CN111099727A - In-situ sewage and odor treatment device for sewage treatment plant - Google Patents
In-situ sewage and odor treatment device for sewage treatment plant Download PDFInfo
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- 239000010865 sewage Substances 0.000 title claims abstract description 83
- 238000011065 in-situ storage Methods 0.000 title claims abstract description 30
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 44
- 239000010802 sludge Substances 0.000 claims abstract description 40
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 22
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 21
- 230000023556 desulfurization Effects 0.000 claims abstract description 21
- 230000001360 synchronised effect Effects 0.000 claims abstract description 21
- 238000005192 partition Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 90
- 239000007789 gas Substances 0.000 claims description 41
- 238000005273 aeration Methods 0.000 claims description 31
- 230000004048 modification Effects 0.000 claims description 22
- 238000012986 modification Methods 0.000 claims description 22
- 239000000945 filler Substances 0.000 claims description 21
- 238000009826 distribution Methods 0.000 claims description 19
- 238000007254 oxidation reaction Methods 0.000 claims description 19
- 230000003647 oxidation Effects 0.000 claims description 16
- 206010021143 Hypoxia Diseases 0.000 claims description 12
- 230000000694 effects Effects 0.000 claims description 11
- 238000005507 spraying Methods 0.000 claims description 10
- 230000009466 transformation Effects 0.000 claims description 9
- 244000005700 microbiome Species 0.000 claims description 8
- 238000012856 packing Methods 0.000 claims description 7
- 229910001220 stainless steel Inorganic materials 0.000 claims description 6
- 239000010935 stainless steel Substances 0.000 claims description 6
- 239000007921 spray Substances 0.000 claims description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000007788 liquid Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 229910000831 Steel Inorganic materials 0.000 claims description 3
- 238000007664 blowing Methods 0.000 claims description 3
- 239000011521 glass Substances 0.000 claims description 3
- 230000014759 maintenance of location Effects 0.000 claims description 3
- 239000005416 organic matter Substances 0.000 claims description 3
- 239000010959 steel Substances 0.000 claims description 3
- 229910002651 NO3 Inorganic materials 0.000 abstract description 29
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 abstract description 29
- 238000000034 method Methods 0.000 abstract description 26
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 abstract description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 7
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 7
- 229910052799 carbon Inorganic materials 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 4
- 229910052717 sulfur Inorganic materials 0.000 abstract description 3
- 239000011593 sulfur Substances 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract 2
- 238000006243 chemical reaction Methods 0.000 abstract 1
- 230000008569 process Effects 0.000 description 20
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 18
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 7
- 230000009471 action Effects 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 238000002474 experimental method Methods 0.000 description 4
- 230000002829 reductive effect Effects 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 3
- 238000004088 simulation Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- 230000001651 autotrophic effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 241001453382 Nitrosomonadales Species 0.000 description 1
- 208000028571 Occupational disease Diseases 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 241000605118 Thiobacillus Species 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
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/406—Ammonia
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Hydrology & Water Resources (AREA)
- Organic Chemistry (AREA)
- Water Supply & Treatment (AREA)
- Environmental & Geological Engineering (AREA)
- Microbiology (AREA)
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Abstract
The invention discloses an in-situ sewage and odor treatment device for a sewage treatment plant, which mainly comprises an odor collecting system, an odor conveying system and an odor treatment system; the odor collecting system consists of a gas collecting hood, an air pipe and a first fan; the odor delivery system consists of a pipeline and a second fan; the odor treatment system utilizes the partition plate to separate the anoxic tank into a preposed selection tank area and a postposition anoxic tank area, wherein the preposed selection tank has three different structures, and can adopt a proper scheme to dissolve odor aiming at different conditions, so as to in-situ treat nitrate-containing sewage and sulfur-containing ammonia-containing odor through a synchronous denitrification and desulfurization and anaerobic ammoxidation reaction mechanism. The method has the advantages of simple scheme, low manufacturing cost and novel thought, removes the odor of the urban sewage treatment plant, simultaneously uses the sulfide and the ammonia in the sewage to reduce nitrate, meets the requirement of denitrification in the sewage, achieves the purpose of treating waste by waste, reduces the carbon source input amount and the residual sludge yield, and has good ecological benefit.
Description
Technical Field
The invention relates to an in-situ sewage and odor treatment device for a sewage treatment plant, belonging to the technical field of biological treatment of wastewater.
