CN113072184A - Anaerobic ammonia oxidation based independent denitrification 'coupled' system and water treatment method - Google Patents

Anaerobic ammonia oxidation based independent denitrification 'coupled' system and water treatment method Download PDF

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CN113072184A
CN113072184A CN202110403239.3A CN202110403239A CN113072184A CN 113072184 A CN113072184 A CN 113072184A CN 202110403239 A CN202110403239 A CN 202110403239A CN 113072184 A CN113072184 A CN 113072184A
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denitrification
ammonia oxidation
anaerobic ammonia
effluent
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CN113072184B (en
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杨宏
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Tianchao Environmental Technology Beijing Co ltd
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    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/30Aerobic and anaerobic processes
    • C02F3/302Nitrification and denitrification treatment
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/30Aerobic and anaerobic processes
    • C02F3/302Nitrification and denitrification treatment
    • C02F3/307Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00Biological treatment of water, waste water, or sewage
    • C02F3/30Aerobic and anaerobic processes
    • C02F3/308Biological phosphorus removal
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00Nature of the contaminant
    • C02F2101/10Inorganic compounds
    • C02F2101/16Nitrogen compounds, e.g. ammonia
    • CCHEMISTRY; METALLURGY
    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02FTREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00General aspects of water treatment
    • C02F2301/08Multistage treatments, e.g. repetition of the same process step under different conditions
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02WCLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00Technologies for wastewater treatment
    • Y02W10/10Biological treatment of water, waste water, or sewage

Abstract

An anaerobic ammonia oxidation based independent denitrification 'coupling' system and a water treatment method belong to the technical field of sewage treatment. The sewage and wastewater nitrogen and phosphorus removal treatment process taking anaerobic ammonia oxidation as the core is established by relying on hydrolytic acidification bioactive fillers, short-range nitrification bioactive fillers, denitrification bioactive fillers, anaerobic ammonia oxidation (denitrifying bacteria are rarely or not exist and relatively pure anaerobic ammonia oxidation bacteria) bioactive fillers and independent biological phosphorus removal unit technology established by an activated sludge method, and various technical problems of low-concentration, low-temperature nitrogen-containing sewage and wastewater treatment of the prior anaerobic ammonia oxidation can be well solved, so that deep nitrogen and phosphorus removal is realized.

Description

Anaerobic ammonia oxidation based independent denitrification 'coupled' system and water treatment method
The technical field is as follows:
the invention belongs to the field of sewage and wastewater treatment, and particularly relates to an anaerobic ammonia oxidation based independent denitrification coupled sewage and wastewater treatment technology.
Background art:
since 1977, the Engelbert Broda of the Austrian theory chemist concluded that anammox was present in the world, the university of Dutch Delff's technology began research into water treatment denitrification process technology using anammox bacteria (AAOB) in the 90's 20 th century. The formed technology is widely applied to research and engineering practice of denitrification treatment of various high ammonia nitrogen sewage and waste water such as sludge digestive fluid, garbage leachate and the like all over the world at present. Anaerobic ammonia oxidation (ANAMMOX) has not been shown to be the most economical biological denitrification pathway in various applications.
In recent decades, including water treatment workers in the Netherlands and China, the technical method is applied to denitrification treatment of sewage and wastewater with relatively low concentration (relative to the nitrogen content of hundreds or even thousands of PPM) and relatively low temperature (relative to 34 ℃ which is suitable for ANAMMOX reaction). In the research and application technology development process, ANAMMOX shows certain capability advantages and advantages independent of an external carbon source compared with the traditional whole-course biological denitrification technology, but in the research and practice process, technical obstacles which are difficult to overcome at present are also shown, so that the ANAMMOX technology has no substantial breakthrough and wide successful application range in biological denitrification aiming at low-temperature and low-ammonia nitrogen sewage.
The following problems exist around these studies, in particular summary of the applied studies:
(1) early applications of ANAMMOX technology, represented by the Netherlands, formed OLAND, CANON, SHARO N-ANAMMOX. The technologies are applied internationally and domestically in China on a large scale aiming at the treatment of high-concentration nitrogen-containing wastewater such as sludge digestive fluid, garbage leachate and the like. In the application process, the suspended particle sludge method is adopted, so that serious bacterial loss exists, the growth rate of Anaerobic Ammonium Oxidation Bacteria (AAOB) is low, and the bacteria with slow overall growth rate is undoubtedly a fatal defect. In recent years, an attached growth mode is applied domestically, so that the bacterial loss phenomenon is relieved, and the stability of a reaction system is improved to a certain extent.
(2) Aiming at the three processes, in the construction of an ANAMMOX system, a low dissolved oxygen control mode is adopted in a nitrosation control stage. The OLAND process directly adopts low dissolved oxygen to control the nitrosation process; in the CANON process, Ammonia Oxidizing Bacteria (AOB) exist on the outer surface of ANAMMOX granular sludge, and the maintenance of a low dissolved oxygen state is strictly controlled in a reaction system in order to not influence the anaerobic environment required by internal AAOB and control the generation of nitrate nitrogen in the ammonia nitrogen oxidation process; in order to control the generation of nitrate nitrogen in the ammonia nitrogen oxidation process, the SHARON-ANAMMOX process not only controls low dissolved oxygen, but also utilizes the inhibition of Free Ammonia (FA) and Free Nitrite (FNA) in a reaction system on Nitrite Oxidizing Bacteria (NOB) in the ammonia nitrogen oxidation process so as to control the generation of nitrate nitrogen in the ammonia oxidation process. The process adopts low dissolved oxygen technique, which results in biochemical treatment of ANAMMOXThe high efficiency of the process is difficult to exert, and the low efficiency (many are 0.5 Kg/m) of the whole AN AMMOX denitrification system at present is formed3D or so).
