CN106745743B - Sewage nitrogen and phosphorus removal system - Google Patents
Sewage nitrogen and phosphorus removal system Download PDFInfo
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- CN106745743B CN106745743B CN201611259305.XA CN201611259305A CN106745743B CN 106745743 B CN106745743 B CN 106745743B CN 201611259305 A CN201611259305 A CN 201611259305A CN 106745743 B CN106745743 B CN 106745743B
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 112
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 87
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 87
- 239000011574 phosphorus Substances 0.000 title claims abstract description 87
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 56
- 239000010865 sewage Substances 0.000 title claims abstract description 47
- 239000010802 sludge Substances 0.000 claims abstract description 147
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 145
- 238000004062 sedimentation Methods 0.000 claims abstract description 84
- 239000007788 liquid Substances 0.000 claims abstract description 73
- 238000000926 separation method Methods 0.000 claims abstract description 67
- 239000006228 supernatant Substances 0.000 claims abstract description 39
- 238000002156 mixing Methods 0.000 claims description 35
- 230000001546 nitrifying effect Effects 0.000 claims description 23
- 229910052799 carbon Inorganic materials 0.000 claims description 14
- 238000006243 chemical reaction Methods 0.000 claims description 14
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 11
- 238000005273 aeration Methods 0.000 claims description 10
- 238000003756 stirring Methods 0.000 claims description 8
- 238000000034 method Methods 0.000 description 69
- 230000008569 process Effects 0.000 description 63
- 241000894006 Bacteria Species 0.000 description 20
- 230000000694 effects Effects 0.000 description 19
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 18
- 244000005700 microbiome Species 0.000 description 15
- 238000010992 reflux Methods 0.000 description 15
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 14
- 230000014759 maintenance of location Effects 0.000 description 12
- 229920000331 Polyhydroxybutyrate Polymers 0.000 description 9
- 230000003647 oxidation Effects 0.000 description 9
- 238000007254 oxidation reaction Methods 0.000 description 9
- 239000005015 poly(hydroxybutyrate) Substances 0.000 description 9
- 239000003344 environmental pollutant Substances 0.000 description 8
- 231100000719 pollutant Toxicity 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 230000006872 improvement Effects 0.000 description 7
- 229910052760 oxygen Inorganic materials 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 238000010521 absorption reaction Methods 0.000 description 5
- 230000009471 action Effects 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 5
- 238000010276 construction Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 5
- 229910002651 NO3 Inorganic materials 0.000 description 4
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 4
- 229910019142 PO4 Inorganic materials 0.000 description 4
- CKUAXEQHGKSLHN-UHFFFAOYSA-N [C].[N] Chemical compound [C].[N] CKUAXEQHGKSLHN-UHFFFAOYSA-N 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000000945 filler Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000006396 nitration reaction Methods 0.000 description 4
- 239000010452 phosphate Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 238000011161 development Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000006213 oxygenation reaction Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 230000001360 synchronised effect Effects 0.000 description 3
- 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 2
- 239000000370 acceptor Substances 0.000 description 2
- 230000004087 circulation Effects 0.000 description 2
- 238000010907 mechanical stirring Methods 0.000 description 2
- 239000005014 poly(hydroxyalkanoate) Substances 0.000 description 2
- 229920000903 polyhydroxyalkanoate Polymers 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 238000003911 water pollution Methods 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 230000031018 biological processes and functions Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 238000001727 in vivo Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000010841 municipal wastewater Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 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
- C02F3/302—Nitrification and denitrification treatment
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- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
The invention provides a sewage nitrogen and phosphorus removal system which comprises an anaerobic tank, a sludge-water separation unit, a nitrification unit, an anoxic tank, an aerobic tank and a secondary sedimentation tank. Wherein, the return sludge 1 of the raw water and the secondary sedimentation tank enters an anaerobic tank, the mixed liquid of the anaerobic tank enters a mud-water separation unit, the supernatant of the mud-water separation unit and the return sludge 2 of the secondary sedimentation tank enter a nitrification unit, the mixed liquid of the nitrification unit and the mud-water separation unit enter an anoxic tank, and the mixed liquid of the anoxic tank sequentially enters an aerobic tank and the secondary sedimentation tank. The invention can realize the deep denitrification and dephosphorization of the urban sewage treatment, is suitable for newly-built sewage plants, and is easy to realize the reconstruction of the built sewage treatment plants.
Description
Technical Field
The invention belongs to the technical field of sewage treatment, and particularly relates to sewage denitrification and dephosphorization treatment.
Technical Field
The efficient removal of nitrogen and phosphorus is always the key and difficult point of town sewage treatment, and the problem of serious water pollution such as water eutrophication and the like is easily caused by the substandard tail water nitrogen and phosphorus. The discharge standard of pollutants for municipal wastewater treatment plant (GB18918-2002) issued in 2002 puts forward higher discharge requirements on sewage treatment, and the specific standard is NH4 +N is less than or equal to 5 mg/L is less than or equal to 15 mg/L is less than or equal to 0.5 mg/L (first-class A standard). some local governments make stricter discharge standards, such as the Water pollution Integrated discharge Standard (D11/307-2013) in Beijing.
