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WO2012036408A2 - Bioréacteur à membrane submergée qui réagit facilement à la régulation de la charge, et méthode de traitement des eaux usées l'utilisant - Google Patents

Bioréacteur à membrane submergée qui réagit facilement à la régulation de la charge, et méthode de traitement des eaux usées l'utilisant Download PDF

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Publication number
WO2012036408A2
WO2012036408A2 PCT/KR2011/006608 KR2011006608W WO2012036408A2 WO 2012036408 A2 WO2012036408 A2 WO 2012036408A2 KR 2011006608 W KR2011006608 W KR 2011006608W WO 2012036408 A2 WO2012036408 A2 WO 2012036408A2
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Prior art keywords
membrane
sewage
air
tank
treatment step
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PCT/KR2011/006608
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English (en)
Korean (ko)
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WO2012036408A3 (fr
Inventor
엄태경
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Eum Tae-Kyoung
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Publication of WO2012036408A2 publication Critical patent/WO2012036408A2/fr
Publication of WO2012036408A3 publication Critical patent/WO2012036408A3/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/145—Ultrafiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/147—Microfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B01D61/18—Apparatus therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • 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
    • C02F3/1273—Submerged membrane bioreactors
    • 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
    • C02F3/28—Anaerobic digestion processes
    • C02F3/2813—Anaerobic digestion processes using anaerobic contact processes
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2315/00—Details relating to the membrane module operation
    • B01D2315/06—Submerged-type; Immersion type
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/18—Use of gases
    • B01D2321/185—Aeration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/002—Construction details of the apparatus
    • C02F2201/005—Valves
    • 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
    • C02F2209/04—Oxidation reduction potential [ORP]
    • 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
    • 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
    • C02F3/006—Regulation methods for biological 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
    • C02F3/308—Biological phosphorus removal
    • 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 relates to a membrane bioreactor used for sewage or wastewater treatment, and more particularly, to a submerged membrane bioreactor and a sewage treatment method using the same. will be.
  • protozoa-induced lesions in the intestinal tract are not included in the water quality criteria, but are also removed by chlorine disinfection. The difficulty is increasing the need to remove these.
  • Membrane bioreactors replace the precipitation function with membranes in conventional bioreactors, and microfiltration membranes (MF) and ultrafiltration membranes are widely used in general applications. It is widely used because it is very effective for removing suspended solids, bacteria and protozoa.
  • the amount of air required for membrane cleaning is 00 to 150 m 3 / itf.hr for the bottom area of the membrane, and the inflow load must be continuously supplied and cleaned at the time the membrane is operating regardless of the load of sewage. If less, the amount of air required for membrane cleaning may be much greater than the amount of air needed for biological treatment in the aerobic tank. Since the dissolved oxygen concentration of excessively increases, there is a big problem that the dissolved oxygen concentration in the aerobic tank cannot be adjusted to an appropriate value.
  • the amount of cleaning air required for membrane cleaning is large and cannot be changed (reduced). Therefore, when the load of sewage flowing into the immersion membrane bioreactor is small, excess oxygen is supplied to the aerobic tank to increase the dissolved oxygen concentration. Total nitrogen and total nitrogen by increasing the dissolved oxygen concentrations in the anaerobic and anaerobic tanks, which are returned from the aerobic tank, and the anaerobic and anaerobic tanks to be aerobic, resulting in no phosphorus release or denitrification of microorganisms that occur only in anaerobic conditions. Phosphorus removal is extremely low or causes problems that cannot be removed.
  • the amount of cleaning air of the filtration membrane described above corresponds to the amount of air required for the sewage treatment of the inflow sewage B0D concentration of 100 mg / L, the above problems occur in the advanced treatment of sewage having a lower B0D concentration.
  • the above example illustrates the case of a microfiltration membrane (MF), but in the case of a high-treatment process in which an ultrafiltration (UF) membrane is applied to a bioreactor with a similar amount of membrane cleaning air but a much smaller membrane permeation rate than a microfiltration membrane.
