CN109354172A - A kind of quick start method of the CANON system based on MBBR - Google Patents

A kind of quick start method of the CANON system based on MBBR Download PDF

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CN109354172A
CN109354172A CN201811477775.2A CN201811477775A CN109354172A CN 109354172 A CN109354172 A CN 109354172A CN 201811477775 A CN201811477775 A CN 201811477775A CN 109354172 A CN109354172 A CN 109354172A
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reactor
control valve
mode
collector pipe
control
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CN109354172B (en
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吴迪
周家中
管勇杰
韩文杰
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Qingdao Si Purun Water Treatment Limited-Liability Co
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Qingdao Si Purun Water Treatment Limited-Liability Co
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Priority to PCT/CN2019/079822 priority patent/WO2020113861A1/en
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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
    • C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • 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
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/22—O2
    • 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
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

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  • Life Sciences & Earth Sciences (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
  • Biological Treatment Of Waste Water (AREA)

Abstract

The quick start method for the CANON system based on MBBR that the invention discloses a kind of, belongs to bio-denitrification technology field.The technical problems such as big, slow, low, fluctuation of service of load of starting which solve inoculum concentrations in the prior art.For the present invention by the way that agent set to be averagely split as to two same reactors and is connected in series, each reactor is independently installed agitating device, aerator, attachment device, and adds suspending carrier in each reactor.By the control of valve between reactor, it can be achieved that five kinds of operational modes, respectively series connection SBR operational mode, series operation mode A, series operation B-mode, series operation C mode, series operation D mode.In starting operation CANON technical process, according to the demand for control of different phase, different operational modes can be used.The present invention runs CANON technique, has many advantages, such as that inoculum concentration is low, the starting time is fast, operation total nitrogen load is high, stable.

Description

A kind of quick start method of the CANON system based on MBBR
Technical field
The invention belongs to bio-denitrification technology fields, and in particular to a kind of quick start of the CANON system based on MBBR Method.
Background technique
CANON technique (Completely Autotrophic Nitrogen Removal Over Nitrite, CANON), i.e., Full Autotrophic Ammonium Removal Process, the technique are to collect short distance nitration process to react with anaerobic ammonium oxidation process in same The process that denitrogenation is completed in device, is presently the most simple and direct, economic biological denitrification process.CANON technique based on MBBR, be Under aerobic condition, the biomembrane of suspending carrier outer layer is using oxygen by ammonia nitrogen partial oxidation at sub- nitrogen, the sub- nitrogen of generation and part Remaining ammonia nitrogen occurs Anammox reaction in the internal layer of suspending carrier and generates nitrogen.Also, after using MBBR technique, in phase To take up an area under same loading condiction and saves, microorganism is attached on suspending carrier and is fluidized in water using aeration or the disturbance stirred, And come into full contact with polluter, achieve the purpose that pollutant efficiently removes.
Two class functional microorganism ammonia oxidation bacterias (AOB) and anaerobic ammonia oxidizing bacteria (AnAOB) in CANON reactor belong to Autotrophic bacterium, the doubling time is long, and especially AnAOB is easy to run off, and being not easy enrichment causes the autotrophic denitrification technique starting time long.2002 Year, first productive anaerobic ammonia oxidation process completes for use in Rotterdam, NED sewage plant in the world, and single starting is just time-consuming Up to 3 years time.So how in engineering quick start autotrophic denitrification technique become solve the technique large-scale application Key.In addition, AOB and AnAOB will form the competition process of ecological niche, longtime running CANON process, meeting on suspending carrier Cause strain out of proportion, the abundance of AOB can fail, and the deficiency of sub- nitrogen will limit the promotion and system of system total nitrogen load Stable operation, so guaranteeing the abundance of AOB on suspending carrier, ensureing has enough sub- nitrogen in Anammox reaction process Be known as the technique can stable operation key.
The prior art has the research report of related fields mainly to have:
106277357 A of CN discloses the autotrophic denitrification system starting that a kind of floc sludge and granule sludge coexist and high Operation method is imitated, wherein reactor floc sludge of the inoculation with short distance nitration function and with Anammox function The mass ratio of grain sludge, floc sludge and granule sludge is water inlet with water distribution 2~3, and intermittent aerating is gradually converted into continuous exposure Gas starts CANON technique；Used time 45d successfully starts up the CANON reactor that the scale of construction is 4L.But the seed sludge of the patent is Mature AOB and AnAOB, is required to cultivate early period.To start 200m3Reactor for, maturation is needed using this method AOB dry weight about 152kg, mature AnAOB dry weight about 74kg, inoculum concentration is excessive, it is clear that is not suitable for the inoculation of project scale Starting；Also, it not can solve activated sludge process bring anaerobic ammonia oxidizing bacteria and be not easy the problem of being enriched with；
Li Huibo, Wang Yinshuan, (China gives fourth Juan etc. " starting and operation of ANITA Mox autotrophic denitrification MBBR reactor " Water draining, 2014,30 (5): 1-5.), CANON process anaerobic sludge digestive juice is started using inocalation method；Inoculation, which suspends, to be carried The gross area of body is than 3% starting 50m3Reactor, by 120d operation (without short distance nitration start), the highest ammonia of system Oxidation volumetric loading reaches 1.2kg/m3/ d, 0.7~1.1kg/m of ammoxidation volumetric loading operating load of stationary phase3/ d, fluctuation It is larger；Although using MBBR runs CANON technique, relevant control mode still uses the control of activated sludge process, fails needle Biomembrane process is adjusted, and in this way, longtime running, the AOB function bacterium of system is gradually lost, and system bacterium colony is difficult to Stablize；During biofilm, AOB and AnAOB also forms the competition of ecological niche, and AnAOB occupies advantage, AOB in low DO It is gradually eliminated in systems, system is finally difficult to stable operation, and specific aim method is needed to be resolved, and realizes CANON-MBBR Stable operation, find out the control mode for meeting biomembrane process, in conjunction with DO control and hydraulic shear, guarantee at AOB and AnAOB In equilibrium state, it is unlikely to longtime running loss of stability；
108408892 A of CN disclose a kind of suspending carrier immobilization anaerobic ammonia oxidizing bacteria membrane bioreactor and its Sewage treatment process, using the membrane bioreactor of suspending carrier immobilization anaerobic ammonia oxidizing bacteria, suspending carrier layer is to take stone, nothing Woven fabric, polyethylene or polyurethane are equipped with anaerobic ammonia oxidizing bacteria in suspending carrier layer.Total nitrogen volumetric loading is not in actual moving process More than 1.0kgN/m3/d.It uses fixed biofilm technology, and total nitrogen load is lower, and is transported using the fixed biofilm technology later period Row has the risk of blocking, needs periodically to backwash, operation expense is higher.
In conclusion although research of the prior art in terms of relevant apparatus and process operation achieves certain progress, But undeniable is that there is also many defects.Existing research is chiefly used in lab scale, and water inlet is mostly water distribution, the inoculation of use Large percentage, reproducibility is not high in engineering, and mostly runs referring to activated sludge process, does not propose specific aim for biomembrane process Solution, and the total nitrogen load in engineering is not high, operation is complicated, and total nitrogen load fluctuates larger, the later period in operational process Operation expense is higher.
Summary of the invention
To solve above-mentioned technological deficiency existing in the prior art, the invention proposes a kind of CANON system based on MBBR The quick start method of system controls reactor series, parallel, continuous operation, intermittent duty by attachment device, by being inoculated with, Alternately the mode of switchover operation realizes the quick start and stable operation of autotrophic denitrification technique.It, can according to processing standard requirements Realize that different technology arrangement forms, the present invention have many advantages, such as that inoculative proportion is small, starting is fast, total nitrogen load is high, stable.
To achieve the goals above, the required technical problem overcome is:
How in limited provenance, inoculative proportion is reduced, the autotrophy deamination technique starting of project scale is realized, leads to It crosses the forms such as control aeration, stirring, different operational modes and realizes the quick start of autotrophic denitrification system, and reach higher total Nitrogen load；How different technology arrangement form realized by the connection of control valve, collector pipe, to reach different processing marks It is quasi-；How by the control of operational mode, guarantee the equiblibrium mass distribution of major function bacterium on suspending carrier in each reactor, guarantees There is sufficient sub- nitrogen to react in system for Anammox, to guarantee that system is run steadily in the long term.
Its technical solution includes:
A kind of quick start method of the CANON system based on MBBR, the CANON system include reaction tank main body, Agitating device, aerator and attachment device, the reaction tank main body include identical two reactors of specification, and respectively One reactor and second reactor, the first reactor and second reactor are arranged side by side；
The upper side of first reactor far from second reactor is provided with the first control valve, side-lower is provided with the tenth Two control valves bottom-up are disposed with the second control valve, the 6th in the side of the first reactor close to second reactor Control valve, the 7th control valve and the 8th control valve；The upper side of second reactor far from first reactor is provided with the 5th Control valve, side-lower are provided with the 13rd control valve, close to first reactor second reactor side it is bottom-up according to It is secondary to be provided with third control valve, the 11st control valve, the tenth control valve and the 9th control valve；
The junction of each control valve and reactor is provided with interception sieve；
An agitating device is respectively provided in each reactor；
The aerator is distributed in each reactor, and has added suspending carrier in each reactor；
The attachment device is catchmented including the first collector pipe, the second collector pipe, third collector pipe, the 4th collector pipe and the 5th Pipe；Second control valve, the 6th control valve, the 7th control valve and the 8th control valve are connected to one by first collector pipe It rises, third control valve, the 11st control valve, the tenth control valve and the 9th control valve are connected to one by second collector pipe It rises, the bottom of first collector pipe and the second collector pipe is connected with third collector pipe, the third collector pipe center 4th control valve is set, and the 4th collector pipe links together first control valve and the 12nd control valve, described 5th collector pipe links together the 5th control valve and the 13rd control valve；
The starting method successively the following steps are included:
A, starting prepares, and each reactor adds suspending carrier, filling rate 20%~67%, is inoculated with aerobic sludge, control the 5~8g/L of sludge concentration in one reactor, second reactor；
B, nitrosation starts, and using SBR operational mode in parallel, the first reactor and second reactor are to close side by side System, each reactor is independently intake, is independently discharged, and intermittent water inflow, intermittent drainage, changes water ratio by control related valves control, So that waste water is by third collector pipe through the 4th control valve discharge system；Control the initial DO of first reactor, second reactor In 2~5mg/L, aeration intensity > 7m3/m2/ h, ammonia oxidation rate > 50%, system initial precipitation time 30min, it is heavy to gradually reduce It forms sediment the time, makes amplitude < 25% that sludge concentration reduces in each periodic reaction device；It runs up to sludge concentration < 0.5g/L, and ammonia Oxidized surface load > 2gN/m2/ d, sub- nitrogen accumulation rate > 0.95, into next step；
C, CANON inoculation starting, using series operation mode A, the first reactor and second reactor series operation, Continuous flow operation, waste water to be processed enter first reactor through the 12nd control valve, by controlling related valves, so that the first reaction The water outlet of device enters second reactor, most afterwards through the 5th control valve discharge system；It suspends and carries to first reactor inoculation CANON Body, rate of vaccination are 3%~5%, control DO in 0.3~2.0mg/L, aeration intensity > 1.0m3/m2/ h, 15~30r/ of speed of agitator Min, ammonia oxidation rate > 80%；Second reactor controls DO in 0.5~1.0mg/L, aeration intensity > 1m3/m2/ h, speed of agitator 15 ~30r/min, as first reactor Asia nitrogen concentration < 8mg/L, system is switched to series operation B-mode, the first reactor With second reactor series operation, waste water to be processed enters second reactor through the 13rd control valve, by controlling related valves, makes The water outlet for obtaining second reactor enters first reactor, most afterwards through the first control valve discharge system；Control the DO of first reactor In 0.3~2.0mg/L, aeration intensity > 1.0m3/m2/ h, 15~30r/min of speed of agitator, ammonia oxidation rate > 80%, the second reaction Device controls DO in 0.5~1.0mg/L, aeration intensity > 1m3/m2/ h, 15~30r/min of speed of agitator, until first reactor system System is switched to series operation mode A after the nitrogen concentration>15mg/L of Asia in uniting, and as first reactor Asia nitrogen concentration<8mg/L, is System is switched to series operation B-mode, successively alternately；Total nitrogen surface loading > 1.6gN/m of the operation up to first reactor2/ D, into next step；
D, CANON expands starting: in first reactor and second reactor 40%~60% suspending carrier is set It changes, using series operation C mode, specific steps are as follows: the first reactor and second reactor series operation, a part of waste water Through the 12nd control valve into people's first reactor, by controlling related valves, so that the water outlet of first reactor enters the second reaction Device, remaining waste water enter second reactor by related valves control through the 4th control valve, and second reactor water outlet is through the 5th control Valve discharge system；The DO for controlling first reactor and second reactor is 1.0~3.0mg/L, aeration intensity > 3m3/m2/ h, stirring 15~30r/min of revolving speed, ammonia oxidation rate > 80%, when nitrogen concentration sub- in second reactor system is Asia in first reactor system At 2~3 times of nitrogen concentration, it is switched to series operation D mode, specific steps are as follows: the first reactor and second reactor string Through transport row, a part of waste water through the 13rd control valve into people's second reactor, by controlling related valves, so that second reactor Water outlet enters first reactor, and remaining waste water enters first reactor, the first reaction by related valves control through the 4th control valve Device is discharged through the first control valve discharge system；The DO for controlling first reactor and second reactor is 1.0~3.0mg/L, aeration Intensity > 3m3/m2/ h, 15~30r/min of speed of agitator, ammonia oxidation rate > 80%, when nitrogen concentration sub- in first reactor system is the It is switched to series operation C mode when 2~3 times of sub- nitrogen concentration in two reactor assemblies, successively alternately；Operation is until first Reactor and the total nitrogen surface loading of second reactor it is equal > 2.0gN/m2/ d, into next step；
E, CANON stable operation: if require < 80% to ammonia nitrogen removal frank, using the series operation C mode and The mode of the series operation D mode alternate run, first reactor and second reactor control DO in 1.0~3.0mg/L, Aeration intensity > 5m3/m2/ h, 30~50r/min of speed of agitator control the series operation C mode and the series connection respectively The runing time for running D mode, using series operation C mode, when nitrogen concentration sub- in second reactor system is first reactor When 2~3 times of sub- nitrogen concentration in system, it is switched to series operation D mode, when nitrogen concentration sub- in first reactor system is second When 2~3 times of sub- nitrogen concentration in reactor assembly, it is switched to series operation C mode, successively alternate run, guarantees the first reaction Device and the total nitrogen surface loading of second reactor difference < 20%；When requiring water outlet ammonia nitrogen lower than 50mg/L, using the string Through transport row mode A, the DO for controlling first reactor are exposed in 2.0~4.0mg/L, the DO of second reactor in 2.0~3.0mg/L Gas intensity is equal > 5m3/m2/ h, 30~50r/min of speed of agitator, when the total nitrogen surface loading of first reactor is that second reactor is total When nitrogen surface loading 1.3~2.5, system is switched to series operation B-mode, controls the DO of first reactor in 2.0~3.0mg/ L, the DO of second reactor are in 2.0~4.0mg/L, and aeration intensity is equal > 5m3/m2/ h, 30~50r/min of speed of agitator, until the The total nitrogen surface loading of two reactors is the 1.3~2.5 of first reactor total nitrogen surface loading, is then switched to series operation again Mode A, successively alternately.
The direct bring advantageous effects of above-mentioned technical proposal are as follows:
Pass through two reactors of setting and limits its connection relationship, it can be achieved that different operational mode, passes through different operations The switching of mode realizes the CANON technique for project scale, and rate of vaccination is low, and the starting time is short；Ensure that system is steady for a long time Fixed operation improves the situation of system operation later period Asia nitrogen hunger；Using the CANON technique based on MBBR, sustainable upgrading Ability is strong, is controlled by reasonable filling rate, and the total nitrogen volumetric loading of system can be made to reach 1.6kgN/m3/d。
As a preferred solution of the present invention, water inlet or treatment sewage, C/N≤1；The first reactor and second The power of agitator of reactor is respectively 15~60W/m3。
As another preferred embodiment of the invention, the step c) in e), in each reaction chamber sludge concentration < 0.5g/L；When system is using series connection C operational mode, the sewage into second reactor is the 10%~50% of total inflow, The total nitrogen surface loading of second reactor is set to be not less than the 30% of first reactor；When system is using series connection D operational mode, into The sewage for entering first reactor is the 10%~50% of total inflow, makes the total nitrogen surface loading of first reactor not less than second The 30% of reactor.
Further, the aerator in each reactor is made of multiple groups boring aeration and micro-pore aeration.
Further, the SBR operational mode specific steps in parallel are as follows: 50% waste water is by the 4th collector pipe through first Control valve enters first reactor, and water outlet is by the second control valve, the 6th control valve, the 7th control valve through the first collector pipe, the Three collector pipes are realized by the 4th control valve discharge system by the second control valve of control, the 6th control valve, the 7th control valve Different changes water ratio；Remaining waste water enters second reactor through the 5th control valve by the 5th collector pipe, and water outlet passes through third control Valve processed, the 11st control valve, the tenth control valve are led to through the second collector pipe, third collector pipe by the 4th control valve discharge system Cross control third control valve, the 11st control valve, the tenth control valve are realized and different change water ratio.
Further, series operation mode A specific steps are as follows: waste water enters first reactor through the 12nd control valve, the The water outlet of one reactor enters second reactor through the 8th control valve, the first collector pipe, third collector pipe, third control valve, and second Reactor is discharged through the 5th control valve, the 5th collector pipe discharge system.
Further, series operation B-mode specific steps are as follows: waste water enters second reactor through the 13rd control valve, the The water outlet of two reactors enters first reactor through the 9th control valve, the second collector pipe, third collector pipe, the second control valve, and first Reactor is discharged through the first control valve, the 4th collector pipe discharge system.
Further, series operation C mode specific steps are as follows: effluent part enters the first reaction through the 12nd control valve Device, first reactor water outlet enter second reactor through the 8th control valve, the first collector pipe, third collector pipe, third control valve, Remaining waste water enters second reactor through the 4th control valve, third collector pipe, third control valve, and second reactor is discharged through the 5th Control valve, the 5th collector pipe discharge system.
Further, series operation D mode specific steps are as follows: effluent part enters the second reaction through the 13rd control valve Device, second reactor water outlet enter first reactor through the 9th control valve, the second collector pipe, third collector pipe, the second control valve, Remaining waste water enters first reactor through the 4th control valve, third collector pipe, the second control valve, and first reactor is discharged through first Control valve, the 4th collector pipe discharge system.
Compared with prior art, present invention offers following advantageous effects:
1) CANON technique is started using inocalation method, rate of vaccination is low, 250m3The water of/d only needs inoculation 3m3Mature CANON Suspending carrier can start, and the CANON suitable for project scale starts；
2) using present invention starting CANON technique, the starting time is short, for the starting of project scale, can open within about 4 months It moves and successfully (starts containing short distance nitration), make system total nitrogen surface loading > 2gN/m2/d；
3) present invention is controlled using different operational modes, can eliminate limitation of the sub- nitrogen to total nitrogen surface loading, always Nitrogen surface loading is up to 3gN/m2/ d or more；
4) present invention is by the switching without operational mode, during stable operation, it is ensured that filled with abundance in system Sub- nitrogen is reacted for Anammox, has ensured the operation steady in a long-term of system, has solved the load that later period AOB deficiency is likely to occur The risk that fluctuation even reduces.
5) present invention is controlled using different operational modes, can meet the requirements of engineering, such as total nitrogen surface loading (land occupation saves), water outlet ammonia nitrogen concentration (low ammonia nitrogen) control etc.；
6) the CANON technique based on MBBR can reach different treatment effects by different filling rates, and system is maximum Volumetric loading is up to 1.6kgN/m3/ d, land occupation save；
7) present invention process mode operation is used, control is simple, it can realize that different operational modes switches by automatic control, with And fluidize and be aerated reasonable balance, high degree of automation；
8) using present invention process completely without outer throwing organic carbon source, in addition, there are a small amount of organic matters in water inlet The further removal of meeting promotion system total nitrogen.
Detailed description of the invention
The present invention will be further described with reference to the accompanying drawing:
Fig. 1 is the top view of present system；
Fig. 2 is the longitudinal sectional drawing of present system；
In figure, R1, first reactor；R2, second reactor；The agitating device of S1, first reactor；S2 second reactor Agitating device；L1-L13,13 control valve of the first control valve-the；C1-C5, first the-the five collector pipe of collector pipe.
Specific embodiment
The quick start method for the CANON system based on MBBR that the invention discloses a kind of, in order to make advantages of the present invention, Technical solution is clearer, clear, elaborates combined with specific embodiments below to the present invention.
Firstly, being explained as follows to relevant technical terms involved in the present invention:
1) MBBR: i.e. moving bed biofilm reactor (Moving Bed Biofilm Reactor, MBBR), this method is By adding a certain number of suspending carriers into reactor, biomass and biological species in reactor are improved, to improve The treatment effeciency of reactor；
2) suspending carrier, specific gravity are filled out in 0.93-0.97, voidage > 90%, also referred to as floating stuffing, abbreviation carrier Material；
3) filling rate: suspending carrier filling rate, the i.e. ratio of the volume of suspending carrier and filling region pool capacity, suspending carrier Volume be natural packing under total volume；Such as 100m3Suspending carrier, filling to 400m3Pool capacity, filling rate 25%；
4) specific gravity: the density ratio that suspending vehicle density and room temperature are lauched；
5) voidage: between suspending carrier and suspending carrier and the volume of suspending carrier intermediate gaps and suspending carrier are natural The ratio between other side's volume；
6) fluidize: suspending carrier is in a liquid with water flow flowing and water pollutant under the active force for being aerated or stirring The state that matter comes into full contact with；
7) effective ratio area: effective ratio area is often referred to the internal surface area of suspending carrier, the i.e. suspension of unit volume Effective surface area possessed by carrier.Effective ratio area=effective surface area ÷ volume, unit m2/m3.Such as effective specific surface Product is 800m2/m3, refer to 1m3The effective surface area of suspending carrier be 800m2；
8) surface loading: the amount for the pollutant that suspending carrier unit area removes daily, gN/m2/d；
9) ammoxidation surface loading: the amount for the ammonia nitrogen that suspending carrier unit area removes daily, gN/m2/ d, if water inlet ammonia Nitrogen concentration 400mg/L is discharged ammonia nitrogen concentration 100mg/L, flow 100m3/ d, suspending carrier total surface area 15000m2, then ammoxidation Surface loading is (400-100) × 100/15000=2gN/m2/d；
10) total nitrogen surface loading: the amount for the total nitrogen that suspending carrier unit area removes daily, gN/m2/d；
11) ammonia oxidation rate: the removal amount of ammonia nitrogen accounts for the ratio of influent ammonia nitrogen.If influent ammonia nitrogen is 400mg/L, removal amount is 350mg/L, then ammonia oxidation rate is 0.875 or 87.5%；
12) nitrosation: microorganism is by ammonia nitrogen (NH4 +) it is oxidized to nitrite nitrogen (NO2 -), without being further oxidized to Nitrate nitrogen (NO3 -) process, i.e., enriching ammonia oxidation bacteria (AOB) in system, and eliminate nitrite oxidizing bacteria (NOB)；
13) sub- nitrogen accumulation rate: the sum of nitrite nitrogen and nitrate nitrogen of the nitrite nitrogen and generation that are generated in reaction Ratio.It is 100mg/L as generated nitrite nitrogen in reaction process, generates nitrate nitrogen 2mg/L, then sub- nitrogen accumulation rate is 100/ (100+2)=0.98；
14) CANON technique: i.e. Full Autotrophic Ammonium Removal Process, the technique refer to and lead in single reactor or biomembrane It crosses control dissolved oxygen and realizes nitrosation and Anammox, to achieve the purpose that denitrogenation.Under aerobic condition, ammonia oxidation bacteria will Ammonia nitrogen partial oxidation occurs Anammox with the ammonia nitrogen of some residual and reacts life at nitrite nitrogen, the nitrite nitrogen of generation At nitrogen；
15) CANON suspending carrier: the suspending carrier of i.e. existing CANON effect, AOB and AnAOB divide in a manner of biomembrane Layer exists；
16) rate of vaccination: the CANON suspending carrier of inoculation accounts for the percentage of total suspending carrier, %.Such as to 50m3Suspension carry Body is vaccinated with 2m3Mature CANON suspending carrier, then rate of vaccination be 4%；
17) aeration intensity: refer to the aeration quantity of unit floor space, unit m3/m2/h.Aeration quantity refers to total aeration quantity, including micro- Hole aeration and boring aeration.Such as reactor floor space 10m2, total aeration quantity 30m3/ h, then aeration intensity is 3m3/m2/h；
18) C/N ratio: refer to BOD in waste water5Concentration and kelvin nitrogen concentration ratio；
19) power of agitator: the i.e. power number of unit basin's effective volume, W/m3；Activated sludge process is usually 3-5W/m3；MBBR In, power of agitator is related to filling rate, and filling rate is higher, and power of agitator is bigger；
20) aerobic sludge: referring in sewage treatment plant that aerobic tank goes out water mixed liquid is excess sludge after sedimentation in secondary sedimentation tank；
21) change water ratio: using SBR technique, the water replaced in each periodic system accounts for the ratio of total Water, such as 100m3 Dischargeable capacity, replaced 50m3Water, then change water ratio be 0.5.
For known to industry professional, intake C/N > 1 when, decarburization pretreating process can be increased and met the requirements.
Following first reactor abbreviation R1, second reactor abbreviation R2,13 control valve abbreviation L1- of the first control valve-the L13, first the-the five collector pipe abbreviation of collector pipe C1-C5.
The first, a kind of CANON system based on MBBR of the present invention in conjunction with described in Fig. 1 and Fig. 2, including is reacted tank main body, is stirred Device, aerator and attachment device are mixed, wherein reaction tank main body includes identical two reactors of specification, respectively first is anti- Answer device R1 and second reactor R2, first reactor and second reactor are arranged side by side, and therebetween by related valve and Collector pipe connection, the location arrangements and connection type of related valve and collector pipe are；
The upper side of first reactor far from second reactor is provided with the first control valve L1, side-lower is provided with ten Two control valve L12 are successively arranged the second control valve L2, the the side of the first reactor close to second reactor is bottom-up Six control valve L6, the 7th control valve L7 and the 8th control valve L8；It is set in the upper side of the second reactor far from first reactor It is equipped with the 5th control valve L5, side-lower is provided with the 13rd control valve L13, one of the second reactor close to first reactor Side is bottom-up to be successively arranged third control valve L3, the 11st control valve L11, the tenth control valve L10 and the 9th control valve L9；
Above-mentioned attachment device includes more collector pipes, respectively the first collector pipe C1, the second collector pipe C2 and third collection Water pipe C3, the 4th collector pipe C4 and the 5th collector pipe C5；First collector pipe controls the second control valve, the 6th control valve, the 7th Valve and the 8th control valve link together, and the second collector pipe is by third control valve, the 11st control valve, the tenth control valve and the 9th Control valve links together, and the bottom of the first collector pipe and the second collector pipe is connected with third collector pipe, and the 4th control valve is located at The center of the third collector pipe, the 4th collector pipe link together first control valve and the 12nd control valve, 5th collector pipe links together the 5th control valve and the 13rd control valve；
The present invention is equipped with agitating device, first reactor as shown in the figure in first reactor and second reactor Agitating device S1 and second reactor agitating device S2, the structure of specific agitating device uses for reference the prior art and can be realized, It is no longer discussed in detail herein.
In addition, the aerator in the present invention, the aerator in preferably each reactor is by multiple groups boring aeration Pipe and multiple microporous aeration discs composition.Suspending carrier is added in each reactor, filling rate is 20%~67%；And it is each The control valve of reactor and the junction of reactor are respectively provided with interception sieve, to intercept suspending carrier；
By above-mentioned control valve and collector pipe, it can be achieved that a variety of water inlets and water side of first reactor and second reactor Plurality of operating modes can be realized in formula.
The second, main explanation is done to operational process of the invention below with reference to above system:
Operational process has following five kinds of control models:
1) parallel connection SBR operational mode: 50% waste water enters R1 through L1 by C4, and R1 water outlet passes through control valve L2, L6, L7, Through C1 and C3, by L3 discharge system, is realized by controlling L2, L6, L7 and different change water ratio；Remaining waste water is entered by C5 through L5 R2, R2 water outlet are realized different by L10, L11, L13, through C2 and C3 by L4 discharge system by control L10, L11, L13 Change water ratio；
2) series operation mode A: waste water enters R1 through L12, and R1 water outlet enters R2 through L8, C1, C3, L3, and R2 water outlet passes through L5, C5 discharge system；
3) series operation B-mode: waste water enters R2 through L13, and R2 water outlet enters R1 by L9, C2, C3, L2, and R1 water outlet is logical Cross L1, C4 discharge system；
4) series operation C mode: effluent part enters R1 through L12, and R1 water outlet enters R2 through L8, C1, C3, L3, remaining Waste water enters R2 through L4, C3, L3, and R2 water outlet passes through L5, C5 discharge system；
5) series operation D mode: effluent part enters R2 through L13, and R2 water outlet enters R1 through L9, C2, C3, L2, remaining Waste water enters R1 through L4, C3, L2, and R1 water outlet passes through L1, C4 discharge system.
Third, starting method of the present invention, comprising the following steps:
1) starting prepares, and each reactor adds suspending carrier, filling rate 20%~67%, is inoculated with aerobic sludge, control R1, 5~8g/L of sludge concentration in R2；
2) nitrosation starts, and using SBR operational mode in parallel, controls the initial DO of R1 and R2 in 2~5mg/L, and aeration intensity > 7m3/m2/ h, ammonia oxidation rate > 50%, system initial precipitation time 30min gradually reduce the sedimentation time, make each periodic reaction device Amplitude<25% that interior sludge concentration reduces is run up to sludge concentration<0.5g/L, and ammoxidation surface loading>2gN/m2/ d, Sub- nitrogen accumulation rate > 0.95 enters in next step；
3) CANON inoculation starting is inoculated with CANON suspending carrier to R1 using series operation mode A, and rate of vaccination is 3%~ 5%, DO is controlled in 0.3~2.0mg/L, aeration intensity > 1.0m3/m2/ h, 15~30r/min of speed of agitator, ammonia oxidation rate > 80%；R2 controls DO in 0.5~1.0mg/L, aeration intensity > 1m3/m2/ h, 15~30r/min of speed of agitator, when the Asia R1 nitrogen concentration When<8mg/L, system is switched to series operation B-mode, controls the DO of R1 in 0.3~2.0mg/L, aeration intensity>1.0m3/m2/ h, 15~30r/min of speed of agitator, ammonia oxidation rate > 80%, R2 control DO in 0.5~1.0mg/L, aeration intensity > 1m3/m2/ h, is stirred 15~30r/min of revolving speed is mixed, until system is switched to series operation mode A after the nitrogen concentration > 15mg/L of Asia in R1 system, when the Asia R1 When nitrogen concentration<8mg/L, system is switched to series operation B-mode, successively alternately, operation until R1 total nitrogen surface loading> 1.6gN/m2/ d, into next step；
4) CANON expands starting: in R1 and R2 40%~60% suspending carrier being replaced, using series operation C Mode controls the DO of R1 and R2 in 1.0~3.0mg/L, aeration intensity > 3m3/m2/ h, 15~30r/min of speed of agitator, ammoxidation Rate > 80% is switched to series operation D mode, controls when nitrogen concentration sub- in R2 system is 2~3 times of sub- nitrogen concentration in R1 system The DO of R1 and R2 processed are in 1.0~3.0mg/L, aeration intensity > 3m3/m2/ h, 15~30r/min of speed of agitator, ammonia oxidation rate > 80%, it is switched to series operation C mode when nitrogen concentration sub- in R1 system is 2~3 times of sub- nitrogen concentration in R2 system, is successively handed over For progress, until the total nitrogen surface loading of R1 and R2 it is equal > 2.0gN/m2/ d, into next step；
5) CANON stable operation: if < 80% is required to ammonia nitrogen removal frank, using series operation C mode and series operation The mode of D mode alternate run, R1 and R2 reactor control DO in 1.0~3.0mg/L, aeration intensity > 5m3/m2/ h, stirring turn 30~50r/min of speed controls the runing time of C mode and D mode respectively, using series operation C mode, when nitrogen sub- in R2 system When concentration is 2~3 times of sub- nitrogen concentration in R1 system, it is switched to series operation D mode, when nitrogen concentration sub- in R1 system is R2 system When 2~3 times of sub- nitrogen concentration in system, it is switched to series operation C mode, successively alternate run；When require water outlet ammonia nitrogen be lower than When 50mg/L, using series operation mode A, the DO of R1 is controlled in 2.0~4.0mg/L, the DO of R2 is in 2.0~3.0mg/L, aeration Intensity is equal > 5m3/m2/ h, 30~50r/min of speed of agitator, when R1 total nitrogen surface loading be R2 total nitrogen surface loading 1.3~ At 2.5 times, system is switched to series operation B-mode, controls the DO of R1 in 2.0~3.0mg/L, the DO of R2 is in 2.0~4.0mg/ L, aeration intensity is equal > 5m3/m2/ h, 30~50r/min of speed of agitator, until the total nitrogen surface loading of R2 is R1 total nitrogen surface loading 1.3~2.5 times, be switched to series operation mode A, successively alternately.
4th, the supplementary explanation of above-mentioned starting method:
1) it why using MBBR form realization CANON, essentially consists in using two stage process, control is complicated, needs to control Nitrosation water outlet proportion processed, meets anaerobic ammonia oxidation process requirement；Using granule sludge mode, AnAOB is not easy to be enriched with, and activity is dirty Mud method is easy to be lost, it is difficult to starting or granulating；For microorganism, attached state and suspended state show entirely different property spy The correlation technique of activated sludge process can not be directly used in biofilm by point, need the spy for two technique of CANON and MBBR Point, specific aim control；
2) each stage DO control requires different, and main cause provides aerobic or anaerobism by control DO for CANON biomembrane Environment guarantees AOB and AnAOB living environment, and with the thickness change and maturing course of biomembrane, adjusts DO level, meet Biomembrane layering requires；Biomembrane is more mature, and biofilm thickness is opposite to be increased, stronger for the tolerance of DO, needs higher DO it is horizontal；Meanwhile the opposite increase of biofilm thickness, it is also desirable to which higher shearing controls biofilm thickness, prevents biomembrane mistake It is thick；Therefore DO and aeration intensity two indices is required to be controlled simultaneously；The CANON of MBBR form, due to belonging to complete biomembrane System, with traditional activated sludge process in control method, feature very different；For activated sludge process, the general DO of CANON technique is not More than 1mg/L；
3) operational mode in each stage is different, mainly considers vaccination ways, the method for operation and the removal situation to waste water It is different；Biofilm detachment falls off naturally although belonging to ageing process, but still has more active bacteria, flows into next stage reactor It is interior to continue to generate activity；
4) when the control of speed of agitator is to be aerated deficiency, auxiliary suspending carrier fluidisation, and prevent from shearing atom Film thickens, or the excessive biofilm detachment of shearing；
5) it is adjusted by the combination of micro-pore aeration, boring aeration, realizes the different aeration intensities under same DO level；
6) it in implementation steps CANON inoculation start-up course, is inoculated with using series operation mode A, and to R1, R2 limit Oxygen operation；The activated sludge in order to fall off on R1 biomembrane, as AOB and AnAOB R2 continue generate activity and in R2 Adhere on suspending carrier；It is to allow R1 to have adequately sub- nitrogen promotion Anammox reaction using series operation B-mode；
7) expand in start-up course in implementation steps CANON, using series operation C mode and D mode, two reactors are each From water inlet, main purpose is the ammonia nitrogen in order to guarantee to have sufficient in two reactors, and two reactors series connection switchover operations are main Syllabus is that the activated sludge for allowing upper level reactor organisms film to fall off continues to play activity in next stage reactor, maintains system Relatively stable, the factor for preventing sub- nitrogen from being promoted as limitation total nitrogen surface loading of system flora；
8) during implementation steps CANON stable operation, if require < 80% to ammonia nitrogen removal frank, using series connection C mode and series operation D mode alternate run are run, provides enough ammonia nitrogens for reactor, and maintain the opposite of system flora Stablize, relatively sufficient sub- nitrogen is provided and is reacted for Anammox, the promotion of total nitrogen surface loading is promoted；If with effluent quality To control target, using series operation mode A and series operation B-mode alternate run, the first stage reactor mainly cuts down ammonia Nitrogen load, the second stage reactor are to ensure water outlet, and the total nitrogen surface loading of the first stage reactor can be higher than the second order reaction Device, longtime running then cause first order reactor organisms film blocked up, and second level reactor organisms film is relatively thin, furthermore the second order reaction Device is run in the case where low ammonia nitrogen for a long time, may be unfavorable to nitrosation system, so being handed over after operation a period of time It changes, the second stage reactor is changed to the first stage reactor, restore the water inlet of high ammonia nitrogen, and long-term alternate run, guarantee each system The stabilization of flora；
9) sludge concentration < 0.5g/L in reaction tank why is required, is because preventing suspended state sludge concentration excessively high, to life Object film generates stronger competition, influences the biofilm and stabilization of biomembrane；Activated sludge is not limited by matrix, for activated sludge system Often DO is lower by the CANON of system, and load is not high；And biofilm system is passed due to biomembrane layer distributed dependent on matrix gradient Matter can use higher DO, the stability of system can't be caused to decline；Once suspended state sludge concentration increases, will break The stability of bad pure membranous system, makes system be intended to activated sludge process；In addition, suspended state sludge concentration is excessively high, it is also possible to cause The blocking of suspending carrier；Although activated sludge and biomembrane are all biochemical treatments, entirely different biochemical characteristic is shown, is needed It treats with a certain discrimination；
10) scope of application, the present invention are suitble to high ammonia nitrogen, C/N≤1, hot waste water, especially anaerobic sludge to digest supernatant The processing such as liquid, landfill leachate.
As water inlet C/N > 1, SS >=100mg/L, to increase pretreatment and meeting the requirements known to industry professional.
When inlet water temperature is not at 25-35 DEG C, to increase heat-exchange system known to industry professional.
For known to industry professional, above-mentioned suspending carrier, i.e., specific gravity is more smaller than water before biofilm, usually 0.93- 0.97, specific gravity and water are close after biofilm, realize suspension effect, generally high density polyethylene (HDPE) material etc..
It elaborates combined with specific embodiments below to the present invention.
Embodiment 1:
It is dehydrated liquid as system using certain municipal sewage plant's anaerobically digested sludge to intake, water 200m3/ d, pH is 7.8 ~8.2,25~35 DEG C of water temperature, 200~400mg/L of inlet COD concentration, mean value 320mg/L, 300~500mg/L of ammonia nitrogen concentration, Ammonia nitrogen mean value 410mg/L, C/N are than mean value 0.78,300~3000mg/L of SS.The total dischargeable capacity 100m of reactor3, wherein R1 and Each 50m of R23.The waste water, which first passes around after SS is reduced to 100mg/L by pretreatment, enters CANON technique.
Starting prepares, and each reactor adds suspending carrier, filling rate 40%, suspending carrier effective ratio area 800m2/m3, Voidage 90% is inoculated with aerobic sludge, controls R1 and R2 sludge concentration 6g/L；
Nitrosation starting controls the initial DO of R1 and R2 in 3.0~3.5mg/L, 8~10m of aeration intensity3/m2/ h, by by Step reduces the sedimentation time, sludge concentration in reduction system, when operation is to 28d, changes water ratio and reaches 1.00, sludge concentration is in system 0.32g/L, ammonia oxidation rate 0.55, ammoxidation surface loading 2.14g/m2/ d, sub- nitrogen accumulation rate reach 0.99, into next step；
CANON inoculation starting is inoculated with CANON suspending carrier, rate of vaccination 5%, control to R1 using series operation mode A The DO of R1 is in 0.4~1.8mg/L, 1.0~4.0m of aeration intensity3/m2/ h, speed of agitator 15r/min；The DO of R2 0.5~ 0.7mg/L, 1~2m of aeration intensity3/m2/ h, speed of agitator 15r/min, as the Asia R1 nitrogen concentration < 8mg/L, switching system is string Through transport row B-mode controls R1 in 0.4~1.8mg/L, 1.0~4.0m of aeration intensity3/m2/ h, speed of agitator 15r/min；R2's DO is controlled in 0.5~0.7mg/L, 1~2m of aeration intensity3/m2Sub- nitrogen concentration reaches in R1 after/h, speed of agitator 15r/min, 2d To 17mg/L.By the way of series operation mode A and series operation B-mode alternate run, all stage controls the ammonia oxygen of R1 Rate > 0.8, after 45d, total nitrogen surface loading reaches 1.65gN/m2/ d, into next step；
CANON expands starting, by R1 and R2 respectively 50% suspending carrier replace, using series operation C mode, control The DO of R1 and R2 processed are in 1.2~2.8mg/L, 3.5~5.0m of aeration intensity3/m2/ h, the water inlet of speed of agitator 25r/min, R2 Amount accounts for the 40%~50% of total Water, and when nitrogen concentration sub- in R2 system is 2.0~2.2 times of R1, switching system is series connection fortune Row D mode controls the DO of R1 and R2 in 1.2~2.8mg/L, and aeration intensity is in 3.5~5.0m3/m2/ h, speed of agitator 25r/ Min is used instead when nitrogen concentration sub- in R1 system is 2.0~2.2 times of R2 using series operation C mode, successively alternately, whole The ammonia oxidation rate of R1 and R2 is stable during a operation is greater than 0.8, and the total nitrogen surface loading by the stable operation R1 of 27d reaches 2.03gN/m2The total nitrogen surface loading of/d, R2 reach 2.10gN/m2/ d, into next step；
CANON stable operation, stable operation need to control water outlet ammonia nitrogen lower than 50mg/L, using series operation mode A, control The DO of R1 is in 2.8~3.5mg/L, 6~8m of aeration intensity3/m2/ h, speed of agitator 30r/min, control the DO of R2 2.0~ 2.5mg/L, 6~8m of aeration intensity3/m2/ h, speed of agitator 30r/min, when the total nitrogen surface loading of R1 is R2 total nitrogen surface loading 1.5~1.9 times when, system is switched to series operation B-mode, control the DO of R1 in 2.0~2.5mg/L, aeration intensity 6~ 8m3/m2The DO of/h, speed of agitator 30r/min, R2 are in 2.8~3.5mg/L, 6~8m of aeration intensity3/m2/ h, speed of agitator 30r/ Min is successively handed over until the total nitrogen film load of R2 is switched to series operation mode A when being 1.5~1.9 times of R1 total nitrogen film load For progress, by the stable operation of 60d, system is always discharged average ammonia nitrogen concentration 41mg/L, minimum to reach 23mg/L.
The implementation case has successfully started up CANON technique (starting containing nitrosation) by 100d, makes the total of two reactors Nitrogen surface loading is equal > 2gN/m2/ d, hereafter system have passed through the stable operation of 60d again, and during which total nitrogen surface loading stabilization is higher than 2gN/m2/ d, it is average in 2.07gN/m2/ d is discharged ammonia nitrogen mean value 36mg/L, ammonia oxidation rate mean value 0.91, nitrogen removal rate mean value 0.82, and the fluctuation of total nitrogen surface loading has good stability within 3%.
Embodiment 2:
Using certain municipal sewage plant's anaerobic digestion solution sludge liquor as research object, which digests flow quantity 1000m3/ d, pH are between 7.6~8.0,250~350mg/L of inlet COD concentration, mean value 310mg/L, 300~420mg/ of ammonia nitrogen L, average ammonia nitrogen concentration 343mg/L, C/N is than mean value 0.90,300~10000mg/L of SS.The case study on implementation is made with above-mentioned waste water For system water inlet, pilot scale research, pilot reactor dischargeable capacity 30m are carried out3, the wherein equal 15m of R1 and R23, waste water first passes around pre- Treatment process removes SS, and CANON technique is directly entered after so that it is reduced to 100mg/L or less (mean value 65mg/L).
Starting prepares, and each reactor adds suspending carrier, filling rate 50%, suspending carrier effective ratio area 800m2/m3, Voidage 90% is inoculated with the sewage plant aerobic sludge, controls R1 and R2 sludge concentration 7.8g/L；
Nitrosation starting controls the initial DO of R1 and R2 in 3.5~4.0mg/L, 8~10m of aeration intensity3/m2/h.By by Step reduces the sedimentation time, and sludge concentration changes water ratio and reach 1.00 after 32d in reduction system, and sludge concentration reduces in system To 0.29g/L, ammonia oxidation rate at this time reaches 0.67, and ammoxidation surface loading is 2.31g/m2/ d, sub- nitrogen accumulation rate is 0.98 Between~1.00, into next step；
CANON inoculation starting is inoculated with maturation CANON suspending carrier to R1 using series operation mode A, rate of vaccination 3%, The DO of R1 is controlled in 0.3~1.7mg/L, 1.0~4.3m of aeration intensity3/m2/ h, speed of agitator 15r/min.The DO control of R2 exists 0.5~0.8mg/L, 1~2m of aeration intensity3/m2/ h, speed of agitator 15r/min, the switching system as the Asia R1 nitrogen concentration < 8mg/L For the operation of series operation B-mode, the DO of R1 is controlled in 0.3~1.7mg/L, 1.0~4.3m of aeration intensity3/m2/ h, speed of agitator 15r/min.The DO of R2 is controlled in 0.5~0.8mg/L, 1~2m of aeration intensity3/m2/ h, speed of agitator 15r/min, after 3d, Sub- nitrogen concentration reaches 16mg/L in R1, is changed to series operation mode A at this time, and successively alternate run, by step up into Water flow maintains the ammonia oxidation rate of R1 to be greater than 0.8, and by the operation of 52d, the total nitrogen surface loading of system R1 reaches 1.61gN/ m2/ d, into next step；
CANON expand starting, by R1 and R2 respectively 50% suspending carrier replace, using series operation C mode, R1 DO is controlled with R2 in 1.4~3.0mg/L, 3.5~5.5m of aeration intensity3/m2/ h, speed of agitator 30r/min, when in R2 system Sub- nitrogen concentration is switched to series operation D mode when being 2.3~2.5 times of sub- nitrogen concentration in R1 system, and R1 and R2 control DO and exist 1.4~3.0mg/L, 3.5~5.5m of aeration intensity3/m2/ h, speed of agitator 30r/min, when nitrogen concentration sub- in R1 system is R2 system It is changed to series operation C mode when 2.3~2.5 times of sub- nitrogen concentration in system, successively alternately, the ammonia oxygen of whole process R1 and R2 Rate is stable to be greater than 0.8, and by the operation of 24d, the total nitrogen surface loading of R1 reaches 2.11gN/m2The total nitrogen surface of/d, R2 Load reaches 2.09gN/m2/ d, into next step.The total process water yield of system is up to 94m at this time3/d。
CANON stable operation, stable operation require < 80% to the removal rate of ammonia nitrogen, are subject to and control total nitrogen surface loading, Continue to lift up flow of inlet water.By the way of series operation C and D mode alternate run, control the DO of R1 and R2 2.7~ 3.5mg/L, 5~8m of aeration intensity3/m2/ h, speed of agitator 35r/min, using series operation C mode, when nitrogen sub- in R2 system is dense When degree is 2.0~2.2 times of sub- nitrogen concentration in R1 system, it is switched to series operation D mode, when nitrogen concentration sub- in R1 system is R2 When 2.0~2.2 times of sub- nitrogen concentration in system, it is switched to series operation C mode, successively alternate run, controls first reactor Pass through the operation of 25d with the total nitrogen surface loading difference < 10%. of second reactor, the film load of R1 reaches 3.11gN/m2/ d, The film load of R2 reaches 3.14gN/m2/ d, and the total nitrogen surface loading of R1 and R2 is controlled with 3.1g/m2Subject to/d, stable operation is close 60d, for each reactor total nitrogen surface loading variation range within 10%, volumetric loading is up to 1.25kgN/m3/d。
Present case successfully starts up CANON technique by 108d, and the total nitrogen surface loading of each reactor is made to reach 2gN/m2/ d.Since pilot scale water inlet is sufficient, continue the promotion for promoting total nitrogen surface loading, and pass through the operation of 25d, each reactor total nitrogen table Face load reaches 3gN/m2/ d or more, and start stable operation.Total Water 160m is handled during stable operation3/ d accounts for sewage plant and disappears The 16% of change liquid total Water, water outlet ammonia nitrogen concentration mean value 85mg/L, ammonia oxidation rate mean value 0.75, nitrogen removal rate mean value 0.68, Total nitrogen surface loading mean value 3.1gN/m2/ d, stability is preferable, and fluctuation range is within 2%.It is negative according to the film of steady operation period Lotus is calculated, and the total measurement (volume) of reactor is expanded to 190m3, the digestion of factory whole can be handled by 50% filling rate Liquid.
The present invention respectively sets inlet and outlet system by two reactors of setting, its string can be achieved by control valve control Connection, in parallel, continuous flow, SBR operation；Present system can be realized for the low inoculative proportion starting under project scale；By not With the control of operational mode, can safeguards system stable operation；System effluent index is low, can stably reach that " sewage is discharged into cities and towns Sewer water standard " A grade standard in (GB/T 31962-2015)；Using the CANON technique based on MBBR, sustainable liter Grade ability is strong, and system total nitrogen elimination capacity is high.
It uses for reference the prior art and can be realized in the part that do not addressed in the present invention.
It should be noted that any equivalent way that those skilled in the art are made under the introduction of this specification, or Obvious variant should all be within the scope of the present invention.

Claims (9)

1. a kind of quick start method of the CANON system based on MBBR, which is characterized in that the CANON system includes anti- Tank main body, agitating device, aerator and attachment device are answered, the reaction tank main body includes identical two reactions of specification Device, respectively first reactor and second reactor, the first reactor and second reactor are arranged side by side；
The upper side of first reactor far from second reactor is provided with the first control valve, side-lower is provided with the 12nd control Valve processed, close to second reactor first reactor side it is bottom-up be disposed with the second control valve, the 6th control Valve, the 7th control valve and the 8th control valve；The upper side of second reactor far from first reactor is provided with the 5th control Valve, side-lower are provided with the 13rd control valve, bottom-up successively set in the side of the second reactor close to first reactor It is equipped with third control valve, the 11st control valve, the tenth control valve and the 9th control valve；
The junction of each control valve and reactor is provided with interception sieve；
An agitating device is respectively provided in each reactor；
The aerator is distributed in each reactor, and has added suspending carrier in each reactor；
The attachment device includes the first collector pipe, the second collector pipe, third collector pipe, the 4th collector pipe and the 5th collector pipe； First collector pipe links together second control valve, the 6th control valve, the 7th control valve and the 8th control valve, Second collector pipe links together third control valve, the 11st control valve, the tenth control valve and the 9th control valve, institute The bottom for stating the first collector pipe and the second collector pipe is connected with third collector pipe, the third collector pipe center setting the Four control valves, the 4th collector pipe link together first control valve and the 12nd control valve, the 5th collection Water pipe links together the 5th control valve and the 13rd control valve；
The starting method successively the following steps are included:
A, starting prepares, and each reactor adds suspending carrier, and filling rate 20%~67% is inoculated with aerobic sludge, and control first is anti- Answer device, 5~8g/L of sludge concentration in second reactor；
B, nitrosation starts, and using SBR operational mode in parallel, the first reactor and second reactor are coordinations, often A reactor is independently intake, is independently discharged, and intermittent water inflow, intermittent drainage, water ratio is changed by control related valves control, so that useless Water is by third collector pipe through the 4th control valve discharge system；Control first reactor, second reactor initial DO 2~ 5mg/L, aeration intensity > 7m3/m2/ h, ammonia oxidation rate > 50%, system initial precipitation time 30min gradually reduce the sedimentation time, Make amplitude < 25% that sludge concentration reduces in each periodic reaction device；It runs up to sludge concentration < 0.5g/L, and ammoxidation table Face load > 2gN/m2/ d, sub- nitrogen accumulation rate > 0.95, into next step；
C, CANON inoculation starting, using series operation mode A, the first reactor and second reactor series operation, continuously Stream operation, waste water to be processed enter first reactor through the 12nd control valve, by controlling related valves, so that first reactor Water outlet enters second reactor, most afterwards through the 5th control valve discharge system；It is inoculated with CANON suspending carrier to first reactor, is connect Kind rate is 3%~5%, controls DO in 0.3~2.0mg/L, aeration intensity > 1.0m3/m2/ h, 15~30r/min of speed of agitator, ammonia Oxygenation efficiency > 80%；Second reactor controls DO in 0.5~1.0mg/L, aeration intensity > 1m3/m2/ h, 15~30r/ of speed of agitator Min, as first reactor Asia nitrogen concentration < 8mg/L, system is switched to series operation B-mode, the first reactor and second Reactor series operation, waste water to be processed enter second reactor through the 13rd control valve, by controlling related valves, so that second The water outlet of reactor enters first reactor, most afterwards through the first control valve discharge system；Control the DO of first reactor 0.3~ 2.0mg/L, aeration intensity > 1.0m3/m2/ h, 15~30r/min of speed of agitator, ammonia oxidation rate > 80%, second reactor control DO In 0.5~1.0mg/L, aeration intensity > 1m3/m2/ h, 15~30r/min of speed of agitator, until sub- nitrogen in first reactor system System is switched to series operation mode A after concentration>15mg/L, and as first reactor Asia nitrogen concentration<8mg/L, system is switched to Series operation B-mode, successively alternately；Total nitrogen surface loading > 1.6gN/m of the operation up to first reactor2/ d, under One step；
D, CANON expands starting: in first reactor and second reactor 40%~60% suspending carrier being replaced, is adopted With series operation C mode, specific steps are as follows: the first reactor and second reactor series operation, a part of waste water is through 12 control valves are into people's first reactor, by controlling related valves, so that the water outlet of first reactor enters second reactor, remain Remaining waste water enters second reactor by related valves control through the 4th control valve, and second reactor water outlet is discharged through the 5th control valve System；The DO for controlling first reactor and second reactor is 1.0~3.0mg/L, aeration intensity > 3m3/m2/ h, speed of agitator 15 ~30r/min, ammonia oxidation rate > 80%, when nitrogen concentration sub- in second reactor system is sub- nitrogen concentration in first reactor system 2~3 times when, be switched to series operation D mode, specific steps are as follows: the first reactor and second reactor series operation, A part of waste water through the 13rd control valve into people's second reactor, by controlling related valves so that the water outlet of second reactor into Enter first reactor, remaining waste water enters first reactor, first reactor water outlet by related valves control through the 4th control valve Through the first control valve discharge system；The DO for controlling first reactor and second reactor is 1.0~3.0mg/L, aeration intensity > 3m3/m2/ h, 15~30r/min of speed of agitator, ammonia oxidation rate > 80%, when nitrogen concentration sub- in first reactor system is second anti- It is switched to series operation C mode when answering 2~3 times of sub- nitrogen concentration in device system, successively alternately；Operation is until the first reaction Device and the total nitrogen surface loading of second reactor it is equal > 2.0gN/m2/ d, into next step；
E, CANON stable operation: if require < 80% to ammonia nitrogen removal frank, using the series operation C mode and described Series operation D mode alternate run mode, first reactor and second reactor control DO are in 1.0~3.0mg/L, aeration Intensity > 5m3/m2/ h, 30~50r/min of speed of agitator control the series operation C mode and the series operation D respectively The runing time of mode, using series operation C mode, when nitrogen concentration sub- in second reactor system is in first reactor system At 2~3 times of sub- nitrogen concentration, it is switched to series operation D mode, when nitrogen concentration sub- in first reactor system is second reactor When 2~3 times of sub- nitrogen concentration in system, it is switched to series operation C mode, successively alternate run, guarantees first reactor and the The total nitrogen surface loading difference < 20% of two reactors；When requiring water outlet ammonia nitrogen lower than 50mg/L, using the series operation Mode A controls the DO of first reactor in 2.0~4.0mg/L, and the DO of second reactor is in 2.0~3.0mg/L, aeration intensity > 5m3/m2/ h, 30~50r/min of speed of agitator, when the total nitrogen surface loading of first reactor is second reactor total nitrogen surface When load 1.3~2.5, system is switched to series operation B-mode, controls the DO of first reactor in 2.0~3.0mg/L, and second The DO of reactor is in 2.0~4.0mg/L, and aeration intensity is equal > 5m3/m2/ h, 30~50r/min of speed of agitator, until the second reaction The total nitrogen surface loading of device is the 1.3~2.5 of first reactor total nitrogen surface loading, is then switched to series operation mode A again, Successively alternately.
2. a kind of quick start method of CANON system based on MBBR according to claim 1, it is characterised in that: into Water or treatment sewage, C/N≤1；The power of agitator of the first reactor and second reactor is respectively 15~60W/m3。
3. a kind of quick start method of CANON system based on MBBR according to claim 1, it is characterised in that: institute Step c) is stated in e), in each reaction chamber sludge concentration < 0.5g/L；When system is using series connection C operational mode, into second The sewage of reactor is the 10%~50% of total inflow, makes the total nitrogen surface loading of second reactor not less than first reactor 30%；When system is using series connection D operational mode, the sewage into first reactor is the 10%~50% of total inflow, The total nitrogen surface loading of first reactor is set to be not less than the 30% of second reactor.
4. a kind of quick start method of CANON system based on MBBR according to claim 1, it is characterised in that: every Aerator in a reactor is made of multiple groups boring aeration and micro-pore aeration.
5. a kind of quick start method of CANON system based on MBBR according to claim 1, it is characterised in that: institute The SBR operational mode specific steps in parallel stated are as follows: 50% waste water enters the first reaction through the first control valve by the 4th collector pipe Device, water outlet, through the first collector pipe, third collector pipe, pass through the 4th control by the second control valve, the 6th control valve, the 7th control valve Valve discharge system processed is realized by the second control valve of control, the 6th control valve, the 7th control valve and different changes water ratio；It is remaining Waste water enters second reactor through the 5th control valve by the 5th collector pipe, and water outlet passes through third control valve, the 11st control valve, the Ten control valves are through the second collector pipe, third collector pipe, by the 4th control valve discharge system, pass through control third control valve, the 11 control valves, the tenth control valve, which are realized, different changes water ratio.
6. a kind of quick start method of CANON system based on MBBR according to claim 1, it is characterised in that: string Through transport row mode A specific steps are as follows: waste water enters first reactor through the 12nd control valve, and first reactor water outlet is through the 8th control Valve processed, the first collector pipe, third collector pipe, third control valve enter second reactor, and second reactor water outlet is through the 5th control Valve, the 5th collector pipe discharge system.
7. a kind of quick start method of CANON system based on MBBR according to claim 1, it is characterised in that: string Through transport row B-mode specific steps are as follows: waste water enters second reactor through the 13rd control valve, and second reactor water outlet is through the 9th control Valve processed, the second collector pipe, third collector pipe, the second control valve enter first reactor, and first reactor water outlet is through the first control Valve, the 4th collector pipe discharge system.
8. a kind of quick start method of CANON system based on MBBR according to claim 1, it is characterised in that: string Through transport row C mode specific steps are as follows: effluent part enters first reactor through the 12nd control valve, and first reactor water outlet is through the Eight control valves, the first collector pipe, third collector pipe, third control valve enter second reactor, remaining waste water through the 4th control valve, Third collector pipe, third control valve enter second reactor, and second reactor water outlet is discharged through the 5th control valve, the 5th collector pipe System.
9. a kind of quick start method of CANON system based on MBBR according to claim 1, it is characterised in that: string Through transport row D mode specific steps are as follows: effluent part enters second reactor through the 13rd control valve, and second reactor water outlet is through the Nine control valves, the second collector pipe, third collector pipe, the second control valve enter first reactor, remaining waste water through the 4th control valve, Third collector pipe, the second control valve enter first reactor, and first reactor water outlet is discharged through the first control valve, the 4th collector pipe System.
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