CN112811593B - 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
- Publication number
- CN112811593B CN112811593B CN202110051432.5A CN202110051432A CN112811593B CN 112811593 B CN112811593 B CN 112811593B CN 202110051432 A CN202110051432 A CN 202110051432A CN 112811593 B CN112811593 B CN 112811593B
- Authority
- CN
- China
- Prior art keywords
- zone
- feamox
- aerobic zone
- aerobic
- pipeline
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 198
- 230000001651 autotrophic effect Effects 0.000 title claims abstract description 101
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 54
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 46
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 32
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 21
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 21
- 239000011574 phosphorus Substances 0.000 title claims abstract description 21
- 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 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 104
- 238000006243 chemical reaction Methods 0.000 claims abstract description 88
- 238000004062 sedimentation Methods 0.000 claims abstract description 82
- 239000010802 sludge Substances 0.000 claims abstract description 39
- 239000010865 sewage Substances 0.000 claims abstract description 19
- 238000010992 reflux Methods 0.000 claims description 50
- 239000000725 suspension Substances 0.000 claims description 39
- 239000007788 liquid Substances 0.000 claims description 25
- 238000005273 aeration Methods 0.000 claims description 21
- 241000894006 Bacteria Species 0.000 claims description 16
- 238000007599 discharging Methods 0.000 claims description 16
- 238000011049 filling Methods 0.000 claims description 16
- 239000000969 carrier Substances 0.000 claims description 15
- 238000011010 flushing procedure Methods 0.000 claims description 15
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 14
- 230000003647 oxidation Effects 0.000 claims description 13
- 238000007254 oxidation reaction Methods 0.000 claims description 13
- 239000006228 supernatant Substances 0.000 claims description 8
- 229910021529 ammonia Inorganic materials 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 5
- 229910019142 PO4 Inorganic materials 0.000 claims description 4
- 238000005189 flocculation Methods 0.000 claims description 4
- 230000016615 flocculation Effects 0.000 claims description 4
- 230000014759 maintenance of location Effects 0.000 claims description 4
- 230000001546 nitrifying effect 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
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 2
- 230000008569 process Effects 0.000 description 25
- 244000005700 microbiome Species 0.000 description 5
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- 230000033558 biomineral tissue development Effects 0.000 description 3
- 239000000376 reactant Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 239000000370 acceptor Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 238000003756 stirring Methods 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
- PMVSDNDAUGGCCE-TYYBGVCCSA-L Ferrous fumarate Chemical compound [Fe+2].[O-]C(=O)\C=C\C([O-])=O PMVSDNDAUGGCCE-TYYBGVCCSA-L 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000000872 anti-mineralization Effects 0.000 description 1
- UMEAURNTRYCPNR-UHFFFAOYSA-N azane;iron(2+) Chemical compound N.[Fe+2] UMEAURNTRYCPNR-UHFFFAOYSA-N 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
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 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
- 230000006378 damage Effects 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
- 230000029087 digestion Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 244000144992 flock Species 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
- -1 iron ammonia oxide Chemical compound 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000011159 matrix material Substances 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
- 239000002994 raw material Substances 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000000126 substance Substances 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
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
- C02F3/308—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
Landscapes
- 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 and is discharged through the total water outlet pipeline after sequentially passing through a first aerobic zone, a primary sedimentation zone, a Feamox reaction zone, a second aerobic zone, a Fe autotrophic denitrification zone, a third aerobic zone and a secondary sedimentation zone; the device also comprises a return pipeline arranged between the third aerobic zone and the first aerobic zone as well as between the Feamox reaction zone and a sludge return pipeline between the secondary sedimentation zone and the Feamox reaction zone. The method can realize quick start by combining Feamox 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 denitrification technology is recently rapidly developed as a novel denitrification process, and is paid attention to by researchers in the field of biological denitrification of wastewater worldwide, and the process is performed by anaerobic ammonia oxidation, so that compared with the traditional nitrification and denitrification, 100% of organic carbon source addition can be saved, and therefore, the process is considered to be the most economical and effective biological denitrification mode of wastewater. However, conventional nitrite type anaerobic ammonium oxidation (ANAMMOX) is used for preparing NH 4 + NO is required in the oxidation process 2 - As electron acceptor, it is therefore necessary to combine with the short-cut nitration process. On the one hand, proper aeration is needed to be provided by adding short-cut nitrification, so that the aeration energy consumption is increased; on the other hand, in the operation control process, the problems of out-of-standard water and the like caused by the destruction of a short-cut nitrification effect due to the instability of the system are easily faced, and the control difficulty is increased, so that the nitrite type anaerobic ammonia oxidation is still not realized in large-scale engineering application at present.
Iron acts as the second highest content transition metal in the crust, and its participation in redox reactions drives the biochemical cycle worldwide. Currently, fe-driven autotrophic denitrification processes are also gradually discovered and are attracting attention, mainly including iron-ammonium oxidation (Feamox) and Fe autotrophic denitrification processes.
Feamox is a newly discovered biological denitrification process in recent years. In anaerobic and iron-containing environments, the microorganisms are in Fe 3+ As electron acceptors, with NH 4 + Implementing NH for electron donor 4 + Oxidation of N with simultaneous addition of Fe 3+ Reduction to Fe 2+ Compared with ANAMMOX, feamox does not need to be combined with an aerobic process, can theoretically further reduce aeration energy consumption and reduce operation difficulty, but the Feamox process still has some problems to be solved, such as Fe 3+ Source problems of iron, how to realize recycling, how to stably enrich Feamox microorganisms, and the like.
