CN112299560A - Continuous flow denitrification dephosphorization series anaerobic ammonia oxidation coupling endogenous denitrification sewage treatment system and method - Google Patents
Continuous flow denitrification dephosphorization series anaerobic ammonia oxidation coupling endogenous denitrification sewage treatment system and method Download PDFInfo
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 96
- 239000010865 sewage Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 51
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 48
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 46
- 230000003647 oxidation Effects 0.000 title claims abstract description 46
- 230000008878 coupling Effects 0.000 title description 16
- 238000010168 coupling process Methods 0.000 title description 16
- 238000005859 coupling reaction Methods 0.000 title description 16
- 239000010802 sludge Substances 0.000 claims abstract description 437
- 238000006243 chemical reaction Methods 0.000 claims abstract description 325
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 111
- 238000003860 storage Methods 0.000 claims abstract description 79
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 57
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 36
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 36
- 239000011574 phosphorus Substances 0.000 claims abstract description 36
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 32
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 32
- 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 claims abstract description 28
- 238000005273 aeration Methods 0.000 claims abstract description 27
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 25
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 22
- 238000004062 sedimentation Methods 0.000 claims description 87
- 238000010992 reflux Methods 0.000 claims description 79
- 230000001276 controlling effect Effects 0.000 claims description 41
- 238000005276 aerator Methods 0.000 claims description 39
- 238000003756 stirring Methods 0.000 claims description 35
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 32
- 229910052760 oxygen Inorganic materials 0.000 claims description 32
- 239000001301 oxygen Substances 0.000 claims description 32
- 239000011259 mixed solution Substances 0.000 claims description 31
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 claims description 30
- 230000014759 maintenance of location Effects 0.000 claims description 26
- 238000004519 manufacturing process Methods 0.000 claims description 26
- 239000006228 supernatant Substances 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 22
- 229910019142 PO4 Inorganic materials 0.000 claims description 21
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 21
- 239000010452 phosphate Substances 0.000 claims description 21
- 230000001105 regulatory effect Effects 0.000 claims description 19
- 239000012528 membrane Substances 0.000 claims description 13
- 230000029087 digestion Effects 0.000 claims description 8
- 239000000243 solution Substances 0.000 claims description 5
- 150000003017 phosphorus Chemical class 0.000 claims 1
- 239000000047 product Substances 0.000 claims 1
- 230000008569 process Effects 0.000 abstract description 20
- 244000005700 microbiome Species 0.000 abstract description 10
- 239000000126 substance Substances 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 239000000463 material Substances 0.000 abstract 1
- 239000005416 organic matter Substances 0.000 abstract 1
- 230000001079 digestive effect Effects 0.000 description 17
- 238000005192 partition Methods 0.000 description 11
- 238000005086 pumping Methods 0.000 description 10
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 9
- 238000007599 discharging Methods 0.000 description 8
- 239000012530 fluid Substances 0.000 description 8
- 238000002156 mixing Methods 0.000 description 6
- 241000894006 Bacteria Species 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 3
- 230000003134 recirculating effect Effects 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 230000003834 intracellular effect Effects 0.000 description 2
- 230000001360 synchronised effect Effects 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000370 acceptor Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010170 biological 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
- 239000003814 drug Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009440 infrastructure construction Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 230000001131 transforming effect Effects 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
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
-
- 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
- C02F3/02—Aerobic processes
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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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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- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
本发明属于污水生物处理技术领域，公开了连续流反硝化除磷串联厌氧氨氧化耦合内源反硝化处理污水的系统与方法。该系统包括原水水池，A2O反应池，脱氮反应池，污泥贮存池和控制单元。所述方法为：低碳氮比污水首先在A2O反应池中实现反硝化除磷工艺，去除有机物、磷和硝态氮，并且在微生物体内贮存内碳源物质，剩余污泥排至污泥贮存池；仅含有氨氮的污水进入后续脱氮反应池，进行短程硝化‑厌氧氨氧化反应，当系统氮负荷较高时，同时将污泥贮存池内富含内碳源物质的微生物输入脱氮反应池，进行内源反硝化反应强化脱氮。本发明能够保障各组合工艺对氮磷去除率较高，且经济、稳定、污泥产量少、曝气能耗低、绿色环保。
The invention belongs to the technical field of sewage biological treatment, and discloses a system and a method for treating sewage by continuous flow denitrification and phosphorus removal in series with anaerobic ammonia oxidation coupled with endogenous denitrification. The system includes raw water tank, A 2 O reaction tank, denitrification reaction tank, sludge storage tank and control unit. The method is as follows: firstly, the denitrification and phosphorus removal process is realized in the A 2 O reaction tank for the sewage with low carbon to nitrogen ratio, the organic matter, phosphorus and nitrate nitrogen are removed, and the internal carbon source material is stored in the microorganism, and the excess sludge is discharged to the sewage. Mud storage tank; sewage containing only ammonia nitrogen enters the subsequent denitrification reaction tank for short-range nitrification-anaerobic ammonia oxidation reaction. When the nitrogen load of the system is high, the microorganisms rich in internal carbon source substances in the sludge storage tank are input into the denitrification tank. Nitrogen reaction tank to carry out endogenous denitrification reaction to strengthen denitrification. The invention can ensure that each combined process has a high removal rate of nitrogen and phosphorus, is economical, stable, has less sludge output, low energy consumption for aeration, and is environmentally friendly.
Description
Technical Field
The invention belongs to the technical field of biological sewage treatment, and particularly relates to a sewage treatment system and method with continuous flow denitrification dephosphorization, serial anaerobic ammonia oxidation and endogenous denitrification coupling.
Background
Tradition A2The O process is generally applied to large-scale sewage treatment plants at home and abroad, the traditional nitrification/denitrification is utilized for denitrification, and only the A process is applied to municipal sewage with low carbon-nitrogen ratio and sludge digestion liquid wastewater with higher ammonia nitrogen concentration2The O process is difficult to obtain the ideal synchronous removal effect of nitrogen and phosphorus or denitrification effect.
Aiming at the denitrification process, the anaerobic ammonia oxidation technology shows great advantages: no carbon source is needed, the aeration energy consumption is low, the excess sludge yield is low, and the greenhouse gas emission is low. However, if the anaerobic ammonium oxidation technology is used as an independent denitrification technology for sewage treatment, the highest nitrogen removal rate is 89%, further improvement is difficult, and the short sludge age, dissolved oxygen and organic matters required by phosphorus removal are difficult to be considered at the same time, so that the phosphorus removal effect is poor.
For the dephosphorization process, most of the applications mainly adopt a biological method as a main method: anaerobic phosphorus release and aerobic phosphorus absorption are carried out, and phosphorus is removed through sludge discharge; meanwhile, chemical agents are added to realize chemical phosphorus removal in an auxiliary mode so as to reach the discharge standard of phosphorus. The denitrification dephosphorization technology can utilize nitrate nitrogen and nitrite nitrogen as electron acceptors, realizes 'one carbon dual-purpose' in an anoxic zone, saves organic matters utilized by the traditional denitrification, saves dissolved oxygen required by the traditional dephosphorization, and realizes the synchronous removal of nitrogen and phosphorus. The denitrification dephosphorization process generally has a longer anoxic zone, the total hydraulic retention time of the anaerobic zone and the anoxic zone is far longer than that of the aerobic zone, the aerobic phosphorus uptake in the denitrification dephosphorization process mainly plays a role in guaranteeing the control, the dissolved oxygen is generally not high, the process conditions enable microorganisms to fully store organic matters in water into carbon source substances in cells, the microorganisms grow slowly under the condition of low DO, the maximum accumulation of internal carbon sources can be realized, the internal carbon sources can be used for further strengthening denitrification, and the system can obtain higher TN removal rate.