The traditional denitrification and dephosphorization technology respectively depends on denitrification microorganisms and dephosphorization microorganisms to respectively complete denitrification and dephosphorization processes. Biological denitrification is a process of finally converting ammonia nitrogen into nitrogen and removing the nitrogen from a system under the participation of nitrifying bacteria and denitrifying bacteria. The mechanism of biological denitrification mainly comprises three processes: ammoniation, nitrification and denitrification. First, in an aerobic or anaerobic environment, nitrogen-containing organic substances in sewage are decomposed into ammoniacal nitrogen by the action of ammoniated bacteria. Second, ammonia Nitrogen (NH)4 +N) is converted into nitrate Nitrogen (NO) by nitrifying bacteria3 -N), the process comprises two reaction stages, the first stage is that ammonia nitrogen is converted into nitrite Nitrogen (NO) under the action of nitrosobacteria2 -N), the second stage is that nitrite nitrogen is converted into nitrate nitrogen under the action of nitrifying bacteria. Finally, denitrifying bacteria use organic carbon source as electron donor in anoxic condition to nitrifyNitrite nitrogen or nitrate nitrogen generated in the process is reduced into nitrogen. The biological phosphorus removal principle is a phosphorus uptake/release principle of polymerized phosphate accumulating microorganisms (PAO), namely, the microorganisms are easy to enrich a type of phosphorus accumulating bacteria (PAO) under the environment of anaerobic/aerobic alternate operation, can absorb a large amount of phosphate from the external environment in excess of the physiological requirement, and are stored in the body in the form of polymerized phosphate, and the phosphorus is removed by discharging the system in the form of residual sludge. The biological phosphorus removal process comprises two processes of anaerobic phosphorus release and aerobic phosphorus absorption.
The biological nitrogen and phosphorus removal process mainly comprises anaerobic, aerobic and anoxic environments, and achieves the purpose of removing nitrogen and phosphorus by changing different units in space or time. At present, the most widely applied sewage treatment plant is A2An O process, an oxidation ditch process, and the like. A. the2the/O and oxidation ditch process is taken as the main process of the current sewage treatment, has the problems of carbon source competition in the denitrification process and the dephosphorization process, contradiction between nitrifying bacteria and phosphorus accumulating bacteria sludge age, influence on anaerobic phosphorus release caused by nitrate reflux and the like, and has insufficient capability of removing nitrogen and phosphorus in urban domestic sewage. To achieve better denitrification and dephosphorization effects, A2the/O and oxidation ditch process has higher requirements on the concentration of a carbon source of inlet water. However, in many cities in China, especially in the southern cities, the carbon source is generally insufficient (namely the carbon-nitrogen ratio is low) in domestic sewage, and A2The total nitrogen and the total phosphorus of the effluent of the O and oxidation ditch process are difficult to reach the standard and be discharged simultaneously.
With the continuous development of the nitrogen and phosphorus removal theory, researchers find out the phenomenon of phosphorus absorption in an anoxic environment and put forward the denitrification phosphorus removal theory. Under anaerobic environment, the phosphorus release process of denitrifying phosphorus accumulating bacteria (DPB) is the same as that of PAO in the traditional phosphorus removal process, namely, the microorganisms release phosphorus in the body into water, and simultaneously, organic matters are taken from the water and stored in the body in the form of PHA (polyhydroxyalkanoate, mainly PHB-polyhydroxybutyrate); under the anoxic environment, the oxygen is different from that of aerobic phosphorus accumulating bacteria (PAO)2As electron acceptors, DPB with NO3 -The energy generated by oxidizing PHB stored in vivo as an electron acceptor can be used for excessive uptake of orthophosphate in solution and storage in cells in the form of polymerized phosphate. In the process of denitrificationIn the phosphorus process, the carbon source realizes the synchronous denitrification and phosphorus absorption effects in a one-carbon dual-purpose mode, the requirement on the carbon source is saved, the aeration quantity and the sludge yield are reduced, and the method has great potential for treating domestic sewage with low carbon-nitrogen ratio.
Various nitrogen and phosphorus removal processes are developed based on the denitrification phosphorus removal theory. According to the existence form of denitrifying phosphorus-accumulating bacteria and nitrifying bacteria in a denitrifying phosphorus-removing system, the denitrifying phosphorus-removing process can be divided into a single-sludge denitrifying phosphorus-removing treatment process and a double-sludge denitrifying phosphorus-removing process. The BCFs technology is a typical single sludge denitrification dephosphorization technology and is a modification of the UCT technology. From the process flow, the BCFS process is in the original A2On the basis of the/O process, a contact tank is added at the rear end of the anaerobic tank, and a mixing tank is added after the anoxic section. And mixing the return sludge and the mixed liquid from the anaerobic tank to adsorb residual organic matters and remove nitrate nitrogen in the return sludge. The mixing tank is arranged between the anoxic tank and the aerobic tank, and synchronous nitrification and denitrification are carried out under the anoxic condition, so that the total nitrogen of the effluent is reduced, and the total nitrogen of the effluent is ensured to reach the standard. The first route of the three internal circulations mainly reduces the concentration of nitrate entering the anaerobic tank as much as possible to ensure the anaerobic condition of the anaerobic tank; the second route is used for assisting in returning the sludge and aims to supplement nitrate to the anoxic pond, and the third route is mainly used for returning the nitrifying liquid and is beneficial to reducing the ammonia nitrogen in the effluent. The process has more reflux and more complex operation, and is not suitable for A2And (3) transformation of the/O process.
The double-sludge process is a typical process based on the double-sludge denitrification dephosphorization theory. Mixing raw water and return sludge in an anaerobic tank, converting COD (chemical oxygen demand) in the sewage into PHB (polyhydroxybutyrate) by denitrifying phosphorus accumulating bacteria, storing the PHB in a body and releasing phosphorus at the same time; and then the mixed liquid enters an intermediate sedimentation tank for mud-water separation, the supernatant enters a nitrification tank, the sludge directly enters an anoxic tank for denitrification phosphorus absorption, and then enters post-aeration for removing unremoved phosphorus and blowing off nitrogen to prevent the sludge from floating upwards. The process has COD for anaerobic phosphorus release and PHB synthesis in the anaerobic tank, and PHB in the mixing tank for simultaneous denitrification and dephosphorization, and is suitable for treating sewage with low carbon-nitrogen ratio. In addition, the process is set to be a double-sludge system, the phosphorus-accumulating bacteria and the nitrifying bacteria are respectively arranged in different reactors, the growth period of the nitrifying bacteria is ensured, the amount of the nitrifying bacteria is increased, the nitrifying efficiency is improved, meanwhile, the contradiction of SRT in the traditional process is well solved, the phosphorus-accumulating bacteria and the nitrifying bacteria grow in respective optimal environments, and the system is stable and efficient to operate. However, the double sludge process requires two sludge systems, which increases the construction cost.
