CN111170456A - MBBR-based non-nitrous-accumulation CANON system and operation method - Google Patents

MBBR-based non-nitrous-accumulation CANON system and operation method Download PDF

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CN111170456A
CN111170456A CN202010065078.7A CN202010065078A CN111170456A CN 111170456 A CN111170456 A CN 111170456A CN 202010065078 A CN202010065078 A CN 202010065078A CN 111170456 A CN111170456 A CN 111170456A
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tank
variable
aerobic
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pool
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CN111170456B (en
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张晶晶
吴迪
周宸宇
井添祺
韩文杰
刘曙
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Qingdao Sipurun Intelligent System Co ltd
Qingdao Sipurun Water Environmental Technology Co ltd
Qingdao Spring Water Treatment Co ltd
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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
    • C02F3/30—Aerobic and anaerobic processes
    • C02F3/302—Nitrification and denitrification treatment
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
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Abstract

The invention discloses a MBBR-based non-nitrous-accumulation CANON system and an operation method thereof, and relates to the technical field of biological sewage denitrification. The device comprises a reaction tank, a water inlet pipe, a water outlet pipe, a carbon source feeding pipeline, an aeration device and a stirring device, wherein the reaction tank comprises a first aerobic tank, a variable tank, a first anoxic tank and a second aerobic tank, inlet water enters a system through the water inlet pipe, flows through the first aerobic tank, the variable tank, the first anoxic tank and the second aerobic tank respectively and is discharged through the water outlet pipe, the denitrification function is realized by adjusting the operation mode of the variable tank in the system starting period, and the CANON function is realized by adjusting the operation mode of the variable tank in the stable operation period. The invention realizes the change of the tank volume ratio of the CANON tank and the anoxic tank by adjusting the operation mode of the variable tank in the starting period and the stable operation period, thereby realizing the rapid starting, starting and operation processes without the accumulation of a large amount of nitrous and ensuring that the water stably reaches the standard.

Description

MBBR-based non-nitrous-accumulation CANON system and operation method
Technical Field
The invention relates to the technical field of biological nitrogen removal of sewage, in particular to a MBBR-based CANON system without nitrite accumulation and an operation method thereof.
Background
The autotrophic nitrogen removal process (CANON) utilizes shortcut nitrification bacteria (AOB) and anaerobic ammonium oxidation bacteria (AnAOB) to carry out coupling of shortcut nitrification and anaerobic ammonium oxidation, and carries out nitrogen removal in the same reactor, compared with the traditional nitrification and denitrification process, the autotrophic nitrogen removal process has the advantages of saving 60% of aeration amount, not needing to add organic carbon sources, reducing 90% of sludge yield, relatively reducing the release amount of nitrogen oxides and the like. In addition, the process has high denitrification load, low operating cost and small occupied space, is known to be one of the most economic biological denitrification processes at present, and the two functional microorganisms involved in the autotrophic denitrification process are autotrophic bacteria, so the generation period is long, the propagation rate is slow, and the strains are easy to run off, so the process starting period is long.
The MBBR technology is one of ideal forms of CANON, two functional microorganisms of the CANON technology are respectively arranged on the outer layer and the inner layer of a biological membrane by adding a suspension carrier into a CANON system, wherein the outer layer of the suspension carrier forms an aerobic biological membrane taking Ammonia Oxidizing Bacteria (AOB) as dominant bacteria, and the inner layer forms an anaerobic/anoxic biological membrane mainly taking anaerobic ammonia oxidizing bacteria (ANAOB), thereby overcoming a series of defects that the traditional activated sludge method has long starting time, low tolerance to high dissolved oxygen, needs to be provided with a secondary sedimentation tank to prevent bacteria loss, is difficult to realize the synergy between the nitrification performance of flocculent sludge and the anaerobic ammonia oxidizing performance of granular sludge, and further becoming the CANON form with the most engineering potential. Of the Netherlands
Figure BDA0002375724650000011
The sewage plant utilizes the CANON-MBBR based process to treat the sludge digestive fluid, and the ammonia nitrogen removal load reaches 1.2 kgN/(m)3D) and the average energy consumption is only 1.45 to 1.75 kW.h.kg-1NH4 +N, in addition, the Himmerfjeren sewage plant in Sweden and the Hattingen sewage plant in Germany also adopt the autotrophic denitrification related process based on MBBR, and both obtain better treatment effect. At present, the CANON process is difficult to reach higher effluent standard, so the CANON process is mostly used together with the traditional nitrification and denitrification process. Currently, MBBsThe R-type CANON process forms a mature starting mode, namely, the mature CANON suspension carrier is used for inoculating the high-load short-range nitrification suspension carrier cultured in the early stage, so that the starting time can be obviously shortened, but a large amount of nitrous nitrogen can be generated in the culture process of the short-range nitrification suspension carrier, and the high FNA caused by the excessive nitrous nitrogen can obviously influence the subsequent traditional denitrification process, so that the effluent cannot reach the standard, and the effluent reaching form of the system in the starting stage is ensured to be severe.
The research reports of the related aspects of the prior art mainly include:
the inhibition of FNA and the cross-influence of denitrification (environmental science 2010,31(4):1030-1035) of Majuan, Wangli, Pengyzhen, etc. on the reduction of nitrate and the cross-influence between 2 electron acceptors under different pH conditions with nitrite of different concentrations were studied by a large number of batch tests. The result shows that the nitrate reduction has a significant correlation with Free Nitrous Acid (FNA), FNA but not nitrite is a real inhibitor of the nitrate reduction, the inhibition degree of the nitrate reduction capability is 60% when the FNA concentration is 0.01-0.025mg/L, and the nitrate reduction reaction is completely inhibited when the FNA concentration is more than 0.2 mg/L. In addition, the nitrite reducing capability of the sludge is inhibited by FNA, and when the concentration of FNA is increased from 0.01mg/L to 0.2mg/L, the nitrite reducing capability is reduced by 80%. This study only demonstrated the inhibition of denitrification by FNA, but no discussion was made as to how to actually eliminate the nitrite and reduce the FNA to reduce the inhibition.
Wanggang and the like (Wanggang, simultaneous shortcut nitrification/anaerobic ammonia oxidation/denitrification (SNAD) technology-based sludge digestion liquid denitrification process research [ D ]. university of great-chain organization, 2017) treat actual engineering sludge digestion liquid by starting a series shortcut nitrification-anaerobic ammonia oxidation first and then starting SNAD, debugging and starting the shortcut nitrification process first in the starting process to obtain stable effluent suitable for the anaerobic ammonia oxidation process, then inoculating anaerobic ammonia oxidation sludge and biofilm formation MBBR fillers which are pre-cultured by two pilot reactors (respectively providing seed sludge and biofilm formation fillers) into an anaerobic ammonia oxidation tank in batches, mixing the sludge of the shortcut nitrification tank and the sludge and fillers of the anaerobic ammonia oxidation tank after the anaerobic ammonia oxidation tank is cultured to obtain more anaerobic ammonia oxidation sludge, and starting the SNAD integrated process by the two tanks. The short-cut nitrification process is debugged and started in the early stage of the project, but the high-nitrite effluent water generated at the moment is not specially treated and does not reach the standard to be discharged.
