CN116874083B - Low-carbon low-energy-consumption nitrogen and phosphorus removal method for urban sewage - Google Patents
Low-carbon low-energy-consumption nitrogen and phosphorus removal method for urban sewage Download PDFInfo
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- 239000010865 sewage Substances 0.000 title claims abstract description 70
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 40
- 239000011574 phosphorus Substances 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 35
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 31
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 238000005265 energy consumption Methods 0.000 title claims abstract description 22
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 13
- 239000010802 sludge Substances 0.000 claims abstract description 226
- 238000004062 sedimentation Methods 0.000 claims abstract description 37
- 238000010992 reflux Methods 0.000 claims abstract description 22
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 claims abstract description 8
- 239000013049 sediment Substances 0.000 claims abstract description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 46
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 45
- 229910021529 ammonia Inorganic materials 0.000 claims description 23
- 238000007254 oxidation reaction Methods 0.000 claims description 23
- 230000003647 oxidation Effects 0.000 claims description 22
- 238000005273 aeration Methods 0.000 claims description 19
- 230000014759 maintenance of location Effects 0.000 claims description 13
- 230000001105 regulatory effect Effects 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims description 10
- 230000001276 controlling effect Effects 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- LPXPTNMVRIOKMN-UHFFFAOYSA-M sodium nitrite Chemical compound [Na+].[O-]N=O LPXPTNMVRIOKMN-UHFFFAOYSA-M 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 5
- 235000010288 sodium nitrite Nutrition 0.000 claims description 3
- 241000894006 Bacteria Species 0.000 abstract description 19
- 241001453382 Nitrosomonadales Species 0.000 abstract description 6
- 238000010521 absorption reaction Methods 0.000 abstract description 6
- 230000001546 nitrifying effect Effects 0.000 abstract description 3
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 abstract description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 9
- 230000000694 effects Effects 0.000 description 6
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 5
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 4
- 208000037534 Progressive hemifacial atrophy Diseases 0.000 description 3
- 230000001651 autotrophic effect Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000012017 passive hemagglutination assay Methods 0.000 description 3
- 229920000903 polyhydroxyalkanoate Polymers 0.000 description 3
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000005416 organic matter Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 1
- 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 1
- 239000002253 acid Substances 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
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- 150000004665 fatty acids Chemical class 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000004060 metabolic process Effects 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
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- 231100000331 toxic Toxicity 0.000 description 1
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Abstract
The invention provides a low-carbon low-energy-consumption nitrogen and phosphorus removal method for urban sewage, belonging to the field of sewage treatment. The invention provides a sludge cyclone separator and a Free Nitrite (FNA) treatment unit which are added in a continuous flow anaerobic-Aerobic (AO) sewage treatment process. The urban sewage and the flocculated sludge of the reflux spin flow separator enter an anaerobic zone to generate anaerobic phosphorus release, and then enter an aerobic zone to generate aerobic phosphorus absorption and short-cut nitrification-anaerobic ammoxidation. Separating the secondary sedimentation tank sediment sludge by a cyclone separator, and enabling heavy granular sludge to enter an aerobic zone, wherein the heavy granular sludge is rich in anaerobic ammonia oxidizing bacteria; the light floccule sludge is rich in nitrifying bacteria and phosphorus accumulating bacteria, one part of the light floccule sludge flows back to the anaerobic zone, the other part of the light floccule sludge flows back to the aerobic zone after being treated by FNA, and the rest of the light floccule sludge is discharged as surplus sludge. The invention can realize low-carbon low-energy-consumption denitrification and dephosphorization of urban sewage with low carbon-nitrogen ratio.
Description
Technical Field
The invention relates to the field of sewage treatment, in particular to a low-carbon low-energy-consumption denitrification and dephosphorization method for urban sewage.
Background
At present, the urban sewage denitrification and dephosphorization generally adopts the traditional A 2 O technology: the anaerobic zone (zone A) generates phosphorus release reaction, the anoxic zone (zone A) generates denitrification reaction, and the aerobic zone (zone O) generates aerobic nitrification reaction. The traditional biological treatment process has the problems of high energy consumption (fossil fuel consumption), emission of a large amount of greenhouse gases (including CO 2、N2 O and the like), addition of external carbon sources, addition of chemical dephosphorization agents and the like.