General A2the/O process and the oxidation ditch process are anaerobic-anoxic-aerobic operation, have denitrification dephosphorization conditions, but have very weak denitrification dephosphorization capability in the process in actual operation. The UCT after transformation can only partially realize denitrification dephosphorization; although BCFS has high denitrification and phosphorus removal degree, the BCFS has more reflux and more complex process and is not suitable for A2Improving the process of the oxidation ditch; the double-sludge process needs two sets of sludge systems, and the construction cost is high. Therefore, the development of a novel single sludge process suitable for reconstruction of the established sewage plant by utilizing the denitrification dephosphorization principle has important significance.
Disclosure of Invention
In view of the problems in the prior art, the invention provides a novel sewage deep nitrogen and phosphorus removal treatment process with denitrification phosphorus removal function, the nitrogen and phosphorus removal effect is obvious, the total nitrogen and total phosphorus content in the effluent is reduced, and the problem that the sewage treatment is difficult to reach the standard can be effectively solved. The invention is suitable for the new construction and the reconstruction of town sewage plants with the requirements of denitrification and dephosphorization, and is also suitable for the denitrification and dephosphorization treatment of industrial wastewater with better biodegradability.
The sewage nitrogen and phosphorus removal system comprises: the device is formed by sequentially connecting an anaerobic tank, a sludge-water separation unit, an anoxic tank, an aerobic tank and a secondary sedimentation tank, and is also provided with a nitrification unit, wherein the anaerobic tank is provided with an inlet of raw water, return sludge 1 of the secondary sedimentation tank enters the anaerobic tank, the nitrification unit contains a nitrification tank, supernatant separated by the sludge-water separation unit and return sludge 2 of the secondary sedimentation tank enter the nitrification unit, mixed liquid flowing out of the nitrification unit and sludge flowing out of the sludge-water separation unit enter the anoxic tank, mixed liquid flowing out of the anoxic tank enters the aerobic tank, mixed liquid flowing out of the aerobic tank enters the secondary sedimentation tank, and the secondary sedimentation tank is provided with a water outlet and a sludge outlet.
The anaerobic tank comprises an inlet, wherein the anaerobic tank is provided with raw water and return sludge 1 of a secondary sedimentation tank, the raw water can be sewage entering a sewage plant, or sewage subjected to pretreatment (such as treatment of grating, sand setting, primary sedimentation and the like) after entering the sewage plant, the anaerobic tank is stirred to fully mix and react the sewage and the sludge, the stirring is usually carried out in a mechanical or hydraulic stirring mode, and air stirring is not adopted to avoid introducing dissolved oxygen, the reaction in the anaerobic tank refers to a biological process of microorganisms (namely active sludge) under the environment with low dissolved oxygen and low nitrate nitrogen concentration, namely, phosphorus in a body is released, and organic matters in water are absorbed to form PHB in the body, under the normal condition, the dissolved oxygen in the anaerobic tank is required to be less than 0.2 mg/L, the nitrate nitrogen concentration is required to be less than 0.5 mg/L, the excessive dissolved oxygen and nitrate nitrogen concentration can inhibit the anaerobic reaction of the microorganisms, the anaerobic tank can be arranged in a multi-lattice tank series connection mode, also can be arranged in a circulation mode, or a combination mode, the hydraulic time of the anaerobic tank is designed according to the water temperature, the pollutant concentration, the effluent concentration, the water concentration, the retention time and the like.
As a further improvement of the invention, raw water can enter the anaerobic tank by adopting a staged water inlet mode, one part of raw water enters the starting end of the anaerobic tank and is mixed with return sludge 1 of the secondary sedimentation tank entering the anaerobic tank, and the other part of raw water enters the anaerobic tank from the position behind the starting end. The return sludge from the secondary sedimentation tank contains nitrate nitrogen, so that the return sludge entering the anaerobic tank possibly influences the anaerobic process (phosphorus release and organic matter intake) of the anaerobic tank, a part of raw water (raw water 1, usually 10-30% of the total amount of the raw water) is firstly mixed with the return sludge 1 of the secondary sedimentation tank, the rest of raw water (raw water 2) enters water from the beginning end of the anaerobic tank, the purpose of removing the nitrate nitrogen in the return sludge 1 at the front section of the anaerobic tank (namely before the raw water 2 enters) is achieved, the influence of the nitrate nitrogen on the rear section of the anaerobic tank (namely after the raw water 2 enters) is avoided, and the hydraulic retention time of the front section of the anaerobic tank is generally 20-60 minutes.
The mud-water separation unit disclosed by the invention is used for carrying out mud-water separation on the mixed liquid flowing out of the anaerobic tank. The mud-water separation unit is provided with an inlet, a supernatant outlet and a sludge outlet. And after the mixed liquid from the anaerobic tank enters the sludge-water separation unit from the inlet for sludge-water separation, the supernatant flows out to the nitrification unit, and the sludge at the bottom flows out to the anoxic tank. The mixed liquid refers to a mixture of sewage and solid; the concentrated solution with higher solid content (solid content) than the mixed solution of the anaerobic tank is obtained at the lower part of the mud-water separation unit and is called sludge; the water having a low solid content obtained at the upper part of the slurry-water separation unit is referred to as a supernatant. The hydraulic retention time of the mud-water separation unit is designed according to factors such as sludge concentration, separation efficiency and the like, and is generally 0.5-3.0 hours.
The nitrification unit comprises a nitrification tank, the secondary sedimentation tank is provided with a sludge backflow inlet unit, the sludge backflow 2 of the secondary sedimentation tank and the supernatant from the sludge-water separation unit complete the nitrification reaction in the nitrification unit, and then the sludge flows out to the anoxic tank. The hydraulic retention time of the nitrification tank is designed according to factors such as sludge concentration, pollutant concentration, water temperature and water outlet requirements, and is generally 2.0-8.0 hours.