(3) The third point is also the most critical, in the ANAMMOX denitrification system, the proportion of ammonia nitrogen and nitrite nitrogen entering the ANAMMOX reaction process (1: 1.32), nitrate nitrogen existing in the ammonia nitrogen oxidation or raw water, and the problem that nitrate nitrogen with the proportion of 0.26mol is generated by oxidizing 1mol of ammonia nitrogen in the ANAMMOX reaction process. The existence of the nitrate nitrogen directly influences the discharge of the effluent total nitrogen of the reaction system after reaching the standard. In this regard, researchers thought about a decade ago that this portion of nitrate nitrogen was treated with denitrifying bacteria (DNB) in ANAMMOX granular sludge or systems. The formed thought is as follows: denitrifying bacteria mixed in anaerobic ammonium oxidation granular flora are utilized to remove the part of nitrogen by denitrification reaction, the denitrifying process can be considered to convert nitrate nitrogen into nitrogen to be removed in the whole denitrifying process, the denitrifying process can also be considered to reduce the nitrate nitrogen into nitrite nitrogen, so that the part of nitrogen participates in the ANAMMOX reaction, and the optimal proportion (such as short-range denitrification technology) required by the ANAMMOX reaction is met by reducing the formation proportion of the ammonia nitrogen and the nitrite nitrogen (1: 1.0-1.2) in the process of oxidizing the ammonia nitrogen into the nitrite nitrogen during process operation. The above works play a more productive role in the control work of the total nitrogen effluent of the system. However, the system stability is difficult to control, because the activity expression of denitrifying bacteria mixed in the anaerobic ammonia oxidation granule flora is difficult to accurately control under the existing process conditions, and is often influenced by unstable organic matters (COD) in the system water intake and COD released by bacteria death in the ANAMMOX system (under the condition that a large amount of COD exists, nitrite nitrogen in the ANAMMOX system is easily reduced to form nitrogen by the denitrifying bacteria, and conversely, the denitrifying bacteria are difficult to reduce and remove nitrate nitrogen under the condition that the COD is insufficient), so that the direct combination of the AAOB + DNB mixture is difficult to control the biochemical activity expression of DNB (short-range denitrification and full-range denitrification), and is particularly suitable for practical engineering application.
(4) Furthermore, the optimum reaction temperature of AAOB bacteria is about 34 ℃, and the conventional ANAMMOX system can be more efficiently adapted to about 20 ℃ through domestication and adaptation of low temperature such as screening of Candida Brocadia fulgida, but the fact that the water temperature of less than 20 ℃ is objectively existed due to seasonal variation aiming at the treatment of a broad-spectrum sewage and wastewater. Therefore, this also limits the large-scale efficient use of the amammox technology.
The invention content is as follows:
despite the various disadvantages of ANAMMOX, it is still the most effective technique for denitrification and its ability to break free from biological denitrification. How to establish a technical system which mainly adopts an anaerobic ammonia oxidation technology and has strong adaptability and can ensure the control of the total nitrogen of final effluent? Is a very challenging task we are faced with.
The idea of technical establishment is as follows:
(1) raw water COD is controlled (or effectively utilized), and the amount of raw water COD entering an ANAMMOX reaction process is reduced;
(2) establishing a control system and a control method capable of controlling the biochemical reaction proceeding amount of Denitrification (DNB) (by establishing an independent denitrification unit, the control of DNB reaction intensity is realized in a carbon source adding amount control mode);
(3) in order to adapt to the requirement of nitrogen removal in a 'low-temperature' season, the capability defect of low biochemical efficiency of ANAMMOX reaction nitrogen removal under the low-temperature condition is compensated by utilizing a short-cut nitrification and denitrification nitrogen removal system.
Aiming at the existing problems, according to the technical establishment thought, the sewage and wastewater nitrogen and phosphorus removal treatment process taking anaerobic ammonia oxidation as the core is established by relying on the hydrolytic acidification bioactive filler, the short-cut nitrification bioactive filler, the denitrification bioactive filler, the anaerobic ammonia oxidation (few or no denitrifying bacteria exist and relatively pure anaerobic ammonia oxidation bacteria) bioactive filler developed by people and the independent biological phosphorus removal unit technology established by the activated sludge method, so that the various technical problems can be effectively solved, and the deep nitrogen and phosphorus removal is realized. The technical device and the process are shown in the attached figure 1.
An independent denitrification 'coupling' system based on anaerobic ammoxidation is characterized in that raw water (1) is connected with a hydrolysis acidification device (A) and used as inlet water of the hydrolysis acidification device (A), wherein the hydrolysis acidification device (A) is filled with hydrolysis acidification embedded bioactive filler and used for hydrolysis acidification, hydrolysis acidification outlet water (2) of the hydrolysis acidification device (A) is connected with a primary denitrification device (B1) and used as inlet water of a primary denitrification device (B1), the primary denitrification device is filled with denitrification embedded bioactive filler and used for primary denitrification, primary denitrification outlet water (3) of the primary denitrification device (B1) is connected with a short-cut nitrification device (C) and used as inlet water of the short-cut nitrification device (C), the short-cut nitrification embedded bioactive filler is filled in the short-cut nitrification device and used for short-cut nitrification, and short-cut nitrification outlet water (4) of the short-cut nitrification device (C) is connected with the anaerobic ammoxidation device (D), anaerobic ammonia oxidation embedded biological active filler is filled in the anaerobic ammonia oxidation device and is used for anaerobic ammonia oxidation, anaerobic ammonia oxidation effluent (5) of the anaerobic ammonia oxidation device (D) is connected with a secondary denitrification device (B2), denitrification embedded biological active filler is filled in the secondary denitrification and is used for secondary denitrification, secondary denitrification effluent (6) of the secondary denitrification device (B2) is connected with a biological phosphorus removal device (E), biological phosphorus removal activated sludge is used for biological phosphorus removal in the biological phosphorus removal device, effluent (9) of the biological phosphorus removal device (E) is connected with a sludge settling device (F), and the sludge settling device (F) is used for settling sludge; one part of sludge precipitated in the sludge precipitation device (F) is discharged as excess sludge, and the other part of sludge is returned through a phosphorus removal sludge return pipeline (11) and is combined with secondary denitrification effluent (6) to enter a biological phosphorus removal device (E); a first external carbon source (G1) is connected with the anaerobic ammonia oxidation effluent (5) and is used for supplying the anaerobic ammonia oxidation effluent (5) with the external carbon source; a second external carbon source (G2) is connected with the secondary denitrification effluent (6) and is used for adding the external carbon source of the biological phosphorus removal unit; meanwhile, the secondary denitrification effluent (6) is also provided with a secondary denitrification effluent return pipeline (8) connected with the short-cut nitrification effluent (4); the short-cut nitrified effluent (4) is provided with a short-cut nitrified effluent return pipeline (7) which is connected with the hydrolyzed and acidified effluent (2).
