CN110615534A - Sulfur-iron autotrophic denitrification device and application thereof - Google Patents
Sulfur-iron autotrophic denitrification device and application thereof Download PDFInfo
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- CN110615534A CN110615534A CN201911043094.XA CN201911043094A CN110615534A CN 110615534 A CN110615534 A CN 110615534A CN 201911043094 A CN201911043094 A CN 201911043094A CN 110615534 A CN110615534 A CN 110615534A
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- 230000001651 autotrophic effect Effects 0.000 title claims abstract description 70
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 title claims abstract description 44
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims abstract description 291
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 129
- 229910052742 iron Inorganic materials 0.000 claims abstract description 104
- 239000000945 filler Substances 0.000 claims abstract description 93
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 52
- 238000012856 packing Methods 0.000 claims abstract description 45
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 44
- 239000011593 sulfur Substances 0.000 claims abstract description 44
- 239000010865 sewage Substances 0.000 claims abstract description 38
- 239000002245 particle Substances 0.000 claims abstract description 37
- 239000004575 stone Substances 0.000 claims abstract description 18
- 238000009826 distribution Methods 0.000 claims abstract description 11
- 238000005273 aeration Methods 0.000 claims description 78
- 238000004062 sedimentation Methods 0.000 claims description 29
- 238000005276 aerator Methods 0.000 claims description 26
- 239000012528 membrane Substances 0.000 claims description 26
- 239000010802 sludge Substances 0.000 claims description 20
- 239000005864 Sulphur Substances 0.000 claims description 16
- 230000014759 maintenance of location Effects 0.000 claims description 12
- 239000000463 material Substances 0.000 claims description 11
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 claims description 11
- 229910052683 pyrite Inorganic materials 0.000 claims description 11
- 239000011028 pyrite Substances 0.000 claims description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 9
- 229910052760 oxygen Inorganic materials 0.000 claims description 9
- 239000001301 oxygen Substances 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- 238000004065 wastewater treatment Methods 0.000 claims 3
- 239000011259 mixed solution Substances 0.000 claims 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 abstract description 66
- 229910052698 phosphorus Inorganic materials 0.000 abstract description 66
- 239000011574 phosphorus Substances 0.000 abstract description 66
- 230000000694 effects Effects 0.000 abstract description 33
- 239000000126 substance Substances 0.000 abstract description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 98
- 238000000034 method Methods 0.000 description 86
- 230000008569 process Effects 0.000 description 83
- 229910052757 nitrogen Inorganic materials 0.000 description 49
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 31
- 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 11
- 239000003344 environmental pollutant Substances 0.000 description 10
- 231100000719 pollutant Toxicity 0.000 description 10
- 229910019142 PO4 Inorganic materials 0.000 description 7
- 238000012360 testing method Methods 0.000 description 6
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 5
- 230000015556 catabolic process Effects 0.000 description 5
- 238000006731 degradation reaction Methods 0.000 description 5
- 230000000593 degrading effect Effects 0.000 description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 5
- 239000010452 phosphate Substances 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000008187 granular material Substances 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 239000005416 organic matter Substances 0.000 description 3
- 238000006213 oxygenation reaction Methods 0.000 description 3
- 238000002798 spectrophotometry method Methods 0.000 description 3
- 239000004912 1,5-cyclooctadiene Substances 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 2
- 239000002033 PVDF binder Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- -1 iron ions Chemical class 0.000 description 2
- 238000006396 nitration reaction Methods 0.000 description 2
- 230000001546 nitrifying effect Effects 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 2
- KMUONIBRACKNSN-UHFFFAOYSA-N potassium dichromate Chemical compound [K+].[K+].[O-][Cr](=O)(=O)O[Cr]([O-])(=O)=O KMUONIBRACKNSN-UHFFFAOYSA-N 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 241000605118 Thiobacillus Species 0.000 description 1
- 241001509286 Thiobacillus denitrificans Species 0.000 description 1
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 description 1
- 229940010552 ammonium molybdate Drugs 0.000 description 1
- 235000018660 ammonium molybdate Nutrition 0.000 description 1
- 239000011609 ammonium molybdate Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910001567 cementite Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000001112 coagulating effect Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000012136 culture method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 239000010840 domestic wastewater Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910000398 iron phosphate Inorganic materials 0.000 description 1
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 description 1
- 229910000399 iron(III) phosphate Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- USHAGKDGDHPEEY-UHFFFAOYSA-L potassium persulfate Chemical compound [K+].[K+].[O-]S(=O)(=O)OOS([O-])(=O)=O USHAGKDGDHPEEY-UHFFFAOYSA-L 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000003403 water pollutant Substances 0.000 description 1
Classifications
-
- 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
- C02F3/302—Nitrification and denitrification treatment
-
- 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
- C02F2101/105—Phosphorus compounds
-
- 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
Landscapes
- 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
The invention discloses a sulfur-iron autotrophic denitrification device and application thereof, and belongs to the technical field of sewage treatment. The invention designs a sulfur-iron filler with discontinuously arranged and replaceable structures, wherein the sulfur-iron filler layer comprises sulfur particles and an iron filler layer, the iron filler layer is provided with a bearing layer at the upper part and the lower part, the middle part is provided with a screen, and the bearing layer is provided with water distribution holes; the iron filler layer is formed by placing iron chips in a screen mesh, and iron filler replacement openings are further formed in the side face of the iron filler layer. According to the invention, the iron chips are placed in the screen and are arranged in a multi-stage sulfur-iron arrangement mode, so that the effect of iron chemical phosphorus removal is fully exerted, and when the iron chips are consumed and cannot meet the phosphorus removal requirement, the iron filler can be replaced through the replacement opening, so that the iron filler is convenient and rapid, and the problems of hardening and replacement of the filler are effectively avoided. The function of adding stone particles in the sulfur packing layer is to distribute water uniformly.
Description
Technical Field
The invention relates to a sulfur-iron autotrophic denitrification device and application thereof, belonging to the technical field of sewage treatment.
