CN109354174B - CANON _ MBBR-based rapid starting method of enhanced denitrification system - Google Patents

CANON _ MBBR-based rapid starting method of enhanced denitrification system Download PDF

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CN109354174B
CN109354174B CN201811477780.3A CN201811477780A CN109354174B CN 109354174 B CN109354174 B CN 109354174B CN 201811477780 A CN201811477780 A CN 201811477780A CN 109354174 B CN109354174 B CN 109354174B
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CN109354174A (en
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吴迪
周家中
韩文杰
管勇杰
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Qingdao Spring Water Processing Co ltd
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1205—Particular type of activated sludge processes
    • C02F3/121—Multistep treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
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    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

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Abstract

The invention discloses a CANON _ MBBR-based rapid starting method of an enhanced denitrification system, and belongs to the technical field of biological denitrification. The method solves the technical problems that related systems in the prior art are large in inoculation amount, slow in starting, greatly influenced by C/N and the like. The invention divides the conventional reaction tank body into five reaction chambers through partition plates, and the reaction chambers are provided with a stirring device, an aeration device, a flow guide device, a water collecting device and a reflux device, and each reaction chamber is added with a suspension carrier. The invention combines denitrification and completely autotrophic nitrogen removal, the denitrification tank is arranged in front, the completely autotrophic nitrogen removal effluent flows back, the removal of nitrate and organic matters is realized in the first stage, and the completely autotrophic nitrogen removal is performed in the second stage. The invention can realize three operation modes, namely a parallel operation mode, a double-series A operation mode and a double-series B operation mode. The invention has the advantages of small inoculation ratio, quick start, high denitrification load, good tolerance to influent organic matters and the like.

Description

CANON _ MBBR-based rapid starting method of enhanced denitrification system
Technical Field
The invention belongs to the technical field of biological denitrification, and particularly relates to a rapid starting method of a CANON-MBBR based enhanced denitrification system.
Background
The CANON process (complete Autotrophic Nitrogen Removal process), which is a novel biological Nitrogen Removal process, is a nitrosation and anaerobic ammonia oxidation process realized by controlling dissolved oxygen in a single reactor or a biomembrane, so as to achieve the purpose of Nitrogen Removal. Under aerobic conditions, ammonia oxidizing bacteria oxidize ammonia nitrogen into nitrous acid, and the generated nitrous acid and part of the rest ammonia nitrogen are subjected to ANAMMOX reaction to generate nitrogen.
The existence of a certain concentration of organic carbon source can inhibit the growth of anammox bacteria, and the main reason is that the growth speed of denitrifying bacteria is far faster than that of anammox bacteria, and the proliferation of denitrifying bacteria has stronger competition on nitrite than anammox bacteria, so that the anammox bacteria are inhibited due to the lack of substrates. Provides a new idea for biological denitrification of wastewater, and is highly favored by researchers in the field of wastewater denitrification with high efficiency and energy conservation. However, with the further improvement of the effluent total nitrogen discharge standard, the treatment of the nitrogen-containing wastewater by the two processes cannot meet the requirement, and the effluent still has higher concentration of total nitrogen. The collision and shearing action of the filler in water enables air bubbles to be finer and more uniform, and the utilization rate of oxygen is improved.
An aerobic zone and an anaerobic zone exist in the MBBR simultaneously, and favorable conditions are created for the co-existence of aerobic bacteria and anaerobic bacteria. The filler and water are in a completely mixed state, and the biological film attached to the filler can be fully contacted with pollutants and air in the water, so that the degradation efficiency of the pollutants is improved.
As can be seen from the anaerobic ammonia oxidation sewage treatment plants which are successfully operated, the long starting time of the project (more than 6 months for most of the projects), the shortage of seed sources and the high requirement on the quality of inlet water (high temperature and low carbon) are the main bottlenecks which limit the industrial application of the anaerobic ammonia oxidation technology for a long time.
The prior art has related research reports that:
zhang Fangzhai, Wang Shuying, Pengyun and the like, a start experiment of CANON process for treating actual late-stage landfill leachate (chemical science report, 2016, 67(9):3910-3And d. The starting method has large dosage in the early stage of manual water distribution and starting engineeringOnly one item of medicine of a large-volume reactor has large investment and is not suitable for engineering popularization;
CN 106673205A discloses a rapid starting method of an integrated autotrophic nitrogen removal system, which adopts a sequencing batch SBR reactor, inoculates shortcut nitrification sludge and anaerobic ammonia oxidation sludge according to the mass ratio of 1: 3-1: 1, adopts an intermittent aeration operation mode, and has the total nitrogen removal load of the reactor of 0.3 kgN/(m) in the first inoculation step3D) total nitrogen removal duty of the reactor of up to 0.63 kgN/(m) in 30 days3D); but also, the inoculation ratio of the method is large and reaches 50-75%, and the method adopts intermittent operation, so that the quantity in engineering application is large, and the method has no significance in large-scale starting.
Li Huibo et al (China Water supply and drainage, 2014,30(5):1-5.) start the CANON process to treat anaerobic sludge digestion liquid. 3% total area of seeded packing Start-Up 50m3After 120 days of operation, the nitrogen removal volume load in the stationary phase is 0.7-1.1 kg/m3And d. The concentration of the ammonia nitrogen in the effluent water is usually lower than 150mg/L, the higher effluent water requirement is difficult to achieve, the ratio of the ammonia nitrogen removed by the method to the generated nitrate nitrogen is 8-15 percent and is higher than the theoretical value of 11 percent, namely a certain amount of NOB exists in the system, the growth speed of the NOB is higher than that of AOB, the hidden danger that the value of the NOB is increased too fast exists in long-term operation, the risk that a biomembrane is blocked by too thick fillers easily occurs in the later operation without arranging a stirring device in the method, and the denitrification effect is influenced;
CN 108191061A discloses a coking wastewater anaerobic ammonia oxidation biochemical treatment method, which comprises a pre-anoxic zone, an MBBR pre-aerobic zone, a pre-anoxic zone, an MBBR nitrosation aerobic zone, an MBBR anaerobic ammonia oxidation zone, an MBBR post-aerobic zone, a sludge post-anoxic zone, a post-sludge aerobic zone and a advection sedimentation zone; partial ammonia nitrogen in the wastewater is subjected to nitration reaction in an MBBR front aerobic zone, partial nitrate generated is subjected to denitrification removal in a pre-anoxic zone and a front anoxic zone, partial ammonia nitrogen is removed in an MBBR nitrosation zone and an MBBR anaerobic ammonia oxidation zone, and residual ammonia nitrogen is subjected to nitration reaction in an MBBR rear aerobic zone. The invention combines preposition, anaerobic ammonia oxidation and postposition denitrification to ensure that the total nitrogen of the discharged water after the coking wastewater treatment reaches the standard. However, the method has long process flow and poor interception of the anammox sludge, the subsequent addition of the organic carbon source increases the treatment cost, and the symbiosis of various strains is not beneficial to the growth of the anammox bacteria.
CN 106630143A discloses an integrated reactor for denitrification of preposed denitrification autotrophic organisms, in the method, denitrifying bacteria, nitrosobacteria and anaerobic ammonium oxidation bacteria are distinguished in a single reactor, so that the semi-denitrification, the nitrosobacteria and the anaerobic ammonium oxidation are carried out in the same device, the method has poor sludge retention capacity, and ammonia nitrogen is required to be partially oxidized into nitrite in the nitrosation process, so that the control is difficult.
In summary, although some progress has been made in the related art on the study of related devices and processes, it is undeniable that there are many drawbacks. The common characteristics of the existing research, namely, the adoption of a larger inoculation ratio or a water distribution mode, the realization of the method in engineering is impossible or expensive, the process flow is long, the starting period is long, the requirement on the quality of inlet water is high, the reliability of the method is low, and the intermittent flow mode is mostly adopted, so that the continuous flow quick starting cannot be realized.
Disclosure of Invention
In order to solve the technical defects in the prior art, the invention provides a rapid starting method of a CANON _ MBBR-based enhanced denitrification system, which combines denitrification and completely autotrophic denitrification, wherein a denitrification tank is arranged in front, the completely autotrophic denitrification effluent flows back, and the effluent direction of a reaction chamber is controlled by a flow guide device to realize the serial, parallel or independent operation of the reaction chambers; the whole autotrophic nitrogen removal process is quickly started by means of inoculation, feeding and the like; different process arrangement forms are realized according to the processing standard requirements. The invention has the advantages of small inoculation ratio, quick start, good tolerance to water inlet organic matters and the like.
In order to achieve the above purpose, the technical problem to be overcome is as follows:
how to reduce the inoculation ratio under the condition of limited seed sources, and through means of feeding, the fast start of the autotrophic nitrogen removal system is realized by controlling aeration, stirring, different process arrangement forms and the like, the tolerance of the system to influent organic matters is enhanced, and higher TN and organic matter removal load are achieved; how to control the opening of a diversion valve, a water inlet valve and the like and realize different process arrangement forms, thereby achieving different treatment standards and realizing the long-term stable operation of the system.