  • MF microfiltration membrane
  • UF ultrafiltration
  • the amount of air required for cleaning becomes more excessive, and the influence on the advanced treatment process is absolute, and thus the application is further limited.
  • the needle In sewage or wastewater treatment, even when the inflow load is low, the needle can maintain the membrane cleaning ability, and easily adjust the dissolved oxygen concentration in the aerobic tank to facilitate the change of load, and always maintain the normal treatment capacity.
  • the present invention provides a membrane bioreactor and a sewage treatment method using the same.
  • ⁇ 21> Inject air from the membrane cleaner blower to the diffuser installed in the lower part of the immersion membrane filter in the membrane filtration tank, and wash the surface of the membrane of the immersion membrane filter by using the air cleaning function. After washing, some or all of the rising air (gas) is circulated to the inlet of the membrane cleaning blower to clean the membrane filter, and the dissolved oxygen concentration of the membrane filter tank is adjusted by adjusting the ratio of the circulating gas amount and the air amount.
  • a sewage treatment method using an immersion membrane bioreactor that can easily cope with load fluctuation, wherein the sewage from the degassing treatment step is returned to the anaerobic treatment step and the anaerobic treatment step.
  • the immersed membrane bioreactor of the present invention maintains the cleaning function by cleaning the air necessary for cleaning the membrane using a separate blower and recirculating some or all of the air rising above the water surface.
  • the dissolved oxygen concentration in the membrane filtration tank can be maintained appropriately by adjusting the ratio of the gas volume and the air volume to be recycled, and the appropriate dissolved oxygen concentration can be maintained by controlling the air volume separately by installing an acid base and an aerobic blower in the aerobic tank. Even under heavy load fluctuations, it is easy to respond, so that the sewage can always be treated in the best condition.
  • Figure 2 is an exemplary view of the second A / 0 processes using a membrane filtration aerobic tank of the present invention.
  • FIG 3 is an exemplary diagram of an aerobic denitrification process using the membrane filtration tank of the present invention.
  • FIG. 4 is a diagram illustrating the configuration of the anaerobic tank of the present invention.
  • 5 is an exemplary view of the configuration of an aerobic denitrification tank of the present invention.
  • FIG. 6 is an exemplary view of the configuration of the membrane filtration tank of the present invention.
  • FIG. 7 is a diagram illustrating the configuration of an aerobic tank according to the present invention.
  • FIG. 9 is an embodiment of an aerobic tank used in the small sewage treatment facility of the present invention.
  • Membrane filters form a unit by fixing a membrane to a frame and combining these units together to form a membrane filter.
  • Membranes include microfiltration membranes (MF) and ultrafiltration membranes, depending on the eye size.
  • UF ultrafiltration membrane
  • NF nano membrane
  • R0 reverse osmosis membrane
  • microfiltration membrane and ultrafiltration membrane are mainly used for advanced treatment of sewage and wastewater.
  • the microfiltration membrane has a pore size in the range of 0.1 to 0.4, and can generally remove bacteria, Escherichia coli, protozoa, and fine suspended solids (SS).
  • the ultrafiltration membrane has a pore size in the range of 0.001 to 0.05 mi, and can usually remove bacteria, E. coli, protozoa and viruses, and fine suspended solids (SS).
  • Membrane filters have a very good performance in water treatment as described above, while the eye size is so small that they tend to be clogged.
  • the membrane filter is immersed in the aerobic tank in which a large microbial floc is present, and the membrane filter is installed at the lower part of the membrane filter to prevent the membrane filter. Air is blown through the device to prevent clogging of the outer surface of the membrane filter using the cleaning power of air bubbles blown out from the diffuser.
  • the amount of air used to clean the membrane filter generally corresponds to the bottom area of the membrane filter.
  • hypochlorite solution is periodically refluxed inside the hollow fiber membrane to clean the contaminants attached to the membrane.
  • the amount of air cleaning the membrane filter is a fixed value and must be kept constant at all times, regardless of the inflow load of sewage.