Background
At present, urban domestic sewage is treated by adopting the traditional biological nitrification/denitrification process (A)2/O, A/O process), while the denitrification process requires organic materialCarbon source as electron donor, NOX -Reduction of-N to N2However, urban domestic sewage in China generally has the problem of low C/N, and the domestic sewage is insufficient in carbon source, so that the denitrification efficiency is low, and the total nitrogen of effluent is too high, so that the effluent can not reach the first-class A discharge standard of pollutant discharge Standard of urban sewage treatment plant (GB 18918-2002); after the process is adopted for treatment, a large amount of excess sludge is generated, and the disposal of the excess sludge is gradually a big problem.
In the process of urban sewage treatment, a large amount of malodorous gas is released to the external environment, and the gas can cause potential harm to the living environment and the health of people. At present, occupational diseases of related workers of urban sewage treatment plants frequently occur, and related standards for gas release of urban sewage treatment plants are lacked, so that the problem of release of malodorous gas in the sewage treatment process becomes a problem to be solved urgently. Meanwhile, the research shows that the inorganic components in the malodorous gas are mainly volatile substances containing sulfur and nitrogen elements, and A is adopted2The detection of possible gas release sources in the treatment process of the sewage and sludge in the/O process shows that a large amount of H is generated in the grids, the lifting pump room, the primary sedimentation tank, the anaerobic zone, the anoxic zone, the secondary sedimentation tank, the sludge concentration tank and the sludge dewatering machine room2S and NH3Mainly malodorous gas.
The synchronous denitrification and desulfurization process and the anaerobic ammonia oxidation process are the key points of the autotrophic denitrification research of the wastewater in recent years. The synchronous denitrification and desulfurization process refers to the process of reducing nitrate nitrogen into N by using certain obligate inorganic chemolithoautotrophic thiobacillus under the oxygen-free or oxygen-deficient environment and using reductive sulfur-containing compounds (such as sulfide and the like) as electron donors2The autotrophic denitrification process. The synchronous denitrification and desulfurization process has the characteristics of no need of adding a carbon source, carbon footprint consumption, low sludge yield, low energy consumption and the like. The anaerobic ammonia oxidation refers to the generation of N under the action of anaerobic ammonia oxidizing bacteria by taking ammonium salt as an electron donor and nitrite/nitrate as an electron acceptor under the anaerobic or anoxic condition2(ii) a Compared with the traditional biological denitrification process, the anaerobic ammonia oxidation process has the advantages of energy consumption saving, no need of an additional carbon source, low sludge yield and the like.
For biological processes employing denitrification (e.g. A)2The invention relates to a sewage treatment plant of/O, A/O process), an industrial wastewater treatment plant or a domestic sewage treatment plant, which utilizes reductive sulfide and ammonia in odor as electron donors, carries out in-situ treatment on nitrate in sewage and sulfide and ammonia in odor by synchronous denitrification and desulfurization and anaerobic ammonia oxidation processes without building an odor treatment device and modifying the original anoxic tank on the basis of the original anoxic tank, solves the problems of insufficient carbon source, nitrogen pollution and high sludge yield in the sewage treatment process, and has wide application prospect and ecological benefit.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides an in-situ sewage and odor treatment device for a sewage treatment plant.