In order to solve the technical problems, the invention adopts the following technical scheme:
a CANON _ MBBR-based rapid starting method of an enhanced nitrogen removal system comprises a reaction tank main body, a stirring device, an aeration device, a flow guide device, a water collecting device and a reflux device, wherein the interior of the reaction tank main body is divided into two rows of four reaction chambers and one reaction chamber positioned in the center of the four reaction chambers through partition plates, namely a first reaction chamber, a second reaction chamber, a third reaction chamber, a fourth reaction chamber and a fifth reaction chamber, wherein the first reaction chamber and the fourth reaction chamber are arranged in a row and positioned at the bottom, the first reaction chamber and the second reaction chamber are arranged in a row, and the fifth reaction chamber is positioned at the center of diagonal connecting lines of the two rows of four reaction chambers;
a first water outlet screen, a second water outlet screen, a third water outlet screen and a fourth water outlet screen are respectively arranged at the diagonal positions of the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber, the first water outlet screen, the second water outlet screen, the third water outlet screen and the fourth water outlet screen are obliquely arranged and form a relatively closed area, and the fifth reaction chamber is positioned in the relatively closed area;
a water inlet pipe is arranged in the middle of the right side of the fifth reaction chamber, sewage to be treated enters the fifth reaction chamber through the water inlet pipe, and a ninth water outlet screen is arranged at the upper part of the fifth reaction chamber; sewage to be treated enters the two rows of four reaction chambers through the ninth water outlet screen, the first water outlet screen, the second water outlet screen, the third water outlet screen and the fourth water outlet screen;
the water collecting device comprises a first water collecting well, a second water collecting well, a first water outlet pipe and a second water outlet pipe which are respectively connected with the first water collecting well and the second water collecting well;
a fifth water outlet screen and a sixth water outlet screen are further arranged below the adjacent sides of the first reaction chamber and the fourth reaction chamber, the first water collecting well is arranged in an area formed by the fifth water outlet screen and the sixth water outlet screen, and the first water collecting well is used for collecting sewage in the reaction tank and then discharging the sewage through the first water outlet pipe;
a seventh water outlet screen and an eighth water outlet screen are further arranged above the adjacent side of the second reaction chamber and the third reaction chamber, and a second water collecting well is arranged in an area formed by the seventh water outlet screen and the eighth water outlet screen and used for collecting sewage in the reaction tank and then discharging the sewage through a second water outlet pipe;
the flow guide device is used for controlling the flow direction of water in the reaction chamber and adjusting the flow direction according to a required operation mode;
suspension carriers are added into each reaction chamber, a stirring device is arranged in each reaction chamber, and the stirring direction is adjusted according to a required operation mode;
the aeration devices are distributed in the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber;
the starting method sequentially comprises the following steps:
a. starting preparation, namely adding a suspension carrier into each reaction chamber, wherein the filling rate is 20-67%; inoculating common activated sludge, wherein the sludge concentration in each reaction chamber is 3-5 g/L;
b. nitrosation and denitrification are started, a parallel operation mode is adopted, and the specific operation mode is as follows: the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber are in parallel relation, sewage to be treated continuously enters the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber through the fifth reaction chamber, effluent is enabled to be collected to the first water collecting well and the second water collecting well by controlling related valves, part of effluent of the water collecting well flows back to the fifth reaction chamber, and the rest of effluent passes through the first water outlet pipe and the second water outlet pipeDischarging through a water outlet pipe; controlling DO of the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber to be 3-6mg/L by the aeration device, and controlling the aeration intensity>5m3/(m2H), controlling the stirring speed of the fifth reaction chamber to be 30-50r/min, controlling the reflux ratio of the water collecting well to be 50-100%, and naturally losing the sludge without refluxing until the concentration of the sludge in the reaction chamber<Ammonia oxidation rate of 1.0g/L in the first, second, third and fourth reaction chambers>50% ammoxidation surface load>1.5gN/(m2D) BOD removal rate of the fifth reaction chamber>50%, entering the next step;
c. CANON pre-starts, adopts two series A running modes, and concrete running mode is: the sewage to be treated continuously enters the first reaction chamber and the fourth reaction chamber through the fifth reaction chamber, water in the first reaction chamber enters the second reaction chamber by controlling a relevant valve, water in the fourth reaction chamber enters the third reaction chamber and finally is collected into the second water collecting well, part of effluent of the water collecting well flows back to the fifth reaction chamber, and the rest of effluent is discharged through the second water outlet pipe; the rotation speed of the stirring devices in the first reaction chamber and the second reaction chamber is 30-45r/min, the DO of the first reaction chamber and the second reaction chamber is controlled to be 1-2mg/L, and the aeration intensity is controlled>3m3/(m2H), controlling DO in the fourth reaction chamber and the third reaction chamber to be 3-6mg/L and controlling aeration intensity>5m3/(m2H) total ammonia oxidation rate of the fourth and third reaction chambers>50 percent; the fifth reaction chamber controls the stirring speed to be 30-50r/min and the reflux ratio of the water collecting well to be 50-100 percent until the total ammonia oxidation rate of the first reaction chamber and the second reaction chamber>50% ammonia oxidation surface load of the first reaction chamber>1.0gN/(m2D) BOD removal rate of the fifth reaction chamber>60% of the solution enters the next step;
d. CANON inoculation is started, the double-series A operation mode is adopted, CANON suspension carriers are inoculated into the first reaction chamber, the inoculation rate is 3-5%, DO is controlled to be 0.5-1.5mg/L, and the aeration intensity>2m3/(m2H), controlling the rotating speed of the stirring device to be 15-30 r/min; the second reaction chamber controls DO to be 1-2mg/L, and aeration is strongDegree of rotation>3m3/(m2H), the rotating speed of the stirring device is 15-30r/min, and the total ammonia oxidation rate of the first reaction chamber and the second reaction chamber>50 percent; the DO of the fourth reaction chamber and the third reaction chamber is controlled to be 3-6mg/L, and the aeration intensity is controlled>5m3/(m2H) total ammonia oxidation rate of the fourth reaction chamber and the third reaction chamber>50 percent; the fifth reaction chamber controls the stirring speed to be 30-50r/min and the reflux ratio of the water collecting well to be 100-150 percent until the surface load of the TN of the first reaction chamber is removed>0.8gN/(m2D) BOD removal rate of the fifth reaction chamber>70%, entering the next step;
e. CANON adds the start-up fedback, adopts two series B operational modes, and specific operational mode is: the sewage to be treated continuously enters the first reaction chamber and the fourth reaction chamber through the fifth reaction chamber, water in the first reaction chamber enters the second reaction chamber and the third reaction chamber by controlling related valves, finally, effluent is converged into a second water collecting well, part of the effluent flows back to the fifth reaction chamber, the rest of the effluent is discharged through a second water outlet pipe, the effluent of the fourth reaction chamber is converged into the first water collecting well, part of the effluent of the water collecting well flows back to the fifth reaction chamber, and the rest of the effluent is discharged through the first water outlet pipe; the first reaction chamber controls DO to be 1.5-3.5mg/L and the aeration intensity>5m3/(m2H), the rotating speed of a stirring device is 15-30 r/min; the second reaction chamber controls DO to be 0.5-1.5mg/L and the aeration intensity>1.5m3/(m2H), the rotating speed of the stirring device is 30-45 r/min; the DO of the third reaction chamber is controlled to be 1-2mg/L, and the aeration intensity is controlled>3m3/(m2H), the rotating speed of the stirring device is 30-45 r/min; controlling DO in the fourth reaction chamber to be 3-6mg/L and controlling aeration intensity>5m3/(m2H) ammoxidation rate>50 percent; the fifth reaction chamber controls the stirring speed to be 30-50r/min and the reflux ratio of the water collecting well to be 100-150 percent until the TN of the second reaction chamber removes the surface load>1.6gN/(m2D) BOD removal rate of the fifth reaction chamber>80%, entering the next step;
f. CANON expansion starting, adopting the double-series A operation mode, and continuously feeding water; reacting the fourth reaction chamber and the third reaction chamber with the first reaction chamber(ii) displacement of 30-50% of the suspended carrier in each of the chamber and the second reaction chamber; the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber are controlled to have DO of 1.0-2.5mg/L and aeration intensity>3m3/(m2H), the rotating speed of the stirring device is 15-30r/min, the rotating speed of the fifth reaction chamber is controlled to be 30-50r/min, the reflux ratio of the water collecting well is controlled to be 100-250%, and the surface load is removed until the TN of the four reaction chambers>1.6gN/(m2D) BOD removal rate of the fifth reaction chamber>70%, entering the next step;
g. the CANON runs stably and water is continuously fed; when the TN removal rate is required<When 90 percent of the total wastewater is treated, the parallel operation mode is adopted, the stirring rotating speed of the fifth reaction chamber is controlled to be 30-50r/min, the reflux ratio of the water collecting well is controlled to be 100-250 percent, and the BOD removal rate of the fifth reaction chamber>70 percent, the DO of the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber is controlled to be 2.0-5.0mg/L, and the aeration intensity is controlled>5m3/(m2H), the rotating speed of the stirring device is 30-45r/min, the ammonia nitrogen in the effluent is 50-80mg/L, and the surface load is removed by TN>2.5gN/(m2D); when the TN removal rate is required to be more than or equal to 90 percent, a double-series A operation mode is adopted, the fifth reaction chamber controls the stirring rotating speed to be 30-50r/min, the reflux ratio of the water collecting well is controlled to be 100-250 percent, and the BOD removal rate of the fifth reaction chamber>70 percent, the DO of the first reaction chamber and the DO of the fourth reaction chamber are controlled to be 2.0-5.0mg/L, and the aeration intensity is controlled>6m3/(m2H), the rotating speed of a stirring device is 30-45r/min, and the removal rate of TN is higher than that of a stirring device>50 percent, the DO of the second reaction chamber and the DO of the third reaction chamber are controlled to be 1.5-2.5mg/L, and the aeration intensity is controlled>3m3/(m2H), the rotating speed of the stirring device is 15-30r/min, and the ammonia nitrogen in the effluent of the second reaction chamber or the third reaction chamber is 30-50 mg/L.
The technical scheme has the following direct beneficial effects:
divide into five reaction chambers with the reaction tank through the baffle, it is through arranging first sump pit, second sump pit to control through relevant valve, can realize the different three kinds of different control modes with prior art, promptly: the reaction chambers are connected in series, parallel or independently operated by controlling the water outlet directions of the first reaction chamber to the fourth reaction chamber, and the three control modes are adopted, so that the inoculation proportion is small, the starting is fast, the denitrification and carbon removal effects are good, and the specific beneficial technical effects are shown in the specific implementation mode of the specification.
As a preferable scheme of the invention, the C/N of the inlet water is less than 2, the sludge concentration of each reaction chamber is less than 0.5g/L in the stable operation stage, and the stirring rotating speed of the fifth reaction chamber is controlled to be 30-50 r/min.
In another preferred embodiment of the present invention, the power of the stirrer in each reaction chamber is 15 to 50W/m3Selecting a model; in the stable operation stage, when the C/N of the inlet water is less than 1, the reflux ratio of the water collecting well is controlled to be 100-150%, when the C/N of the inlet water is less than or equal to 1 and less than 1.5, the reflux ratio of the water collecting well is controlled to be 150-200%, and when the C/N of the inlet water is less than or equal to 1.5 and less than 2, the reflux ratio of the water collecting well is controlled to be 200-250%.
