [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 5
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims 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 claims description 4
- 229910021380 Manganese Chloride Inorganic materials 0.000 claims description 4
- GLFNIEUTAYBVOC-UHFFFAOYSA-L Manganese chloride Chemical compound Cl[Mn]Cl GLFNIEUTAYBVOC-UHFFFAOYSA-L 0.000 claims description 4
- 229910004619 Na2MoO4 Inorganic materials 0.000 claims description 4
- 229910021586 Nickel(II) chloride Inorganic materials 0.000 claims description 4
- 230000001580 bacterial effect Effects 0.000 claims description 4
- 229910052927 chalcanthite Inorganic materials 0.000 claims description 4
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 claims description 4
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 4
- 239000011565 manganese chloride Substances 0.000 claims description 4
- QMMRZOWCJAIUJA-UHFFFAOYSA-L nickel dichloride Chemical compound Cl[Ni]Cl QMMRZOWCJAIUJA-UHFFFAOYSA-L 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 4
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 4
- 239000011780 sodium chloride Substances 0.000 claims description 4
- 239000011684 sodium molybdate Substances 0.000 claims description 4
- TVXXNOYZHKPKGW-UHFFFAOYSA-N sodium molybdate (anhydrous) Chemical compound [Na+].[Na+].[O-][Mo]([O-])(=O)=O TVXXNOYZHKPKGW-UHFFFAOYSA-N 0.000 claims description 4
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 claims description 4
- 229910000368 zinc sulfate Inorganic materials 0.000 claims description 4
- 239000011686 zinc sulphate Substances 0.000 claims description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims 2
- 238000004088 simulation Methods 0.000 claims 1
- 238000002474 experimental method Methods 0.000 description 11
- 229910002651 NO3 Inorganic materials 0.000 description 8
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 8
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000005728 strengthening Methods 0.000 description 3
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 2
- 241001453382 Nitrosomonadales Species 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000005189 flocculation Methods 0.000 description 2
- 230000016615 flocculation Effects 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 230000027756 respiratory electron transport chain Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 239000007836 KH2PO4 Substances 0.000 description 1
- 241001052560 Thallis Species 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000019522 cellular metabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 1
- 208000005135 methemoglobinemia Diseases 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910000402 monopotassium phosphate Inorganic materials 0.000 description 1
- 239000008239 natural water Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 230000037361 pathway Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000003403 water pollutant Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
An integrated semi-nitrification-anaerobic ammonia oxidation reactor denitrification sewage treatment method relates to a sewage treatment method, and the integrated semi-nitrification-anaerobic ammonia oxidation reactor used in the method is mainly characterized by comprising a water inlet tank, a reactor main body, a sedimentation tank and a control system: the water inlet pool is connected with a water inlet at the bottom of the reactor main body through a peristaltic pump; a filling frame is arranged in the reactor main body, an aeration head is arranged at the bottom in the reactor, the aeration rate of the aeration head is controlled by an aeration pump, and a pH online determinator and a heating rod are arranged at the middle upper part; the reactor main body is connected with an alkali barrel, and alkali is supplied into the reactor through a liquid replenishing pump; the reactor main body is connected with the sedimentation tank through a water outlet. When the system is used for sewage treatment, the device needs to be started firstly, then the ammonia nitrogen water inflow load is increased, and humic acid is added in an experimental stage. The invention improves the denitrification capability by adding humic acid, and the ammonia nitrogen removal rate reaches 95 percent.
Description
Technical Field
The invention relates to a sewage treatment method, in particular to a sewage treatment method by denitrification of an integrated semi-nitrification-anaerobic ammonia oxidation reactor.