The system composed of the reaction units has better flexibility by combining the independent biological phosphorus removal system composed of the short-cut nitrification water outlet return pipeline (7), the secondary denitrification return pipeline (8) and the subsequent biological phosphorus removal device (E) and the precipitated sludge device (F), thereby solving the four problems existing in the application of the anaerobic ammonia oxidation technology.
The water treatment method adopting the system comprises the following steps:
the first working condition is as follows: the water temperature is 20 ℃ or above, and most of the system depends on the denitrification of the anaerobic ammonia oxidation reaction;
the raw water sequentially passes through a hydrolytic acidification device (A), a primary denitrification device (B1), a short-cut nitrification device (C), an anaerobic ammonia oxidation device (D), a secondary denitrification device (B2), a biological phosphorus removal device (E) and a precipitated sludge device (F) to carry out hydrolytic acidification, primary denitrification, short-cut nitrification (partial short-cut nitrification), anaerobic ammonia oxidation, secondary denitrification and biological phosphorus removal; the working condition mainly depends on anaerobic ammonia oxidation for denitrification, the first-stage denitrification utilizes bioavailable organic matters (COD) in raw water through partial reflux of the shortcut nitrification liquid so as to reduce waste of the biochemical COD to organic matter oxidation in the next shortcut nitrification process and influence on the anaerobic ammonia oxidation, and the influence of nitrate brought by the raw water on the anaerobic ammonia oxidation can be eliminated in the process; part of reaction liquid after short-cut nitrification (the proportion of ammonia nitrogen and nitrite nitrogen is strictly controlled to be 1:1.32 theoretically, the amount of nitrite nitrogen returned by secondary denitrification backflow is considered during accounting), the reaction liquid enters an anaerobic ammonia oxidation device for denitrification, nitrate formed in the anaerobic ammonia oxidation process can be reduced through secondary denitrification, the secondary denitrification process is considered to be controlled to be a short-cut denitrification stage (the denitrification process is due to the arrangement of an independent denitrification unit (B2), the effective control of the short-cut denitrification can be realized through the control of the adding amount of a first external carbon source (G1) and then flows back to the anaerobic ammonia oxidation device through a secondary denitrification effluent return pipeline (8), and more thorough denitrification is realized; the secondary denitrification effluent (6) of the secondary denitrification device (B2) is connected with the biological phosphorus removal device (E) for biological phosphorus removal, and secondary carbon source feeding is carried out through a second external carbon source (G2) according to the phosphorus content of the secondary denitrification effluent (6); the effluent (9) of a biological phosphorus removal unit (mixed liquid containing sludge) of the biological phosphorus removal device (E) is connected with a sludge precipitation device (F), and the sludge precipitation device (F) is used for precipitating sludge; and a part of sludge precipitated in the sludge precipitation device (F) is discharged, and a part of sludge flows back to the secondary denitrification effluent (6) through a phosphorus removal sludge return pipeline (11) to enter the biological phosphorus removal device (E), so that the circulation of phosphorus removal activated sludge is realized.
Although the system still has the addition of an external carbon source, the high efficiency of the ANAMMOX denitrification is fully utilized, the effective control of the total nitrogen of the effluent of the system is realized, and the ideal index performance which is pursued in the industry at present and is difficult to deeply denitrify by simply applying the ANAMMOX denitrification is complemented. The adding amount of the carbon source is far less than that of the prior denitrification system. The system can be completely automatically controlled by adding a detection instrument and a control system in operation.
The second working condition is as follows: the water temperature is lower than 20 ℃, and the system part depends on anaerobic ammoxidation for denitrification and mainly depends on partial nitrification and denitrification for denitrification.
Raw water sequentially passes through a hydrolysis acidification device (A), a primary denitrification device (B1), a short-cut nitrification device (C), an anaerobic ammonia oxidation device (D), a secondary denitrification device (B2), a biological phosphorus removal device (E) and a precipitated sludge device (F) to be subjected to hydrolysis acidification, primary denitrification, short-cut nitrification, anaerobic ammonia oxidation, secondary denitrification and biological phosphorus removal; meanwhile, part of the short-cut nitrification effluent (4) is connected with a first-stage denitrification device (B1), namely hydrolysis acidification effluent (2), through a short-cut nitrification return pipeline (7); although anaerobic ammonia oxidation and denitrification are biochemical reactions, the adaptability of the two reactions to low temperature is greatly different;
the working condition mainly depends on short-range nitrification and denitrification (primary denitrification and secondary denitrification) for denitrification, the primary denitrification utilizes bioavailable organic matters (COD) in raw water through partial reflux (7) of short-range nitrification liquid so as to reduce waste of the biochemical COD to oxidize the organic matters in the short-range nitrification process; in the process state, for partial nitrification, reaction liquid after most of ammonia nitrogen is oxidized (partial ammonia nitrogen oxidation amount properly retains partial ammonia nitrogen according to biochemical capacity remained at low temperature of anaerobic ammonia oxidation) is correspondingly the residual part of partial nitrification effluent (4), the reaction liquid firstly enters an anaerobic ammonia oxidation device (D) for partial denitrification (the partial denitrification is the nitrogen amount which can be removed by utilizing the biochemical denitrification capacity remained at the ANAMMOX under the condition of low temperature), anaerobic ammonia oxidation effluent (5) (the effluent of the anaerobic ammonia oxidation (5) in the state contains most nitrite remained after the ANAMMOX (D) reaction and a small amount of nitrate generated by the ANAMMOX (D) reaction) completely enters a secondary denitrification device (B2) for denitrification, and the secondary denitrification process needs a first external carbon source (G1); the effluent (6) of the secondary denitrification device (B2) is connected with a biological phosphorus removal device (E) for biological phosphorus removal; the secondary denitrification device (B2) is used for reducing all nitrite nitrogen and nitrate nitrogen into nitrogen for removing, and the secondary denitrification return pipe (8) is not used for returning under the working condition. And simultaneously, adding a carbon source required by phosphorus removal by using a second external carbon source (G2). The effluent (9) of the biological phosphorus removal unit of the biological phosphorus removal device (E) is connected with a sludge precipitation device (F), and the sludge precipitation device (F) is used for precipitating sludge; and a part of sludge precipitated in the sludge precipitation device (F) is discharged, and a part of sludge flows back to the secondary denitrification effluent (6) through a phosphorus removal sludge return pipeline (11) to enter the biological phosphorus removal device (E), so that the circulation of phosphorus removal activated sludge is realized.