  • the air volume required in the aerobic tank decreases.
  • the inflow load of sewage during the commissioning stage or the initial stage of operation is typically 30 ⁇ 50 ⁇ 3 ⁇ 4 Since there are many places, the air volume required for the aerobic tank should also be supplied only 30-50% of the air volume calculated during design.
  • the amount of air required for the membrane filter is usually 70 «3 ⁇ 4 of the total required air volume, so that the aerobic tank becomes an excessively high dissolved oxygen concentration, and therefore, the anaerobic tank and the anoxic tank also become aerobic, which leads to extremely low nitrogen removal efficiency. And a treatment method using a membrane filter causes a problem in operation at the initial low load for the same reason.
  • nitrogen is 78% and oxygen is 21%.
  • concentration of nitrogen and oxygen in water is determined by each Henry's constant.
  • Henry's constant E of nitrogen is 9.24 (EX10 -4 ) for water at 30 ° C
  • Henry's constant of oxygen is 4/75 (EX10 ⁇ 4 )
  • the larger the Henry's constant the less dissolved in water.
  • nitrogen is dissolved in water about 1/2 times less than oxygen, and in nitrogen at low pressure, inorganic nitrogen is dissolved at a low solubility that is equilibrium with the partial pressure of nitrogen gas in the air. Since it is not consumed by the air, nitrogen is not further dissolved even if it is continuously given up by supplying air or nitrogen gas into sewage.
  • the oxygen gas ratio decreases as much as dissolved, but the nitrogen gas remains as it was originally supplied, collects the air used for cleaning, and enters the membrane cleaning blower 620.
  • the oxygen gas rate is lowered and reduced to the partial pressure equilibrated with the dissolved oxygen concentration in the water. If no external air is supplied, all the oxygen in the circulating gas is consumed, and the oxygen partial pressure becomes zero, and the dissolved oxygen concentration in the membrane filtration tank becomes zero, resulting in anaerobic condition. will be.
  • the circulating gas is supplied to the inlet of the membrane cleaning blower, and only a part of the external air is supplied to adjust the ratio of the circulating gas amount and the external air amount, for example, when the inflow load of the sewage is small, the external air supply amount is reduced.
  • the inflow load of sewage increases, it increases the external air supply, circulates the circulating gas, maintains the amount of gas necessary for membrane cleaning, and effectively washes the membrane filter, while easily maintaining the dissolved oxygen concentration in the membrane filtration tank to the desired level. I can regulate it.
  • the membrane filtration treatment step is configured using the same principle as above, and the configuration of the membrane filtration tank of the membrane filtration step is shown in FIG. 6.
  • the membrane filter 630 is installed in the water of the membrane filtration tank 610, and the membrane cleaning air diffuser 640 is installed below the membrane filter, and the membrane cleaning air diffuser is discharged from the outlet of the membrane cleaning blower 620.
  • An air line was connected to the inlet of the device 640.
  • a ventilation pipe 670 was provided in the shutoff cover to prevent negative pressure or static pressure from acting on the space sealed by the shutoff cover through the exhaust of remaining gas.
  • the circulating gas collected in the upper space of the membrane filtration tank is supplied to the membrane cleaning blower 620 through the gas circulation pipe 660 connected to the inlet pipe of the membrane cleaning blower 620 at the upper portion of the blocking cover 660.
  • the gas circulation pipe 660 connected to the inlet pipe of the membrane cleaning blower 620 at the upper portion of the blocking cover 660.
  • An inlet pipe is installed at the inlet side of the membrane cleaning blower 620 to suck external air, and an air volume control valve 690 is installed at the inlet pipe to adjust the intake air amount.
  • the membrane filtration tank is maintained while controlling the ratio of supplying circulating gas and external air to the membrane cleaning blower according to the load amount of the inflow sewage, while maintaining the air amount (gas amount) required for membrane cleaning.
  • the dissolved oxygen concentration in 610) can be easily adjusted to the desired concentration.