Further, the diversion device comprises a first diversion valve, a second diversion valve and a third diversion valve, wherein the first diversion valve is positioned on a horizontal leftward partition plate connected with the fifth reaction chamber, the second diversion valve is positioned on a vertical downward partition plate connected with the second water collecting well, and the third diversion valve is positioned on a horizontal rightward partition plate connected with the fifth reaction chamber; the fifth reaction chamber is also provided with a first water outlet valve, a second water outlet valve, a third water outlet valve and a fourth water outlet valve which are used for controlling the water outlet of the fifth reaction chamber, the first water collecting well is also provided with a fifth water outlet valve and a sixth water outlet valve which are used for controlling the water outlet of the first reaction chamber and the fourth reaction chamber, and the second water collecting well is provided with a seventh water outlet valve and an eighth water outlet valve which are used for controlling the water outlet of the second reaction chamber and the third reaction chamber.
Furthermore, two rows of aeration devices in the four reaction chambers are formed by arranging a plurality of groups of perforated aeration pipes and microporous aeration pipes at intervals, and each group of perforated aeration pipes is arranged along the length direction of the reaction chambers.
Furthermore, the first water collecting well and the second water collecting well are both provided with reflux pumps, the reflux pumps are connected with reflux pipes, the other ends of the reflux pipes reflux to the fifth reaction chamber, the water collecting device further comprises a ninth water outlet valve and a tenth water outlet valve, the ninth water outlet valve is positioned on the first water outlet pipe orifice, and the tenth water outlet valve is positioned on the second water outlet pipe orifice.
Further, the parallel operation mode specifically comprises the following steps: the sewage to be treated continuously enters a fifth reaction chamber through a water inlet pipe, the effluent water passes through a ninth water outlet screen, a first water outlet valve, a second water outlet valve, a third water outlet valve and a fourth water outlet valve, and then the effluent water of the first reaction chamber and the fourth reaction chamber flows through a fifth effluent screen, a fifth effluent valve, a sixth effluent screen and a sixth effluent valve to a first water collecting well, part of the effluent water flows back to the fifth reaction chamber, the rest of the effluent water is discharged through a first water outlet pipe, the effluent water of the second reaction chamber and the third reaction chamber flows through a seventh effluent screen, a seventh effluent valve, an eighth effluent screen and an eighth effluent valve to a second water collecting well, part of the effluent water flows back to the fifth reaction chamber, and the rest of the effluent water is discharged through a second water outlet pipe.
Further, the above-mentioned double series a operation mode specifically includes the steps of: continuously feeding the sewage to be treated into a fifth reaction chamber through a water inlet pipe, continuously feeding the effluent into a first reaction chamber and a fourth reaction chamber through a ninth effluent screen, a first effluent valve, a first effluent screen, a fourth effluent valve and a fourth effluent screen, feeding the effluent from the first reaction chamber into a second reaction chamber through the first effluent screen, a first flow guide valve and a second effluent screen, returning part of the effluent to the fifth reaction chamber after passing through a seventh effluent screen, a seventh effluent valve and a second water collecting well, and discharging the rest of the effluent through a second water outlet pipe; and the effluent of the fourth reaction chamber enters the third reaction chamber through the fourth water outlet screen, the third diversion valve and the third water outlet screen, part of the effluent of the third reaction chamber passes through the eighth water outlet screen, the eighth water outlet valve and the second water collecting well, then flows back to the fifth reaction chamber, and the rest of the effluent is discharged through the second water outlet pipe.
Further, the above-mentioned double series B operation mode specifically includes the steps of: continuously feeding the sewage to be treated into a fifth reaction chamber through a water inlet pipe, continuously feeding the effluent into a first reaction chamber and a fourth reaction chamber through a ninth water outlet screen, a first water outlet valve, a first water outlet screen, a fourth water outlet valve and a fourth water outlet screen, feeding the effluent from the first reaction chamber into the second reaction chamber through the first water outlet screen, a first flow guide valve and a second water outlet screen, feeding the effluent from the second reaction chamber into a third reaction chamber through a seventh water outlet screen, a second flow guide valve and an eighth water outlet screen, returning part of the effluent from the third reaction chamber to the fifth reaction chamber through an eighth water outlet screen, an eighth water outlet valve and a second water collecting well, and discharging the rest of the effluent through a second water outlet pipe; and after the effluent of the fourth reaction chamber passes through a sixth water outlet screen, a sixth water outlet valve and the first water collecting well, part of the effluent flows back to the fifth reaction chamber, and the rest of the effluent is discharged through the first water outlet pipe.
Compared with the prior art, the invention has the beneficial technical effects that:
1) the starting time is short, and the starting can be successful only in 120 days;
2) the inoculation ratio is small, and is not more than 5 percent;
3) the starting scale is large, and the method is suitable for large-scale starting of large-volume engineering;
4) a sludge reflux system is not needed, and the process flow is simple;
5) the aeration power consumption is low, the occupied area is small, the management is convenient and easy to operate, and the stability and the running performance of the system are better;
6) the contact time of the wastewater and the carrier biological membrane is long, and the impact load resistance is strong;
7) the biological membrane is continuously updated under the action of water flow shearing force, keeps higher biological activity, and has the highest volume load of 1.5 kgN/(m)3·d)；
8) The operation mode is flexible, and the reaction tanks can be operated in series, in parallel or independently according to the effluent standard to realize stable operation;
9) the preposed denitrification can reduce the adverse effect of influent COD on autotrophic denitrification functional microorganisms, improve the application range of the CANON process and improve the removal rate of total nitrogen and COD to a certain extent;
10) the denitrification can supplement certain alkalinity for the CANON reaction tank and enhance the nitrification effect.
Drawings
The invention is further described below with reference to the accompanying drawings:
FIG. 1 is a plan view of an enhanced denitrification system based on CANON _ MBBR according to the present invention;
FIG. 2 is a left side view of the enhanced denitrification system based on CANON _ MBBR of the present invention;
FIG. 3 is a plan view of an aeration device of the enhanced denitrification system based on CANON _ MBBR of the invention;
FIG. 4 is a schematic view of a fifth reaction chamber according to the present invention;
FIG. 5 is a schematic cross-sectional view of a fifth reaction chamber according to the present invention;
fig. 6 is a schematic view of a sump well according to the present invention.
In the figure 1, a reaction tank main body; 2. a partition plate; 3. a stirring device; 4. a microporous aeration pipe; 5. perforating an aeration pipe; K1-K2, first sump well-second sump well; l0, water inlet pipe; L1-L2, a first water outlet pipe-a second water outlet pipe; C1-C5, reaction chamber (first reaction chamber-fifth reaction chamber); F1-F3, a diversion valve (first diversion valve-third diversion valve); M1-M10, outlet valve (first outlet valve-tenth outlet valve); S1-S9, a water outlet screen (a first water outlet screen-a ninth water outlet screen).
Detailed Description
The invention provides a rapid starting method of a CANON _ MBBR-based enhanced denitrification system, and in order to make the advantages and technical scheme of the invention clearer and clearer, the invention is described in detail with reference to specific embodiments.
First, the related art terms involved in the present invention are explained as follows:
1) the suspension carrier, the specific gravity is 0.93-0.97, the void ratio is more than 90%, and the suspension carrier is also called suspension filler, carrier and filler for short;
2) effective specific surface area: since the outer surfaces of the carriers rub against each other and it is difficult for microorganisms to attach to them, the effective specific surface area generally refers to the inner surface area, i.e., the effective surface area per unit volume of the carriers. Effective specific surface area ═ effective surface area ÷ volume, in m2/m3；
3) Specific gravity: the ratio of the density of the carrier to the density of water at normal temperature;
4) porosity: the ratio of the volume of the gaps between the carriers and the gaps among the carriers to the stacking volume of the carriers;
5) fluidization: under the action of aeration or stirring, the filler flows along with the water flow in the liquid and is in full contact with water pollutants, and the suspended carriers do not accumulate and can freely flow along with the water flow in the tank;
6) filling rate: the filling rate of the suspension carrier, namely the ratio of the volume of the suspension carrier to the pool capacity of the filling area, wherein the volume of the suspension carrier is the total volume under natural accumulation; e.g. 100m3Suspending vehicle, filled to 400m3The tank capacity is 25 percent;
7) surface loading: the amount of pollutants removed per day per unit specific surface area of the filler, gN/(m)2·d)；
8) Ammonia oxidation surface loading: the mass of the unit filler specific surface area oxidized ammonia nitrogen every day; gN/(m)2D); if the ammonia nitrogen of the inlet water is 400mg/L, the ammonia nitrogen of the outlet water is 200mg/L, and the inlet water flow is 5m3D, biofilm area 1000m2The ammonia oxidation surface load is 1.0 gN/(m) at (400-2·d)；
9) TN removal of surface load: the mass of total nitrogen per unit of effective specific surface area of the filler removed per day, gN/(m)2D); if the inlet water TN is 500mg/L, the outlet water TN is 100mg/L, and the inlet water flow is 10m3D, biofilm area 2000m2If the TN removal surface load is (500-100). times. 10/2000 ═ 2 gN/(m)2·d)；
10) Autotrophic nitrogen removal: the process is a general name of nitrosation and anaerobic ammonia oxidation (ANAMMOX), so that the aim of denitrification is fulfilled; under aerobic conditions, Ammonia Oxidizing Bacteria (AOB) oxidize ammonia nitrogen part into nitrous acid, and the generated nitrous acid and part of the rest ammonia nitrogen are subjected to anaerobic ammonia oxidation (ANAMMOX) reaction under the action of anaerobic ammonia oxidizing bacteria (ANAOB) to generate nitrogen;
11) CANON process, i.e. autotrophic nitrogen removal in a single reactor; in CANON, AOB and AnAOB coexist in the same reactor; the AOB is positioned on the outer layer of the carrier, and oxygen is used as an electron acceptor to oxidize ammonia nitrogen into nitrite; the AnAOB is positioned in the inner layer of the carrier, and the nitrite is used as an electron acceptor to be converted into nitrogen together with the residual ammonia nitrogen;
12) CANON suspension vector: namely, the suspension carrier with CANON effect exists, AOB and AnAOB exist in a biomembrane mode in a layered mode;
13) nitrosation: microorganism will ammonia Nitrogen (NH)4 +) Oxidation to nitrite Nitrogen (NO)2 -) Without further oxidation to nitrate Nitrogen (NO)3 -) The process of (1), namely enriching Ammonia Oxidizing Bacteria (AOB) in the system and eliminating Nitrite Oxidizing Bacteria (NOB);
14) denitrification: refers to the bacterial reduction of Nitrate (NO)3 -) Nitrogen (N) in (A) is passed through a series of intermediates (NO)2 -、NO、N2O) reduction to nitrogen (N)2) The biochemical process of (a);
15) reflux ratio: the ratio of the water amount which flows back to the biological section for continuous treatment to the total water amount is percent;
16) MBBR: moving Bed Biofilm reactor MBBR (moving Bed Biofilm reactor) the method increases the biomass and the biological species in the reactor by adding a certain amount of suspension carriers into the reactor, thereby increasing the treatment efficiency of the reactor;
17) aeration strength: aeration per unit area in m3/(m2H) including the sum of the two parts of micro-aeration and perforating aeration; for example, the aeration rate of the micropores is 10m3H, perforation aeration rate of 5m3H, the bottom area of the reactor is 5m2The aeration intensity is (10+ 5)/5-3 m3/(m2·h)；
18) The reflux ratio of the water collecting well is as follows: the ratio of the water amount which flows back to the biological section for continuous treatment to the total water amount is percent;
19) total ammonia oxidation rate: the ratio of the total amount of ammonia nitrogen oxidized after the intake water passes through the multi-stage aerobic reaction tank to the total amount of ammonia nitrogen in the intake water is percent; if the ammonia nitrogen in the inlet water is 400mg/L, the ammonia nitrogen in the outlet water is 100mg/L after passing through the two-stage aerobic reaction tank, and the total ammonia oxidation rate is (400-100)/400-75%; for single stage reactors, it is generally referred to directly as the ammoxidation rate; for a multistage reactor, the ammonia oxidation rate refers to the ammonia nitrogen oxidation condition of each stage, and if the performance of the multistage whole is analyzed, the total ammonia oxidation rate is used;
20) TN removal rate: the total nitrogen removal amount accounts for the ratio of the total nitrogen of the inlet water;
21) common activated sludge: namely activated sludge in a biochemical pool of a sewage plant, and the inoculation of the sludge mainly comprises the primary acquisition of AOB strains and the accelerated biofilm formation;
22) C/N: i.e. the ratio of carbon to nitrogen in the feed water, refers to BOD in the feed water5The ratio to Kjeldahl nitrogen (organic nitrogen + ammonia nitrogen);
23) pretreatment: if the C/N of the inlet water is too large and is not suitable for the treatment of the autotrophic nitrogen removal related process, the pretreatment is carried out to reduce the content of organic matters until the water quality requirement of autotrophic nitrogen removal is met;
24) stirrer power: i.e. the power per unit effective tank volume, W/m3(ii) a The activated sludge process is usually 3-5W/m3(ii) a In MBBR, the agitation power is correlated with the filling rate, and the higher the filling rate, the higher the agitation power.