The purpose of the invention is realized by the following technical scheme: an in-situ sewage and odor treatment device for a sewage treatment plant mainly comprises an odor collecting system, an odor conveying system and an odor treatment system;
the odor collecting system consists of a gas collecting hood, an air pipe and a first fan; the gas collecting hood is used for collecting odor in a sewage treatment plant and conveying the odor to the odor conveying system through the air pipe, and the first fan is connected with the air pipe to extract the odor of the gas collecting hood;
the odor delivery system consists of a pipeline and a second fan; the pipeline is connected with an air pipe in the odor collecting system and is used for conveying odor to the odor treatment system, and the second fan is connected with the pipeline and is used for extracting odor in the pipeline;
the odor treatment system is obtained by oxygen deficiency pond normal position transformation, utilizes the baffle to separate the oxygen deficiency pond, divide into leading selection pond area and rearmounted oxygen deficiency pond area, the baffle is the perforated plate, and the overflow mouth is established on baffle upper portion, and leading selection pond can have three kinds of transformation modes, is respectively:
a. the front selection tank consists of a water pump, a circulation pipeline and a tank body, wherein the tank body is divided into an air distribution layer, an aeration layer, a packing layer and a spraying layer from bottom to top, the air distribution layer is provided with a gas inlet, and the spraying layer is provided with a water inletA port and a spray device; the gas inlet of the gas distribution layer is connected with a pipeline in the odor conveying system and is used for conveying odor to the preposed selection pool; the circulating pipeline connects a water inlet of the front-mounted selection pool with a water outlet of the rear-mounted anoxic pool through a water pump to circulate water in the anoxic pool; the modification mode a is suitable for H in odor needing to be treated and requiring water flow to continuously flow through the filler2S≥500g/m3；
b. The preposed selection tank consists of a humidifier, a circulating pipeline, a water pump and a tank body, wherein the tank body is divided into an air distribution layer, an aeration layer and a packing layer from bottom to top, and the top of the tank body is provided with a water inlet; the humidifier is connected with a pipeline in the odor delivery system to humidify odor, and the air distribution layer is provided with an air inlet which is connected with the humidifier and used for delivering the humidified odor to a preposed selection pool; the circulating pipeline connects the humidifier of the front selection pool with the water outlet of the rear anoxic pool through a water pump and is used for humidifying odor; the transformation mode b is suitable for the mass concentration of the air inlet organic matter at 600-5000mg/m3The odor amount range to be treated is 1000-150000m3/h；
c. The preposed selection tank consists of a water pump, a circulating pipeline and a tank body, wherein the tank body is divided into an air distribution layer and an aeration layer from bottom to top, and the top of the tank body is provided with a water inlet; the circulating pipeline connects a water inlet of the front-mounted selection pool with a water outlet of the rear-mounted anoxic pool through a water pump to circulate water in the anoxic pool; modification mode c is suitable for conveying the odor at the speed of 20m3/(m2 .h) The following;
a. b, water in the front selection pool in the three schemes of b and c flows into the rear anoxic pool through the partition plate, and when the water level is overhigh, the water can flow into the rear anoxic pool through the overflow port; the rear anoxic pond area device is not changed, and microorganisms with the functions of synchronous denitrification and desulfurization and anaerobic ammonia oxidation after enrichment are added into the anoxic pond.
Furthermore, the gas collecting hood is made of a stainless steel framework and a sunlight plate or a stainless steel framework and a glass steel plate, and the gas collecting mode adopts an air suction type or a blowing suction type; the air pipes are configured in a main pipe mode, the air speed of the branch pipes is less than or equal to 6m/s, and the air speed of the main pipe is less than or equal to 12 m/s.
Furthermore, the partition board is arranged at 1/10-1/3 of the whole anoxic tank close to one side of the water inlet, the height of the partition board is 5-10cm lower than that of the water inlet of the front selection tank and the water outlet of the rear anoxic tank, and the width of the partition board is equal to that of the anoxic tank.
Furthermore, the height of the air distribution layer in the preposed selection tank is 0.2-0.8m higher than the bottom of the tank, and the aeration quantity of the aeration layer is determined according to the air quantity of the odor.
For modification a, the velocity of the odor in the aeration layer is 1.5-6m/s, and the retention time is 20-30 s.
For the modification mode b, the velocity of the odor in the aeration layer is 0.3-1.5m/s, the pressure drop is 0.15-0.6kPa/m of the filler, and the liquid-gas ratio is 0.5-2.0 kg/kg.
For modification mode c, the velocity of odor in the aeration layer is 1-2.5m/s, and the liquid flow is 1.5-3.8m calculated according to the section of the aeration layer3/(m2 .h)。
Furthermore, the specific surface area of the filler layer in the preposed selection pool is 1-100cm2Per gram, the diameter of 60 percent of filler particles in the filler layer is more than 4mm, and the filling height of all the fillers in the filler layer is 0.5-2 m.
Furthermore, the water inflow of the spraying layer of the preposed selection pool is 1/4-1/3 of the air volume of the odor, and the spraying intensity is 10m3/(m2 .h) The above.
Further, the flow rate of the backflow water in the circulating pipeline of the preposed selection pool is 10% -40% of the water inflow.
Furthermore, the sludge concentration MLSS of the post-positioned anoxic tank is 3000-5000mg/L, the pH is controlled to be 6.5-7.5, the dissolved oxygen is less than or equal to 0.5mg/L, and the HRT is 2.5-10 h. .