In conclusion, the denitrification dephosphorization, the endogenous denitrification and the anaerobic ammonia oxidation process are combined, the advantages of the processes are fully exerted, and higher denitrification and dephosphorization efficiency can be obtained, so that the process for treating the municipal sewage with the low carbon-nitrogen ratio by coupling the continuous flow denitrification dephosphorization, the serial anaerobic ammonia oxidation and the endogenous denitrification is provided at the forefront.
Disclosure of Invention
The invention aims to provide a sewage treatment system and method with continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupled with endogenous denitrification aiming at the defects of the prior art. The process can reasonably solve the contradiction of denitrification and dephosphorization microorganisms on the aspects of organic matters, oxygen, sludge age and the influence of nitrate in return sludge on the anaerobic phosphorus release of phosphorus-accumulating bacteria, can realize the efficient removal of nitrogen and phosphorus, is economic and environment-friendly, and is the optimal denitrification and dephosphorization process for treating low-carbon-nitrogen-ratio urban sewage and high-ammonia-nitrogen sludge digestive fluid wastewater, upgrading and transforming a sewage treatment plant and building a sewage advanced treatment plant.
In order to achieve the aim, the invention provides a continuous flow denitrification dephosphorization series anaerobic ammonia oxidation coupling endogenous denitrification sewage treatment system in a first aspect, which comprises a raw water pool, A2The system comprises an O reaction tank, a denitrification reaction tank, a sludge storage tank and a control unit;
a is described2The O reaction tank comprises an anaerobic zone, an anoxic zone and an aerobic zone; the anaerobic zone, the anoxic zone and the aerobic zone are communicated through a partition plate with a through hole at the bottom or the upper part in sequence; the raw water pool is connected with the water inlet end of the anaerobic zone through a water inlet pump; the anaerobic zone and the anoxic zone are respectively provided with a first stirring device and a second stirring device; the aerobic zone is provided with a first aerator, a first online dissolved oxygen detector, an online COD detector and an online phosphate detector, the water outlet end of the aerobic zone is connected with an intermediate sedimentation tank, the intermediate sedimentation tank is respectively connected with the anaerobic zone and a first sludge discharge valve through a first sludge reflux pump, and the first sludge discharge valve is connected with the sludge storage tank;
the denitrification reaction tank comprises a plurality of denitrification reaction zones, and the former denitrification reaction zone is communicated with the latter denitrification reaction zone through a partition plate with a through hole at the bottom or the upper part; the water outlet end of the intermediate sedimentation tank is connected with the water inlet end of the first denitrification reaction zone; the first denitrification reaction zone is provided with a third stirring device and a second aerator; the other denitrification reaction areas are provided with third aerators; an MBR membrane module, a second online dissolved oxygen detector, an online ammonia nitrogen detector and an online nitrate nitrogen detector are also arranged in the last denitrification reaction zone; the MBR membrane component is connected with a water production pump, the water production pump is used for discharging the effluent of the denitrification reaction tank out of the system and/or refluxing the effluent to the anoxic zone through a water production reflux valve, the last denitrification reaction zone is respectively connected with the first denitrification reaction zone and a second sludge discharge valve through a second sludge reflux pump, and the second sludge discharge valve is connected with the sludge storage tank;
the sludge storage tank is also respectively connected with one end of the raw water tank and one end of a sludge pump, the other end of the sludge pump is provided with a sludge regulating valve and a system main sludge discharge valve, the sludge regulating valve is connected with the first denitrification reaction zone, and the system main sludge discharge valve is used for discharging system sludge out of the system; the control unit is used for chain reaction control of the system.
The invention provides a method for treating low-carbon-nitrogen-ratio municipal sewage by continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, which adopts the sewage treatment system with continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, and comprises the following steps:
s1: inoculating short-cut nitrification floc sludge and anaerobic ammonia oxidation floc sludge in the denitrification reaction tank, wherein A is2Inoculating sludge in a secondary sedimentation tank in an O reaction tank, and pumping the low-carbon-nitrogen-ratio urban sewage in the raw water tank to the A reaction tank2An O reaction tank; the low-carbon-nitrogen-ratio urban sewage enters the aerobic zone to be subjected to first aeration treatment; controlling the phosphate concentration of the effluent of the aerobic zone to be lower than a first threshold value;
s2: the effluent of the aerobic zone enters an intermediate sedimentation tank, part of precipitated sludge in the intermediate sedimentation tank flows back to the anaerobic zone, residual precipitated sludge in the intermediate sedimentation tank is discharged to a sludge storage tank, and secondary sedimentation tank sludge, the low-carbon-nitrogen-ratio municipal sewage and the precipitated sludge flowing back to the anaerobic zone are mixed to form a first mixed solution; the supernatant in the intermediate sedimentation tank enters the denitrification reaction tank;
s3: performing second aeration treatment on the supernatant, wherein the second sludge reflux pump reflows a part of sludge in the last denitrification reaction zone to the first denitrification reaction zone, and discharges the residual sludge in the denitrification reaction tank to the sludge storage tank; the water-producing pump reflows the effluent of the denitrification reaction tank to the anoxic zone and/or discharges the effluent out of the system; mixing the first mixed solution with effluent of a denitrification reaction tank which flows back to the anoxic zone to form a second mixed solution;
s4: the second mixed liquid enters the aerobic zone, and the steps S1-S3 are repeated;
controlling the concentration of nitrate nitrogen in the effluent of the denitrification reaction tank to be lower than a second threshold value; controlling the concentration of the ammonia nitrogen in the effluent of the denitrification reaction tank to be lower than a third threshold value;
s5: and the steps are sequentially and circularly carried out, and the supernatant of the sludge storage pool is refluxed to the raw water pool.
The third aspect of the invention provides a method for treating sludge digestive juice with low carbon-nitrogen ratio by continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, the method adopts the sewage treatment system with continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, and the method comprises the following steps:
s1: inoculating short-cut nitrification floc sludge and anaerobic ammonia oxidation floc sludge in the denitrification reaction tank, wherein A is2Inoculating sludge in a secondary sedimentation tank in an O reaction tank, and pumping low-carbon-nitrogen-ratio sludge digestive juice in the raw water tank to the A2An O reaction tank; the sludge digestive fluid with low carbon-nitrogen ratio enters the aerobic zone to carry out first aeration treatment; controlling the phosphate concentration of the effluent of the aerobic zone to be lower than a first threshold value;
s2: the effluent of the aerobic zone enters an intermediate sedimentation tank, part of precipitated sludge in the intermediate sedimentation tank flows back to the anaerobic zone, residual precipitated sludge in the intermediate sedimentation tank is discharged to a sludge storage tank, and secondary sedimentation tank sludge, the low-carbon-nitrogen-ratio sludge digestive fluid and the precipitated sludge flowing back to the anaerobic zone are mixed to form a first mixed solution; the supernatant in the intermediate sedimentation tank enters the denitrification reaction tank;
s3: performing second aeration treatment on the supernatant, wherein the second sludge reflux pump reflows a part of sludge in the last denitrification reaction zone to the first denitrification reaction zone, and discharges the residual sludge in the denitrification reaction tank to the sludge storage tank; the water-producing pump reflows the effluent of the denitrification reaction tank to the anoxic zone and/or discharges the effluent out of the system; mixing the first mixed solution with effluent of a denitrification reaction tank which flows back to the anoxic zone to form a second mixed solution;
s4: the second mixed liquid enters the aerobic zone, and the steps S1-S3 are repeated;
controlling the concentration of nitrate nitrogen in the effluent of the denitrification reaction tank to be lower than a second threshold value; controlling the concentration of the ammonia nitrogen in the effluent of the denitrification reaction tank to be lower than a third threshold value;
s5: and the steps are sequentially and circularly carried out, and the supernatant of the sludge storage pool is refluxed to the raw water pool.