Background
With the rapid development of chemical fertilizer, food, petroleum, chemical industry and other industries in China, the discharge amount of ammonia nitrogen wastewater is rapidly increased. The high-concentration ammonia nitrogen wastewater is discharged into an environmental water body, so that the massive propagation of algae or other microorganisms in the water is easily caused, the eutrophication of a natural water body is caused, and the species distribution in an aqueous ecosystem is unbalanced. Nitrate and nitrite generated by ammonia nitrogen in water body are easy to induce methemoglobinemia and generate 'three-cause' effect, which is harmful to human health. The current relevant environmental protection standards in China relate to discharge indexes of ammonia nitrogen wastewater, and include surface water environment quality standard (GB 3838-2002), underground water environment quality standard (GB/T14848-93), comprehensive sewage discharge standard (GB 8978-199) and water pollutant discharge standards of relevant industries, and the limit value range of the ammonia nitrogen standard is regulated to be 0.02 mg/L-150 mg/L. Due to strict ammonia nitrogen discharge standards, the traditional denitrification technology is difficult to meet high treatment requirements. Therefore, the development of efficient and economical denitrification methods has become a hot research point in the field of wastewater treatment in recent years.
Currently, Anammox (Anammox) is recognized as one of the most energy efficient denitrification pathways among biological denitrification processes. Compared with the traditional nitrification-denitrification process, the process does not need aeration and an external carbon source. However, the anammox process requires the addition of nitrite to effect ammonia nitrogen removal. Therefore, an integrated semi-nitrification-anaerobic ammonia oxidation (SNAP) process was developed based on anaerobic ammonia oxidation, and the process is that semi-nitrification and anaerobic ammonia oxidation are carried out simultaneously in one reactor: carrying out short-cut nitrification reaction on Ammonia Oxidizing Bacteria (AOB) on the outer layer of the biomembrane under the condition of oxygen limitation to oxidize about half of ammonia nitrogen into nitrite; anaerobic ammonia oxidation bacteria in the inner layer of the biomembrane perform anaerobic ammonia oxidation reaction under anaerobic condition, nitrite is used as an electron acceptor, and ammonia nitrogen is oxidized to generate nitrogen and a small amount of nitrate. Compared with the anaerobic ammonia oxidation process, the SNAP process can save 100% of nitrite. Compared with a sectional process, the process has the advantages of small occupied space, low sludge yield, energy conservation and cost consumption saving. The technology is one of the nitrogen removal technologies with great potential in the future.
However, the reported integrated semi-nitrification-anaerobic ammonia oxidation process has the problem that the system is unstable due to poor flocculation property of sludge. The microbial cell EPS surface has large electronegativity and large repulsive force between cells, so that the flocculation performance of sludge is poor, the sludge is not favorable for gathering the sludge to form a biological membrane, and the stable operation of the reactor is finally influenced.
Disclosure of Invention
The invention aims to provide a sewage denitrification treatment method of an integrated semi-nitrification-anaerobic ammonia oxidation reactor. The effective critical potential of the cells is reduced by the extracellular electron transfer, so that the cell thalli are easier to agglomerate on a biological membrane, and the cell aggregate is prevented from losing along with the effluent, thereby keeping the stability and the high efficiency of the reactor. In addition, the extracellular electron transfer can accelerate the metabolism of cell thallus and provide energy for the growth of the cell thallus so as to obtain higher denitrification efficiency. .
