CN113072184B - Anaerobic ammonia oxidation-based independent denitrification 'coupling' system and water treatment method - Google Patents
Anaerobic ammonia oxidation-based independent denitrification 'coupling' system and water treatment method Download PDFInfo
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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
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.
The background art comprises the following steps:
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, waste 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, particularly the 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 causes high efficiency of ANAMMOX biochemical process to be difficult to exert, and forms low efficiency (much at 0.5 Kg/m) of the whole ANAMMOX denitrification system 3 D or so).
(3) The third point is also the most critical, in the ANAMMOX denitrification system, the ratio of ammonia nitrogen to nitrite nitrogen entering the ANAMMOX reaction process (1. 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 the ANAMMOX granular sludge or system. The formed idea is as follows: denitrifying bacteria mixed in anaerobic ammonium oxidation granular flora are utilized to remove the part of nitrogen by utilizing a denitrifying reaction, the denitrifying process can consider that nitrate nitrogen is converted into nitrogen to be removed through the whole denitrifying process, and can also consider that the nitrate nitrogen is reduced into nitrite nitrogen by utilizing the denitrifying process, so that the part of nitrogen participates in the ANAMMOX reaction, and the optimal proportion (such as a short-range denitrifying technology) required by the ANAMMOX reaction is met by reducing the formation proportion of the ammonia nitrogen and the nitrite nitrogen in the process of oxidizing the ammonia nitrogen into the nitrite nitrogen (1.0-1.2). 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 ANAMMOX granule flora is difficult to accurately control under the existing process conditions, and is often influenced by unstable system influent organic matters (COD) and COD released by bacteria death in the ANAMMOX system (under the condition that a large amount of COD exists, denitrifying bacteria easily reduce nitrite nitrogen in the ANAMMOX system to form nitrogen, and conversely, denitrifying bacteria hardly reduce and remove nitrate nitrogen under the condition that 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), especially in practical engineering applications.
(4) Furthermore, the optimum reaction temperature of AAOB bacteria is about 34 ℃, and after domestication and adaptation to low temperature such as screening of Candida Brocadia fulgida, the conventional ANAMMOX system can be adapted to about 20 ℃ with high efficiency, but the fact that the water temperature is objectively lower than 20 ℃ due to seasonal variation in 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 raw water COD is reduced to enter an ANAMMOX reaction process;
(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 DNB reaction strength is controlled 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 figure 1.
An independent denitrification '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 the primary denitrification device (B1), denitrification embedded bioactive filler is filled in the primary denitrification device 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), short-cut nitrification embedded bioactive filler is filled in the short-cut nitrification device and used for short-cut nitrification, denitrification outlet water (4) of the short-cut nitrification device (C) is connected with an anaerobic ammonia oxidation device (D), anaerobic ammonia oxidation device is filled with biological bioactive filler and used for anaerobic embedding phosphorus removal, anaerobic ammonia oxidation and anaerobic phosphorus removal, anaerobic ammonia oxidation device (D) is connected with secondary denitrification embedded bioactive filler (B) and used for secondary denitrification device (B) and secondary denitrification device (C), and secondary denitrification device (B) is connected with secondary denitrification active denitrification filler (6), the effluent (9) 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 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); the first additional carbon source (G1) is connected with the anaerobic ammonia oxidation effluent (5) and is used for adding a carbon source to the anaerobic ammonia oxidation effluent (5); a second external carbon source (G2) is connected with the secondary denitrification effluent (6) and is used for adding an 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 shortcut 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 short-cut nitrification effluent return pipeline (7) and the secondary denitrification return pipeline (8) with the independent biological phosphorus removal system composed of the subsequent biological phosphorus removal device (E) and the sedimentation 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 first-stage denitrification device (B1), a short-cut nitrification device (C), an anaerobic ammonia oxidation device (D), a second-stage denitrification device (B2), a biological phosphorus removal device (E) and a precipitated sludge device (F) to be subjected to hydrolytic acidification, first-stage denitrification, short-cut nitrification (partial short-cut nitrification), anaerobic ammonia oxidation, second-stage 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 1.32 theoretically, the amount of nitrite nitrogen returned by secondary denitrification backflow is considered during accounting) 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 can realize effective control of short-cut denitrification through the control of the adding amount of a first external carbon source (G1) and an independent denitrification unit (B2)), and then the reaction liquid flows back to the anaerobic ammonia oxidation device through a secondary denitrification effluent 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 addition is carried out through a second additional 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 hydrolytic acidification device (A), a first-stage denitrification device (B1), a short-cut nitrification device (C), an anaerobic ammonia oxidation device (D), a second-stage denitrification device (B2), a biological phosphorus removal device (E) and a precipitated sludge device (F) to be subjected to hydrolytic acidification, first-stage denitrification, short-cut nitrification, anaerobic ammonia oxidation, second-stage denitrification and biological phosphorus removal; meanwhile, part of the short-cut nitrification effluent (4) is connected with the water inlet, namely hydrolysis acidification effluent (2) of the primary denitrification device (B1) 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; the process state requires that most of ammonia nitrogen is oxidized (partial ammonia nitrogen oxidation amount properly retains partial ammonia nitrogen according to biochemical capacity of anaerobic ammonia oxidation remained at low temperature) for partial denitrification (namely, partial denitrification refers to nitrogen amount capable of being removed by using biochemical denitrification capacity remained by ANAMMOX under low temperature condition) in the reaction liquid of partial ammonia oxidation (4) is correspondingly the residual part of partial nitrification effluent, anaerobic ammonia oxidation effluent (5) (the effluent of (5) in the state contains most of nitrite remained after ANAMMOX (D) reaction and a small amount of nitrate generated by ANAMMOX (D) reaction) completely enters a secondary denitrification device (B2) for denitrification, and the secondary denitrification process needs a first additional 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 implemented to completely reduce all nitrite nitrogen and nitrate nitrogen into nitrogen for removal, and the secondary denitrification return pipe (8) is not used for returning under the working condition. And simultaneously, a second additional carbon source (G2) is utilized to carry out the addition of 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.
