CN116253433A - Sewage efficient denitrification and dephosphorization process and system based on iron biochemical conversion - Google Patents
Sewage efficient denitrification and dephosphorization process and system based on iron biochemical conversion Download PDFInfo
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 title claims abstract description 159
- 239000010865 sewage Substances 0.000 title claims abstract description 84
- 229910052742 iron Inorganic materials 0.000 title claims abstract description 53
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 34
- 230000008569 process Effects 0.000 title claims abstract description 31
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 33
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 22
- 239000011259 mixed solution Substances 0.000 claims abstract description 16
- 239000004575 stone Substances 0.000 claims abstract description 15
- 238000010992 reflux Methods 0.000 claims abstract description 12
- 239000013078 crystal Substances 0.000 claims abstract description 10
- 230000000694 effects Effects 0.000 claims abstract description 8
- 239000012528 membrane Substances 0.000 claims abstract description 8
- 238000007599 discharging Methods 0.000 claims abstract description 5
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 45
- 229910052698 phosphorus Inorganic materials 0.000 claims description 45
- 239000011574 phosphorus Substances 0.000 claims description 45
- 229910019142 PO4 Inorganic materials 0.000 claims description 28
- 239000010452 phosphate Substances 0.000 claims description 28
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 28
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 20
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 18
- QYTBWVFCSVDTEC-UHFFFAOYSA-N azane;iron Chemical compound N.[Fe] QYTBWVFCSVDTEC-UHFFFAOYSA-N 0.000 claims description 17
- 238000007254 oxidation reaction Methods 0.000 claims description 15
- 241000894006 Bacteria Species 0.000 claims description 12
- 241001453382 Nitrosomonadales Species 0.000 claims description 12
- 230000001105 regulatory effect Effects 0.000 claims description 12
- 230000014759 maintenance of location Effects 0.000 claims description 10
- 238000006722 reduction reaction Methods 0.000 claims description 10
- 229910021529 ammonia Inorganic materials 0.000 claims description 9
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 8
- 230000001590 oxidative effect Effects 0.000 claims description 8
- 230000003301 hydrolyzing effect Effects 0.000 claims description 6
- 150000002505 iron Chemical class 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 239000002351 wastewater Substances 0.000 claims description 6
- 229960004887 ferric hydroxide Drugs 0.000 claims description 5
- IEECXTSVVFWGSE-UHFFFAOYSA-M iron(3+);oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Fe+3] IEECXTSVVFWGSE-UHFFFAOYSA-M 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 230000009467 reduction Effects 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 230000001360 synchronised effect Effects 0.000 claims description 5
- 244000005700 microbiome Species 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000000969 carrier Substances 0.000 claims description 2
- 239000000945 filler Substances 0.000 claims description 2
- 238000001179 sorption measurement Methods 0.000 claims description 2
- 230000009466 transformation Effects 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 2
- 230000003647 oxidation Effects 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 229910052799 carbon Inorganic materials 0.000 description 8
- 238000011084 recovery Methods 0.000 description 8
- 239000010802 sludge Substances 0.000 description 8
- 238000002425 crystallisation Methods 0.000 description 5
- 230000008025 crystallization Effects 0.000 description 5
- 238000005273 aeration Methods 0.000 description 3
- 230000001651 autotrophic effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000012851 eutrophication Methods 0.000 description 2
- 238000000855 fermentation Methods 0.000 description 2
- 230000004151 fermentation Effects 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 229910002588 FeOOH Inorganic materials 0.000 description 1
- 238000002441 X-ray diffraction Methods 0.000 description 1
- CUPCBVUMRUSXIU-UHFFFAOYSA-N [Fe].OOO Chemical compound [Fe].OOO CUPCBVUMRUSXIU-UHFFFAOYSA-N 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 230000001939 inductive effect Effects 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910021519 iron(III) oxide-hydroxide Inorganic materials 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 230000000153 supplemental effect Effects 0.000 description 1
- 239000002699 waste material Substances 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
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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
- C02F3/302—Nitrification and denitrification treatment
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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
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- 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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Abstract
The invention discloses a sewage high-efficiency denitrification and dephosphorization process and system based on iron biochemical conversion, comprising the following steps: s1: fe is added to II Putting into an aerobic MBR tank; s2: fe-containing reaction generated by aerobic MBR tank III The mixed solution is respectively input into an anaerobic tank I and an anaerobic tank II; s3: continuously introducing sewage into the anaerobic tank I through the water inlet and refluxing the sewage from the aerobic MBR tank with Fe III Mixing the mixed solution for reaction to form blue iron stone crystals; s4: introducing sewage after the reaction of the anaerobic tank I into the anaerobic tank II, and refluxing with the Fe-containing sewage from the aerobic MBR tank III 、NO 2 ‑ 、NO 3 ‑ The mixed liquor reaction further reduces the nitrogen concentration in the sewage and forms blueCrystallization of the iron stone; s5: and (3) introducing the effluent of the anaerobic tank II into an aerobic MBR tank for further denitrification and dephosphorization, and discharging the treated sewage from a water outlet after mud-water separation by a membrane assembly. The sewage high-efficiency denitrification and dephosphorization system comprises an anaerobic tank I, an anaerobic tank II, an aerobic MBR tank and an iron adding device. The system has low energy consumption in operation and has high-efficiency and stable denitrification and dephosphorization effects.