As a further improvement of the invention, the nitrification unit can be only a nitrification tank, the inlet water comes from the supernatant of the mud-water separation unit and the return sludge 2 of the secondary sedimentation tank, oxygenation and mixing are realized in the tank through aeration, and microorganisms oxidize ammonia nitrogen in the water in an aerobic environment to generate nitrate nitrogen. The nitrification efficiency of the nitrification tank is high because: firstly, the returned sludge in the secondary sedimentation tank flows through the aerobic tank and the secondary sedimentation tank before returning, and organic matters are consumed after full aerobic biological reaction in the aerobic tank, so that the influence of the organic matters on the nitration process is avoided; and secondly, the supernatant of the mud-water separation unit passes through the anaerobic process of the anaerobic tank, most of organic matters are transferred into microorganisms, and the influence of the organic matters on the nitrification process is also avoided. In order to strengthen the nitration reaction, biological fillers can be added into the nitration tank.
As a further improvement of the invention, the nitrification unit can be a combination of a mixing tank and a nitrification tank, and supernatant of the sludge-water separation unit and the return sludge 2 of the secondary sedimentation tank enter the mixing tank and then enter the nitrification tank. The muddy water is completely mixed in the mixing tank by stirring modes such as mechanical stirring, hydraulic stirring and the like, and aeration and oxygenation are not carried out; aerating in the nitrification tank. Because the return sludge of the secondary sedimentation tank contains nitrate nitrogen, the supernatant of the mud-water separation unit still contains organic matters (the higher the COD in the raw water is, the higher the COD in the supernatant is), and the arrangement of the mixing tank is beneficial to fully utilizing the organic matters in the supernatant of the mud-water separation unit to remove the nitrate nitrogen in the return sludge 2, is beneficial to more efficiently utilizing a carbon source in the raw water and improves the denitrification effect. On the other hand, the arrangement of the mixing tank can further reduce the concentration of the organic matters entering the nitrification tank, and is beneficial to improving the nitrification effect of the nitrification tank. The residence time of the mixing tank is generally 20-120 minutes, and the residence time of the nitrification tank is generally 2.0-8.0 hours.
The water (sludge) entering the anoxic tank comprises a mixed liquid from a nitrification unit and sludge from a sludge-water separation unit, and the mixed liquid and the sludge are mixed and reacted in the anoxic tank through mechanical stirring, hydraulic stirring and the like, wherein the reaction in the anoxic tank refers to denitrification of organic matters and nitrate nitrogen by using microorganisms, the nitrate nitrogen is reduced into nitrogen while the organic matters are oxidized, and in the anoxic tank, the organic matters are mainly stored in microorganisms in a PHB form, and synchronous phosphorus removal can be realized while denitrification is performed, particularly, one-carbon dual-purpose is realized for low-carbon nitrogen sewage, the nitrogen and phosphorus removal effects of the sewage can be greatly improved, aeration and oxygenation are not performed in the anoxic tank, the dissolved oxygen requirement is as low as possible, usually not more than 0.5 mg/L, so that the anoxic denitrification process of the microorganisms is facilitated, and the designed hydraulic retention time of the anoxic tank is selected according to factors such as sludge concentration, pollutant concentration, water temperature and effluent requirement, and the like, and is generally 1.5-5.0 hour.
The water inlet of the aerobic tank of the invention is from the anoxic tank, and the aerobic tank is stirred and oxygenated by adopting aeration. Under the aerobic condition, the microorganisms further remove organic matters and ammonia nitrogen in the water, and simultaneously further reduce the concentration of phosphorus in the water through aerobic phosphorus absorption. With the tradition A2Compared with the O process, in the system of the invention, most of organic matters, ammonia nitrogen and phosphorus are removed in a unit before an aerobic tank, and the aerobic tank is used for more thoroughly removing pollutants in water. When the raw water has good quality and low pollutant content, the retention time of the aerobic tank can be reduced, or the aerobic tank can be operatedThe aeration quantity of the aerobic tank is reduced in the process, and the main function of the aerobic tank is to blow off nitrogen generated by denitrification in the anoxic tank, so that the condition that sludge containing fine bubbles cannot be normally precipitated in the secondary precipitation tank is avoided. The designed hydraulic retention time of the aerobic tank is selected according to factors such as sludge concentration, pollutant concentration, water temperature and water outlet requirements, and is generally 0.5-5.0 hours.
As a further improvement of the invention, a nitrifying liquid return pipeline from the aerobic tank to the anoxic tank can be arranged, and the mixed liquid after reaction in the aerobic tank is conveyed to the anoxic tank through the nitrifying liquid return pipeline. The return pipeline can be in the form of a pipeline, a channel, a perforated wall and the like from the aerobic tank to the anoxic tank. The reaction in the aerobic tank refers to the action of aerobic organisms of microorganisms in an aerobic environment, under the action, ammonia nitrogen in sewage is oxidized into nitrate nitrogen, and the mixed liquid rich in the nitrate nitrogen is also called nitrifying liquid. The reflux ratio of the nitrifying liquid (the ratio of the flow of the nitrifying liquid to the flow of raw water) is generally 0-200%, and in the actual operation process of the system, the reflux ratio is adjusted according to the concentration of pollutants (especially total nitrogen), the effluent standard, design parameters of other units in the system, the operation condition and other factors, or the reflux ratio is adjusted in real time according to the standard reaching condition of the total nitrogen of the effluent. For example, when the total nitrogen concentration of the feed water is not high (e.g.<45 mg/L), when the effluent is the first-class A standard, the reflux ratio can be 0 percent, namely, the reflux of the nitrifying liquid is not started, and when the total nitrogen concentration of the influent is high (for example, the total nitrogen concentration is high)>45 mg/L) or high effluent standard (e.g.. ltoreq.10 mg/L), the nitrification liquid reflux is started, and the denitrification effect can be enhanced and the total nitrogen removal rate can be improved by utilizing the nitrification liquid reflux2In the/O and oxidation ditch process, in order to realize denitrification, nitrification liquid reflux is required to be set, and in order to achieve a high denitrification effect, the nitrification liquid reflux ratio generally reaches 100-300%.