The condition requires relatively more first external carbon source (G1) dependence for denitrification compared with the first condition system. 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 and P) in sewage and wastewater by adopting the device according to the flow sequence comprises the following steps:
firstly: 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 using 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 at the stage, and mainly aim at utilizing anaerobic hydrolysis acidification organic matters which can be utilized by organisms in the 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 (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 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 1.32 in 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 denitrifying embedded filler, the reaction substrate is nitrate generated in the anaerobic ammonia oxidation and denitrification process in the upper-stage anaerobic ammonia oxidation device (D), and biochemical organic matters in water are almost completely utilized in the secondary denitrification stage after the nitrate passes through each reaction process of the preorder anaerobic ammonia oxidation device (D), so that the denitrification of the part needs a first additional carbon source (G1); the biological process of the secondary denitrification can realize two kinds of denitrification control, 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 short-range denitrification, and then effluent flows back to the anaerobic ammonia oxidation reaction process section through a secondary denitrification effluent return pipeline (8) so that the generated part of nitrite participates in the anaerobic ammonia oxidation denitrification process, thus the required added carbon source can be saved;
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 wider application of the anaerobic ammonia oxidation technology;
2. through the coupling design of the pure ANAMMOX (D) and the 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 (8) and the control of the adding amount of the first external carbon source (G1), so that the denitrification degree is controllable (the point is completely superior to 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 that the embedded bioactive filler is used for establishing a pure ANAMMOX (D) and a pure secondary denitrification device (B2);
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 deep denitrification;
4. the independent first additional carbon source (G1) and the second additional carbon source (G2) are separately arranged, so that the effective control of the denitrification degree of the secondary denitrification (B2) can be realized.
Drawings
FIG. 1 is a structural device 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 first-stage denitrification device (B1) is filled with denitrification embedding bioactive filler for first-stage 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 embedding 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 implementing and controlling the secondary denitrification external carbon source; and the second additional carbon source (G2) is used for adding a carbon source required by biological phosphorus removal.
The method comprises the following steps of (1) raw water, (2) hydrolysis acidification effluent, (3) primary denitrification effluent, (4) short-cut nitrification effluent, (5) anaerobic ammonia oxidation effluent, (6) secondary denitrification effluent, (7) short-cut 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 by the invention belong to 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 municipal wastewater 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 hydrolytic acidification bacteria embedded bioactive filler is 15-20%, and the reaction time HRT:2-4h;
first-order denitrification device (B1): the filling rate of the biological active filler embedded by the denitrifying bacteria is 15-20%, and the reaction time HRT:1-2h;
short-cut nitrification device (C): the filling rate of the nitrosation bacteria embedded bioactive filler is 10-20%, and the reaction time HRT:2-4h;
anammox apparatus (D): the packing rate of the anaerobic ammonium oxidation bacteria embedded bioactive filler is 10-20%, and the reaction time HRT:3-4h;
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:1-2h;
biological phosphorus removal (E) (anaerobic + aerobic device): activated sludge concentration MLSS:3000-5000mg/L, reaction time HRT:1-1.5h;
a sedimentation tank: sludge age: 0.5d.
Operation regulation and control:
a, subtracting the biological degradation-resistant 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 backflow water quantity by using the value and the quantity of nitrite nitrogen and nitrate nitrogen in the short-cut nitrification effluent (7);
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 ammonia nitrogen and 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 the 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 additional 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-class A of pollutant discharge standard GB 18918-2002 of urban sewage treatment plant: 50mg/L, 5 (8) mg/L, 15mg/L and 0.5 mg/L. Under a good running state, the effluent can reach the first-class A standard DB 11/890-2012 standard of discharge of pollutants from municipal wastewater 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 0.2mg/L.
Example 2 (temperature of municipal wastewater: 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 hydrolytic acidification bacteria embedded bioactive filler is 15-20%, and the reaction time HRT:2-4h;
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:1-2h;
short-cut nitrification device (C): the filling rate of the nitrosation bacteria embedded bioactive filler is 10-20%, and the reaction time HRT:2-4h;
anammox apparatus (D): the packing rate of the anaerobic ammonium oxidation bacteria embedded bioactive filler is 10-20%, and the reaction time HRT:3-4h;
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:1-2h;
biological phosphorus removal (E) (anaerobic + aerobic devices): activated sludge concentration MLSS:3000-5000mg/L, reaction time HRT:1-1.5h;
a sedimentation tank: sludge age: 0.5d.