Description
Technical Field
The invention relates to the field of environmental engineering water treatment, in particular to a sewage high-efficiency denitrification and dephosphorization process and system based on iron biochemical conversion.
Background
In the global area, eutrophication caused by nitrogen and phosphorus pollution in aquatic ecosystems has become a serious environmental problem due to the excessive use of nitrogen and phosphorus fertilizers in agricultural activities and the large input of nitrogen and phosphorus elements caused by the discharge of industrial wastewater and domestic sewage. On the other hand, phosphorus is one of the elements indispensable for maintaining vital activities and modern agricultural production, and is also a nonmetallic mineral resource which is difficult to regenerate, and the reserves of phosphorus ores are very limited. Under such circumstances, the sewage treatment technology has gradually progressed to the direction of high-efficiency denitrification and dephosphorization while recovering phosphorus. According to measurement and calculation, the phosphorus recovery of the urban sewage can meet 15% -20% of phosphorus ore demands in the global scope. Therefore, the removal of nitrogen and phosphorus from sewage and the realization of phosphorus recovery become one of the key links for preventing and treating water eutrophication and realizing sewage recycling.
Biological denitrification and dephosphorization are commonly adopted in current sewage treatment plants, traditional biological denitrification comprises processes such as nitrification and denitrification, wherein the nitrification needs to be carried out through long-time aeration of an aerobic tank to finish the ammoxidation process of autotrophic nitrifying bacteria, and the denitrification needs organic carbon as an electron donor. Biological phosphorus removal utilizes the phosphorus release and excessive phosphorus absorption effects of phosphorus accumulating bacteria, and realizes the removal of phosphorus by discharging phosphorus-rich sludge. Both denitrifying bacteria and phosphorus accumulating bacteria require carbon sources, but the carbon sources in town sewage often cannot meet the requirements, so that high-efficiency removal of nitrogen and phosphorus is difficult to realize, and additional carbon sources are often required to be added, so that the sewage treatment cost is increased. Meanwhile, the phosphorus-rich sludge generated in the process needs subsequent safe disposal, and the effective recovery of phosphorus cannot be realized, so that phosphorus resource waste is caused. At present, the phosphorus recovery project of urban sewage treatment plants at home and abroad is mainly based on the reinforced biological phosphorus removal process, takes surplus sludge as an object, recovers phosphorus from sludge concentration and fermentation supernatant, and mainly belongs to the side flow recovery technology.
Disclosure of Invention
The invention provides a sewage treatment process and a system for co-denitrification and dephosphorization by ferric ammonia oxidation and blue iron stone crystallization, which are used for overcoming the defects that the prior art has insufficient carbon source of sewage, high energy consumption and complex sludge treatment and cannot realize efficient recovery of phosphorus.