Background
At present, the national urban sewage treatment plant generally executes the primary A discharge standard (hereinafter referred to as the primary A standard) in the pollutant discharge standard of the urban sewage treatment plant (GB18918-2002), and the indexes of main pollutants such as effluent COD, total nitrogen, ammonia nitrogen, total phosphorus and the like respectively do not exceed 50mg/L, 15mg/L, 5mg/L and 0.5 mg/L. In 2018, 6 and 1, the emission limits of main water pollutants of urban sewage treatment plants in Taihu lake regions and key industrial industries (DB 32/1072-2018) are issued, and the urban sewage treatment plants in Taihu lake regions in Jiangsu province are required to be standardized again on the basis of the first-level A standard, wherein the emission standards of the main pollutants such as COD, total nitrogen, ammonia nitrogen, total phosphorus and the like in the effluent of the urban sewage treatment plants in the first-level and second-level protection areas of the Taihu lake basin are respectively improved to 40mg/L, 10mg/L, 3mg/L and 0.3mg/L, and the difficulty in sewage treatment is remarkably improved. In order to realize the standard discharge of effluent, most sewage treatment plants need to ensure enough hydraulic retention time in a biochemical tank, wherein the hydraulic retention time of anaerobic, anoxic and aerobic sections is generally not less than 1h, 3h and 8h respectively, and in order to realize the deep removal of nitrogen and phosphorus, the effluent of the biochemical tank generally needs to be provided with a denitrification filter tank for deep denitrification, coagulating sedimentation filtration or air flotation process to realize deep phosphorus removal, so that the process flow of sewage treatment is overlong, the occupied area is large, the adding amount of carbon source and phosphorus removal agent is large, the operation cost is increased, and the low-carbon discharge and the circular economy development mode are not facilitated. The mixed layer is directly formed by iron filings and sulfur in the prior art, so that the iron filings and sulfur particles are easy to harden, short flow is caused, and nitrogen and phosphorus removal is not facilitated.
Disclosure of Invention
In order to solve the problems, the invention designs the ferro-sulphur filler with the discontinuous arrangement and the replaceable structure, compared with a mixed layer formed by iron chips and sulphur directly and a filler structure in which the added iron chips are placed in the sulphur filler in a plastic ball wrapping mode, the ferro-sulphur filler with the special structure has the characteristics of difficult hardening and easy replacement. The S-Fe filter is provided with a packing layer, and the packing layer comprises stone particles and a pyrite packing layer from bottom to top; the sulphur and iron fillers are arranged in an intermittent arrangement. The S-Fe filter tank is used for simultaneously removing nitrogen and phosphorus. Scrap iron and sulfur directly form a mixed layer, so that the scrap iron and sulfur particles are easily hardened, short flow is caused, and removal of nitrogen and phosphorus is not facilitated. Although the packing structure which is wrapped by plastic balls and placed in the sulfur packing can avoid the hardening condition, the structure is not beneficial to the replacement of the iron packing. The iron chips are placed in the screen and are arranged in a multi-stage sulfur-iron arrangement mode, so that the effect of chemical phosphorus removal of iron is fully exerted, and when the iron chips are consumed and cannot meet the phosphorus removal requirement, the iron filler can be replaced through the replacement opening, so that the iron filler is convenient and quick, and the problems of hardening and replacement of the filler are effectively avoided. The function of adding stone particles in the sulfur packing layer is to distribute water uniformly.
The invention provides a sulfur-iron autotrophic denitrification device, wherein a sulfur-iron filler layer comprises sulfur particles and an iron filler layer, the iron filler layer is provided with a bearing layer at the upper part and the lower part, a screen is arranged in the middle, and water distribution holes are arranged in the bearing layer; the iron filler layer is formed by placing iron chips in a screen mesh, and iron filler replacement openings are further formed in the side face of the iron filler layer. The device is an upflow filter, the sulfur-iron autotrophic denitrification filter is provided with a packing layer, and stone grains and the sulfur-iron packing layer are distributed on the packing layer from bottom to top.
In one embodiment of the invention, the sulfur particles in the sulfur-iron filler layer and the iron filler layer are arranged in a discontinuous arrangement; the dosage ratio of the sulfur to the iron is (1-5): 1. according to the invention, the iron chips are placed in the screen and are arranged in a multi-stage sulfur-iron arrangement mode, so that the effect of chemical phosphorus removal of iron can be fully exerted, and when the iron chips are consumed and cannot meet the phosphorus removal requirement, the iron filler can be replaced through the replacement opening, so that the iron filler is convenient and rapid, and the problems of hardening and replacement of the filler are effectively avoided.
The second purpose of the invention is to provide a sewage treatment device, which comprises the sulfur-iron autotrophic denitrification device and adopts the S-Fe autotrophic denitrification device to carry out advanced treatment on sewage.
A third object of the invention is to provide an application of the above device in sewage treatment.
The fourth purpose of the invention is to provide a sewage treatment device, which comprises an aeration tank, a sedimentation tank and the sulfur-iron autotrophic denitrification filter tank; the aeration tank comprises a water inlet, a water outlet and an aeration device; the water inlet is positioned at the lower part of the aeration tank and is connected with a water inlet pump; the aeration device is positioned at the bottom of the aeration tank and comprises a fan, an aeration pipe and an aerator, wherein the fan is positioned outside the aeration tank and is connected with the aerator through the aeration pipe; the sedimentation tank is in an inverted cone shape and comprises a flow guide pipe, a water outlet weir and a mud collecting hopper; the guide pipe is positioned in the center of the sedimentation tank and is connected with the water outlet of the aeration tank through a guide pipe; the effluent weir is positioned at the top of the sedimentation tank; the sludge collecting hopper is positioned at the bottom of the sedimentation tank; the bottom of the sedimentation tank is also provided with a sludge discharge port which is connected with the aeration tank through a sludge reflux pump; the sedimentation tank is connected with the sulfur-iron autotrophic denitrification filter tank through a secondary lift pump.
In one embodiment of the present invention, the aerator is provided with 2 or more, and functions to supply oxygen as an electron acceptor to the nitrifying bacteria and the aerobic organic matter degrading bacteria.
The fifth purpose of the invention is to provide the application of the device in sewage treatment, wherein the specific parameters of the application are as follows: the effective volumes of the aeration tank, the sedimentation tank and the S-Fe filter tank are respectively as follows: 24L, 9L, 21L and 6L; the Hydraulic Retention Time (HRT) of the aeration tank is 6-8h, the Sludge age (SRT) is 10-15d, the Dissolved Oxygen (DO) range is 2-4mg/L, and the suspended solid concentration (MLSS) of the mixed liquid is 4000-5000 mg/L; HRT of the sedimentation tank is 2-3h, and surface hydraulic load is 1.0-1.2m3/(m2H); the diameter of the S-Fe autotrophic denitrification filter tank is 10cm, the effective height is 77cm, and the empty bed H isRT is 1.5-2h, the grain size of filler sulfur is 2-4 mm, and the porosity is 50%.