Fe autotrophic denitrification can utilize Fe and Fe 2+ Etc. as electron donor, NO 2 - Or NO 3 - Reduction to N 2 At the same time Fe, fe 2+ Oxidation to Fe 3+ And researches report that the denitrification rate is higher than that of hydrogen autotrophic denitrification or sulfur autotrophic denitrification, but the Fe autotrophic denitrification has NO in application at present 2 - Or NO 3 - Source of Fe (2) 3+ Is to recover and Fe 3+ Deposition affects mass transfer and the like.
The related research reports of the prior art mainly include:
CN 105271514A discloses a biological denitrification method based on anaerobic iron ammonia oxide, comprising the following steps: adding sludge containing Feamox microorganisms into an anaerobic reactor, introducing ammonia-containing sewage into the reactor, and oxidizing NH in the sewage by Fe (III) 4 + NO generation 2 - Further advanced denitrification treatment is carried out, the invention aims at NO generated by Feamox 2 - The by-product needs to be additionally provided with a deep denitrification process, which increases the process flow and the operation complexity, and relates to Fe 3+ The source of (2) is not illustrated.
CN 109650536A provides a device and method for anaerobic in-situ treatment of ammonia nitrogen based on iron circulation driving, which is characterized in that: nitrate was added to the Feamox system containing iron, causing nitrate dependent iron oxidation (NDFO) by periodically adding NO to the Feamox system 3 - Oxidizing Fe 2+ Fe produced 3+ Continuing to participate in Feamox, fe produced 2+ New NO additionally added 3 - Oxidation is carried out by periodically adding NO 3 - The limited iron will bring about more nitrogen removal. However, the process requires external nitrate addition, on one hand, new nitrogen is introduced, on the other hand, the operation cost is increased, and the deep denitrification process is not realized, and the higher total nitrogen removal can not be realized only by Feamox.
Zhang Ningbo (Zhang Ningbo, li Xiang, huang Yong, etc. zero-valent iron autotrophic denitrification process activated sludge mineralization and solving measures [ J ]. Environmental science, 2017,38 (9): 3793-3800.DOI: 10.13227/j.hjkx.201703032.) by inoculating activated sludge of domestic sewage treatment plant, starting zero-valent iron autotrophic denitrification reaction in an up-flow anaerobic reactor, and wrapping sludge by ferric iron and ferric oxide gradually formed in the operation process, so that the sludge mineralization is caused, the problem of activity reduction is solved, the feasibility study of feeding sludge and changing two anti-mineralization modes of backflow is carried out, a backflow mode is changed, a backflow pool is arranged outside a reaction column, water at the upper part of the backflow pool is utilized for hydraulic circulation and rising flushing, the generated ferric iron and ferric oxide flow out along with effluent and are deposited in an external backflow pool, and the problem of sludge mineralization in long-term operation is solved. However, how to realize the source of the nitrate nitrogen by the process is not studied too much, and the practical application may be hindered.
Therefore, the autotrophic denitrification process using Fe as a reactant has the problems of matrix source, fe element circulation and the like, and the process can only realize denitrification but cannot realize synchronous dephosphorization, 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 through different process coupling, the autotrophic denitrification process taking Fe as a reactant has better application prospect.
Disclosure of Invention
The invention aims to provide an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR, wherein the reaction zone of the system is used for treating sewage in a mode of combining Feamox and iron autotrophic denitrification, and the system has the advantages of simplicity in operation, stable treatment effect, low treatment cost and good impact resistance.
In order to achieve the above purpose, the present 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 Feamox 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 main water inlet pipeline is connected to the tank body of the first aerobic zone, the main water outlet pipeline is connected to the tank body of the secondary sedimentation zone, and water to be treated enters from the main water inlet pipeline and is discharged through the main water outlet pipeline after sequentially passing through the first aerobic zone, the primary sedimentation zone, the Feamox reaction zone, the second aerobic zone, the Fe autotrophic denitrification zone, the third aerobic zone and the secondary sedimentation zone;
a first reflux pipeline is arranged between the first aerobic zone and the third aerobic zone, and reflux liquid flows from the third aerobic zone to the lower part of the first aerobic zone; a second reflux pipeline is arranged between the Feamox reaction zone and the third aerobic zone, and reflux liquid flows from the third aerobic zone to the lower part of the Feamox reaction zone; a reflux pipeline in the Fe autotrophic denitrification region is arranged in the Fe autotrophic denitrification region, and reflux liquid 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 Feamox reaction zone, and return sludge flows from the lower part of the secondary sedimentation zone to the upper part of the Feamox reaction zone;
a water distributor and a back flushing device are arranged at the lower part of the Fe autotrophic denitrification region, and the back flushing device comprises an air flushing pipe and a water flushing pipe;
and an iron-based fixed bed is assembled in the Fe autotrophic denitrification region, the iron-based fixed bed is distributed according to units, and the filling rate of the region filter material 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 Feamox 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/cm 3 The density of the suspension carrier in the Feamox reaction zone is 0.96-0.98g/cm 3 The effective specific surface area of the suspension carrier is 450-1200m 2 /m 3 。
As another preferable scheme of the invention, the total water inlet pipeline is connected to the tank body at the lower part of the first aerobic zone, and the total 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 Feamox reaction zone through a second interception screen arranged at the upper part of the water outlet end of the primary sedimentation zone; the Feamox reaction zone and the second aerobic zone are communicated through a third interception screen arranged at the lower part of the water outlet end of the Feamox reaction zone; the second aerobic zone and the Fe autotrophic denitrification zone are mutually communicated through a fourth interception 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 mutually communicated through a fifth interception 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 mutually communicated through a water passing hole arranged at the lower part of the water outlet end of the third aerobic zone.