Therefore, the invention provides a sewage high-efficiency denitrification and dephosphorization process and system based on iron biochemical conversion. The technical scheme of the invention is realized in such a way that the sewage high-efficiency denitrification and dephosphorization process based on the biochemical conversion of iron comprises the following steps:
s1: sewage sequentially passes through an anaerobic tank I and an anaerobic tank II to be treated, then enters an aerobic MBR tank, and Fe is fed into an iron feeding device II Putting into the aerobic MBR tank, and Fe II Oxidized to Fe III And hydrolyzing to generate ferric hydroxide to adsorb the soluble phosphate;
s2: fe-containing reaction generated by aerobic MBR tank III The mixed liquid is respectively input into an anaerobic tank I and an anaerobic tank II through a return pipe I and a return pipe II;
s3: continuously introducing new sewage into the anaerobic tank I through the water inlet, wherein the new sewage and the Fe-containing sewage flowing back from the aerobic MBR tank III Fully contacting the mixed solution with Fe III Carrying out reduction reaction of iron dissimilate with organic matters in the new sewage, and denitrifying ammonia nitrogen in the sewage through iron ammonia oxidation reaction, and Fe III Reduction of Fe by microorganisms II The method comprises the steps of carrying out a first treatment on the surface of the At the same time, contain Fe III The phosphate in the mixed solution is released, and the phosphate in the mixed sewage is jointly mixed with the Fe II The blue iron stone crystals are formed by combination to achieve the effect of dephosphorization;
s4: introducing sewage after the reaction of the anaerobic tank I in the step S3 into an anaerobic tank II, and refluxing with the Fe-containing sewage from an aerobic MBR tank III 、NO 2 - 、NO 3 - The mixed solution reacts, and under the action of iron ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria in the anaerobic tank II, the anaerobic tank I is not treatedThe nitrogen concentration in the sewage is further reduced by the ammonia nitrogen through ferric ammonia oxidation reaction and anaerobic ammonia oxidation reaction, and Fe is generated by the reaction II Unreacted Fe in the mixed anaerobic tank I II Forming blue iron stone crystals by combining with phosphate in water;
s5: introducing the effluent after the S4 reaction into an aerobic MBR tank, wherein the residual ammonia nitrogen in the effluent is oxidized into NO 2- And NO 3- Partially converting ammonia nitrogen into nitrogen through synchronous nitrification and denitrification processes to complete denitrification; meanwhile, fe carried in the effluent II And Fe supplemented by an iron adding device II Oxidizing the mixture into Fe in an aerobic MBR tank III ，Fe III And (3) hydrolyzing and adsorbing residual soluble phosphate in the water, separating mud from water of the treated sewage by a membrane assembly, and discharging the sewage from a water outlet.
Preferably, fe as described in S1 II The mol ratio of the iron salt to the phosphorus in the sewage is 1:1-2:1, and the removal of nitrogen and phosphorus is regulated and controlled by changing the adding amount of the iron salt.
Preferably, the Fe-containing material in S2 flows back from the aerobic MBR tank III The mixed solution contains dissolved phosphate of ferric hydroxide through chemical adsorption and dissolved phosphate of phosphorus accumulating bacteria through biological absorption, and the Fe-containing material III The reflux ratio of the mixed solution is 60% -100%.
Preferably, the Fe-containing material described in S2 III The mixed liquor is respectively input into the anaerobic tank I and the anaerobic tank II through the return pipe I and the return pipe II, the sludge quantity ratio is 1:1-1:2, and the dominant reaction in the anaerobic tank I is regulated and controlled to be the reduction reaction of the iron oxide and the dominant reaction in the anaerobic tank II is regulated and controlled to be the ammoxidation reaction of the iron by regulating the quantity of the mixed liquor which flows back into the anaerobic tank I and the anaerobic tank II.
Preferably, the hydraulic retention time of the anaerobic tank I is 2-3h, the hydraulic retention time of the anaerobic tank II is 2-4h, and the hydraulic retention time of the aerobic MBR tank is 0.5-2h.