The sixth purpose of the invention is to provide a sewage treatment device, which is sequentially provided with an MBR tank and the sulfur-iron autotrophic denitrification filter tank; the ferro-sulphur autotrophic denitrification filter tank is connected with an MBR water outlet pipe through an MBR water outlet pump; the MBR tank is connected with a water inlet pump through a water inlet pipe; the MBR tank comprises a membrane component and an aeration device; an aeration device is arranged below the MBR tank, and comprises an aeration pipe, an aerator and a fan; the upper part of the aeration pipe is connected with an aerator, and the lower part of the aeration pipe is connected with a fan; the membrane module is arranged right above the aeration device, and the MBR water outlet pump is connected with the membrane module through an MBR water outlet pipe.
In one embodiment of the invention, the membrane material in the membrane module is PVDF, the pore diameter is 0.01 micron, and the function is to perform sufficient mud-water separation.
In one embodiment of the invention, the number of the membrane modules is the same as that of the aerators, one aerator is arranged right below each membrane module, and a water outlet pipe is arranged right above each membrane module. The effect of this arrangement is to ensure that a uniform water outlet can be achieved per unit of membrane module.
The seventh purpose of the present invention is to provide an application of the above device in sewage treatment, wherein the specific parameter conditions of the application are as follows: the material of the reactor is acrylic plates, HRT of the MBR tank is 4-5h, Sludge Retention Time (SRT) is 15-20d, DO (Dissolved oxygen) range is 4-6mg/L, and MLSS (mixed suspended solid) concentration is 8000-9000 mg/L. The diameter of the S-Fe autotrophic denitrification filter tank is 10cm, the HRT of an empty bed is 1.5-2h, the particle size of filler sulfur is 2-4 mm, and the porosity is 50%.
The eighth purpose of the invention is to provide a sewage treatment device, which is sequentially provided with a BAF filter tank, an intermediate water tank and the ferro-sulphur autotrophic denitrification filter tank; the BAF filter tank is connected with a water inlet pump through a water inlet pipe; the BAF filter tank comprises an aeration device and filler, wherein the aeration device is arranged below the BAF filter tank and comprises an aeration pipe, an aerator and a fan; the upper part of the aeration pipe is connected with an aerator, and the lower part of the aeration pipe is connected with a fan; the filler of the BAF filter tank consists of cobblestones and stone particle filter materials, the effective diameter is 16cm, and the heights are 10cm and 120cm respectively; the S-Fe filter tank water inlet pump is connected with the BAF water outlet pipe through the middle water tank; the sulfur-iron autotrophic denitrification filter is connected with an S-Fe filter water inlet pump through an S-Fe filter water inlet pipe.
The ninth purpose of the present invention is to provide an application of the above device in sewage treatment, wherein the specific parameters of the application are as follows: the reactor is made of an acrylic plate, the combined process mainly comprises a BAF filter tank, an intermediate water tank and an S-Fe filter tank, and the effective volumes are respectively as follows: 24L, 3L and 6L. The HRT of the hollow bed of the BAF filter is 6-8h, the filtering speed is 0.11-0.15m/h, the grain diameter of the stone grain filter material is 3-5mm, and the porosity is 60%; the HRT of the empty bed of the S-Fe autotrophic denitrification filter is 1.5-2h, the filtering speed is 0.289-0.385m/h, the grain diameter of the filler sulfur is 2-4 mm, and the porosity is 50%.
The invention has the beneficial effects that:
(1) in the prior art, a mixed layer is directly formed by iron chips and sulfur, so that the iron chips and sulfur particles are easy to harden, short flow is caused, and removal of nitrogen and phosphorus is not facilitated; although the packing structure which is wrapped by plastic balls and placed in the sulfur packing can avoid the hardening condition, the structure is not beneficial to the replacement of the iron packing. The iron filings are placed in the screen mesh and are arranged in a multi-stage sulfur-iron arrangement mode, so that the iron chemical dephosphorization effect is fully exerted, when the iron filings are consumed and the dephosphorization requirement cannot be met, the iron fillings can be replaced through the replacement openings, the operation is convenient and rapid, and the problems of hardening and replacement of the fillings are effectively avoided.
(2) The invention adopts the CAS/S-Fe autotrophic denitrification combined process to carry out experiments on raw water of the sewage treatment plant, thereby realizing better pollutant deep removal effect. In the combined process, the CAS process section realizes the complete nitrification of ammonia nitrogen and the removal of COD; and the S-Fe autotrophic denitrification realizes the removal of nitrate nitrogen and phosphate, and completes the denitrification and dephosphorization process. Experimental results show that indexes of main pollutants such as COD, total nitrogen, ammonia nitrogen, total phosphorus and the like in the effluent of the combined process are respectively lower than 40mg/L, 5mg/L, 1.2mg/L and 0.3mg/L, so that a high-standard discharge target is realized, and the new standard improvement and transformation requirements can be met. In addition, the HRT of the CAS process section is only 8h, the arrangement of anaerobic and anoxic process sections in the traditional A2O process is omitted, and the floor area is saved by more than 45%; and because no carbon source and phosphorus removal agent are added, the operation cost can be saved by about 25 percent, and the sewage treatment cost is effectively reduced.
(3) According to the invention, the MBR/S-Fe autotrophic denitrification combined process is adopted to test the actual inlet water of the sewage treatment plant, and the good COD and nitrogen and phosphorus removal effects are realized under the conditions of short process flow and low HRT. The MBR process section realizes COD removal and ammonia nitrogen nitration; and the S-Fe autotrophic denitrification realizes the removal of nitrate nitrogen and phosphate, and completes the denitrification and dephosphorization process. Experimental results show that indexes of main pollutants such as COD, total nitrogen, ammonia nitrogen, total phosphorus and the like in the effluent of the combined process are respectively lower than 40mg/L, 5mg/L, 2mg/L and 0.3mg/L, and the high-standard discharge target is realized. In addition, the hydraulic retention time of the MBR/S-Fe autotrophic denitrification combined process is only 7h, under the condition of achieving the same treatment effect, the hydraulic retention time is shortened by more than 50% compared with that of the traditional sewage treatment process, the reduction of the hydraulic retention time means the saving of the floor area, the vertical space is fully utilized by the upflow S-Fe filter tank, the comprehensive floor area of the combined process can be saved by about 60% compared with that of the traditional process, and the combined process is a novel efficient sewage treatment technology with great application prospect.
