CN112811593A - Iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and operation method - Google Patents
Iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and operation method Download PDFInfo
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 188
- 230000001651 autotrophic effect Effects 0.000 title claims abstract description 103
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 44
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 38
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 25
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 25
- 239000011574 phosphorus Substances 0.000 title claims abstract description 25
- AHEWZZJEDQVLOP-UHFFFAOYSA-N monobromobimane Chemical compound BrCC1=C(C)C(=O)N2N1C(C)=C(C)C2=O AHEWZZJEDQVLOP-UHFFFAOYSA-N 0.000 title claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 102
- 238000006243 chemical reaction Methods 0.000 claims abstract description 88
- 238000004062 sedimentation Methods 0.000 claims abstract description 67
- 239000010802 sludge Substances 0.000 claims abstract description 56
- 239000010865 sewage Substances 0.000 claims abstract description 17
- 239000000725 suspension Substances 0.000 claims description 36
- 238000010992 reflux Methods 0.000 claims description 28
- 239000007788 liquid Substances 0.000 claims description 22
- 238000005273 aeration Methods 0.000 claims description 21
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 claims description 17
- 239000000969 carrier Substances 0.000 claims description 15
- 238000011049 filling Methods 0.000 claims description 15
- 241000894006 Bacteria Species 0.000 claims description 13
- 230000003647 oxidation Effects 0.000 claims description 12
- 238000007254 oxidation reaction Methods 0.000 claims description 12
- 238000011001 backwashing Methods 0.000 claims description 8
- 239000000470 constituent Substances 0.000 claims description 6
- 230000003311 flocculating effect Effects 0.000 claims description 6
- 238000005189 flocculation Methods 0.000 claims description 5
- 230000016615 flocculation Effects 0.000 claims description 5
- 239000006228 supernatant Substances 0.000 claims description 5
- 229910019142 PO4 Inorganic materials 0.000 claims description 4
- 238000011010 flushing procedure Methods 0.000 claims description 4
- 230000014759 maintenance of location Effects 0.000 claims description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 4
- 239000010452 phosphate Substances 0.000 claims description 4
- 241000108664 Nitrobacteria Species 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 238000011017 operating method Methods 0.000 claims 2
- 230000000694 effects Effects 0.000 abstract description 7
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 3
- 230000008569 process Effects 0.000 description 23
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 15
- 229910002651 NO3 Inorganic materials 0.000 description 10
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 10
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 4
- 238000009826 distribution Methods 0.000 description 4
- 244000005700 microbiome Species 0.000 description 4
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000000370 acceptor Substances 0.000 description 2
- 230000033558 biomineral tissue development Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QALQXPDXOWOWLD-UHFFFAOYSA-N [N][N+]([O-])=O Chemical compound [N][N+]([O-])=O QALQXPDXOWOWLD-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000005276 aerator Methods 0.000 description 1
- 230000000872 anti-mineralization Effects 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- VTYYLEPIZMXCLO-UHFFFAOYSA-L calcium carbonate Substances [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
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- 230000007613 environmental effect Effects 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011159 matrix material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
-
- 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
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/16—Total nitrogen (tkN-N)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/18—PO4-P
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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- Life Sciences & Earth Sciences (AREA)
- Microbiology (AREA)
- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention discloses an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and an operation method thereof, and relates to the technical field of sewage treatment. The system comprises a reaction tank, a total water inlet pipeline and a total water outlet pipeline, wherein water to be treated enters from the total water inlet pipeline, sequentially passes through a first aerobic zone, a primary sedimentation zone, a Feammox reaction zone, a second aerobic zone, a Fe autotrophic denitrification zone, a third aerobic zone and a secondary sedimentation zone, and is discharged through the total water outlet pipeline; the system also comprises a return pipeline arranged between the third aerobic zone and the first aerobic zone and between the third aerobic zone and the Feammox reaction zone, and a sludge return pipeline arranged between the secondary sedimentation zone and the Feammox reaction zone. The invention can realize quick start by combining Feammox and Fe autotrophic denitrification technology, and has the advantages of simple operation, stable treatment effect, low treatment cost, good impact resistance and the like.
Description
Technical Field
The invention relates to the technical field of sewage treatment, in particular to an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and an operation method.
Background
Autotrophic nitrogen removal technology is a novel nitrogen removal process which is developed rapidly in recent years, and is concerned by researchers in the field of biological nitrogen removal of wastewater all over the world, the process performs nitrogen removal through anaerobic ammonia oxidation, and compared with the traditional nitrification and denitrification, the organic carbon source addition can be saved by 100%, so that the autotrophic nitrogen removal technology is considered as the most economic and effective biological nitrogen removal mode for wastewater. But conventional nitrite-type ANAMMOX (amammox) is used to oxidize NH4 +NO is required in the oxidation process2 -As an electron acceptor, it is therefore necessary to combine with the short-cut nitration process in order to be able to do so. Due to the addition of the short-cut nitrification, on one hand, a proper amount of aeration needs to be provided, and the aeration energy consumption is increased; on the other hand, the problem that the effluent exceeds the standard due to the fact that the shortcut nitrification effect is damaged caused by system instability is easily faced in the operation control process, and the control difficulty is increased, so that large-scale engineering application of nitrite type anaerobic ammonia oxidation is not realized at present.