The invention further aims at providing a sewage high-efficiency denitrification and dephosphorization system which comprises an anaerobic tank I (2), an anaerobic tank II (3), an aerobic MBR tank (4) and an iron adding device (5), wherein one end of the anaerobic tank I (2) is connected with a water inlet (1), the other end of the anaerobic tank I is communicated with the anaerobic tank II (3) through a pipeline I (9), the anaerobic tank II (3) is communicated with the aerobic MBR tank (4) through a pipeline II (10), the aerobic MBR tank (4) is communicated with a water outlet (6), the iron adding device (5) and a membrane assembly are arranged on the aerobic MBR tank (4), and the aerobic MBR tank (4) is respectively communicated with the anaerobic tank I (2) and the anaerobic tank II (3) through a return pipe I (8) and a return pipe II (7).
Preferably, the anaerobic tanks I (2) and II (3) are internally provided with biological carrier fillers, and the biological carriers are enriched with iron ammonia oxidizing bacteria and iron dissimilatory reducing bacteria; the abundance ratio of the iron dissimilatory reducing bacteria enriched by the biological carrier in the anaerobic tank I (2) is higher; the abundance ratio of the iron ammonia oxidizing bacteria enriched by the biological carrier in the anaerobic tank II (3) is higher.
The invention has the beneficial effects that: (1) the invention has good denitrification and dephosphorization effects, can obviously improve the removal rate and stability of nitrogen and phosphorus in the sewage treatment effluent, and the concentration of phosphorus in the sewage effluent can be lower than 0.2mg/L, and the total nitrogen concentration can be lower than 15mg/L, thereby reaching the first-level A standard or the surface quasi-IV water quality standard in the pollutant emission standard of urban sewage treatment plants in China; (2) the invention adopts autotrophic processes such as iron ammonia oxidation and the like to realize denitrification, wherein ammonia nitrogen is removed and Fe is removed II The generation of the waste water does not need to consume a carbon source, so that after organic matters are partially removed in the anaerobic tank I and the anaerobic tank II through the reduction and fermentation processes of the iron oxide, the residual organic matters can provide the carbon source for the synchronous nitrification and denitrification process of the aerobic tank, and the problem that the traditional nitrification and denitrification process needs to be additionally provided with the carbon source is avoided; (3) the ammonia nitrogen in the sewage is mainly removed through iron ammonia oxidation and iron ammonia oxidation-anaerobic ammonia oxidation reaction, and only a small amount of ammonia nitrogen enters the aerobic tank, so that the main purpose of aeration of the aerobic tank is to aerate Fe II Oxidation to Fe III Compared with the traditional nitrification and denitrification process, the aeration intensity and time of the invention are greatly reduced, and the operation energy consumption of the system is saved; (4) the invention adds Fe into the aerobic tank II The amorphous FeOOH generated by oxidation absorbs and carries phosphorus to an anaerobic tank, and passes through Fe III And reducing and inducing the in-situ crystallization of the blue iron stone to realize dephosphorization. Wherein Fe is II The generation of Fe is coupled with the ammonia oxidation of Fe to realize the cascade utilization of Fe; (5) compared with the traditional side-flow chemical crystallization, the invention can realize in-situ continuous removal and recovery of sewageThe phosphorus in (3) does not need to be provided with a side stream phosphorus release device and a crystallization device, thereby reducing the operation cost. Meanwhile, the added ferric salt is a common chemical agent for chemical dephosphorization of a sewage treatment plant, and the dosage is less than that of the conventional chemical dephosphorization, i.e. the sewage treatment cost is not increased. In addition, fe is added II Can be recovered by the crystallization of the blue iron stone, thereby further producing economic benefit.
Drawings
FIG. 1 is a schematic flow chart of a sewage high-efficiency denitrification and dephosphorization process based on iron biochemical conversion;
FIG. 2 is a schematic diagram of a sewage high-efficiency denitrification and dephosphorization system;
FIG. 3 is a photograph and XRD pattern of the phosphorus recovery product of the treatment process of the present invention, blue iron stone.
1. A water inlet; 2. an anaerobic tank I; 3. an anaerobic tank II; 4. an aerobic MBR tank; 5. an iron adding device; 6. a water outlet; 7. a return pipe II; 8. a return pipe I; 9. a pipeline I; 10. pipeline II.
Detailed Description
This patent is described in further detail below in conjunction with examples. The examples are merely exemplary and do not limit the scope of the invention in any way, and modifications and substitutions may be made in the details and form of the technical solution of the invention without departing from the scope of the invention, but these modifications and substitutions fall within the scope of the invention.