(4) The invention combines BAF and S-Fe autotrophic denitrification process to form a complementary combined process, and takes the effluent of the actual primary sedimentation tank of the sewage treatment plant as the inlet water of the reactor for test, thereby realizing good COD and nitrogen and phosphorus removal effect. The BAF process section realizes removal of COD and nitration of ammonia nitrogen; the S-Fe autotrophic denitrification realizes the removal of nitrate nitrogen and phosphate, and completes the process of nitrogen and phosphorus removal. Experimental results show that indexes of main pollutants such as COD, TN, NH3-N, TP and the like in effluent of the combined process are respectively lower than 40mg/L, 6mg/L, 1.5mg/L and 0.3mg/L, so that the deep removal target of the pollutants is realized, and the new upgrading and transformation requirements can be met. In addition, the hydraulic retention time of the BAF/S-Fe autotrophic denitrification combined process is only 10 hours, under the condition of achieving the same treatment effect, the hydraulic retention time is shortened by more than 30 percent compared with the traditional sewage treatment process by an activated sludge method, the reduction of the hydraulic retention time means the saving of floor area, the BAF and the S-Fe autotrophic denitrification are of upflow filter tank structures, the vertical space can be fully utilized, the comprehensive floor area of the combined process can be saved by about 70 percent compared with the traditional process, and the BAF/S-Fe autotrophic denitrification combined process is a novel efficient sewage treatment technology with great application prospect.
Drawings
Fig. 1 is a schematic structural diagram of a pyrite filler of the present invention, wherein, 1: sulfur particles; 2: water distribution holes; 3: a support layer; 4: replacing the opening with iron filler; 5: scrap iron.
FIG. 2 is a CAS/S-Fe autotrophic denitrification process flow of the present invention, 1: a water inlet pump; 2: a fan; 3: an aeration tank; 4: an aeration pipe; 5: an aerator; 6: a sludge reflux pump; 7: a sedimentation tank; 8: a secondary lift pump; 9: stone particles; 10: a sulfur filler layer; 11: water distribution holes; 12: a support layer; 13: replacing the opening with iron filler; 14: scrap iron; 15: an S-Fe filter; 16: a flow guide pipe; 17: an effluent weir; 18: a mud collection hopper.
Figure 3 shows the effect of the CAS process stage on total nitrogen removal.
FIG. 4 shows the effect of CAS process on ammonia nitrogen removal.
FIG. 5 shows the effect of the CAS process stage on total phosphorus removal.
FIG. 6 shows the effect of the CAS process stage on COD removal.
FIG. 7 shows the effect of the combined process on the removal of total nitrogen, ammonia nitrogen, total phosphorus and COD.
FIG. 8 is a process flow of MBR/S-Fe autotrophic denitrification process of the present invention, wherein 1: a water inlet pump; 2: a fan; 3: an aeration pipe; 4: an aerator; 5: a membrane module; 6: an MBR water outlet pipe; 7: an MBR tank; 8: an MBR water outlet pump; 9: stone particles; 10: sulfur particles; 11: water distribution holes; 12: a support layer; 13: replacing the opening with iron filler; 14: scrap iron; 15: a sulfur-iron autotrophic denitrification filter.
FIG. 9 shows the effect of MBR process stage on COD removal.
Figure 10 shows the effect of the MBR process stage on total nitrogen removal.
FIG. 11 shows the effect of MBR process stage on ammonia nitrogen removal.
Figure 12 shows the effect of the MBR process stage on total phosphorus removal.
FIG. 13 shows the effect of the combined process on the removal of total nitrogen, ammonia nitrogen, total phosphorus and COD.
FIG. 14 is a technological process of BAF/S-Fe autotrophic denitrification double filtration tank of the present invention, 1: a water inlet pump; 2: a water inlet pipe; 3: a BAF filter tank; 4: a BAF water outlet pipe; 5: a fan; 6: an aeration pipe; 7: an aerator; 8: cobblestones; 9: a stone particle filter material; 10: a middle water tank; 11: an S-Fe filter tank water inlet pump; 12: sand grains; 13: sulfur particles; 14: water distribution holes; 15: a support layer; 16: replacing the opening with iron filler; 17: scrap iron; 18: and (4) an S-Fe filter.
FIG. 15 shows the effect of BAF process stage on COD removal;
FIG. 16 shows the effect of a BAF process stage on total nitrogen removal;
FIG. 17 shows the effect of BAF process on ammonia nitrogen removal;
FIG. 18 shows the effect of the BAF process stage on total phosphorus removal;
FIG. 19 shows the effect of the combined process on the removal of total nitrogen, ammonia nitrogen, total phosphorus and COD.
Detailed Description
The following description of the preferred embodiments of the present invention is provided for the purpose of better illustrating the invention and is not intended to limit the invention thereto.
The total nitrogen is measured by alkaline potassium persulfate digestion ultraviolet spectrophotometry (HJ 636-2012); the total phosphorus is measured by ammonium molybdate spectrophotometry (GB/T11893-1989); ammonia nitrogen is measured by adopting a nano reagent spectrophotometry (HJ 535-2009); chemical oxygen demand COD is determined by the potassium dichromate method (GB 11914-1989).
Example 1: sulphur iron packing layer
The structure of the pyrite filler is shown in figure 1, the pyrite filler layer comprises sulfur particles 1 and an iron filler layer, the iron filler layer is provided with a supporting layer 3 at the upper part and the lower part, the middle part is provided with a screen, and the supporting layer is provided with water distribution holes 2; the iron filler layer is formed by placing iron chips 5 in a screen mesh, and iron filler replacement openings 4 are further formed in the side face of the iron filler layer. The iron chips 5 are placed in the screen and are arranged in a multi-stage sulfur-iron arrangement mode, so that the effect of iron chemical dephosphorization is fully exerted, when the iron chips are consumed and the dephosphorization requirement cannot be met, the iron filler can be replaced through the replacement opening, the operation is convenient and fast, and the problems of hardening and replacement of the filler are effectively avoided. The filler sulfur has a particle size of 2-4 mm, a porosity of 50% and a sulfur-iron dosage ratio of 2: 1.
Example 2: CAS/S-Fe autotrophic denitrification process
As shown in fig. 2, the reactor is made of acrylic plates, and the combined process comprises an aeration tank 3, a sedimentation tank 7 and a sulfur-iron autotrophic denitrification filter 15; the aeration tank 3 comprises a water inlet, a water outlet and an aeration device; the water inlet is positioned at the lower part of the aeration tank and is connected with a water inlet pump 1; the aeration device is positioned at the bottom of the aeration tank 3 and comprises a fan 2, an aeration pipe 4 and an aerator 5, wherein the fan 2 is positioned outside the aeration tank 3 and is connected with the aerator 5 through the aeration pipe 4.