Iron, as the second highest transition metal in the earth's crust, participates in redox reactions that drive the biochemical cycle worldwide. Meanwhile, at present, an autotrophic denitrification process driven by Fe is also gradually discovered and attracts attention, mainly including ferric ammonium oxidation (Feammox) and an Fe autotrophic denitrification process.
Feammox is a newly discovered biological denitrification process in recent years. In anaerobic and iron-containing environment, the microorganism takes Fe3+As electron acceptors, with NH4 +Effecting NH for electron donor4 +Oxidation of N with simultaneous addition of Fe3+Reduction to Fe2+Compared with ANAMMOX, Feammox does not need to be combined with an aerobic process, aeration energy consumption can be further reduced theoretically, operation difficulty is reduced, but problems still exist in the Feammox process and need to be solved, such as Fe3+The source problem of the iron element, how to realize the recycling of the iron element, how to stably enrich Feammox microorganisms and the like.
Fe autotrophic denitrification can utilize Fe and Fe2+Etc. as electron donors, with NO2 -Or NO3 -Reduction to N2While mixing Fe and Fe2+Oxidation to Fe3+Research reports that the denitrification rate is higher than that of hydrogen autotrophic denitrification or sulfur autotrophic denitrification, but the prior Fe autotrophic denitrification also has NO in application2 -Or NO3 -Source of (3), Fe3+Recovery of (2) and Fe3+Deposition affects mass transfer and the like.
The research reports of the related aspects of the prior art mainly include:
CN 105271514A discloses a biological denitrification method based on anaerobic iron-oxidized ammonia, which comprises the following steps: adding sludge containing Feammox microbe into anaerobic reactor, introducing ammonia-containing sewage into the reactor, and oxidizing NH in sewage with Fe (III)4 +Generation of NO2 -Then carrying out deep denitrification treatment, aiming at NO generated by Feammox2 -The by-product needs to be additionally provided with a deep denitrification process, thereby increasing the process flow and the operation complexity, and the Fe content3+The source of (a) is also not specified.
CN 109650536A provides a device and method based on iron cycle driven ammonia nitrogen anaerobism in situ treatment, its characterized in that: nitrate-dependent iron oxidation (NDFO) is initiated by adding nitrate to a Feammox system containing iron by periodic addition of NO to the Feammox system3 -Oxidizing Fe2+Produced Fe3+Continued participation in Feammox, production of Fe2+And additionally added new NO3 -By oxidation, thus by periodic addition of NO3 -The limited iron will be available for more nitrogen removal. However, the process needs external nitrate, on one hand, new nitrogen is introduced, on the other hand, the operation cost is increased, the deep denitrification process is not needed, and only Feammox cannot realize high total nitrogen removal.
Zhang Ningbo et al (Zhang Ningbo, Li Xiang, Huang Yong, etc.. zero-valent iron autotrophic denitrification process activated sludge mineralization and solution [ J ]. environmental science, 2017,38(9):3793-3800.DOI:10.13227/j.hjkx.201703032.) initiate zero-valent iron autotrophic denitrification reaction in an upflow anaerobic reactor by inoculating activated sludge of a domestic sewage treatment plant, and the sludge is mineralized by the ferric iron and the iron oxide which are gradually formed in the operation process, so that the activity is reduced, the feasibility research of two anti-mineralization modes of feeding the sludge in a flowing mode and changing backflow is carried out, the backflow mode is changed, a backflow pool is arranged outside the reaction column, water on the upper portion of the backflow pool is used for hydraulic circulation and ascending scouring, the generated ferric iron and the iron oxide flow out along with effluent and are deposited in the external backflow pool, and the sludge mineralization problem in long-term operation is solved. However, how to realize the source of the nitro-nitrogen in the process is not researched too much, and the practical application may be hindered.
Therefore, the autotrophic nitrogen removal process using Fe as a reactant faces the problems of matrix source, Fe element circulation and the like, and the process can only realize nitrogen removal but cannot realize synchronous phosphorus removal, so that the application and development of related processes are restricted. If the problems can be solved on the basis of minimum cost and process complexity by coupling different processes, the autotrophic nitrogen removal process using Fe as a reactant has better application prospect.
Disclosure of Invention
One of the purposes of the invention is to provide an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR, wherein a reaction zone of the system treats sewage in a mode of combining Feammox and iron autotrophic denitrification, and the system has the advantages of simple operation, stable treatment effect, low treatment cost and good impact resistance.