The first reaction chamber, the second reaction chamber, the third reaction chamber, the fourth reaction chamber and the fifth reaction chamber are abbreviated as C1, C2, C3, C4 and C5, the first diversion valve, the second diversion valve and the third diversion valve are abbreviated as F1, F2 and F3, the first water outlet valve, the second water outlet valve, the third water outlet valve … and the tenth water outlet valve are abbreviated as M1, M2 and M3 …, M10, the water inlet pipe of the fifth reaction chamber is abbreviated as L0, the first water collecting well and the second water collecting well are respectively K1 and K2, and the first water outlet screen is a ninth water outlet screen S1-S9.
First, the present invention is an enhanced denitrification system based on CANON _ MBBR, as shown in fig. 1 to 3, comprising a reaction tank body 1, a stirring device 3, an aeration device, and a water collection device, wherein the interior of the reaction tank body is divided into two rows of four reaction chambers, namely a first reaction chamber, a second reaction chamber, a third reaction chamber, and a fourth reaction chamber, by partition plates 2, wherein the first reaction chamber and the fourth reaction chamber are arranged in a row and located at the bottom, the first reaction chamber and the second reaction chamber are arranged in a row, which is equivalent to the first reaction chamber located at the lower left, and then the first reaction chamber, the third reaction chamber, and the fourth reaction chamber are respectively located in the clockwise direction, the centers of the partition plates are not crossed, and the center of the partition plate is the fifth reaction chamber.
A first water outlet screen, a second water outlet screen, a third water outlet screen and a fourth water outlet screen are respectively arranged at the diagonal positions of the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber, the first water outlet screen, the second water outlet screen, the third water outlet screen and the fourth water outlet screen are obliquely arranged and form a relatively closed area, and the fifth reaction chamber is positioned in the relatively closed area;
a water inlet pipe is arranged in the middle of the right side of the fifth reaction chamber, water is fed into the water inlet pipe through a water inlet pipe L0, and a ninth water outlet screen is arranged at the upper part of the fifth reaction chamber;
a fifth water outlet screen and a sixth water outlet screen are arranged below the first reaction chamber and the fourth reaction chamber, a first water collecting well is arranged in an area formed by the fifth water outlet screen and the sixth water outlet screen, and the first water collecting well K1 is used for collecting sewage in the reaction tank and then discharging the sewage through a first water outlet pipe L1;
a seventh water outlet screen and an eighth water outlet screen are arranged above the second reaction chamber and the third reaction chamber, the second water collecting well is arranged in an area formed by the seventh water outlet screen and the eighth water outlet screen, and the second water collecting well K2 is used for collecting sewage in the reaction tank and then discharging the sewage through a second water outlet pipe L2;
the suspension carrier is added into each reaction chamber, a stirring device is arranged in each reaction chamber, and the stirring direction is adjusted according to a required operation mode, and the method specifically comprises the following steps: in the parallel operation mode, the directions of C1 and C3 are the same and are anticlockwise stirring, and the directions of C2 and C4 are the same and are clockwise stirring; when the double-series A operation mode is adopted, the directions of C1 and C2 are the same and clockwise stirring is adopted, and the directions of C3 and C4 are the same and counterclockwise stirring is adopted; in the double series B mode of operation, C1, C2, and C4 are in the same direction and are stirring clockwise, and C3 is stirring counterclockwise. The concrete structure and the operation mode of the stirring device can be realized by referring to the prior art, and if the stirring device can select a variable-frequency stirrer.
The aeration devices are distributed in two rows and two columns of four reaction chambers, the aeration devices in each reaction chamber are formed by arranging a plurality of groups of perforated aeration pipes 4 and microporous aeration pipes 5 at intervals, and each group of perforated aeration pipes and each group of microporous aeration pipes are arranged along the length direction of the reaction chamber.
Preferably, the first water collecting well and the second water collecting well are both provided with reflux pumps, the reflux pumps are connected with reflux pipes, the other ends of the reflux pipes reflux to the fifth reaction chamber, the water collecting device further comprises a ninth water outlet valve and a tenth water outlet valve, the ninth water outlet valve is positioned on a first water outlet pipe orifice connected with the first water collecting well, and the tenth water outlet valve is positioned on a second water outlet pipe orifice connected with the second water collecting well.
As shown in fig. 4 to 6, the preferred flow guiding structure of the present invention is as follows:
the system comprises a first diversion valve, a second diversion valve and a third diversion valve, wherein the first diversion valve is positioned on a horizontal leftward partition plate connected with a fifth reaction chamber, the second diversion valve is positioned on a vertical downward partition plate connected with a second water collecting well, and the third diversion valve is positioned on a horizontal rightward partition plate connected with the fifth reaction chamber; the first water collecting well is also provided with a first water outlet valve, a second water outlet valve, a third water outlet valve and a fourth water outlet valve which are used for controlling the water outlet of each reaction chamber, and the second water collecting well is provided with a fifth water outlet valve and a sixth water outlet valve which are used for controlling the water outlet of the reaction chambers. The water outlet direction of each reaction chamber is controlled by a flow guide device.
Secondly, the operation flow of the present invention is mainly described below with reference to the above system.
The operation flow comprises the following 3 control modes:
1) parallel operation mode: the sewage to be treated continuously enters a reaction chamber C5 through a water inlet pipe L0, the effluent water respectively passes through outlet valves M1-M4 and then passes through an outlet screen S1-S4 to reach a reaction chamber C1-C4; C1-C4 are in parallel connection and operate independently, and finally are gathered into water collecting wells K1 and K2, part of effluent of the water collecting wells flows back to the fifth reaction chamber, the rest of effluent flows through a K1 connecting valve M9, K2 is connected with an effluent valve M10, and the effluent is controlled by a valve in the process; the valves are not described as being in a closed state;
2) dual series a mode of operation: the sewage to be treated continuously enters a reaction chamber C5 through a water inlet pipe L0, the effluent water respectively passes through outlet valves M1 and M4, and then continuously enters reaction chambers C1 and C4 through outlet screens S1 and S4; c1 effluent enters a reaction chamber C2 through an effluent screen S1, a diversion valve F1 and an effluent screen S2, and C2 effluent is converged into an outlet pipe L2 to be discharged through an effluent screen S7, an outlet valve M7, a water collecting well K2 and an outlet valve M10; c4 effluent enters a reaction chamber C3 through an effluent screen S4, a diversion valve F3 and an effluent screen S3, C3 effluent passes through an effluent screen S8, an effluent valve M8 and a water collecting well K2, and the effluent valve M10 is converged into an effluent pipe L2 to be discharged; the double-series A mode is that two groups of C1-C4 are connected in parallel, and two grids of each group are respectively connected in series, namely C1-C2 and C4-C3;
3) dual series B mode of operation: the sewage to be treated continuously enters a reaction chamber C5 through a water inlet pipe L0, the effluent water respectively passes through outlet valves M1 and M4, and then continuously enters reaction chambers C1 and C4 through outlet screens S1 and S4; c1 effluent enters a reaction chamber C2 through an effluent screen S1, a diversion valve F1 and a screen S2, C2 effluent enters C3 through an effluent screen S7, a diversion valve F2 and an effluent screen S8, and C3 effluent is converged into an outlet pipe L2 effluent after passing through an effluent screen S8, an outlet valve M8, a water collecting well K2 and an outlet valve M10; c4 effluent is converged into an outlet pipe L1 to be discharged after passing through an outlet screen S6, an outlet valve M6, a water collecting well K1 and an outlet valve M9; the double series B mode, namely two groups of C1-C4 are connected in parallel: a group of three grids are connected in series, and a group of single grids, namely C1-C2-C3 and C4, finally water is discharged from a water collecting well K1.