Von (activated sludge process) was used as a starting and stability study [ D ] changan university 2015 ] for a single-stage autotrophic nitrogen removal process, and starting and nitrogen removal performance of the activated sludge process was studied by using a Sequencing Batch Reactor (SBR) and using common aerobic activated sludge as inoculation sludge. The result shows that after the SBR system realizes the stable short-cut nitrification process, a small amount of biomembranes with the single-stage autotrophic nitrogen removal function are inoculated, the activated sludge autotrophic nitrogen removal system is successfully started after 113d, the research adopts a mode of starting the short-cut nitrification in the starting autotrophic nitrogen removal process, and the high-nitrite effluent water in the starting stage is not specially treated.
In conclusion, the prior art has matured the research on inhibition of anammox and nitrification-denitrification by FNA. It is also clear during CANON start-up that starting short-cut nitrification first can shorten start-up time, but relevant studies on how the CANON start-up phase eliminates the phenomenon of nitrite accumulation through process optimization are not yet mature.
Disclosure of Invention
The invention aims to provide a CANON system without nitrous accumulation based on MBBR and an operation method thereof, which realize the change of the tank volume ratio of an autotrophic denitrification tank and an anoxic tank by adjusting the operation mode of a variable tank in a starting period and a stable operation period, thereby realizing the purposes of quick starting, no nitrous accumulation in the operation process and stable standard reaching of effluent.
One of the tasks of the invention is to provide a CANON system without the accumulation of the nitrous oxides based on MBBR, which adopts the following technical scheme:
a CANON system without nitrite accumulation based on MBBR comprises a reaction tank, a water inlet pipe, a water outlet pipe, a carbon source adding pipeline, an aeration device and a stirring device, wherein the reaction tank comprises a first aerobic tank, a variable tank, a first anoxic tank and a second aerobic tank, and system flowing water enters from the water inlet pipe, flows through the first aerobic tank, the variable tank, the first anoxic tank and the second aerobic tank respectively and then is discharged through the water outlet pipe;
the ratio of the tank volume of the first aerobic tank to the tank volume of the variable tank is 1:0.5-1:2, the ratio of the tank volume of the variable tank to the tank volume of the first anoxic tank is 1:0.5-1:2, and the ratio of the tank volume of the first anoxic tank to the tank volume of the second aerobic tank is 1:0.5-1: 1;
the variable pool is used for playing a denitrification function by adjusting the operation mode of the variable pool in the system starting period and playing a CANON function by adjusting the operation mode of the variable pool in the stable operation period;
the carbon source adding pipeline is used for adding a carbon source into the variable tank and the first anoxic tank;
the aeration device is arranged in the first aerobic tank, the variable tank and the second aerobic tank;
the stirring device is arranged in the variable pool and the first anoxic pool.
As a preferable mode of the present invention, the variable cells are provided in 2 to 4 groups.
In another preferred embodiment of the present invention, the variable tanks are provided in four groups, a mixed liquid return pipe is provided between the second aerobic tank and the first anoxic tank, and a mixed liquid return pump is provided in the mixed liquid return pipe.
Further, the four groups of variable pools are arranged in two rows and two columns and are respectively a first variable pool, a second variable pool, a third variable pool and a fourth variable pool, a carbon source feeding pipeline branch led out by the carbon source feeding pipeline is arranged in each variable pool, and a carbon source feeding valve is installed on the carbon source feeding pipeline branch.
Further, a water passing port and an intercepting screen are arranged between the adjacent tank bodies in the flowing water direction of the system.
Further, the water passing opening comprises a first aerobic pool water passing opening between the first aerobic pool and the first variable pool, a first variable pool water passing opening between the first variable pool and the second variable pool, a second variable pool water passing opening between the second variable pool and the third variable pool, a third variable pool water passing opening between the third variable pool and the fourth variable pool, a fourth variable pool water passing opening between the fourth variable pool and the first anoxic pool, a first anoxic pool water passing opening between the first anoxic pool and the second aerobic pool, and a second aerobic pool water outlet. The front ends of all the water outlets are respectively provided with the intercepting screens, namely a first aerobic tank intercepting screen between a first aerobic tank and a first variable tank, a first variable tank intercepting screen between the first variable tank and a second variable tank, a second variable tank intercepting screen between the second variable tank and a third variable tank, a third variable tank intercepting screen between the third variable tank and a fourth variable tank, a fourth variable tank intercepting screen between the fourth variable tank and a first anoxic tank, a first anoxic tank intercepting screen between the first anoxic tank and a second aerobic tank intercepting screen at the water outlet of the second aerobic tank.
Furthermore, the aeration device refers to aeration pipes positioned at the bottoms of the first aerobic tank, the first variable tank, the second variable tank, the third variable tank, the fourth variable tank and the second aerobic tank.
Further, the stirring device is a submersible stirrer located in the first variable tank, the second variable tank, the third variable tank, the fourth variable tank and the first anoxic tank.
Another task of the present invention is to provide an operation method of the CANON system based on MBBR without accumulation of nitrous oxides, which comprises the following steps:
a. starting preparation, namely adding a suspension carrier into each reaction tank, wherein the filling rate is 20-67%; inoculating common activated sludge in each reaction tank, wherein the sludge concentration in each reaction tank is 3-5 g/L;
b. starting short-cut nitrification and denitrification, continuously feeding water, and discharging system inlet water through a water outlet pipe after the system inlet water flows through a first aerobic tank, a first variable tank, a second variable tank, a first anoxic tank and a second aerobic tank respectively;
if the ammonia nitrogen concentration of the inlet water is less than 200mg/L, controlling the DO of the first aerobic tank to be 1.0-2.0mg/L and the aeration intensity>2.0m3/(m2H), turning on the aeration devices in the first variable tank, the second variable tank, the third variable tank and the fourth variable tank, turning off the stirring devices,controlling DO of each variable pool to be 2.0-6.0mg/L and aeration intensity to be more than 2.5m3/(m2H), opening a carbon source adding valve of the first anoxic tank, closing the other carbon source adding valves, ensuring that the C/N of the water inlet of the first anoxic tank is 4-6, and closing a mixed liquid reflux pump;
if the ammonia nitrogen concentration of the inlet water is 200-400mg/L, controlling the DO of the first aerobic tank to be 1.5-2.5mg/L and the aeration intensity>2.5m3/(m2H), turning on the aeration devices in the first variable tank to the third variable tank, turning off the stirring devices, controlling DO of each variable tank to be 2.0-6.0mg/L and aeration intensity to be more than 3.0m3/(m2H), opening a stirring device in the fourth variable tank, closing an aeration device, controlling the stirring speed to be 30-45r/min, opening a carbon source adding valve in the fourth variable tank, closing the rest carbon source adding valves, ensuring that the C/N of water inlet of the fourth variable tank is 4-6, controlling the stirring speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and controlling the aeration intensity to be more than 5.0m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 50-100%;