In order to achieve the purpose, the invention adopts the following technical scheme:
an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR comprises a reaction tank, a total water inlet pipeline and a total water outlet pipeline, wherein the reaction tank is sequentially divided into a first aerobic zone, a primary sedimentation zone, a Feammox reaction zone, a second aerobic zone, an Fe autotrophic denitrification zone, a third aerobic zone and a secondary sedimentation zone from front to back;
the total water inlet pipeline is connected to the tank body of the first aerobic zone, the total water outlet pipeline is connected to the tank body of the secondary sedimentation zone, and water to be treated enters from the total water inlet pipeline and passes through the first aerobic zone, the primary sedimentation zone, the Feammox reaction zone, the second aerobic zone, the Fe autotrophic denitrification zone, the third aerobic zone and the secondary sedimentation zone in sequence and then is discharged through the total water outlet pipeline;
a first return pipeline is arranged between the first aerobic zone and the third aerobic zone, and return liquid flows to the lower part of the first aerobic zone from the third aerobic zone; a second return pipeline is arranged between the Feammox reaction zone and the third aerobic zone, and return liquid flows to the lower part of the Feammox reaction zone from the third aerobic zone; a return pipeline in the Fe autotrophic denitrification region is arranged in the Fe autotrophic denitrification region, and return fluid flows from the upper part of the Fe autotrophic denitrification region to the lower part of the Fe autotrophic denitrification region; a sludge return pipeline is arranged between the secondary sedimentation zone and the Feammox reaction zone, and returned sludge flows to the upper part of the Feammox reaction zone from the lower part of the secondary sedimentation zone;
a water distributor and a backwashing device are arranged at the lower part of the Fe autotrophic denitrification zone, and the backwashing device comprises an air flushing pipe and a water flushing pipe;
an iron-based fixed bed is arranged in the Fe autotrophic denitrification zone, the iron-based fixed bed is distributed according to units, and the filling rate of filter materials in the zone can be changed by placing different unit numbers.
As a preferable scheme of the invention, suspension carriers are added into the first aerobic zone, the Feammox reaction zone and the second aerobic zone, wherein the density of the suspension carriers in the first aerobic zone and the second aerobic zone is 0.95-0.97g/cm3The density of the suspension carrier in the Feammox reaction zone is 0.96-0.98g/cm3The effective specific surface area of the suspension carrier is 450-1200m2/m3。
As another preferred scheme of the invention, the main water inlet pipeline is connected to the tank body at the lower part of the first aerobic zone, and the main water outlet pipeline is connected to the tank body at the upper part of the secondary sedimentation zone; the first aerobic zone is communicated with the primary sedimentation zone through a first interception screen arranged at the upper part of the water outlet end of the first aerobic zone, and the primary sedimentation zone is communicated with the Feammox reaction zone through a second interception screen arranged at the upper part of the water outlet end of the primary sedimentation zone; the Feammox reaction zone and the second aerobic zone are communicated through a third interception screen mesh arranged at the lower part of the water outlet end of the Feammox reaction zone; the second aerobic zone and the Fe autotrophic denitrification zone are communicated with each other through a fourth intercepting screen arranged at the upper part of the water outlet end of the second aerobic zone, the Fe autotrophic denitrification zone and the third aerobic zone are communicated with each other through a fifth intercepting screen arranged at the upper part of the water outlet end of the Fe autotrophic denitrification zone, and the third aerobic zone and the secondary sedimentation zone are communicated with each other through water passing holes arranged at the lower part of the water outlet end of the third aerobic zone.
Preferably, the water inlet ends of the primary sedimentation zone and the Fe autotrophic denitrification zone are respectively provided with a first guide wall and a second guide wall, the upper ends of the first guide wall and the second guide wall are higher than the liquid level in the system, and the distance between the lower ends of the first guide wall and the second guide wall and the bottom of the tank is 10-30% of the depth of the tank.
Preferably, the lower parts of the primary settling zone and the secondary settling zone are respectively provided with a sludge discharge pipeline, and a sludge discharge valve of the primary settling zone and a sludge discharge valve of the secondary settling zone are correspondingly arranged on the respective sludge discharge pipelines.
Preferably, a submersible stirrer is installed on the inner wall of the tank body of the Feammox reaction zone, and aeration pipelines are installed at the lower parts of the first aerobic zone, the second aerobic zone and the third aerobic zone.
The invention also aims to provide an operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on the MBBR, which sequentially comprises the following steps:
a. the sewage to be treated firstly enters a first aerobic zone, the organic matters in the inlet water are removed by heterotrophic bacteria attached and grown on the suspension carrier under the aeration condition, SS, phosphate and the like in the inlet water and Fe in the reflux liquid3+The flocculating constituent is generated by contact flocculation, and the reflux ratio of the first reflux pipeline is 10-100%;
b. the effluent of the first aerobic zone enters a primary sedimentation zone, and a flocculating constituent is settled and discharged through a sludge discharge pipeline of the primary sedimentation zone;
c. the effluent from the primary sedimentation zone enters a Feammox reaction zone, and Feammox bacteria growing on the suspension carrier are attached to the suspension carrier to carry Fe in the reflux liquid3+Partial NH carried in the feed water is completed as an electron donor4 +Removal of-N and generation of small amounts of NO2 -N, the reflux ratio of the second return line is 50-200%, and the effluent NH of the Feammox reaction zone4 +N is less than 50mg/L, and compared with inlet water, the ammoxidation rate of outlet water of the Feammox reaction zone is more than 50 percent;
d. the effluent of the Feammox reaction zone enters a second aerobic zone, and the residual NH of the raw water is completed through nitrobacteria attached and grown on the suspension carrier4 +-N and NO2 -Removal of-N and generation of NO3 -N, second aerobic zone effluent NH4 +-N＜1.5mg/L；
e. The effluent of the second aerobic zone enters an Fe autotrophic denitrification zone, the deep total nitrogen removal is completed through autotrophic denitrifying bacteria attached and grown on an iron-based fixed bed, and Fe is generated2+The reflux ratio in the Fe autotrophic denitrification zone is 200-400 percent;
f. the effluent of the Fe autotrophic denitrification zone enters a third aerobic zone, and Fe is treated under the aeration condition2+Total oxidation to Fe3+And respectively reflows to the first aerobic zone and the Feammox reaction zone along with the reflow liquid;
g. the effluent of the third aerobic zone enters a secondary sedimentation zone, and the residual Fe carried by the effluent3+And a part of the settled SS is returned to the Feammox reaction zone through a sludge return line to ensure that Fe3+The sludge is recycled, the reflux ratio of the sludge is 10 to 100 percent, the other part of the sludge is discharged through a sludge discharge valve of the secondary sedimentation area, and the supernatant reaches the discharge standard of the sewage and is discharged through a main water outlet pipeline at the upper part of the secondary sedimentation area.