Further 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 and the bottom of the pool is 10% -30% of the depth of the pool.
Further preferably, the lower parts of the primary sedimentation zone and the secondary sedimentation zone are respectively provided with a mud discharge pipeline, and the mud discharge pipelines are respectively provided with a mud discharge valve of the primary sedimentation zone and a mud discharge valve of the secondary sedimentation zone.
Preferably, the inner wall of the tank body of the Feamox reaction zone is provided with a submersible stirrer, and the lower parts of the first aerobic zone, the second aerobic zone and the third aerobic zone are respectively provided with an aeration pipeline.
The invention further aims to provide an operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on 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 a suspension carrier under the aeration condition, and SS, phosphate and the like in the inlet water and Fe in the reflux liquid are removed 3+ Generating floccules by contact flocculation, wherein 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 floccules are settled and discharged through a sludge discharge pipeline of the primary sedimentation zone;
c. the effluent of the primary sedimentation zone enters a Feamox reaction zone, and Feamox bacteria growing on a suspension carrier are attached to the suspension carrier to carry Fe in a reflux liquid 3+ Completion of partial NH carried in the incoming water as electron donor 4 + N removal and production of small amounts of NO 2 - -N, the reflux ratio of the second reflux pipeline is 50% -200%, and the water NH is discharged from the Feamox reaction zone 4 + N is less than 50mg/L, and compared with the inlet water, the ammonia oxidation rate of the outlet water of the Feamox reaction zone is more than 50 percent;
d. the effluent of the Feamox reaction zone enters a second aerobic zone, and the residual NH of raw water is completed through nitrifying bacteria attached to and growing on the suspension carrier 4 + -N and NO 2 - -removal of N and generation of NO 3 - -N, second aerobic zone effluent NH 4 + -N＜1.5mg/L；
e. The effluent of the second aerobic zone enters an Fe autotrophic denitrification zone, and the autotrophic denitrification bacteria attached and grown on the iron-based fixed bed are used for removing total nitrogen deeply and generating Fe 2+ The reflux ratio in the Fe autotrophic denitrification area is 200% -400%;
f. the effluent of the Fe autotrophic denitrification zone enters a third aerobic zone, and Fe is added under the aeration condition 2+ All oxygenated to Fe 3+ And respectively refluxing to the first aerobic zone and the Feamox reaction zone along with the reflux liquid;
g. the effluent of the third aerobic zone enters a secondary sedimentation zone, and the residual Fe carried by the effluent 3+ And a part of the precipitated SS is returned to the Feamox reaction zone through a sludge return pipeline to enable Fe to be reacted 3+ And (3) recycling, namely discharging the other part of the sludge through a sludge discharge valve of the secondary sedimentation zone, wherein the supernatant reaches the discharge standard of sewage, and discharging the supernatant through a total water outlet pipeline at the upper part of the secondary sedimentation zone.
Further, in step a, the hydraulic retention time in the first aerobic zone is 1-4h.
Further, the sludge concentration of the Feamox reaction zone, the Fe autotrophic denitrification zone, the first aerobic zone, the second aerobic zone and the third aerobic zone is less than 500mg/L; the filling rate of the suspended carriers in the first aerobic zone and the second aerobic zone is 30-60%, DO in the third aerobic zone is 3-6mg/L, DO in the Feamox reaction zone is 1-3mg/L, the filling rate of the suspended carriers in the Feamox reaction zone is 10-50%, and DO in the Fe autotrophic denitrification zone is less than 0.4mg/L.
Compared with the prior art, the invention has the following beneficial technical effects:
(1) The method has the advantages that the operation cost is saved, feamox and Fe autotrophic denitrification processes are combined to perform high-efficiency autotrophic denitrification, and the addition of 100% of carbon sources can be saved;
(2) And partial Fe generated by denitrification of Fe autotrophy is taken into consideration in denitrification and dephosphorization 3+ The wastewater flows back to the water inlet end to be used as a condensation agent to realize chemical dephosphorization, and simultaneously ensure the removal of nitrogen and phosphorus of a system, thereby realizing one-iron multi-purpose;
(3) The treatment load is high, feamox and iron autotrophic denitrification are both in the form of MBBR, and the carrier is highly enriched with effective strains, so that the treatment load is high.
(4) The first aerobic tank can reduce adverse effects of inflow COD on subsequent Feamox and Fe autotrophic denitrification microorganisms through denitrification, a good environment is created for the biochemical reaction tank, and the Fe autotrophic denitrification effluent can supplement certain alkalinity for the Feamox reaction tank, 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 of the present invention;
in the figure:
1. the device comprises a first aerobic zone, 2, a primary sedimentation zone, 3, a Feamox reaction zone, 4, a second aerobic zone, 5, an Fe autotrophic denitrification zone, 6, a third aerobic zone, 7, a secondary sedimentation zone, 8, an iron-based fixed bed, 9, a water distribution plate, 10, a back flushing device, 11, a suspension carrier, I1, a total water inlet pipeline, I2, a first return pipeline, I3, a second return pipeline, I4, an Fe autotrophic denitrification zone internal return pipeline, I5, a sludge return pipeline, I6, a total water outlet pipeline, S1, a first interception screen, S2, a second interception screen, S3, a third interception screen, S4, a fourth interception screen, S5, a fifth interception screen, C1, a first aerobic zone aeration pipeline, C2, a second aerobic zone aeration pipeline, C3, a third aerobic zone aeration pipeline, M, a submerged agitator, P1, a primary sedimentation zone mud valve, P2, a secondary sedimentation zone mud valve, Q1, a first diversion wall, a second diversion wall and a second diversion wall.