The technical scheme of the invention has the following beneficial effects:
1) the invention combines three processes of denitrifying phosphorus removal, series anaerobic ammonia oxidation and endogenous denitrification, can give full play to the advantages of each process, and can obtain higher nitrogen and phosphorus removal efficiency.
2) The invention can reasonably solve the contradiction of denitrification and dephosphorization microorganisms on the aspects of organic matters, oxygen, sludge age, influence of nitrate in the returned sludge on anaerobic phosphorus release of phosphorus-accumulating bacteria and the like, and can realize the high-efficiency removal of nitrogen and phosphorus.
3) A of the invention2The denitrifying phosphorus accumulating bacteria in the O reaction tank are dominant strains, can fully utilize a carbon source in raw water, store intracellular carbon source substances to the maximum extent, and perform denitrifying phosphorus removal reaction by combining nitrate nitrogen generated by anaerobic ammonia oxidation, so that 'one-carbon dual-purpose' is realized, and the anaerobic ammonia oxidation nitrogen removal efficiency can be improved on the basis of phosphorus removal; and the hydraulic retention time is short, the aerobic zone is short, and the aeration energy consumption is saved.
4) The intermediate sedimentation tank is not easy to cause the sludge floating phenomenon, the sludge expansion phenomenon is not easy to occur in the system, the operation is stable, and the water outlet effect is good.
5) In the denitrification reaction tank, the shortcut nitrifying bacteria and the anaerobic ammonium oxidation bacteria are dominant strains, autotrophic denitrification is performed, a carbon source is not needed, aeration energy consumption is saved, and the sludge yield is low; aiming at the sewage with high total nitrogen load, the denitrification reaction area can be adjusted to be an anoxic condition, sludge rich in intracellular carbon source substances is input, endogenous denitrification is carried out to strengthen denitrification reaction, and the total nitrogen removal rate of the system is further improved.
6) Compared with the traditional activated sludge method, the excess sludge amount of the invention is less, the tank volume and the infrastructure construction cost are reduced, and the sludge disposal cost is reduced; the aeration energy consumption is low, carbon source substances and medicament cost are not needed, and the operation cost is saved; the total nitrogen removal rate is higher, and the difficulty and the cost are reduced for the subsequent treatment of the sewage; reduces the emission of greenhouse gases and is green and environment-friendly.
7) The invention is economic and environment-friendly, and is an optimized nitrogen and phosphorus removal process for treating low-carbon-nitrogen-ratio municipal sewage and high-ammonia-nitrogen sludge digestive juice wastewater, upgrading and modifying a sewage treatment plant and building a sewage advanced treatment plant.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
FIG. 1 shows a schematic diagram of a sewage treatment system with continuous flow denitrification dephosphorization, series anaerobic ammonia oxidation and endogenous denitrification coupled provided by the invention.
The reference numerals are explained below:
1-a raw water pool; 2-A2An O reaction tank; 3-denitrification reaction tank; 4-a sludge storage tank; 1.1-water inlet pump; 2.1-anaerobic zone; 2.2-anoxic zone; 2.3-aerobic zone; 2.4-a first stirring device; 2.5-a first aerator; 2.6-blower; 2.7-intermediate sedimentation tank; 2.8-a first sludge reflux pump; 2.9-first mud valve; 2.10-a second stirring device; 3.1-denitrification reaction zone; 3.2-MBR membrane module; 3.3-water pump production; 3.4-produced water reflux valve; 3.5-a second sludge reflux pump; 3.6-second mud valve; 3.7-a third stirring device; 3.8-a second aerator; 3.9-a third aerator; 4.1-sludge pump; 4.2-sludge regulating valve; 4.3-system main sludge discharge valve.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.
The invention provides a continuous flow denitrification dephosphorization series anaerobic ammonia oxidation coupling endogenous denitrification sewage treatment system in a first aspect, which comprises a raw water pool A2The system comprises an O reaction tank, a denitrification reaction tank, a sludge storage tank and a control unit;
a is described2The O reaction tank comprises an anaerobic zone, an anoxic zone and an aerobic zone; the anaerobic zone, the anoxic zone and the aerobic zone are communicated through a partition plate with a through hole at the bottom or the upper part in sequence; the raw water pool is connected with the water inlet end of the anaerobic zone through a water inlet pump; the anaerobic zone and the anoxic zone are respectively provided with a first stirring device and a second stirring device; the aerobic zone is provided with a first aerator, a first online dissolved oxygen detector, an online COD detector and an online phosphate detector, the water outlet end of the aerobic zone is connected with an intermediate sedimentation tank, the intermediate sedimentation tank is respectively connected with the anaerobic zone and a first sludge discharge valve through a first sludge reflux pump, and the first sludge discharge valve is connected with the sludge storage tank;
the denitrification reaction tank comprises a plurality of denitrification reaction zones, and the former denitrification reaction zone is communicated with the latter denitrification reaction zone through a partition plate with a through hole at the bottom or the upper part; the water outlet end of the intermediate sedimentation tank is connected with the water inlet end of the first denitrification reaction zone; the first denitrification reaction zone is provided with a third stirring device and a second aerator; the other denitrification reaction areas are provided with third aerators; an MBR membrane module, a second online dissolved oxygen detector, an online ammonia nitrogen detector and an online nitrate nitrogen detector are also arranged in the last denitrification reaction zone; the MBR membrane component is connected with a water production pump, the water production pump is used for discharging the effluent of the denitrification reaction tank out of the system and/or refluxing the effluent to the anoxic zone through a water production reflux valve, the last denitrification reaction zone is respectively connected with the first denitrification reaction zone and a second sludge discharge valve through a second sludge reflux pump, and the second sludge discharge valve is connected with the sludge storage tank;
the sludge storage tank is also respectively connected with one end of the raw water tank and one end of a sludge pump, the other end of the sludge pump is provided with a sludge regulating valve and a system main sludge discharge valve, the sludge regulating valve is connected with the first denitrification reaction zone, and the system main sludge discharge valve is used for discharging system sludge out of the system;
the control unit is used for chain reaction control of the system.
According to the present invention, preferably, the first aerator, the second aerator and the third aerator are all connected to a blower.
According to the present invention, it is preferred that the volume ratio of the anaerobic zone, the anoxic zone and the aerobic zone is from 1:1 to 5:1 to 2.
According to the present invention, preferably, the control unit is a PLC control unit.
