WO2019031726A1 - 적층형 구조와 세정볼을 이용한 상향류식 mbr 하폐수 처리 시스템 - Google Patents

적층형 구조와 세정볼을 이용한 상향류식 mbr 하폐수 처리 시스템 Download PDF

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WO2019031726A1
WO2019031726A1 PCT/KR2018/008184 KR2018008184W WO2019031726A1 WO 2019031726 A1 WO2019031726 A1 WO 2019031726A1 KR 2018008184 W KR2018008184 W KR 2018008184W WO 2019031726 A1 WO2019031726 A1 WO 2019031726A1
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tank
membrane
anaerobic
water
cleaning
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PCT/KR2018/008184
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English (en)
French (fr)
Korean (ko)
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박병선
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정우이엔티㈜
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Priority to CN201880007878.4A priority Critical patent/CN110225892B/zh
Publication of WO2019031726A1 publication Critical patent/WO2019031726A1/ko

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/02—Hollow fibre modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
    • B01D63/08—Flat membrane modules
    • 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
    • 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
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge 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
    • 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 an MBR wastewater treatment apparatus capable of preventing and preventing contamination of a separation membrane immersed in an upflow type membrane separation tank, and more particularly, to an MBR wastewater treatment apparatus using a cleaning ball and a MBR wastewater treatment method using the same.
  • the MBR (membrane bioreactor) process which can maintain a high concentration of MLSS (about 8,000 ⁇ 15,000 mg / L), is suggested as a countermeasure in view of the increase in water quality regulation standards and water resource reuse penetration And has a high processing efficiency and a relatively simple operation and maintenance. Therefore, the number of introduction cases is rapidly increasing and many studies are being conducted.
  • MBR process Most of the MBR process in the early 1990s was a side-stream type in which the membrane module was settled outside the reactor and the sludge in the reactor was circulated through a filtration-loop to perform solid-liquid separation. However, And it was limited to the application of municipal sewage treatment. To solve this problem, the concept of submerged knowledge process was born in mid-1990, and it became a widespread use of MBR in urban sewage treatment. Compared with the conventional activated sludge process, the MBR process has the following advantages.
  • HRT Hydraulic residence time
  • SRT solids residence time
  • An object of the present invention is to maximize the effect of releasing phosphorus without adding coagulant and to improve the efficiency of maintenance by constructing an upflow MBR by constructing a DO reduction tank, anoxic tank and anaerobic tank in a laminated form.
  • it is intended to maintain the planned flux at all times by minimizing TMP by using physical cleaning technology and gravity filtration and to minimize the stress of the separator to ensure a long life of the separator.
  • the present invention relates to an MBR wastewater treatment apparatus including an DO reduction tank, an anoxic tank, an anaerobic tank, an aerobic tank, and an upward flow type membrane separation tank, wherein the DO reduction tank and the anoxic tank are located above the anaerobic tank, And a bottom wall of the DO reduction tank and the anoxic tank constitute a top wall of the anaerobic tank so that the anaerobic tank is closed so that the DO reduction tank and the anaerobic tank are integrated with each other and a double wall is formed on the side of the aerobic tank Characterized in that the MBR wastewater treatment device is connected to the MBR wastewater treatment device so as to smoothly move the sludge, and the hollow fiber membrane type or flat membrane type separation membrane is immersed in the upward flow type membrane separation vessel, .
  • the present invention also relates to a MBR wastewater treatment method using an MBR wastewater treatment apparatus according to various embodiments of the present invention, wherein the separation membrane is subjected to cleaning using a cleaning ball, air cleaning, and backwashing.
  • the MBR wastewater treatment device can maximize treatment efficiency by dividing inflow water into inflow water into the bioreactor arranged in an integrated manner and the bioreactor.
  • the physical washing technique can be applied to the membrane separation tank of the MBR wastewater treatment apparatus to prevent and prevent the contamination of the separation membrane, the number of times of strengthened cleaning can be carried out once or less per year. From this, it is possible to remarkably reduce the amount of the medicine to be injected into the washing, thereby reducing the cost of the medicine.
  • Figure 1 illustrates a laboratory scale device used in the examples and test examples.
  • FIG. 2 is a view showing a laboratory scale apparatus used in Examples and Test Examples, and a membrane of a membrane separation tank used in pilot apparatus experiments.
  • Figure 3 shows the fluidized-bed cleaning balls used in the examples and test examples.
  • FIG. 4 is a view showing an MBR wastewater treatment apparatus used in Examples and Test Examples.
  • 5 is a graph showing the recovery rate according to backwash flow rate.
  • 6 is a graph showing a change in TMP with or without backwash application.