Different operation modes are set, and the functional requirements of different operation stages and different water outlet standards are mainly considered to be met.
Thirdly, the starting method of the invention comprises the following steps:
1) starting preparation, namely adding a suspension carrier into each reaction chamber, wherein the filling rate is 20-67%; inoculating common activated sludge, wherein the sludge concentration in each reaction chamber is 3-5 g/L;
2) nitrosation and denitrification are started, a parallel operation mode is adopted, DO of C1-C4 is controlled to be 3-6mg/L through an aeration device, and the aeration intensity is controlled>5m3/(m2H); c5, controlling the stirring speed to be 30-50r/min and controlling the reflux ratio of the water collecting well to be 50-100%; running until the sludge concentration in each reaction chamber<1.0g/L, BOD removal rate of reaction chamber C5>50% ammonia oxidation rate of C1-C4 in reaction chamber>50% ammoxidation surface load>1.5gN/(m2D), go to the next step;
3) CANON pre-start, adopting a double-series A operation mode, controlling DO at 3-6mg/L by C3 and C4, and controlling aeration intensity>5m3/(m2H) overall ammoxidation rate>50％；The rotation speed of the C1 and C2 stirring devices is 30-45r/min, DO is controlled to be 1-2mg/L, and the aeration intensity is controlled>3m3/(m2H); c5, controlling the stirring speed to be 30-50r/min and controlling the reflux ratio of the water collecting well to be 50-100%; the operation is carried out until the total ammoxidation rates of C1 and C2 are reached>50% C1 ammoxidation surface load>1.0gN/(m2D), BOD removal rate of C5>60%, entering the next step;
4) CANON inoculation is started, the double-series A operation mode is adopted, CANON suspension carriers are inoculated to C1, the inoculation rate is 3-5%, the stirring speed is controlled to be 15-30r/min by C1, the DO is controlled to be 0.5-1.5mg/L, and the aeration intensity is controlled>2m3/(m2H); c2 stirring speed of 15-30r/min, DO controlled at 1-2mg/L, aeration intensity>3m3/(m2H) total ammoxidation rates of C1 and C2>50 percent; c3 and C4 control DO at 3-6mg/L, aeration intensity>5m3/(m2H) overall ammoxidation rate>50 percent; c5, controlling the stirring speed to be 30-50r/min and controlling the reflux ratio of the water collecting well to be 100-150%; run until TN at C1 removes surface loading>0.8gN/(m2D), BOD removal rate of C5>70%, entering the next step;
5) CANON feeding starting, adopting a double-series B operation mode, controlling the stirring speed at 15-30r/min by C1, controlling the DO at 1.5-3.5mg/L, and aerating the mixture>5m3/(m2H); c2 controlling stirring speed at 30-45r/min, DO at 0.5-1.5mg/L, and aeration intensity>1.5m3/(m2H); c3 controlling DO at 1-2mg/L, aeration intensity>3m3/(m2H), the rotating speed of the stirring device is 30-45 r/min; c4 controlling DO at 3-6mg/L, aeration intensity>5m3/(m2H) ammoxidation rate>50 percent; c5, controlling the stirring speed to be 30-50r/min and controlling the reflux ratio of the water collecting well to be 100-150%; run until TN at C2 removes surface loading>1.6gN/(m2D), BOD removal rate of C5>80%, entering the next step;
6) CANON expansion start, adopting the above-mentioned double series A operation mode to respectively replace 30-50% of suspension carriers in C4 and C3 and C1 and C2; C1-C4, stirring speed is controlled to be 15-30r/min, DO is controlled to be 1.0-2.5mg/L, and aeration intensity is controlled>3m3/(m2H), C5 controlling the stirring speed to be 30-50r/min and the reflux ratio of the water collecting well to be 100-250%(ii) a Running until TN of each reaction cell removes surface load>1.6gN/(m2D), BOD removal rate of C5>70%, entering the next step;
7) stable operation of CANON, when TN removal rate requires<When 90 percent of the total water content is in the parallel operation mode, the stirring speed is controlled to be 30-50r/min by C5, the reflux ratio of the water collecting well is controlled to be 100-250 percent, and the BOD removal rate of C5>70 percent, C1-C4 are controlled to DO between 2.0 mg/L and 5.0mg/L, and the aeration intensity is controlled>5m3/(m2H), the rotating speed of the stirring device is 30-45r/min, the ammonia nitrogen in the effluent is 50-80mg/L, and the surface load is removed by TN>2.5gN/(m2D); when the TN removal rate is required to be more than or equal to 90 percent, a double-series A operation mode is adopted, the stirring rotation speed is controlled by C5 to be 30-50r/min, the reflux ratio of the water collecting well is controlled to be 100-250 percent, and the BOD removal rate of C5>70 percent, C1 and C4 are controlled to ensure that DO is between 2.0 and 5.0mg/L and the aeration intensity is controlled>6m3/(m2H), the rotating speed of a stirring device is 30-45r/min, and the removal rate of TN is higher than that of a stirring device>50 percent, C2 and C3 are controlled to ensure that DO is between 1.5 and 2.5mg/L and the aeration intensity is controlled>3m3/(m2H), the rotating speed of the stirring device is 15-30r/min, and the ammonia nitrogen of the effluent of C2 or C3 is 30-50 mg/L.
In the steps, the C/N of inlet water is less than 2, the sludge concentration of each reaction chamber is less than 0.5g/L in the stable operation stage, and the stirring rotating speed of the fifth reaction chamber is controlled to be 30-50 r/min.
The power of the stirrer of each reaction chamber in the step is 15-50W/m3Selecting a model; in the stable operation stage, when the C/N of the inlet water is less than 1, the reflux ratio of the water collecting well is controlled to be 100-150%, when the C/N of the inlet water is less than or equal to 1 and less than 1.5, the reflux ratio of the water collecting well is controlled to be 150-200%, and when the C/N of the inlet water is less than or equal to 1.5 and less than 2, the reflux ratio of the water collecting well is controlled to be 250% in an area of 200-;
supplementary explanation:
1) considering the stirring direction of each reaction chamber, mainly preventing the short flow phenomenon of water inflow, for example, when a double-series A operation mode is adopted, sewage to be treated enters C1 through a first water inlet, C1 water flows into C2 through a first water outlet screen, a second diversion valve and a second water outlet screen, C1 is anticlockwise stirring, C2 is clockwise stirring, the sewage is converged into a water outlet pipe to be discharged after fully reacting C2 through a fifth water outlet screen, a fifth water outlet valve and a second water collecting well, otherwise, C2 is anticlockwise stirring, and the sewage is converged into the water outlet pipe to be discharged after not fully reacting C2 through the fifth water outlet screen, the fifth water outlet valve and the second water collecting well;
2) DO control requirements of all stages are different, nitrosation starting is controlled to be 3-6mg/L, and nitrosation biofilm formation is accelerated by controlling DO to improve ammoxidation rate; the method is characterized in that the DO level is adjusted to meet the requirement of biomembrane layering by providing an anaerobic environment for a CANON biomembrane to ensure the Anamox living environment when CANON pre-start, CANON inoculation start and CANON fed-batch start control DO is lower; the important difference between the biomembrane method and the activated sludge method is that the existing mode of the microorganism belongs to an attached state or a suspended state; the suspended state microorganism is not limited by mass transfer, while the attached state carries mass transfer through matrix gradient, and the requirements on mixing and shearing are high;
3) the operation modes of all stages are different, and the inoculation mode and the operation mode are mainly considered;
4) the control of the stirring rotating speed is different, the CANON pre-start, the CANON flow and start control stirring rotating speed is 30-45r/min for the purpose of assisting carrier fluidization when the aeration is insufficient, CANON inoculation start, CANON expansion start control stirring rotating speed is 15-30r/min to prevent the falling of the biological membrane caused by overlarge shearing force, and CANON stable operation control stirring rotating speed is 30-45r/min to prevent the thickening of the biological membrane caused by small shearing force;
5) the difference of the aeration intensity is to achieve the purposes of assisting the fluidization of the carrier and the oxygenation of the system and prevent the thickening of the biomembrane when the shearing force is too small or the falling of the biomembrane when the shearing force is too large;
6) the method has the application range, is suitable for high-ammonia nitrogen, high-C/N and high-temperature wastewater, and is particularly suitable for treating anaerobic sludge digestion supernatant, landfill leachate and the like;
7) the sludge concentration in each reaction chamber in the stable operation stage is less than 0.5g/L, and the purpose is mainly to ensure the pure membrane effect, namely microorganisms mainly exist in an attached state, and when the concentration of suspended sludge is increased, the microorganisms and a biological membrane form a competitive relationship to influence the growth of the biological membrane;
8) aiming at different inlet water C/N, different reflux ratios of the water collecting well need to be set, and the main reason is that along with the increase of the inlet water C/N, the denitrification process can be enhanced by adjusting the reflux ratio of the water collecting well upwards, the influence of COD in the inlet water on an autotrophic nitrogen removal system is eliminated, and the nitrogen and carbon removal efficiency is improved;
9) different reflux ratios are set in the starting stage, sufficient nitrite is set to ensure a lower reflux ratio after nitrosation is considered in the early stage, sufficient BOD is favorable for denitrification biofilm formation, and CANON consumption nitrous acid is considered in the later stage to improve the reflux ratio to cause insufficient decarburization and incomplete decarburization of denitrification matrix.
As is well known to those skilled in the art, when the C/N of the inlet water is more than or equal to 2, the pretreatment decarburization is added to meet the requirement.
As is well known to those skilled in the art, the addition of a heat exchange system can be achieved when the water temperature is not between 25 ℃ and 35 ℃.
As is well known to those skilled in the art, implementation of micro-pore aeration and perforation aeration achieves the same DO requirement and different aeration strengths by adjusting the flow ratio of the micro-pore aeration and the perforation aeration.
As is well known to those skilled in the art, the specific gravity of the suspension carrier before membrane formation is slightly smaller than that of water, usually 0.93-0.97, and the specific gravity after membrane formation is close to that of water, so as to achieve the suspension effect, and the suspension carrier is generally made of high-density polyethylene.
The present invention is further illustrated by the following specific examples.