In the invention, the number of the anoxic zones is multiple, the anoxic zones are communicated through the partition plate with the through hole at the bottom or the upper part, the second stirring device is arranged in each anoxic zone, the first anoxic zone is communicated with the anaerobic zone through the partition plate with the through hole at the bottom or the upper part, and the last anoxic zone is communicated with the aerobic zone through the partition plate with the through hole at the bottom or the upper part.
In the invention, the volume ratio of the anaerobic zone, the anoxic zone and the aerobic zone is the ratio of the volume of the anaerobic zone, the total volume of the anoxic zones and the volume of the aerobic zone.
In the invention, the water inlet pump, the water production pump, the air blower, the first sludge reflux pump, the first sludge discharge valve, the water production reflux valve, the second sludge reflux pump, the second sludge discharge valve, the first stirring device, the second stirring device, the third stirring device, the first aerator, the second aerator, the third aerator, the sludge pump, the sludge regulating valve and the system total sludge discharge valve are all connected with the control unit and can be automatically regulated according to a set program.
In the present invention, the first online dissolved oxygen detector, the online COD detector, the online phosphate detector, the second online dissolved oxygen detector, the online ammonia nitrogen detector and the online nitrate nitrogen detector are not shown.
The invention provides a method for treating low-carbon-nitrogen-ratio municipal sewage by continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, which adopts the sewage treatment system with continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, and comprises the following steps:
s1: inoculating short-cut nitrification floc sewage in the denitrification reaction tankSludge and anammox floc sludge, in said A2Inoculating sludge in a secondary sedimentation tank in an O reaction tank, and pumping the low-carbon-nitrogen-ratio urban sewage in the raw water tank to the A reaction tank2An O reaction tank; the low-carbon-nitrogen-ratio urban sewage enters the aerobic zone to be subjected to first aeration treatment; controlling the phosphate concentration of the effluent of the aerobic zone to be lower than a first threshold value;
s2: the effluent of the aerobic zone enters an intermediate sedimentation tank, part of precipitated sludge in the intermediate sedimentation tank flows back to the anaerobic zone, residual precipitated sludge in the intermediate sedimentation tank is discharged to a sludge storage tank, and secondary sedimentation tank sludge, the low-carbon-nitrogen-ratio municipal sewage and the precipitated sludge flowing back to the anaerobic zone are mixed to form a first mixed solution; the supernatant in the intermediate sedimentation tank enters the denitrification reaction tank;
s3: performing second aeration treatment on the supernatant, wherein the second sludge reflux pump reflows a part of sludge in the last denitrification reaction zone to the first denitrification reaction zone, and discharges the residual sludge in the denitrification reaction tank to the sludge storage tank; the water-producing pump reflows the effluent of the denitrification reaction tank to the anoxic zone and/or discharges the effluent out of the system; mixing the first mixed solution with effluent of a denitrification reaction tank which flows back to the anoxic zone to form a second mixed solution;
s4: the second mixed liquid enters the aerobic zone, and the steps S1-S3 are repeated;
controlling the concentration of nitrate nitrogen in the effluent of the denitrification reaction tank to be lower than a second threshold value; controlling the concentration of the ammonia nitrogen in the effluent of the denitrification reaction tank to be lower than a third threshold value;
s5: and the steps are sequentially and circularly carried out, and the supernatant of the sludge storage pool is refluxed to the raw water pool.
In the invention, the low carbon nitrogen ratio municipal sewage is firstly treated with A2Realizing a denitrification dephosphorization process in the O reaction tank, removing organic matters, phosphorus and nitrate nitrogen, storing internal carbon source substances in a microorganism body, and discharging residual sludge to a sludge storage tank; the sewage only containing ammonia nitrogen enters a subsequent denitrification reaction tank to carry out shortcut nitrification-anaerobic ammonium oxidation reaction, and when the nitrogen of the system isWhen the load is higher, simultaneously, the microorganism rich in the internal carbon source substances in the sludge storage tank is input into the denitrification reaction tank for carrying out the enhanced denitrification of the internal source denitrification reaction.
In the invention, the short-cut nitrification floc sludge is discharged from a high ammonia nitrogen wastewater treatment system which operates stably; the anaerobic ammonia oxidation floc sludge is cultured anaerobic ammonia oxidation floc sludge.
According to the invention, preferably, in the step S1, the sludge concentration of the denitrification reaction tank is 6-10g/L, wherein the concentration of the shortcut nitrification floc sludge and the anaerobic ammonia oxidation floc sludge are both 3-5 g/L; the sludge in the secondary sedimentation tank is the sludge returned from the secondary sedimentation tank of the municipal sewage treatment plant.
In the invention, the low-carbon-nitrogen-ratio urban sewage in the raw water pool is pumped to the sewage A through the water inlet pump2And (4) an O reaction tank.
According to the present invention, preferably, in step S2, the reflux ratio of settled sludge refluxed into the intermediate settling tank of the anaerobic zone is 50% to 200%; a is described2The sludge age of the O reaction tank sludge is 4-15d, and the residual precipitated sludge in the intermediate precipitation tank is discharged to the sludge storage tank; a is described2The sludge concentration in the first mixed liquid in the O reaction tank is 6-10 g/L.
In the present invention, the reflux ratio of the precipitated sludge refluxed into the intermediate settling tank of the anaerobic zone is the amount of the precipitated sludge refluxed into the intermediate settling tank of the anaerobic zone to the amount of the precipitated sludge entering the intermediate settling tank a2The ratio of low carbon nitrogen to the water amount of the municipal sewage in the O reaction tank. The secondary sedimentation tank sludge, the low-carbon-nitrogen-ratio municipal sewage and the sedimentation sludge which flows back to the anaerobic zone are mixed in the anaerobic zone, and are uniformly stirred by a first stirring device to form a first mixed solution.
According to the present invention, preferably, in step S1, the first threshold value is 0.35-0.45 mg/L; the step of controlling the phosphate concentration of the effluent of the aerobic zone to be below a first threshold value comprises adjusting the first sludge recirculation pump with the control unit to increase the recirculation ratio of the settled sludge recirculated into the intermediate settling tank of the anaerobic zone,adjusting the first mud valve to shorten the distance A2And (3) increasing the sludge age of the sludge in the O reaction tank, increasing the sludge amount discharged from the residual precipitated sludge in the intermediate precipitation tank to the sludge storage tank until the detected phosphate concentration is less than 0.35-0.45mg/L, and restoring and adjusting the first sludge reflux pump and the first sludge discharge valve to an initial state.
According to the present invention, it is preferable that the reflux ratio of the denitrification sludge refluxed to the last denitrification reaction zone of the first denitrification reaction zone is 100 to 300% in step S3; the sludge age of the denitrification reaction tank is 60-100d, and the residual sludge of the denitrification reaction tank is discharged to the sludge storage tank; the water production reflux ratio of the effluent which flows back to the denitrification reaction tank of the anoxic zone is 0-300%.
In the present invention, the reflux ratio of the denitrification sludge refluxed to the last denitrification reaction zone of the first denitrification reaction zone is the amount of the denitrification sludge refluxed to the last denitrification reaction zone of the first denitrification reaction zone and the amount of the denitrification sludge entering the A2The ratio of low carbon nitrogen to the water amount of the municipal sewage in the O reaction tank.
In the invention, the water production reflux ratio of the effluent of the denitrification reaction tank which flows back to the anoxic zone is the effluent amount of the denitrification reaction tank which flows back to the anoxic zone and the effluent amount entering the anoxic zone A2The ratio of low carbon nitrogen to the water amount of the municipal sewage in the O reaction tank.