The sedimentation tank 7 is in an inverted cone shape, and the sedimentation tank 7 comprises a flow guide pipe 16, an effluent weir 17 and a mud collection hopper 18; the draft tube 16 is positioned in the center of the sedimentation tank 7 and is connected with the water outlet of the aeration tank 3 through a guide tube; the effluent weir 17 is positioned at the top of the sedimentation tank 7; the sludge collecting hopper 18 is positioned at the bottom of the sedimentation tank 7; the bottom of the sedimentation tank is also provided with a sludge discharge port which is connected with the aeration tank 3 through a sludge reflux pump 6; the sedimentation tank 7 is connected with a sulfur-iron autotrophic denitrification filter 15 through a secondary lift pump 8.
The sulfur-iron autotrophic denitrification filter 15 is provided with a packing layer, and the packing layer comprises stone grains 9 and a sulfur-iron packing layer from bottom to top; the sulfur iron packing layer comprises sulfur particles 10 and an iron packing layer, the iron packing layer is provided with a bearing layer 12 at the upper part and the lower part, the middle part is provided with a screen, and the bearing layer is provided with water distribution holes 11; iron filings 14 are placed in the iron filler layer, and an iron filler replacement opening 13 is also arranged on the side surface of the iron filler layer; the sulfur granules 10 and the iron packing layer are arranged in a discontinuous arrangement. The iron chips are placed in the screen and are arranged in a multi-stage sulfur-iron arrangement mode, so that the effect of iron chemical dephosphorization is favorably and fully exerted, and when the iron chips are consumed and the dephosphorization requirement cannot be met, the iron filler can be replaced through the replacement opening, the method is convenient and fast, and the problems of hardening and replacement of the filler are effectively avoided.
The hydraulic retention time of the aeration tank is 6-8h, the sludge age is 10-15d, and the dissolved oxygen range is 2-4mg/L, the concentration of suspended solid in the mixed liquid is 4000-5000 mg/L. HRT of the sedimentation tank is 2-3h, and surface hydraulic load is 1.0-1.2m3/(m2H). The HRT of the empty bed of the S-Fe autotrophic denitrification filter is 1.5-2 h.
As shown in the figures 2-5, the test influent is domestic sewage, the total nitrogen concentration ranges from 20.2 mg/L to 47.1mg/L, and the average value is 33.6 mg/L; most of the total nitrogen components of the inlet water are ammonia nitrogen, and the average concentration is 26.9 mg/L. The COD of the inlet water was 198-442mg/L, and the average value was 298 mg/L. The total phosphorus concentration of the inlet water is 1.29-5.4mg/L, and the average value is 3.29 mg/L. The CAS process section provides an electron acceptor for aerobic microorganisms through aeration and oxygenation to realize degradation of ammonia nitrogen and organic matters. The average COD concentration of effluent of the CAS process section is 27.8mg/L, and the average removal rate reaches 91.7 percent; the ammonia nitrogen concentration is stabilized below 3mg/L, the average value is 0.85mg/L, and the average removal rate is 96.8%. Because no anaerobic and anoxic functional areas are arranged, the total nitrogen and total phosphorus removal effect is slightly poor, the total nitrogen and total phosphorus concentration of effluent of the CAS process section are respectively 19.8mg/L and 2.04mg/L, and the average removal rate is respectively 29 percent and 40.4 percent.
The CAS process removes most COD in the inlet water and degrades ammonia nitrogen into nitrate nitrogen. The inlet water of the S-Fe autotrophic denitrification process section has the characteristics of low organic matter content, high nitrate nitrogen content and high phosphate content, and the deep removal of nitrogen and phosphorus is realized through S autotrophic nitrogen removal and iron chemical phosphorus removal. Autotrophic thiobacillus denitrificans exists in an activated sludge system, but has very limited effect in a general biochemical system due to low relative abundance. By an enrichment culture method, denitrifying thiobacillus is enriched on the surface of the flaky sulfur granules to form an autotrophic denitrification biomembrane, and nitrate nitrogen is used as an electron acceptor and elemental sulfur is used as an electron donor to realize the removal of nitrogen. As shown in FIG. 6, the average COD concentration of the inlet water of the S-Fe filter is 27.8, the average outlet water concentration is 24.7, and the average removal rate is 11.2%; the average concentration of ammonia nitrogen in inlet water of the S-Fe filter is 0.85, the average concentration of outlet water is 0.58, and the average removal rate is 31.8%; the average concentration of inlet water total nitrogen of the S-Fe filter tank is 19.8, the total nitrogen of outlet water is stably lower than 5mg/L, the average concentration is 2.81, and the average removal rate is 85.8%; the average concentration of total phosphorus in inlet water of the S-Fe filter tank is 2.04, the average concentration of outlet water is 0.13, and the average removal rate is 93.6%.
The S-Fe autotrophic denitrification filter has higher nitrate nitrogen removal efficiency, realizes the aim of deep denitrification, saves the addition of carbon sources under the condition of shortening the HRT of the whole water treatment process, and greatly reduces the operation cost. The iron filings are industrial byproducts, are low in price and wide in source, are placed in the flaky sulfur in a filler ball wrapping mode, can neutralize H & lt + & gt generated by S autotrophic denitrification, maintain the relative stability of the pH value of the system, and ensure the continuous performance of autotrophic denitrification. In addition, the iron carbide and impurities in the iron scrap filler are dispersed in the iron scrap filler in the form of extremely small particles, so that a complete micro-battery loop can be formed, and Fe can be further prevented from being generated3+/Fe2+Continuously separate out of Fe3+/Fe2+And PO4 3-And (4) combining to generate precipitate, thereby realizing the removal of phosphorus in the sewage. Under the normal operation condition, the total phosphorus of the effluent is stabilized below 0.2 mg/L; but the loss of iron is fast, when the reactor runs for about 80 days, the dephosphorization efficiency is reduced to some extent, the total phosphorus concentration of effluent is continuously increased to 0.26 mg/L; the iron filler is replaced at 108d, and the total phosphorus in the effluent is obviously reduced and stabilized below 0.1mg/L after replacement.
Example 3: MBR/S-Fe autotrophic denitrification process
As shown in fig. 8, the reactor is made of acrylic plates, the combined process comprises an MBR tank 7 and an S-Fe filter tank 15, and the effective volumes are respectively: 15L and 6L, wherein the MBR/S-Fe autotrophic denitrification device is sequentially provided with an MBR tank 7 and a pyrite autotrophic denitrification filter 15; the ferro-sulphur autotrophic denitrification filter 15 is connected with an MBR water outlet pipe 6 through an MBR water outlet pump 8; the sulfur-iron autotrophic denitrification filter 15 is provided with a packing layer, and the packing layer comprises stone grains 9 and a sulfur-iron packing layer from bottom to top; the sulfur-iron filler layer comprises sulfur particles 10 and an iron filler layer, the iron filler layer is provided with a bearing layer 12 at the upper part and the lower part, a screen is arranged in the middle, and the bearing layer 12 is provided with water distribution holes 11; iron filings 14 are placed in the iron filler layer, and iron filler replacement openings 13 are further arranged on the side surface of the iron filler layer.
