WO2020113861A1 - Procédé de démarrage rapide d'un système canon utilisant un bioréacteur à lit mobile - Google Patents

Procédé de démarrage rapide d'un système canon utilisant un bioréacteur à lit mobile Download PDF

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WO2020113861A1
WO2020113861A1 PCT/CN2019/079822 CN2019079822W WO2020113861A1 WO 2020113861 A1 WO2020113861 A1 WO 2020113861A1 CN 2019079822 W CN2019079822 W CN 2019079822W WO 2020113861 A1 WO2020113861 A1 WO 2020113861A1
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reactor
control valve
mode
water
series
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PCT/CN2019/079822
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English (en)
Chinese (zh)
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吴迪
周家中
管勇杰
韩文杰
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青岛思普润水处理股份有限公司
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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

Definitions

  • the present invention belongs to the technical field of biological denitrification, and in particular relates to a quick start method of a CANON system based on MBBR.
  • the CANON process (Completely Autotrophic Nitrogen Removal Over Nitrite, CANON), that is, the full-process autotrophic denitrification process, is a process that combines the short-range nitrification process and the anaerobic ammonia oxidation process in the same reactor to complete the denitrification process, is At present, the most simple and economical biological nitrogen removal process.
  • the biofilm on the outer layer of the suspension carrier uses oxygen to partially oxidize the ammonia nitrogen to nitrous acid. The generated nitrous acid and part of the remaining ammonia nitrogen undergo anaerobic ammonia oxidation in the inner layer of the suspension carrier The reaction generates nitrogen.
  • the microorganisms are attached to the suspended carrier to be fluidized in the water by the aeration or stirring disturbance, and fully contact with the pollutants to achieve the purpose of efficient removal of pollutants.
  • AOB ammonia oxidizing bacteria
  • AnA OB anaerobic ammonia oxidizing bacteria
  • AOB and AnAOB will form a niche competition process on the suspension carrier.
  • Long-term operation of the CANON process will lead to imbalance of bacterial species, the abundance of AOB will decline, and the shortage of nitrous will limit the increase of the total nitrogen load of the system and
  • the stable operation of the system so to ensure the abundance of AOB on the suspended carrier and to ensure that there is sufficient nitrogen in the anaerobic ammonia oxidation reaction process is also called the key to the stable operation of the process.
  • CN 106277357 A discloses a method for starting and efficient operation of an autotrophic denitrification system in which flocculent sludge and granular sludge coexist, in which the reactor is inoculated with flocculent sludge having a short-range nitrification function and having anaerobic ammonia oxidation
  • the mass ratio of functional granular sludge, flocculent sludge and granular sludge is 2 ⁇ 3, with water distribution as influent, intermittent
  • the aeration gradually changed to continuous aeration, and the CANON process was started; it took 45 days to successfully start the CA NON reactor with a volume of 4L.
  • the inoculated sludge of this patent are both mature AOB and AnAOB, both of which need to be cultivated in advance. Taking a 200m 3 reactor as an example, this method requires a mature AOB dry weight of about 152kg and a mature AnAOB dry weight of about 74kg. The inoculation amount is too large, which is obviously not suitable for the inoculation start-up on a project scale; The problem of anaerobic ammonia oxidizing bacteria that is not easily enriched by the activated sludge method;
  • the inoculation method was used to start the CANON process to treat the anaerobic sludge digestion solution; the total area of the inoculated suspension carrier was 3%, and the 50m 3 reactor was started after 120 days. Operation (excluding short-range nitrification start), the highest ammonia oxidation volume load of the system reaches 1.2kg/m Vd, and the stable ammonia oxidation volume load operating load is 0.7 ⁇ l.lkg/m 3 /d, with large fluctuations; The MBBR runs the CANON process, but the relevant control method is still controlled by the activated sludge method, and it has not been adjusted for the biofilm process.
  • CN 108408892 A discloses a membrane bioreactor for immobilizing anaerobic ammonia oxidizing bacteria with a suspension carrier and a sewage treatment process thereof.
  • the membrane bioreactor for immobilizing anaerobic ammonia oxidizing bacteria with a suspension carrier is: Fei Shi, non-woven fabric, polyethylene or polyurethane, with anaerobic ammonia oxidizing bacteria in the suspension carrier layer.
  • the total nitrogen volume load does not exceed 1.0 kgN/m Vd. It uses fixed biofilm technology, has a low total nitrogen load, and uses fixed biofilm technology to run the risk of clogging in the later stage, which requires regular backwashing, and high operation and maintenance costs.
  • the present invention proposes a quick start method of the CAN ON system based on MBBR, through the connection device to control the reactor series, parallel, continuous operation, intermittent operation, through inoculation , Alternately switch the operation mode to achieve fast start of the autotrophic denitrification process and stable operation.
  • the invention has the advantages of small inoculation ratio, fast start-up, high total nitrogen load, stable operation and the like.
  • a quick start method of a CANON system based on MBBR includes a reaction cell body, a stirring device, an aeration device and a connection device, the reaction cell body includes two reactors with the same specifications, They are a first reactor and a second reactor, and the first reactor and the second reactor are arranged side by side;
  • a first control valve is provided above the side of the first reactor away from the second reactor, and a twelfth control valve is provided below the side, from the bottom of the first reactor near the second reactor
  • a second control valve, a sixth control valve, a seventh control valve, and an eighth control valve are sequentially arranged upward;
  • a fifth control valve is provided above the side of the second reactor away from the first reactor, and a Thirteenth control valve, a third control valve, an eleventh control valve, a tenth control valve and a ninth control valve are provided in this order from the bottom to the side of the second reactor near the first reactor;
  • Each control valve and the reactor are provided with an intercepting screen; [0016] A stirring device is provided in each reactor;
  • the aeration device is distributed in each reactor, and a suspension carrier is added in each reactor;
  • the connection device includes a first water collection tube, a second water collection tube, a third A water collecting pipe, a fourth water collecting pipe and a fifth water collecting pipe; the first water collecting pipe connects the second control valve, the sixth control valve, the seventh control valve and the eighth control valve together, and the first The second water collecting pipe connects the third control valve, the eleventh control valve, the tenth control valve and the ninth control valve together, and the bottoms of the first water collecting pipe and the second water collecting pipe are connected to the third water collecting pipe, A fourth control valve is provided at the center of the third water collecting pipe, the fourth water collecting pipe connects the first control valve and the twelfth control valve together, and the fifth water collecting pipe connects the fifth control valve and the first Thirteen control valves are connected together;
  • the startup method in turn includes the following steps:
  • each reactor is added suspension carrier, filling rate 20% ⁇ 67%, aerobic sludge inoculation, control the first reactor, the second reactor sludge concentration 5 ⁇ 8g/L;
  • ammonia oxidation rate >50%
  • the initial settling time of the system is 30min, and gradually reduce the settling time, so that the sludge concentration in the reactor in each cycle decreases by less than 25%; run until the sludge concentration is less than 0.5g/L, and Ammonia oxidation surface load> 2gN/m 2 /d, N2 accumulation rate> 0.95, enter the next step;
  • CANON inoculation starts, using series operation A mode, the first reactor and the second reactor operate in series, continuous flow operation, the wastewater to be treated enters the first reactor through the twelfth control valve, and is controlled by Related valves, so that the effluent from the first reactor enters the second reactor, and finally exits the system through the fifth control valve; inoculates the CANON suspension carrier into the first reactor, the inoculation rate is 3% ⁇ 5%, and the control DO is 0.3 ⁇ 2.0 mg/L, aeration intensity>1.0m 3 /m 2 /h, stirring speed 15 ⁇ 30r/min, ammonia oxidation rate>80%; the second reactor controls DO at 0.5 ⁇ 1.0mg/L, aeration intensity> lm 3 /m 2 /h, stirring speed 15 ⁇ 30r/min, when the nitrous concentration of the first reactor is less than 8mg/L, the system is switched to series operation B mode, the first reactor and the second reactor are connected in series Operation,
  • CANON expansion start replacing 40% to 60% of the suspended carrier in the first reactor and the second reactor, using the C mode in series operation, the specific steps are: the first reactor and the second The reactors are operated in series, part of the wastewater enters the first reactor through the twelfth control valve, and the effluent of the first reactor enters the second reactor through the control of the relevant valve, and the remaining wastewater is controlled through the relevant valve through the fourth control valve.
  • the second reactor, the second reactor effluent is discharged from the system through the fifth control valve;
  • the DO of the first reactor and the second reactor is controlled to 1.0 ⁇ 3.0mg/L, and the aeration intensity>3m 3 /m 2 /h, Stirring speed 15 ⁇ 30r/min, ammonia oxidation rate> 80 %, when the nitrous concentration in the second reactor system is 2 ⁇ 3 times of the nitrous concentration in the first reactor system, switch to series operation D mode, specific
  • the steps are: the first reactor and the second reactor operate in series, a part of the wastewater enters the second reactor through the thirteenth control valve, and the effluent of the second reactor enters the first reactor by controlling the relevant valve, The remaining wastewater is controlled to enter the first reactor through the relevant valve through the fourth control valve, and the effluent of the first reactor is discharged from the system through the first control valve; the DO of the first reactor and the second reactor is controlled to 1.0 ⁇ 3.0mg/L, Aeration intensity> 3m 3
  • influent or sewage to be treated C/N ⁇ 1; the stirring power of the first reactor and the second reactor are 15 ⁇ 60W/m 3 respectively .
  • the steps c) to e), the sludge concentration in each reaction chamber are ⁇ 0.
  • the aeration device in each reactor is composed of multiple groups of perforated aeration and microporous aeration.
  • the specific steps of the parallel SBR operation mode are: 50% of the wastewater enters the first reactor through the first control valve from the fourth water collection pipe, and the effluent passes through the second control valve, the sixth control valve, the first Seven control valves are discharged from the system through the first water collection pipe, the third water collection pipe, through the fourth control valve, and different water exchange ratios are realized by controlling the second control valve, the sixth control valve, and the seventh control valve;
  • the five water collecting pipes enter the second reactor through the fifth control valve, and the effluent passes through the third control valve, the eleventh control valve, and the tenth control valve through the second water collecting pipe, the third water collecting pipe, and exits the system through the fourth control valve.
  • Different water exchange ratios are realized by controlling the third control valve, the eleventh control valve, and the tenth control valve.
  • wastewater enters the first reactor through the twelfth control valve
  • the effluent from the first reactor enters the second reactor through the eighth control valve, first water collection tube, third water collection tube, and third control valve, and the effluent from the second reactor exits the system through the fifth control valve and fifth water collection tube.
  • the specific steps of the B mode in series operation are: the wastewater enters the second reactor through the thirteenth control valve, and the effluent from the second reactor passes through the ninth control valve, the second water collecting pipe, the third water collecting pipe, and the second The control valve enters the first reactor, and the water from the first reactor exits the system through the first control valve and the fourth water collecting pipe.
  • the specific steps of the C mode in series operation are: part of the wastewater enters the first reactor through the twelfth control valve, and the effluent of the first reactor passes through the eighth control valve, the first water collecting pipe, the third water collecting pipe, the first The three control valves enter the second reactor, the remaining wastewater enters the second reactor through the fourth control valve, the third water collection pipe, and the third control valve, and the second reactor effluent exits the system through the fifth control valve and the fifth water collection pipe.
  • the specific steps of the D mode in series operation are: part of the wastewater enters the second reactor through the thirteenth control valve, and the effluent from the second reactor passes through the ninth control valve, the second water collecting pipe, the third water collecting pipe, the first The second control valve enters the first reactor, the remaining wastewater enters the first reactor through the fourth control valve, the third water collection pipe, and the second control valve, and the first reactor outlet water exits the system through the first control valve and the fourth water collection pipe.
  • the inoculation method is used to start the CANON process, the inoculation rate is low, and the water volume of 250m 3 /d only needs to be inoculated with 3m 3 of mature CANON suspension carrier to start, suitable for engineering-scale CANON startup;
  • the start-up time is short, for the project-scale start-up, it can be successfully started in about 4 months (including short-range nitrification start), so that the total nitrogen surface load of the system> 2gN/m 2 /d ;
  • the present invention uses different operating modes for control, which can eliminate the limitation of nitrous nitrogen on the surface load of total nitrogen
  • the total nitrogen surface load can reach more than 3gN/m 2 /d;
  • the present invention can ensure that the system is filled with sufficient nitrous acid for anaerobic ammonium oxidation reaction during the stable operation by not switching the operating mode, ensuring the long-term stable operation of the system, and solving the possibility of insufficient AOB in the later period The risk of load fluctuations even reduced.
  • the present invention adopts different operation mode controls, which can meet various engineering requirements, such as total nitrogen surface load (occupying a small area), effluent ammonia nitrogen concentration (low ammonia nitrogen) control, etc.;
  • the process mode of the present invention is used for operation, the control is simple, and different operation modes can be switched through automatic control, and the fluidization and aeration are reasonably balanced, and the degree of automation is high;
  • FIG. 1 is a top view of the system of the present invention
  • FIG. 2 is a longitudinal sectional view of the system of the present invention.
  • R1 the first reactor; R2, the second reactor; S1, the stirring device of the first reactor; S2, the stirring device of the second reactor; L1-L13, the first control valve-tenth Three control valves; C1-C5, the first water collecting pipe-the fifth water collecting pipe.
  • the present invention discloses a quick start method of CANBR system based on MBBR.
  • MBBR Moving Bed Biofilm Reactor (Moving Bed Biofilm Reactor, MBBR), this method is to increase the biomass and species in the reactor by adding a certain amount of suspension carrier to the reactor, Thereby improving the processing efficiency of the reactor;
  • the filling rate of the suspended carrier that is, the ratio of the volume of the suspended carrier to the pool volume of the filled area, the volume of the suspended carrier is the total volume under natural accumulation; for example, 100m 3 suspended carrier, filled to 400m 3 pool volume , The filling rate is 25%;
  • Fluidization the state in which the suspended carrier flows in the liquid along with the water flow and is fully in contact with the pollutants in the water under the action of aeration or stirring;
  • Ammonia oxidation surface load the amount of ammonia nitrogen removed per unit area of the suspended carrier, gN/m Vd, if the influent ammonia nitrogen concentration is 400 mg/L, the effluent ammonia nitrogen concentration is 100 mg/L, and the flow rate is 100 m 3
  • Total nitrogen surface load the amount of total nitrogen removed per unit area of the suspended carrier per day, gN/m 2 /d;
  • Ammonia oxidation rate the ratio of ammonia nitrogen removal to the intake water ammonia nitrogen. If the influent ammonia nitrogen is 400mg/L and the removal amount is 350mg/L, the ammonia oxidation rate is 0.875 or 87.5%;
  • Nitrosification the process in which microorganisms oxidize ammonia nitrogen (NH 4 + ) to nitrite nitrogen (NO 2- ) without further oxidation to nitrate nitrogen (N 0 3- ), that is, enrichment within the system Ammonia oxidizing bacteria (AOB), while eliminating nitrite oxidizing bacteria (NOB);
  • CANON process the whole process of autotrophic denitrification process, the process refers to the control of dissolved oxygen in a single reactor or biofilm to achieve nitrosation and anaerobic ammonia oxidation, so as to achieve the purpose of nitrogen removal.
  • ammonia-oxidizing bacteria partially oxidize ammonia nitrogen into nitrite nitrogen, and the nitrite nitrogen produced will react with part of the remaining ammonia nitrogen to form nitrogen through anaerobic ammonia oxidation;
  • CANON suspension carrier That is, a suspension carrier with CANON effect, AOB and AnAOB are layered in the form of biofilm;
  • Inoculation rate the percentage of inoculated CANON suspension carrier in the total suspension carrier, %. Such as 50m 3
  • the suspension carrier was inoculated with 2m 3 of mature CANON suspension carrier, the inoculation rate was 4%;
  • Aeration intensity refers to the amount of aeration per unit area of the bottom, the unit is m 3 /m 2 /h. Aeration is the total aeration
  • C/N ratio refers to the ratio of the concentration of BOD 5 in the wastewater to the Kjeldahl nitrogen concentration
  • the stirring power is related to the filling rate, the higher the filling rate, the greater the stirring power
  • Aerobic sludge refers to the residual sludge after the aerobic tank effluent mixture in the sewage treatment plant is precipitated by the secondary sedimentation tank
  • Water exchange ratio using SBR process, the ratio of the amount of water replaced in the system to the total water amount in each cycle, such as
  • the water exchange ratio is 0.5.
  • the following first reactor is abbreviated as R1
  • the second reactor is abbreviated as R2
  • the first control valve-thirteenth control valve is referred to as L1-L13
  • the first water collecting pipe-fifth water collecting pipe is referred to as Cl-C5.
  • a CANBR system based on MBBR of the present invention includes a reaction cell body, a stirring device, an aeration device and a connection device, wherein the reaction cell body includes two of the same specifications
  • the reactors are respectively the first reactor R1 and the second reactor R2, the first reactor and the second reactor are arranged side by side, and the two are connected by a related valve and a water collection pipe, and the positions of the related valves and the water collection pipe are arranged
  • the connection method is;
  • a first control valve L1 is provided above the side of the first reactor away from the second reactor, and a twelve control valve L12 is provided below the side, from the side of the first reactor near the second reactor.
  • a second control valve L2, a sixth control valve L6, a seventh control valve L7, and an eighth control valve L8 are provided in this order from bottom to top;
  • a fifth control valve L5 is provided above the side of the second reactor away from the first reactor ,
  • a thirteenth control valve L13 is provided below the side, and a third control valve L3, an eleventh control valve LI 1, and a tenth control valve are provided in order from the bottom to the side of the second reactor near the first reactor L10 and ninth control valve L9;
  • the above connection device includes a plurality of water collecting pipes, namely a first water collecting pipe C1, a second water collecting pipe C2 and a third water collecting pipe C3, a fourth water collecting pipe C4 and a fifth water collecting pipe C5;
  • the first water collecting pipe will The second control valve, the sixth control valve, the seventh control valve and the eighth control valve are connected together, and the second water collecting pipe connects the third control valve, the first The eleventh control valve, the tenth control valve and the ninth control valve are connected together, the bottoms of the first and second water collection pipes are connected with a third water collection pipe, and the fourth control valve is located at the center of the third water collection pipe
  • the fourth water collecting pipe connects the first control valve and the twelfth control valve together, and the fifth water collecting pipe connects the fifth control valve and the thirteenth control valve together;
  • the first reactor and the second reactor are equipped with stirring devices, as shown in the first reactor stirring device S1 and the second reactor stirring device S2, specific stirring device
  • the structure can be realized with reference to the existing technology, and will not be described in detail here.
  • the aeration device in each reactor is composed of multiple sets of perforated aeration tubes and a plurality of microporous aeration disks.
  • Suspension carrier is added in each reactor, the filling rate is 20% ⁇ 6 7%; and the connection between the control valve of each reactor and the reactor is equipped with an interception screen to intercept the suspended carrier;
  • the operation process has the following five control modes:
  • L6, L7, through C1 and C3, through L3 discharge system by controlling L2, L6, L7 to achieve different water exchange ratio; the remaining wastewater from C5 through L5 into R2, R2 effluent through L10, Lll, L13, through C2 and C3, the system is discharged from L4, and different water exchange ratios are realized by controlling L10, Lll, L13;
  • R2 effluent is discharged from the system through L5 and C5;
  • R1 effluent is discharged from the system through LI and C4;
  • R2 the remaining wastewater enters R2 through L4, C3, L3, and the R2 effluent exits the system through L5, C5;
  • R1 the remaining wastewater enters Rl through L4, C3, L2, and the effluent of R1 exits the system through LI, C4.
  • the startup method of the present invention includes the following steps: [0087] 1) Preparation for start-up, adding a suspension carrier to each reactor, the filling rate is 20% ⁇ 67%, inoculated with aerobic sludge, control the sludge concentration in Rl, R2 5 ⁇ 8g/L;
  • CANON inoculation is started.
  • a mode is used in series operation to inoculate CAN suspension carrier to R1, the inoculation rate is 3% to 5%, the DO is controlled at 0.3 to 2.0 mg/L, and the aeration intensity is greater than 1.0 m 3 /m 2
  • R2 controls DO at 0.5 ⁇ 1.0mg/L, aeration intensity>lm 3 /m 2 /h, stirring speed 15 ⁇ 30r/min, when When the nitrous concentration of R1 is less than 8mg/L, the system switches to series operation B mode, the DO of R1 is controlled at 0.3 ⁇ 2.0mg/L, and the aeration intensity is greater than 1.0m 3 /m 2
  • CANON expansion start replace 40% to 60% of the suspended carrier in R1 and R2, adopt series operation C mode, control the DO of R1 and R2 at 1.0 ⁇ 3.0mg/L, aeration intensity> 3m 3 /m 2
  • CANON in the form of MBBR is in the control method with the traditional activated sludge method , The characteristics vary greatly; for the activated sludge method, the CANON process generally DO does not exceed lmg/L;
  • each stage is different, mainly considering the inoculation mode, operation mode and the removal of wastewater; the biofilm shedding, although it belongs to the natural aging process, but there are still more active strains, flowing into the next Can continue to produce activity in the reactor;
  • the control of the stirring rotation speed is to assist the fluidization of the suspended carrier when the aeration is insufficient, and to prevent the biofilm from thickening or the biofilm from falling off due to excessive shearing force;
  • step CANON inoculation start process using series operation A mode, and inoculation of R1, R2 oxygen-limited operation; is for the activated sludge off R1 biofilm, such as AOB and AnAOB in R2 Continue to generate activity and attach to the suspended carrier of R2; the series B mode is used to allow R1 to have sufficient nitrous acid to promote the anaerobic ammonia oxidation reaction;
  • the C mode and D mode are used in series operation, and the two reactors are fed with water respectively.
  • the main purpose is to ensure that both reactors have sufficient ammonia nitrogen and two reactions.
  • the main purpose of the series switching operation of the reactor is to allow the activated sludge shed by the biofilm of the upper reactor to continue to play an active role in the lower reactor, maintain the relative stability of the system flora, and prevent nitrous nitrogen from becoming a limitation of the total nitrogen surface load.
  • the series operation C mode and the series operation D mode are used alternately to provide sufficient ammonia nitrogen for the reactor and maintain system bacteria.
  • the group is relatively stable, providing relatively sufficient nitrous acid for anaerobic ammonia oxidation, and promoting the increase of the total nitrogen surface load; if the effluent water quality is the control goal, the series A mode and series B mode are used alternately, the first level
  • the reactor is mainly to reduce the ammonia nitrogen load.
  • the second-stage reactor is to protect the effluent. The total nitrogen surface load of the first-stage reactor will be higher than that of the second-stage reactor.
  • the second-stage reactor has a thin biofilm.
  • the second-stage reactor is operated under low ammonia nitrogen for a long time, which may be detrimental to the nitrosation system. Therefore, after a period of operation, the second-stage reactor is exchanged and the second-stage reactor is changed. It is the first-stage reactor, which restores the high ammonia nitrogen influent and runs it alternately for a long time to ensure the stability of the bacterial flora of each system;
  • the reason why the sludge concentration in the reaction tank is required to be ⁇ 0.5g/L is to prevent the suspended sludge concentration from being too high, which will cause strong competition to the biofilm and affect the biofilm hang and stability;
  • the sludge is not limited by the matrix.
  • the CANON usually has a low DO and low load; while the biofilm system, due to the stratified distribution of the biofilm, depends on the matrix gradient mass transfer, and a higher DO can be used.
  • the present invention is suitable for high ammonia nitrogen, C/N ⁇ 1.
  • the above-mentioned suspension carrier that is, the specific gravity before film hanging is slightly smaller than water, usually 0.93-0.97, and the specific gravity after film hanging is close to water to achieve the suspension effect, generally made of high-density polyethylene Wait.
  • the anaerobic digestion sludge dewatering liquid of a certain urban sewage treatment plant is used as the system influent, the water volume is 200m 3
  • the total effective volume of the reactor is 100m 3 , of which R1 and R2 are 50m 3 each.
  • the wastewater is first pretreated to reduce the SS to 100 mg/L and enters the CANON process.
  • CANON inoculation starts, adopts series operation A mode, inoculates CANON suspension carrier to R1, inoculation rate
  • a series operation mode A and series operation mode B are used alternately to control the ammonia oxidation rate of R1>0.8 throughout the stage. After 45 days, the total nitrogen surface load reaches 1.65 gN/m 2 /d, enter the next step;
  • CANON expansion start replace 50% of each of R1 and R2 suspended carrier, using series operation C mode, control DO of R1 and R2 are 1.2 ⁇ 2.8mg/L, aeration intensity 3.5 ⁇ 5.0 m 3 / m 2
  • the stable operation needs to control the effluent ammonia nitrogen is less than 50mg/L, adopt series operation A mode, control the DO of R1 in 2.8 ⁇ 3.5mg/L, aeration intensity 6 ⁇ 8 m 3 /m 2 /h , Stirring speed 30r/min, controlling DO of R2 at 2.0 ⁇ 2.5mg/L, aeration intensity 6 ⁇ 8 m 3 /m 2 /h, stirring speed 30r/min, when the total nitrogen surface load of R1 is R2 total nitrogen When the surface load is 1.5 ⁇ 1.9 times, the system switches to series operation B mode, the DO of R1 is controlled at 2.0 ⁇ 2.5mg/L, and the aeration intensity is 6 ⁇ 8 m 3 /m 2
  • the CANON process (including nitrosation start) was successfully started after 100 days, so that the total nitrogen surface load of both reactors was> 2 gN/m 2 /d, and then the system went through a stable operation for 60 days.
  • TN stable surface load than 2 gN / m 2 / d, average 2.07gN / m 2 / d, effluent ammonia mean 36mg / L, the mean rate ammoxidation 0.91, 0.82 average TN removal and total nitrogen loading surface The fluctuation is within 3% and the stability is good.
  • the flow rate of the digestion solution in this sewage treatment plant is 1000m 3 /d
  • the pH is between 7.6 and 8.0
  • the influent COD concentration is 250 to 350 mg/L.
  • the average value is 310mg/L
  • the ammonia nitrogen is 300 ⁇ 420mg/L
  • the average ammonia nitrogen concentration is 343mg/L
  • the average C/N ratio is 0.90
  • the SS 300 ⁇ 10000mg/L the above wastewater was used as the system influent to conduct a pilot test.
  • the effective volume of the pilot reactor was 30m 3, of which R1 and R2 were 15m 3.
  • the wastewater was first removed by a pretreatment process to reduce it to below 100mg/L (Average 65mg/L) After that, directly enter the CANON process.
  • each reactor is charged with suspended carrier, the filling rate is 50%, the effective specific surface area of the suspended carrier is 800m 2 /m 3 , the void rate is 90%, inoculate the sewage plant aerobic sludge, control the concentration of R1 and R2 sludge 7.8g/L;
  • CANON inoculation starts, adopts series operation A mode, inoculates mature CANON suspension carrier to R1, inoculation rate is 3%, controls DO of R1 at 0.3 to 1.7 mg/L, and aeration intensity 1.0 to 4.3 m 3 /m 2
  • the DO of R2 is controlled at 0.5 ⁇ 0.8mg/L, the aeration intensity is 1 ⁇ 2 111 3 /111 2 /11, the stirring speed is 15r/min, and when the N1 concentration of R1 is less than 8mg/L, the system is switched to series operation B mode operation , Control the DO of R 1 at 0.3 ⁇ 1.7mg/L, aeration intensity 1.0 ⁇ 4.3 m 3 /m 2 /h, stirring speed 15r/min.
  • the DO of R2 is controlled at 0.5 ⁇ 0.8mg/L, the aeration intensity is 1 ⁇ 2 m 3 /m 2 /h, and the stirring speed is 15r/min.
  • CANON expansion start replace 50% of each of R1 and R2 suspended carrier, using series operation C mode, R1 and R2 both control DO at 1.4 ⁇ 3.0mg/L, aeration intensity 3.5 ⁇ 5.5 m 3 /m 2
  • the total nitrogen surface load of R1 reached 2.11 gN/m 2 /d, and the total nitrogen surface load of R2 reached 2.09 gN/m 2 /d.
  • the total treated water volume of the system can reach 94m Vd.
  • the stable operation of CANON requires the removal rate of ammonia nitrogen to be ⁇ 80% in the stable operation, subject to the control of the total nitrogen surface load, and continue to increase the influent flow rate.
  • Adopt series operation C and D mode alternate operation mode, control DO of R1 and R2 at 2.7 ⁇ 3.5mg/L, aeration intensity 5 ⁇ 8 m 3 /m 2 /h, stirring speed 35r/min, use series operation C Mode, when the N2 concentration in the R2 system is 2.0 ⁇ 2.2 times of the N2 concentration in the R1 system, switch to the D mode in series operation, when the N2 concentration in the R1 system is 2.0 ⁇ 2.2 times the N2 concentration in the R2 system , Switch to C mode in series operation, alternately run in sequence, control the total nitrogen surface of the first reactor and the second reactor negative The charge difference is less than 10%. After 25 days of operation, the membrane load of R1 reaches 3.11 gN/m 2
  • the membrane load of R2 reaches 3.14 gN/m 2 /d
  • the total nitrogen surface load of R1 and R2 is controlled to 3.1g/m 2 /d
  • the stable operation is nearly 60 days.
  • the total nitrogen surface load of each reactor changes The range is within 10%, and the volume load is up to 1.25kgN/m 3 /d.
  • the CANON process was successfully started after 108 days, and the total nitrogen surface load of each reactor reached 2 g N/m 2 /d. Due to sufficient water intake in the pilot plant, the total nitrogen surface load continued to be promoted. After 25 days of operation, the total nitrogen surface load of each reactor reached more than 3 gN/m 2 /d and started stable operation. During the stable operation, the total water treatment volume is 160 m 3 /d, which accounts for 16% of the total amount of digestive juice in the sewage plant.
  • the average ammonia nitrogen concentration in the effluent is 85 mg/L.
  • the average ammonia oxidation rate is 0.75.
  • the average removal rate of total nitrogen is 0.68.
  • the average surface load of total nitrogen is 3.1.
  • the stability is good, the fluctuation range is within 2%.
  • the total volume of the reactor is expanded to 190m 3 , and all the digestion liquid of the plant can be processed at a filling rate of 50%.
  • the present invention can realize its series, parallel, continuous flow, SBR operation by setting two reactors, each with a water inlet and outlet system controlled by a control valve; the system of the present invention can achieve a low inoculation ratio startup for a project scale ; Through the control of different operation modes, it can ensure the stable operation of the system; The system has a low effluent index, which can stably reach the A-level standard in the "Water Quality Standards for Wastewater Discharge into Urban Sewers" (GB/T 31962-2015); adopt MBBR-based CANON process has strong ability of sustainable upgrade and high total nitrogen removal load.

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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

L'invention concerne un procédé de démarrage rapide d'un système CANON utilisant un bioréacteur à lit mobile, comprenant un corps principal de cuve de réaction, des dispositifs d'agitation, des dispositifs d'aération et des dispositifs de raccordement, le corps principal de cuve de réaction comprenant deux réacteurs identiques connectés en parallèle ou en série, chacun des réacteurs est indépendamment équipé d'un dispositif d'agitation, d'un dispositif d'aération et d'un dispositif de raccordement, et un support suspendu est ajouté à chaque réacteur. Au moyen de la commande de vannes entre les réacteurs, cinq modes de fonctionnement peuvent être réalisés, à savoir un mode de fonctionnement RBS en série, un mode de fonctionnement en série A, un mode de fonctionnement en série B, un mode de fonctionnement en série C et un mode de fonctionnement en série D. Dans le processus de démarrage d'un processus CANON, différents modes de fonctionnement peuvent être utilisés selon des exigences de commande à différents stades.
PCT/CN2019/079822 2018-12-05 2019-03-27 Procédé de démarrage rapide d'un système canon utilisant un bioréacteur à lit mobile WO2020113861A1 (fr)

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CN117865347B (zh) * 2024-01-04 2025-02-14 长江生态环保集团有限公司 一种促进颗粒污泥快速形成的连续流反应装置及运行方法

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