The secondary sedimentation tank is provided with two sets of sludge reflows which respectively enter the anaerobic tank and the nitrification unit, the secondary sedimentation tank carries out sedimentation separation on mixed liquid from the aerobic tank, supernatant liquid flows out as effluent, one part of the precipitated sludge reflows to the anaerobic tank (reflowing sludge 1), one part of the precipitated sludge reflows to the nitrification unit (reflowing sludge 2), and the other part of the precipitated sludge is used as residual sludge to be discharged and treated. After the excess sludge is discharged, it is usually subjected to concentration, dehydration, and the like. The return sludge 1 and the return sludge 2 can be independently provided with a sludge return pump or a shared sludge return pump.
As a further improvement of the invention, a chemical phosphorus removal unit can be arranged, the chemical phosphorus removal unit comprises a reaction tank and a sedimentation tank, 5-30% of the supernatant of the mud-water separation unit enters the chemical phosphorus removal unit, a chemical phosphorus removal agent is added into the reaction tank, the mixture is stirred and reacted, then the mixture enters the sedimentation tank, the supernatant after sedimentation enters a nitrification unit, and the sludge is discharged and treated. Because the phosphorus concentration of the supernatant of the mud-water separation unit can reach more than 2-4 times of the phosphorus concentration of the raw water, the phosphorus removal capability of the system can be greatly improved even if 5-30% of the supernatant is subjected to phosphorus removal treatment.
The process of the system comprises the following specific processes:
A. raw water enters an anaerobic tank;
B. the mixed liquid treated by the anaerobic tank enters a mud-water separation unit;
C. the sludge treated by the sludge-water separation unit enters an anoxic tank, and the supernatant enters a nitrification unit;
D. the mixed liquid treated by the nitrification unit enters an anoxic tank;
as a further development of the invention, the nitrification unit can be provided in different forms.
D01: the nitrification unit is only a nitrification tank;
d02: the nitrification unit comprises a mixing tank and a nitrification tank.
E. The mixed liquid in the anoxic tank enters an aerobic tank;
as a further improvement of the invention, a nitrifying liquid return pipeline can be arranged between the aerobic tank and the anoxic tank, and the mixed liquid after reaction in the aerobic tank is conveyed to the anoxic tank through the nitrifying liquid return pipeline.
F. The mixed liquid in the aerobic tank enters a secondary sedimentation tank;
G. and (4) refluxing and discharging sludge generated in the secondary sedimentation tank, and allowing supernatant to flow out as effluent. And returning a part of sludge generated by precipitation to the anaerobic tank, returning a part of sludge to the nitrification unit, and discharging other sludge as residual sludge.
The beneficial effects of the invention over the prior art include, but are not limited to:
(1) the invention overcomes A2The method has the advantages that the method has the problem of insufficient nitrogen and phosphorus removal capability in the O/oxidation ditch process, has good nitrogen and phosphorus removal effect, and can solve the problems of insufficient denitrification carbon source and difficult standard reaching of total nitrogen and total phosphorus in effluent particularly for the treatment of sewage with low carbon-nitrogen ratio.
(2) The system of the invention introduces the return sludge of the secondary sedimentation tank into the nitrification unit, the nitrification unit comprises a nitrification tank, and the activated sludge is utilized for nitrification. Compared with a double-sludge process combining activated sludge and filler, the double-sludge process reduces one set of sludge system, reduces the use of the filler, effectively avoids the work of installing and replacing the filler and the like, reduces the construction cost and simplifies the operation and maintenance cost. Compared with the double-sludge process combining activated sludge and activated sludge, the method avoids the arrangement of a sedimentation tank behind a nitrification tank, and reduces the occupied area and the construction and operation costs.
(3) The nitrification efficiency of the nitrification tank in the system is high. When organic matters (soluble organic matters and organic matters in the activated sludge) in the system are fully consumed, the influence of the organic matters on the nitrification of the activated sludge is small, and the nitrification rate of the activated sludge can be greatly improved. General A2In the processes of/O, oxidation ditch and the like, the nitrification efficiency of the front section in the aerobic tank is low due to the existence of organic matters. In the invention, firstly, the returned sludge in the secondary sedimentation tank flows through the aerobic tank and the secondary sedimentation tank before returning, and organic matters are consumed after full aerobic biological reaction in the aerobic tank, thereby avoiding the influence of the organic matters on the nitration process; and secondly, the supernatant of the mud-water separation unit passes through the anaerobic process of the anaerobic tank, most of organic matters are transferred into microorganisms, and the influence of the organic matters on the nitrification process is also avoided.
(4) The preposed mixing tank of the nitrification tank in the nitrification unit is an important extension of the invention, and has the advantages that ① can enhance the denitrification effect of the system, organic matters in the supernatant of the sludge-water separation unit can be fully utilized to remove part of nitrate nitrogen in the returned sludge 2 from the secondary sedimentation tank, ② enhances the nitrification effect, and due to the denitrification effect of the mixing tank, the concentration of carbon sources entering the nitrification tank is reduced, a more appropriate habitat is provided for nitrifying bacteria, and the improvement of the nitrification effect is facilitated.