A sewage high-efficiency denitrification and dephosphorization process based on iron biochemical conversion comprises the following steps:
s1: sewage sequentially passes through an anaerobic tank I and an anaerobic tank II to be treated, then enters an aerobic MBR tank, and Fe is fed into an iron feeding device II Putting into the aerobic MBR tank, and Fe II Oxidized to Fe III And hydrolyzing to generate ferric hydroxide to adsorb the soluble phosphate; fe (Fe) II The mol ratio of the iron salt to the phosphorus in the sewage is 1:1-2:1, and the removal of nitrogen and phosphorus is regulated and controlled by changing the adding amount of the iron salt;
s2: fe-containing reaction generated by aerobic MBR tank III The mixed liquid is respectively input into an anaerobic tank I and an anaerobic tank II through a return pipe I and a return pipe II; the Fe-containing material flows back from the aerobic MBR tank III Mixed liquid middle bagSoluble phosphate by chemisorption containing iron oxyhydroxide and soluble phosphate by bioabsorption containing phosphorus accumulating bacteria, said Fe containing III The reflux ratio of the mixed solution is 60% -100%. The Fe-containing alloy contains III The mixed liquor is respectively input into the anaerobic tank I and the anaerobic tank II through the return pipe I and the return pipe II, the sludge quantity ratio is 1:1-1:2, and the dominant reaction in the anaerobic tank I is regulated and controlled to be the reduction reaction of the iron oxide and the dominant reaction in the anaerobic tank II is regulated and controlled to be the ammoxidation reaction of the iron by regulating the quantity of the mixed liquor which flows back into the anaerobic tank I and the anaerobic tank II.
S3: continuously introducing new sewage into the anaerobic tank I through the water inlet, wherein the new sewage and the Fe-containing sewage flowing back from the aerobic MBR tank III Fully contacting the mixed solution with Fe III Carrying out reduction reaction of iron dissimilate with organic matters in the new sewage, and denitrifying ammonia nitrogen in the sewage through iron ammonia oxidation reaction, and Fe III Reduction of Fe by microorganisms II The method comprises the steps of carrying out a first treatment on the surface of the At the same time, contain Fe III The phosphate in the mixed solution is released, and the phosphate in the mixed sewage is jointly mixed with the Fe II The blue iron stone crystals are formed by combination to achieve the effect of dephosphorization; the hydraulic retention time of the anaerobic tank I is 2-3h.
S4: introducing sewage after the reaction of the anaerobic tank I in the step S3 into an anaerobic tank II, and refluxing with the Fe-containing sewage from an aerobic MBR tank III 、NO 2 - 、NO 3 - The mixed solution reacts, under the action of iron ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria in the anaerobic tank II, the untreated ammonia nitrogen in the anaerobic tank I further reduces the nitrogen concentration in the sewage through the iron ammonia oxidizing reaction and the anaerobic ammonia oxidizing reaction, and Fe is generated by the reaction II Unreacted Fe in the mixed anaerobic tank I II Forming blue iron stone crystals by combining with phosphate in water; the hydraulic retention time of the anaerobic tank II is 2-4h.
S5: introducing the effluent after the S4 reaction into an aerobic MBR tank, wherein the residual ammonia nitrogen in the effluent is oxidized into NO 2- And NO 3- Partially converting ammonia nitrogen into nitrogen through synchronous nitrification and denitrification processes to complete denitrification; meanwhile, fe carried in the effluent II And Fe supplemented by an iron adding device II Oxidizing the mixture into Fe in an aerobic MBR tank III ，Fe III And (3) hydrolyzing and adsorbing residual soluble phosphate in the water, separating mud from water of the treated sewage by a membrane assembly, and discharging the sewage from a water outlet. The hydraulic retention time of the aerobic MBR tank is 0.5-2h.