Detailed Description
The invention provides an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and an operation method thereof, and in order to make the advantages and the technical scheme of the invention clearer and more definite, the invention is further described below by combining specific embodiments.
The invention relates to a Moving Bed Biofilm Reactor (MBBR), which refers to a moving bed biofilm reactor MBBR (Moving Bed Biofilm Reactor), and the method utilizes biofilm growing on a suspension carrier to enrich functional microorganisms by adding a certain amount of suspension carrier into the system, so as to improve biomass and biological species in a treatment system, thereby improving the treatment efficiency of the system.
The filling rate refers to the filling rate of the suspension carrier, namely the ratio of the volume of the suspension carrier to the cell capacity of a filling area, wherein the volume of the suspension carrier is the total volume of the suspension carrier in natural accumulation; such as 100m 3 Suspending carrier, filling to 400m 3 Pool volume, filling rate is 25%.
The iron-based fixed bed refers to a fixed bed, wherein reactants filled in the fixed bed mainly take elemental iron as raw materials;
the water distributor and the back flushing device can be realized by referring to the structure and the working method in the prior art.
As a main improvement point of the invention, sewage is treated by combining Feamox with 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 divided into a first aerobic zone 1, a primary sedimentation zone 2, a ferammox reaction zone 3, a second aerobic zone 4, a Fe autotrophic denitrification zone 5, a third aerobic zone 6 and a secondary sedimentation zone 7 from front to back in sequence;
the total water inlet pipeline I1 is used for feeding water into the reaction tank, is connected to the tank body of the first aerobic zone positioned at the lower part, the total water outlet pipeline I6 is connected to the tank body of the second sedimentation zone positioned at the upper part, water to be treated enters from the total water inlet pipeline and sequentially passes through the first aerobic zone, the primary sedimentation zone, the Feamox reaction zone, the second aerobic zone, the Fe autotrophic denitrification zone, the third aerobic zone and the secondary sedimentation zone, and then is discharged through the total water outlet pipeline. The adjacent reaction areas are communicated, the first aerobic area and the primary sedimentation area are communicated through a first interception screen S1 arranged at the upper part of the water outlet end of the first aerobic area, and the primary sedimentation area and the Feamox reaction area are communicated through a second interception screen S2 arranged at the upper part of the water outlet end of the primary sedimentation area; the Feamox 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 Feamox reaction zone; the second aerobic zone and the Fe autotrophic denitrification zone are mutually communicated through a fourth interception 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 mutually communicated through a fifth interception 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 mutually communicated through water holes arranged at the lower part of the water outlet end of the third aerobic zone.
A first reflux pipeline I2 is arranged between the first aerobic zone and the third aerobic zone, and reflux liquid flows from the third aerobic zone to the lower part of the first aerobic zone; a second reflux pipeline I3 is arranged between the Feamox reaction zone and the third aerobic zone, and reflux liquid flows from the third aerobic zone to the lower part of the Feamox reaction zone; a reflux pipeline I4 in the Fe autotrophic denitrification region is arranged in the Fe autotrophic denitrification region, and reflux liquid 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 I5 is arranged between the secondary sedimentation zone and the Feamox reaction zone, and return sludge flows from the lower part of the secondary sedimentation zone to the upper part of the Feamox reaction zone.
The first aerobic zone, the second aerobic zone and the third aerobic zone are respectively provided with a first aerobic zone aeration pipeline C1, a second aerobic zone aeration pipeline C2 and a third aerobic zone aeration pipeline C3, and aeration is carried out to the corresponding aerobic zones through the respective aeration pipelines.
A water distributor and a back flushing device 10 are arranged at the lower part of the Fe autotrophic denitrification region, the water distributor comprises a water distribution plate 9, the water distribution plate 9 can distribute water according to a certain rule, and the back flushing device comprises an air flushing pipe and a water flushing pipe;
and an iron-based fixed bed 8 is assembled in the Fe autotrophic denitrification region, the iron-based fixed bed is distributed according to units, and the filling rate of the region filter material can be changed by placing different unit numbers.
As a preferable scheme of the invention, suspension carriers 11 are added into the first aerobic zone, the Feamox 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/cm 3 The density of the suspension carrier in the Feamox reaction zone is 0.96-0.98g/cm 3 The effective specific surface area of the suspension carrier is 450-1200m 2 /m 3 。
Further, a submersible stirrer M is arranged on the inner wall of the tank body of the Feamox reaction zone and is used for propelling and stirring sewage, so that the stirring function is enhanced;
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 and the bottom of the pool is 10% -30% of the depth of the pool.
Mud discharging pipelines are arranged at the lower parts of the primary sedimentation zone and the secondary sedimentation zone, and a primary sedimentation zone mud discharging valve P1 and a secondary sedimentation zone mud discharging valve P2 are correspondingly arranged on the respective mud discharging pipelines.
The operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on the MBBR is described in detail below.