The sulfur granules 10 and the iron packing layer are arranged in a discontinuous arrangement. The iron chips are placed in the screen, and are arranged in a multi-stage sulfur-iron arrangement mode, so that the effect of iron chemical dephosphorization is favorably and fully exerted, and when the iron chips are consumed and the dephosphorization requirement cannot be met, the iron filler can be replaced through the replacement opening, the operation is convenient and fast, and the problems of hardening and replacement of the filler are effectively avoided.
The MBR tank 7 is connected with the water inlet pump 1 through a water inlet pipe; the MBR tank 7 comprises a membrane module 5 and an aeration device; the aeration device is positioned at the bottom of the MBR tank 7 and comprises a fan 2, an aeration pipe 3 and an aerator 4, wherein the fan 2 is positioned outside the MBR tank 7 and is connected with the aerator 4 through the aeration pipe 3. The aeration tank is used for realizing the degradation of organic matters and the nitrification of ammonia nitrogen.
The membrane component 5 is arranged right above the aeration device and is 10-20cm away from the bottom of the MBR tank 7, so that full aeration disturbance is facilitated, and membrane pollution is reduced; the MBR water outlet pump 8 is connected with the membrane module 5 through an MBR water outlet pipe 6. The membrane material in the membrane component 5 is PVDF, the aperture is 0.01 micron, and the effect is to carry out sufficient mud-water separation. The number of the membrane modules 5 is the same as that of the aerators 4, one aerator 4 is arranged right below each membrane module 5, and a water outlet pipe 6 is arranged right above each membrane module 5. The effect of this arrangement is to ensure that a uniform water outlet can be achieved per unit of membrane module. The function of adding stone particles in the sulfur packing layer is to distribute water uniformly. The filler sulfur has a particle size of 2-4 mm, a porosity of 50% and a sulfur-iron dosage ratio of 2: 1.
HRT of the MBR tank is 4-5h, sludge age is 15-20d, dissolved oxygen range is 4-6mg/L, and suspended solid concentration of mixed liquid is 8000-9000 mg/L. The diameter of the S-Fe autotrophic denitrification filter tank is 10cm, and the HRT of an empty bed is 1.5-2 h.
As shown in FIGS. 9-13, the inlet water of the test device is domestic sewage, the COD concentration range is 265-382mg/L, and the average value is 313 mg/L; the concentration range of the total nitrogen is 29.5-43.2mg/L, the average value is 36.8mg/L, the ammonia nitrogen is the main component of the total nitrogen, the average value is 23.3mg/L, and the average proportion reaches 72.9%; the total phosphorus concentration of the inlet water is 2.25-4.81mg/L, and the average value is 3.08 mg/L. And in the MBR process section, aeration and oxygenation are carried out by blast to provide an electron acceptor for aerobic microorganisms in the activated sludge, so that degradation of ammonia nitrogen and organic matters is realized. Due to the characteristics of MBR membrane filtered water, relatively high sludge concentration and dissolved oxygen can be maintained, the pollutant degradation efficiency is far higher than that of a common biochemical aeration tank, under the running condition that HRT is 5 hours, the average COD concentration of effluent water of an MBR process section is 33.7mg/L, and the average removal rate is 88.6%; the average concentration of the ammonia nitrogen in the effluent of the MBR process section is 1.3mg/L, and the average removal rate is 94.5 percent; the average concentration of total nitrogen of effluent of the MBR process section is 24.2mg/L, and the average removal rate is 28.4 percent; the average concentration of total phosphorus in effluent of the MBR process section is 1.87mg/L, and the average removal rate is 40.5%. The MBR process section mainly realizes removal of COD and ammonia nitrogen, has relatively low removal rate of total nitrogen and total phosphorus, and mainly depends on subsequent S-Fe process sections for removal.
The MBR process section is used for degrading organic matters in the inlet water and degrading ammonia nitrogen into nitrate nitrogen through nitrification; the deep removal of nitrogen and phosphorus is realized through S autotrophic nitrogen removal and iron chemical phosphorus removal. The S autotrophic denitrification filter forms an autotrophic denitrification biomembrane by enriching denitrobacillus on the surface of elemental sulfur filler, and realizes nitrogen removal by taking elemental sulfur as an electron donor and nitrate nitrogen as an electron acceptor. The iron filings are industrial byproducts, have wide sources and low price, can neutralize H & lt + & gt generated by S autotrophic denitrification, ensure the relative stability of the pH of the whole system, and can combine the separated iron ions with phosphate to generate iron phosphate precipitate so as to realize the removal of phosphorus in the sewage. The average COD concentration of the inlet water of the S-Fe filter tank is 33.7mg/L, the average outlet water concentration is 29.1mg/L, and the average removal rate is 13.6 percent; the average concentration of ammonia nitrogen in inlet water of the S-Fe filter tank is 1.3mg/L, the average concentration of outlet water is 0.6mg/L, and the average removal rate is 53.8 percent; the average concentration of total nitrogen of inlet water of the S-Fe filter tank is 24.2mg/L, the total nitrogen of outlet water is stably lower than 5mg/L, the average concentration is 2.1mg/L, and the average removal rate is 91.3%; the average concentration of total phosphorus in inlet water of the S-Fe filter is 1.87mg/L, the average concentration of outlet water is 0.12mg/L, and the average removal rate is 93.6%. Finally, the deep removal of nitrogen and phosphorus is realized. Under the normal operation condition, the total phosphorus in the effluent is stabilized below 0.2mg/L, when the reactor operates to about 90d, the phosphorus removal efficiency is obviously reduced, and the total phosphorus concentration in the effluent is continuously increased to reach 0.27 mg/L; the iron filler is replaced at 120d, and the total phosphorus in the effluent is obviously reduced and stabilized below 0.1mg/L after replacement.