The purpose of the invention is realized by the following technical scheme:
an integrated semi-nitrification-anaerobic ammonia oxidation reactor denitrification sewage treatment method adopts an integrated semi-nitrification-anaerobic ammonia oxidation system, and the system comprises a water inlet tank, a reactor main body, a sedimentation tank and a control system: the water inlet pool is connected with a water inlet at the bottom of the reactor main body through a peristaltic pump; a filling frame is arranged in the reactor main body, an aeration head is arranged at the bottom in the reactor, the aeration rate of the aeration head is controlled by an aeration pump, and a pH online determinator and a heating rod are arranged at the middle upper part; the reactor main body is connected with an alkali barrel, and alkali is supplied into the reactor through a liquid replenishing pump; the reactor main body is connected with the sedimentation tank through a water outlet;
the integrated semi-nitrification-anaerobic ammonia oxidation reactor denitrogenation sewage treatment method comprises the following treatment processes:
first, reactor start-up procedure
Firstly, starting a reactor, inoculating strains in an SNAP reactor, and introducing artificially configured simulated wastewater; from ammonium sulfate (NH4)2SO4Providing a nitrogen source for microbial growth from NaHCO3As a pH regulator, the pH of the reactor is kept between 7.5 and 7.8, and the temperature of the reactor is controlled between 33 and 35 ℃; adding nutrient solution matrix, trace elements I and mineralsMaterial element, trace element II; in the water distribution process, 0.5 ml of matrix, 0.5 ml of trace element I, 0.1 ml of trace element II and 1 ml of mineral elements are respectively added into 1 liter of water; in the starting process of the reactor, intermittent aeration is adopted, aeration is carried out for 5min, and stopping for 5 min; keeping the dissolved oxygen of the reactor at 2-3 mg/L, the hydraulic retention time at 18h, and the ammonia nitrogen inflow concentration at 300 mg/L; gradually increasing the aeration time until continuous aeration is started when the dissolved oxygen of the reactor is reduced and the nitrite nitrogen is reduced;
secondly, regulating and controlling the operation
The second stage of the reactor is a load lifting stage, after the initial starting stage of the reactor, the ammonia nitrogen inflow concentration and load are gradually improved in the stage, and the ammonia nitrogen removal capability of the domesticated bacteria is improved; the duration of this phase was 48 days; controlling dissolved oxygen at 1-2 mg/L, adopting a continuous water inlet mode, keeping the hydraulic retention time for 10h at the final stage of starting, adopting ammonium sulfate to simulate ammonia nitrogen 400-700 mg/L, monitoring the ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentrations of inlet water and outlet water of the reactor every day, and improving the load of the reactor by increasing the inlet water concentration when the outlet water data (ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentrations) of the reactor are stable and the ammonia nitrogen removal rate reaches more than 85% for three consecutive days;
third, experiment stage
The experimental period is divided into five stages according to the water inlet concentration of COD (completely provided by humic acid) for 92 days; in the whole process of adding humic acid into the reactor, the ammonia nitrogen inlet water concentration is maintained at 672.24-929.82 mg/L, and the COD inlet water concentration is gradually increased from 88.59 mg/L to 1702.63 mg/L; monitoring the ammonia nitrogen, nitrite nitrogen, nitrate nitrogen concentration and COD concentration of inlet water and outlet water of the reactor every day, and observing the removal capability of the reactor on the ammonia nitrogen through the COD concentration when the outlet water data (ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentration) of the reactor is stable and the ammonia nitrogen removal rate reaches more than 85% for three consecutive days.
The method for denitrifying sewage by using the integrated semi-nitrification-anaerobic ammonia oxidation reactor is characterized in that the added nutrient solution substrate KH2PO4136 g/L, and the trace element I is FeSO418 g/L EDTA 10 g/L, 1.4 g/L, NaCl 1 g mineral element KCl 1 g/L、MgSO4 1 g/L、CaCl21.4 g/L, and the microelement II is MnCl2·4H2O 9.9 mg/L、NiCl2·6H2O 1.9 mg/L、Na2MoO4·2H2O 2.2 mg/L、ZnSO4·7H2O 4.3 mg/L、CaCl2·6H2O 12 mg/L、CuSO4·5H2O 12.5 mg/L、H3BO4 0.14 mg/L。
According to the method for denitrifying sewage by using the integrated semi-nitrification-anaerobic ammonia oxidation reactor, the inoculated strains in the starting process of the reactor are bacterial sludge enriched in the SNAP reactor, MLSS is 10.1 g/L, MLSS is 12.5 g/L, and the sludge is reddish brown in color.
The integrated semi-nitrification-anaerobic ammonia oxidation reactor is started to simulate the condition that the wastewater is treated by ammonium sulfate (NH4)2SO4And a nitrogen source for microbial growth is provided, and the concentration of inlet water is gradually increased along with the growth condition of bacteria in the reactor, so that the load of inlet water nitrogen is increased.