The method specifically comprises the following steps:
firstly, sewage to be treated firstly enters a first aerobic zone, organic matters in the inlet water are removed through heterotrophic bacteria attached and grown on a suspension carrier under the aeration condition, and SS, phosphate and the like in the inlet water and Fe in a reflux liquid 3+ Contact flocculation occurs to produce flocks. The reflux ratio of the first reflux pipeline is 10% -100%; 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 floccules are settled and discharged through a sludge discharge pipeline of the primary sedimentation zone;
thirdly, the effluent of the primary sedimentation zone enters a Feamox reaction zone, and Feamox bacteria growing on a suspension carrier are attached to the suspension carrier to carry Fe in a reflux liquid 3+ Completion of partial NH carried in the incoming water as electron donor 4 + N removal and production of small amounts of NO 2 - -N, a second return pipeThe reflux ratio of the circuit is 50% -200%. Feamox reaction zone effluent NH 4 + N is less than 50mg/L, and compared with the inlet water, the ammonia oxidation rate of the outlet water of the Feamox reaction zone is more than 50 percent;
fourthly, the effluent of the Feamox reaction zone enters a second aerobic zone, and the residual NH of the raw water is completed through nitrifying bacteria attached to the suspended carrier for growth 4 + -N and NO 2 - -removal of N and generation of NO 3 - -N, second aerobic zone effluent NH 4 + -N＜1.5mg/L；
Fifthly, the effluent of the second aerobic zone enters an Fe autotrophic denitrification zone, deep total nitrogen removal is completed through autotrophic denitrification bacteria attached and grown on an iron-based fixed bed, and Fe is generated 2+ . The reflux ratio in the Fe autotrophic denitrification area is 200% -400%.
Step six, the effluent of the Fe autotrophic denitrification zone enters a third aerobic zone, and Fe is added under the aeration condition 2+ All oxygenated to Fe 3+ And respectively refluxing to the first aerobic zone and the Feamox reaction zone along with the reflux liquid;
seventh, the effluent of the third aerobic zone enters a secondary sedimentation zone, and the residual Fe carried by the effluent 3+ And a part of the precipitated SS is returned to the Feamox reaction zone through a sludge return pipeline to enable Fe to be reacted 3+ And (3) recycling, namely discharging the other part of the sludge through a sludge discharge valve of the secondary sedimentation zone, wherein the supernatant reaches the discharge standard of sewage, and discharging the supernatant through a total water outlet pipeline at the upper part of the secondary sedimentation zone.
Further, the sludge concentration of the Feamox reaction zone, the Fe autotrophic denitrification zone, the first aerobic zone, the second aerobic zone and the third aerobic zone is less than 500mg/L; the filling rate of the suspended carriers in the first aerobic zone and the second aerobic zone is 30-60%, DO in the third aerobic zone is 3-6mg/L, DO in the Feamox reaction zone is 1-3mg/L, the filling rate of the suspended carriers in the Feamox reaction zone is 10-50%, and DO in the Fe autotrophic denitrification zone is less than 0.4mg/L.
The present invention will be described in detail with reference to specific examples.
Example 1:
treating anaerobic sludge digestion supernatant of certain sewage plant by adopting iron-based autotrophic nitrogen and phosphorus removal system based on MBBRWater volume 100m 3 The average water temperature is 29 ℃, the average ammonia nitrogen concentration is 450mg/L, the average COD concentration is 600mg/L, the average BOD5 concentration is 290mg/L, the average TP is 15mg/L, and the average alkalinity (CaCO is used 3 Calculated) 3900mg/L. The depth of the system pool is 4.4m, suspension carriers are added into the first aerobic zone, the Feamox reaction zone and the second aerobic zone of the system, and the density is 0.95g/cm in the first aerobic zone and the second aerobic zone of the system 3 The filling rate of the suspension carriers is 30 percent, and the density of the suspension carriers is 0.97g/cm in a Feamox reaction zone 3 The filling rate of the suspension carrier is 40 percent, and the effective specific surface area of the suspension carrier added by the system is 800m 2 /m 3 . 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 and the bottom of the pool is 0.6m.
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 a suspension carrier under the aeration condition, and SS, phosphate and the like in the inlet water and Fe in the reflux liquid are removed 3+ Generating floccules by contact flocculation, wherein the reflux ratio of the first reflux pipeline is 10%, the hydraulic retention time of the first aerobic zone is 1h, the sludge concentration is 322mg/L, and the DO2.6mg/L;
b. the effluent of the first aerobic zone enters a primary sedimentation zone, and floccules are settled and discharged through a sludge discharge pipeline of the primary sedimentation zone;
c. the effluent of the primary sedimentation zone enters a Feamox reaction zone, and Feamox bacteria growing on a suspension carrier are attached to the suspension carrier to carry Fe in a reflux liquid 3+ Completion of partial NH carried in the incoming water as electron donor 4 + -N removal and NO generation 2 - -N, the second return line return ratio 100%. Feamox reaction zone effluent NH 4 + The ammonia oxidation rate of the effluent water of the Feamox reaction zone is up to 90% compared with that of the inlet water, and the average value of the sludge concentration is 368mg/L;
d. the effluent of the Feamox reaction zone enters a second aerobic zone, and the residual NH of raw water is completed through nitrifying bacteria attached to and growing on the suspension carrier 4 + -N and NO 2 - -removal of N and generation of NO 3 - N, sludge concentration average 377mg/L in the second aerobic zone, DO4.3mg/L, effluent NH 4 + -N means 1.1mg/L;
e. the effluent of the second aerobic zone enters an Fe autotrophic denitrification zone, and the autotrophic denitrification bacteria attached and grown on the iron-based fixed bed are used for removing total nitrogen deeply and generating Fe 2+ . The sludge concentration in the Fe autotrophic denitrification area is 383mg/L, and the internal reflux ratio is 300%;
f. the effluent of the Fe autotrophic denitrification zone enters a third aerobic zone, and Fe is added under the aeration condition 2+ All oxygenated to Fe 3+ And respectively refluxing the reflux liquid to the first aerobic zone and the Feamox reaction zone, wherein the sludge concentration in the third aerobic zone is 401mg/L and the sludge concentration in the third aerobic zone is DO5.5mg/L;
g. the effluent of the third aerobic zone enters a secondary sedimentation zone, and the residual Fe carried by the effluent 3+ And a part of the precipitated SS is returned to the Feamox reaction zone through a sludge return pipeline to enable Fe to be reacted 3+ And (3) recycling, discharging the other part of the sewage through a mud valve of the secondary sedimentation zone, wherein the supernatant reaches the sewage discharge standard, and discharging the sewage through a total water outlet pipeline at the upper part of the secondary sedimentation zone. The ammonia nitrogen and TN, COD, TP of the effluent are respectively 0.6, 6.8, 44.6 and 0.4mg/L.