Example 1
The specific water quality of the treated domestic sewage is as follows: COD concentration is 380mg/L, PO 4 The concentration of P is 3.4mg/L, TN is 40-50mg/L, NH 4+ The concentration of N is 30-40mg/L. The hydraulic retention time of the aerobic MBR tank is set to be 2 hours, and FeSO is added into the aerobic MBR tank 4 By letting Fe II The molar ratio of the total phosphorus in the domestic sewage is 1.5:1. The aerobic MBR pool flows back to the anaerobic pool I and the anaerobic pool II to contain Fe III The reflux ratio of the sludge was 66%, wherein the reflux ratio to both anaerobic tank I and anaerobic tank II was 33%.
(1) Sewage firstly enters an anaerobic tank I, and Fe flows back from an aerobic MBR tank III Reducing iron dissimilate with organic matters, simultaneously ammonia oxidizing and denitrifying ammonia nitrogen in ammonia nitrogen generated in the inflow water, and Fe III Reduction of Fe by microorganisms II . Meanwhile, fe III Phosphate adsorbed in the aerobic MBR pool and phosphate enriched by the phosphorus accumulating bacteria are released, and the released phosphate, phosphate in sewage and generated Fe II Combining to form a blue iron stone crystal;
(2) The effluent enters an anaerobic tank II, and under the existence of iron ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria, the rest ammonia nitrogen and Fe flowing back from an aerobic MBR tank III And NO 2- 、NO 3- The reaction further reduces the nitrogen concentration in the sewage through the processes of iron ammonia oxidation and anaerobic ammonia oxidation, and Fe is generated by the reaction II Fe remaining from anaerobic tank I II Further forming blue iron stone crystals by combining with phosphate in water;
(3) The effluent enters an aerobic MBR tank, on one hand, the residual ammonia nitrogen in the water is oxidized into NO 2- 、NO 3- And converting ammonia nitrogen into nitrogen to complete denitrification partially through synchronous nitrification and denitrification processes. Fe from anaerobic tank II II And supplemental Fe II Fe generated by oxidation in aerobic MBR (Membrane biological reactor) III Adsorbing residual soluble phosphate in water and further reducing phosphate in effluentThe concentration of the effluent is improved, and the effluent is discharged after mud-water separation by a membrane module in an aerobic MBR tank.
After the process is operated stably, the effluent PO 4 -P≤0.2mg/L，TN≤15mg/L，NH 4 + N is less than or equal to 5mg/L, COD is less than or equal to 50mg/L, and meets the first-level A standard in pollutant emission standards of urban sewage treatment plants in China. Precipitated particles in the anaerobic tank were analyzed by XRD and determined to be blue iron stone crystals.
Claims (7)
1. A sewage high-efficiency denitrification and dephosphorization process based on iron biochemical conversion comprises the following steps:
s1: sewage sequentially passes through an anaerobic tank I and an anaerobic tank II to be treated, then enters an aerobic MBR tank, and Fe is fed into an iron feeding device II Putting into the aerobic MBR tank, and Fe II Oxidized to Fe III And hydrolyzing to generate ferric hydroxide to adsorb the soluble phosphate;
s2: fe-containing reaction generated by aerobic MBR tank III The mixed liquid is respectively input into an anaerobic tank I and an anaerobic tank II through a return pipe I and a return pipe II;
s3: continuously introducing new sewage into the anaerobic tank I through the water inlet, wherein the new sewage and the Fe-containing sewage flowing back from the aerobic MBR tank III Fully contacting the mixed solution with Fe III Carrying out reduction reaction of iron dissimilate with organic matters in the new sewage, and denitrifying ammonia nitrogen in the sewage through iron ammonia oxidation reaction, and Fe III Reduction of Fe by microorganisms II The method comprises the steps of carrying out a first treatment on the surface of the At the same time, contain Fe III The phosphate in the mixed solution is released, and the phosphate in the mixed sewage is jointly mixed with the Fe II The blue iron stone crystals are formed by combination to achieve the effect of dephosphorization;
s4: introducing sewage after the reaction of the anaerobic tank I in the step S3 into an anaerobic tank II, and refluxing with the Fe-containing sewage from an aerobic MBR tank III 、NO 2 - 、NO 3 - The mixed solution reacts, under the action of iron ammonia oxidizing bacteria and anaerobic ammonia oxidizing bacteria in the anaerobic tank II, the untreated ammonia nitrogen in the anaerobic tank I further reduces the nitrogen concentration in the sewage through the iron ammonia oxidizing reaction and the anaerobic ammonia oxidizing reaction, and Fe is generated by the reaction II Unreacted Fe in the mixed anaerobic tank I II Forming blue iron stone crystals by combining with phosphate in water;
s5: introducing the effluent after the S4 reaction into an aerobic MBR tank, wherein the residual ammonia nitrogen in the effluent is oxidized into NO 2- And NO 3- Partially converting ammonia nitrogen into nitrogen through synchronous nitrification and denitrification processes to complete denitrification; meanwhile, fe carried in the effluent II And Fe supplemented by an iron adding device II Oxidizing the mixture into Fe in an aerobic MBR tank III ，Fe III And (3) hydrolyzing and adsorbing residual soluble phosphate in the water, separating mud from water of the treated sewage by a membrane assembly, and discharging the sewage from a water outlet.