if the ammonia nitrogen concentration of the inlet water is 400-600mg/L, controlling the DO of the first aerobic tank to be 2.0-3.0mg/L and the aeration intensity>3m3/(m2H), turning on the aeration devices in the first variable tank and the second variable tank, turning off the stirring device, controlling DO of the first variable tank and the second variable tank to be 2.0-6.0mg/L, and controlling the aeration intensity to be more than 4.5m3/(m2H), the stirring devices in the third variable tank and the fourth variable tank are opened, the aeration device is closed, the stirring rotating speed of the third variable tank and the fourth variable tank is controlled to be 30-45r/min, a carbon source adding valve in the third variable tank is opened, the other carbon source adding valves are closed, the C/N of the inlet water of the third variable tank is ensured to be 4-6, the stirring rotating speed of the first anoxic tank is controlled to be 30-45r/min, the DO of the second aerobic tank is controlled to be 4.0-7.0mg/L, the aeration intensity is more than 5.0m3/(m2H), starting a mixed liquid reflux pump to ensure that the reflux ratio of the mixed liquid is 100-150%;
if the ammonia nitrogen concentration of the inlet water is 600-800mg/L, controlling the DO of the first aerobic tank to be 2.5-3.5mg/L and the aeration intensity>3.5m3/(m2H) opening the aeration device in the first variable tank to stirThe stirring device is closed, the DO of the first variable pool is controlled to be 2.0-6.0mg/L, and the aeration intensity is more than 3.0m3/(m2H), closing the aeration devices in the second variable tank and the fourth variable tank, opening the stirring device, controlling the stirring rotating speed of the second variable tank and the fourth variable tank to be 30-45r/min, opening a carbon source adding valve in the second variable tank, closing the rest carbon source adding valves, ensuring that the C/N of the inlet water of the second variable tank is 4-6, controlling the stirring rotating speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and controlling the aeration intensity to be more than 6.0m3/(m2H), starting a mixed liquid reflux pump to ensure that the reflux ratio of the mixed liquid is 200-250%;
if the ammonia nitrogen concentration of the inlet water is more than 800mg/L, controlling the DO of the first aerobic tank to be 3.0-4.0mg/L and the aeration intensity>3.5m3/(m2H), closing the aeration devices in the first to fourth variable tanks, opening the stirring device, variably controlling the stirring rotating speed to be 30-45r/min from the first to fourth variable tanks, opening a carbon source adding valve in the first variable tank, closing the rest carbon source adding valves, ensuring that the C/N of the inlet water of the first variable tank is 4-6, controlling the stirring rotating speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and ensuring that the aeration intensity is more than 6.0m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 300%; running until the sludge concentration in each reaction tank is less than 0.5 g/L; controlling DO of the first aerobic tank to be 3-6mg/L and controlling the aeration intensity>4.0m3/(m2H) ammoxidation rate>50 percent, controlling DO of the second aerobic tank to be 4.0-7.0mg/L and the aeration intensity to be more than 4.0m3/(m2H), the ammoxidation rate is > 90%;
the sludge concentration in each reaction tank is less than 0.5 g/L; continuously feeding water, and running until the ammonia oxidation surface load of the first aerobic tank>1.5gN/(m2D), go to the next step;
c. starting autotrophic denitrification inoculation, inoculating the CANON suspension carrier into the first aerobic tank, wherein the inoculation rate is 3-5%, DO in the first aerobic tank is controlled to be 0.5-1.5mg/L, and the aeration intensity is controlled>2m3/(m2H); the stirring devices of the first variable tank to the fourth variable tank are closed, the aeration device is opened, DO is controlled to be 0.5-1.5mg/L, and the aeration intensity is more than 2m3/(m2H), opening a carbon source adding valve in the first anoxic tank, closing the other carbon source adding valves to ensure that the C/N of the water inlet of the first anoxic tank is 4-6, opening a mixed liquid reflux pump, controlling the reflux ratio to be 100%, and running until the surface load of TN of the first aerobic tank is removed>0.8gN/(m2D), go to the next step;
d. the autotrophic nitrogen removal load is lifted, water is continuously fed, and the operation is carried out until the TN from the first variable tank to the fourth variable tank removes the surface load>0.8gN/(m2D), go to the next step;
e. the autotrophic nitrogen removal runs stably, water is continuously fed, DO of the first reaction tank and the first to fourth variable tanks is controlled to be 2.0-5.0mg/L, and the aeration intensity is controlled>2m3/(m2H), running until the surface load of the first aerobic tank TN is removed>2.5gN/(m2D) the first to fourth variable cells TN remove the surface load>1.5gN/(m2·d)。
The working principle of the MBBR-based CANON system without the accumulation of the nitrous oxides is as follows:
in the stage of starting the short-range nitrification, a large amount of nitrite is generated by ammonia oxidizing bacteria, so that the concentration of Free Nitrite (FNA) is too high, and the subsequent process is poisoned, therefore, the variable tank is adjusted to be an anoxic tank in the stage, the capacity of the anoxic denitrification tank is enlarged, the generated nitrite is completely denitrified, the poisoning effect on the subsequent system is reduced, and the effluent is ensured to reach the standard stably.
After the system enters an inoculation starting stage, the system starts to operate in a CANON form, the generated nitrite is reduced, a CANON biological film falling off from a first aerobic tank has a dynamic inoculation function on a variable tank, the variable tank is changed from an anoxic operation state to an aerobic operation state to be changed from an anoxic denitrification tank to the CANON tank, the function of the variable tank is flexibly adjusted through different inflow ammonia nitrogen, so that no nitrite is greatly accumulated in the whole operation process, the toxic action of FNA on the system is reduced, and the stable standard of the effluent is ensured.
Compared with the prior art, the invention has the following beneficial technical effects:
1) energy conservation and consumption reduction, based on the autotrophic nitrogen removal technology, 60 percent of aeration cost and 100 percent of external carbon source can be saved, and the nitrogen removal is not limited by inlet water C/N; in addition, the sludge yield of the autotrophic denitrification process is low, and the project sludge treatment cost can be reduced;
2) and (3) saving the occupied area of the project: the whole process is a CANON process and an AO process based on MBBR pure membranes, a traditional secondary sedimentation tank is not needed, and project occupation can be saved compared with the traditional process;
3) the starting time is short, and only about 110 days are needed for successful starting;
4) the effluent has high guarantee, the effluent of the high ammonia nitrogen wastewater is effectively prevented from exceeding the standard during the high ammonia nitrogen operation through the design of mixed liquid reflux, the effluent is ensured to stably meet the design requirement, the first anoxic tank is added with the matrix capable of utilizing the reflux of the nitrifying liquid and COD contained in the influent water for denitrification, the effluent TN is reduced, a certain alkalinity can be supplemented for the nitrifying tank, and the denitrification effect is enhanced; the second aerobic tank can further reduce the COD process of the effluent on the basis of nitrification, and the effluent can stably reach the standard through the functional combination of each reaction tank;
5) through the flexible adjustment of the function of the variable tank, the denitrification function of the variable tank is ensured to be exerted in the starting stage, and the CANON function is exerted in the stable operation stage, so that the effluent is ensured to stably reach the standard.
Drawings
The invention is further described below with reference to the accompanying drawings:
FIG. 1 is a schematic diagram of the construction of the MBBR-based CANON system without the accumulation of nitrous oxides;
in the figure: o1, a first aerobic tank; C1-C4, first to fourth variable pools; F1-F4, first to fourth variable cell carbon source pipeline valves; f5, a first anoxic tank carbon source pipeline valve; a1, a first anoxic tank; o2, a second aerobic tank; SO1, a first aerobic tank intercepting screen; SC1-SC4, first to fourth variable cell intercepting screens; SA1, first anoxic tank interception screen; SO2, a second aerobic tank intercepting screen; b, a mixed liquid reflux pump; i1, water inlet pipe; i2, a carbon source adding pipeline; i3 and a water outlet pipe.