In the invention, the first mixed liquid and the effluent of the denitrification reaction tank which flows back to the anoxic zone are mixed in the anoxic zone and are uniformly stirred by a second stirring device to form a second mixed liquid. And the effluent of the denitrification reaction tank which flows back to the anoxic zone is nitrate nitrogen-containing solution.
According to the present invention, preferably, in step S4, the second threshold value is 4.5-5.5 mg/L; controlling the nitrate nitrogen concentration of the effluent of the denitrification reaction tank to be lower than a second threshold value comprises the steps of utilizing the control unit to open the sludge regulating valve, pumping the stored sludge of the sludge storage tank into the first denitrification reaction zone, closing the second aerator, opening a third stirring device, adjusting the produced water reflux valve, increasing the reflux ratio of the effluent of the denitrification reaction tank which is refluxed to the anoxic zone until the nitrate nitrogen concentration is detected to be lower than 4.5-5.5mg/L, recovering the normal operation, closing the sludge regulating valve, opening the second aerator, closing the third stirring device, adjusting the produced water reflux valve, and reducing the reflux ratio of the effluent of the denitrification reaction tank which is refluxed to the anoxic zone; preferably, the amount of the sludge stored in the sludge storage tank and pumped into the first denitrification reaction zone is set according to the hydraulic retention time of 1-3h under the anoxic condition of the first denitrification reaction zone;
the third threshold value is 4-5 mg/L; the step of controlling the ammonia nitrogen concentration of the effluent of the denitrification reaction tank to be lower than a third threshold value comprises the steps of adjusting the second sludge reflux pump by using the control unit, increasing the reflux ratio of the denitrification sludge refluxed to the last denitrification reaction zone of the first denitrification reaction zone, increasing the aeration amount until the ammonia nitrogen concentration is detected to be less than 4-5mg/L, and restoring and adjusting the second sludge reflux pump and the air blower to the initial state.
According to the invention, preferably, the carbon-nitrogen ratio of the municipal sewage with the low carbon-nitrogen ratio is 0.8-4.5, and the ammonia nitrogen concentration is 35-65 mg/L.
According to the invention, preferably, A is2The dissolved oxygen concentration of the aerobic zone of the O reaction tank is 1-4 mg/L; a is described2The hydraulic retention time of the O reaction tank is 1-8 h.
According to the invention, preferably, the concentration of dissolved oxygen in the denitrification reaction tank is 0.1-2 mg/L; the hydraulic retention time of the denitrification reaction tank is 7-12 h.
According to the invention, the hydraulic retention time of the sludge storage tank is preferably 2-5 h.
In the invention, the dissolved oxygen concentration of the MBR membrane module is 1.4-1.6 mg/L.
The third aspect of the invention provides a method for treating sludge digestive juice with low carbon-nitrogen ratio by continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, the method adopts the sewage treatment system with continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, and the method comprises the following steps:
s1: inoculating short-cut nitrification in the denitrification reaction tankFloc sludge and anammox floc sludge as described in A2Inoculating sludge in a secondary sedimentation tank in an O reaction tank, and pumping low-carbon-nitrogen-ratio sludge digestive juice in the raw water tank to the A2An O reaction tank; the sludge digestive fluid with low carbon-nitrogen ratio enters the aerobic zone to carry out first aeration treatment; controlling the phosphate concentration of the effluent of the aerobic zone to be lower than a first threshold value;
s2: the effluent of the aerobic zone enters an intermediate sedimentation tank, part of precipitated sludge in the intermediate sedimentation tank flows back to the anaerobic zone, residual precipitated sludge in the intermediate sedimentation tank is discharged to a sludge storage tank, and secondary sedimentation tank sludge, the low-carbon-nitrogen-ratio sludge digestive fluid and the precipitated sludge flowing back to the anaerobic zone are mixed to form a first mixed solution; the supernatant in the intermediate sedimentation tank enters the denitrification reaction tank;
s3: performing second aeration treatment on the supernatant, wherein the second sludge reflux pump reflows a part of sludge in the last denitrification reaction zone to the first denitrification reaction zone, and discharges the residual sludge in the denitrification reaction tank to the sludge storage tank; the water-producing pump reflows the effluent of the denitrification reaction tank to the anoxic zone and/or discharges the effluent out of the system; mixing the first mixed solution with effluent of a denitrification reaction tank which flows back to the anoxic zone to form a second mixed solution;
s4: the second mixed liquid enters the aerobic zone, and the steps S1-S3 are repeated;
controlling the concentration of nitrate nitrogen in the effluent of the denitrification reaction tank to be lower than a second threshold value; controlling the concentration of the ammonia nitrogen in the effluent of the denitrification reaction tank to be lower than a third threshold value;
s5: and the steps are sequentially and circularly carried out, and the supernatant of the sludge storage pool is refluxed to the raw water pool.
In the invention, the sludge digestive fluid with low carbon-nitrogen ratio is firstly in A2Realizing a denitrification dephosphorization process in the O reaction tank, removing organic matters, phosphorus and nitrate nitrogen, storing internal carbon source substances in a microorganism body, and discharging residual sludge to a sludge storage tank; the sewage only containing ammonia nitrogen enters a subsequent denitrification reaction tank for shortcut nitrification-anaerobic ammonia oxidationAnd (3) reacting, when the nitrogen load of the system is higher, simultaneously inputting the microorganisms rich in the internal carbon source substances in the sludge storage tank into the denitrification reaction tank to perform endogenous denitrification reaction to enhance denitrification.
According to the invention, preferably, in the step S1, the sludge concentration of the denitrification reaction tank is 6-10g/L, wherein the concentration of the shortcut nitrification floc sludge and the anaerobic ammonia oxidation floc sludge are both 3-5 g/L; the sludge in the secondary sedimentation tank is the sludge returned from the secondary sedimentation tank of the municipal sewage treatment plant.
In the invention, the low carbon nitrogen ratio sludge digestive fluid in the raw water pool is pumped to the A through the water inlet pump2And (4) an O reaction tank.
According to the present invention, preferably, in step S2, the reflux ratio of settled sludge refluxed into the intermediate settling tank of the anaerobic zone is 50% to 200%; a is described2The sludge age of the O reaction tank sludge is 4-15d, and the residual precipitated sludge in the intermediate precipitation tank is discharged to the sludge storage tank; a is described2The sludge concentration in the first mixed liquid in the O reaction tank is 6-10 g/L.
In the present invention, the reflux ratio of the precipitated sludge refluxed into the intermediate settling tank of the anaerobic zone is the amount of the precipitated sludge refluxed into the intermediate settling tank of the anaerobic zone to the amount of the precipitated sludge entering the intermediate settling tank a2The ratio of the low carbon nitrogen to the water amount of the sludge digestion liquid in the O reaction tank. And the sludge in the secondary sedimentation tank, the sludge digestion liquid and the precipitated sludge which flows back to the anaerobic zone are mixed in the anaerobic zone, and are uniformly stirred by a first stirring device to form a first mixed solution.