The parts not described in the invention can be realized by referring to the prior art.
It should be noted that: any equivalent or obvious modifications made by those skilled in the art under the teachings of this specification shall fall within the scope of this invention.
Claims (7)
1. An operation method of an iron-based autotrophic nitrogen and phosphorus removal system based on MBBR uses the iron-based autotrophic nitrogen and phosphorus removal system based on MBBR, which comprises a reaction tank, a total water inlet pipeline and a total water outlet pipeline, and is characterized in that:
the reaction tank is divided into a first aerobic zone, a primary sedimentation zone, a Feamox reaction zone, a second aerobic zone, a Fe autotrophic denitrification zone, a third aerobic zone and a secondary sedimentation zone from front to back in sequence;
the main water inlet pipeline is connected to the tank body of the first aerobic zone, the main water outlet pipeline is connected to the tank body of the secondary sedimentation zone, and water to be treated enters from the main water inlet pipeline and is discharged through the main water outlet pipeline after sequentially passing through the first aerobic zone, the primary sedimentation zone, the Feamox reaction zone, the second aerobic zone, the Fe autotrophic denitrification zone, the third aerobic zone and the secondary sedimentation zone;
suspension carriers are added into the first aerobic zone, the Feamox 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/cm 3 The density of the suspension carrier in the Feamox reaction zone is 0.96-0.98g/cm 3 The effective specific surface area of the suspension carrier is 450-1200m 2 /m 3 ；
A first reflux pipeline is arranged between the first aerobic zone and the third aerobic zone, and reflux liquid flows from the third aerobic zone to the lower part of the first aerobic zone; a second reflux pipeline is arranged between the Feamox reaction zone and the third aerobic zone, and reflux liquid flows from the third aerobic zone to the lower part of the Feamox reaction zone; a reflux pipeline in the Fe autotrophic denitrification region is arranged in the Fe autotrophic denitrification region, and reflux liquid 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 Feamox reaction zone, and return sludge flows from the lower part of the secondary sedimentation zone to the upper part of the Feamox reaction zone;
a water distributor and a back flushing device are arranged at the lower part of the Fe autotrophic denitrification region, and the back flushing device comprises an air flushing pipe and a water flushing pipe;
an iron-based fixed bed is assembled in the Fe autotrophic denitrification region, the iron-based fixed bed is distributed according to units, and the filling rate of the region filter material is changed by placing different unit numbers;
the operation method 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 a suspension carrier under the aeration condition, and SS, phosphate and Fe in the reflux liquid in the inlet water 3+ Generating floccules by contact flocculation, and a first refluxThe reflux ratio of the pipeline is 10% -100%;
b. the effluent of the first aerobic zone enters a primary sedimentation zone, and floccules are settled and discharged through a sludge discharge pipeline of the primary sedimentation zone;
c. the effluent of the primary sedimentation zone enters a Feamox reaction zone, and Feamox bacteria growing on a suspension carrier are attached to the suspension carrier to carry Fe in a reflux liquid 3+ Completion of partial NH carried in the incoming water as electron donor 4 + N removal and production of small amounts of NO 2 - -N, the reflux ratio of the second reflux pipeline is 50% -200%, and the water NH is discharged from the Feamox reaction zone 4 + N is less than 50mg/L, and compared with the inlet water, the ammonia oxidation rate of the outlet water of the Feamox reaction zone is more than 50 percent;
d. the effluent of the Feamox reaction zone enters a second aerobic zone, and the residual NH of raw water is completed through nitrifying bacteria attached to and growing on the suspension carrier 4 + -N and NO 2 - -removal of N and generation of NO 3 - -N, second aerobic zone effluent NH 4 + -N＜1.5mg/L；
e. The effluent of the second aerobic zone enters an Fe autotrophic denitrification zone, and the autotrophic denitrification bacteria attached and grown on the iron-based fixed bed are used for removing total nitrogen deeply and generating Fe 2+ The reflux ratio in the Fe autotrophic denitrification area is 200% -400%;
f. the effluent of the Fe autotrophic denitrification zone enters a third aerobic zone, and Fe is added under the aeration condition 2+ All oxygenated to Fe 3+ And respectively refluxing to the first aerobic zone and the Feamox reaction zone along with the reflux liquid;
g. the effluent of the third aerobic zone enters a secondary sedimentation zone, and the residual Fe carried by the effluent 3+ And a part of the precipitated SS is returned to the Feamox reaction zone through a sludge return pipeline to enable Fe to be reacted 3+ And (3) recycling, namely discharging the other part of the sludge through a sludge discharge valve of the secondary sedimentation zone, wherein the supernatant reaches the discharge standard of sewage, and discharging the supernatant through a total water outlet pipeline at the upper part of the secondary sedimentation zone.