Detailed Description
The invention provides a MBBR-based CANON system without nitrous accumulation and an operation method thereof, and in order to make the advantages and technical scheme of the invention clearer and clearer, the invention is described in detail by combining specific embodiments.
First, the related art terms involved in the present invention are explained as follows:
1) 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 improving the treatment efficiency of the Reactor;
2) 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;
3) 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;
4) short-range nitration: 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);
5) 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;
6) 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);
7) ammonia oxidation surface loading: the mass of the unit specific surface area of the filler, 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 (400-200). times.5/10002·d)；
8) 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 is5m2The aeration intensity is (10+ 5)/5-3 m3/(m2·h)；
9) CANON, 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;
10) CANON suspension vector: namely, the suspension carrier with CANON effect exists, AOB and AnAOB exist in a biomembrane mode in a layered mode;
11) 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 1.5 gN/(m) at (500-200). times.5/10002·d)；
12) 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 and the outlet water TN is 100mg/L, the inlet water flow is 10m3D, biofilm area 2000m2And TN divided surface load is 2 gN/(m) at (500-100). times.10/20002·d)；
13) 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;
14) FNA: namely free nitrous acid, the calculation method:
Figure BDA0002375724650000071
the concentration of the compound is positively correlated with the concentration of the nitrite, and negatively correlated with pH and temperature, the compound has high toxicity, and the current research shows that the compound has the inhibition concentration of 0.4mg/L on AOB and about 0.1mg/L on AnAOB.
The stirring device and the aeration device provided by the invention can be obtained by referring to the structure of the device in the prior art, for example, the stirring device is a submersible stirrer, and the aeration device is formed by laying an aeration pipeline in a corresponding reaction tank.
As shown in figure 1, the CANON system without the accumulation of the nitrous oxides based on the MBBR comprises a reaction tank, a water inlet pipe, a water outlet pipe, a carbon source adding pipeline, an aeration device and a stirring device.
The reaction tank comprises a first aerobic tank O1, a variable tank, a first anoxic tank A1 and a second aerobic tank O2, system running water enters from a water inlet pipe I1 and flows through the first aerobic tank, the variable tank, the first anoxic tank and the second aerobic tank respectively and then is discharged through a water outlet pipe I3;
the ratio of the tank volume of the first aerobic tank to the tank volume of the variable tank is 1:0.5-1:2, the ratio of the tank volume of the variable tank to the tank volume of the first anoxic tank is 1:0.5-1:2, and the ratio of the tank volume of the first anoxic tank to the tank volume of the second aerobic tank is 1:0.5-1: 1; the purpose of setting like this is in that adaptable different technology form, such as MBBR pure membrane method, activated sludge process, mud membrane complex method, different technology form pollutant removal load is different:
as the main improvement point of the invention, the denitrification effect is enhanced by changing the operation mode of the variable tank. Therefore, the design shape, arrangement and number of the variable pools of the present invention are developed around the main technical concept of the present invention of "changing the operation mode of the variable pools", and the present invention preferably selects 2 or 4 groups of variable pools, more preferably 4 groups of variable pools, as shown in fig. 1, a first variable pool C1, a second variable pool C2, a third variable pool C3 and a fourth variable pool C4, respectively, and an aeration device and a stirring device are provided in each variable pool.
The carbon source adding pipeline I2 is divided into a plurality of carbon source adding pipeline branches, and is respectively communicated with each variable tank and each first anoxic tank, a first variable tank carbon source pipeline valve F1 is arranged on a branch pipeline for providing a carbon source for the first variable tank, a second variable tank carbon source pipeline valve F2 is arranged on a branch pipeline for providing a carbon source for the second variable tank, a third variable tank carbon source pipeline valve F3 is arranged on a branch pipeline for providing a carbon source for the third variable tank, a fourth variable tank carbon source pipeline valve F4 is arranged on a branch pipeline for providing a carbon source for the fourth variable tank, and a first anoxic tank carbon source pipeline valve F5 is arranged on a branch pipeline for providing a carbon source for the first anoxic tank. The carbon source pipeline valve can realize the control of the carbon source in each reaction tank.
The aeration device is arranged in the first aerobic tank, the variable tank and the second aerobic tank;
the stirring device is arranged in the variable tank and the first anoxic tank.
The variable pool is adjusted to play a denitrification function by adjusting the operation mode of the variable pool in the system starting period, and is adjusted to play a CANON function by adjusting the operation mode of the variable pool in the stable operation period, and the specific adjustment mode is described in detail in the following operation method.
The intercepting screen comprises a first aerobic tank intercepting screen SO1 between the aerobic tanks and the first variable tank, a first variable tank intercepting screen SC1 between the first variable tank and the second variable tank, a second variable tank intercepting screen SC2 between the second variable tank and the third variable tank, a third variable tank intercepting screen SC3 between the third variable tank and the fourth variable tank, a fourth variable tank intercepting screen SC4 between the fourth variable tank and the first anoxic tank, a first anoxic tank intercepting screen SA1 between the first anoxic tank and the second aerobic tank, and a second aerobic tank intercepting screen SO2 at the water outlet of the second aerobic tank.
A mixed liquid return pipe is arranged between the second aerobic tank and the first anoxic tank, and a mixed liquid return pump B is arranged on the mixed liquid return pipe.
The operation of the present invention will be described in detail with reference to the above system to further understand and clarify how the variable cell(s) of the present invention can be adjusted.