  • Figure 1 is an exemplary view configure the membrane using a filtration tank, A 2/0 process described above.
  • a 2/0 process is one of the advanced treatment process of wastewater treatment, the method for removing the organic matter as well as nitrogen and phosphorus at the same time, how the biological process contained in the sewage, the most widely used worldwide, showing a good treatment outcome .
  • Figure 1 shows a modification of the example 2 a standard A / 0 processes of the invention, numerous modifications, such as changing the process sequence or to a part omitted should be considered to be within the scope of the invention.
  • the sewage from which the contaminants and sand are removed is introduced into the flow adjustment tank in the flow adjustment step and the flow rate is reduced while staying for a predetermined time, and the sewage is transferred to the anaerobic treatment step 300, which is the next process, by the inflow pump.
  • the return water 1 (860) returned from the degassing treatment step (700) and the sewage are equally mixed in the anaerobic tank, and the microorganisms in the sewage discharge the phosphorus in the living body while remaining in the anaerobic state for a certain time. .
  • the 0RP (redox potential) value should be maintained at -300 ⁇ 400mV and the dissolved oxygen concentration should be kept below O.lmg / L.
  • the sewage that has passed through the anaerobic stage is sent to an anaerobic treatment stage 400.
  • the sewage and return water 2 flows into the anaerobic tank 410 and is mixed evenly by the action of the anaerobic tank stirrer 320.
  • the nitrate nitrogen is converted to inorganic nitrogen by the denitrification of the denitrifying bacteria in the anaerobic state, and released into the atmosphere, thereby removing nitrogen from the sewage.
  • the anaerobic and anaerobic tanks need to be sealed or covered with a top to prevent contact with oxygen or air.
  • the sewage that has passed the anaerobic treatment step is sent to the aerobic treatment step 500.
  • the aerobic treatment step the organic matter in the sewage is decomposed, nitrification is carried out to convert ammonia nitrogen to nitrate nitrogen, and the phosphorus-treated microorganism that has released phosphorus in the anaerobic treatment step 300 is about 2 to 6 times more than the normal phosphorus absorption amount.
  • Phosphorus over-absorption acts to absorb a larger amount of phosphorus in the vessel, and the phosphorus in the sewage is removed by releasing the excess phosphorus microorganisms into the excess sludge in the subsequent degassing step.
  • the aerobic treatment step maintains the dissolved oxygen concentration at 2.0 to 4.0 mg / L in the advanced treatment process for nitrogen and phosphorus removal.
  • the aerobic treatment step should be kept low unless the concentration of organic matter in the sewage is low, as long as it does not interfere with nitrification. It is desirable to maintain 1.5 ⁇ 2.0mg / L.
  • the air diffuser for supplying air as shown in FIG.
  • an aeration tank stirrer 520 for agitation may be optionally installed.
  • the sewage passing through the aerobic treatment step is transferred to the membrane filtration treatment step 600, as shown in FIG. 6, the supernatant is separated from the membrane filter 630, and the remaining sewage is transferred to the degassing treatment step 700.
  • the present invention can effectively clean the membrane filter by adjusting the ratio of supplying circulating gas and external air to the membrane cleaning blower 620, and also maintain the dissolved oxygen concentration in the membrane filter tank 610 in an appropriate range. It was. (See Figure 6)
  • the sewage remaining after separating the supernatant from the membrane filtration treatment step (600), is maintained in the degassing step (700) with the air supply interrupted for a certain time, so that the dissolved oxygen concentration in the sewage to less than 0.5mg / L Lowering, a part is returned to the anaerobic treatment step 300 (860), and a part is returned to the anaerobic treatment step 400 (850).
  • Returning refers to the transfer of a mixture containing sewage and activated sludge to an anaerobic or anaerobic treatment step, and the returned sewage is called "return water"
  • the remaining sludge is more than the amount of sludge needed in the treatment process, and the excess sludge is disposed of by discharging it out of the process to remove phosphorus in the sewage due to the disposal of the excess sludge.