The integrated semi-nitrification-anaerobic ammonia oxidation reactor denitrification sewage treatment method is characterized in that the ammonia nitrogen concentration of inlet water is started from 300 mg/L when the reactor is started, and the starting load is 0.3 kgN/m3/d。
The invention has the advantages and effects that:
1. according to the method for strengthening integrated semi-nitrification-anaerobic ammonia oxidation denitrification, disclosed by the invention, when the concentration of the ammonia nitrogen in the inlet water is up to 700-800 mg/L, humic acid is added into the reactor, so that the removal rate of the ammonia nitrogen is improved to 95% at most.
2. According to the method for strengthening integrated semi-nitrification-anaerobic ammonia oxidation denitrification, humic acid is added into the reactor, and for a designed and well-operated integrated semi-nitrification-anaerobic ammonia oxidation system, under the condition that the ammonia nitrogen index does not reach the standard, the effect of removing ammonia nitrogen can be achieved by only adding humic acid without newly building a system, and the method is simple, convenient and feasible for the reconstruction of the current urban sewage plant and industrial nitrogen-containing wastewater treatment plant. At present, no report is found about a method for enhancing integrated semi-nitrification anaerobic ammonia oxidation by humic acid.
Drawings
FIG. 1 is a schematic view of the process of the present invention;
FIG. 2 is a graph showing the change in COD of the SNAP-C reactor during the experiment.
In the figure: 1. a water inlet pool; 2. a peristaltic pump; 3. an aeration head; 4. an aeration pump; 5. a heating rod; 6, a pH electrode; a pH controller; 8. a liquid supplementing pump; 9. saturated sodium bicarbonate solution; 10. a sedimentation tank.
Detailed Description
The present invention will be described in detail with reference to the embodiments shown in the drawings.
The invention relates to an integrated semi-nitrification-anaerobic ammonia oxidation denitrification reactor, which comprises a water inlet tank, a reactor main body, a sedimentation tank and a control system: the water inlet pool is connected with a water inlet at the bottom of the reactor main body through a peristaltic pump; a filling frame is arranged in the reactor main body, an aeration head is arranged at the bottom in the reactor, the aeration rate of the aeration head is controlled by an aeration pump, and a pH online determinator and a heating rod are arranged at the middle upper part; the reactor main body is connected with an alkali barrel, and alkali is supplied into the reactor through a liquid replenishing pump; the reactor main body is connected with the sedimentation tank through a water outlet.
The invention relates to a process for strengthening integrated semi-nitrification-anaerobic ammonia oxidation, which comprises the following steps:
1. start-up reactor and start-up process
Firstly, starting the SNAP reactor, wherein the inoculated strains of the SNAP reactor adopt bacterial sludge which is cultured in the laboratory and enriched by the SNAP reactor and runs for more than one year, MLSS is 10.1 g/L, MLSS is 12.5 g/L, and the color of the sludge is reddish brown. Introducing artificially prepared simulated waste water (NH)4)2SO4And providing a nitrogen source for the growth of microorganisms, wherein the water inlet concentration of the nitrogen source is gradually increased along with the growth condition of bacteria in the reactor, so that the load of the ammonia nitrogen in the inlet water is increased. From NaHCO3As a pH regulator, the pH of the reactor is kept at about 7.5-7.8, and the temperature of the reactor is controlled at 33-35 ℃ by a heating rod. Nutrient solution matrix KH added in the experiment2PO4136 g/L, and the trace element I is FeSO418 g/L