Operation regulation and control:
a, subtracting the difficultly biodegraded COD (such as 30-50 mg/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) by using 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) (namely determining the oxidation amount of the shortcut nitrification to the ammonia nitrogen according to the biochemical capacity of the anaerobic ammonia oxidation device (D) which is remained in a low-temperature state) (at the moment, the surplus of the ammonia nitrogen in the shortcut nitrification effluent (4) is the capacity of the anaerobic ammonia oxidation device (D) for removing 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 additional 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-class A of pollutant discharge standard GB 18918-2002 of urban sewage treatment plant: 50mg/L, 5 (8) mg/L, 15mg/L and 0.5 mg/L. Under a good running state, the effluent can reach the first-class A standard DB 11/890-2012 standard of discharge of pollutants from municipal wastewater treatment plants: the organic matter (chemical oxygen demand), ammonia nitrogen, total nitrogen and total phosphorus are respectively 20mg/L, 1mg/L, 10mg/L and 0.2mg/L.
Claims (4)
1. An independent denitrification '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 the primary denitrification device (B1), denitrification embedded bioactive filler is filled in the primary denitrification device 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), short-cut nitrification embedded bioactive filler is filled in the short-cut nitrification device and used for short-cut nitrification, denitrification outlet water (4) of the short-cut nitrification device (C) is connected with an anaerobic ammonia oxidation device (D), anaerobic ammonia oxidation device is filled with biological bioactive filler and used for anaerobic embedding phosphorus removal, anaerobic ammonia oxidation and anaerobic phosphorus removal, anaerobic ammonia oxidation device (D) is connected with secondary denitrification embedded bioactive filler (B) and used for secondary denitrification device (B), secondary denitrification active denitrification filler (6) and secondary denitrification device (B) is connected with secondary denitrification active denitrification device and used for secondary denitrification device (B) and denitrification device, the effluent (9) 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 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); the 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 external carbon sources; a second external carbon source (G2) is connected with the secondary denitrification effluent (6) and is used for adding an 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 shortcut 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 operating mode is as follows: the water temperature is 20 ℃ or above, and most of the system depends on the denitrification of anaerobic ammonia oxidation reaction;
the 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 sludge precipitation device (F) to carry out hydrolysis acidification, primary denitrification, 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 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 to be 1.32 theoretically in the part of reaction liquid after short-cut nitrification, the amount of nitrite nitrogen returned by the return flow of the secondary denitrification is considered during 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 a secondary denitrification device (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) to realize more thorough denitrification; 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 adding 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 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 reflows to secondary denitrification effluent (6) through a phosphorus removal sludge reflow pipeline (11) and enters a 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 sludge precipitation 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 outlet water (4) is connected with the primary denitrification device (B1) inlet water, namely hydrolysis acidification outlet water (2) through a short-cut nitrification outlet water 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, primary denitrification and secondary denitrification for denitrification, the primary denitrification utilizes bioavailable organic matters (COD) in raw water through a short-range nitrification water outlet return pipeline (7) so as to reduce waste of the biochemical COD on oxidation of the organic matters in the short-range 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 the nitrogen quantity which can be removed by utilizing 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 additional carbon source (G1); the secondary denitrification effluent (6) is connected with a biological phosphorus removal device (E) to carry out 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 condition that the second-stage denitrification effluent return pipeline (8) is used for backflow; simultaneously, a second additional carbon source (G2) is utilized to carry out carbon source addition required by phosphorus removal; the effluent (9) 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. A water treatment method according to 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 major pollutants C, N and P in sewage and wastewater by adopting the system of claim 1 according to the sequence of the process 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 using a primary denitrification device (B1); the main function of the reaction process is to utilize nitrite nitrogen and nitrate nitrogen returned by a short-cut nitrification effluent return pipeline (7) in the next stage, combine with hydrolysis acidification effluent to 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 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 according to the subsequent process requirement by partial nitrification;
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 short-cut nitrification effluent (4) 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 shortcut nitrification outlet water (4), nitrate nitrogen with the proportion of 0.26mol is generated when 1mol of ammonia nitrogen is oxidized in the reaction, and the nitrate nitrogen cannot be removed by utilizing a simple anaerobic ammonia oxidation process, so that a secondary denitrification biological process is established;
fifth: establishing a secondary denitrification reaction process by utilizing a secondary denitrification device (B2); in the secondary denitrification process, the core main body of biochemical reaction is denitrifying bacteria in denitrifying embedded filler, the reaction substrate is nitrate produced 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 kinds of denitrification control, 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, has a stable biological phosphorus removal function, can realize deep phosphorus removal due to the biological phosphorus removal system after nitrogen removal, needs to add a second external carbon source (G2) to the water inlet of the biological phosphorus removal unit, and can effectively control the total nitrogen of the effluent after the whole sewage and wastewater passes through the five nitrogen removal processes.
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