The system denitrification requires a relatively greater dependence of the first external carbon source (G1) than the first operating conditions. However, the whole system can adapt to stable denitrification in a low-temperature state due to the fact that the system can operate under the second working condition (relatively low temperature), and therefore the defect that the system is not suitable for low temperature due to the fact that the system only depends on anaerobic ammonia oxidation denitrification is overcome;
in the second working condition, the first additional carbon source G1 is mainly considered for low carbon-nitrogen ratio sewage (such as municipal sewage) and wastewater, and if the carbon source of the wastewater is not deficient, ideal denitrification can be realized by mainly relying on primary denitrification; the system is not applied with an external carbon source.
The method for treating three main pollutants (C, N, P) in sewage and wastewater by adopting the device according to the flow sequence comprises the following steps:
firstly, the method comprises the following steps: the hydrolysis acidification device (A) is utilized to establish an anaerobic hydrolysis acidification reaction process, so that macromolecular organic matters in raw water are hydrolyzed, long-chain and macromolecular substances are decomposed into micromolecular organic matters, organic nitrogen is released as far as possible in the process, and a better ammonia nitrogen oxidation condition and micromolecular organic matter electron acceptors as much as possible are provided for the oxidation and removal of ammonia nitrogen in the subsequent process.
Secondly, the method comprises the following steps: establishing a primary denitrification reaction process by utilizing a primary denitrification device (B1); the main function of the reaction process is to utilize nitrite nitrogen and nitrate nitrogen returned from the short-cut nitrification biological process (7) in the next stage, combine with hydrolysis acidification effluent (COD), carry out denitrification in the stage, and mainly aim to utilize anaerobic hydrolysis acidification effluent to remove organic matters which can be utilized by organisms, thereby ensuring that the subsequent biological process is influenced by the organic matters (COD) as little as possible or not, and creating good reaction conditions for anaerobic ammonia oxidation;
thirdly, the method comprises the following steps: establishing an aerobic short-cut nitrification reaction process by using a short-cut nitrification device (C); the part is subjected to a nitrification biochemical process of oxidizing ammonia nitrogen into nitrite nitrogen; aiming at the next anaerobic ammonia oxidation, partial nitrosation of ammonia nitrogen is carried out by partial nitrification according to the requirements of the subsequent process (the oxidation ratio of the ammonia nitrogen can be adjusted according to the requirements of the subsequent process);
fourthly: establishing an anaerobic ammonia oxidation reaction process by using an anaerobic ammonia oxidation device (D); the part utilizes ammonia nitrogen and nitrite nitrogen in the effluent (4) of the short-cut nitrification process to carry out ammonia nitrogen oxidation and nitrite nitrogen reduction processes, and nitrogen is generated to realize denitrification; in the process, the proportion of ammonia nitrogen and nitrite nitrogen of inflow water, namely the effluent water (4) of the short-cut nitrification process, is required by anaerobic ammonia oxidation (the proportion of the effluent water is required to be 1:1.32 under the first working condition, and the second low-temperature working condition is adjusted according to the biochemical capacity of subsequent anaerobic ammonia oxidation), nitrate nitrogen with the proportion of 0.26mol is generated by oxidizing 1mol of ammonia nitrogen in the reaction, and the part of nitrate nitrogen cannot be removed by utilizing a simple anaerobic ammonia oxidation process, so that a secondary denitrification biological process is established.
Fifth, the method comprises the following steps: establishing a secondary denitrification reaction process by utilizing a secondary denitrification device (B2); in the secondary denitrification process, the core main body of the biochemical reaction is denitrifying bacteria in the denitrifying embedded filler, the reaction substrate is nitrate generated in the anaerobic ammonia oxidation and denitrification process in the upper anaerobic ammonia oxidation device (D), and biochemical organic matters in water are almost completely utilized in the secondary denitrification stage after the reaction processes of the anaerobic ammonia oxidation device (D) are performed, so that the partial denitrification needs a first external carbon source (G1); the biological process of the secondary denitrification can realize two denitrification controls, and further calculate the amount of a first additional carbon source (G1) before the secondary denitrification by selecting different denitrification controls: firstly, the nitrate of the anaerobic ammonia oxidation effluent (5) at the section is completely denitrified, so that relatively more organic matters need to be added; the other control is that the part of nitrate nitrogen only completes the short-range denitrification, and then the effluent flows back to the anaerobic ammonia oxidation reaction process section through a secondary denitrification effluent return pipeline (8) to enable the generated part of nitrite to participate in the anaerobic ammonia oxidation denitrification process, so that part of carbon source required to be added can be saved relatively;
sixth: the independent biological phosphorus removal unit is built by activated sludge in the biological phosphorus removal device (E), and further comprises a subsequent sludge precipitation device (F) which consists of an anoxic part, an aerobic part and a precipitation part; the part can be constructed by phosphorus accumulating bacteria or phosphorus accumulating bacteria and denitrifying phosphorus removal bacteria, and has a stable biological phosphorus removal function. Because the biological phosphorus removal system after nitrogen removal is completed, deep phosphorus removal can be realized. The part needs to be added with a second external carbon source (G2) in the water inlet of the biological phosphorus removal unit. After the whole sewage and wastewater is subjected to the five denitrification processes, the total nitrogen of the effluent can be effectively controlled.
The system has the advantages that:
1. through the system design, a 'coupling' working form of two sets of systems after short-cut nitrification is established, the advantages of ANAMMOX (D) are fully utilized, and meanwhile, the system can have good adaptability under 'high-temperature' and 'low-temperature' conditions, and a technical approach is developed for the wider application of the anaerobic ammonia oxidation technology;
2. through the coupling design of pure ANAMMOX (D) and pure secondary denitrification device (B2), the control of the secondary denitrification (B2) on the nitrate reduction degree can be completely realized through the adjustment of the flow rate (8) and the control of the adding amount of the first external carbon source (G1), so that the denitrification degree is controllable (which completely surpasses the technology that the ANAMMOX and denitrifying bacteria are mixed in the same reactor at present and the denitrification intensity or degree is difficult to control); the establishment of the technical system can be simply realized only under the condition of establishing a pure ANAMMOX (D) and a pure secondary denitrification device (B2) by utilizing the embedded bioactive filler;
3. the secondary denitrification device (B2) realizes active total nitrogen control on the total nitrogen of the effluent (6) of the whole denitrification part system, and plays a final role in keeping the key for deep denitrification;
4. the separate arrangement of the independent first additional carbon source (G1) and the second additional carbon source (G2) allows effective control of the degree of denitrification by secondary denitrification (B2).
Drawings
FIG. 1 is a structural arrangement and process flow diagram of the present invention:
wherein: a hydrolytic acidification device (A) which is filled with hydrolytic acidification embedded bioactive filler and is used for hydrolytic acidification; the primary denitrification device (B1) is filled with denitrification embedded bioactive filler for primary denitrification; a short-cut nitrification device (C) filled with short-cut nitrification embedded bioactive filler for short-cut nitrification; anaerobic ammonia oxidation embedding biological active filler is filled in the anaerobic ammonia oxidation device (D) and is used for anaerobic ammonia oxidation; the secondary denitrification device (B2) is filled with denitrification embedded bioactive filler for secondary denitrification; biological phosphorus removal activated sludge is filled in the biological phosphorus removal device (E) and is used for biological phosphorus removal; a sludge precipitation device (F) for precipitating activated sludge; a first external carbon source (G1) for the implementation and control of a secondary denitrification external carbon source; and a second additional carbon source (G2) is used for adding the carbon source required by the biological phosphorus removal.
(1) Raw water, (2) hydrolysis acidification effluent, (3) primary denitrification effluent, (4) partial nitrification effluent, (5) anaerobic ammonia oxidation effluent, (6) secondary denitrification effluent, (7) partial nitrification effluent return pipeline, (8) secondary denitrification effluent return pipeline, (9) biological phosphorus removal unit effluent, (10) system effluent, and (11) phosphorus removal sludge return pipeline.
Detailed Description
The present invention will be further illustrated with reference to the following examples, but the present invention is not limited to the following examples.
The anaerobic ammonia oxidation embedded bioactive filler, the denitrifying bacteria embedded bioactive filler, the ammonia oxidizing bacteria embedded bioactive filler and the hydrolysis acidification embedded bioactive filler relied on by the invention are the prior art, for example, the technologies in ZL201410137209.2, ZL201410137270.7, ZL201410137401.1, CN111470625A and the like or similar technologies are adopted.
Example 1 (temperature of urban Sewage 20-25 ℃ C.)
Aiming at urban sewage treatment, parameters are set based on an independent denitrification coupling technical process of anaerobic ammonia oxidation, and specific devices are connected, as shown in an attached figure 1.
Anaerobic hydrolysis acidification device (a): the filling rate of the biological active filler embedded by the hydrolytic acidification bacteria is 15-20%, and the reaction time HRT: 2-4 h;
primary denitrification device (B1): the filling rate of the biological active filler embedded by the denitrifying bacteria is 15-20%, and the reaction time HRT: 1-2 h;
short-cut nitrification device (C): the filling rate of the nitrosation bacteria embedded bioactive filler is 10-20%, and the reaction time HRT: 2-4 h;
anammox apparatus (D): the packing rate of the anaerobic ammonium oxidation bacteria embedded bioactive filler is 10-20%, and the reaction time HRT: 3-4 h;
secondary denitrification device (B2): the filling rate of the biological active filler embedded by the denitrifying bacteria is 15-20%, and the reaction time HRT: 1-2 h;
biological phosphorus removal (E) (anaerobic + aerobic devices): activated sludge concentration MLSS: 3000-5000mg/L, reaction time HRT: 1-1.5 h;
a sedimentation tank: sludge age: 0.5 d.
Operation regulation and control:
a, subtracting the difficultly biodegradable COD (such as 30-50mg/L of municipal sewage) from the COD value of the hydrolyzed and acidified effluent, and determining the short-cut nitrification reflux water flow rate (7) by using the value and the amount of nitrite nitrogen and nitrate nitrogen in the short-cut nitrification effluent;
b, determining the flow rate (8) of the secondary denitrification return water according to the nitrite nitrogen content of the secondary denitrification outlet water and the total nitrogen content required by the total outlet water; calculating and controlling the proportion of the ammonia nitrogen and the nitrite nitrogen in the short-cut nitrification effluent (namely the oxidation amount of the short-cut nitrification to the ammonia nitrogen) according to the reflux water amount;
c, calculating the amount of a first additional carbon source (G1) before secondary denitrification according to the nitrate nitrogen content of the anaerobic ammonia oxidation effluent (5) (the calculation of the part considers the calculation amount of reducing all nitrate nitrogen into nitrite nitrogen.)
d, determining the adding amount of the second external carbon source (G2) according to the required phosphorus removal amount of the biological phosphorus removal system.
Under the condition of the parameters, aiming at organic matters (chemical oxygen demand), ammonia nitrogen, total nitrogen and total phosphorus of the effluent of urban sewage treatment, the effluent can reach the first grade A of GB 18918 + 2002: 50mg/L, 5(8) mg/L, 15mg/L and 0.5 mg/L. Under a good running state, the effluent can reach the first-grade A standard of DB 11/890-2012 standard of pollutant discharge in urban sewage treatment plants: the organic matter (chemical oxygen demand), ammonia nitrogen, total nitrogen and total phosphorus are respectively less than or equal to 20mg/L, less than or equal to 1mg/L, less than or equal to 10mg/L and less than or equal to 0.2 mg/L.
Example 2 (urban sewage temperature 13-20 ℃ C.)
Aiming at urban sewage treatment, parameters are set based on the denitrification bypass coupling technical process of anaerobic ammonia oxidation, and specific devices are connected, as shown in the attached figure 1.
Anaerobic hydrolysis acidification device (a): the filling rate of the biological active filler embedded by the hydrolytic acidification bacteria is 15-20%, and the reaction time HRT: 2-4 h;
primary denitrification device (B1): the filling rate of the biological active filler embedded by the denitrifying bacteria is 15-20%, and the reaction time HRT: 1-2 h;
short-cut nitrification device (C): the filling rate of the nitrosation bacteria embedded bioactive filler is 10-20%, and the reaction time HRT: 2-4 h;
anammox apparatus (D): the packing rate of the anaerobic ammonium oxidation bacteria embedded bioactive filler is 10-20%, and the reaction time HRT: 3-4 h;
secondary denitrification device (B2): the filling rate of the biological active filler embedded by the denitrifying bacteria is 15-20%, and the reaction time HRT: 1-2 h;
biological phosphorus removal (E) (anaerobic + aerobic devices): activated sludge concentration MLSS: 3000-5000mg/L, reaction time HRT: 1-1.5 h;
a sedimentation tank: sludge age: 0.5 d.
Operation regulation and control:
a, subtracting the difficultly biodegraded COD (such as 30-50mg/L) from the COD value of the hydrolyzed and acidified effluent, and determining the water quantity of the short-cut nitrified effluent (4) returned to the primary denitrification device (B1) through the short-cut nitrifying reflux pipeline (7) according to the value and the quantity of nitrite nitrogen and nitrate nitrogen in the short-cut nitrified effluent;
b, calculating and controlling the proportion of ammonia nitrogen and nitrite nitrogen of the shortcut nitrification effluent (4) according to the biochemical capacity remained in the anaerobic ammonia oxidation device (D) in a low-temperature state (namely determining the oxidation amount of the shortcut nitrification to the ammonia nitrogen, wherein the surplus of the ammonia nitrogen in the shortcut nitrification effluent (4) is the capacity of the anaerobic ammonia oxidation device (D) to remove the ammonia nitrogen);
c, calculating the amount of an external carbon source before secondary denitrification according to the content of nitrate nitrogen and nitrite nitrogen in the anaerobic ammonia oxidation effluent (5) (the part calculates the calculated amount of the carbon source required by completely reducing all nitrite nitrogen and nitrate nitrogen into nitrogen)
d, determining the adding amount of the second external carbon source (G2) according to the required phosphorus removal amount of the biological phosphorus removal system. .
Under the condition of the parameters, aiming at organic matters (chemical oxygen demand), ammonia nitrogen, total nitrogen and total phosphorus of the effluent of urban sewage treatment, the effluent can reach the first grade A of GB 18918 + 2002: 50mg/L, 5(8) mg/L, 15mg/L and 0.5 mg/L. Under a good running state, the effluent can reach the first-grade A standard of DB 11/890-2012 standard of pollutant discharge in urban sewage treatment plants: the organic matter (chemical oxygen demand), ammonia nitrogen, total nitrogen and total phosphorus are respectively 20mg/L, 1mg/L, 10mg/L and 0.2 mg/L.

Claims (4)

1. A denitrification bypass 'coupling' system based on anaerobic ammonia oxidation is characterized in that raw water (1) is connected with a hydrolysis acidification device (A) and used as inlet water of the hydrolysis acidification device (A), wherein the hydrolysis acidification device (A) is filled with hydrolysis acidification embedded bioactive filler and used for hydrolysis acidification, hydrolysis acidification outlet water (2) of the hydrolysis acidification device (A) is connected with a primary denitrification device (B1) and used as inlet water of a primary denitrification device (B1), the primary denitrification device is filled with denitrification embedded bioactive filler and used for primary denitrification, primary denitrification outlet water (3) of the primary denitrification device (B1) is connected with a short-cut nitrification device (C) and used as inlet water of the short-cut nitrification device (C), the short-cut nitrification embedded bioactive filler is filled in the short-cut nitrification device and used for short-cut nitrification, and short-cut nitrification outlet water (4) of the short-cut nitrification device (C) is connected with the anaerobic ammonia oxidation device (D), anaerobic ammonia oxidation embedded biological active filler is filled in the anaerobic ammonia oxidation device and is used for anaerobic ammonia oxidation, anaerobic ammonia oxidation effluent (5) of the anaerobic ammonia oxidation device (D) is connected with a secondary denitrification device (B2), denitrification embedded biological active filler is filled in the secondary denitrification and is used for secondary denitrification, secondary denitrification effluent (6) of the secondary denitrification device (B2) is connected with a biological phosphorus removal device (E), biological phosphorus removal active sludge is filled in the biological phosphorus removal device and is used for biological phosphorus removal, effluent (9) of the biological phosphorus removal device (E) is connected with a sludge settling device (F), and the sludge settling device (F) is used for settling sludge; one part of sludge precipitated in the sludge precipitation device (F) is discharged as excess sludge, and the other part of sludge is returned through a phosphorus removal sludge return pipeline (11) and is combined with secondary denitrification effluent (6) to enter a biological phosphorus removal device (E); a first external carbon source (G1) is connected with the anaerobic ammonia oxidation effluent (5) and is used for supplying the anaerobic ammonia oxidation effluent (5) with the external carbon source; a second external carbon source (G2) is connected with the denitrification effluent (6) and is used for adding the external carbon source of the biological phosphorus removal unit; meanwhile, the secondary denitrification effluent (6) is also provided with a secondary denitrification effluent return pipeline (8) connected with the short-cut nitrification effluent (4); the short-cut nitrified effluent (4) is provided with a short-cut nitrified effluent return pipeline (7) which is connected with the hydrolyzed and acidified effluent (2).