Example 4: BAF/S-Fe autotrophic denitrification process
As shown in fig. 14, the reactor is made of acrylic plates, the combined process comprises a BAF filter 3, an intermediate water tank 10 and an S-Fe filter 18, and the effective volumes are respectively as follows: 24L, 3L and 6L, wherein the BAF/S-Fe autotrophic denitrification device is sequentially provided with a BAF filter 3, a middle water tank 10 and an S-Fe filter 18; the BAF filter 3 is connected with a water inlet pump 1 through a water inlet pipe 2; the BAF filter 3 comprises an aeration device and filler, the aeration device is arranged below the BAF filter 3 and comprises an aeration pipe 6, an aerator 7 and a fan 5; the upper part of the aeration pipe 6 is connected with an aerator 7, and the lower part is connected with a fan 5; the filler of the BAF filter 3 consists of cobblestones 8 and stone particle filter materials 9, the effective diameter is 16cm, and the heights are 10cm and 120cm respectively; the S-Fe filter tank water inlet pump is connected with a BAF water outlet pipe 4 through an intermediate water tank 10; the S-Fe filter 18 is connected with an S-Fe filter water inlet pump 11 through an S-Fe filter water inlet pipe; the S-Fe filter 18 is provided with a packing layer, and the packing layer comprises stone particles 12 and a pyrite packing layer from bottom to top; the sulfur iron packing layer comprises sulfur particles 13 and an iron packing layer, the upper part and the lower part of the iron packing layer are provided with bearing layers 15, and the middle part is provided with a screen; a water distribution hole 14 is arranged in the supporting layer 15; the iron filling layer is characterized in that iron chips 17 are placed in a screen, the iron filling layer is also provided with iron filling replacement openings 16, the effective diameter is 10cm, and the heights are 10cm, 10cm and 77cm respectively.
The specific enlarged structure diagram of the ferro-sulphur filler is shown in fig. 1, and sulphur particles in the ferro-sulphur filler layer and the ferro-sulphur filler layer are arranged in a discontinuous arrangement mode. The S-Fe filter tank is used for simultaneously removing nitrogen and phosphorus. Scrap iron and sulfur directly form a mixed layer, so that the scrap iron and sulfur particles are easily hardened, short flow is caused, and removal of nitrogen and phosphorus is not facilitated. Although the packing structure which is wrapped by plastic balls and placed in the sulfur packing can avoid the hardening condition, the structure is not beneficial to the replacement of the iron packing. This embodiment is through placing iron fillings in the screen cloth, and arranges with multistage sulphur-iron mode of arranging, does benefit to the effect of full play iron chemical dephosphorization, and when iron fillings consume to some extent can not satisfy the dephosphorization requirement, the change of iron packing is carried out to the accessible replacement opening, and convenient and fast has effectively avoided the hardening and the change problem of packing. The function of adding stone particles in the sulfur packing layer is to distribute water uniformly.
The HRT of the BAF pool empty bed is 6-8h, the filtering speed is 0.15-0.2m/h, the particle size of the stone particle filter material is 3-5mm, and the porosity is 60%; the HRT of the empty bed of the S-Fe autotrophic denitrification filter is 1.5-2h, the filtering speed is 0.308-0.385m/h, the grain size of the filler sulfur is 2-4 mm, the porosity is 50%, and the dosage ratio of sulfur to iron is 2: 1.
As shown in FIGS. 15-19, the influent water of the test apparatus is the domestic wastewater, wherein the COD concentration is 172-; the concentration of TP is 2.44-4.99mg/L, and the average value is 3.79 mg/L; the concentration of TN is 29-43mg/L, the average value is 35.7mg/L, NH3N is the main component of TN, the average concentration is 23.4mg/L, and the average proportion is 66.3%; the BAF process section enriches aerobic microorganisms on the surface of the filter material by blast aeration oxygenation to form a biological membrane, provides an electron acceptor for the aerobic microorganisms in the biological membrane, and realizes NH3N and degradation of organic matter. The average COD concentration of effluent of the BAF process section is 28.9mg/L, and the average removal rate is 88.8 percent; the average concentration of ammonia nitrogen in effluent of the BAF process section is 0.59mg/L, and the average removal rate is 97.4 percent; the average concentration of total nitrogen in effluent of the BAF process section is 17mg/L, and the average removal rate is 49.7 percent; the average concentration of total phosphorus in the effluent of the BAF process section is 1.7mg/L, and the average removal rate is 33.5 percent. The BAF process section mainly realizes removal of COD and ammonia nitrogen, has low removal rate of total nitrogen and total phosphorus, and mainly depends on subsequent S-Fe filter tanks for removal.
The BAF process section is used for degrading organic matters in the inlet water, enriching a nitrifying biomembrane on the surface of the filter material and degrading ammonia nitrogen into nitrate nitrogen through nitrification. The effluent of the BAF process section enters an S-Fe filter process section. The sulfur autotrophic denitrification is to enrich denitrobacillus on the surface of a sulfur filler to form an autotrophic denitrification biomembrane, take S as an electron donor and nitrate nitrogen as an electron acceptor to perform denitrification so as to remove nitrogen in sewage. The iron filings added in the test are industrial byproducts, have wide sources and low price, and can continuously neutralize H generated by the S autotrophic denitrification+The separated iron ions can be reacted with PO4 3--P binding to FePO4Precipitating to remove the phosphorus. The average value of COD of inlet water of the S-Fe filter process section is 28.9mg/L, the average value of COD of outlet water is 24mg/L, and the average removal rate is 17 percent; average value of ammonia nitrogen in water fed into S-Fe filter tank process section0.59mg/L, the average value of the ammonia nitrogen in the effluent is 0.45mg/L, and the average removal rate is 23.7 percent; the average value of total nitrogen of inlet water of the S-Fe filter process section is 17mg/L, the total nitrogen of outlet water is stably lower than 5mg/L, the average value is 2.8mg/L, and the average removal rate is 83.5 percent; the average value of total phosphorus of inlet water of the S-Fe filter process section is 1.7mg/L, the average value of total phosphorus of outlet water is 0.12mg/L, the average removal rate is 92.9 percent, and the deep nitrogen and phosphorus removal is realized. Under the normal operation condition, the total phosphorus in the effluent is stabilized below 0.2mg/L, when the reactor operates to about 85d, the phosphorus removal efficiency is obviously reduced, and the total phosphorus concentration in the effluent is continuously increased to reach 0.28 mg/L; the iron filler is replaced at 97d, and the total phosphorus in the effluent is obviously reduced and stabilized below 0.1mg/L after replacement.