According to the present invention, preferably, in step S1, the first threshold value is 0.35-0.45 mg/L; the step of controlling the phosphate concentration of the effluent of the aerobic zone to be lower than a first threshold comprises adjusting the first sludge recirculation pump by the control unit, increasing the recirculation ratio of the settled sludge in the intermediate settling tank recirculating to the anaerobic zone, adjusting the first sludge discharge valve, shortening the A2The sludge age of the sludge in the O reaction tank is increased, and the sludge amount discharged from the residual precipitated sludge in the intermediate precipitation tank to the sludge storage tank is increased until the detected phosphate concentration is less than 0.35-0.45mg/L, and restoring and adjusting the first sludge return pump and the first sludge discharge valve to the initial state.
According to the present invention, it is preferable that the reflux ratio of the denitrification sludge refluxed to the last denitrification reaction zone of the first denitrification reaction zone is 100 to 300% in step S3; the sludge age of the denitrification reaction tank is 60-100d, and the residual sludge is discharged to the sludge storage tank; the water production reflux ratio of the effluent which flows back to the denitrification reaction tank of the anoxic zone is 0-300%.
In the present invention, the reflux ratio of the denitrification sludge refluxed to the last denitrification reaction zone of the first denitrification reaction zone is the amount of the denitrification sludge refluxed to the last denitrification reaction zone of the first denitrification reaction zone and the amount of the denitrification sludge entering the A2The ratio of the low carbon nitrogen to the water amount of the sludge digestion liquid in the O reaction tank.
In the invention, the water production reflux ratio of the effluent of the denitrification reaction tank which flows back to the anoxic zone is the effluent amount of the denitrification reaction tank which flows back to the anoxic zone and the effluent amount entering the anoxic zone A2The ratio of the low carbon nitrogen to the water amount of the sludge digestion liquid in the O reaction tank.
In the invention, the first mixed liquid and the effluent of the denitrification reaction tank which flows back to the anoxic zone are mixed in the anoxic zone and are uniformly stirred by a second stirring device to form a second mixed liquid. And the effluent of the denitrification reaction tank which flows back to the anoxic zone is nitrate nitrogen-containing solution.
According to the present invention, preferably, in step S4, the second threshold value is 95-105 mg/L; controlling the nitrate nitrogen concentration of the effluent of the denitrification reaction tank to be lower than a second threshold value comprises the steps of utilizing the control unit to open the sludge regulating valve, pumping the stored sludge of the sludge storage tank into the first denitrification reaction zone, closing the second aerator, opening a third stirring device, adjusting the produced water reflux valve, increasing the reflux ratio of the effluent of the denitrification reaction tank which flows back to the anoxic zone until the nitrate nitrogen concentration is detected to be lower than 95-105mg/L, recovering the normal operation, closing the sludge regulating valve, opening the second aerator, closing the third stirring device, adjusting the produced water reflux valve, and reducing the reflux ratio of the effluent of the denitrification reaction tank which flows back to the anoxic zone; preferably, the amount of the sludge stored in the sludge storage tank and pumped into the first denitrification reaction zone is set according to the hydraulic retention time of 1-4d under the anoxic condition of the first denitrification reaction zone;
the third threshold value is 45-55 mg/L; the step of controlling the ammonia nitrogen concentration of the effluent of the denitrification reaction tank to be lower than a third threshold value comprises the steps of adjusting the second sludge reflux pump by using the control unit, increasing the reflux ratio of the denitrification sludge refluxed to the last denitrification reaction zone of the first denitrification reaction zone, increasing the aeration amount until the ammonia nitrogen concentration is detected to be lower than 45-55mg/L, and restoring and adjusting the second sludge reflux pump and the air blower to be in an initial state.
According to the invention, preferably, the carbon-nitrogen ratio of the sludge digestion solution with low carbon-nitrogen ratio is 0.8-1.5, and the ammonia nitrogen concentration is 2-2.5 g/L.
According to the invention, preferably, A is2The dissolved oxygen concentration of the aerobic zone of the O reaction tank is 1-4 mg/L; a is described2The hydraulic retention time of the O reaction tank is 1-8 h.
According to the invention, preferably, the concentration of dissolved oxygen in the denitrification reaction tank is 0.1-2 mg/L; the hydraulic retention time of the denitrification reaction tank is 1-3 d.
According to the invention, the hydraulic retention time of the sludge storage tank is preferably 1-3 d.
In the invention, the concentration of dissolved oxygen at the effluent of the MBR membrane module is 1.4-1.6 mg/L.
The present invention is specifically illustrated by the following examples.
Example 1
This example provides a continuous flow denitrification dephosphorization series anaerobic ammonia oxidation coupled endogenous denitrification sewage treatment system, as shown in fig. 1, the system includes a raw water pool 1, a2An O reaction tank 2, a denitrification reaction tank 3, a sludge storage tank 4 and a PLC control unit;
a is described2The O reaction tank comprises an anaerobic zone 2.1, an anoxic zone 2.2 and an aerobic zone 2.3, and the volume ratio of the anaerobic zone 2.1 to the anoxic zone 2.2 to the aerobic zone 2.3 is 1:1: 1; the anaerobic zone 2.1 and the anoxic zone 2.2The aerobic zone 2.3 is communicated with the baffle plate with a through hole at the bottom or the upper part in sequence; the raw water pool 1 is connected with the water inlet end of the anaerobic zone 2.1 through a water inlet pump 1.1; the anaerobic zone 2.1 and the anoxic zone 2.2 are respectively provided with a first stirring device 2.4 and a second stirring device 2.10; the aerobic zone 2.3 is provided with a first aerator 2.5, a first online dissolved oxygen detector, an online COD detector and an online phosphate detector, the water outlet end of the aerobic zone 2.3 is connected with an intermediate sedimentation tank 2.7, the intermediate sedimentation tank 2.7 is respectively connected with the anaerobic zone 2.1 and a first sludge discharge valve 2.9 through a first sludge reflux pump 2.8, and the first sludge discharge valve 2.9 is connected with the sludge storage tank 4;
the denitrification reaction tank 3 comprises a plurality of denitrification reaction zones 3.1, and the former denitrification reaction zone 3.1 is communicated with the latter denitrification reaction zone 3.1 through a partition plate with a through hole at the bottom or the upper part; the water outlet end of the intermediate sedimentation tank 2.7 is connected with the water inlet end of the first denitrification reaction zone 3.1; the first denitrification reaction zone 3.1 is provided with a third stirring device 3.7 and a second aerator 3.8; the other denitrification reaction zones 3.1 are provided with third aerators 3.9; an MBR membrane component 3.2, a second online dissolved oxygen detector, an online ammonia nitrogen detector and an online nitrate nitrogen detector are also arranged in the last denitrification reaction zone 3.1; a water production pump 3.3 is connected to the MBR membrane module 3.2, the water production pump 3.3 is used for discharging the effluent of the denitrification reaction tank 3 out of the system and/or refluxing the effluent to the anoxic zone 2.2 through a water production reflux valve 3.4, the last denitrification reaction zone 3.1 is respectively connected with the first denitrification reaction zone 3.1 and a second sludge discharge valve 3.6 through a second sludge reflux pump 3.5, and the second sludge discharge valve 3.6 is connected with the sludge storage tank 4;
the sludge storage tank 4 is also respectively connected with one end of the raw water tank 1 and one end of a sludge pump 4.1, the other end of the sludge pump 4.1 is provided with a sludge regulating valve 4.2 and a system main sludge discharge valve 4.3, the sludge regulating valve 4.2 is connected with the first denitrification reaction zone 3.1, and the system main sludge discharge valve 4.3 is used for discharging system sludge out of the system;
the PLC control unit is used for controlling the chain reaction of the system.