2. The water treatment method by using the system of claim 1 is characterized by comprising the following working conditions:
the first working condition is as follows: the water temperature is 20 ℃ or above, and most of the system depends on the denitrification of the anaerobic ammonia oxidation reaction;
the raw water sequentially passes through a hydrolytic acidification device (A), a primary denitrification device (B1), a short-cut nitrification device (C), an anaerobic ammonia oxidation device (D), a secondary denitrification device (B2), a biological phosphorus removal device (E) and a precipitated sludge device (F) to carry out hydrolytic acidification, primary denitrification, short-cut nitrification (partial short-cut nitrification), anaerobic ammonia oxidation, secondary denitrification and biological phosphorus removal; the working condition mainly depends on anaerobic ammonia oxidation for denitrification, the first-stage denitrification consumes bioavailable organic matters (COD) in raw water through partial backflow of the shortcut nitrification liquid, so that waste of the biochemical COD to organic matter oxidation in the next shortcut nitrification process and influence on the anaerobic ammonia oxidation are reduced, and the influence of nitrate on the anaerobic ammonia oxidation brought by the raw water can be eliminated; part of reaction liquid after the short-cut nitrification enters an anaerobic ammonia oxidation device for denitrification, nitrate formed in the anaerobic ammonia oxidation process can be reduced through secondary denitrification, the proportion of ammonia nitrogen and nitrite nitrogen is strictly controlled in theory by the part of reaction liquid after the short-cut nitrification, the ratio of the ammonia nitrogen to the nitrite nitrogen is 1:1.32, the amount of the nitrite nitrogen returned by the secondary denitrification is considered during the accounting, the secondary denitrification process is considered to be a short-cut denitrification stage, the short-cut denitrification process can realize effective control of the short-cut denitrification through the arrangement of an independent denitrification unit (B2) and the control of the adding amount of a first additional carbon source (G1) and an additional carbon source, and then the short-cut denitrification liquid flows back to the anaerobic ammonia oxidation device through a secondary denitrification water outlet return pipeline (8), so that more thorough denitrification is realized; the secondary denitrification effluent (6) of the secondary denitrification device (B2) is connected with the biological phosphorus removal device (E) for biological phosphorus removal, and secondary carbon source feeding is carried out through a second external carbon source (G2) according to the phosphorus content of the secondary denitrification effluent (6); the biological phosphorus removal effluent (9) of the mixed liquid containing sludge of the biological phosphorus removal device (E) is connected with a sludge precipitation device (F), and the sludge precipitation device (F) is used for precipitating sludge; one part of sludge precipitated in the sludge precipitation device (F) is discharged, and the other part of sludge flows back to the secondary denitrification effluent (6) through a phosphorus removal sludge return pipeline (11) and enters the biological phosphorus removal device (E), so that the circulation of phosphorus removal activated sludge is realized;
the second working condition is as follows: the water temperature is lower than 20 ℃, part of the system is denitrified by anaerobic ammoxidation, and the system is mainly denitrified by partial nitrification and denitrification;
raw water sequentially passes through a hydrolysis acidification device (A), a primary denitrification device (B1), a short-cut nitrification device (C), an anaerobic ammonia oxidation device (D), a secondary denitrification device (B2), a biological phosphorus removal device (E) and a precipitated sludge device (F) to be subjected to hydrolysis acidification, primary denitrification, short-cut nitrification, anaerobic ammonia oxidation, secondary denitrification and biological phosphorus removal; meanwhile, part of the short-cut nitrification effluent (4) is connected with a first-stage denitrification device (B1), namely hydrolysis acidification effluent (2), through a short-cut nitrification return pipeline (7); although anaerobic ammonia oxidation and denitrification are biochemical reactions, the adaptability of the two reactions to low temperature is greatly different;
the working condition mainly depends on short-cut nitrification, primary denitrification and secondary denitrification for denitrification, the primary denitrification utilizes bioavailable organic matters (COD) in raw water through partial reflux (7) of short-cut nitrification liquid so as to reduce waste of the biochemical COD to oxidize the organic matters in the short-cut nitrification process; according to the process state, for short-cut nitrification, reaction liquid after most of ammonia nitrogen is oxidized, namely the corresponding residual part of the short-cut nitrification effluent (4), firstly enters an anaerobic ammonia oxidation device (D) for partial denitrification, the partial denitrification means that nitrogen quantity which can be removed by using the biochemical denitrification capability remained by ANAMMOX under the condition of low temperature is utilized, all the anaerobic ammonia oxidation effluent (5) enters a secondary denitrification device (B2) for denitrification, and the anaerobic ammonia oxidation effluent (5) in the state contains most of nitrite remained after the anaerobic ammonia oxidation device (D) reacts and a small amount of nitrate generated by the anaerobic ammonia oxidation reaction; the secondary denitrification process requires a first external carbon source (G1); the effluent (6) of the secondary denitrification device (B2) is connected with a biological phosphorus removal device (E) for biological phosphorus removal; the second-stage denitrification device (B2) reduces all nitrite nitrogen and nitrate nitrogen into nitrogen for removal, and does not consider the use of the second-stage denitrification return pipe (8) for return flow under the working condition; simultaneously, a second additional carbon source (G2) is used for adding the carbon source required by phosphorus removal; the effluent (9) of the biological phosphorus removal unit of the biological phosphorus removal device (E) is connected with a sludge precipitation device (F), and the sludge precipitation device (F) is used for precipitating sludge; and a part of sludge precipitated in the sludge precipitation device (F) is discharged, and a part of sludge flows back to the secondary denitrification effluent (6) through a phosphorus removal sludge return pipeline (11) to enter the biological phosphorus removal device (E), so that the circulation of phosphorus removal activated sludge is realized.