EDTA 10 g/L, 1.4 g/L, NaCl 1 g/L, MgSO of mineral element KCl4 1 g/L、CaCl21.4 g/L, and the microelement II is MnCl2·4H2O 9.9 mg/L、NiCl2·6H2O 1.9 mg/L、Na2MoO4·2H2O 2.2 mg/L、ZnSO4·7H2O 4.3 mg/L、CaCl2·6H2O 12 mg/L、CuSO4·5H2O 12.5 mg/L、H3BO40.14 mg/L. In the process of water distribution, 0.5 ml of matrix, 0.5 ml of trace element I, 0.1 ml of trace element II and 1 ml of mineral elements are respectively added into 1 liter of water. In the starting process of the reactor, intermittent aeration is adopted, aeration is carried out for 5min, and stopping is carried out for 5 min. The dissolved oxygen of the reactor is kept at 2-3 mg/L, the hydraulic retention time is 18h, and the ammonia nitrogen inlet concentration is 300 mg/L. And when the dissolved oxygen of the reactor is reduced and the nitrite nitrogen is reduced, gradually increasing the aeration time until continuous aeration. The ammonia nitrogen concentration of the inlet water when the reactor is started from 300 mg/L, and the starting load is 0.3 kgN/m3/d，
2. Regulating operation
And the second stage of the reactor is a load increasing stage, and after the initial starting stage of the reactor, the ammonia nitrogen inflow concentration and load are gradually increased in the stage, so that the ammonia nitrogen removal capability of the bacteria is domesticated. The duration of this phase was 48 days. Controlling dissolved oxygen at 1-2 mg/L, adopting a continuous water inlet mode, keeping hydraulic retention time for 10h at the final stage of starting, adopting ammonium sulfate to simulate ammonia nitrogen 400-700 mg/L, monitoring the ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentration of inlet water and outlet water of the reactor every day, and improving the load of the reactor by increasing the inlet water concentration when the outlet water data (ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentration) of the reactor is stable and the ammonia nitrogen removal rate reaches more than 85% for three consecutive days.
3. Experimental stage
The experimental period, which took 92 days, was divided into five stages according to the COD (completely supplied by humic acid) influent concentration. In the whole process of adding humic acid into the reactor, the ammonia nitrogen inlet water concentration ranges from 672.24 mg/L to 929.82 mg/L, the average value of the ammonia nitrogen outlet water concentration is 63.31mg/L, the average value of the ammonia nitrogen removal rate is 92%, and the COD inlet water concentration is gradually increased from 88.59 mg/L to 1702.63 mg/L. Monitoring the ammonia nitrogen, nitrite nitrogen, nitrate nitrogen concentration and COD concentration of inlet water and outlet water of the reactor every day, and observing the removal capability of the reactor on the ammonia nitrogen through the COD concentration when the outlet water data (ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentration) of the reactor is stable and the ammonia nitrogen removal rate reaches more than 85% for three consecutive days.
Example 1
The integrated semi-nitrification-anaerobic ammonia oxidation system adopted by the invention is shown in the attached figure 1 and comprises a water inlet tank, a reactor main body, a sedimentation tank and a control system: the water inlet pool is connected with a water inlet at the bottom of the reactor main body through a peristaltic pump; a filling frame is arranged in the reactor main body, an aeration head is arranged at the bottom in the reactor, the aeration rate of the aeration head is controlled by an aeration pump, and a pH online determinator and a heating rod are arranged at the middle upper part; the reactor main body is connected with an alkali barrel, and alkali is supplied into the reactor through a liquid replenishing pump; the reactor main body is connected with the sedimentation tank through a water outlet.