Wherein the first aerator 2.5, the second aerator 3.8 and the third aerator 3.9 are all connected to a blower 2.6; the number of the anoxic zones 2.2 is 2, and the 2 anoxic zones 2.2 are communicated through a partition plate with a through hole at the bottom or the upper part; the 2 anoxic zones 2.2 are provided with second stirring devices 2.10; the first anoxic zone of 2 anoxic zones 2.2 is communicated with the anaerobic zone 2.1 through a partition plate with a through hole at the bottom or the upper part, and the second anoxic zone of 2 anoxic zones 2.2 is communicated with the aerobic zone 2.3 through a partition plate with a through hole at the bottom or the upper part.
The water inlet pump 1.1, the water production pump 3.3, the air blower 2.6, the first sludge reflux pump 2.8, the first sludge discharge valve 2.9, the water production reflux valve 3.4, the second sludge reflux pump 3.5, the second sludge discharge valve 3.6, the first stirring device 2.4, the second stirring device 2.10, the third stirring device 3.7, the first aerator 2.5, the second aerator 3.8, the third aerator 3.9, the sludge pump 4.1, the sludge regulating valve 4.2 and the system total sludge discharge valve 4.3 are all connected with the control unit and can be automatically controlled and adjusted according to a set program.
Example 2
This example provides a continuous flow denitrification dephosphorization tandem anaerobic ammonia oxidation coupled endogenous denitrification sewage treatment system, as shown in fig. 1, the system only differs from example 1 in that the volume ratio of the anaerobic zone 2.1, the anoxic zone 2.2 and the aerobic zone 2.3 is 1:5:2, and the other settings are the same as example 1.
Example 3
The embodiment provides a method for treating low-carbon-nitrogen-ratio urban sewage by continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, wherein the water quality of the low-carbon-nitrogen-ratio urban sewage is characterized in that: 70-300mg/L of COD, 30-60mg/L of TN, and NH4 +27-60mg/L of N, 3-7mg/L of TP and 1.1-4.5 of C/N (average value is 2.3), the method adopts the sewage treatment system with continuous flow denitrification dephosphorization, serial anaerobic ammonia oxidation and endogenous denitrification coupled as described in the example 1, as shown in figure 1, and comprises the following steps:
s1: 3-4g/L of short-cut nitrification floc sludge and anaerobic ammonium oxygen are inoculated in the denitrification reaction tank3-4g/L of floc sludge is formed in the A2Inoculating sludge in a secondary sedimentation tank in an O reaction tank 2, and pumping the low-carbon-nitrogen-ratio urban sewage in the raw water tank to the A reaction tank2An O reaction tank 2; the low-carbon-nitrogen-ratio urban sewage enters the aerobic zone for 2.3, and is subjected to first aeration treatment; and controlling the phosphate concentration of the effluent of the aerobic zone 2.3 to be lower than a first threshold value of 0.4 mg/L.
S2: the effluent water of the aerobic zone 2.3 enters the intermediate sedimentation tank 2.7, a part of the precipitated sludge in the intermediate sedimentation tank 2.7 flows back to the anaerobic zone 2.1, and A2The sludge age of the sludge in the O reaction tank is 12 days, the residual precipitated sludge in the intermediate sedimentation tank 2.7 is discharged to the sludge storage tank 4, and the sludge in the secondary sedimentation tank, the municipal sewage with low carbon-nitrogen ratio and the precipitated sludge which flows back to the anaerobic zone 2.1 are mixed to form a first mixed solution; the supernatant in the intermediate sedimentation tank 2.7 enters the denitrification reaction tank 3;
wherein the reflux ratio of the settled sludge refluxed into the intermediate settling tank 2.7 of the anaerobic zone 2.1 is 100%; the sludge concentration in the first mixed solution is maintained at 4-5 g/L; the step of controlling the phosphate concentration of the effluent from the aerobic zone 2.3 to be lower than the first threshold value of 0.4mg/L of the above step S1 comprises adjusting the first sludge recirculation pump 2.8 by the control unit to increase the recirculation ratio of the settled sludge in the intermediate settling tank 2.7 recirculating to the anaerobic zone 2.1; adjusting the first mud valve 2.9 to shorten A2And the sludge age of the sludge in the O reaction tank is increased, and the sludge amount of the residual precipitated sludge in the intermediate sedimentation tank 2.7 discharged to the sludge storage tank 4 is increased.
S3: performing second aeration treatment on the supernatant, wherein a part of sludge in the last denitrification reaction zone 3.1 is refluxed to the first denitrification reaction zone 3.1 by a second sludge reflux pump 3.5, the sludge age of the denitrification reaction tank is 100 days, and the residual sludge in the denitrification reaction tank is discharged to the sludge storage tank 4; the water producing pump 3.3 reflows the effluent of the denitrification reaction tank 3 to the anoxic zone 2.2 and/or discharges the effluent out of the system; mixing the first mixed solution with effluent of a denitrification reaction tank 3 which flows back to the anoxic zone 2.2 to form a second mixed solution; wherein the reflux ratio of the denitrified sludge refluxed to the last denitrification reaction zone 3.1 of the first denitrification reaction zone 3.1 is 100 percent; the sludge concentration in the denitrification reaction tank 3 is maintained at 6-8 g/L; the water production reflux ratio of the effluent which flows back to the denitrification reaction tank 3 of the anoxic zone 2.2 is 50 percent.
S4: the second mixed liquid enters the aerobic zone 2.3, and the steps S1-S3 are repeated;
controlling the nitrate nitrogen concentration of the effluent of the denitrification reaction tank 3 to be lower than a second threshold value of 5 mg/L; controlling the concentration of the ammonia nitrogen in the effluent of the denitrification reaction tank 3 to be lower than a third threshold value of 4.5 mg/L;
the step of controlling the nitrate nitrogen concentration of the effluent of the denitrification reaction tank 3 to be lower than a second threshold value comprises the steps of utilizing the control unit to open the sludge regulating valve 4.2, pumping the stored sludge of the sludge storage tank 4 into the first denitrification reaction zone 3.1, closing the second aerator 3.8, opening a third stirring device 3.7, regulating the water production reflux valve 3.4 and increasing the reflux ratio of the effluent of the denitrification reaction tank 3 which is refluxed to the anoxic zone 2.2; wherein the amount of the sludge stored in the sludge storage tank 4 pumped into the first denitrification reaction zone 3.1 is set according to the hydraulic retention time of 2h under the anoxic condition of the first denitrification reaction zone 3.1; the step of controlling the ammonia nitrogen concentration of the effluent of the denitrification reaction tank 3 to be lower than a third threshold value comprises the steps of adjusting the second sludge reflux pump 3.5 by using the control unit, increasing the reflux ratio of the denitrification sludge refluxed to the last denitrification reaction zone 3.1 of the first denitrification reaction zone 3.1 and increasing the aeration amount.
S5: and the steps are sequentially and circularly carried out, and the supernatant of the sludge storage tank 4 is refluxed to the raw water tank.