Example 1:
anaerobic digestion sludge dewatering liquid of a certain municipal sewage treatment plant is used as system inlet water, part of chemical wastewater is contained in the inlet water, and the water quantity is 2500m3The pH value is 7.9-8.2, the water temperature is 30-35 ℃, the BOD concentration of inlet water is 800-3Is divided into five reaction chambers C1-C5, and the effective volume of C5 is 200m3The effective volumes of C1-C4 are all 250m3。
Starting preparation, adding a suspension carrier into each reaction chamber, wherein the effective specific surface area of the carrier is 800m2/m3The porosity is 90 percent, the filling rate of the composite material meets the industry standard of high density polyethylene suspension carrier for water treatment (CJ/T461-2014), the filling rate of C5 is 60 percent, and the filling rate of C1-C4 is 55 percent; inoculating common activated sludge, wherein the sludge concentration in each reaction chamber is about 4.3 g/L;
nitrosation and denitrification are started, a parallel operation mode is adopted, DO of C1-C4 is controlled to be 3.5-3.8mg/L through an aeration device, and the aeration intensity is 5.5m3/(m2H); and (3) collecting the effluent to a water collecting well by opening a water outlet valve, wherein 50% of the effluent of the water collecting well flows back to C5 for inoculation in a denitrification tank, the residual effluent is discharged through a water outlet pipe, and the sludge does not flow back and naturally runs off. The operation is carried out for 32 days until the sludge concentration in each reaction chamber reaches 0.5 to 0.8g/L, the BOD removal rate of the reaction chamber C5 reaches 63 percent, the ammonia oxidation rate of the reaction chamber C1 to C4 reaches 51 percent, and the ammonia oxidation surface load is 1.87gN/(m < n >)2D), go to the next step;
CANON pre-starting, controlling the rotation speed of the C1 and C2 stirring devices to be 30r/min, controlling the DO to be about 1.2mg/L, and controlling the aeration intensity to be 3.3m3/(m2H). The DO of the C4 and the C3 is controlled to be about 3mg/L, and the aeration intensity is 5.1m3/(m2H), the total ammoxidation rate of C4 and C3 reaches 62 percent. And part of effluent from the water collecting well flows back to C5, and the reflux ratio is 50%. After 16 days of operation, the total ammoxidation rate of C1 and C2 reaches 51 percent, and the ammoxidation surface load of C1 reaches 1.59 gN/(m)2D), BOD removal rate of C5 is 70%, and the next step is carried out;
CANON inoculation is started, CANON suspension carriers are inoculated to C1, the inoculation rate is 4%, DO is controlled to be 0.8-1.2mg/L, the rotating speed of a stirring device is controlled to be 20r/min, and the aeration intensity is 2.5m3/(m2H). C2 controlling DO at 1-2mg/L, controlling the rotation speed of the stirring device at 20r/min and the aeration intensity at 3.5m3/(m2H). C3 and C4 control DO at 3-3.5mg/L, aeration intensity is 5.1m3/(m2H). The reflux ratio of the water collecting well is 100 percent. After the operation is carried out for 35 days, the total ammoxidation rate of C3 and C4 is maintained at more than 70 percent, and the TN removal surface load of C1 exceeds 1.08 gN/(m)2D), BOD removal rate of C5% and proceeding to the next step;
CANON feeding is started, C1 controls the rotation speed of the stirring device to be 30r/min, DO is controlled to be 2.5-3.0mg/L, and the aeration intensity is 5.5m3/(m2H). C2 controlling the rotation speed of the stirring device to 35r/min, controlling DO to be about 1.5mg/L and controlling the aeration intensity to be 3.0m3/(m2H), controlling DO at 3.5-4.0mg/L by C4 and aeration intensity at 6m3/(m2H), the ammoxidation rate is maintained at about 75%. C3 controlDO is about 2mg/L, and the aeration intensity is 3.0m3/(m2H). The reflux ratio of the water collecting well is 150 percent. After 26 days of operation, the surface load of TN-removed C2 reaches 1.63 gN/(m)2D), BOD removal rate of C5 is 85%, and the next step is carried out;
CANON expansion start, displacing the C4 and C3 reaction chambers with 50% of the suspended carrier in the C1 and C2 reaction chambers, respectively; the DO of the C1-C4 is controlled to be 2.3-2.5mg/L, and the aeration intensity is 3.5m3/(m2H). The reflux ratio of the water collecting well is 200 percent. After 15 days of operation, each reaction chamber TN had a surface load removal of more than 2.1 gN/(m)2D), BOD removal rate of C5 is 80%, and the next step is carried out;
the CANON runs stably in a double-series A running mode, wherein DO of C1 and C4 is controlled to be 3.5mg/L, and the aeration intensity is 5.0m3/(m2H), the ammoxidation rate is greater than 61%; both C2 and C3 controlled DO at 2.5mg/L, aeration intensity at 3.5m3/(m2H). The reflux ratio of the water collecting well is 200 percent. The ammonia nitrogen of the effluent of C2 or C3 is about 30 mg/L. The maximum membrane load of the C1-C4 reaction chamber TN removal film reaches 3.49 gN/(m)2D) corresponding to a volume loading of up to 1.53kgN/m3And d, the TN removal rate of the reaction tank reaches 95 percent, and the BOD removal rate is more than 70 percent.
In the above step, the stirring speed of the reaction chamber C5 is controlled to be 45 r/min.
Example 2:
the designed water inlet amount of a certain coking wastewater treatment plant is 1000m3The COD concentration of inlet water is about 3500mg/L, the BOD concentration is about 1000mg/L, NH4 -The average concentration of N is 560mg/L, TN, the average concentration is 600mg/L, the pH value is 7.9-8.1, the water temperature is 30-35 ℃, and the total effective volume of the reaction tank is designed to be 900m3Effective volume of C5 reaction chamber 300m3The effective volumes of the C1-C4 reaction chambers are all 150m3。
Starting preparation, adding a suspension carrier into each reaction chamber, wherein the effective specific surface area of the carrier is 800m2/m3The porosity is 90 percent, the filling rate of the composite material meets the industry standard of high-density polyethylene suspension carrier for water treatment (CJ/T461-2014), the filling rate of C5 is 60 percent, and the filling rate of C1-C4 is 35 percent; inoculating common activated sludge, wherein the sludge concentration in each reaction chamber is about 4.0 g/L;
nitrosation is started, DO of a C1-C4 reaction chamber is controlled to be 3.0-4.0mg/L, and the aeration intensity is 5.3m3/(m2H), collecting the effluent to a water collecting well by opening a water outlet valve, wherein 50% of the effluent of the water collecting well flows back to C5, the carrier of the denitrification tank is coated, the rest effluent is discharged through a water outlet pipe, and the sludge does not flow back and naturally runs off. The sludge concentration in the reaction chamber reaches 0.86g/L after 28 days of operation, the ammoxidation rate of C1-C4 reaches 55 percent, and the ammoxidation surface load is 1.79 gN/(m)2D), BOD removal rate of the reaction chamber C5 is 58%, and the next step is carried out;
CANON pre-starting, controlling the rotation speed of the C1 and C2 stirring devices to be 30r/min, controlling the DO to be about 1.2mg/L, and controlling the aeration intensity to be 3.5m3/(m2H), the total ammoxidation rate of C1 and C2 reaches 53 percent. The DO of the C4 and the C3 is controlled to be about 3mg/L, and the aeration intensity is 5.1m3/(m2H), the total ammoxidation rate of C4 and C3 reaches 72 percent. The reflux ratio of the water collecting well is controlled by 50 percent. After 16 days of operation, the ammonia oxidation surface load of C1 was 1.17 gN/(m)2D), BOD removal rate of the reaction chamber C5 is 65%, and the next step is carried out;
CANON inoculation is started, CANON suspension carriers are inoculated to C1, the inoculation rate is 4%, DO is controlled to be 0.8-1.2mg/L, the rotating speed of a stirring device is controlled to be 20r/min, and the aeration intensity is 2.5m3/(m2H). C2 controlling DO at 1-2mg/L, controlling the rotation speed of the stirring device at 20r/min and the aeration intensity at 3.5m3/(m2H). C3 and C4 control DO at 3-3.5mg/L, aeration intensity is 5.1m3/(m2H). The reflux ratio of the water collecting well is controlled to be 100 percent. After the operation for 38 days, the total ammoxidation rate of C3 and C4 is maintained above 70 percent, the BOD removal rate of the reaction chamber C5 is 80 percent, and the TN removal surface load of C1 exceeds 0.99 gN/(m)2D), go to the next step;
CANON feeding is started, C1 controls the rotation speed of the stirring device to be 30r/min, DO is controlled to be 2.5-3.0mg/L, and the aeration intensity is 5.5m3/(m2H). C2 controlling the rotation speed of the stirring device to 35r/min, controlling DO to be about 1.5mg/L and controlling the aeration intensity to be 3.0m3/(m2H), controlling DO at 3.5-4.0mg/L by C4 and aeration intensity at 6m3/m2The ammonia oxidation rate is kept about 75 percent. C3 controlling DO at 2mg/L and aeration intensity at 3.0m3/(m2H). The reflux ratio of the water collecting well is controlled to be 150 percent. After 32 days of operation, the surface load of TN-removed C2 reaches 1.63 gN/(m)2D), BOD removal rate of the reaction chamber C5 of 81%, proceeding to the next step;
CANON expansion start, displacing the C4 and C3 reaction chambers with 50% of the suspended carrier in the C1 and C2 reaction chambers, respectively; controlling DO at 2.5-3.0mg/L and aeration intensity at 4.5m by C1-C43/(m2H). The reflux ratio of the water collecting well is controlled to be 200 percent. After 15 days of operation, each reaction chamber TN had a surface loading removal of more than 1.66 gN/(m)2D), BOD removal rate of the reaction chamber C5 is 79%, and the next step is carried out;
the CANON runs stably in a parallel running mode, DO of the reaction chambers C1-C4 is controlled to be 3.5mg/L, and the aeration intensity is controlled to be 5.0m3/(m2H), controlling the reflux ratio of the water collecting well at 250%. The total nitrogen removal membrane load of the C1-C4 reaction chamber reaches 2.7 gN/(m)2D), the total nitrogen removal rate of the reaction tank reaches 88 percent; the ammonia nitrogen of the effluent is about 50 mg/L. The BOD of the effluent is less than or equal to 200 mg/L.
In the above step, the stirring speed of the reaction chamber C5 is controlled to be 45 r/min.