  • FIG. 7 is a graph showing the change in TMP according to the amount of the cleaning ball.
  • FIG. 9 is a graph showing a change in TMP according to the amount of fine bubbles to be supplied.
  • 11 is a graph showing the phosphorus concentration removal efficiency according to the divided raw water injection.
  • 13 is a graph showing changes in phosphorus concentration of treated water during long-term operation in a pilot plant.
  • Figure 14 is a graph showing TMP and flux changes during long term operation in a pilot plant.
  • 15 is a graph showing changes in MLSS concentration during long term operation in a pilot plant.
  • 16 is a graph showing the amount of power consumption per hour per major unit process during long-term operation in a pilot plant.
  • One aspect of the present invention is an MBR wastewater treatment apparatus including a DO reduction tank, an anoxic tank, an anaerobic tank, an aerobic tank, and an upward flow type membrane separation tank, wherein the DO reduction tank and the anoxic tank are located above the anaerobic tank, wherein the anaerobic tank is a laminated water tank and the lower wall of the DO reducing tank and the anaerobic tank constitutes a top wall of the anaerobic tank so that the anaerobic tank is closed so that the DO reducing tank and anoxic tank are integrally formed with the anaerobic tank, (See FIG. 4), the membrane separation tank is immersed in a hollow fiber membrane type or membrane type separation membrane, and the overflow of the membrane separation tank is connected so as to be transported to the aerobic tank in a non-reciprocating manner To an MBR wastewater treatment device.
  • the DO reduction tank and the anoxic tank and the anaerobic tank integrally constitute, it is possible to block the air contact of the anaerobic tank, thereby maximizing the anaerobic condition of the anaerobic tank, .
  • the membrane separation tank is configured to be compact on the outside of the oxic tank, low load aeration using fine bubbles is possible, and gravity filtration is possible by positioning the treatment tank below the membrane separation tank, So that the membrane separation tank functions as a cleaning tank during the strong cleaning, so that it can be cleaned without equipment such as a hoist, and the labor cost and the equipment usage fee can be reduced accordingly.
  • the wastewater source water may be divided into the DO reduction tank and the anaerobic tank, and the oxygen storage tank, the anaerobic tank, the aerobic tank, and the membrane separation tank may be sequentially treated through the DO reduction tank.
  • the effect of the anaerobic microorganism as an energy source for the phosphorus release can be maximized, thereby maximizing the release without the coagulant injection.
  • some of the treated water that has passed through the aerobic tank is transported to the DO reduction tank and reprocessed.
  • the drainage of the membrane separation tank is constituted by the overflow water and the treatment water, and the overflow water is transported and reprocessed by the aerobic tank without motive power, and the treated water is discharged or introduced into the reclaimed water treatment process.
  • the treated water can be discharged or used as an influent water for the reused water treatment process when used for the purpose of reuse. Further, by returning the overflow of the upward flow type membrane separation tank having a high DO concentration to the aerobic tank by the non-reciprocating operation, the amount of blowing air of the oxic tank can be reduced, thereby reducing power consumption and preventing excessive aeration.
  • the anoxic tank is disposed in contact with the downstream end of the DO reduction tank, and is located in contact with the upper portion of the anaerobic tank.
  • the lower wall of the DO reduction tank and the anoxic tank constitute the upper wall of the anaerobic tank so that the anaerobic tank is sealed, so that the DO reduction tank and the anaerobic tank are integrally formed with the anaerobic tank, and a double wall is formed on the side of the aerobic tank, It should be smooth.
  • the raw wastewater water is dividedly introduced into the DO reduction tank and the anaerobic tank through the inlet, and the treated water treated in the DO reduction tank can be moved to the anoxic tank.
  • the treated water treated in the anoxic tank is moved to the anaerobic tank
  • the treated water treated in the anaerobic tank is moved to the aerobic tank
  • a part of the treated water treated in the aerobic tank is moved to the membrane separation tank, It is transported to the low-level tank and reprocessed.
  • the effluent from the membrane separation tank is composed of overflow water and treated water, and the overflow water is transported and reprocessed in the aerobic tank, and the treated water is discharged or introduced into the reused water treatment process.
  • the device is located at the bottom of the separator.
  • Another aspect of the present invention relates to a MBR wastewater treatment method using an MBR wastewater treatment apparatus according to various embodiments of the present invention, wherein the separation membrane is subjected to cleaning using a cleaning ball, air cleaning, and backwashing.
  • the MBR wastewater treatment apparatus uses the MBR wastewater treatment apparatus having the structure according to the preferred embodiment of the present invention, (ii) the separation membrane is cleaned using a cleaning ball, Air cleaning, and backwash.