  • a stirrer it is preferable to install a stirrer to prevent sludge settling in the degassing step.
  • the sewage is treated while repeating the above process.
  • FIG. 2 is by way of illustration of A 2/0 process using a membrane filtration aerobic tank of the present invention, wherein Fig.
  • the sewage that has passed through the anaerobic treatment stage is an anaerobic treatment stage in the anaerobic treatment stage 400 and the sewage and return water 1 (850) evenly mixed in the anaerobic tank, the action of the stirrer, while staying in an anaerobic state for a certain time With the action of denitrifying bacteria, nitric acid nitrogen in sewage is converted to inorganic nitrogen gas and released into the atmosphere to remove nitrogen.
  • the sewage that has passed through the anaerobic treatment step is sent to the membrane filtration aerobic treatment step 500B.
  • a membrane filter 630 is installed in the internal water of the aerobic tank 510, and a membrane cleaning diffuser 640 is installed at the lower portion of the membrane filter to remove the membrane cleaner.
  • the outlets were connected by air piping.
  • an air diffuser 530 for supplying air to the exhalation tank was installed, and also connected to the discharge port of the membrane filtration exhalation tank blower 550 by an air pipe.
  • the upper portion of the exhalation tank 510 was installed by blocking the cover 650, the upper space of the exhalation tank was sealed by air, and the ventilation cover 670 was installed in the blocking cover to communicate with the atmosphere.
  • the aeration pipe is to prevent the occurrence of negative pressure (-pressure) or positive pressure (+ pressure) in the space above the aeration tank and to exhaust the air (circulating gas) remaining after the aeration.
  • a gas circulating pipe 660 was connected from the upper portion of the blocking cover 650 to the inlet of the membrane filtration aeration tank blower 550, and a circulating gas flow control valve 560 was installed in the gas circulation pipe. It was done.
  • an air inlet pipe for inhaling air in the atmosphere is installed, and an air volume control valve for adjusting the intake air amount is installed.
  • the opening degree of the air flow control valve 570 and the circulating gas flow control valve 560 provided at the inlet of the membrane filtration aerobic blower 550 is controlled. Adjust the ratio between the amount of intake air and the amount of circulating gas to achieve the desired dissolved oxygen concentration.
  • the amount of air sucked in and the amount of circulating gas change depending on the opening degree of the valve, the amount of air discharged from the membrane filtration aeration tank blower 550 (combined air of the air and the circulating gas) is constant. Due to the low load, the amount of air required to maintain the dissolved oxygen concentration appropriately decreases, so that even if the amount of air supplied from the outside is reduced, the cleaning action for cleaning the membrane filter is kept constant.
  • FIG. 8 shows the oxygen concentration meter 10, the automatic controller 30, the circulating gas volume automatic control valve 560a and the air volume automatically in the water of the aerobic tank 510 in the membrane filtration aerobic treatment step of the present invention.
  • the example which installed the valve 570a and controls it automatically so that the dissolved oxygen concentration in an aerobic tank may be kept at the set value is shown.
  • the automatic controller 30 increases the opening degree of the air volume control valve 570a and increases the amount of air sucked from the outside. If the dissolved oxygen concentration in the exhalation tank is larger than the set value, the automatic controller sets the dissolved oxygen concentration in the exhalation tank by increasing the opening degree of the circulating gas amount automatic control valve 560a and decreasing the opening degree of the air volume automatic control valve 570a. Keep it constant at one value.
  • FIG 9 shows an embodiment of an aerobic tank in which the present invention is applied to a small sewage treatment facility. All.
  • the upper portion of the aerobic tank may be closed with a shield cover, and the upper portion of each membrane filter 630 may be closed. It is often more economical to install the blocking covers 650 individually.
  • the membrane filter 630 is installed in the water of the aerobic tank 510, the membrane cleaning diffuser 640 is installed below the membrane filter, and the membrane cleaning diffuser and the membrane cleaning blower 620 are provided. ) Between the discharge port is connected to the air piping.