Further, the added enriched microorganism with the functions of synchronous denitrification and desulfurization and anaerobic ammonia oxidation is obtained by respectively adding sludge with the functions of synchronous denitrification and desulfurization [ VSS is 10-15g/L, specific sludge activity is 0.8-1.5g TS/(gVSS. d) ] and sludge with the function of anaerobic ammonia oxidation [ VSS is 10-15g/L, specific sludge activity is 1.2-1.9g TN/(gVSS. d) ] into sludge in an anoxic pond, and the adding ratio (volume ratio) of the two kinds of sludge is 2.4-5.2% and 2-4% respectively.
The invention has the following beneficial effects:
1. an external odor treatment device is not needed, and the sewage and odor in the sewage treatment plant can be treated in situ.
2. Solves the problem of insufficient carbon source in the biological denitrification process of sewage.
3. The production of sludge is reduced, and the cost of sludge treatment and disposal is reduced.
Drawings
FIG. 1 is a schematic view of a modification scheme a of the anoxic tank according to the present invention;
FIG. 2 is a schematic view of a modification scheme b of the anoxic tank according to the present invention;
FIG. 3 is a schematic view of a modification scheme c of the anoxic tank according to the present invention;
FIG. 4 is a bar graph of nitrate, sulfide and ammonia nitrogen removal rates at different nitrate concentrations;
FIG. 5 is a bar graph of nitrate, sulfide and ammonia nitrogen removal rates over long term operation.
Wherein: 1. an odor inlet; 2. a fan; 3. a gas distribution layer; 4. an aeration layer; 5. a filler layer; 6. selecting a pool; 7. a spray layer; 8. a water inlet; 9. a purge gas discharge port; 10. a partition plate; 11. an overflow port; 12. a stirrer; 13. a water outlet; 14. a circulating water flow meter; 15. a water pump; 16. an anoxic tank; 17. a humidifier drain port; 18. a humidifier.
Detailed Description
The invention is described in further detail below with reference to the figures and specific examples.
An in-situ sewage and odor treatment device for a sewage treatment plant mainly comprises an odor collecting system, an odor conveying system and an odor treatment system;
the odor collecting system consists of a gas collecting hood, an air pipe and a first fan; the gas collecting hood is used for collecting odor in a sewage treatment plant and conveying the odor to the odor conveying system through the air pipe, and the first fan is connected with the air pipe to extract the odor of the gas collecting hood; the gas collecting hood is made of a stainless steel framework and a sunlight plate or the stainless steel framework and a glass steel plate, and the gas collecting mode adopts an air suction type or a blowing suction type; the air pipes are configured in a main pipe mode, the air speed of the branch pipes is less than or equal to 6m/s, and the air speed of the main pipe is less than or equal to 12 m/s.
The odor delivery system consists of a pipeline and a second fan; the pipeline is connected with an air pipe in the odor collecting system and is used for conveying odor to the odor treatment system, and the second fan is connected with the pipeline and is used for extracting odor in the pipeline;
the odor treatment system is obtained by oxygen deficiency pond normal position transformation, utilizes the baffle to separate the oxygen deficiency pond, divide into leading selection pond area and rearmounted oxygen deficiency pond area, the baffle is the perforated plate, and the overflow mouth is established on baffle upper portion, 1/10-1/3 department that is close to the whole oxygen deficiency pond of water inlet one side is arranged in to the baffle, and the baffle sets up highly to be less than leading selection pond water inlet and rearmounted oxygen deficiency pond delivery port 5-10cm, width and oxygen deficiency pond aequilate. The height of the air distribution layer in the preposed selection tank is 0.2-0.8m higher than the bottom of the tank, and the aeration quantity of the aeration layer is determined according to the air quantity of the odor. The selective specific surface area of the filler layer in the preposed selective pool is 1-100cm2Per gram, the diameter of 60 percent of filler particles in the filler layer is more than 4mm, and the filling height of all the fillers in the filler layer is 0.5-2 m. The water inflow of the spraying layer of the front-mounted selection pool is 1/4-1/3 of the odor air quantity, and the spraying intensity is 10m3/(m2 .h) The above. The flow rate of the backflow water in the circulating pipeline of the preposed selection pool is 10-40% of the water inflow. The preposed selection pool can have three transformation modes which are respectively as follows:
as shown in figure 1, the in-situ sewage and odor treatment device of the sewage treatment plant provided by the invention is a modification scheme a of in-situ reconstruction of an anoxic tank part, the modified anoxic tank is divided into a selection tank 6 and an anoxic tank 16 from left to right, the selection tank 6 and the anoxic tank 16 are separated by a partition plate 10, odor firstly enters a fan 2 through an odor inlet 1, is introduced into an air distribution layer 3 through the fan, and then is exposed into the tank part through an aeration head of an aeration layer 4, sewage in the anaerobic tank flows into a spraying layer through a water inlet 8, water is distributed into the tank part through a spray head, and when wet odor passes through a packing layer, H in the odor2S and NH3Fully dissolved in water to purify gas, and the purified gas is discharged through gasThe water in the selective tank 6 flows into an anoxic tank 16 through a partition plate 10, is fully mixed with the water circulated back in the aerobic tank under the action of a stirrer 12, microorganisms (sludge) with synchronous denitrification, desulfurization and anaerobic ammonia oxidation functions after enrichment are added into the anoxic tank, synchronous denitrification, desulfurization and anaerobic ammonia oxidation reactions are carried out in situ under the action of the sludge with synchronous denitrification, desulfurization and anaerobic ammonia oxidation bacteria in the anoxic tank 16, sulfide and nitrite/nitrate react and oxidize into sulfate or elemental sulfur, and ammonia nitrogen and nitrite/nitrate react to generate N2And the reacted sewage flows into the aerobic tank through the water outlet 13, meanwhile, the effluent flows back in a certain proportion, the flow of the return flow is controlled through the flowmeter 14, and part of the effluent flows back to the water inlet 8 through the water pump 15 for treatment again. The modification mode a is suitable for H in odor needing to be treated and requiring water flow to continuously flow through the filler2S≥500g/m3. For modification a, the velocity of the odor in the aeration layer is 1.5-6m/s, and the retention time is 20-30 s.
As shown in figure 2, the in-situ sewage and odor treatment device of the sewage treatment plant provided by the invention is a modification scheme b of in-situ reconstruction of an anoxic tank part, the modified anoxic tank is divided into a selection tank 6 and an anoxic tank 16 from left to right, the selection tank 6 and the anoxic tank 16 are separated by a partition board 10, odor firstly enters a fan 2 through an odor inlet 1, and is introduced into a humidifier 18 through the fan, in the humidifier, the odor is humidified by water flowing back through a water outlet 13 to remove particles and increase the humidity, and then is introduced into an air distribution layer 3, and is exposed into the tank part through an aeration head of an aeration layer 4, when the humidified odor passes through a packing layer 5, H in the odor2S and NH3Fully dissolve in water to achieve the purpose of purifying gas, the purified gas is discharged through a gas outlet 9, the water in the selection tank 6 flows into an anoxic tank 16 through a partition plate 10, is fully mixed with the water circulating back in the aerobic tank under the action of a stirrer 12, microorganisms (sludge) with synchronous denitrification, desulfurization and anaerobic ammonia oxidation functions after enrichment are added into the anoxic tank, and synchronous denitrification, desulfurization and anaerobic ammonia oxidation reactions are carried out in situ under the action of the sludge with synchronous denitrification and desulfurization and the anaerobic ammonia oxidation bacteria in the anoxic tank 16, and vulcanization is carried outThe substance reacts with nitrite/nitrate to be oxidized into sulfate or elemental sulfur, and the ammonia nitrogen reacts with nitrite/nitrate to generate N2And the reacted water flows into the aerobic tank through a water outlet 13. The transformation mode b is suitable for the mass concentration of the air inlet organic matter at 600-5000mg/m3The odor amount range to be treated is 1000-150000m3H is used as the reference value. For the modification mode b, the velocity of the odor in the aeration layer is 0.3-1.5m/s, the pressure drop is 0.15-0.6kPa/m of the filler, and the liquid-gas ratio is 0.5-2.0 kg/kg.