  • the cleaning ball is used in an amount of 9 to 10 kg / m 3 based on the unit volume of the treated water in the membrane separation tank, (iv) ≪ / RTI > (V) the produced bubbles have a diameter of 0.5 to 1.5 mm, (vi) the amount of bubbles to be produced is 0.5 to 0.7 m 3 / m 2 ⁇ g / m 2 based on the unit time and the unit area of the membrane in the membrane separation tank. hr, and (vii) the backwash flow rate is 25 to 35 L / m 2 ⁇ hr (LMH). At this time, the backwashing may be performed for 0.3 to 0.6 minutes at a filtration period of 5 to 15 minutes. For example, a 10 minute filtration cycle can be run with a cycle of 8 minutes 30 seconds filtration, 30 seconds rest, 30 seconds backwash, and 30 seconds rest.
  • the laboratory scale apparatus and the pilot apparatus used in the present embodiment were installed in an actual operating environment establishment, and the conditions of the raw water used in the experiment of the laboratory scale apparatus were the same as those of the pilot apparatus operation condition.
  • the raw water constructions and the pilot apparatus operating conditions are shown in Tables 1 and 2, respectively.
  • the separation membrane used in the experiment of the laboratory scale apparatus and the pilot apparatus is shown in FIG. 2.
  • the separation membrane is a back-washable flat plate membrane having a pore size of 0.04 ⁇ m and a material of Polyethersulfone (PES) Respectively.
  • FIG. 3 is an elliptical carrier having a size of 3 to 4 mm and is loaded into a membrane separation tank to prevent the sludge deposit on the membrane surface .
  • FIG. 1 shows the structure of the laboratory scale device. Specifically, a cooler was installed in a 100 L container to maintain the water temperature and the experiment was conducted by circulating the membrane separation tank of the pilot device. In the case of process control, And the flow rate is controlled by a constant flow rate. Also, the configuration of the bioreactor in the configuration of the pilot apparatus is an upflow type separation membrane process based on the A 2 / O process, and is shown in FIG.
  • the air bubbles (6-10 mm) used for air cleaning were applied to air bubbles (1-5 mm: EPA, 1989) with high shear force but high oxygen delivery efficiency (3-10% Has a disadvantage in that the shear force is excellent but the oxygen transfer efficiency (1-3%) is lowered.
  • the optimum operating conditions for air cleaning using micro-bubbles were calculated by using the specific area demand membrane area (SADm) per membrane area, and it was calculated as 0.4 m 3 / m 2 ⁇ hr and 0.5 m 3 / m 2 ⁇ hr , 0.6 m 3 / m 2 ⁇ hr, 0.7 m 3 / m 2 ⁇ hr and 0.8 m 3 / m 2 ⁇ hr, respectively.
  • the filtration rate was 40 LMH (at 20 °C) and backwashing flow was selected as 10, 20, 30, 40 and 50 LMH.
  • the backwash efficiency was estimated by determining the reduced filtration resistance value after backwashing. The experimental conditions are shown in Table 5 below.
  • the experimental conditions were 5.6 MCB-kg / m 3 , 7.6 MCB-kg / m 3 , and 9.6 MCB-kg / m 3 , respectively, to obtain the optimum factors for the operation of the cleaning ball (MCB) m 3 and 11.6 MCB-kg / m 3 , respectively, and the air cleaning flow rate was set to a previously derived value (0.6 m 3 / m 2 ⁇ hr).
  • the experimental conditions are shown in Table 6 below.
  • Pilot Plant operated for about 6 months including winter season.
  • the pilot plant operating conditions are shown in Table 2.
  • the backwash efficiency of the pilot plant was evaluated by applying the backwash flow rate set by the lab test.
  • the TMP increase rate in the control group without backwashing was about -0.002 bar / day, which was about three times higher than that in the backwashed experimental group.
  • the backwash function serves to remove the reversible membrane contaminants between the pores. Therefore, in the control group without backwash, the reversible membrane contaminants between the pores are continuously accumulated. As a result, the effective membrane area decreases due to the pore clogging, so that the membrane contamination gradually accelerates.
  • Fig. 7 is a graph showing the results of the titration of the washing ball titration amount.
  • Experimental results show that the TMP of each filtration section is changed according to the amount of the fluidized cleaning ball and stable filtration and TMP tendency is shown as the amount of fluidized cleaning ball is increased.
  • the filtration and TMP tendency is less than 10 kg / m 3 . Therefore, 10 MCB-kg / m 3 was selected as the optimal cleaning ball input amount in the pilot device application evaluation.
  • the efficiency of the cleaning ball in the pilot plant was compared and evaluated by applying the set amount of cleaning ball set through the Lab test.