Further, in the step a, the hydraulic retention time in the first aerobic zone is 1-4 h.
Further, the sludge concentration of the Feammox reaction zone, the Fe autotrophic denitrification zone, the first aerobic zone, the second aerobic zone and the third aerobic zone is less than 500 mg/L; the filling rate of the suspended carriers in the first aerobic zone and the second aerobic zone is 30-60%, the DO is 3-6mg/L, the DO in the third aerobic zone is 1-3mg/L, the filling rate of the suspended carriers in the Feammox reaction zone is 10-50%, and the DO in the Feammox reaction zone and the Fe autotrophic denitrification zone is less than 0.4 mg/L.
Compared with the prior art, the invention has the following beneficial technical effects:
(1) the operation cost is saved, the Feammox and the Fe autotrophic denitrification process are combined to carry out high-efficiency autotrophic nitrogen removal, and 100% of carbon source addition can be saved;
(2) taking nitrogen and phosphorus removal into consideration, and generating part of Fe by Fe autotrophic denitrification3+The water flows back to the water inlet end to be used as a coagulant to realize chemical phosphorus removal, and simultaneously, the removal of nitrogen and phosphorus of the system is ensured, so that the iron is multipurpose;
(3) the treatment load is high, both Feammox and iron autotrophic denitrification adopt MBBR forms, effective strains are highly enriched on the carrier, and the treatment load is high.
(4) The aerobic pool is added to reduce the adverse effect of the COD of the inlet water on the subsequent Feammox and Fe autotrophic denitrifying microorganisms through denitrification, so as to create a good environment for the biochemical reaction pool, and the Fe autotrophic denitrification outlet water can supplement certain alkalinity for the Feammox reaction pool, so that the denitrification effect is enhanced.
Drawings
The invention is further described below with reference to the accompanying drawings:
FIG. 1 is a schematic structural diagram of an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR according to the present invention;
in the figure:
1. a first aerobic zone, a 2, a primary sedimentation zone, a 3, a Feammox reaction zone, a 4, a second aerobic zone, a 5, a Fe autotrophic denitrification zone, a 6, a third aerobic zone, a 7, a secondary sedimentation zone, a 8, an iron-based fixed bed, a 9, a water distribution plate, a 10, a backwashing device, 11, a suspension carrier, I1, a total water inlet pipeline, I2, a first return pipeline, I3, a second return pipeline, I4, an internal return pipeline of the Fe autotrophic denitrification zone, I5, a sludge return pipeline, I6, a total water outlet pipeline, S1, a first screen, S2, a second screen, S3, a third screen, S4, a fourth screen, S5, a fifth screen, C1, a first aeration zone aeration pipeline, C2, a second aerobic zone pipeline, C3, a third aerobic zone aeration pipeline, M, a submerged primary aerator, a P1, a P guide valve, a P precipitation zone, a P2, a second aerobic sedimentation zone and a sludge settling wall 1, q2, second guide wall.
Detailed Description
The invention provides an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and an operation method thereof, and the invention is further explained by combining specific embodiments in order to make the advantages and technical scheme of the invention clearer and more clear.
The 'MBBR' referred in the invention refers to moving Bed Biofilm reactor (moving Bed Biofilm reactor), and the method increases the biomass and the biological species in the treatment system by adding a certain amount of suspension carriers into the system and utilizing the Biofilm growing on the suspension carriers to enrich the functional microorganisms, thereby increasing the treatment efficiency of the system.
The filling rate, namely the filling rate of the suspension carrier, namely the ratio of the volume of the suspension carrier to the pool volume of the filling area, is referred to in the invention, and the volume of the suspension carrier is the total volume under natural accumulation; e.g. 100m3Suspending vehicle, filled to 400m3The tank capacity and the filling rate are 25 percent.
The iron-based fixed bed mentioned in the invention means that reactants filled in the fixed bed mainly take elementary substance iron as raw materials;
the water distributor and the backwashing device can be realized by referring to the structure and the working method of the prior art.