As shown in figure 3, the in-situ sewage and odor treatment device of the sewage treatment plant provided by the invention is a modification scheme c of in-situ reconstruction of an anoxic tank part, the modified anoxic tank is divided into a selection tank 6 and an anoxic tank 16 from left to right, the selection tank 6 and the anoxic tank 16 are separated by a partition plate 10, sewage in the anaerobic tank flows into the selection tank through a water inlet 8, odor enters a fan 2 through an odor inlet 1, is introduced into an air distribution layer 3 through the fan, is then aerated into the tank body part through an aeration head of an aeration layer 4, the aerated gas is directly dispersed into mixed liquid flowing into the anaerobic tank, the purified gas is discharged through a gas outlet 9, water in the selection tank flows into the anoxic tank 16 through the partition plate 10, is fully mixed with water circulating back in an aerobic tank under the action of a stirrer 12, and microorganisms (sludge) with synchronous desulphurization and anaerobic ammonia oxidation functions are added into the anoxic tank after enrichment, under the action of the sludge with synchronous denitrification and desulfurization and the anaerobic ammonium oxidation bacteria in the anoxic tank 16, the synchronous denitrification and desulfurization and the anaerobic ammonium oxidation reaction are carried out in situ, the sulfide reacts with the nitrite/nitrate to be oxidized into sulfate or elemental sulfur, and the ammonia nitrogen reacts with the nitrite/nitrate to generate N2And the reacted water flows into the aerobic tank through the water outlet 11, meanwhile, the effluent is refluxed in a certain proportion, the reflux flow is controlled through the flowmeter 14, and part of the effluent is refluxed to the water inlet 8 by the water pump 15 for treatment again. Modification mode c is suitable for conveying the odor at the speed of 20m3/(m2 .h) The following. For modification mode c, the velocity of odor in the aeration layer is 1-2.5m/s, and the liquid flow is 1.5-3.8m calculated according to the section of the aeration layer3/(m2 .h)。
The added enriched microorganism with the functions of synchronous denitrification and desulfurization and anaerobic ammonia oxidation is obtained by respectively adding sludge with the functions of synchronous denitrification and desulfurization [ VSS is 10-15g/L, specific sludge activity is 0.8-1.5 gTS/(gVSS. d) ] and sludge with the function of anaerobic ammonia oxidation [ VSS is 10-15g/L, specific sludge activity is 1.2-1.9 gTN/(gVSS. d) ] into sludge in an anoxic pond, and the adding ratios (volume ratios) of the two kinds of sludge are 2.4-5.2% and 2-4% respectively.
The sludge concentration MLSS of the post-positioned anoxic tank is 3000-5000mg/L, the pH is controlled to be 6.5-7.5, the dissolved oxygen is less than or equal to 0.5mg/L, and the HRT is 2.5-10 h.
Example 1
The method is characterized in that a simulation experiment is carried out on sewage and odor treatment of a sewage treatment plant in a laboratory, namely after the odor in the sewage treatment plant is simulated to be dissolved in the sewage containing nitrate, the removal performance of sulfide, nitrate and ammonia nitrogen in the sewage is inspected. The concentration range of the sulfide tested by the experiment is 60mg/L-540mg/L, the concentration range of the nitrate is 10.5mg/L-94.5mg/L, and the concentration range of the ammonia nitrogen is 70-80 mg/L.
When the concentrations of sulfide, nitrate and ammonia nitrogen in the inlet water are respectively 60mg/L, 10.5mg/L and 70.9mg/L, the removal rates of sulfide, nitrate and ammonia nitrogen are respectively 94%, 90% and 13%. As the influent substrate concentration further increased, sulfide, nitrate and ammonia nitrogen removal rates remained above 90%, 89% and 21%, respectively.
Through multiple experiments, the average removal rate of sulfides in each group is 97%, the average removal rate of nitrates is 94%, the average removal rate of ammonia nitrogen is 32%, and the removal effect is good and stable. The removal rate of sulfide, nitrate and ammonia nitrogen in each group is shown in figure 4.
The implementation case adopts an activated sludge method, the pH value is controlled to be 7.0 +/-0.1, and the temperature is controlled to be 25-35 ℃.
Example 2
The method is characterized in that a simulation experiment is carried out on sewage and odor treatment of a sewage treatment plant in a laboratory, namely after the odor in the sewage treatment plant is simulated to be dissolved in the sewage containing nitrate, the removal performance of sulfide, nitrate and ammonia nitrogen in the sewage is inspected. What the experiment tests is that when the concentration of the sulfide in the inlet water is 60mg/L, the concentration of the nitrate is 10.5mg/L and the concentration range of the ammonia nitrogen is 72-78mg/L, the treatment device can remove the sulfide, the nitrate and the ammonia nitrogen for a long time.
Under the condition of low concentration of the sulfide in the inlet water, the multi-day removal efficiency of the sulfide in the outlet water is stabilized to be more than 90 percent, and the average removal rate is 94 percent; the removal rate of nitrate is stabilized above 88% for many days, and the average removal rate is 90%; meanwhile, the method also has a certain effect of removing ammonia nitrogen, and the average removal rate of the ammonia nitrogen is 14%. The experimental result shows that the in-situ sewage and odor treatment device has good and stable removal effect when running under low concentration close to the practical engineering. The results of the experiment are shown in FIG. 5.
The implementation case adopts an activated sludge method, the pH value is controlled to be 7.0 +/-0.1, and the temperature is controlled to be 25-35 ℃.
Through carrying out the simulation experiment to sewage treatment plant sewage and odor treatment in the laboratory, the experimental result shows, no matter under the intake water sulphide, the nitrate of high concentration condition, or press close to the intake water sulphide, the nitrate condition of actual engineering low concentration, the effect of getting rid of sulphide, nitrate in sewage is all better, also has certain removal effect to the ammonia nitrogen simultaneously, shows that sewage treatment plant normal position sewage and odor treatment device can realize the synchronous processing of the sewage that contains the nitrate and contain sulphur and contain ammonia odor.
The above-described embodiments are intended to illustrate rather than to limit the invention, and any modifications and variations of the present invention are within the spirit of the invention and the scope of the appended claims.
Claims (10)
1. An in-situ sewage and odor treatment device of a sewage treatment plant is characterized by mainly comprising an odor collecting system, an odor conveying system and an odor treatment system;
the odor collecting system consists of a gas collecting hood, an air pipe and a first fan; the gas collecting hood is used for collecting odor in a sewage treatment plant and conveying the odor to the odor conveying system through the air pipe, and the first fan is connected with the air pipe to extract the odor of the gas collecting hood;
the odor delivery system consists of a pipeline and a second fan; the pipeline is connected with an air pipe in the odor collecting system and is used for conveying odor to the odor treatment system, and the second fan is connected with the pipeline and is used for extracting odor in the pipeline;
the odor treatment system is obtained by oxygen deficiency pond normal position transformation, utilizes the baffle to separate the oxygen deficiency pond, divide into leading selection pond area and rearmounted oxygen deficiency pond area, the baffle is the perforated plate, and the overflow mouth is established on baffle upper portion, and leading selection pond can have three kinds of transformation modes, is respectively:
a. the preposed selection tank consists of a water pump, a circulating pipeline and a tank body, wherein the tank body is divided into an air distribution layer, an aeration layer, a packing layer and a spraying layer from bottom to top, the air distribution layer is provided with a gas inlet, and the spraying layer is provided with a water inlet and a spraying device; the gas inlet of the gas distribution layer is connected with a pipeline in the odor conveying system and is used for conveying odor to the preposed selection pool; the circulating pipeline connects a water inlet of the front-mounted selection pool with a water outlet of the rear-mounted anoxic pool through a water pump to circulate water in the anoxic pool;
b. the preposed selection tank consists of a humidifier, a circulating pipeline, a water pump and a tank body, wherein the tank body is divided into an air distribution layer, an aeration layer and a packing layer from bottom to top, and the top of the tank body is provided with a water inlet; the humidifier is connected with a pipeline in the odor delivery system to humidify odor, and the air distribution layer is provided with an air inlet which is connected with the humidifier and used for delivering the humidified odor to a preposed selection pool; the circulating pipeline connects the humidifier of the front selection pool with the water outlet of the rear anoxic pool through a water pump and is used for humidifying odor;
c. the preposed selection tank consists of a water pump, a circulating pipeline and a tank body, wherein the tank body is divided into an air distribution layer and an aeration layer from bottom to top, and the top of the tank body is provided with a water inlet; the circulating pipeline connects a water inlet of the front-mounted selection pool with a water outlet of the rear-mounted anoxic pool through a water pump to circulate water in the anoxic pool;
a. b, water in the front selection pool in the three schemes of b and c flows into the rear anoxic pool through the partition plate, and when the water level is overhigh, the water can flow into the rear anoxic pool through the overflow port; the rear anoxic pond area device is not changed, and microorganisms with the functions of synchronous denitrification and desulfurization and anaerobic ammonia oxidation after enrichment are added into the anoxic pond.