The reaction chambers are connected in series, in parallel or independently operated by controlling the water outlet directions of the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber; the CANON process is quickly started by means of inoculation, feeding and the like; according to the processing standard requirements, different process arrangement forms are realized; high-efficiency denitrification and decarbonization realized by combining CANON process with denitrification process
The parts which are not described in the invention can be realized by taking the prior art as reference.
It is intended that any equivalents, or obvious variations, which may be made by those skilled in the art in light of the teachings herein, be within the scope of the present invention.

Claims (9)

1. A CANON _ MBBR-based rapid starting method of an enhanced denitrification system is characterized by comprising the following steps: the enhanced denitrification system comprises a reaction tank main body, a stirring device, an aeration device, a flow guide device, a water collecting device and a reflux device, wherein the interior of the reaction tank main body is divided into two rows of four reaction chambers and one reaction chamber positioned in the center of the four reaction chambers through partition plates, namely a first reaction chamber, a second reaction chamber, a third reaction chamber, a fourth reaction chamber and a fifth reaction chamber, wherein the first reaction chamber and the fourth reaction chamber are arranged in a row and positioned at the bottom, the first reaction chamber and the second reaction chamber are arranged in a row, and the fifth reaction chamber is positioned at the center of diagonal connecting lines of the two rows of four reaction chambers;
a first water outlet screen, a second water outlet screen, a third water outlet screen and a fourth water outlet screen are respectively arranged at the diagonal positions of the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber, the first water outlet screen, the second water outlet screen, the third water outlet screen and the fourth water outlet screen are obliquely arranged and form a relatively closed area, and the fifth reaction chamber is positioned in the relatively closed area;
a water inlet pipe is arranged in the middle of the right side of the fifth reaction chamber, sewage to be treated enters the fifth reaction chamber through the water inlet pipe, and a ninth water outlet screen is arranged at the upper part of the fifth reaction chamber; sewage to be treated enters the two rows of four reaction chambers through the ninth water outlet screen, the first water outlet screen, the second water outlet screen, the third water outlet screen and the fourth water outlet screen;
the water collecting device comprises a first water collecting well, a second water collecting well, a first water outlet pipe and a second water outlet pipe which are respectively connected with the first water collecting well and the second water collecting well;
a fifth water outlet screen and a sixth water outlet screen are further arranged below the adjacent sides of the first reaction chamber and the fourth reaction chamber, the first water collecting well is arranged in an area formed by the fifth water outlet screen and the sixth water outlet screen, and the first water collecting well is used for collecting sewage in the reaction tank and then discharging the sewage through the first water outlet pipe;
a seventh water outlet screen and an eighth water outlet screen are further arranged above the adjacent side of the second reaction chamber and the third reaction chamber, and a second water collecting well is arranged in an area formed by the seventh water outlet screen and the eighth water outlet screen and used for collecting sewage in the reaction tank and then discharging the sewage through a second water outlet pipe;
the flow guide device is used for controlling the flow direction of water in the reaction chamber and adjusting the flow direction according to a required operation mode;
suspension carriers are added into each reaction chamber, a stirring device is arranged in each reaction chamber, and the stirring direction is adjusted according to a required operation mode;
the aeration devices are distributed in the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber;
the starting method sequentially comprises the following steps:
a. starting preparation, namely adding a suspension carrier into each reaction chamber, wherein the filling rate is 20-67%; inoculating common activated sludge, wherein the sludge concentration in each reaction chamber is 3-5 g/L;
b. nitrosation and denitrification are started, a parallel operation mode is adopted, and the specific operation mode is as follows: the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber are in parallel relation, sewage to be treated continuously enters the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber through the fifth reaction chamber, effluent is converged into the first water collecting well and the second water collecting well by controlling related valves, part of effluent of the water collecting well flows back to the fifth reaction chamber, and the rest of effluent is discharged through the first water outlet pipe and the second water outlet pipe; controlling DO of the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber to be 3-6mg/L by the aeration device, and controlling the aeration intensity>5m3/(m2H), controlling the stirring speed of the fifth reaction chamber to be 30-50r/min, controlling the reflux ratio of the water collecting well to be 50-100%, and naturally losing the sludge without refluxing until the sludge concentration in each reaction chamber<Ammonia oxidation rate of 1.0g/L in the first, second, third and fourth reaction chambers>50% ammoxidation surface load>1.5gN/(m2D) BOD removal rate of the fifth reaction chamber>50%, entering the next step;
c. CANON pre-starts, adopts two series A running modes, and concrete running mode is: the first reaction chamber and the second reaction chamber are in a group, the third reaction chamber and the fourth reaction chamber are in a group, sewage to be treated continuously enters the first reaction chamber and the fourth reaction chamber through the fifth reaction chamber, and the first reaction chamber is enabled to be in the first reaction chamber through controlling the relevant valvesThe water in the reaction chamber enters a second reaction chamber, so that the water in a fourth reaction chamber enters a third reaction chamber and is finally collected into a second water collecting well, part of the effluent from the water collecting well flows back to a fifth reaction chamber, and the rest of the effluent is discharged through a second water outlet pipe; the rotation speed of the stirring devices in the first reaction chamber and the second reaction chamber is 30-45r/min, the DO of the first reaction chamber and the second reaction chamber is controlled to be 1-2mg/L, and the aeration intensity is controlled>3m3/(m2H), controlling DO in the fourth reaction chamber and the third reaction chamber to be 3-6mg/L and controlling aeration intensity>5m3/(m2H) total ammonia oxidation rate of the fourth and third reaction chambers>50 percent; the fifth reaction chamber controls the stirring speed to be 30-50r/min and the reflux ratio of the water collecting well to be 50-100 percent until the total ammonia oxidation rate of the first reaction chamber and the second reaction chamber>50% ammonia oxidation surface load of the first reaction chamber>1.0gN/(m2D) BOD removal rate of the fifth reaction chamber>60% of the solution enters the next step;
d. CANON inoculation is started, the double-series A operation mode is adopted, CANON suspension carriers are inoculated into the first reaction chamber, the inoculation rate is 3-5%, DO is controlled to be 0.5-1.5mg/L, and the aeration intensity>2m3/(m2H), controlling the rotating speed of the stirring device to be 15-30 r/min; the second reaction chamber controls DO to be 1-2mg/L and the aeration intensity>3m3/(m2H), the rotating speed of the stirring device is 15-30r/min, and the total ammonia oxidation rate of the first reaction chamber and the second reaction chamber>50 percent; the DO of the fourth reaction chamber and the third reaction chamber is controlled to be 3-6mg/L, and the aeration intensity is controlled>5m3/(m2H) total ammonia oxidation rate of the fourth reaction chamber and the third reaction chamber>50 percent; the fifth reaction chamber controls the stirring speed to be 30-50r/min and the reflux ratio of the water collecting well to be 100-150 percent until the surface load of the TN of the first reaction chamber is removed>0.8gN/(m2D) BOD removal rate of the fifth reaction chamber>70%, entering the next step;
e. CANON adds the start-up fedback, adopts two series B operational modes, and specific operational mode is: the first reaction chamber, the second reaction chamber and the third reaction chamber are in a group, the fourth reaction chamber is in a group, sewage to be treated continuously enters the first reaction chamber and the fourth reaction chamber through the fifth reaction chamber, and water in the first reaction chamber enters the second reaction chamber by controlling the relevant valvesThe system comprises a chamber, a third reaction chamber, a fifth reaction chamber, a fourth reaction chamber, a fifth reaction chamber and a fourth reaction chamber, wherein finally the effluent is collected to a second water collecting well, part of the effluent flows back to the fifth reaction chamber, the rest of the effluent is discharged through a second water outlet pipe, the effluent of the fourth reaction chamber is collected to a first water collecting well, part of the effluent of the water collecting well flows back to the fifth reaction chamber, and the rest of the effluent is discharged through a first water outlet pipe; the first reaction chamber controls DO to be 1.5-3.5mg/L and the aeration intensity>5m3/(m2H), the rotating speed of a stirring device is 15-30 r/min; the second reaction chamber controls DO to be 0.5-1.5mg/L and the aeration intensity>1.5m3/(m2H), the rotating speed of the stirring device is 30-45 r/min; the DO of the third reaction chamber is controlled to be 1-2mg/L, and the aeration intensity is controlled>3m3/(m2H), the rotating speed of the stirring device is 30-45 r/min; controlling DO in the fourth reaction chamber to be 3-6mg/L and controlling aeration intensity>5m3/(m2H) ammoxidation rate>50 percent; the fifth reaction chamber controls the stirring speed to be 30-50r/min and the reflux ratio of the water collecting well to be 100-150 percent until the TN of the second reaction chamber removes the surface load>1.6gN/(m2D) BOD removal rate of the fifth reaction chamber>80%, entering the next step;
f. CANON expansion starting, adopting the double-series A operation mode, and continuously feeding water; replacing 30-50% of the suspended carriers in the fourth reaction chamber and the third reaction chamber and in the first reaction chamber and the second reaction chamber respectively; the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber are controlled to have DO of 1.0-2.5mg/L and aeration intensity>3m3/(m2H), the rotating speed of the stirring device is 15-30r/min, the rotating speed of the fifth reaction chamber is controlled to be 30-50r/min, the reflux ratio of the water collecting well is controlled to be 100-250%, and the surface load is removed until the TN of the four reaction chambers>1.6gN/(m2D) BOD removal rate of the fifth reaction chamber>70%, entering the next step;
g. the CANON runs stably and water is continuously fed; when the TN removal rate is required<When 90 percent of the total wastewater is treated, the parallel operation mode is adopted, the stirring rotating speed of the fifth reaction chamber is controlled to be 30-50r/min, the reflux ratio of the water collecting well is controlled to be 100-250 percent, and the BOD removal rate of the fifth reaction chamber>70 percent, the DO of the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth reaction chamber is controlled to be 2.0-5.0mg/L, and the aeration intensity is controlled>5m3/(m2H) agitation equipmentThe speed is 30-45r/min, the ammonia nitrogen of the effluent is 50-80mg/L, and the surface load is removed by TN>2.5gN/(m2D); when the TN removal rate is required to be more than or equal to 90 percent, a double-series A operation mode is adopted, the fifth reaction chamber controls the stirring rotating speed to be 30-50r/min, the reflux ratio of the water collecting well is controlled to be 100-250 percent, and the BOD removal rate of the fifth reaction chamber>70 percent, the DO of the first reaction chamber and the DO of the fourth reaction chamber are controlled to be 2.0-5.0mg/L, and the aeration intensity is controlled>6m3/(m2H), the rotating speed of a stirring device is 30-45r/min, and the removal rate of TN is higher than that of a stirring device>50 percent, the DO of the second reaction chamber and the DO of the third reaction chamber are controlled to be 1.5-2.5mg/L, and the aeration intensity is controlled>3m3/(m2H), the rotating speed of the stirring device is 15-30r/min, and the ammonia nitrogen in the effluent of the second reaction chamber or the third reaction chamber is 30-50 mg/L.