As a main improvement point of the invention, the sewage is treated by combining Feammox and iron autotrophic denitrification. Specifically, as shown in fig. 1, the iron-based autotrophic nitrogen and phosphorus removal system based on MBBR of the present invention comprises a reaction tank, a total water inlet pipeline I1 and a total water outlet pipeline I6, wherein the reaction tank is sequentially divided into a first aerobic zone 1, a primary settling zone 2, a Feammox reaction zone 3, a second aerobic zone 4, a Fe autotrophic denitrification zone 5, a third aerobic zone 6 and a secondary settling zone 7 from front to back;
the total water inlet pipeline I1 is used for feeding water into the reaction tank and is connected to the tank body with the first aerobic zone at the lower part, the total water outlet pipeline I6 is connected to the tank body with the second sedimentation zone at the upper part, and the water to be treated enters from the total water inlet pipeline and is discharged through the total water outlet pipeline after sequentially passing through the first aerobic zone, the primary sedimentation zone, the Feammox reaction zone, the second aerobic zone, the Fe autotrophic denitrification zone, the third aerobic zone and the second sedimentation zone. The adjacent reaction zones are communicated, the first aerobic zone and the primary sedimentation zone are communicated through a first interception screen S1 arranged at the upper part of the water outlet end of the first aerobic zone, and the primary sedimentation zone and the Feammox reaction zone are communicated through a second interception screen S2 arranged at the upper part of the water outlet end of the primary sedimentation zone; the Feammox reaction zone and the second aerobic zone are communicated through a third interception screen S3 arranged at the lower part of the water outlet end of the Feammox reaction zone; the second aerobic zone and the Fe autotrophic denitrification zone are communicated with each other through a fourth intercepting screen S4 arranged at the upper part of the water outlet end of the second aerobic zone, the Fe autotrophic denitrification zone and the third aerobic zone are communicated with each other through a fifth intercepting screen S5 arranged at the upper part of the water outlet end of the Fe autotrophic denitrification zone, and the third aerobic zone and the secondary sedimentation zone are communicated with each other through water passing holes arranged at the lower part of the water outlet end of the third aerobic zone.
A first return pipeline I2 is arranged between the first aerobic zone and the third aerobic zone, and return liquid flows to the lower part of the first aerobic zone from the third aerobic zone; a second return pipeline I3 is arranged between the Feammox reaction zone and the third aerobic zone, and return liquid flows to the lower part of the Feammox reaction zone from the third aerobic zone; a return pipeline I4 in the Fe autotrophic denitrification zone is arranged in the Fe autotrophic denitrification zone, and return fluid flows from the upper part of the Fe autotrophic denitrification zone to the lower part of the Fe autotrophic denitrification zone; and a sludge return pipeline I5 is arranged between the secondary sedimentation zone and the Feammox reaction zone, and returned sludge flows to the upper part of the Feammox reaction zone from the lower part of the secondary sedimentation zone.
A first aerobic zone aeration pipeline C1, a second aerobic zone aeration pipeline C2 and a third aerobic zone aeration pipeline C3 are respectively arranged in the first aerobic zone, the second aerobic zone and the third aerobic zone, and aeration is carried out on the corresponding aerobic zones through respective aeration pipelines.
A water distributor and a backwashing device 10 are arranged at the lower part of the Fe autotrophic denitrification zone, the water distributor comprises a water distribution plate 9, the water distribution plate 9 can realize water distribution according to a certain rule, and the backwashing device comprises an air blast pipe and a water blast pipe;
an iron-based fixed bed 8 is arranged in the Fe autotrophic denitrification zone, the iron-based fixed beds are distributed according to units, and the filling rate of filter materials in the zone can be changed by placing different numbers of units.
As a preferable scheme of the invention, suspension carriers 11 are added into the first aerobic zone, the Feammox reaction zone and the second aerobic zone, wherein the density of the suspension carriers in the first aerobic zone and the second aerobic zone is 0.95-0.97g/cm3The density of the suspension carrier in the Feammox reaction zone is 0.96-0.98g/cm3The effective specific surface area of the suspension carrier is 450-1200m2/m3。
Further, a submersible stirrer M is arranged on the inner wall of the tank body of the Feammox reaction zone and used for propelling and stirring sewage and strengthening the stirring function;
the water inlet ends of the primary sedimentation zone and the Fe autotrophic denitrification zone are respectively provided with a first guide wall Q1 and a second guide wall Q2, the upper ends of the first guide wall and the second guide wall are higher than the liquid level in the system, and the distance between the lower ends of the first guide wall and the bottom of the tank is 10-30% of the depth of the tank.
The lower parts of the primary settling area and the secondary settling area are respectively provided with a sludge discharge pipeline, and a primary settling area sludge discharge valve P1 and a secondary settling area sludge discharge valve P2 are correspondingly arranged on the respective sludge discharge pipelines.
The operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on MBBR is described in detail below.