In the traditional biological phosphorus removal system, phosphorus accumulating bacteria (PAOs) convert Volatile Fatty Acids (VFAs) in sewage into internal carbon sources PHAs in an anaerobic zone, release phosphate, and then excessively absorb phosphorus in an aerobic zone or an anoxic zone, so that the aim of biological phosphorus removal of the sewage is fulfilled. For urban sewage with low C/N ratio, the organic matter content is insufficient, so that the phosphorus release amount is low, the subsequent phosphorus absorption amount is low, and the biological phosphorus removal effect is difficult to ensure, so that chemical agents are required to be added for chemical phosphorus removal, and the effluent phosphorus reaches the standard.
In the traditional biological nitrification and denitrification technology, carbon sources are needed for denitrification, and for sewage with lower C/N ratio, denitrification cannot be effectively performed without adding an organic carbon source. In view of this limitation, a novel denitrification process, namely, a short-cut nitrification-anaerobic ammonia oxidation process, has emerged in recent years. The process comprises the steps of oxidizing ammonia nitrogen into nitrite nitrogen through short-cut nitrification, and then converting the nitrite nitrogen and ammonia nitrogen in sewage into nitrogen through anaerobic ammonia oxidation reaction, so that the total nitrogen is removed. Because the anaerobic ammonia oxidation denitrification does not need an organic carbon source and oxygen, the technology can realize low-carbon and low-energy-consumption biological denitrification. It was found that organic matter had an effect on the growth and metabolism of anammox bacteria. In the urban sewage continuous flow activated sludge process denitrification and dephosphorization process, the reflux sludge and sewage enter an anaerobic zone together, so that organic matters in the sewage have adverse effects on anaerobic ammonia oxidizing bacteria in the sludge.
In the earlier stage, we propose a method for realizing autotrophic denitrification of urban sewage by symbiotic floc sludge and granular sludge, and the patent publication No. CN 104529056A is that organic matters in sewage are removed in a high-load activated sludge reactor, short-cut nitrification anaerobic ammonia oxidation denitrification is realized in an autotrophic denitrification reactor, and sewage denitrification can be realized under a low-carbon condition. However, the method does not involve dephosphorization, and the high-load activated sludge reactor in front of the method is continuous flow, and the autotrophic denitrification reactor in back is intermittent operation, so that a water tank is needed to adjust the flow in the middle, and the complexity is brought to the operation of the system.
In conclusion, in the current state, how to realize low-carbon denitrification and dephosphorization of continuous flow sewage has important significance.
Disclosure of Invention
In view of the above, the invention provides a low-carbon low-energy-consumption nitrogen and phosphorus removal method for urban sewage, and aims to solve the problem that low-carbon urban sewage is difficult to remove nitrogen and phosphorus in a high-efficiency low-energy-consumption biological manner.
The invention provides a low-carbon low-energy-consumption nitrogen and phosphorus removal method for urban sewage, which comprises the following steps: inputting sewage into an AO biochemical pool, wherein the AO biochemical pool consists of an anaerobic zone and an aerobic zone, inoculating activated sludge of a sewage treatment plant to the anaerobic zone and the aerobic zone of the AO biochemical pool, inoculating anaerobic ammoxidation granular sludge to the aerobic zone of the AO biochemical pool; the effluent from the aerobic zone of the AO biochemical tank enters a secondary sedimentation tank for sedimentation, and the water after sedimentation is discharged; separating the precipitated sludge into granular sludge and flocculated sludge by a cyclone separator, and refluxing the granular sludge to an aerobic zone; and part of the flocculated sludge flows back to the anaerobic zone of the AO biochemical tank, part of the flocculated sludge enters the anaerobic zone of the AO biochemical tank after being treated by the FNA sludge treatment tank (FNA, free nitrous acid), and the other part of the flocculated sludge is discharged as surplus sludge.
In the invention, a sludge cyclone separator and a Free Nitrite (FNA) treatment unit are added in a continuous flow anaerobic-Aerobic (AO) sewage treatment process; the urban sewage and the flocculated sludge of the reflux spin flow separator enter an anaerobic zone to generate anaerobic phosphorus release, and then enter an aerobic zone to generate aerobic phosphorus absorption and short-cut nitrification-anaerobic ammoxidation; separating the secondary sedimentation tank sediment sludge by a cyclone separator, and enabling heavy granular sludge to enter an aerobic zone, wherein the heavy granular sludge is rich in anaerobic ammonia oxidizing bacteria; the light floccule sludge is rich in nitrifying bacteria and phosphorus accumulating bacteria, one part of the light floccule sludge flows back to the anaerobic zone, the other part of the light floccule sludge flows back to the aerobic zone after being treated by FNA, and the rest of the light floccule sludge is discharged as surplus sludge. The method of the invention can better realize low-carbon low-energy-consumption denitrification and dephosphorization of urban sewage with low carbon-nitrogen ratio.