2. The method of claim 1, wherein the CANON _ MBBR-based enhanced denitrification system is started quickly by the method comprising the following steps: the C/N of the inlet water is less than 2, the sludge concentration of each reaction chamber is less than 0.5g/L in the stable operation stage, and the stirring rotating speed of the fifth reaction chamber is controlled to be 30-50 r/min.
3. The method of claim 1, wherein the CANON _ MBBR-based enhanced denitrification system is started quickly by the method comprising the following steps: the power of the stirrer of each reaction chamber is 15-50W/m3Selecting a model; in the stable operation stage, when the C/N of the inlet water is less than 1, the reflux ratio of the water collecting well is controlled to be 100-150%, when the C/N of the inlet water is less than or equal to 1 and less than 1.5, the reflux ratio of the water collecting well is controlled to be 150-200%, and when the C/N of the inlet water is less than or equal to 1.5 and less than 2, the reflux ratio of the water collecting well is controlled to be 200-250%.
4. The method of claim 1, wherein the CANON _ MBBR-based enhanced denitrification system is started quickly by the method comprising the following steps: the diversion device comprises a first diversion valve, a second diversion valve and a third diversion valve, wherein the first diversion valve is positioned on a horizontal leftward partition plate connected with the fifth reaction chamber, the second diversion valve is positioned on a vertical downward partition plate connected with the second water collecting well, and the third diversion valve is positioned on a horizontal rightward partition plate connected with the fifth reaction chamber; the fifth reaction chamber is also provided with a first water outlet valve, a second water outlet valve, a third water outlet valve and a fourth water outlet valve which are used for controlling the water outlet of the fifth reaction chamber, the first water collecting well is also provided with a fifth water outlet valve and a sixth water outlet valve which are used for controlling the water outlet of the first reaction chamber and the fourth reaction chamber, and the second water collecting well is provided with a seventh water outlet valve and an eighth water outlet valve which are used for controlling the water outlet of the second reaction chamber and the third reaction chamber.
5. The method of claim 1, wherein the CANON _ MBBR-based enhanced denitrification system is started quickly by the method comprising the following steps: two rows of aeration devices in four reaction chambers are formed by arranging a plurality of groups of perforated aeration pipes and microporous aeration pipes at intervals, and each group of perforated aeration pipes and each group of microporous aeration pipes are arranged along the length direction of the reaction chambers.
6. The method of claim 1, wherein the CANON _ MBBR-based enhanced denitrification system is started quickly by the method comprising the following steps: the first water collecting well and the second water collecting well are both provided with reflux pumps, the reflux pumps are connected with reflux pipes, the other ends of the reflux pipes flow back to the fifth reaction chamber, the water collecting device further comprises a ninth water outlet valve and a tenth water outlet valve, the ninth water outlet valve is positioned on the first water outlet pipe, and the tenth water outlet valve is positioned on the second water outlet pipe.
7. The method for rapidly starting the CANON-MBBR-based enhanced nitrogen removal system according to claim 4, wherein the parallel operation mode comprises the following specific steps: the sewage to be treated continuously enters a fifth reaction chamber through a water inlet pipe, the effluent water passes through a ninth water outlet screen, a first water outlet valve, a second water outlet valve, a third water outlet valve and a fourth water outlet valve, and then the effluent water of the first reaction chamber and the fourth reaction chamber flows through a fifth effluent screen, a fifth effluent valve, a sixth effluent screen and a sixth effluent valve to a first water collecting well, part of the effluent water flows back to the fifth reaction chamber, the rest of the effluent water is discharged through a first water outlet pipe, the effluent water of the second reaction chamber and the third reaction chamber flows through a seventh effluent screen, a seventh effluent valve, an eighth effluent screen and an eighth effluent valve to a second water collecting well, part of the effluent water flows back to the fifth reaction chamber, and the rest of the effluent water is discharged through a second water outlet pipe.
8. The method of claim 4, wherein the double-series A operation mode comprises the following steps: continuously feeding the sewage to be treated into a fifth reaction chamber through a water inlet pipe, continuously feeding the effluent into a first reaction chamber and a fourth reaction chamber through a ninth effluent screen, a first effluent valve, a first effluent screen, a fourth effluent valve and a fourth effluent screen, feeding the effluent from the first reaction chamber into a second reaction chamber through the first effluent screen, a first flow guide valve and a second effluent screen, returning part of the effluent to the fifth reaction chamber after passing through a seventh effluent screen, a seventh effluent valve and a second water collecting well, and discharging the rest of the effluent through a second water outlet pipe; and the effluent of the fourth reaction chamber enters the third reaction chamber through the fourth water outlet screen, the third diversion valve and the third water outlet screen, part of the effluent of the third reaction chamber passes through the eighth water outlet screen, the eighth water outlet valve and the second water collecting well, then flows back to the fifth reaction chamber, and the rest of the effluent is discharged through the second water outlet pipe.
9. The method as claimed in claim 4, wherein the dual-series B operation mode comprises the following steps: continuously feeding the sewage to be treated into a fifth reaction chamber through a water inlet pipe, continuously feeding the effluent into a first reaction chamber and a fourth reaction chamber through a ninth water outlet screen, a first water outlet valve, a first water outlet screen, a fourth water outlet valve and a fourth water outlet screen, feeding the effluent from the first reaction chamber into the second reaction chamber through the first water outlet screen, a first flow guide valve and a second water outlet screen, feeding the effluent from the second reaction chamber into a third reaction chamber through a seventh water outlet screen, a second flow guide valve and an eighth water outlet screen, returning part of the effluent from the third reaction chamber to the fifth reaction chamber through an eighth water outlet screen, an eighth water outlet valve and a second water collecting well, and discharging the rest of the effluent through a second water outlet pipe; and after the effluent of the fourth reaction chamber passes through a sixth water outlet screen, a sixth water outlet valve and the first water collecting well, part of the effluent flows back to the fifth reaction chamber, and the rest of the effluent is discharged through the first water outlet pipe.
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Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002224688A (en) * 2000-11-28 2002-08-13 Kurita Water Ind Ltd Denitrifying method and denitrifying apparatus
WO2007069899A1 (en) * 2005-12-15 2007-06-21 St. Katholieke Universiteit Radboud Universiteit Nijmegen Anaerobic oxidation of methane and denitrification
CN103936145A (en) * 2014-04-12 2014-07-23 北京工业大学 CANON (Completely Autotrophic Nitrogen removal Over Nitrite) process starting method for MBR (Membrane Bioreactor)
CN106745754A (en) * 2017-03-13 2017-05-31 济南大学 A kind of biofilter of Anammox coupling denitrification dephosphorization and operation method
CN106830310A (en) * 2017-02-21 2017-06-13 浙江艾摩柯斯环境科技有限公司 Formula of having holidays by turns Anammox nitrogen rejection facility and its technique
CN106830318A (en) * 2017-02-24 2017-06-13 苏州科技大学 One kind realizes full autotrophic denitrogenation wastewater treatment equipment and processing method based on aerobic particle mud
CN106966500A (en) * 2017-04-18 2017-07-21 华南理工大学 Ammonia nitrogen waste water biochemical denitrification processing unit and technique that short distance nitration is combined with Anammox
EP3255016A1 (en) * 2016-06-10 2017-12-13 FCC Aqualia, S.A. Method for starting up and controlling a biological process for ammonium removal at low ammonium concentrations and low temperature through the use of a two stage autotrophic nitrogen removal process
CN108178294A (en) * 2017-11-28 2018-06-19 郑州轻工业学院 A kind of method of the low matrix anaerobic ammonia oxidation process of synchronous tandem promoter

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002224688A (en) * 2000-11-28 2002-08-13 Kurita Water Ind Ltd Denitrifying method and denitrifying apparatus
WO2007069899A1 (en) * 2005-12-15 2007-06-21 St. Katholieke Universiteit Radboud Universiteit Nijmegen Anaerobic oxidation of methane and denitrification
CN103936145A (en) * 2014-04-12 2014-07-23 北京工业大学 CANON (Completely Autotrophic Nitrogen removal Over Nitrite) process starting method for MBR (Membrane Bioreactor)
EP3255016A1 (en) * 2016-06-10 2017-12-13 FCC Aqualia, S.A. Method for starting up and controlling a biological process for ammonium removal at low ammonium concentrations and low temperature through the use of a two stage autotrophic nitrogen removal process
CN106830310A (en) * 2017-02-21 2017-06-13 浙江艾摩柯斯环境科技有限公司 Formula of having holidays by turns Anammox nitrogen rejection facility and its technique
CN106830318A (en) * 2017-02-24 2017-06-13 苏州科技大学 One kind realizes full autotrophic denitrogenation wastewater treatment equipment and processing method based on aerobic particle mud
CN106745754A (en) * 2017-03-13 2017-05-31 济南大学 A kind of biofilter of Anammox coupling denitrification dephosphorization and operation method
CN106966500A (en) * 2017-04-18 2017-07-21 华南理工大学 Ammonia nitrogen waste water biochemical denitrification processing unit and technique that short distance nitration is combined with Anammox
CN108178294A (en) * 2017-11-28 2018-06-19 郑州轻工业学院 A kind of method of the low matrix anaerobic ammonia oxidation process of synchronous tandem promoter

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
Start-up of moving bed biofilm reactors for deammonification: the role of hydraulic retention time, alkalinity and oxygen suppl;Gaul, T等;《WATER SCIENCE AND TECHNOLOGY》;20051231;第52卷(第7期);第127-133页 *
基于MBBR的CANON工艺处理消化液中试启动;周家中等;《中国环境科学》;20190630;第39卷(第6期);第2378-2386页 *
完全自养脱氮SBR反应器的运行、强化及模拟优化;蔡庆;《中国博士学位论文全文数据库工程科技Ⅰ辑》;20140215;B027-46 *

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