2. The operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on the MBBR as claimed in claim 1, wherein the operation method comprises the following steps: the total water inlet pipeline is connected to the tank body at the lower part of the first aerobic zone, and the total 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 Feamox reaction zone through a second interception screen arranged at the upper part of the water outlet end of the primary sedimentation zone; the Feamox reaction zone and the second aerobic zone are communicated through a third interception screen arranged at the lower part of the water outlet end of the Feamox reaction zone; the second aerobic zone and the Fe autotrophic denitrification zone are mutually communicated through a fourth interception 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 mutually communicated through a fifth interception 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 mutually communicated through a water passing hole arranged at the lower part of the water outlet end of the third aerobic zone.
3. The operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on the MBBR as claimed in claim 1, wherein the operation method comprises the following steps: 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 end and the bottom of the pool is 10% -30% of the depth of the pool.
4. The operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on the MBBR as claimed in claim 1, wherein the operation method comprises the following steps: mud discharging pipelines are arranged at the lower parts of the primary sedimentation zone and the secondary sedimentation zone, and a primary sedimentation zone mud discharging valve and a secondary sedimentation zone mud discharging valve are correspondingly arranged on the respective mud discharging pipelines.
5. The operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on the MBBR as claimed in claim 1, wherein the operation method comprises the following steps: the inner wall of the tank body of the Feamox reaction zone is provided with a submersible stirrer, and the lower parts of the first aerobic zone, the second aerobic zone and the third aerobic zone are respectively provided with an aeration pipeline.
6. The operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on the MBBR as claimed in claim 1, wherein the operation method comprises the following steps: in step a, the hydraulic retention time in the first aerobic zone is 1-4h.
7. The operation method of the iron-based autotrophic nitrogen and phosphorus removal system based on the MBBR as claimed in claim 1, wherein the operation method comprises the following steps: the sludge concentration of the Feamox reaction zone, the Fe autotrophic denitrification zone, the first aerobic zone, the second aerobic zone and the third aerobic zone is less than 500mg/L; the filling rate of the suspended carriers in the first aerobic zone and the second aerobic zone is 30-60%, DO in the third aerobic zone is 3-6mg/L, DO in the Feamox reaction zone is 1-3mg/L, the filling rate of the suspended carriers in the Feamox reaction zone is 10-50%, and DO in the Fe autotrophic denitrification zone is less than 0.4mg/L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110051432.5A CN112811593B (en) | 2021-01-15 | 2021-01-15 | Iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and operation method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110051432.5A CN112811593B (en) | 2021-01-15 | 2021-01-15 | Iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and operation method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112811593A CN112811593A (en) | 2021-05-18 |
| CN112811593B true CN112811593B (en) | 2023-11-28 |
Family
ID=75869319
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110051432.5A Active CN112811593B (en) | 2021-01-15 | 2021-01-15 | Iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and operation method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112811593B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113307448B (en) * | 2021-05-24 | 2022-12-06 | 东华大学 | Underground water denitrification method and reactor of zero-valent iron autotrophic denitrification coupling biochar PRB |
| CN114409101B (en) * | 2022-03-31 | 2022-07-12 | 北京林业大学 | Nitrogen and phosphorus removal sewage treatment system and method based on iron reduction and oxidation circulation |
| CN114804514B (en) * | 2022-04-12 | 2023-08-11 | 北京大学 | Biological denitrification method coupled with iron flocculation process |
| CN114804354A (en) * | 2022-06-24 | 2022-07-29 | 北京涞澈科技发展有限公司 | Biological rotary drum denitrification filter tank and denitrification treatment system based on sulfur autotrophy |
| CN115124142B (en) * | 2022-07-28 | 2024-06-07 | 兰州资源环境职业技术大学 | Device for removing nitrogen in sewage by using ferric ammonium oxidation and denitrification process |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100314311A1 (en) * | 2007-08-08 | 2010-12-16 | Guanghao Peng | Method for removing the contamination of c,n utilizing heterotrophic ammonia-oxidizing bacteria |
| CN105836881A (en) * | 2016-06-04 | 2016-08-10 | 北京工业大学 | Reclaimed water deep denitrification and dephosphorization method based on low C/N ratio |
| CN107162184A (en) * | 2017-06-07 | 2017-09-15 | 南京大学 | A kind of utilization Anammox sulphur autotrophic denitrification couples the UBF reactors and its system and denitrogenation method of denitrogenation |
| CN107253762A (en) * | 2017-07-05 | 2017-10-17 | 扬州大学 | A kind of short-cut denitrification dephosphorization couples the quick start method of Anammox |
| CN109626729A (en) * | 2018-12-26 | 2019-04-16 | 东华大学 | A kind of method that the recycling of sanitary sewage organic matter couples iron autotrophic denitrification/nitrification denitrogenation and dephosphorization |
| CN110386731A (en) * | 2019-08-05 | 2019-10-29 | 青岛思普润水处理股份有限公司 | A kind of mainstream autotrophic denitrification system and method based on MBBR |
| CN110510743A (en) * | 2019-09-26 | 2019-11-29 | 西安建筑科技大学 | A kind of step nitrogen rejection facility and method based on molysite circulation |