1. Starting step
Firstly, a reactor is started, inoculated strains of the SNAP reactor adopt bacterial sludge which is cultured in a laboratory and enriched by the SNAP reactor and runs for more than one year, MLSS is 10.1 g/L, MLSS is 12.5 g/L, and the color of the sludge is reddish brown. From NaHCO3As a pH regulator, the pH of the reactor is kept at about 7.5-7.8, and the temperature of the reactor is controlled at 33-35 ℃. Nutrient solution matrix KH added in the experiment2PO4136 g/L, and the trace element I is FeSO418 g/L EDTA 10 g/L, 1.4 g/L, NaCl 1 g/L, MgSO of mineral element KCl4 1 g/L、CaCl21.4 g/L, and the microelement II is MnCl2·4H2O 9.9 mg/L、NiCl2·6H2O 1.9 mg/L、Na2MoO4·2H2O 2.2 mg/L、ZnSO4·7H2O 4.3 mg/L、CaCl2·6H2O 12 mg/L、CuSO4·5H2O 12.5 mg/L、H3BO40.14 mg/L. In the water distribution process, 0.5 ml of matrix, 0.5 ml of trace element I, 0.1 ml of trace element II and 1 ml of mineral elements are respectively added into 1 liter of water. On days 1-40, the ammonia nitrogen concentration of the inlet water is stabilized at 400 +/-68 mg/L, the ammonia nitrogen concentration of the outlet water is 30.95-261.56 mg/L, the average value of the outlet water concentration is 170 mg/L, and the removal rate is flatThe average value is stabilized at about 57 percent, the average value of the ammonia nitrogen removal load is 0.41kgN/m3/d, and the retention time is as follows: 18h (1-5 d); 14h (6-24 d); 10h (25-40 d). On the 40 th day, the removal rate of ammonia nitrogen is improved to 64 percent, and the load is reduced from 0.3 kgN/m along with the reduction of the retention time from 18h to 14h3The/d is increased to 0.6 kgN/m3And d, after the stage is maintained for 40 days, the ammonia nitrogen concentration of the effluent of the reactor is 93.43 mg/L, the removal rate is higher than 60%, and the start is successful.
2. Stage of lifting load
The concentration of dissolved oxygen is controlled to be 1-2 mg/L, ammonia nitrogen in the simulated wastewater is adopted, humic acid simulates COD in the wastewater, the continuous water feeding mode is adopted, the pH value of the reactor is controlled to be 7.4-7.6, the temperature of the reactor is controlled to be 33-35 ℃, and the hydraulic retention time is 10 hours. In the I stage (42-55 d), the ammonia nitrogen concentration of the inlet water is maintained at about 430-559 mg/L, and the average value of the outlet water concentration is 100 mg/L. The ammonia nitrogen removal increased from 61% at day 46 to 84% at day 54. NO2 -The concentration of N is less than 10 mg/L from this stage, with NO3 -The concentration of the-N is increased from 16 mg/L to 30 mg/L, and the concentration of the ammonia nitrogen effluent is decreased from 177 mg/L to 88 mg/L. In the stage II (56-77 d), the ammonia nitrogen inlet concentration is gradually increased from 570mg/L to 654 mg/L, the ammonia nitrogen removal rate reaches 87% when the ammonia nitrogen removal rate is highest, and the ammonia nitrogen removal load is stabilized at 1.0 kgN/m3And/d is about. NO2 -The effluent concentration of the-N is 4.9-5.9 mg/L, and the concentration is relatively stable at this stage. And NO3 -The concentration of-N tended to rise slightly around 38 mg/L. In the stage III (78-89 d), the ammonia nitrogen inlet water concentration is further improved to about 746 mg/L, the ammonia nitrogen removal rate is obviously improved compared with the stage II, the average removal rate reaches 84%, and the ammonia nitrogen removal load also reaches 1.2 kgN/m3And d. NO at this stage2 -the-N still maintains 5.0 mg/L-7.45 mg/L. At the 86d, the ammonia nitrogen inlet water concentration is 745 mg/L, NO2 -N is 7.45 mg/L, NO3 -the-N increased to 42.9 mg/L. The SNAP bacteria can be proved to be completely adaptive to the ammonia nitrogen concentration with high concentration.