  • the inlet side of the membrane cleaning blower 620 was connected to the gas circulation pipe 660, and the gas circulation pipe was provided with a circulating gas flow control valve 680.
  • a suction pipe for inhaling air in the atmosphere was installed, and an air volume control valve 690 for adjusting the intake air amount was installed.
  • an air diffuser 530 for abandoning the aerobic tank was installed near the inner bottom of the aerobic tank 510, and the air outlet was connected between the air diffuser and the discharge port of the membrane filtration aerobic blower 550.
  • the amount of air supplied to the air diffuser is controlled by releasing some discharged air into the atmosphere from the noise blower 590 and controlling the number of revolutions of the blower. Can be.
  • the method of adjusting the ratio of the amount of circulating gas and the amount of hop-in air is the same as described above.
  • FIG 3 is an exemplary view of a sewage treatment process using the membrane filtration tank of the present invention.
  • Flow rate adjustment step 200 to maintain the sewage for a certain time
  • An aerobic denitrification treatment step 500A that maintains a low dissolved oxygen concentration and a specific redox potential value, decomposes organic matter in the sewage, denitrates nitrogen, and allows the microorganism to absorb excessively phosphorus;
  • Membrane that keeps dissolved oxygen concentration of sewage at l ⁇ 2.0mg / L, activates microorganism, converts some untreated ammonia nitrogen to nitrate nitrogen, and separates supernatant Filtration treatment step 600;
  • Degassing treatment step 700 to lower the dissolved oxygen concentration in the sewage
  • a sewage treatment method using a submerged membrane bioreaction device that is easy to vary in load, characterized by consisting of a conveying pump 800 and a conveying water 900.
  • the pretreatment step 100 and the flow rate adjusting step 200 are as described above, and in the anaerobic treatment step 300, the return water 900 and the sewage are mixed in the anaerobic tank 310 as shown in FIG. During a certain period of time, the phosphorus contained in the microorganisms is released, and the nitric acid nitrogen contained in traces in the return water is converted to nitrogen gas by the action of denitrifying bacteria.
  • an air diffuser 530 is installed near the inner bottom of the aerobic denitrification tank 510a, and an aerobic denitrification stirrer 520a is installed.
  • the discharge port of the air diffuser and the blower blower 540 was connected by air piping.
  • the dissolved oxygen concentration of the aerobic denitrification tank (510a) is kept relatively low at 0.3 ⁇ 0.5mg / L by controlling the air supply of the aerobic blower, and the redox potential (0RP) is maintained at + 330mV based on the hydrogen electrode.
  • the redox potential (0RP) is maintained at + 330mV based on the hydrogen electrode.
  • ammonia nitrogen in sewage is oxidized to nitrate nitrogen by the action of aerobic denitrification bacteria, and at the same time, denitrification occurs by conversion to nitrogen gas.
  • microorganisms that released phosphorus in the anaerobic treatment step absorb excess phosphorus in aerobic state, and organic matter is decomposed and treated in aerobic state.
  • the membrane filtration tank of the membrane filtration treatment step 600 was configured as shown in FIG. 6, and the configuration and operation were as described above, but the dissolved oxygen concentration in the membrane filtration tank 610 was maintained at 1.0 to 2.0 mg / L for a predetermined time.
  • the activity of the microorganism is increased, and ammonia nitrogen, which may not be partially nitrified in the aerobic denitrification tank 510a due to the action of nitrifying bacteria, is oxidized to nitrate nitrogen.
  • sewage and supernatant are separated in membrane filter 630.
  • the advantage of aerobic denitrification is that the amount of air required is low, and in theory, 100% of denitrification is possible if the operating conditions such as pH, ORP and HRT are ideally maintained.
  • the supply of air to the sewage is stopped for a certain time, and the dissolved oxygen concentration of the sewage is kept lower than 0.5 mg / L to increase the treatment effect of the anaerobic treatment step, which is a connecting process.