Drawings
FIG. 1 is a schematic flow chart of a system for removing nitrogen and phosphorus from wastewater according to the present invention;
FIG. 2 is a schematic diagram of different arrangement modes of nitrification units of examples 1 and 2 of the present invention, wherein FIG. 2A is a scheme of only a nitrification unit of a nitrification tank in example 1, and FIG. 2B is a scheme of a nitrification unit of a mixing tank and a nitrification tank in series in example 2;
FIG. 3 is a schematic flow chart of a staged water feeding mode of an anaerobic tank in embodiment 3 of the invention;
FIG. 4 is a schematic flow chart of a nitrifying liquid return pipeline provided with an aerobic tank in example 4 of the present invention;
FIG. 5 is a schematic flow chart of a chemical phosphorus removal unit in example 5 of the present invention;
FIG. 6 is a processing effect diagram of the present invention, wherein FIG. 6A is a processing effect diagram of embodiment 1, and FIG. 6B is a processing effect diagram of embodiment 2.
Detailed Description
The present invention and its effective technical effects will be described in further detail below with reference to examples and drawings, showing specific forms in actual industrial applications, but the embodiments of the invention are not limited thereto.
Example 1:
the sewage nitrogen and phosphorus removal treatment system shown in fig. 2A is formed by sequentially connecting an anaerobic tank, a mud-water separation unit, an anoxic tank, an aerobic tank and a secondary sedimentation tank, and is further provided with a nitrification unit, wherein the water inlet flow rate Q is 10L/h, the anaerobic tank is provided with inlets for raw water and return sludge 1 of the secondary sedimentation tank, the nitrification unit only comprises a nitrification tank, supernatant separated by the mud-water separation unit and return sludge 2 of the secondary sedimentation tank enter the nitrification tank, mixed liquid flowing out of the nitrification tank and sludge flowing out of the mud-water separation unit enter the anoxic tank, mixed liquid flowing out of the anoxic tank enter the aerobic tank, mixed liquid flowing out of the aerobic tank enters the secondary sedimentation tank, the secondary sedimentation tank is provided with a water outlet, part of sludge of the secondary sedimentation tank returns to the anaerobic tank, part of sludge returns to the nitrification tank, and.
The retention time (according to a water inlet flow meter) is respectively 2.5h of an anaerobic tank, 1.5h of a mud-water separation unit, 4h of a nitrification tank, 3.5h of an anoxic tank, 2.5h of an aerobic tank and 3.0h of a secondary sedimentation tank, the flow rates of returned sludge 1 and returned sludge 2 in the anaerobic tank are both 5L/h, the discharge amount of residual sludge is calculated according to 15-20 days of sludge age, and the flow rate of supernatant liquid of mud-water separation is 10L/h.
FIG. 6A shows that the system has good denitrification and dephosphorization effects on domestic sewage in the case of low carbon source, the total nitrogen in the effluent reaches 12.1 mg/L and the total phosphorus reaches 0.39 mg/L, the effluent stably reaches the first-level A standard, and the denitrification and dephosphorization capability is superior to that of the traditional A standard2The process is carried out by adopting a/O technology.
Example 2
The sewage nitrogen and phosphorus removal treatment system shown in fig. 2B is formed by connecting an anaerobic tank, a sludge-water separation unit, an anoxic tank, an aerobic tank and a secondary sedimentation tank in sequence, and is further provided with a nitrification unit, wherein the water inlet flow rate Q is 10L/h, the anaerobic tank is provided with inlets for raw water and secondary sedimentation tank return sludge 1, the nitrification unit comprises a mixing tank and a nitrification tank, supernatant separated by the sludge-water separation unit and secondary sedimentation tank return sludge 2 enter the mixing tank, mixed liquid flowing out of the mixing tank enters the nitrification tank, mixed liquid flowing out of the nitrification tank and sludge flowing out of the sludge-water separation unit enter the anoxic tank, mixed liquid flowing out of the anoxic tank enters the aerobic tank, mixed liquid flowing out of the aerobic tank enters the secondary sedimentation tank, the secondary sedimentation tank is provided with a water outlet, a part of the secondary sedimentation tank returns to the anaerobic tank, a part of the sludge flows back to the.
The retention time (according to a water inlet flow meter) is respectively 2.5h of an anaerobic tank, 1.5h of a mud-water separation unit, 40min of a mixing tank, 4h of a nitrification tank, 3.5h of an anoxic tank, 2.5h of an aerobic tank and 3.0h of a secondary sedimentation tank, the flow rates of returned sludge 1 and returned sludge 2 in the anaerobic tank are both 5L/h, the discharge amount of residual sludge is calculated according to 15-20 days of sludge age, and the flow rate of supernatant liquid of mud-water separation is 10L/h.
Compared with the embodiment 1, the nitrification unit of the embodiment adds a mixing tank, and the rest of the arrangement is the same.
FIG. 6B shows the average removal effect of the system in this example on ammonia nitrogen, total phosphorus and COD over a long period of time, compared with example 1, the effluent concentration of total phosphorus and COD is not significantly different, while the ammonia nitrogen is reduced by 0.4 mg/L, and the total nitrogen is reduced by 2.0 mg/L, which indicates that the denitrification capability of the system is improved by the arrangement of the mixing tank.
Embodiment 3
The sewage nitrogen and phosphorus removal treatment system shown in fig. 3 is formed by sequentially connecting an anaerobic tank, a sludge-water separation unit, an anoxic tank, an aerobic tank and a secondary sedimentation tank, and is further provided with a nitrification unit, wherein the water inlet flow rate Q is 10L/h, the anaerobic tank is provided with inlets for raw water and secondary sedimentation tank return sludge 1, the nitrification unit comprises a mixing tank and a nitrification tank, supernatant separated by the sludge-water separation unit and secondary sedimentation tank return sludge 2 enter the mixing tank, mixed liquid flowing out of the mixing tank enters the nitrification tank, mixed liquid flowing out of the nitrification tank and sludge flowing out of the sludge-water separation unit enter the anoxic tank, mixed liquid flowing out of the anoxic tank enters the aerobic tank, mixed liquid flowing out of the aerobic tank enters the secondary sedimentation tank, the secondary sedimentation tank is provided with a water outlet, a part of the secondary sedimentation tank returns to the anaerobic tank, a part of the sludge flows back to the nitrification.
The retention time (according to a water inlet flow meter) is respectively 2.5h of an anaerobic tank, 1.5h of a mud-water separation unit, 30min of a mixing tank, 4h of a nitrification tank, 3.5h of an anoxic tank, 2.5h of an aerobic tank and 3.0h of a secondary sedimentation tank, the flow rates of returned sludge 1 and returned sludge 2 in the anaerobic tank are both 5L/h, the discharge amount of residual sludge is calculated according to 15-20 days of sludge age, and the flow rate of supernatant liquid of mud-water separation is 10L/h.
Different from the embodiment 2, the anaerobic tank is divided into four tanks which are connected in series, and raw water enters the anaerobic tank in a sectional water inlet mode. 25% of raw water enters the first grid pool, 75% of raw water enters the second grid pool, and all returned sludge enters the first grid pool.
Compared with the embodiment 2, the system has no significant difference in removing COD, ammonia nitrogen and total nitrogen, the average concentration of total phosphorus in the effluent of the anaerobic tank can be improved by about 1.0 mg/L, the stability of removing the total phosphorus by the system is improved, and the average concentration of the total phosphorus in the effluent of the system is reduced by 0.03 mg/L.
Example 4
The sewage nitrogen and phosphorus removal treatment system shown in fig. 4 is formed by sequentially connecting an anaerobic tank, a mud-water separation unit, an anoxic tank, an aerobic tank and a secondary sedimentation tank, and is further provided with a nitrification unit, wherein the water inlet flow rate Q is 10L/h, the anaerobic tank is provided with inlets for raw water and return sludge 1 of the secondary sedimentation tank, the nitrification unit is only a nitrification tank, supernatant of the mud-water separation unit enters the nitrification tank, mixed liquid flowing out of the nitrification tank and sludge flowing out of the mud-water separation unit enter the anoxic tank, mixed liquid flowing out of the anoxic tank enters the aerobic tank, the aerobic tank is provided with a nitrified liquid return pipeline to the anoxic tank, mixed liquid flowing out of the aerobic tank enters the secondary sedimentation tank, the secondary sedimentation tank is provided with a water outlet, part of sludge in the secondary sedimentation tank returns to the anaerobic tank, part of sludge returns to the.
The retention time (according to a water inlet flow meter) is respectively 2.5h of an anaerobic tank, 1.5h of a mud-water separation unit, 30min of a mixing tank, 4h of a nitrification tank, 3.5h of an anoxic tank, 2.5h of an aerobic tank and 3.0h of a secondary sedimentation tank, the flow rates of returned sludge 1 and returned sludge 2 in the anaerobic tank are both 5L/h, the discharge amount of residual sludge is calculated according to 15-20 days of sludge age, the flow rate of supernatant liquid of mud-water separation is 10L/h, and the return amount of nitrified liquid is 10L/h.
Compared with the example 1, the method increases the return flow of the nitrifying liquid, and compared with the example 1, the method has no significant difference in the removal of COD, ammonia nitrogen and total phosphorus, and improves the removal amount of the total nitrogen by 2.8 mg/L.
Example 5:
the sewage nitrogen and phosphorus removal treatment system shown in fig. 5 is formed by sequentially connecting an anaerobic tank, a sludge-water separation unit, an anoxic tank, an aerobic tank and a secondary sedimentation tank, and is further provided with a nitrification unit and a phosphorus removal unit, wherein the inflow rate Q is 10L/h, the anaerobic tank is provided with inlets for raw water and return sludge 1 of the secondary sedimentation tank, the nitrification unit comprises a mixing tank and a nitrification tank, 10% of supernatant of the sludge-water separation unit enters the phosphorus removal unit, the rest 90% of supernatant and water of the phosphorus removal unit are discharged, return sludge 2 of the secondary sedimentation tank enters the mixing tank, mixed liquid flowing out of the mixing tank enters the nitrification tank, mixed liquid flowing out of the nitrification tank and sludge flowing out of the sludge-water separation unit enter the anoxic tank, mixed liquid flowing out of the anoxic tank enters the aerobic tank, mixed liquid flowing out of the aerobic tank enters the secondary sedimentation tank, the secondary sedimentation tank is provided with a water outlet, a part of sludge of the secondary sedimentation tank returns to the.
The retention time (according to a water inlet flow meter) is respectively 2.5h of an anaerobic tank, 1.5h of a mud-water separation unit, 30min of a mixing tank, 4h of a nitrification tank, 3.5h of an anoxic tank, 2.5h of an aerobic tank and 3.0h of a secondary sedimentation tank, 0.05h of a reaction tank of a phosphorus removal unit, 0.2h of a sedimentation tank, the flow rates of the reflux sludge 1 and the reflux sludge 2 of the anaerobic tank are both 5L/h, the discharge amount of the residual sludge is calculated according to the sludge age of 15-20 days, and the flow rate of supernatant liquid of mud-water separation is 10L/h.
Compared with the embodiment 2, the system has no significant difference in removal of COD, ammonia nitrogen and total nitrogen, the removal capability of the system on phosphorus is significantly improved, and the average concentration of total phosphorus in effluent is reduced to 0.12 mg/L.
The foregoing is a more detailed description of the invention in connection with specific preferred embodiments and it is not intended that the invention be limited to these specific details. For those skilled in the art to which the invention pertains, several simple deductions or substitutions can be made without departing from the spirit of the invention, and all shall be considered as belonging to the protection scope of the invention.