Comparative example 1:
the ferrosulfur filler of example 1 was replaced with a direct blend of sulfur and iron shot, with other conditions or parameters consistent with example 1. The average concentration of the total nitrogen and the total phosphorus of the effluent is respectively 3.4mg/L and 0.2mg/L, the fluctuation is large, the probability of 8 percent of the total nitrogen existing exceeds 5mg/L, the probability of 15.7 percent of the total phosphorus existing exceeds 0.3mg/L, and the ultralow emission requirements that the total nitrogen is stably lower than 5mg/L and the total phosphorus is stably lower than 0.3mg/L cannot be met. The direct mixing mode of the sulfur particles and the iron particles is easy to cause the hardening of the filler layer, thereby causing short flow and obviously reducing the pollutant removal efficiency.
Comparative example 2:
the ferro-sulphur filler in example 1 is replaced by iron filings and filled in the middle of sulphur granules in a plastic ball wrapping mode, and other conditions or parameters are consistent with those of example 1. When the reactor runs to 70 days, the total phosphorus concentration of effluent is obviously increased, the iron filler is replaced, but the iron chips are filled in a plastic ball wrapping mode and need to be disassembled one by one, the replacement time of the iron filler is 46h, effective water treatment cannot be carried out in the period, and production is influenced; the time required for replacing the iron filler by adopting the pyrite filler layer in the embodiment 1 is 4 hours, so that the replacement time of the iron filler is obviously shortened, and the influence on normal sewage treatment is greatly reduced.
Although the present invention has been described with reference to the preferred embodiments, it should be understood that various changes and modifications can be made therein by those skilled in the art without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (10)
1. A sulfur-iron autotrophic denitrification device is characterized in that the sulfur-iron autotrophic denitrification device is provided with a packing layer, and stone grains and a sulfur-iron packing layer are distributed on the packing layer from bottom to top; the sulfur iron packing layer comprises sulfur particles and an iron packing layer, the iron packing layer is provided with a bearing layer at the upper part and the lower part, the middle part is provided with a screen, and the bearing layer is provided with water distribution holes; the iron filler layer is formed by placing iron chips in a screen mesh, and iron filler replacement openings are further formed in the side face of the iron filler layer.
2. The device of claim 1, wherein the sulfur particles in the sulfur-iron filler layer and the iron filler layer are arranged in a discontinuous arrangement.
3. Use of a ferrosulfur autotrophic denitrification device according to claim 1 or 2 in sewage treatment.
4. A sewage treatment apparatus comprising the pyrite autotrophic denitrification apparatus according to claim 1 or 2.
5. The wastewater treatment apparatus according to claim 4, wherein the apparatus comprises an aeration tank, a sedimentation tank and the pyrite autotrophic denitrification apparatus according to claim 1 or 2; the aeration tank comprises a water inlet, a water outlet and an aeration device; the water inlet is positioned at the lower part of the aeration tank and is connected with a water inlet pump; the aeration device is positioned at the bottom of the aeration tank and comprises a fan, an aeration pipe and an aerator, wherein the fan is positioned outside the aeration tank and is connected with the aerator through the aeration pipe; the sedimentation tank is in an inverted cone shape and comprises a flow guide pipe, a water outlet weir and a mud collecting hopper; the guide pipe is positioned in the center of the sedimentation tank and is connected with the water outlet of the aeration tank through a guide pipe; the effluent weir is positioned at the top of the sedimentation tank; the sludge collecting hopper is positioned at the bottom of the sedimentation tank; the bottom of the sedimentation tank is also provided with a sludge discharge port which is connected with the aeration tank through a sludge reflux pump; the sedimentation tank is connected with the sulfur-iron autotrophic denitrification device through a secondary lift pump.
6. The wastewater treatment device according to claim 4, wherein the device is provided with an MBR tank and the pyrite autotrophic denitrification device according to claim 1 or 2 in sequence; the ferro-sulphur autotrophic denitrification device is connected with an MBR water outlet pipe through an MBR water outlet pump; the MBR tank is connected with a water inlet pump through a water inlet pipe; the MBR tank comprises a membrane component and an aeration device; an aeration device is arranged below the MBR tank, and comprises an aeration pipe, an aerator and a fan; the upper part of the aeration pipe is connected with an aerator, and the lower part of the aeration pipe is connected with a fan; the membrane module is arranged right above the aeration device, and the MBR water outlet pump is connected with the membrane module through an MBR water outlet pipe.
7. The wastewater treatment device according to claim 4, wherein the device is provided with a BAF filter tank, an intermediate water tank and the pyrite autotrophic denitrification device according to claim 1 or 2 in sequence; the BAF filter tank is connected with a water inlet pump through a water inlet pipe; the BAF filter tank comprises an aeration device and filler, wherein the aeration device is arranged below the BAF filter tank and comprises an aeration pipe, an aerator and a fan; the upper part of the aeration pipe is connected with an aerator, and the lower part of the aeration pipe is connected with a fan; the filler of the BAF filter tank consists of cobblestones and stone particle filter materials; and a water inlet pump of the ferro-sulphur autotrophic denitrification device is connected with a BAF water outlet pipe through an intermediate water tank.
8. The application of the device of claim 5 in sewage treatment is characterized in that the specific parameter conditions in the application are as follows: the hydraulic retention time of the aeration tank is 6-8h, the sludge age is 10-15d, the dissolved oxygen range is 2-4mg/L, and the suspended solid concentration of the mixed solution is 4000-; HRT of the sedimentation tank is 2-3h, and surface hydraulic load is 1.0-1.2m3/(m2·h)。
9. The application of the device of claim 6 in sewage treatment is characterized in that the specific parameter conditions in the application are as follows: HRT of the MBR tank is 4-5h, sludge age is 15-20d, dissolved oxygen range is 4-6mg/L, and suspended solid concentration of mixed liquid is 8000-9000 mg/L.
10. The application of the device of claim 7 in sewage treatment is characterized in that the specific parameter conditions in the application are as follows: the HRT of the empty bed of the BAF filter is 6-8h, the filtering speed is 0.11-0.15m/h, the HRT of the empty bed of the sulfur-iron autotrophic denitrification filter is 1.5-2h, and the filtering speed is 0.289-0.385 m/h.
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| CN112919626A (en) * | 2021-01-21 | 2021-06-08 | 臻和慧联(常山)环境科技有限公司 | Ferrosulfur autoxidation denitrification device and reaction control method |
| CN113683202A (en) * | 2021-06-07 | 2021-11-23 | 浙江建投环保工程有限公司 | Sulphur iron coupling effluent treatment plant |
| CN113582335A (en) * | 2021-08-17 | 2021-11-02 | 哈尔滨工创环保科技有限公司 | In-situ device and method for improving nitrate nitrogen removal rate of coal pyrolysis wastewater |
| CN114180716A (en) * | 2021-12-01 | 2022-03-15 | 南京扬子江生态环境产业研究院有限公司 | Combined denitrification reactor |
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