The method specifically comprises the following steps:
firstly, sewage to be treated enters a first aerobic zone, influent organic matters are removed by heterotrophic bacteria attached to and grown on a suspension carrier under the aeration condition, SS, phosphate and the like in the influent water and Fe in a reflux liquid3+Contact flocculation occurs to generate floccules. The reflux ratio of the first reflux pipeline is 10-100 percent; the hydraulic retention time in the first aerobic zone is 1-4 h;
secondly, the effluent of the first aerobic zone enters a primary sedimentation zone, and a flocculating constituent is settled and discharged through a sludge discharge pipeline of the primary sedimentation zone;
thirdly, the effluent from the primary sedimentation zone enters a Feammox reaction zone, Feammox bacteria growing on the suspended carrier adhere to the suspended carrier and Fe carried in the reflux liquid3+Partial NH carried in the feed water is completed as an electron donor4 +-N removalAnd generating a small amount of NO2 --N, the second return line reflux ratio is 50-200%. Feammox reaction zone effluent NH4 +N is less than 50mg/L, and compared with inlet water, the ammoxidation rate of outlet water of the Feammox reaction zone is more than 50 percent;
fourthly, the effluent of the Feammox reaction zone enters a second aerobic zone, and the residual NH of the raw water is completed through nitrobacteria attached and grown on the suspension carrier4 +-N and NO2 -Removal of-N and generation of NO3 -N, second aerobic zone effluent NH4 +-N＜1.5mg/L；
Fifthly, the effluent of the second aerobic zone enters an Fe autotrophic denitrification zone, the deep total nitrogen removal is completed through autotrophic denitrifying bacteria attached and grown on an iron-based fixed bed, and Fe is generated2+. The reflux ratio in the Fe autotrophic denitrification zone is 200-400%.
Sixthly, the effluent of the Fe autotrophic denitrification zone enters a third aerobic zone, and Fe is treated under the aeration condition2+Total oxidation to Fe3+And respectively reflows to the first aerobic zone and the Feammox reaction zone along with the reflow liquid;
the seventh step, the effluent of the third aerobic zone enters a secondary sedimentation zone, and the residual Fe carried by the effluent3+And a part of the settled SS is returned to the Feammox reaction zone through a sludge return line to ensure that Fe3+The sludge is recycled, the reflux ratio of the sludge is 10 to 100 percent, the other part of the sludge is discharged through a sludge discharge valve of the secondary sedimentation area, and the supernatant reaches the discharge standard of the sewage and is discharged through a main water outlet pipeline at the upper part of the secondary sedimentation area.
Further, the sludge concentration of the Feammox reaction zone, the Fe autotrophic denitrification zone, the first aerobic zone, the second aerobic zone and the third aerobic zone is less than 500 mg/L; the filling rate of the suspended carriers in the first aerobic zone and the second aerobic zone is 30-60%, the DO is 3-6mg/L, the DO in the third aerobic zone is 1-3mg/L, the filling rate of the suspended carriers in the Feammox reaction zone is 10-50%, and the DO in the Feammox reaction zone and the Fe autotrophic denitrification zone is less than 0.4 mg/L.
The present invention will be described in detail with reference to specific examples.
Example 1:
iron-based autotrophy using MBBRThe nitrogen and phosphorus removal system treats the anaerobic sludge digestion supernatant of a certain sewage plant, and the water quantity is 100m3The mean water temperature is 29 ℃, the mean ammonia nitrogen concentration is 450mg/L, the COD concentration is 600mg/L, the mean BOD5 concentration is 290mg/L, the mean TP is 15mg/L, and the mean alkalinity is CaCO3Meter) 3900 mg/L. The depth of the system pool is 4.4m, suspension carriers are added into the first aerobic zone, the Feammox reaction zone and the second aerobic zone of the system, and the adding density in the first aerobic zone and the second aerobic zone of the system is 0.95g/cm3The filling rate of the suspension carrier is 30 percent, and the adding density in the Feammox reaction zone is 0.97g/cm3The filling rate of the suspension carrier is 40 percent, and the effective specific surface areas of the suspension carrier added in the system are all 800m2/m3. And the water inlet ends of the primary sedimentation zone and the Fe autotrophic denitrification zone are respectively provided with a first guide wall and a second guide wall, the upper ends of the first guide wall and the second guide wall are higher than the liquid level in the system, and the distance between the lower ends of the first guide wall and the second guide wall and the bottom of the tank is 0.6 m.