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  • Life Sciences & Earth Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Hydrology & Water Resources (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

La présente invention concerne un processus de traitement avancé des eaux d'égout ou des eaux usées utilisant un filtre à membrane, et plus particulièrement un bioréacteur à membrane submergée qui réagit facilement à la régulation de la charge ainsi qu'une méthode de traitement des eaux usées l'utilisant. La présente invention concerne entre autres un bioréacteur à membrane submergée qui réagit facilement à la régulation de la charge, et spécifiquement à celle des charges faibles. Pour cela, la présente invention concerne un bioréacteur à membrane submergée qui réagit facilement à la régulation de la charge de façon à pouvoir réaliser efficacement un traitement avancé des eaux d'égout ou des eaux usées à l'aide d'un filtre à membrane submergée dans lequel une partie de l'air (du gaz) utilisé pour nettoyer la membrane est recirculé afin d'ajuster facilement une concentration en oxygène dissout tout en maintenant une fonction de nettoyage de membrane, ainsi qu'une méthode de traitement des eaux usées l'utilisant. Comme le bioréacteur à membrane submergée peut réagir facilement à la régulation de la charge, et spécifiquement à celle des charges faibles, les processus de traitement des eaux d'égout et des eaux usées domestiques, qui sont effectués fréquemment à charge faible dans des opérations et des processus d'exploitation d'essai initiaux, peuvent être effectués efficacement et de façon stable. De plus la qualité de l'eau peut être améliorée et on peut promouvoir l'utilisation d'un appareil de traitement utilisant le filtre à membrane submergée.
PCT/KR2011/006608 2010-09-14 2011-09-07 Bioréacteur à membrane submergée qui réagit facilement à la régulation de la charge, et méthode de traitement des eaux usées l'utilisant WO2012036408A2 (fr)

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KR10-2010-0089834 2010-09-14
KR20100089834A KR101050375B1 (ko) 2010-09-14 2010-09-14 부하변동에 대응이 용이한 침지식 막 생물 반응장치 및 이를 이용한 하수처리 방법

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WO2012036408A2 true WO2012036408A2 (fr) 2012-03-22
WO2012036408A3 WO2012036408A3 (fr) 2012-06-21

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CN106745725A (zh) * 2017-02-28 2017-05-31 广东维清环境工程有限公司 一种限氧型膜生物反应器污水处理系统
CN110054295A (zh) * 2019-05-15 2019-07-26 桂林市全净生物科技有限公司 多功能污水处理机
IT202300002535A1 (it) * 2023-02-15 2024-08-15 Giovambattista Greco Sistema di micro-ultrafiltrazione con membrane tubolari

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KR101367711B1 (ko) 2011-12-09 2014-02-27 (주)필로스 하수의 고도 처리 방법
KR101367229B1 (ko) 2012-01-03 2014-02-25 (주)필로스 침수식 막 고도처리공정의 운전방법과 그 방법을 이용한 침수식 막 고도처리장치
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KR101424045B1 (ko) * 2012-07-10 2014-08-13 (주)필로스 침지식 막 여과장치를 사용하는 하수처리시설 및 이를 이용하여 에너지를 절약하는 방법
CN105008027A (zh) 2013-02-22 2015-10-28 通用电气公司 用于支承生物膜的膜片组件
EP3119724A2 (fr) 2014-03-20 2017-01-25 General Electric Company Traitement d'eaux usées par un traitement primaire et réacteur mbr ou mabr-ifas
CN110093892A (zh) * 2019-05-22 2019-08-06 上海砼仁环保技术发展有限公司 一种便捷式透水路面清洗车

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CN110054295A (zh) * 2019-05-15 2019-07-26 桂林市全净生物科技有限公司 多功能污水处理机
IT202300002535A1 (it) * 2023-02-15 2024-08-15 Giovambattista Greco Sistema di micro-ultrafiltrazione con membrane tubolari
WO2024171001A1 (fr) * 2023-02-15 2024-08-22 Greco Giovambattista Système de micro-ultrafiltration à membranes tubulaires

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