  • the TMP rate of increase in the control group without the fluidized-bed cleaning ball was about -0.0038 bar / day, which was expected to take about 80 days to reach the limit pressure difference of -0.4 bar.
  • the TMP increase rate in the ball-treated group was -0.0007 bar / day, which was about 5.4 times lower.
  • the pilot plant was assessed for TMP changes with or without air cleaning, backwash and cleaning balls for about 3 months.
  • periodical operation was performed using backwash and cleaning balls and the efficiency was compared with the control group without backwashing and cleaning balls.
  • the hardened cleaning was carried out once, and after about 15 days, the differential pressure reached again and the hardened cleaning was reexamined.
  • backwashing and cleaning balls were applied, it was possible to operate under stable filtration pressure, and the same strong washing as the control group was not required.
  • the DO reduction tank, the anoxic tank and the anaerobic tank are stacked so that the microorganisms in the anaerobic tank can be prevented from contacting with oxygen in the atmosphere, thereby enabling complete anaerobic conditions. Also, in order to supply sufficient organic matter, raw water is divided into DO reduction tank and anaerobic tank, so that it is possible to discharge the water in a smooth manner.
  • the biological removal efficiency increased as the ratio was gradually increased without the introduction of raw water into the anaerobic tank.
  • the concentration of the treated water was lower than that of the treated water of 7: 3 and 6: 4 .
  • the raw water division inflow was selected as 7: 3.
  • the phosphor release effect and phosphorus removal were evaluated according to the ratio of raw water (7: 3) fed into the DO reduction tank and the anaerobic tank for about 7 months.
  • the average ORP of the anaerobic tank was kept at -386 mV, It shows a lower ORP value than the anaerobic conditions in the general process, which means that complete anaerobic conditions are formed.
  • the concentration of PO 4 -P in the anaerobic tank was maintained in the range of 8.4 ⁇ 20.2 mg / L, which indicates that active phosphorus release is being performed by PAOs when the phosphorus concentration of raw water is taken into consideration.
  • the experimental results are shown in Fig.
  • the pilot plant was evaluated for TMP and flux changes for about 6 months, including the winter season, by applying the set operating conditions through the Lab test. During the winter and summer months, the throughputs were 25 LMH and 30 LMH, respectively. After 4 months from the start of operation, the differential pressure reached -0.2 bar, and maintenance was performed. As shown in FIG. 14, if it is assumed that the periodic maintenance cleaning is applied, the enhanced cleaning can be performed once or less per year.
  • Figure 15 shows the MLSS concentration changes in the aerobic tank and the upflow type membrane tank during the operation period of the demonstration plant.
  • the average MLSS concentration in the aerobic tank was 8,616 mg / L and the mean MLSS concentration in the upflow type membrane was 16,331 mg / L.
  • the MLSS concentration in the upward flow separation membrane bath is about twice as high as that in MBR process using general flat membrane. This suggests that the MBR process, which is different from the conventional MBR process, can be operated at a high MLSS condition with a relatively high concentration. As a result, the sludge treatment cost can be reduced as compared with the general process.
  • the sludge cake layer is likely to form on the surface of the separation membrane from the MLSS retention of high concentration compared to the general process.
  • the present technology can solve the above-described problem by effectively removing the attached sludge by colliding with the separation membrane surface during the backwash process and filtration.
  • the pollutant concentration in the treated water was stable, and the average treatment efficiency was found to be BOD 99.2%, CODCr 97.4%, CODMn 97.7%, SS 100.0%, TN 85.2% and TP 98.2% .
  • Table 10 shows the pollutant treatment efficiency during the survey period.
  • Item unit Contaminant concentration (mg / L) Treatment efficiency (%) Influent Effluent Lowest to highest Average Lowest to highest Average Reference value BOD mg / L 132.8 to 440.0 261.6 1.2 to 3.9 1.9 10 99.2 CODcr mg / L 219.0 to 584.0 440.1 5.1 to 18.0 11.0 - 97.4 COD Mn mg / L 100.1 to 490.0 293.2 4.0 to 8.8 5.9 40 97.7 SS mg / L 134.0 to 345.2 271.6 - - 10 100 T-N mg / L 18.1 to 54.0 33.1 2.3 ⁇ 7.8 4.7 20 85.2 T-P mg / L 2.20 ⁇ 7.80 5.14 0.02 to 0.18 0.09 2.00 98.2
  • DO reduction tank 20 anoxic tank 30: anaerobic tank

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PCT/KR2018/008184 2017-08-10 2018-07-19 적층형 구조와 세정볼을 이용한 상향류식 mbr 하폐수 처리 시스템 WO2019031726A1 (ko)

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