The operation method adopted by the system is as follows:
a. the sewage to be treated firstly enters a first aerobic zone, the organic matters in the inlet water are removed by heterotrophic bacteria attached and grown on the suspension carrier under the aeration condition, SS, phosphate and the like in the inlet water and Fe in the reflux liquid3+The flocculation is generated by contact flocculation, the reflux ratio of the first return pipeline is 10 percent, the hydraulic retention time of the first aerobic zone is 1h, the sludge concentration is 322mg/L, and DO2.6mg/L;
b. the effluent of the first aerobic zone enters a primary sedimentation zone, and a flocculating constituent is settled and discharged through a sludge discharge pipeline of the primary sedimentation zone;
c. the effluent from the primary sedimentation zone enters a Feammox reaction zone, and Feammox bacteria growing on the suspension carrier are attached to the suspension carrier to carry Fe in the reflux liquid3+Partial NH carried in the feed water is completed as an electron donor4 +Removal of-N and generation of NO2 --N, second return line reflux ratio 100%. Feammox reaction zone effluent NH4 +The average value of N is 42mg/L, compared with the inlet water, the ammoxidation rate of the outlet water of the Feammox reaction zone is up to 90%, and the average value of the sludge concentration is 368 mg/L;
d. the effluent of the Feammox reaction zone enters a second aerobic zone and passes through a suspension carrier to be attachedThe grown nitrifying bacteria complete the residual NH of the raw water4 +-N and NO2 -Removal of-N and generation of NO3 --N, the average sludge concentration of the second aerobic zone is 377mg/L, DO4.3mg/L and the effluent NH4 +-N mean 1.1 mg/L;
e. the effluent of the second aerobic zone enters an Fe autotrophic denitrification zone, the deep total nitrogen removal is completed through autotrophic denitrifying bacteria attached and grown on an iron-based fixed bed, and Fe is generated2+. The sludge concentration of the Fe autotrophic denitrification zone is 383mg/L, and the internal reflux ratio is 300 percent;
f. the effluent of the Fe autotrophic denitrification zone enters a third aerobic zone, and Fe is treated under the aeration condition2+Total oxidation to Fe3+Respectively refluxing to the first aerobic zone and the Feammox reaction zone along with the reflux liquid, wherein the sludge concentration of the third aerobic zone is 401mg/L and DO5.5mg/L;
g. the effluent of the third aerobic zone enters a secondary sedimentation zone, and the residual Fe carried by the effluent3+And a part of the settled SS is returned to the Feammox reaction zone through a sludge return line to ensure that Fe3+The other part is discharged through a mud valve of the secondary sedimentation area, and the supernatant reaches the discharge standard of sewage and is discharged through a main water outlet pipeline at the upper part of the secondary sedimentation area. The ammonia nitrogen, TN, COD and TP of the effluent are respectively 0.6, 6.8, 44.6 and 0.4 mg/L.
The parts which are not described in the invention can be realized by taking the prior art as reference.
It should be noted that: any equivalents or obvious modifications thereof which may occur to persons skilled in the art and which are given the benefit of this description are deemed to be within the scope of the invention.
Claims (9)
1. The utility model provides an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR, it includes reaction tank, total inlet channel and total outlet pipeline, its characterized in that:
the reaction tank is sequentially divided into a first aerobic zone, a primary sedimentation zone, a Feammox reaction zone, a second aerobic zone, a Fe autotrophic denitrification zone, a third aerobic zone and a secondary sedimentation zone from front to back;
the total water inlet pipeline is connected to the tank body of the first aerobic zone, the total water outlet pipeline is connected to the tank body of the secondary sedimentation zone, and water to be treated enters from the total water inlet pipeline, passes through the first aerobic zone, the primary sedimentation zone, the Feammox reaction zone, the second aerobic zone, the Fe autotrophic denitrification zone, the third aerobic zone and the secondary sedimentation zone in sequence and is discharged through the total water outlet pipeline;
a first return pipeline is arranged between the first aerobic zone and the third aerobic zone, and return liquid flows to the lower part of the first aerobic zone from the third aerobic zone; a second return pipeline is arranged between the Feammox reaction zone and the third aerobic zone, and return liquid flows to the lower part of the Feammox reaction zone from the third aerobic zone; a return pipeline in the Fe autotrophic denitrification region is arranged in the Fe autotrophic denitrification region, and return fluid flows from the upper part of the Fe autotrophic denitrification region to the lower part of the Fe autotrophic denitrification region; a sludge return pipeline is arranged between the secondary sedimentation zone and the Feammox reaction zone, and returned sludge flows to the upper part of the Feammox reaction zone from the lower part of the secondary sedimentation zone;
a water distributor and a backwashing device are arranged at the lower part of the Fe autotrophic denitrification zone, and the backwashing device comprises an air flushing pipe and a water flushing pipe;
an iron-based fixed bed is arranged in the Fe autotrophic denitrification zone, the iron-based fixed bed is distributed according to units, and the filling rate of filter materials in the zone can be changed by placing different unit numbers.
2. The MBBR-based iron-based autotrophic nitrogen and phosphorus removal system according to claim 1, wherein: suspension carriers are added into the first aerobic zone, the Feammox reaction zone and the second aerobic zone, wherein the density of the suspension carriers in the first aerobic zone and the second aerobic zone is 0.95-0.97g/cm3The density of the suspension carrier in the Feammox reaction zone is 0.96-0.98g/cm3The effective specific surface area of the suspension carrier is 450-1200m2/m3。
3. The MBBR-based iron-based autotrophic nitrogen and phosphorus removal system according to claim 1, wherein: the main water inlet pipeline is connected to the tank body at the lower part of the first aerobic zone, and the main water outlet pipeline is connected to the tank body at the upper part of the secondary sedimentation zone; the first aerobic zone is communicated with the primary sedimentation zone through a first interception screen arranged at the upper part of the water outlet end of the first aerobic zone, and the primary sedimentation zone is communicated with the Feammox reaction zone through a second interception screen arranged at the upper part of the water outlet end of the primary sedimentation zone; the Feammox reaction zone and the second aerobic zone are communicated through a third interception screen mesh arranged at the lower part of the water outlet end of the Feammox reaction zone; the second aerobic zone and the Fe autotrophic denitrification zone are communicated with each other through a fourth intercepting screen arranged at the upper part of the water outlet end of the second aerobic zone, the Fe autotrophic denitrification zone and the third aerobic zone are communicated with each other through a fifth intercepting screen arranged at the upper part of the water outlet end of the Fe autotrophic denitrification zone, and the third aerobic zone and the secondary sedimentation zone are communicated with each other through water passing holes arranged at the lower part of the water outlet end of the third aerobic zone.