3. The water treatment method as recited in claim 2, characterized in that the second operating condition requires a relatively greater dependence of the first external carbon source (G1) on the system denitrification than the first operating condition; however, the operation under the second working condition can be realized at relatively low temperature, so that the whole system can adapt to stable denitrification in a low-temperature state, and the defect of low-temperature inadaptation caused by purely relying on anaerobic ammonia oxidation denitrification is compensated.
4. The method for treating three main types of pollutants (C, N, P) in sewage and wastewater by using the system of claim 1 according to the sequence of the flow: the method is characterized by comprising the following steps:
firstly, the method comprises the following steps: establishing an anaerobic hydrolysis acidification reaction process by using a hydrolysis acidification device (A), hydrolyzing macromolecular organic matters in raw water to decompose long-chain and macromolecular substances into micromolecular organic matters, and releasing organic nitrogen as much as possible in the process to provide better ammonia nitrogen oxidation conditions and micromolecular organic matter electron acceptors as much as possible for ammonia nitrogen oxidation and removal in the subsequent process;
secondly, the method comprises the following steps: establishing a primary denitrification reaction process by utilizing a primary denitrification device (B1); the main function of the reaction process is to utilize nitrite nitrogen and nitrate nitrogen returned from the short-cut nitrification biological process reflux (7) of the next stage, combine with hydrolysis acidification effluent (COD), carry out denitrification in the stage, and mainly aim to consume or utilize organic matters which can be utilized by organisms in anaerobic hydrolysis acidification effluent, thereby ensuring that the subsequent biological process is influenced by the organic matters (COD) as little as possible or not, and further creating good reaction conditions for anaerobic ammonia oxidation;
thirdly, the method comprises the following steps: establishing an aerobic short-cut nitrification reaction process by using a short-cut nitrification device (C); the part is subjected to a nitrification biochemical process of oxidizing ammonia nitrogen into nitrite nitrogen; aiming at the next anaerobic ammonia oxidation, partial nitrosation of ammonia nitrogen is carried out by partial nitrification according to the requirements of the subsequent process;
fourthly: establishing an anaerobic ammonia oxidation reaction process by using an anaerobic ammonia oxidation device (D); the part utilizes ammonia nitrogen and nitrite nitrogen in the effluent (4) of the short-cut nitrification process to carry out ammonia nitrogen oxidation and nitrite nitrogen reduction processes, and nitrogen is generated to realize denitrification; in the process, the anaerobic ammonia oxidation requires the proportion of ammonia nitrogen and nitrite nitrogen of inlet water, namely outlet water (4) in the short-cut nitrification process (the proportion of the outlet water is required to be 1:1.32 under the first working condition, the second low-temperature working condition is adjusted according to the biochemical capacity of subsequent anaerobic ammonia oxidation), nitrate nitrogen with the proportion of 0.26mol is generated when 1mol of ammonia nitrogen is oxidized in the reaction, and the part of nitrate nitrogen cannot be removed by utilizing the simple anaerobic ammonia oxidation process, so that a secondary denitrification biological process is established;
fifth, the method comprises the following steps: establishing a secondary denitrification reaction process by utilizing a secondary denitrification device (B2); in the secondary denitrification process, the core main body of the biochemical reaction is denitrifying bacteria in the denitrifying embedded filler, the reaction substrate is nitrate generated in the anaerobic ammonia oxidation and denitrification process in the upper anaerobic ammonia oxidation device (D), and biochemical organic matters in water are almost completely utilized in the secondary denitrification stage after the reaction processes of the anaerobic ammonia oxidation device (D) are performed, so that the partial denitrification needs a first external carbon source (G1); the biological process of the secondary denitrification can realize two denitrification controls, and further calculate the amount of a first additional carbon source (G1) before the secondary denitrification by selecting different denitrification controls: firstly, the nitrate of the anaerobic ammonia oxidation effluent (5) at the section is completely denitrified, so that relatively more organic matters need to be added; the other control is that the part of nitrate nitrogen only completes the short-range denitrification, and then the effluent flows back to the anaerobic ammonia oxidation reaction process section through a secondary denitrification effluent return pipeline (8) to enable the generated part of nitrite to participate in the anaerobic ammonia oxidation denitrification process, so that part of carbon source required to be added can be saved relatively;
sixth: the independent biological phosphorus removal unit is built by activated sludge in the biological phosphorus removal device (E), and further comprises a subsequent sludge precipitation device (F) which consists of an anoxic part, an aerobic part and a precipitation part; the part can be constructed by phosphorus accumulating bacteria or phosphorus accumulating bacteria and denitrifying phosphorus removal bacteria, and has a stable biological phosphorus removal function. Because the biological phosphorus removal system after nitrogen removal is completed, deep phosphorus removal can be realized. The part needs to be added with a second external carbon source (G2) in the water inlet of the biological phosphorus removal unit. After the whole sewage and wastewater is subjected to the five denitrification processes, the total nitrogen of the effluent can be effectively controlled.
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