Wherein the ammonia nitrogen concentration of the municipal sewage with the low carbon-nitrogen ratio is 35-65 mg/L;
a is described2The dissolved oxygen concentration of an aerobic zone 2.3 of the O reaction tank 2 is 1-2.5 mg/L; a is described2The hydraulic retention time of the O reaction tank 2 is 3 h;
the concentration of dissolved oxygen in the denitrification reaction tank 3 is 0.1-0.3 mg/L; the hydraulic retention time of the denitrification reaction tank 3 is 7 hours;
the hydraulic retention time of the sludge storage tank 4 is 2 hours.
The concentration of dissolved oxygen at the effluent of the MBR membrane module is 1.5 mg/L.
The throughput Q in this example was 5L/h.
The effluent of the denitrification reaction tank 3 which is discharged from the system through the water production pump 3.3 has the following water quality characteristics: COD is less than 50mg/L, NH4 +N is within 5mg/L, TN is within 12mg/L, and TP is within 0.5 mg/L.
Example 4
The embodiment provides a method for treating sludge digestive juice with a low carbon-nitrogen ratio by continuous flow denitrification dephosphorization and series anaerobic ammonia oxidation coupling endogenous denitrification, wherein the water quality of the sludge digestive juice with the low carbon-nitrogen ratio is characterized in that: COD 2-3.3g/L, TN 2-2.5g/L, NH4 +2-2.5g/L of N, 3-20mg/L of TP and 0.8-1.4 of C/N (average value is 1.1), the method adopts the sewage treatment system with continuous flow denitrification dephosphorization, serial anaerobic ammonia oxidation and endogenous denitrification coupled as described in example 2, and as shown in figure 1, the method comprises the following steps:
s1: 4-5g/L of short-cut nitrification floc sludge and 4-5g/L of anaerobic ammonia oxidation floc sludge are inoculated in the denitrification reaction tank 3, and A is2Inoculating sludge in a secondary sedimentation tank into an O reaction tank 2, and pumping the sludge digestive juice with low carbon-nitrogen ratio in the raw water tank 1 to the A2An O reaction tank 2; the sludge digestive fluid with low carbon-nitrogen ratio enters the aerobic zone for 2.3, and first aeration treatment is carried out; and controlling the phosphate concentration of the effluent of the aerobic zone 2.3 to be lower than a first threshold value of 0.4 mg/L.
S2: the effluent water of the aerobic zone 2.3 enters the intermediate sedimentation tank 2.7, a part of the precipitated sludge in the intermediate sedimentation tank 2.7 flows back to the anaerobic zone 2.1, and A2The sludge age of the sludge in the O reaction tank is 10 days, the residual precipitated sludge in the intermediate sedimentation tank 2.7 is discharged to the sludge storage tank 4, and the sludge in the secondary sedimentation tank, the sludge digestive juice with low carbon-nitrogen ratio and the precipitated sludge which flows back to the anaerobic zone 2.1 are mixed to form a first mixed solution; the supernatant in the intermediate sedimentation tank 2.7 enters the denitrification reaction tank 3;
wherein, reflux to theThe reflux ratio of the settled sludge in the intermediate settling tank 2.7 of the anaerobic zone 2.1 is 100 percent; the sludge concentration in the first mixed solution is maintained at 8-10 g/L; the step of controlling the phosphate concentration of the effluent from the aerobic zone 2.3 to be lower than the first threshold value of 0.4mg/L in step S1 comprises adjusting the first sludge recirculation pump 2.8 by the control unit to increase the recirculation ratio of the settled sludge in the intermediate settling tank 2.7 recirculating to the anaerobic zone 2.1; adjusting the first mud valve 2.9 to shorten A2And the sludge age of the sludge in the O reaction tank is increased, and the sludge amount of the residual precipitated sludge in the intermediate sedimentation tank 2.7 discharged to the sludge storage tank 4 is increased.
S3: performing second aeration treatment on the supernatant, wherein a part of sludge in the last denitrification reaction zone 3.1 is refluxed to the first denitrification reaction zone 3.1 by a second sludge reflux pump 3.5, the sludge age of the denitrification reaction tank is 100 days, and the residual sludge in the denitrification reaction tank 3 is discharged to the sludge storage tank 4; the water producing pump 3.3 reflows the effluent of the denitrification reaction tank 3 to the anoxic zone 2.2 and/or discharges the effluent out of the system; mixing the first mixed solution with effluent of a denitrification reaction tank 3 which flows back to the anoxic zone 2.2 to form a second mixed solution; wherein the reflux ratio of the denitrified sludge refluxed to the last denitrification reaction zone 3.1 of the first denitrification reaction zone 3.1 is 100 percent; the sludge concentration in the denitrification reaction tank 3 is maintained at 8-10 g/L; the water production reflux ratio of the effluent which flows back to the denitrification reaction tank 3 of the anoxic zone 2.2 is 300 percent.
S4: the second mixed liquid enters the aerobic zone 2.3, and the steps S1-S3 are repeated;
controlling the nitrate nitrogen concentration of the effluent of the denitrification reaction tank 3 to be lower than a second threshold value of 100 mg/L; controlling the concentration of the ammonia nitrogen in the effluent of the denitrification reaction tank 3 to be lower than a third threshold value of 50 mg/L;
the step of controlling the nitrate nitrogen concentration of the effluent of the denitrification reaction tank 3 to be lower than a second threshold value comprises the steps of utilizing the control unit to open the sludge regulating valve 4.2, pumping the stored sludge of the sludge storage tank 4 into the first denitrification reaction zone 3.1, closing the second aerator 3.8, opening a third stirring device 3.7, regulating the water production reflux valve 3.4 and increasing the reflux ratio of the effluent of the denitrification reaction tank 3 which is refluxed to the anoxic zone 2.2; wherein the amount of the sludge stored in the sludge storage tank 4 pumped into the first denitrification reaction zone 3.1 is set according to the hydraulic retention time of 3h under the anoxic condition of the first denitrification reaction zone 3.1; the step of controlling the ammonia nitrogen concentration of the effluent of the denitrification reaction tank 3 to be lower than the third threshold value comprises the steps of adjusting the second sludge reflux pump 3.5 by using the control unit, increasing the reflux ratio of the denitrification sludge refluxed to the last denitrification reaction zone.1 of the first denitrification reaction zone 3.1 and increasing the aeration amount.
S5: and the steps are sequentially and circularly carried out, and the supernatant of the sludge storage tank 4 is refluxed to the raw water tank 1.
Wherein the ammonia nitrogen concentration of the sludge digestion solution is 2-2.5 g/L;
a is described2The dissolved oxygen concentration of an aerobic zone 2.3 of the O reaction tank 2 is 2.5-3.5 mg/L; a is described2The hydraulic retention time of the O reaction tank 2 is 8 h;
the concentration of dissolved oxygen in the denitrification reaction tank 3 is 0.1-0.3 mg/L; the hydraulic retention time of the denitrification reaction tank 3 is 48 hours;
the hydraulic retention time of the sludge storage tank 4 is 2 d.
The concentration of dissolved oxygen at the effluent of the MBR membrane module is 1.5 mg/L.
The throughput Q in this example was 1L/h.
The effluent of the denitrification reaction tank 3 which is discharged from the system through the water production pump 3.3 has the following water quality characteristics: COD is less than 50mg/L, NH4 +N is within 50mg/L, TN is within 150mg/L, and TP is within 0.5 mg/L.
Having described embodiments of the present invention, the foregoing description is intended to be exemplary, not exhaustive, and not limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (10)
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