4. The MBBR-based iron-based autotrophic nitrogen and phosphorus removal system according to claim 1, wherein: and the water inlet ends of the primary sedimentation zone and the Fe autotrophic denitrification zone are respectively provided with a first guide wall and a second guide wall, the upper ends of the first guide wall and the second guide wall are higher than the liquid level in the system, and the distance between the lower ends of the first guide wall and the second guide wall and the bottom of the tank is 10-30% of the depth of the tank.
5. The MBBR-based iron-based autotrophic nitrogen and phosphorus removal system according to claim 1, wherein: the lower parts of the primary settling area and the secondary settling area are respectively provided with a sludge discharge pipeline, and a primary settling area sludge discharge valve and a secondary settling area sludge discharge valve are correspondingly arranged on the respective sludge discharge pipelines.
6. The MBBR-based iron-based autotrophic nitrogen and phosphorus removal system according to claim 1, wherein: and a submersible stirrer is arranged on the inner wall of the tank body of the Feammox reaction zone, and aeration pipelines are arranged at the lower parts of the first aerobic zone, the second aerobic zone and the third aerobic zone.
7. The operation method of the MBBR-based iron-based autotrophic nitrogen and phosphorus removal system according to any one of claims 1-6, comprising the following steps in sequence:
a. the sewage to be treated firstly enters a first aerobic zone, the organic matters in the inlet water are removed by heterotrophic bacteria attached and grown on the suspension carrier under the aeration condition, SS, phosphate and the like in the inlet water and Fe in the reflux liquid3+The flocculating constituent is generated by contact flocculation, and the reflux ratio of the first reflux pipeline is 10-100%;
b. the effluent of the first aerobic zone enters a primary sedimentation zone, and a flocculating constituent is settled and discharged through a sludge discharge pipeline of the primary sedimentation zone;
c. the effluent from the primary sedimentation zone enters a Feammox reaction zone, and Feammox bacteria growing on the suspension carrier are attached to the suspension carrier to carry Fe in the reflux liquid3+Partial NH carried in the feed water is completed as an electron donor4 +Removal of-N and generation of small amounts of NO2 -N, the reflux ratio of the second return line is 50-200%, and the effluent NH of the Feammox reaction zone4 +N is less than 50mg/L, and compared with inlet water, the ammoxidation rate of outlet water of the Feammox reaction zone is more than 50 percent;
d. the effluent of the Feammox reaction zone enters a second aerobic zone, and the residual NH of the raw water is completed through nitrobacteria attached and grown on the suspension carrier4 +-N and NO2 -Removal of-N and generation of NO3 -N, second aerobic zone effluent NH4 +-N＜1.5mg/L；
e. The effluent of the second aerobic zone enters an Fe autotrophic denitrification zone, the deep total nitrogen removal is completed through autotrophic denitrifying bacteria attached and grown on an iron-based fixed bed, and Fe is generated2+The reflux ratio in the Fe autotrophic denitrification zone is 200-400 percent;
f. the effluent of the Fe autotrophic denitrification zone enters a third aerobic zone, and Fe is treated under the aeration condition2+Total oxidation to Fe3+And respectively reflows to the first aerobic zone and the Feammox reaction zone along with the reflow liquid;
g. the effluent of the third aerobic zone enters a secondary sedimentation zone, and the residual Fe carried by the effluent3+And part of the precipitated SS is returned to Fe through a sludge return lineAmmox reaction zone for Fe3+The sludge is recycled, the reflux ratio of the sludge is 10 to 100 percent, the other part of the sludge is discharged through a sludge discharge valve of the secondary sedimentation area, and the supernatant reaches the discharge standard of the sewage and is discharged through a main water outlet pipeline at the upper part of the secondary sedimentation area.
8. The operating method of the MBBR-based iron-based autotrophic nitrogen and phosphorus removal system according to claim 7, wherein: in the step a, the hydraulic retention time in the first aerobic zone is 1-4 h.
9. The operating method of the MBBR-based iron-based autotrophic nitrogen and phosphorus removal system according to claim 7, wherein: the sludge concentration of the Feammox reaction zone, the Fe autotrophic denitrification zone, the first aerobic zone, the second aerobic zone and the third aerobic zone is less than 500 mg/L; the filling rate of the suspended carriers in the first aerobic zone and the second aerobic zone is 30-60%, the DO is 3-6mg/L, the DO in the third aerobic zone is 1-3mg/L, the filling rate of the suspended carriers in the Feammox reaction zone is 10-50%, and the DO in the Feammox reaction zone and the Fe autotrophic denitrification zone is less than 0.4 mg/L.
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