The method sequentially comprises the following steps:
a. starting preparation, namely adding a suspension carrier into each reaction tank, wherein the filling rate is 20-67%; inoculating common activated sludge in each reaction tank, wherein the sludge concentration in each reaction tank is 3-5 g/L;
b. starting short-cut nitrification and denitrification, wherein system inlet water flows through the first aerobic tank, the first to fourth variable tanks, the first anoxic tank and the second aerobic tank respectively and is discharged through the water outlet pipe;
if the ammonia nitrogen concentration of the inlet water is less than 200mg/L, controlling the DO of the first aerobic tank to be 1.0-2.0mg/L and the aeration intensity>2.0m3/(m2H) the first variable pool, the second variable pool, the third variable pool,The aeration device in the fourth variable tank is started, the stirring device is closed, the DO of each variable tank is controlled to be 2.0-6.0mg/L, and the aeration intensity is more than 2.5m3/(m2H), opening a carbon source adding valve of the first anoxic tank, closing the other carbon source adding valves, ensuring that the C/N of the water inlet of the first anoxic tank is 4-6, and closing a mixed liquid reflux pump;
if the ammonia nitrogen concentration of the inlet water is 200-400mg/L, controlling the DO of the first aerobic tank to be 1.5-2.5mg/L and the aeration intensity>2.5m3/(m2H), turning on the aeration devices in the first variable tank to the third variable tank, turning off the stirring devices, controlling DO of each variable tank to be 2.0-6.0mg/L and aeration intensity to be more than 3.0m3/(m2H), opening a stirring device in the fourth variable tank, closing an aeration device, controlling the stirring speed to be 30-45r/min, opening a carbon source adding valve in the fourth variable tank, closing the rest carbon source adding valves, ensuring that the C/N of water inlet of the fourth variable tank is 4-6, controlling the stirring speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and controlling the aeration intensity to be more than 5.0m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 50-100%;
if the ammonia nitrogen concentration of the inlet water is 400-600mg/L, controlling the DO of the first aerobic tank to be 2.0-3.0mg/L and the aeration intensity>3.0m3/(m2H), turning on the aeration devices in the first variable tank and the second variable tank, turning off the stirring device, controlling DO of the first variable tank and the second variable tank to be 2.0-6.0mg/L, and controlling the aeration intensity to be more than 4.5m3/(m2H), the stirring devices in the third variable tank and the fourth variable tank are opened, the aeration device is closed, the stirring rotating speed of the third variable tank and the fourth variable tank is controlled to be 30-45r/min, a carbon source adding valve in the third variable tank is opened, the other carbon source adding valves are closed, the C/N of the inlet water of the third variable tank is ensured to be 4-6, the stirring rotating speed of the first anoxic tank is controlled to be 30-45r/min, the DO of the second aerobic tank is controlled to be 4.0-7.0mg/L, the aeration intensity is more than 5.0m3/(m2H), starting a mixed liquid reflux pump to ensure that the reflux ratio of the mixed liquid is 100-150%;
if the ammonia nitrogen concentration of the inlet water is 600-800mg/L, controlling the DO of the first aerobic tank to be 2.5-3.5mg/L and the aeration intensity>3.5m3/(m2H), turning on the aeration device in the first variable tank, turning off the stirring device, and controlling the DO in the first variable tank to be 2.0-6.0mg/L and the aeration intensity to be more than 3.0m3/(m2H), closing the aeration devices in the second variable tank and the fourth variable tank, opening the stirring device, controlling the stirring rotating speed of the second variable tank and the fourth variable tank to be 30-45r/min, opening a carbon source adding valve in the second variable tank, closing the rest carbon source adding valves, ensuring that the C/N of the inlet water of the second variable tank is 4-6, controlling the stirring rotating speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and controlling the aeration intensity to be more than 6.0m3/(m2H), starting a mixed liquid reflux pump to ensure that the reflux ratio of the mixed liquid is 200-250%;
if the ammonia nitrogen concentration of the inlet water is more than 800mg/L, controlling the DO of the first aerobic tank to be 3.0-4.0mg/L and the aeration intensity>3.5m3/(m2H), closing the aeration devices in the first to fourth variable tanks, opening the stirring device, variably controlling the stirring rotating speed to be 30-45r/min from the first to fourth variable tanks, opening a carbon source adding valve in the first variable tank, closing the rest carbon source adding valves, ensuring that the C/N of the inlet water of the first variable tank is 4-6, controlling the stirring rotating speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and ensuring that the aeration intensity is more than 6.0m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 300%; running until the sludge concentration in each reaction tank is less than 0.5 g/L; controlling DO of the first aerobic tank to be 3-6mg/L and controlling the aeration intensity>3.5m3/(m2H) ammoxidation rate>50 percent, controlling DO of the second aerobic tank to be 4.0-7.0mg/L and the aeration intensity to be more than 4.0m3/(m2H), the ammoxidation rate is > 90%;
the sludge concentration in each reaction tank is less than 0.5 g/L; continuously feeding water, and running until the ammonia oxidation surface load of the first aerobic tank>1.5gN/(m2D), go to the next step;
c. starting autotrophic denitrification inoculation, inoculating the CANON suspension carrier into the first aerobic tank, wherein the inoculation rate is 3-5%, DO in the first aerobic tank is controlled to be 0.5-1.5mg/L, and the aeration intensity is controlled>2m3/(m2H); the stirring devices of the first variable tank to the fourth variable tank are closed, the aeration device is opened,controlling DO to be 0.5-1.5mg/L and aeration intensity to be more than 2m3/(m2H), opening a carbon source adding valve in the first anoxic tank, closing the other carbon source adding valves to ensure that the C/N of the water inlet of the first anoxic tank is 4-6, opening a mixed liquid reflux pump, controlling the reflux ratio to be 100%, and running until the surface load of TN of the first aerobic tank is removed>0.8gN/(m2D), go to the next step;
d. the autotrophic nitrogen removal load is lifted, water is continuously fed, and the operation is carried out until the TN from the first variable tank to the fourth variable tank removes the surface load>0.8gN/(m2D), go to the next step;
e. the autotrophic nitrogen removal runs stably, water is continuously fed, DO of the first reaction tank and the first to fourth variable tanks is controlled to be 2.0-5.0mg/L, and the aeration intensity is controlled>2m3/(m2H), running until the surface load of the first aerobic tank TN is removed>2.5gN/(m2D) the first to fourth variable cells TN remove the surface load>1.5gN/(m2·d)。
The following is a further description with reference to specific examples.
In example 1 and example 2, four groups of variable pools are provided, in example 3, two groups of variable pools are provided, and in example 4, three groups of variable pools are provided.
Example 1:
design water volume of 1000m for a certain sewage treatment plant3D, COD, BOD of the influent water5、NH3TN and design values are respectively 500, 260, 800 and 850mg/L, a CANON system without nitrous accumulation based on MBBR is adopted for treatment, the tank volume ratio of the first aerobic tank to the variable tank is 1.0:1.0, the tank volume ratio of the variable tank to the first anoxic tank is 1.0:1.0, and the tank volume ratio of the first anoxic tank to the second aerobic tank is 1.0: 1.0. Starting a preparation stage, adding a suspension carrier (the filling rate is 50%) into each system, inoculating common activated sludge into each reaction tank, wherein the sludge concentration in each reaction tank is 4.5 g/L; and in the short-distance nitrification starting stage, the inlet water of the system flows through the first aerobic tank, the first to fourth variable tanks, the first anoxic tank and the second aerobic tank respectively and is discharged through the main water discharge pipe. Controlling DO in the first aerobic tank to be 3.0mg/L and the aeration intensity to be 2.5m3/(m2H) aeration in the first to fourth variable tanksClosing the device, opening the stirring device, variably controlling the stirring speed to be 45r/min from the first to the fourth, opening a carbon source adding valve in the first variable tank, closing the rest carbon source adding valves, ensuring that the C/N of the water inlet of the first variable tank is 4, controlling the stirring speed of the first anoxic tank to be 45r/min, controlling the DO of the second aerobic tank to be 5.0mg/L and the aeration intensity to be 6.0m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 300%; running until the sludge concentration in each reaction tank is less than 0.5 g/L; controlling DO of the first aerobic tank to be 3.0mg/L and the aeration intensity to be 3.5m3/(m2H) ammoxidation rate>50 percent, controlling the DO of the second aerobic tank to be 5.5mg/L and the aeration intensity to be more than 6.2m3/(m2H), the ammoxidation rate is > 90%; the operation is carried out until the ammonia oxidation surface load of the first aerobic tank is 1.6 gN/(m)2D). Inoculating CANON suspension carrier into the first aerobic tank with inoculation rate of 5%, controlling DO in the first aerobic tank at 0.7mg/L and aeration intensity of 2.2m3/(m2H); the stirring devices of the first variable tank to the fourth variable tank are closed, the aeration device is opened, DO is controlled to be 1.0mg/L, and the aeration intensity is 2.5m3/(m2H), opening a carbon source adding valve in the first anoxic tank, and closing the other carbon source adding valves to ensure that the C/N of the inlet water of the first anoxic tank is 4. The mixed liquid reflux pump is started, the reflux ratio is controlled to be 100 percent, the operation is carried out to 105d, and the surface load of TN removal of the first aerobic tank is 0.9 gN/(m)2D). Continuously feeding water, and running until the surface load of TN removal of the first variable pool to the fourth variable pool is 0.9 gN/(m)2D). Continuously feeding water, controlling DO in the first reaction tank and the first to fourth variable tanks to be 2.0mg/L and controlling aeration intensity to be 3m3/(m2H), running until the surface load of the first aerobic tank TN is removed by 2.7 gN/(m)2D), the surface load of the first to fourth variable cells TN is removed by 1.6 gN/(m)2D). The effluent nitrous is relatively stable in the whole operation process, no large amount of accumulation is generated, and COD and BOD of the effluent are5、NH3、TN、NO2Average values of 32.14, 19.21, 4.32, 10.33, 4.31mg/L, respectively.
Example 2:
the process parameters are set as follows:
a certain integrated equipment, design waterAmount of 24m3D, COD, BOD of the influent water5、NH3The TN and the design value are respectively 250, 120, 650 and 750mg/L, a CANON system without the accumulation of the nitrous acid based on MBBR is adopted for treatment, the tank volume ratio of the first aerobic tank to the variable tank is 1.0:1.0, the tank volume ratio of the variable tank to the first anoxic tank is 1.0:0.8, and the tank volume ratio of the first anoxic tank to the second aerobic tank is 1.0: 1.2. And in the preparation stage, suspension carriers (the filling rate is 55%) are added into each system, and each reaction tank is inoculated with common activated sludge, and system inlet water flows through the first aerobic tank, the first to fourth variable tanks, the first anoxic tank and the second aerobic tank respectively and is discharged through a main water discharge pipe. Controlling DO of the first aerobic tank to be 2.5mg/L and the aeration intensity to be 3.5m3/(m2H), turning on the aeration device in the first variable tank, turning off the stirring device, controlling the DO in the first variable tank to be 3.0mg/L and the aeration intensity to be 2.5m3/(m2H), closing the aeration devices in the second variable tank and the fourth variable tank, opening the stirring device, controlling the stirring rotating speed of the second variable tank and the fourth variable tank to be 45r/min, opening a carbon source adding valve in the second variable tank, closing the rest carbon source adding valves, ensuring that the C/N of the inlet water of the second variable tank is 4-6, controlling the stirring rotating speed of the first anoxic tank to be 45r/min, controlling the DO of the second aerobic tank to be 6.0mg/L and the aeration intensity to be 6.5m3/(m2H), starting a mixed liquid reflux pump to ensure that the reflux ratio of the mixed liquid is 200-250%; running until the sludge concentration in each reaction tank is less than 0.5 g/L; controlling DO of the first aerobic tank to be 2.5mg/L and the aeration intensity to be 3.5m3/(m2H) ammoxidation rate>50 percent, controlling DO of the second aerobic tank to be 6.0mg/L and the aeration intensity to be more than 6.5m3/(m2H), the ammoxidation rate is > 90%; the operation is carried out until the ammonia oxidation surface load of the first aerobic tank is 2.0 gN/(m)2D). Inoculating CANON suspension carrier into the first aerobic tank with inoculation rate of 5%, controlling DO in the first aerobic tank at 0.6mg/L and aeration intensity of 2.1m3/(m2H); the stirring devices of the first variable tank to the fourth variable tank are closed, the aeration device is opened, the DO is controlled to be 0.8mg/L, and the aeration intensity is 2.4m3/(m2H), opening a carbon source adding valve in the first anoxic tank, and closing the rest carbon source adding valves to ensure that water enters the first anoxic tankThe ratio of C to N was 4.5. The mixed liquid reflux pump is started, the reflux ratio is controlled to be 100 percent, the operation is carried out to 110d, and the surface load of TN removal of the first aerobic tank is 1.0 gN/(m)2D). Continuously feeding water, and running until the TN-removed surface load of the first variable pool to the fourth variable pool reaches 0.9 gN/(m)2D). Continuously feeding water, controlling DO in the first reaction tank and the first to fourth variable tanks to be 2.5mg/L and controlling aeration intensity to be 2.5m3/(m2H), running until the surface load of the first aerobic tank TN is removed by 2.7 gN/(m)2D), the surface load of the first to fourth variable cells TN removal reaches 1.6 gN/(m)2D). The effluent nitrous is relatively stable in the whole operation process, no large amount of accumulation is generated, and COD and BOD of the effluent are5、NH3、TN、NO2 -The average values were 41.52, 17.53, 3.14, 8.67, 2.17mg/L, respectively.
Example 3:
the designed water volume of a certain high ammonia nitrogen sewage treatment project is 1000m3D, COD, BOD of the influent water5、NH3、TN、NO2 -The design values are respectively 500, 240, 450 and 500mg/L, a CANON system based on MBBR and free of nitrous accumulation is adopted for treatment, the tank volume ratio of a first aerobic tank to a variable tank is 1:1.2, the tank volume ratio of the variable tank to the first anoxic tank is 1:1.0, the tank volume ratio of the first anoxic tank to the second aerobic tank is 1:1.0, and the variable tanks are divided into two groups.
Starting a preparation stage, adding suspension carriers (the filling rate is 60%) into each system, inoculating common activated sludge into each reaction tank until the sludge concentration in the reaction tank is 4.0 g/L; and in the short-distance nitrification starting stage, the inlet water of the system flows through the first aerobic tank, the first to second variable tanks, the first anoxic tank and the second aerobic tank respectively and is discharged through the main water discharge pipe. Controlling DO of the first aerobic tank to be 2.5mg/L and the aeration intensity to be 4.5m3/(m2H), controlling the DO of the first variable pool to be 3.0mg/L and the aeration intensity to be 4.5m3/(m2H), opening a stirring device in the second variable tank, closing an aeration device, controlling the stirring speed of the second variable tank to be 30-45r/min, opening a carbon source adding valve in the second variable tank, closing the rest carbon source adding valves, ensuring that the C/N of water fed into the second variable tank is 4-6, and controlling the stirring speed of the first anoxic tank to be 4-6The stirring speed is 45r/min, the DO of the second aerobic tank is controlled to be 5.0mg/L, and the aeration intensity is 5.5m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 100%; the operation is carried out until the sludge concentration in each reaction tank is 0.4 g/L; continuously feeding water to the aerobic pool and running the aerobic pool to 103 days, wherein the surface load of TN removed by the first aerobic pool is 0.9gN/(m2D). Continuously feeding water, and running until the surface load of TN removal of the first variable pool to the fourth variable pool is 0.9 gN/(m)2D). Continuously feeding water, controlling DO in the first reaction tank and the first to fourth variable tanks to be 2.0mg/L and controlling aeration intensity to be 3m3/(m2H), running until the surface load of the first aerobic tank TN is removed by 2.5 gN/(m)2D), the first to second variable cells TN remove the surface load 1.7 gN/(m)2D). The effluent nitrous is relatively stable in the whole operation process, no large amount of accumulation is generated, and COD and BOD of the effluent are5、NH3、TN、NO2 -The average values are 29.21, 18.20, 3.22, 8.17 and 1.59mg/L respectively.
Example 4:
design water volume of 5m for certain integrated equipment3D, COD, BOD of the influent water5、NH3TN and design values are respectively 340 mg/L, 160 mg/L, 650 mg/L and 700mg/L, a CANON system based on MBBR and free of nitrous accumulation is adopted for treatment, the tank volume ratio of the first aerobic tank to the variable tank is 1.0:1.0, the tank volume ratio of the variable tank to the first anoxic tank is 1.0:1.0, and the tank volume ratio of the first anoxic tank to the second aerobic tank is 1.0: 1.0. And in the preparation stage, suspension carriers (the filling rate is 55%) are added into each system, and each reaction tank is inoculated with common activated sludge, and system inlet water flows through the first aerobic tank, the first to third variable tanks, the first anoxic tank and the second aerobic tank respectively and is discharged through a main water discharge pipe. Controlling DO of the first variable pool to be 2.5mg/L and aeration intensity to be 3.0m3/(m2H), closing the aeration devices in the second variable tank and the third variable tank, opening the stirring device, controlling the stirring speed of the second variable tank and the third variable tank to be 45r/min, opening a carbon source adding valve in the second variable tank, closing the rest carbon source adding valves, ensuring that the C/N of the inlet water of the second variable tank is 5.0, controlling the stirring speed of the first anoxic tank to be 45r/min, controlling the DO of the second aerobic tank to be 5.0mg/L and the aeration intensity to be 6.0m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 200%; running until the sludge concentration in each reaction tank is less than 0.5 g/L; controlling DO of the first aerobic tank to be 2.5mg/L and the aeration intensity to be 3.5m3/(m2H), the ammonia oxidation rate is 52 percent, the DO of the second aerobic tank is controlled to be 6.0mg/L, and the aeration intensity is 6.5m3/(m2H), the ammoxidation rate was 88%; the operation is carried out until the ammonia oxidation surface load of the first aerobic tank is 2.0 gN/(m)2D). Inoculating CANON suspension carrier into the first aerobic tank with inoculation rate of 5%, controlling DO in the first aerobic tank at 0.7mg/L and aeration intensity of 2.2m3/(m2H); the stirring devices of the first variable tank and the third variable tank are closed, the aeration device is opened, DO is controlled to be 1.0mg/L, and the aeration intensity is 2.4m3/(m2H), opening a carbon source adding valve in the first anoxic tank, and closing the other carbon source adding valves to ensure that the C/N of the inlet water of the first anoxic tank is 5.0. The mixed liquid reflux pump is started, the reflux ratio is controlled to be 100 percent, the operation is carried out to 108d, and the surface load of TN removal of the first aerobic tank is 1.1 gN/(m)2D). Continuously feeding water, and running until the TN-removed surface load of the first variable pool to the third variable pool reaches 0.85 gN/(m)2D). Continuously feeding water, controlling DO in the first reaction tank and the first to third variable tanks to be 2.3mg/L and controlling the aeration intensity to be 2.4m3/(m2H), running until the surface load of the first aerobic tank TN is removed by 2.5 gN/(m)2D), the surface load of the first to third variable cells TN removal reaches 1.7 gN/(m)2D). The effluent nitrous is relatively stable in the whole operation process, no large amount of accumulation is generated, and COD and BOD of the effluent are5、NH3、TN、NO2 -The average values are 42.55, 9.25.25, 1.52, 7.66 and 0.59mg/L respectively.
In the description of the present invention, it is to be understood that the terms "center", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention.
The specific embodiments described herein are merely illustrative of the spirit of the invention. Various modifications or additions may be made to the described embodiments or alternatives may be employed by those skilled in the art without departing from the spirit or ambit of the invention as defined in the appended claims.

Claims (9)

1. The utility model provides a CANON system based on MBBR's no nitrous accumulation, includes that reaction tank, inlet tube, outlet pipe, carbon source throw with pipeline, aeration equipment and agitating unit, its characterized in that:
the reaction tank comprises a first aerobic tank, a variable tank, a first anoxic tank and a second aerobic tank, and system inlet water enters from the water inlet pipe, flows through the first aerobic tank, the variable tank, the first anoxic tank and the second aerobic tank respectively and is discharged through the water outlet pipe;
the ratio of the tank volume of the first aerobic tank to the tank volume of the variable tank is 1:0.5-1:2, the ratio of the tank volume of the variable tank to the tank volume of the first anoxic tank is 1:0.5-1:2, and the ratio of the tank volume of the first anoxic tank to the tank volume of the second aerobic tank is 1:0.5-1: 1;
the variable pool is used for playing a denitrification function by adjusting the operation mode of the variable pool in the system starting period and playing a CANON function by adjusting the operation mode of the variable pool in the stable operation period;
the carbon source adding pipeline is used for adding a carbon source into the variable tank and the first anoxic tank;
the aeration device is arranged in the first aerobic tank, the variable tank and the second aerobic tank;
the stirring device is arranged in the variable pool and the first anoxic pool.
2. The MBBR-based CANON system without accumulation of nitrous oxides according to claim 1, wherein: the variable pools are provided with 2-4 groups.
3. The MBBR-based CANON system without accumulation of nitrous oxides according to claim 1, wherein: the variable tanks are provided with four groups, a mixed liquid return pipe is arranged between the second aerobic tank and the first anoxic tank, and a mixed liquid return pump is arranged on the mixed liquid return pipe.
4. The MBBR-based CANON system without accumulation of nitrous oxides according to claim 3, wherein: the variable tanks are arranged in two rows and two columns and are respectively a first variable tank, a second variable tank, a third variable tank and a fourth variable tank, a carbon source feeding pipeline branch led out by the carbon source feeding pipeline is arranged in each variable tank, and a carbon source feeding valve is installed on the carbon source feeding pipeline branch.
5. The MBBR-based CANON system without accumulation of nitrous oxides according to claim 4, wherein: and a water passing port and an intercepting screen are arranged between the adjacent tank bodies in the flowing water direction of the system.
6. The MBBR-based CANON system without accumulation of nitrous oxides according to claim 5, wherein:
the water passing port comprises a first aerobic pool water passing port between a first aerobic pool and a first variable pool, a first variable pool water passing port between the first variable pool and a second variable pool, a second variable pool water passing port between the second variable pool and a third variable pool, a third variable pool water passing port between the third variable pool and a fourth variable pool, a fourth variable pool water passing port between the fourth variable pool and a first anoxic pool, a first anoxic pool water passing port between the first anoxic pool and a second aerobic pool water outlet;
the front ends of all the water outlets are provided with the intercepting screens, namely a first aerobic tank intercepting screen between a first aerobic tank and a first variable tank, a first variable tank intercepting screen between the first variable tank and a second variable tank, a second variable tank intercepting screen between the second variable tank and a third variable tank, a third variable tank intercepting screen between the third variable tank and a fourth variable tank, a fourth variable tank intercepting screen between the fourth variable tank and a first anoxic tank, a first anoxic tank intercepting screen between the first anoxic tank and a second aerobic tank intercepting screen at the water outlet of the second aerobic tank.
7. The MBBR-based CANON system without accumulation of nitrous oxides according to claim 6, wherein: the aeration device is an aeration pipe positioned at the bottom of the first aerobic tank, the first variable tank, the second variable tank, the third variable tank, the fourth variable tank and the second aerobic tank.
8. The MBBR-based CANON system without accumulation of nitrous oxides according to claim 7, wherein: the stirring device is a submersible stirrer positioned in the first variable pool, the second variable pool, the third variable pool, the fourth variable pool and the first anoxic pool.
9. The method of claim 4, comprising the following steps in sequence:
a. starting preparation, namely adding a suspension carrier into each reaction tank, wherein the filling rate is 20-67%; inoculating common activated sludge in each reaction tank, wherein the sludge concentration in each reaction tank is 3-5 g/L;
b. starting short-cut nitrification and denitrification, continuously feeding water, and discharging system inlet water through a water outlet pipe after the system inlet water flows through a first aerobic tank, a first variable tank, a second variable tank, a first anoxic tank and a second aerobic tank respectively;
if the ammonia nitrogen concentration of the inlet water is less than 200mg/L, controlling the DO of the first aerobic tank to be 1.0-2.0mg/L and the aeration intensity>2.0m3/(m2H), turning on the aeration devices in the first variable tank, the second variable tank, the third variable tank and the fourth variable tank, turning off the stirring device, controlling DO of each variable tank to be 2.0-6.0mg/L, and controlling the aeration intensity to be more than 2.5m3/(m2H), opening a carbon source adding valve of the first anoxic tank, and closing the other carbon source adding valves to ensure that the first anoxic tank entersC/N of water is 4-6, and a mixed liquid reflux pump is closed;
if the ammonia nitrogen concentration of the inlet water is 200-400mg/L, controlling the DO of the first aerobic tank to be 1.5-2.5mg/L and the aeration intensity>2.5m3/(m2H), turning on the aeration device in the first variable tank to the third variable tank, turning off the stirring device, controlling DO in the first variable tank to the third variable tank to be 2.0-6.0mg/L, and controlling the aeration intensity to be more than 3.0m3/(m2H), opening a stirring device in the fourth variable tank, closing an aeration device, controlling the stirring speed to be 30-45r/min, opening a carbon source adding valve in the fourth variable tank, closing the rest carbon source adding valves, ensuring that the C/N of water inlet of the fourth variable tank is 4-6, controlling the stirring speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and controlling the aeration intensity to be more than 5.0m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 50-100%;
if the ammonia nitrogen concentration of the inlet water is 400-600mg/L, controlling the DO of the first aerobic tank to be 2.0-3.0mg/L and the aeration intensity>3m3/(m2H), turning on the aeration devices in the first variable tank and the second variable tank, turning off the stirring device, controlling DO of the first variable tank and the second variable tank to be 2.0-6.0mg/L, and controlling the aeration intensity to be more than 4.5m3/(m2H), the stirring devices in the third variable tank and the fourth variable tank are opened, the aeration device is closed, the stirring rotating speed of the third variable tank and the fourth variable tank is controlled to be 30-45r/min, a carbon source adding valve in the third variable tank is opened, the other carbon source adding valves are closed, the C/N of the inlet water of the third variable tank is ensured to be 4-6, the stirring rotating speed of the first anoxic tank is controlled to be 30-45r/min, the DO of the second aerobic tank is controlled to be 4.0-7.0mg/L, the aeration intensity is more than 5.0m3/(m2H), starting a mixed liquid reflux pump to ensure that the reflux ratio of the mixed liquid is 100-150%;
if the ammonia nitrogen concentration of the inlet water is 600-800mg/L, controlling the DO of the first aerobic tank to be 2.5-3.5mg/L and the aeration intensity>3.5m3/(m2H), turning on the aeration device in the first variable tank, turning off the stirring device, and controlling the DO in the first variable tank to be 2.0-6.0mg/L and the aeration intensity to be more than 3.0m3/(m2H) turning off the aeration devices in the second to fourth variable tanks and turning on the stirring devicesStarting the system, controlling the stirring speed of the second variable tank to the fourth variable tank to be 30-45r/min, opening a carbon source adding valve in the second variable tank, closing the rest carbon source adding valves, ensuring that the C/N of water inlet of the second variable tank is 4-6, controlling the stirring speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and controlling the aeration intensity to be more than 6.0m3/(m2H), starting a mixed liquid reflux pump to ensure that the reflux ratio of the mixed liquid is 200-250%;
if the ammonia nitrogen concentration of the inlet water is more than 800mg/L, controlling the DO of the first aerobic tank to be 3.0-4.0mg/L and the aeration intensity>3.5m3/(m2H), closing the aeration devices in the first to fourth variable tanks, opening the stirring device, variably controlling the stirring rotating speed to be 30-45r/min from the first to fourth variable tanks, opening a carbon source adding valve in the first variable tank, closing the rest carbon source adding valves, ensuring that the C/N of the inlet water of the first variable tank is 4-6, controlling the stirring rotating speed of the first anoxic tank to be 30-45r/min, controlling the DO of the second aerobic tank to be 4.0-7.0mg/L, and ensuring that the aeration intensity is more than 6.0m3/(m2H), starting a mixed liquid reflux pump to enable the reflux ratio of the mixed liquid to be 300%; controlling DO of the first aerobic tank to be 3-6mg/L and controlling the aeration intensity>3.5m3/(m2H) ammoxidation rate>50 percent, controlling DO of the second aerobic tank to be 4.0-7.0mg/L and the aeration intensity to be more than 6.0m3/(m2H), the ammoxidation rate is > 90%;
the sludge concentration in each reaction tank is less than 0.5 g/L; continuously feeding water, and running until the ammonia oxidation surface load of the first aerobic tank>1.5gN/(m2D), go to the next step;
c. starting autotrophic denitrification inoculation, inoculating the CANON suspension carrier into the first aerobic tank, wherein the inoculation rate is 3-5%, DO in the first aerobic tank is controlled to be 0.5-1.5mg/L, and the aeration intensity is controlled>2m3/(m2H); the stirring devices of the first variable tank to the fourth variable tank are closed, the aeration device is opened, DO is controlled to be 0.5-1.5mg/L, and the aeration intensity is more than 2m3/(m2H), opening a carbon source adding valve in the first anoxic tank, closing the other carbon source adding valves to ensure that the C/N of the water inlet of the first anoxic tank is 4-6, opening a mixed liquid reflux pump, controlling the reflux ratio to be 100%, and running until the surface load of TN of the first aerobic tank is removed>0.8gN/(m2D), go to the next step;
d. the autotrophic nitrogen removal load is lifted, water is continuously fed, and the operation is carried out until the TN from the first variable tank to the fourth variable tank removes the surface load>0.8gN/(m2D), go to the next step;
e. the autotrophic nitrogen removal runs stably, water is continuously fed, DO of the first reaction tank and the first to fourth variable tanks is controlled to be 2.0-5.0mg/L, and the aeration intensity is controlled>2m3/(m2H), running until the surface load of the first aerobic tank TN is removed>2.5gN/(m2D) the first to fourth variable cells TN remove the surface load>1.5gN/(m2·d)。
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