| CN111943444A (en) * | 2020-08-19 | 2020-11-17 | 苏州科技大学 | Sewage treatment device and method for enhancing municipal sewage autotrophic nitrogen removal and synchronous phosphorus recovery |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6227509B2 (en) * | 2014-09-08 | 2017-11-08 | 株式会社日立製作所 | Waste water treatment apparatus and waste water treatment method |
-
2021
- 2021-01-15 CN CN202110051432.5A patent/CN112811593B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100314311A1 (en) * | 2007-08-08 | 2010-12-16 | Guanghao Peng | Method for removing the contamination of c,n utilizing heterotrophic ammonia-oxidizing bacteria |
| CN105836881A (en) * | 2016-06-04 | 2016-08-10 | 北京工业大学 | Reclaimed water deep denitrification and dephosphorization method based on low C/N ratio |
| CN107162184A (en) * | 2017-06-07 | 2017-09-15 | 南京大学 | A kind of utilization Anammox sulphur autotrophic denitrification couples the UBF reactors and its system and denitrogenation method of denitrogenation |
| CN107253762A (en) * | 2017-07-05 | 2017-10-17 | 扬州大学 | A kind of short-cut denitrification dephosphorization couples the quick start method of Anammox |
| CN109626729A (en) * | 2018-12-26 | 2019-04-16 | 东华大学 | A kind of method that the recycling of sanitary sewage organic matter couples iron autotrophic denitrification/nitrification denitrogenation and dephosphorization |
| CN110386731A (en) * | 2019-08-05 | 2019-10-29 | 青岛思普润水处理股份有限公司 | A kind of mainstream autotrophic denitrification system and method based on MBBR |
| CN110510743A (en) * | 2019-09-26 | 2019-11-29 | 西安建筑科技大学 | A kind of step nitrogen rejection facility and method based on molysite circulation |
| CN111943444A (en) * | 2020-08-19 | 2020-11-17 | 苏州科技大学 | Sewage treatment device and method for enhancing municipal sewage autotrophic nitrogen removal and synchronous phosphorus recovery |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112811593A (en) | 2021-05-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112811593B (en) | Iron-based autotrophic nitrogen and phosphorus removal system based on MBBR and operation method | |
| CN112158952B (en) | Device and method for treating low-carbon-nitrogen-ratio wastewater through continuous flow AOA (argon oxygen decarburization) shortcut nitrification and anaerobic ammonia oxidation coupling sludge fermentation denitrification | |
| CN110436704B (en) | Urban sewage treatment upgrading and reforming process based on anaerobic ammonia oxidation | |
| CN107010736B (en) | Device and method for coupling short-cut denitrification-anaerobic ammonia oxidation denitrification with biological phosphorus removal | |
| CN110510739B (en) | Device and method for realizing semi-short-range coupling anaerobic ammonia oxidation of continuous flow AOA (argon oxygen decarburization) biomembrane through hydroxylamine | |
| CN103787498B (en) | Rapid starting method of low-temperature low C/N sewage improvement A2/O process | |
| CN109970200B (en) | Device and method for treating urban domestic sewage based on coupling of short-cut denitrification dephosphorization and anaerobic ammonia oxidation | |
| CN110028158B (en) | Method and device for endogenous short-cut denitrification coupling anaerobic ammonia oxidation nitrogen and phosphorus removal of municipal domestic sewage | |
| CN103936229A (en) | Municipal sewage improved A2/O enhanced denitrification and dephosphorization treatment device and process | |
| CN109896628B (en) | Device and method for deep denitrification by AOA (PD-ANAMMOX) biomembrane technology | |
| CN112897696B (en) | Device and method for biological nitrogen and phosphorus removal based on staged water inflow | |
| CN103663696A (en) | Membrane bio-reactor (MBR) used for treating preserved szechuan pickle wastewater and reinforcing biological phosphorous and nitrogen removal | |
| CN101654300A (en) | Biological full-denitrification treatment technology for 'F/O/F' coking wastewater | |
| CN101182072B (en) | Method for sludge decrement by using endogenous denitrification denitrification dephosphorization and reaction system | |
| CN108083581B (en) | A kind of low energy consumption autotrophic denitrification municipal sewage system and method | |
| CN201240944Y (en) | Facultative aerobic / aerobic / facultative aerobic coking waste water biological full denitrification processing device | |
| CN107417047B (en) | Device and method for complete denitrification and synchronous phosphorus recovery | |
| CN110171904B (en) | Continuous flow AAO dephosphorization and partial denitrification series-connection combined type fixed biological membrane activated sludge autotrophic denitrification device and method | |
| CN105923771A (en) | Self-circulation biological denitrification reactor | |
| CN105084536A (en) | Biologically enhanced treatment method for medium-and-low concentration ammonia-nitrogen wastewater | |
| CN209024270U (en) | A kind of double dirt water treatment systems of synchronous denitrification denitrogenation dephosphorizing | |
| CN102491602A (en) | Sequencing batch domestic sewage treatment method for forcibly denitrifying and dephosphorizing, and recycling phosphorus | |
| CN114409082A (en) | High-ammonia-nitrogen and low-carbon-nitrogen-ratio sewage wastewater OAO coupling zero-valent iron nitrogen and phosphorus removal method | |
| Lin et al. | Solving the problem of high concentration aniline inhibiting nitrogen removal: starting the SBBR with the prolonged aeration mode | |
| CN214270372U (en) | Iron-based autotrophic nitrogen and phosphorus removal system based on MBBR |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20231025 Address after: The entire factory building at No. 155 Yanhe Road, Huangdao District, Qingdao City, Shandong Province, 266500 Applicant after: QINGDAO SPRING WATER TREATMENT Co.,Ltd. Applicant after: Qingdao Sipurun Intelligent System Co.,Ltd. Applicant after: Qingdao Sipurun Water Environmental Technology Co.,Ltd. Address before: No. 155, Yanhe Road, Huangdao District, Qingdao City, Shandong Province 266500 Applicant before: QINGDAO SPRING WATER TREATMENT Co.,Ltd. |
|
| TA01 | Transfer of patent application right | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |