WO2020113863A1 - Procédé de démarrage rapide d'un système d'élimination d'azote entièrement autotrophe de bioréacteur à lit mobile - Google Patents

Procédé de démarrage rapide d'un système d'élimination d'azote entièrement autotrophe de bioréacteur à lit mobile Download PDF

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WO2020113863A1
WO2020113863A1 PCT/CN2019/079824 CN2019079824W WO2020113863A1 WO 2020113863 A1 WO2020113863 A1 WO 2020113863A1 CN 2019079824 W CN2019079824 W CN 2019079824W WO 2020113863 A1 WO2020113863 A1 WO 2020113863A1
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Prior art keywords
reaction chamber
water
water outlet
valve
reaction
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PCT/CN2019/079824
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English (en)
Chinese (zh)
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吴迪
管勇杰
周家中
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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Publication of WO2020113863A1 publication Critical patent/WO2020113863A1/fr

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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 specifically relates to a method for quickly starting an MBBR full-autotrophic denitrification system.
  • the CANON process (Completely Autotrophic Nitrogen Removal Over Nitrite), that is, the whole process of autotrophic nitrogen removal process, is a new type of biological nitrogen removal process, which refers to the realization of nitrosation by controlling dissolved oxygen in a single reactor or biofilm And anaerobic ammonia oxidation, so as to achieve the purpose of nitrogen removal.
  • ammonia-oxidizing bacteria Under aerobic conditions, ammonia-oxidizing bacteria partially oxidize ammonia nitrogen into nitrous acid, and the generated nitrous acid reacts with part of the remaining ammonia nitrogen to produce nitrogen.
  • the MBBR autotrophic denitrification system occupies less space, and only requires 20% of the volume of a common oxidation tank under the same load conditions; microorganisms adhere to the carrier and flow with the water flow using the aeration or agitation disturbance to fully contact with pollutants To increase the removal load. The friction between the carrier and the water flow and carrier makes the carrier less clogged.
  • Ammonia oxidizing bacteria AOB
  • AnAOB anaerobic ammonia oxidizing bacteria
  • the growth is very slow, the doubling time is longer, it is difficult to maintain a higher biological concentration
  • AOB is aerobic bacteria
  • AnAOB is strictly anaerobic bacteria
  • too high Dissolved oxygen will inhibit AnAOB
  • too low dissolved oxygen can not guarantee the conversion of ammonia nitrogen to nitrite
  • too low nitrite will lead to insufficient AnAOB matrix
  • growth is inhibited.
  • the ability to quickly start and stabilize high-load operation is the key to the application of the entire autotrophic denitrification system.
  • the inoculation ratios are 8.7%, 43%, and 8.7%, respectively, and the start-up time is 368 days. , 50d and 137d, the shortest start-up time is 50d, but the inoculation ratio is large; the initiation cycle with the inoculation ratio of 8.7% is 368d and 137d respectively, the method has a long start-up period, but the reliability is insufficient; the sponge filler is a soft filler, and the sponge is operated for a long time It is easy to be blocked inside and difficult to be applied on a large scale in the project; volcanic rock filler is a heavy filler, which is easy to be blocked between long-term running fillers, and the operation and maintenance remain unchanged; although the research thinks of using a suspended carrier (polyethylene filler), the control is still in accordance with the activated pollution
  • the mud system was carried out, failing to address the characteristics of the MBBR biofilm, failing to take advantage of MBBR in the CANON process; the relevant method engineering did not have the
  • the ratio of ammonia nitrogen removed by this method to the generated nitrate nitrogen is 8% ⁇ 15%, which is higher than the theoretical value of 11%, that is, it exists in the system A certain amount of NOB, and the growth rate of NOB is faster than that of AOB, there is a hidden danger of excessive value increase of NOB in long-term operation.
  • the stirring device is not set up, and the risk of clogging of biofilm over-thick filler is prone to occur in the later operation, which affects the effect of nitrogen removal;
  • CN 106673205 A discloses a quick start method of an integrated autotrophic denitrification system.
  • a sequential batch SBR reactor is used, and a short-range nitrification sludge is inoculated according to a mass ratio of 1:3 to 1:1 and The anaerobic ammonia oxidation sludge adopts the operation mode of intermittent aeration.
  • the total nitrogen removal load of the reactor is 0.3kgN/(m 3 ⁇ d) during the first step of inoculation
  • the total nitrogen removal load of the reactor can be It reaches 0.63kgN/(m ⁇ d) ; but also, this method has a large inoculation ratio, reaching 50%-75%, and uses intermittent operation. It has a large volume in engineering applications and does not have the significance of large-scale startup.
  • the present invention proposes a quick start method of MBBR full autotrophic denitrification system, which controls the water outlet direction of the four-grid reaction chamber through a diversion structure to realize the series connection of the reaction chambers , Parallel or separate operation, to achieve the rapid start of the autotrophic denitrification process by means of inoculation, feeding, etc., according to the requirements of the treatment standard, different process layouts can be realized.
  • the present invention has the advantages of small inoculation ratio and fast startup.
  • a quick start method of an MBBR full-course autotrophic denitrification system includes a reaction tank body, a stirring device, an aeration device, a diversion device and a water collection device,
  • the main body of the reaction cell is divided into two rows and two columns of four reaction chambers by a partition plate, which are a first reaction chamber, a second reaction chamber, a third reaction chamber and a fourth reaction chamber, among them, the first reaction chamber and the fourth
  • the reaction chambers are in a row and located at the bottom, and the first reaction chamber and the second reaction chamber are in a row;
  • the first reaction chamber and the fourth reaction chamber are respectively provided with a first water inlet and a fourth water inlet below the side, and the second reaction chamber and the third reaction chamber are respectively provided with a first A second water inlet and a third water inlet, through the first water inlet, the second water inlet, the third water inlet and the fourth water inlet to the first reaction chamber, the second reaction chamber, the third reaction chamber and the fourth water inlet respectively Water in the reaction chamber;
  • the first water inlet, the second water inlet, the third water inlet, and the fourth water inlet are diagonally provided with a first water outlet screen, a second water outlet screen, and a third water outlet screen, respectively And a fourth water outlet screen, the first water outlet screen, the second water outlet screen, the third water outlet screen, and the fourth water outlet screen are all arranged diagonally and Form a relatively closed area;
  • the water collection device includes a first water collection well, a second water collection well and a water outlet pipe connected thereto, the first water collection well is located in a relatively closed area at the center of four reaction chambers, The first water collection well is used to collect the sewage in the reaction tank and discharge it through the water outlet pipe;
  • a fifth water outlet screen and a sixth water outlet screen are also provided above the second reaction chamber and the third reaction chamber, and the second water collection well is provided in the area formed by the two, the The second water collection well is used to collect the sewage in the reaction tank and discharge it through the water outlet pipe;
  • the diversion device is used to control the flow direction of water in the reaction chamber and adjust according to the required operation mode
  • a stirring device is provided in each reaction chamber, and the first reaction chamber and the third reaction chamber are stirred in the same direction
  • the second reaction chamber and the fourth reaction chamber are stirred in the same direction, and the stirring direction of the stirring device in the first reaction chamber and the second reaction chamber is opposite;
  • the aeration device is distributed in each reaction chamber, and a suspension carrier is added in each reaction chamber;
  • the starting method in turn includes the following steps:
  • a start preparation, adding a suspension carrier in each reaction chamber, the filling rate is 20%-67% ; aerobic sludge inoculation, the sludge concentration in each reaction chamber are 3-5g/L;
  • CANON pre-startup adopts the dual series A operation mode
  • the specific operation mode is: the first reaction chamber and the second reaction chamber are a group, and the third reaction chamber and the fourth reaction chamber are In one group, the sewage to be treated continuously enters the first reaction chamber and the fourth reaction chamber through the first water inlet and the fourth water inlet respectively, and the water in the first reaction chamber enters the second reaction chamber by controlling the relevant valves, so that the fourth reaction The water in the room enters the third reaction chamber and is finally collected and discharged to the second water collection well; the first reaction chamber and the second reaction chamber control D 0 at 1-2 mg/L, and the aeration intensity> 3 m 3 /m 2 /h, stirring The rotation speed of the device is 30-45r/min, the total ammonia oxidation rate of the first and second reaction chambers is >50%; the control of DO in the fourth and third reaction chambers is 3-6mg/L, exposure Gas intensity>5m Vm 2 /h, the total ammonia
  • CANON inoculation starts, using the described double series A operation mode, inoculate CAN ON suspension carrier into the first reaction chamber, inoculation rate is 3-5%, control DO at 0.5-1.5mg/L, aeration Intensity>2m 3 /m 2 /h, control the stirring device speed 15-30r/min; the second reaction chamber controls DO at l-2mg/L, aeration intensity>3m 3 /m 2 /h, stirring device speed 15- 30r/min; the fourth and third reaction chambers control DO at 3-6mg/L, the aeration intensity> 5m Vm 2 /h, the total ammonia oxidation rate of the fourth and third reaction chambers>50%; operation Until the surface load of TN in the first reaction chamber is removed>0.8gN/m 2 /d, enter the next step;
  • the specific operation mode is: the first reaction chamber, the second reaction chamber, the third reaction chamber as a group, the fourth reaction chamber As a group, the sewage to be treated continuously enters the first reaction chamber and the fourth reaction chamber through the first water inlet and the fourth water inlet respectively, and the water in the first reaction chamber enters the second reaction chamber and the third by controlling relevant valves In the reaction chamber, the effluent is finally collected and discharged to the first water collection well; the first reaction chamber controls DO at 1.5-3.5mg/L, and the aeration intensity is> 5m 3 /m 2
  • the speed of the stirring device is 15-30r/min; the second reaction chamber controls DO at 0.5-1.5mg/L, and the aeration intensity>1.5 m 3 /m 2
  • the speed of the stirring device is 30-45r/min;
  • the third reaction chamber controls DO at l-2mg/L, the aeration intensity is >3m 3 /m 2/h, the speed of the stirring device is 30-45r/min;
  • the fourth reaction chamber Control DO at 3-6mg/L, aeration intensity>5m 3 /m 2/h, ammonia oxidation rate>50%; run until the TN removal surface load of the second reaction chamber>1.6gN/m 2 /d, enter the next step;
  • the rotation speed of the stirring device is 15-30r/min; run until the TN of each reaction chamber removes the surface load>1.6gN/m 2 /d, enter the next step;
  • each reaction chamber controls DO at 2.0-5.0 mg/L, aeration intensity> 5m 3 /m 2 /h, stirring device rotation speed 30-45r/min, ammonia nitrogen concentration in the effluent of each reaction chamber is 60-100mg/L, TN removal table of each reaction chamber Area load> 2.5gN/m 2 /d; when TN removal rate requires 280%, adopt double series A operation mode, the first reaction chamber and the fourth reaction chamber both control DO at 2.0-5.0mg/L, aeration intensity >6m 3 /m 2 /h, stirring device rotation speed 30-45r/min, TN removal rate>50%, the second and third reaction chambers are controlled DO at 1.5-2.5mg/L, aeration intensity>3m 3 /m 2 /h, stirring device speed 15-30r/min.
  • the reaction tank is divided into four reaction chambers through a partition plate, which is arranged by a first water collection well, a second water collection well, and controlled by related valves, which can realize three different control modes different from the prior art, That is: by controlling the water outlet direction from the first reaction chamber to the fourth reaction chamber, the reaction chambers are connected in series, in parallel, or separately, and by using these three control methods, the inoculation ratio is small and the startup is fast.
  • a partition plate which is arranged by a first water collection well, a second water collection well, and controlled by related valves, which can realize three different control modes different from the prior art, That is: by controlling the water outlet direction from the first reaction chamber to the fourth reaction chamber, the reaction chambers are connected in series, in parallel, or separately, and by using these three control methods, the inoculation ratio is small and the startup is fast.
  • the above influent that is, sewage to be treated, C/N ⁇ 1; in the above steps c) to g), the sludge concentration in each reaction chamber is ⁇ 0.5g/L;
  • the power of the reaction chamber stirrer is 20-50W/m 3
  • the above-mentioned diversion device includes a first diversion valve, a second diversion valve, a third diversion valve, and a fourth diversion valve, wherein the above-mentioned first diversion device
  • the valve is located on the vertical downward partition connected to the first water collection well
  • the second diversion valve is located on the horizontal left partition connected to the first water collection well
  • the fourth diversion valve is located A horizontally-connected partition board connected to a water collection well
  • the above-mentioned third diversion valve is located on a vertically downward partition board connected to the second water collection well
  • there is also provided at the first water collection well for controlling each A first water outlet valve, a second water outlet valve, a third water outlet valve, and a fourth water outlet valve in the reaction chamber, a fifth water outlet valve and a sixth water outlet valve for controlling the water outlet in the reaction chamber are provided at the second water collection well .
  • the aeration device in each reaction chamber is composed of multiple sets of perforated aeration tubes and microporous aeration tubes
  • a return pump is provided in both the first and second water collection wells, the return pump is connected to a return pipe, and the other end of the return pipe returns to the first reaction chamber and
  • the water collection device further includes a seventh water outlet valve and an eighth water outlet valve, the seventh water outlet valve is located at a water outlet port connected to the first water collection well, and the eighth water outlet The valve is located above Connected to the outlet of the second water collection well.
  • the specific steps of the above-mentioned parallel operation mode are: the sewage to be treated respectively enters the reaction chambers continuously through the first water inlet, the second water inlet, the third water inlet and the fourth water inlet, and the effluent passes through the first The water outlet screen, the second water outlet screen, the third water outlet screen and the fourth water outlet screen, then pass the first water outlet valve, the second water outlet valve, the third water outlet valve and the fourth water outlet valve to the first water collection well, and finally Discharge from the water outlet pipe.
  • the specific steps of the above-mentioned double series A operation mode are: the sewage to be treated respectively enters the first reaction chamber and the fourth reaction chamber continuously through the first water inlet and the fourth water inlet, and the first reaction chamber effluent passes through the first A water outlet screen, a second diversion valve, and a second water outlet screen enter the second reaction chamber, pass through the fifth water outlet screen, the fifth water outlet valve, and the second water collection well, and then merge into the water outlet pipe; the water in the fourth reaction chamber Enter the third reaction chamber through the fourth outlet screen, the fourth diversion valve, and the third outlet screen.
  • the outlet of the third reaction chamber passes through the sixth outlet screen, the sixth outlet valve, and the second water collection well, and then merges into the outlet pipe Out of water.
  • the specific steps of the above-mentioned double series B operation mode are: the sewage to be treated continuously enters the first reaction chamber and the fourth reaction chamber through the first water inlet and the fourth water inlet respectively, and the first reaction chamber effluent passes through the first A water outlet screen, a second diversion valve, and a second water outlet screen enter the second reaction chamber, and the water in the second reaction chamber passes through the fifth water outlet screen, third diversion valve, and sixth water outlet screen to the third reaction chamber
  • the reaction chamber, the third reaction chamber effluent passes through the third outlet screen, the third outlet valve, and the first water collection well into the outlet pipe; the fourth reaction chamber effluent passes through the fourth outlet screen, the fourth outlet valve, the first After collecting the well, the water will flow into the outlet pipe.
  • the inoculation ratio is small, the inoculation ratio does not exceed 5%;
  • the start-up scale is large, suitable for large-scale project scale start-up;
  • the operation mode is flexible, and the water outlet direction of the four-cell reaction chamber is controlled by the diversion structure according to the water outlet standard to realize the series, parallel or separate operation of the reaction chamber to achieve stable operation;
  • the load is high, occupying a province, the volume load can reach up to 1.5kgN/m 3 /d;
  • the operation control is simple, the system adopts the MBBR form, the carrier is highly enriched in effective strains, and the processing load is high.
  • FIG. 1 is a plan view of the MBBR autotrophic denitrification system of the present invention
  • FIG. 2 is a left side view of the MBBR autotrophic denitrification system of the present invention
  • FIG. 3 is a plan view of the piping layout of the MBBR autotrophic denitrification system of the present invention.
  • FIG. 4 and FIG. 5 are schematic structural views of a flow guiding device in the present invention.
  • FIG. 6 is a schematic cross-sectional view of a flow guiding device
  • the present invention proposes a quick start method of MBBR full autotrophic denitrification system.
  • the present invention will be described in detail below in conjunction with specific embodiments.
  • Porosity the ratio of the volume occupied by the carrier itself to the natural accumulation volume of the carrier
  • CANON That is the whole process of autotrophic denitrification, which refers to the realization of nitrosation and anaerobic ammonia oxidation by controlling dissolved oxygen in a single reactor or biofilm, so as to achieve the purpose of nitrogen removal.
  • autotrophic denitrification which refers to the realization of nitrosation and anaerobic ammonia oxidation by controlling dissolved oxygen in a single reactor or biofilm, so as to achieve the purpose of nitrogen removal.
  • Ammonia oxidizing bacteria partially oxidize ammonia nitrogen to nitrous acid.
  • the generated nitrous acid and part of the remaining ammonia nitrogen undergo ANAMMOX reaction under the action of anaerobic ammonia oxidizing bacteria (AnAOB) to generate nitrogen;
  • 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%;
  • Ammonia oxidation surface load the mass of ammonia nitrogen oxide per unit specific surface area per day, gN/m 2 /d; if the influent ammonia nitrogen is 500 mg/L, the effluent ammonia nitrogen is 100 mg/L, and the influent flow rate is 10 m 3
  • the biofilm area is 2000m 2
  • the surface load of ammonia oxidation is (500-100)
  • xl0/2000 2gN/m 2 /d
  • TN removal surface load the total nitrogen mass removed per unit effective specific surface area per day, gN/m 2 /d
  • the biofilm area is 2000m 2
  • TN removal rate the ratio of the total nitrogen removal to the total nitrogen in the influent
  • MBBR Moving bed biofilm reactor MBBR (Moving Bed Biofilm Reactor) This method increases the biomass and species of the reactor by adding a certain amount of suspension carrier to the reactor, thereby improving the reactor Processing efficiency;
  • Nitrosification the process of microorganisms oxidizing ammonia nitrogen (NH 4 + ) to nitrite nitrogen (N0 2- ) without further oxidation to nitrate nitrogen (N0 3- ), that is, enrichment in the system Ammonia oxidizing bacteria (AOB), while eliminating nitrite oxidizing bacteria (NOB);
  • Carbon-to-nitrogen ratio refers to the ratio of the total content of organic matter in sewage to the total content of nitrogen, generally expressed as "C/N", and the content of organic matter refers to the five-day BOD (BOD 5 ), the nitrogen content is total nitrogen, such as BOD 5 in sewage
  • Aerobic sludge activated sludge in the aerobic section of the sewage plant biochemical tank, mainly used to inoculate nitrifying bacteria, to speed up the startup speed;
  • CANON suspension carrier that is, a suspension carrier with CANON effect, AOB and AnAOB both exist in layers in the form of biofilms;
  • the activated sludge method is usually 3-5W/m 3 ;
  • the activated sludge method is usually 3-5W/m 3 ;
  • the stirring power is related to the filling rate. The higher the filling rate, the greater the stirring power.
  • first reaction chamber, second reaction chamber, third reaction chamber, fourth reaction chamber are referred to as Cl, C2, C3, C4, first diversion valve, second diversion valve, third diversion Valve, the fourth diversion valve is referred to as FI, F2, F3, F4, the first outlet valve, the second outlet valve, the third outlet valve...
  • the eighth outlet valve is referred to as Ml, M2, M3... M8, the first The water inlet pipe of the first reaction chamber, the water inlet pipe of the second reaction chamber, the water inlet pipe of the third reaction chamber, and the water inlet pipe of the fourth reaction chamber are LI, L2, L3, L4 in this order, and the first and second water collection wells are respectively For Kl, K2.
  • an MBBR full-process autotrophic denitrification system as shown in FIGS. 1 to 3, includes a reaction tank body 1, a stirring device 3, an aeration device, a diversion device 5, and a water collection device
  • the interior of the main body of the reaction cell is divided into two rows and two columns of four reaction chambers by a partition 2, which are respectively a first reaction chamber, a second reaction chamber, a third reaction chamber and a fourth reaction chamber, wherein the first reaction chamber and the first reaction chamber The four reaction chambers are in a row and located at the bottom.
  • the first reaction chamber and the second reaction chamber are in a row, which is equivalent to the first reaction chamber is located at the lower left, and then the second reaction chamber, the third reaction chamber and the first reaction chamber are clockwise.
  • the center of the partition does not cross, and the center of the partition is the water collecting device and the flow guiding device.
  • a first water inlet and a fourth water inlet are respectively provided below the sides of the first reaction chamber and the fourth reaction chamber, and water is fed into them through L1 and L4, and the sides above the second reaction chamber and the third reaction chamber are respectively Equipped with a second water inlet And the third water inlet, into which water is fed through L2 and L3, the first water outlet, the second water inlet, the third water inlet and the fourth water inlet are diagonally provided with a first water outlet screen and a second water inlet respectively
  • the outlet screen, the third outlet screen and the fourth outlet screen, the first outlet screen, the second outlet screen, the third outlet screen and the fourth outlet screen are all arranged diagonally and form a relatively closed area;
  • the water collecting device includes a first water collecting well, a second water collecting well and water pipes connected thereto, and the first water collecting well is located in a relatively closed area at the central position of the four reaction chambers. After the sewage in the reaction tank is collected, it is discharged through the water outlet pipe 4.
  • a seventh water outlet valve is provided at the outlet of the water outlet connected to the first water collection well K1. The seventh water outlet valve is opened, and the sewage can be discharged from the water outlet pipe .
  • a fifth water outlet screen and a sixth water outlet screen are also provided above the second reaction chamber and the third reaction chamber, and a second water collection well K2 is provided in the area formed by the two, the second collection The water well is used to collect the sewage in the reaction tank and discharge through the above water outlet pipe;
  • the above-mentioned diversion device is used to control the flow direction of water in the reaction chamber and adjust according to the required operation mode
  • a stirring device is provided in each reaction chamber, and the first reaction chamber and the third reaction chamber are stirred in the same direction, the second reaction chamber and the fourth reaction chamber are stirred in the same direction, the first reaction chamber and the second reaction chamber
  • the stirring direction of the stirring device is opposite, and the specific structure and operation mode of the stirring device can be realized by referring to the existing technology.
  • the stirring device can use a variable frequency mixer.
  • the aeration device is distributed in each reaction chamber, and a suspension carrier is added in each reaction chamber.
  • the aeration device in each reaction chamber is composed of multiple sets of perforated aeration pipes 6 and microporous aeration pipes 7 arranged at intervals, and each set of perforated aeration pipes is arranged along the length of the reaction chamber;
  • a micro-power aeration tube 8 is provided on one side of the net to prevent the outlet screen from being blocked.
  • a return pump is provided in both the first and second water collection wells, and the return pump is connected to the return pipe 9, and the other end of the return pipe is returned to the front ends of the first reaction chamber and the fourth reaction chamber.
  • the water device further includes a seventh water outlet valve and an eighth water outlet valve. The seventh water outlet valve is located on the water outlet pipe connected to the first water collection well, and the eighth water outlet valve is located on the water outlet pipe connected to the second water collection well.
  • the structure of the preferred flow guiding device of the present invention is as follows.
  • the first diversion valve is located on a vertically downward partition connected to the first water collection well
  • the second diversion valve is located on the horizontally-left partition connected to the first water collection well
  • the fourth diversion valve is located on the horizontally right connecting to the first water collection well
  • the third diversion valve is located on the vertically downward partition connected to the second water collection well
  • the first water collection valve is also provided with a first water outlet valve and a second water outlet for controlling the water outlet in each reaction chamber
  • the valve, the third water outlet valve and the fourth water outlet valve are provided with a fifth water outlet valve and a sixth water outlet valve for controlling water outlet in the reaction chamber at the second water collection well.
  • the flow direction of each reaction chamber is controlled by a flow guiding device.
  • the operating process has the following three control modes:
  • Double series A operation mode the sewage to be treated respectively enters the reaction chamber C1 continuously through the water inlet pipes LI and L4
  • Double series B operation mode the sewage to be treated respectively enters the reaction chamber C1 continuously through the water inlet pipes LI and L4
  • the startup method of the present invention includes the following steps:
  • the suspension carrier is added to the reaction chamber, the filling rate is 20%-67% ; aerobic sludge inoculation, the sludge concentration in each reaction chamber is 3-5g/L;
  • CANON inoculation starts, using double series A operation mode, continuous water infusion; inoculate CAN1 with CON suspension carrier, inoculation rate is 3-5%, control DO at 0.5-1.5mg/L, aeration intensity> 2m 3 /m 2 /h, control the agitator speed 15-30r/min; C2 control DO at l-2mg/L, aeration intensity> 3m 3 /m 2 /h, agitator speed 15-30r/min; C4, C3 controls DO at 3-6mg/L, aeration intensity>5m 3 /m 2 /h, C4 and C3 total ammonia oxidation rate>50%; Operation until C1 TN removal surface load>0.8gN/m 2 /d, Go to the next step
  • C2 control DO is 0.5-1.5mg/L, aeration intensity>1.5m 3 /m 2 /h, stirring device speed 30-45r/min;
  • C3 control DO at l -2mg/L, aeration intensity>3m 3 /m 2 /h, stirring device speed 30-45r/min;
  • C4 control DO at 3-6mg/L, aeration intensity>5m 3 /m 2
  • the speed of the stirring device is 30-45r/min
  • the ammonia nitrogen concentration in the effluent of each reaction chamber is 60-100mg/L
  • the TN removal surface load of each reaction chamber is> 2.5gN/m 2 /d; when the TN removal rate is required to be> 80%
  • the rotation speed of the stirring device is 15-30r/min, and the ammonia nitrogen in the C2 or C3 effluent is 30-50mg/L.
  • C1 and C3 are in the same stirring direction, C2 and C4 are in the same stirring direction, and C1 and C2 are in the opposite stirring direction; the difference in the stirring direction is mainly to prevent the short flow phenomenon of the inlet water, such as when using the double series A operation mode,
  • the sewage to be treated enters Cl through the first water inlet, and the C1 effluent enters C2 through the first effluent screen, the second diversion valve, and the second effluent screen.
  • the stirring direction of C1 and C2 is opposite.
  • the outlet screen, the fifth outlet valve, and the second water collection well will be discharged into the outlet pipe, otherwise C1 and C2 will be stirred in the same direction, and the sewage will not directly react through the fifth outlet screen, the fifth outlet valve, and the second set in C2. After the well, it enters the outlet pipe and discharges
  • nitrosation start control DO is 3-6mg/L, the main reason is to increase the ammonia oxidation rate by controlling the DO to accelerate the nitrosation film; CANON pre-start, CANON inoculation start, CAN ON flow Adding lower start-up control DO is to provide an anaerobic environment for CANON biofilm, and to ensure the survival environment of Anammox. CANON runs stably.
  • the DO level is adjusted to meet the requirements of biofilm layering; biofilm
  • biofilm The important difference between the method and the activated sludge method is that the presence of microorganisms is in the attached or suspended state; suspended microorganisms are not subject to mass transfer restrictions, while the attached state is transferred through the matrix gradient, which requires high mixing and shearing;
  • the operation mode is different in each stage, mainly considering the inoculation mode and operation mode;
  • 45r/min is to assist the fluidization of the carrier when the aeration is insufficient, CANON inoculation start, CANON expansion start control stirring speed 15-30r/min to prevent excessive shear force caused by biofilm fall off, CANON stable operation control stirring speed 30-45r/ min is to prevent thickening of biofilms with small shear forces;
  • the sludge concentration in each reaction chamber is ⁇ 0.5g/L, mainly to ensure the effect of pure membrane, that is, microorganisms mainly exist in the form of attached state, when the concentration of suspended sludge increases, it will compete with biofilm Relationship, affecting biofilm growth.
  • microporous aeration and perforated aeration achieves the same DO requirement and different aeration intensity by adjusting the ratios of the microporous aeration and perforated aeration flow rates.
  • 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 inlet water, the water volume is 2500m 3 /d, the pH value is 7.9-8.2, the water temperature is 30-35°C, and the inlet water COD concentration is 300-500mg/L, The average ammonia nitrogen concentration is 821mg/L, and the total effective volume of the reaction cell is 1200m. It is evenly divided into four compartments. The effective volume of each compartment is 300m3. The influent enters the four compartments.
  • the suspension carrier is added in the reaction chamber, the effective specific surface area of the carrier is 800m 2 /m 3
  • the void rate is 90%, the filling rate is 55%; the aerobic sludge is inoculated, and the sludge concentration in each reaction chamber is about 4.3g/L;
  • the aeration intensity is 3.3m 3 /m 2
  • CANON inoculation starts, inoculates CANON suspension carrier to Cl, the inoculation rate is 4%, the control DO is 0.8-1
  • C2 controls DO at 1-2mg/L, controls the speed of the stirring device at 20r/min, and the aeration intensity is 3.5m 3 /m 2 /h.
  • C3 and C4 control DO at 3-3.5mg/L and aeration intensity 5.1m 3 /m 2 /h. After 35 days of operation, the total ammonia oxidation rate of C3 and C4 remains above 70%, and the surface load of TN removal of C 1 exceeds 1.62gN/m 2 /d.
  • C1 controls the rotation speed of the stirring device 30 r/min, controls the DO at 2.5-3.0 mg/L, and the aeration intensity is 5.5 m 3 /m 2 /h.
  • C2 controls the speed of the stirring device at 35r/min, controls DO at about 1.5mg/L, the aeration intensity is 3.0m 3 /m 2 /h,
  • C4 controls DO at 3.5-4.0mg/L, the aeration intensity is 6m 3 /m 2 /h, the ammonia oxidation rate remains about 75%.
  • C3 controls DO at about 2mg/L, and the aeration intensity is 3.0m 3 /m 2 /h.
  • the TN removal surface load of C2 reached 1.63gN/m 2 /d, and the next step was entered;
  • the ammonia nitrogen in C2 or C3 effluent is about 40mg/L.
  • the membrane load of each reaction chamber can reach a maximum of 3.44gN/m 2 /d, and the corresponding volume load can reach a maximum of 1.51kgN/m 3 /d.
  • the suspension carrier is added in the reaction chamber, the effective specific surface area of the carrier is 800m 2 /m 3
  • the void rate is 90%, the filling rate is 50%; the aerobic sludge is inoculated, and the sludge concentration in each reaction chamber is about 4.0g/L;
  • the aeration intensity is 3.5m 3 /m 2
  • C2 controls DO at 1-2mg/L, controls the speed of the stirring device at 20r/min, and the aeration intensity is 3.5m 3 /m 2 /h.
  • C3 and C4 control DO at 3-3.5mg/L and aeration intensity 5.1m 3 /m 2 /h.
  • C2 controls the speed of the stirring device at 35r/min, controls DO at about 1.5mg/L, the aeration intensity is 3.0m 3 /m 2 /h, C4 controls DO at 3.5-4.0mg/L, the aeration intensity is 6m 3 /m 2 /h, the ammonia oxidation rate remains about 75%.
  • C3 controls DO at about 2mg/L, and the aeration intensity is 3.0m 3 /m 2 /h. After 32 days of operation, the TN removal surface load of C2 reached 1.63gN/m 2 /d, and the next step was entered;
  • CANON expansion start replacing 50% of the suspended carrier in the C4 and C3 reaction chambers with the C1 and C2 reaction chambers; each cell controls DO at 2.5-3.0 mg/L, and the aeration intensity is 4.5 m Vm 2 /h .
  • the surface load of each reaction chamber TN was removed more than 1.66gN/m 2 /d, and the next step was entered;
  • each reaction chamber controls DO at 3.5 mg/L, aeration intensity 5.0 m 3 /m 2 /h, total nitrogen removal rate reaches 80%; effluent ammonia nitrogen is at 90 mg/ Around L.
  • the membrane load of each reaction chamber reaches a maximum of 1.80 gN/m 2 /d.
  • the present invention realizes the series, parallel or separate operation of the reaction chamber by controlling the water outlet direction of the four-cell reaction chamber through the diversion device; the rapid start of the autotrophic denitrification process is achieved by means of low proportion inoculation and series start; according to the requirements of the treatment standard, Realize different process layout forms.

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  • 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)

Abstract

L'invention concerne un procédé de démarrage rapide d'un système d'élimination d'azote entièrement autotrophe de bioréacteur à lit mobile. Selon la présente invention, un corps de cuve de réaction (1) est divisé en quatre chambres de réaction (C1-C4) au moyen d'une cloison (2); des dispositifs d'agitation (3), un dispositif d'aération, un dispositif de guidage d'écoulement (5) et un dispositif de collecte d'eau sont disposés dans les chambres de réaction (C1-C4), le dispositif d'aération est réparti dans chacune des chambres de réaction (C1-C4), et un support de suspension est ajouté à chacune des chambres de réaction (C1-C4); trois modes de fonctionnement peuvent être mis en œuvre lors du démarrage, et sont respectivement un mode de fonctionnement parallèle, un mode de fonctionnement à double série A et un mode de fonctionnement en double série B; le dispositif de guidage d'écoulement (5) commande les directions de sortie d'eau des chambres de réaction (C1-C4) pour mettre en œuvre une connexion en série, une connexion parallèle et un fonctionnement indépendant des chambres de réaction dans les modes de fonctionnement; et un démarrage rapide d'un processus d'élimination d'azote autotrophe est mis en œuvre par le biais des étapes de préparation de démarrage, un démarrage de nitrification, un prédémarrage du procédé CANON, un démarrage d'inoculation du procédé CANON, un démarrage d'addition d'écoulement du procédé CANON, un démarrage d'expansion du procédé CANON et un fonctionnement stable du procédé CANON. Le procédé de démarrage présente les avantages d'un faible taux d'inoculation et d'un démarrage rapide.
PCT/CN2019/079824 2018-12-05 2019-03-27 Procédé de démarrage rapide d'un système d'élimination d'azote entièrement autotrophe de bioréacteur à lit mobile WO2020113863A1 (fr)

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