3. Experimental stage
The experimental period is 92 days after the experiment according to CODAll supplied by humic acid) feed water concentration divided the experimental stages into five stages. The I stage of the experiment is 90-108 days, and the water inlet concentration of COD is 88.59-275.67 mg/L. The average ammonia nitrogen removal value is 1.35 kgN/m3/d。NO2 -N concentration ranging from 9.13 to 13.75 mg/L, NO3 --N ranges from 44.91-86.41 mg/L. At the end of the experiment stage II for 109-125 days, the COD concentration of the inlet water is 291.99-442.46 mg/L, the ammonia nitrogen concentration is 800 mg/L, the ammonia nitrogen removal rate is 94%, and the average ammonia nitrogen removal load value reaches 1.49 kgN/m3The COD removal rate was 28%. NO2 -N concentration 10.04 mg/L and NO3 -The average value of-N was 69.37 mg/L. The third stage of the experiment is 126-140 days, when the COD concentration of the inlet water is increased from 449.00 to 691.06 mg/L, the average ammonia nitrogen removal rate and the average removal load can be respectively increased to 95 percent and 1.55kgN/m3At most, 99% and 1.61 kgN/m respectively3And the average removal rate of COD reaches 35 percent. NO2 -Average value of-N18.56 mg/L, NO3 -The average value of-N was 68.50 mg/L. The IV stage of the experiment is 141-164 days, along with the gradual increase of the COD concentration of the inlet water, the removal rate of ammonia nitrogen begins to be reduced to less than 90 percent, and the removal load is reduced to 1.45 kgN/m3And/d is about. The COD concentration of the inlet water in the V stage of the experiment at 165-181 days was greatly increased from 942.92 to 1702.67 mg/L. The average removal rate of ammonia nitrogen is maintained at 91%, the minimum removal rate can exceed 85%, and the ammonia nitrogen removal load is maintained at 1.4 kgN/m3And/d is about. However, the removal rate of COD gradually decreased to about 15%.
The test results show that:
the ammonia nitrogen inlet water concentration is 800 mg/L, the humic acid concentration is 500-600 mg/L, the pH value is controlled to be 7.5-7.8, the hydraulic retention time is 10h, the water temperature range is 33-35 ℃, the ammonia nitrogen removal rate is 95%, and the ammonia nitrogen removal load reaches 1.59 kgN/m3And d, the removal rate of humic acid reaches about 40 percent.
FIG. 2 is a graph showing the trend of ammonia nitrogen removal rate, COD influent concentration, effluent concentration and COD removal rate during the experiment.
The features in the above-described embodiments may be combined with each other without conflict. It should be understood that the above description of specific embodiments of the present invention is only for the purpose of illustrating the technical lines and features of the present invention, and is intended to enable those skilled in the art to understand the contents of the present invention and to implement the present invention, but the present invention is not limited to the specific embodiments described above. It is intended that all such changes and modifications as fall within the scope of the appended claims be embraced therein.
Claims (5)
1. The method for denitrifying and treating sewage by using the integrated semi-nitrification-anaerobic ammonia oxidation reactor is characterized by adopting an integrated semi-nitrification-anaerobic ammonia oxidation system, wherein the system comprises a water inlet tank, a reactor main body, a sedimentation tank and a control system: the water inlet pool is connected with a water inlet at the bottom of the reactor main body through a peristaltic pump; a filling frame is arranged in the reactor main body, an aeration head is arranged at the bottom in the reactor, the aeration rate of the aeration head is controlled by an aeration pump, and a pH online determinator and a heating rod are arranged at the middle upper part; the reactor main body is connected with an alkali barrel, and alkali is supplied into the reactor through a liquid replenishing pump; the reactor main body is connected with the sedimentation tank through a water outlet;
a method for denitrifying sewage by an integrated semi-nitrification-anaerobic ammonia oxidation reactor comprises the following treatment processes;
firstly, a reactor starting process:
firstly, starting a reactor, inoculating strains in an SNAP reactor, and introducing artificially configured simulated wastewater; from ammonium sulfate (NH4)2SO4Providing a nitrogen source for microbial growth from NaHCO3As a pH regulator, the pH of the reactor is kept between 7.5 and 7.8, and the temperature of the reactor is controlled between 33 and 35 ℃; adding nutrient solution matrix, trace elements I, mineral elements and trace elements II; in the water distribution process, 0.5 ml of matrix, 0.5 ml of trace element I, 0.1 ml of trace element II and 1 ml of mineral elements are respectively added into 1 liter of water; in the starting process of the reactor, intermittent aeration is adopted, aeration is carried out for 5min, and stopping for 5 min; keeping the dissolved oxygen of the reactor at 2-3 mg/L, the hydraulic retention time at 18h, and the ammonia nitrogen inflow concentration at 300 mg/L; gradually increasing the aeration time until continuous aeration is started when the dissolved oxygen of the reactor is reduced and the nitrite nitrogen is reduced;
secondly, regulating and controlling operation:
the second stage of the reactor is a load lifting stage, after the initial starting stage of the reactor, the ammonia nitrogen inflow concentration and load are gradually improved in the stage, and the ammonia nitrogen removal capability of the domesticated bacteria is improved; the duration of this phase was 48 days; controlling dissolved oxygen at 1-2 mg/L, adopting a continuous water inlet mode, keeping the hydraulic retention time for 10h at the final stage of starting, adopting ammonium sulfate to simulate ammonia nitrogen 400-700 mg/L, monitoring the ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentrations of inlet water and outlet water of the reactor every day, and improving the load of the reactor by increasing the inlet water concentration when the outlet water data (ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentrations) of the reactor are stable and the ammonia nitrogen removal rate reaches more than 85% for three consecutive days;
thirdly, an experimental stage:
the experimental period is divided into five stages according to the water inlet concentration of COD (completely provided by humic acid) for 92 days; in the whole process of adding humic acid into the reactor, the ammonia nitrogen inlet water concentration is maintained at 672.24-929.82 mg/L, and the COD inlet water concentration is gradually increased from 88.59 mg/L to 1702.63 mg/L; monitoring the ammonia nitrogen, nitrite nitrogen, nitrate nitrogen concentration and COD concentration of inlet water and outlet water of the reactor every day, and observing the removal capability of the reactor on the ammonia nitrogen through the COD concentration when the outlet water data (ammonia nitrogen, nitrite nitrogen and nitrate nitrogen concentration) of the reactor is stable and the ammonia nitrogen removal rate reaches more than 85% for three consecutive days.
2. The integrated denitrification-anammox reactor of claim 1, wherein said nutrient solution matrix KH is added2PO4136 g/L, and the trace element I is FeSO418 g/L EDTA 10 g/L, 1.4 g/L, NaCl 1 g/L, MgSO of mineral element KCl4 1 g/L、CaCl21.4 g/L, and the microelement II is MnCl2·4H2O 9.9 mg/L、NiCl2·6H2O 1.9 mg/L、Na2MoO4·2H2O 2.2 mg/L、ZnSO4·7H2O 4.3 mg/L、CaCl2·6H2O 12 mg/L、CuSO4·5H2O 12.5 mg/L、H3BO4 0.14 mg/L。
3. The method for denitrifying sewage in an integrated semi-nitrification-anaerobic ammonium oxidation reactor according to claim 1, wherein the inoculated strains in the starting process of the reactor are bacterial sludge enriched in the SNAP reactor, MLSS is 10.1 g/L, MLSS is 12.5 g/L, and the color of the sludge is reddish brown.
4. The integrated semi-nitrification-anaerobic ammonium oxidation reactor nitrogen removal sewage treatment method according to claim 1, wherein the reactor start-up simulation wastewater is ammonium sulfate (NH4)2SO4And a nitrogen source for microbial growth is provided, and the concentration of inlet water is gradually increased along with the growth condition of bacteria in the reactor, so that the load of inlet water nitrogen is increased.
5. The method for denitrifying sewage according to claim 1, wherein the ammonia nitrogen concentration of the inlet water at the start-up of the reactor is from 300 mg/L, and the start-up load is 0.3 kgN/m3/d。
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