2. The efficient denitrification and dephosphorization process for wastewater based on iron biochemical transformation according to claim 1, wherein the Fe in S1 is as follows II The mol ratio of the iron salt to the phosphorus in the sewage is 1:1-2:1, and the removal of nitrogen and phosphorus is regulated and controlled by changing the adding amount of the iron salt.
3. The efficient denitrification and dephosphorization process for wastewater based on iron biochemical conversion according to claim 1, wherein the process in S2 is characterized in that the wastewater is fed back from an aerobic MBR tank and contains Fe III The mixed solution contains dissolved phosphate of ferric hydroxide through chemical adsorption and dissolved phosphate of phosphorus accumulating bacteria through biological absorption, and the Fe-containing material III The reflux ratio of the mixed solution is 60% -100%.
4. The efficient denitrification and dephosphorization process for wastewater based on iron biochemical conversion according to claim 1, wherein the Fe-containing wastewater in S2 is III The mixed liquid is respectively input into the anaerobic tank I and the anaerobic tank II through the return pipe I and the return pipe II in a ratio of 1:1-1:2, and the dominant reaction in the anaerobic tank I is regulated and controlled to be the reduction reaction of the iron oxide and the dominant reaction in the anaerobic tank II is regulated and controlled to be the ammoxidation reaction of the iron by regulating the quantity of the mixed liquid which flows back into the anaerobic tank I and the anaerobic tank II.
5. The efficient denitrification and dephosphorization process for sewage based on iron biochemical conversion according to claim 1, wherein the hydraulic retention time of the anaerobic tank I is 2-3h, the hydraulic retention time of the anaerobic tank II is 2-4h, and the hydraulic retention time of the aerobic MBR tank is 0.5-2h.
6. The sewage high-efficiency nitrogen and phosphorus removal system based on the sewage high-efficiency nitrogen and phosphorus removal process of iron biochemical conversion is characterized by comprising an anaerobic tank I (2), an anaerobic tank II (3), an aerobic MBR tank (4) and an iron adding device (5), wherein one end of the anaerobic tank I (2) is connected with a water inlet (1), the other end of the anaerobic tank I is communicated with the anaerobic tank II (3) through a pipeline I (9), the anaerobic tank II (3) is communicated with the aerobic MBR tank (4) through a pipeline II (10), the aerobic MBR tank (4) is communicated with a water outlet (6), the iron adding device (5) and a membrane assembly are arranged on the aerobic MBR tank (4), and the aerobic MBR tank (4) is respectively communicated with the anaerobic tank I (2) and the anaerobic tank II (3) through a reflux pipe I (8) and a reflux pipe II (7).
7. The sewage high-efficiency nitrogen and phosphorus removal system according to claim 6, wherein the anaerobic tank I (2) and the anaerobic tank II (3) are internally provided with biological carrier fillers, and the biological carriers are enriched with iron ammonia oxidizing bacteria and iron dissimilatory reducing bacteria; the abundance ratio of the iron dissimilatory reducing bacteria enriched by the biological carrier in the anaerobic tank I (2) is higher; the abundance ratio of the iron ammonia oxidizing bacteria enriched by the biological carrier in the anaerobic tank II (3) is higher.
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