Further, inoculating activated sludge of a sewage treatment plant to an anaerobic zone and an aerobic zone of an AO biochemical pool, so that the sludge concentration is 3000-4500mg/L; inoculating anaerobic ammonia oxidation granular sludge to an aerobic zone of an AO biochemical pool, so that the concentration of the anaerobic ammonia oxidation granular sludge is 800-1800mg/L; the runtime adjustment operation is as follows:
1) The sludge reflux ratio of the anaerobic zone of the AO biochemical pool is 50-120%;
2) The total hydraulic retention time of the AO biochemical pool is 8.5-12h, wherein the hydraulic retention time of the anaerobic zone is 2.8-4h, and the hydraulic retention time of the aerobic zone is 5.6-8h;
3) The concentration of dissolved oxygen in the aerobic zone of the AO biochemical pool is controlled to be 0.2-0.5mg/L;
4) Controlling the flow dividing ratio of the bottom flow opening of the cyclone separator to be 17-20% and the flow dividing ratio of the overflow opening to be 80-83%;
5) Sodium nitrite is added into the FNA sludge treatment tank, the sludge treatment time is controlled to be 20-24 hours, and the sludge reflux ratio is 20% -25%;
6) Part of the flocculated sludge generated by the cyclone separator is used as surplus sludge to be discharged.
The invention provides a low-carbon low-energy-consumption nitrogen and phosphorus removal system for municipal sewage, which comprises a municipal sewage tank, an AO biochemical tank, a secondary sedimentation tank, a cyclone separator and an FNA sludge treatment tank which are sequentially connected, wherein the AO biochemical tank consists of an anaerobic area and an aerobic area, the bottom of the cyclone separator is connected with the aerobic area of the AO biochemical tank, and the cyclone separator is also respectively connected with the FNA sludge treatment tank, the anaerobic area of the AO biochemical tank and a sludge discharge valve.
Further, the municipal sewage tank is provided with an overflow pipe and a blow-down pipe.
Furthermore, the AO biochemical pool is divided into six cells, and overflow holes are arranged in an up-down staggered manner according to the water flow direction and are connected with the cells; the first and second cells are anaerobic regions, and the third to sixth cells are aerobic regions.
Further, an anaerobic zone of the AO biochemical pool is provided with a stirrer and an aeration head, and the aeration head is sequentially connected with a gas flow regulating valve, a gas flowmeter and an air compressor.
Further, in the operation of 5), the nitrite concentration of the FNA sludge treatment tank is controlled to be 300-1000mg/L.
Further, in the operation of 5), the pH value in the FNA sludge treatment tank is controlled to be 5.5-6.0.
Further, in the operation of 6), the mud age of the flocculated mud is controlled to be 3-7d.
Furthermore, the low-carbon low-energy-consumption nitrogen and phosphorus removal method for the municipal sewage is provided with a municipal sewage tank, an AO biochemical tank, a secondary sedimentation tank, a cyclone separator and an FNA sludge treatment tank; the urban sewage tank is provided with an overflow pipe and a blow-down pipe; the urban sewage tank is connected with an AO biochemical tank water inlet valve through an AO biochemical tank water inlet pump; the AO biochemical pool is divided into a plurality of cells, and overflow holes are arranged in an up-and-down staggered manner according to the water flow direction and are connected with the cells; the first and second cells are anaerobic areas, and the third to sixth cells are aerobic areas; the anaerobic zone is provided with a stirrer and an aeration head, and the aeration head is sequentially connected with a gas flow regulating valve, a gas flowmeter and an air compressor; the AO biochemical tank water outlet pipe is connected with a secondary sedimentation tank water inlet valve, and finally the effluent is discharged through the secondary sedimentation tank water outlet pipe; the sediment sludge in the secondary sedimentation tank enters a cyclone separator through a sludge inlet pump of the cyclone separator to separate the sediment sludge in the secondary sedimentation tank, and heavy granular sludge flows back to an aerobic zone; part of light flocculated sludge is discharged as surplus sludge through a surplus sludge discharge valve, part of light flocculated sludge flows back to an anaerobic zone through a sludge reflux pump, and part of light flocculated sludge enters the FNA sludge treatment tank through a sludge inlet valve of the FNA sludge treatment tank and a sludge inlet pump of the FNA sludge treatment tank; the FNA sludge treatment tank is provided with an FNA sludge treatment tank stirrer, and is connected with the aerobic zone of the AO biochemical tank through a FNA sludge treatment tank sludge discharge valve.
By adopting the method, urban sewage and flocculated sludge of the reflux self-cyclone separator enter an anaerobic zone, and PAOs are subjected to anaerobic phosphorus release and internal carbon source PHAs storage; then the sludge mixed liquor enters an aerobic zone; simultaneously, the cyclone separator is used for separating the returned sludge, and the heavy granular sludge enters an aerobic zone and mainly takes anaerobic ammonia oxidizing bacteria; part of light floccule sludge flows back to the anaerobic zone, and the other floccule sludge is discharged as surplus sludge after the part of light floccule sludge is treated by FNA to inhibit nitrite oxidizing bacteria and then flows back to the aerobic zone; the aerobic zone has short-cut nitrification anaerobic ammonia oxidation and phosphorus absorption function, so that synchronous denitrification and phosphorus removal are realized.
Compared with the prior art, the invention has the beneficial effects that:
(1) Aiming at the problem that low-carbon urban sewage is difficult to realize high-efficiency low-energy-consumption biological denitrification and dephosphorization, the hydrocyclone is arranged to separate granular sludge rich in anaerobic ammonia oxidation bacteria from floccule sludge containing phosphorus accumulating bacteria and nitrifying bacteria, and the floccule sludge is returned to an anaerobic zone, so that limited organic matters in raw water are utilized by the phosphorus accumulating bacteria, and meanwhile, the granular sludge does not enter the anaerobic zone to contact with organic matters in the raw water, thereby avoiding adverse effects of the organic matters on the anaerobic ammonia oxidation bacteria; on the other hand, part of floccule sludge is treated by Free Nitrous Acid (FNA), so that short-cut nitrification is promoted, and granular sludge rich in anaerobic ammonia oxidizing bacteria is not treated by FNA, so that toxic action of FNA on the anaerobic ammonia oxidizing bacteria is avoided; in addition, the floc sludge after aerobic phosphorus absorption is used as surplus sludge to be discharged, so that the reinforced phosphorus removal is realized; the granular sludge does not need to be discharged, so that the retention of anaerobic ammonia oxidation bacteria in the system is promoted, and the stable maintenance of anaerobic ammonia oxidation denitrification is promoted.
(2) Compared with the traditional A 2 O process, the low-carbon low-energy-consumption nitrogen and phosphorus removal method for urban sewage has the following advantages:
1) The organic matters in the water are only utilized by the floccule sludge rich in the phosphorus accumulating bacteria, and the limited organic matters are utilized by the phosphorus accumulating bacteria, so that the phosphorus accumulating bacteria can store more PHAs as an internal carbon source, and the subsequent phosphorus absorption is facilitated.
2) The separation process of the cyclone separator ensures that the floccule sludge containing the phosphorus accumulating bacteria is used as a residual sludge discharge system, the dephosphorization effect is enhanced, and meanwhile, the loss of anaerobic ammonia oxidation bacteria from the system is avoided.
3) The realization of short-cut nitrification anaerobic ammonia oxidation reduces the demand of denitrification for organic carbon sources in sewage, and simultaneously saves aeration energy consumption.
4) Measures such as FNA sludge treatment process, low-oxygen conditions, periodic sludge discharge, anaerobic ammonia oxidation granular sludge and the like are comprehensively applied, so that the method is beneficial to stabilizing short-cut nitrification, ensuring the denitrification performance of anaerobic ammonia oxidation bacteria and realizing the high-efficiency denitrification of short-cut nitrification anaerobic ammonia oxidation.
Drawings
FIG. 1 is a schematic diagram of a low-carbon low-energy-consumption denitrification and dephosphorization system for urban sewage.
In the figure, the urban sewage tank 1, the AO biochemical tank 2, the secondary sedimentation tank 3, the cyclone separator 4, the FNA sludge treatment tank 5, the overflow pipe 11, the blow-down pipe 12, the AO biochemical tank water inlet pump 21, the AO biochemical tank water inlet valve 22, the anaerobic zone 23, the aerobic zone 24, the aeration head 25, the stirrer 26, the air flow regulating valve 27, the air compressor 28, the air flowmeter 29, the AO biochemical tank water outlet pipe 210, the secondary sedimentation tank water inlet valve 31, the secondary sedimentation tank water outlet pipe 32, the cyclone separator sludge inlet pump 41, the surplus sludge discharge valve 42, the aerobic zone sludge reflux valve 43, the anaerobic zone sludge reflux valve 44, the anaerobic zone sludge reflux pump 45, the FNA sludge treatment tank sludge inlet valve 51, the FNA sludge treatment tank sludge inlet pump 52, the FNA sludge treatment tank sludge discharge valve 53 and the FNA sludge treatment tank stirrer 54.
Detailed Description
In order to better understand the technical content of the present invention, the following provides specific examples to further illustrate the present invention.
Example 1
A low-carbon low-energy-consumption nitrogen and phosphorus removal system for municipal sewage comprises a municipal sewage tank 1, an AO biochemical tank 2, a secondary sedimentation tank 3, a cyclone separator 4 and an FNA sludge treatment tank 5, wherein the municipal sewage tank 1, the AO biochemical tank 2, the secondary sedimentation tank 3, the cyclone separator 4 and the FNA sludge treatment tank 5 are sequentially connected; the municipal sewage tank 1 is provided with an overflow pipe 11 and a blow-down pipe 12; the urban sewage tank 1 is connected with an AO biochemical tank water inlet valve 22 through an AO biochemical tank water inlet pump 21; the AO biochemical pool 2 is divided into a plurality of cells, in the embodiment, 6 cells are preferable, the flow holes are arranged up and down in a staggered way according to the water flow direction and are connected with the cells, the first cell and the second cell are anaerobic areas 23, and the third cell to the sixth cell are aerobic areas 24; each cell of the anaerobic zone 23 is provided with a stirrer 26; the aerobic zone 24 is provided with an air compressor 28, an air flowmeter 29, a plurality of air flow regulating valves 27 and a plurality of aeration heads 25, wherein the air compressor 28, the air flowmeter 29, the air flow regulating valves 27 and the aeration heads 25 are sequentially connected, each cell is provided with one aeration head 25, and each aeration head 25 is connected with one air flow regulating valve 27; the AO biochemical tank water outlet pipe 210 is connected with a secondary sedimentation tank water inlet valve 31, and the secondary sedimentation tank 3 is provided with a secondary sedimentation tank water outlet pipe 32 for discharging final water; the bottom of the cyclone separator 4 is connected with the aerobic zone 24 of the AO biochemical tank 2 through an aerobic zone sludge reflux valve 43; the cyclone separator 4 is connected with the FNA sludge treatment tank 5 through a FNA sludge treatment tank inlet valve 51 and a FNA sludge treatment tank inlet pump 52, the FNA sludge treatment tank 5 is provided with a FNA sludge treatment tank stirrer 54, and is connected with the aerobic zone 24 of the AO biochemical tank through a FNA sludge treatment tank discharge valve 53; the cyclone separator 4 is connected with the anaerobic zone 23 of the AO biochemical pool 2 through an anaerobic zone sludge reflux valve 44 and an anaerobic zone sludge reflux pump 45; the cyclone 4 is connected to a surplus sludge discharge valve 42.
The working method comprises the following steps: inputting municipal sewage into an AO biochemical pool 2, inoculating activated sludge of a municipal sewage treatment plant to an anaerobic zone 23 and an aerobic zone 24 of the AO biochemical pool 2, and inoculating anaerobic ammoxidation granular sludge to the aerobic zone 24 of the AO biochemical pool 2; the effluent from the aerobic zone 24 of the AO biochemical tank enters the secondary sedimentation tank 3 for sedimentation, and finally the effluent is discharged through a secondary sedimentation tank water outlet pipe 32; the sediment sludge of the secondary sedimentation tank 3 enters a cyclone separator 4 through a cyclone separator mud inlet pump 41, the cyclone separator 4 sorts the return sludge, and after sorting, the heavy granular sludge returns to the aerobic zone 24; part of the light flocculated sludge is returned to the anaerobic zone 23 by a sludge return pump 45, and the other part of the light flocculated sludge is fed into the FNA sludge treatment tank 5 by a FNA sludge treatment tank feed valve 51 and a FNA sludge treatment tank feed pump 52; enters the aerobic zone 24 of the AO biochemical tank through the FNA sludge treatment tank sludge discharge valve 53, and a part of the sludge is discharged as surplus sludge through the surplus sludge discharge valve 42.