Claims (9)
1. A sewage nitrogen and phosphorus removal system is characterized in that: the device is formed by sequentially connecting an anaerobic tank, a sludge-water separation unit, an anoxic tank, an aerobic tank and a secondary sedimentation tank, and is also provided with a nitrification unit, wherein the anaerobic tank is provided with an inlet of raw water, secondary sedimentation tank backflow sludge (1) enters the anaerobic tank, the nitrification unit contains a nitrification tank, supernatant separated by the sludge-water separation unit and secondary sedimentation tank backflow sludge (2) enter the nitrification unit, a carbon source in the raw water is utilized, mixed liquid flowing out of the nitrification unit and sludge flowing out of the sludge-water separation unit enter the anoxic tank, mixed liquid flowing out of the anoxic tank enters the aerobic tank, mixed liquid flowing out of the aerobic tank enters the secondary sedimentation tank, and the secondary sedimentation tank is provided with a water outlet and a sludge outlet.
2. The sewage nitrogen and phosphorus removal system of claim 1, wherein: the anaerobic tank is provided with inlets of raw water and secondary sedimentation tank return sludge (1), and the raw water and the secondary sedimentation tank return sludge (1) are stirred in the anaerobic tank to realize mixing and reaction after entering the anaerobic tank, and then flow out to the mud-water separation unit.
3. The sewage nitrogen and phosphorus removal system of claim 2, wherein: raw water enters the anaerobic tank in a sectional water inlet mode, one part of raw water enters the initial end of the anaerobic tank and is mixed with return sludge (1) of the secondary sedimentation tank entering the anaerobic tank, and the other part of raw water enters the anaerobic tank from the position behind the initial end.
4. The sewage nitrogen and phosphorus removal system of claim 1, wherein: the sludge-water separation unit is provided with an inlet, a supernatant outlet and a sludge outlet, and after mixed liquid from the anaerobic tank enters the sludge-water separation unit from the inlet for sludge-water separation, the supernatant flows out to the nitrification unit, and the sludge flows out to the anoxic tank.
5. The sewage nitrogen and phosphorus removal system of claim 1, wherein: the nitrification unit is only a nitrification tank, aeration is arranged in the nitrification tank, supernatant from the mud-water separation unit and return sludge (2) from the secondary sedimentation tank enter the nitrification tank, are mixed and react in the nitrification tank, and then flow out to the anoxic tank; or the nitrification unit is a combination of a mixing tank and a nitrification tank, supernatant from the mud-water separation unit and return sludge (2) from the secondary sedimentation tank enter the mixing tank, are mixed and reacted in the mixing tank through stirring, then enter the nitrification tank, are mixed and reacted in the nitrification tank through aeration, and mixed liquor in the nitrification tank flows out to the anoxic tank.
6. The sewage nitrogen and phosphorus removal system of claim 1, wherein: the mixed liquid from the nitrification unit and the sludge from the mud-water separation unit enter an anoxic tank, are mixed and reacted in the anoxic tank through stirring, and then flow out to an aerobic tank.
7. The sewage nitrogen and phosphorus removal system of claim 1, wherein: the mixed liquid from the anoxic tank enters the aerobic tank, and the mixed liquid is mixed and reacted in the aerobic tank through aeration and then flows out to the secondary sedimentation tank.
8. The system of claim 6 or 7, wherein: a nitrifying liquid return pipeline is arranged between the anoxic tank and the aerobic tank, and the reacted mixed liquid in the aerobic tank is conveyed to the anoxic tank through the return pipeline.
9. The sewage nitrogen and phosphorus removal system of claim 1, wherein: the secondary sedimentation tank is provided with a water outlet and a sludge outlet, the secondary sedimentation tank carries out sedimentation separation on the mixed liquid from the aerobic tank, supernatant liquid flows out as effluent, the precipitated sludge flows out from the sludge outlet, one part of the precipitated sludge flows back to the anaerobic tank, one part of the precipitated sludge flows back to the nitrification unit, and the other part of the precipitated sludge is used as residual sludge to be discharged and treated.
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| CN108793614B (en) * | 2018-07-12 | 2021-04-20 | 军事科学院军事医学研究院环境医学与作业医学研究所 | Continuous sewage treatment method and device |
| CN108821517A (en) * | 2018-07-31 | 2018-11-16 | 中交信远(北京)建设工程有限公司 | A kind of sewage disposal device and its processing method |
| CN109179652A (en) * | 2018-08-16 | 2019-01-11 | 海天水务集团股份公司 | A kind of low C/N is than organic wastewater denitrifying method |
| CN109320012B (en) * | 2018-10-26 | 2021-11-09 | 首创爱华(天津)市政环境工程有限公司 | Municipal sewage treatment system and method |
| CN109293164A (en) * | 2018-11-09 | 2019-02-01 | 深圳市市政设计研究院有限公司 | A kind of method of sewage deep denitrogenation dephosphorizing |
| CN110217892B (en) * | 2019-04-28 | 2020-07-03 | 皇宝（福建）环保工程投资有限公司 | Sewage nitrogen and phosphorus removal process based on integrated biochemical reaction tank |
| CN110606629B (en) * | 2019-10-15 | 2024-08-20 | 北京首创股份有限公司 | System and method for treating urban sewage based on denitrification dephosphorization process |
| CN110950503A (en) * | 2019-12-25 | 2020-04-03 | 北京博汇特环保科技股份有限公司 | Integrated sewage biochemical treatment device |
| CN111847799B (en) * | 2020-08-03 | 2022-06-03 | 苏州博净源环境科技有限公司 | Method for removing nitrogen in water |
| CN112723666A (en) * | 2020-12-17 | 2021-04-30 | 天津创业环保集团股份有限公司 | AHCR-A2O sewage treatment system and sewage treatment method |
| CN113735378B (en) * | 2021-09-15 | 2023-05-30 | 北控(秦皇岛)水务有限责任公司 | Sewage treatment system and method for denitrification and dephosphorization |
| CN115626748B (en) * | 2022-11-29 | 2023-08-15 | 深圳永清水务有限责任公司 | Sewage treatment system for denitrification and dephosphorization |
| CN116239227B (en) * | 2023-04-28 | 2023-11-07 | 湖南星湘盈环保科技有限公司 | Tower type sewage treatment plant of cover |
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