2. The in-situ sewage and odor treatment apparatus of sewage treatment plant according to claim 1, wherein the modification manner a is adapted to the odor H to be treated by the water flow continuously flowing through the filler2S≥500g/m3(ii) a The transformation mode b is suitable for the mass concentration of the air inlet organic matter at 600-5000mg/m3The odor amount range to be treated is 1000-150000m3H; modification mode c is suitable for conveying the odor at the speed of 20m3/(m2 .h) The following.
3. The in-situ sewage and odor treatment device of a sewage treatment plant according to claim 1, wherein the gas collecting hood is made of stainless steel framework + sunlight plate or stainless steel framework + glass steel plate, and the gas collecting mode is suction type or blowing suction type; the air pipes are configured in a main pipe mode, the air speed of the branch pipes is less than or equal to 6m/s, and the air speed of the main pipe is less than or equal to 12 m/s.
4. The in-situ sewage and odor treatment device of a sewage treatment plant according to claim 1, wherein the partition is disposed at 1/10-1/3 of the whole anoxic tank near one side of the water inlet, the height of the partition is 5-10cm lower than the water inlet of the front selection tank and the water outlet of the rear anoxic tank, and the width of the partition is equal to the width of the anoxic tank.
5. The in-situ sewage and odor treatment apparatus of sewage treatment plant according to claim 1, wherein the height of the air distribution layer in the front selected tank is 0.2-0.8m higher than the bottom of the tank, and the aeration rate of the aeration layer is determined according to the air volume of the odor.
For modification a, the velocity of the odor in the aeration layer is 1.5-6m/s, and the retention time is 20-30 s.
For the modification mode b, the velocity of the odor in the aeration layer is 0.3-1.5m/s, the pressure drop is 0.15-0.6kPa/m of the filler, and the liquid-gas ratio is 0.5-2.0 kg/kg.
For modification mode c, the velocity of odor in the aeration layer is 1-2.5m/s, and the liquid flow is 1.5-3.8m calculated according to the section of the aeration layer3/(m2 .h)。
6. The in situ sewage and odor treatment apparatus of sewage treatment plant according to claim 1, wherein the packing layer in the front selection tank has a selected specific surface area of 1-100cm2Per gram, the diameter of 60 percent of filler particles in the filler layer is more than 4mm, and the filling height of all the fillers in the filler layer is 0.5-2 m.
7. The in-situ sewage and odor treatment apparatus of sewage treatment plant according to claim 1, wherein the water inflow of the spray layer of the front selection tank is 1/4-1/3 of the air volume of the odor, and the spray intensity is 10m3/(m2 .h) The above.
8. The in-situ sewage and odor treatment apparatus of a sewage treatment plant according to claim 1 wherein a flow rate of a recirculation water in a circulation pipe of the pre-positioned option tank is 10% to 40% of a flow rate of a water inflow.
9. The in-situ sewage and odor treatment device of a sewage treatment plant according to claim 1, wherein the sludge concentration MLSS of the post-positioned anoxic tank is 3000-5000mg/L, the pH is controlled to be 6.5-7.5, the dissolved oxygen is less than or equal to 0.5mg/L, and the HRT is 2.5-10 h.
10. The apparatus for treating in-situ sewage and odor of sewage treatment plant according to claim 1, wherein the added enriched microorganisms having simultaneous denitrification and desulfurization and anammox functions are obtained by adding sludge having simultaneous denitrification and desulfurization [ VSS is 10-15g/L, specific sludge activity is 0.8-1.5g TS/(gVSS. d) ] and sludge having anammox function [ VSS is 10-15g/L, specific sludge activity is 1.2-1.9g TN/(gVSS. d) ] to the anoxic pond sludge, and the adding ratio (volume ratio) of the two kinds of sludge is 2.4-5.2% and 2-4% respectively.
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| CN212127697U (en) * | 2020-01-16 | 2020-12-11 | 浙江工商大学 | In-situ sewage and odor treatment device for sewage treatment plant |
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| CN108325375A (en) * | 2018-04-15 | 2018-07-27 | 重庆水务集团股份有限公司 | A kind of sewage treatment plant's aerobic activated sludge synchronization aeration deodorizing technique |
| CN110639349A (en) * | 2018-06-27 | 2020-01-03 | 郑州大学 | Chemical coupling biological synchronous waste gas desulfurization, deamination and sulfur combination recycling process |
| CN212127697U (en) * | 2020-01-16 | 2020-12-11 | 浙江工商大学 | In-situ sewage and odor treatment device for sewage treatment plant |
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