Example 2
A low-carbon low-energy-consumption denitrification and dephosphorization method for urban sewage comprises the following steps: the system for low-carbon and low-energy denitrification and dephosphorization of the municipal sewage according to the embodiment 1 is provided with a municipal sewage tank 1, an AO biochemical tank 2, a secondary sedimentation tank 3, a cyclone separator 4 and an FNA sludge treatment tank 5; the municipal sewage tank 1 is provided with an overflow pipe 11 and a blow-down pipe 12; the urban sewage tank 1 is connected with an AO biochemical tank water inlet valve 22 through an AO biochemical tank water inlet pump 21; the AO biochemical pool 2 is divided into a plurality of cells, in this embodiment, preferably 6 cells, and the flow holes are arranged up and down in a staggered manner according to the water flow direction to connect the cells; the first and second cells are anaerobic zones 23, and the third to sixth cells are aerobic zones 24; each cell of the anaerobic zone 23 is provided with a stirrer 26; the aerobic zone 24 is provided with an air compressor 28, an air flowmeter 29, a plurality of air flow regulating valves 27 and a plurality of aeration heads 25, wherein the air compressor 28, the air flowmeter 29, the air flow regulating valves 27 and the aeration heads 25 are sequentially connected, each cell is provided with one aeration head 25, and each aeration head 25 is connected with one air flow regulating valve 27; the AO biochemical pond water outlet pipe 210 is connected with the secondary sedimentation pond water inlet valve 31, and finally the effluent is discharged through the secondary sedimentation pond water outlet pipe 32; the sediment sludge of the secondary sedimentation tank enters a cyclone separator 4 through a cyclone separator mud feeding pump 41, the cyclone separator 4 sorts the return sludge, and after sorting, the heavy granular sludge returns to the aerobic zone 24; part of the light flocculated sludge is discharged as surplus sludge through a surplus sludge discharge valve 42, part of the light flocculated sludge is returned to the anaerobic zone through a sludge return pump 45, and the other part of the light flocculated sludge enters an FNA sludge treatment tank 5 through an FNA sludge treatment tank inlet valve 51 and an FNA sludge treatment tank inlet pump 52; the FNA sludge treatment tank 5 is provided with a FNA sludge treatment tank stirrer 54, and is connected with the aerobic zone 24 of the AO biochemical tank through a FNA sludge treatment tank discharge valve 53.
The test adopts artificial water distribution as simulated urban sewage, and the specific water quality is as follows: COD concentration is 150-300mg/L; NH 4 + -N concentration is 50-80mg/L, NO 2 - -N concentration is 0-0.5mg/L, NO 3 - -N concentration is 0-0.5mg/L, and TP concentration is 3-7 mg/L. As shown in FIG. 1, each reactor is made of organic glass, the effective volume of the AO biochemical tank is 30L, the AO biochemical tank is divided into 6 cells, and the volume of the FNA sludge treatment tank is 10L.
1) Starting a system: inoculating activated sludge of a municipal sewage treatment plant to an anaerobic zone and an aerobic zone of an AO biochemical tank, and enabling the sludge concentration to be 4000mg/L; inoculating anaerobic ammonia oxidation granular sludge, and adding the anaerobic ammonia oxidation granular sludge into an aerobic zone 23 of an AO biochemical tank to ensure that the concentration of the anaerobic ammonia oxidation granular sludge is 1200mg/L;
2) The runtime adjustment operation is as follows:
2.1 The sludge reflux ratio of the anaerobic zone of the AO biochemical pool is 100 percent;
2.2 The total hydraulic retention time of the AO biochemical pool is 12 hours, wherein the hydraulic retention time of the anaerobic zone is 4 hours, and the hydraulic retention time of the aerobic zone is 8 hours;
2.3 The dissolved oxygen concentration in the aerobic zone of the AO biochemical pool is controlled to be 0.5mg/L by controlling a gas flowmeter 29 and a gas quantity regulating valve 27;
2.4 The flow rate is controlled by a mud feeding pump of the water conservancy cyclone separator 4, so that the flow dividing ratio of a bottom flow opening of the water conservancy cyclone separator 4 is 20%, the flow dividing ratio of an overflow opening is 80%, heavy granular sludge is discharged from the bottom flow opening, and light floccule sludge is discharged from the overflow opening;
2.5 Sodium nitrite is added into the FNA sludge treatment tank, the nitrite concentration of the FNA sludge treatment tank is controlled to be 400mg/L, acid or alkali is added to control the pH value of the FNA sludge treatment tank to be 6, the sludge treatment time is controlled to be 24 hours, and the sludge reflux ratio is 25%;
2.6 The system periodically discharges the flocculent sludge, and the sludge age is controlled to be 7d.
The test results show that: after stable operation, the COD concentration of the system effluent is 25-70mg/L, and the average COD concentration is 40 mg/L; NH 4 + -N concentration is 0-2.5 mg/L, average 1.3 mg/L, NO 2 - -N concentration is 0-1mg/L, average 0.05mg/L, NO 3 - -N concentration is 0-5mg/L, average 2.5 mg/L, TP concentration is 0-0.7mg/L, average 0.3mg/L.
In addition, inoculating activated sludge of a sewage treatment plant to ensure that the concentration of the sludge is 3000-4500mg/L; inoculating anaerobic ammonia oxidation granular sludge to ensure that the sludge concentration is 800-1800mg/L;2.1 The sludge reflux ratio of the anaerobic zone of the AO biochemical pool is 50-120 percent; 2.2 The total hydraulic retention time of the AO biochemical pool is 8.5-12h, wherein the hydraulic retention time of the anaerobic zone is 2.8-4h, and the hydraulic retention time of the aerobic zone is 5.6-8h;2.3 The concentration of dissolved oxygen in the aerobic zone is controlled to be 0.2-0.5mg/L;2.4 The diversion ratio of the bottom flow port of the cyclone separator is 17-20%, and the diversion ratio of the overflow port is 80-83%; 2.5 Feeding nitrite to the FNA sludge treatment tank, controlling the concentration of nitrite to be 300-1000mg/L, controlling the pH value to be 5.5-6, controlling the sludge treatment time to be 20-24h, and controlling the sludge reflux ratio to be 20% -25%;2.6 Controlling the mud age of the floccule mud to be 3-7d. The process can be adjusted within the above range, and the object of the present invention can be achieved.
Comparative example
In the municipal sewage treated by the basic adjustment process of example 2, the concentration of TN and TP in the treated effluent can be greatly increased by adopting the conventional AO process under the conditions that a cyclone separator is not used, an FNA sludge treatment tank is not used (FNA treatment is not used), sludge precipitated in a secondary sedimentation tank only flows back to an anaerobic zone, and anaerobic ammonia oxidation granular sludge is not inoculated. Because the organic matters in the inlet water are limited, the requirement of denitrification on a carbon source is difficult to meet, and therefore the TN concentration of the outlet water can be increased; meanwhile, the demand of biological phosphorus removal on organic matters cannot be met, and the concentration of effluent TP is increased; in addition, if the effect of ammonia nitrogen in the effluent is consistent with that of example 2, the aeration energy consumption of the comparative example is increased, because all ammonia nitrogen needs to be oxidized into nitrite nitrogen first and then oxidized into nitrate nitrogen continuously, and only part of ammonia nitrogen needs to be oxidized into nitrite nitrogen in example 2.
Claims (8)
1. The low-carbon low-energy-consumption nitrogen and phosphorus removal method for the urban sewage is characterized by comprising the following steps of: inputting sewage into an AO biochemical pool, wherein the AO biochemical pool consists of an anaerobic zone and an aerobic zone, inoculating activated sludge of a sewage treatment plant to the anaerobic zone and the aerobic zone of the AO biochemical pool, inoculating anaerobic ammoxidation granular sludge to the aerobic zone of the AO biochemical pool; the effluent from the aerobic zone of the AO biochemical tank enters a secondary sedimentation tank for sedimentation, and the water after sedimentation is discharged; separating the precipitated sludge into granular sludge and flocculated sludge by a cyclone separator, and refluxing the granular sludge to an aerobic zone; the flocculated sludge partially flows back to the anaerobic zone of the AO biochemical tank, and partially enters the anaerobic zone of the AO biochemical tank after being treated by the FNA sludge treatment tank, and partially is discharged as surplus sludge;
Inoculating activated sludge of a sewage treatment plant to an anaerobic zone and an aerobic zone of an AO biochemical pool, so that the sludge concentration is 3000-4500mg/L; inoculating anaerobic ammonia oxidation granular sludge to an aerobic zone of an AO biochemical pool, so that the concentration of the anaerobic ammonia oxidation granular sludge is 800-1800mg/L;
the runtime adjustment operation is as follows:
1) The sludge reflux ratio of the anaerobic zone of the AO biochemical pool is 50-120%;
2) The total hydraulic retention time of the AO biochemical pool is 8.5-12h, wherein the hydraulic retention time of the anaerobic zone is 2.8-4h, and the hydraulic retention time of the aerobic zone is 5.6-8h;
3) The concentration of dissolved oxygen in the aerobic zone of the AO biochemical pool is controlled to be 0.2-0.5mg/L;
4) Controlling the flow dividing ratio of the bottom flow opening of the cyclone separator to be 17-20% and the flow dividing ratio of the overflow opening to be 80-83%;
5) Sodium nitrite is added into the FNA sludge treatment tank, the sludge treatment time is controlled to be 20-24 hours, and the sludge reflux ratio is 20% -25%;
6) Part of the flocculated sludge generated by the cyclone separator is used as surplus sludge to be discharged.
2. The method according to claim 1, wherein in 5), the nitrite concentration of the FNA sludge treatment tank is controlled to 300-1000mg/L.
3. The method according to claim 1, wherein in 5), the pH is controlled to 5.5-6.0 in the FNA sludge treatment pond.
4. The method according to claim 1, wherein in 6), the sludge age of the flocculated sludge is controlled to be 3-7d.
5. The method according to any one of claims 1-4, wherein there is provided a municipal sewage tank, an AO biochemical tank, a secondary sedimentation tank, a cyclone separator, an FNA sludge treatment tank; the urban sewage tank is provided with an overflow pipe and a blow-down pipe; the urban sewage tank is connected with an AO biochemical tank water inlet valve through an AO biochemical tank water inlet pump; the AO biochemical pool is divided into six cells, and the overflow holes are arranged in an up-and-down staggered manner according to the water flow direction and are connected with the cells; the first and second cells are anaerobic areas, and the third to sixth cells are aerobic areas; the anaerobic zone is provided with a stirrer and an aeration head, and the aeration head is sequentially connected with a gas flow regulating valve, a gas flowmeter and an air compressor; the AO biochemical tank water outlet pipe is connected with a secondary sedimentation tank water inlet valve, and finally the effluent is discharged through the secondary sedimentation tank water outlet pipe; the sediment sludge in the secondary sedimentation tank enters a cyclone separator through a sludge inlet pump of the cyclone separator to separate the sediment sludge in the secondary sedimentation tank, and heavy granular sludge flows back to an aerobic zone; part of light flocculated sludge is discharged as surplus sludge through a surplus sludge discharge valve, part of light flocculated sludge flows back to an anaerobic zone through a sludge reflux pump, and part of light flocculated sludge enters the FNA sludge treatment tank through a sludge inlet valve of the FNA sludge treatment tank and a sludge inlet pump of the FNA sludge treatment tank; the FNA sludge treatment tank is provided with an FNA sludge treatment tank stirrer, and is connected with the aerobic zone of the AO biochemical tank through a FNA sludge treatment tank sludge discharge valve.
6. A system for operating the low-carbon low-energy-consumption denitrification and dephosphorization method for municipal sewage according to any one of claims 1 to 4, which is characterized by comprising a municipal sewage tank, an AO biochemical tank, a secondary sedimentation tank, a cyclone separator and an FNA sludge treatment tank which are sequentially connected, wherein the AO biochemical tank consists of an anaerobic zone and an aerobic zone, the bottom of the cyclone separator is connected with the aerobic zone of the AO biochemical tank, and the cyclone separator is also respectively connected with the FNA sludge treatment tank, the anaerobic zone of the AO biochemical tank and a sludge discharge valve; the AO biochemical pool is divided into six cells, and the overflow holes are arranged in an up-and-down staggered manner according to the water flow direction and are connected with the cells; the first and second cells are anaerobic regions, and the third to sixth cells are aerobic regions.
7. The system of claim 6, wherein the municipal sewage tank is provided with an overflow pipe and a blow-down pipe.
8. The system of claim 6, wherein the anaerobic zone of the AO biochemical pond is provided with a stirrer and an aeration head, and the aeration head is sequentially connected with a gas flow regulating valve, a gas flow meter and an air compressor.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104529056A (en) * | 2014-11-29 | 2015-04-22 | 北京工业大学 | Method for realizing autotrophic nitrogen removal of city sewage through symbiosis of flocculent sludge and granular sludge |
| CN111960538A (en) * | 2020-09-02 | 2020-11-20 | 北京城市排水集团有限责任公司 | System and method for realizing stable operation of shortcut nitrification-anaerobic ammonia oxidation denitrification of low-ammonia nitrogen wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104529056A (en) * | 2014-11-29 | 2015-04-22 | 北京工业大学 | Method for realizing autotrophic nitrogen removal of city sewage through symbiosis of flocculent sludge and granular sludge |
| CN111960538A (en) * | 2020-09-02 | 2020-11-20 | 北京城市排水集团有限责任公司 | System and method for realizing stable operation of shortcut nitrification-anaerobic ammonia oxidation denitrification of low-ammonia nitrogen wastewater |
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