KR101236004B1 - Submerged MBR system comprising U―form inline mixer - Google Patents

Abstract

The present invention provides an immersion type MBR system for effectively treating total nitrogen and total phosphorus in raw water by chemical / biological treatment methods and a U-shaped inline mixer used therein. In the U-shaped in-line mixer, the vortex generation allows rapid and slow agitation to effectively process and at the same time effectively control the coagulant supply pump and the membrane separation suction pump to extend the life of the membrane and increase the treatment effect.

Description

Submerged MBR system comprising U-form inline mixer

The present invention relates to an immersion type MBR (membrane bioreactor) system for effectively treating total nitrogen and total phosphorus in raw water by chemical / biological treatment methods and a U-shaped inline mixer used therein.

Total phosphorus in wastewater (hereinafter TP) is easily removed by chemical bonding and adsorption, and treatment efficiency is relatively high.

The conventional chemical treatment method has a disadvantage in that it requires a device for solid-liquid separation of the floc and the treated water formed by sedimentation or filter after slow and rapid aggregation, and takes up a lot of site.

Conventional biological treatment methods proceed by the phenomenon in which activated sludge releases phosphorus in the anaerobic state and again intakes of phosphorus in the aerobic state. Phosphorus release and overdose processes of activated sludge microorganisms release ortho-phosphate in the anaerobic state, increasing the concentration of ortho-phosphate in the mixed liquor. After a certain time in the anaerobic state to switch to aerobic state activated sludge reversely absorbs the ortho-phosphoric acid in the mixture, the concentration of phosphorus in the mixture is reduced.

It can be seen that organic matter is ingested from the substrate concentration of the mixed solution even under anaerobic conditions. Fermentation materials are produced from fermentation reactions by random microorganisms that normally occur in the anaerobic state, mainly due to the breakdown of VFAs (Volatile Fatty Acids). This fermentation product is very easily decomposed and stored by dephosphorous microorganisms, which takes advantage of the energy generated by the hydrolysis of polyphosphates in the anaerobic state.

That is, energy is released as the phosphate polymer stored in the cell changes, and this energy is used for active transfer of substrate and fermentation of acetoacetate. Dephosphorus bacteria can decompose fermentation materials in the anaerobic state, so that they can proliferate more actively than other microorganisms in activated sludge systems.

In aerobic dephosphorization, phosphorus is removed by consuming excess soluble phosphorus in the form of phosphate while using the substrate stored in the cells, and discarding the excess phosphorus in excess sludge with excess sludge.

Thus, the degree of biological removal is influenced by the formation of complete anaerobic conditions, the amount of substrates (VFAs) used in the microorganisms in the anaerobic state, and by the introduction of nitrifying microorganisms into the anaerobic tank.

On the other hand, in the conventional flocculation and admixture process, a flocculant injection device, a slow stirring tank, a rapid stirring tank, and a precipitation tank were all required. In particular, when the sedimentation capacity of the sludge is badly affected by the season in the sedimentation tank, there is a problem that the sludge flows out of the effluent and the treatment is not possible, and the consumption of the site was large because the slow and rapid stirring tanks were set apart.

The present invention has been made to solve the above problems.

In other words, by applying the chemical treatment and biological treatment together, the treatment efficiency becomes low, the process becomes complicated and difficult, the amount of flocculant used and the process uptime increases, the maintenance cost increases, and the treatment efficiency varies depending on the season. To solve the problem that the site of the facility is increased.

In order to solve the above problems, the present invention, an oxygen-free tank; An anaerobic tank in fluid communication with the anoxic tank; A membrane separation tank in fluid communication with the anaerobic tank; And a U-shaped inline mixer in fluid communication with the membrane separator, wherein the U-shaped inline mixer comprises one or more venturi tubes and U-shaped connectors, and the membrane separator is adapted to supply raw water therein. It can be pumped to the U-shaped in-line mixer, the coagulant tank provides an immersion type MBR system comprising a U-shaped in-line mixer, characterized in that the internal coagulant can be pumped to the U-shaped in-line mixer.

In another embodiment, the present invention includes a first venturi tube in fluid communication with the membrane separation tank; A second venturi tube positioned below or above the first venturi tube and in fluid communication with the coagulant tank; And a U-shaped connecting tube connecting the first venturi tube and the second venturi tube, wherein the raw water introduced from the membrane separation tank and the coagulant introduced from the coagulant tank are mixed while generating a vortex therein. It features a U-shaped inline mixer.

According to the present invention, chemical and biological treatments can be combined in an immersion MBR system, resulting in an effective treatment while simplifying the procedure.

In addition, by utilizing the U-shaped in-line mixer can increase the flocculation efficiency of the flocculant without a separate stirrer, both rapid and slow stirring is possible.

In accordance with the present invention, flocculants are automatically injected and sludge is automatically drawn so that the entire system is automated to facilitate process management and maintenance.

In addition, fouling due to coagulant injection can be reduced and the life of the separator can be extended.

As a result of numerous experiments, it was found that TP can be treated to 0.2 ppm or less, while reducing the amount of flocculant injected by about 67% according to the present invention.

1 schematically shows a process flow diagram of an immersion type MBR system according to the present invention.
2A-2C show a plan view, front view, and side view, respectively, of a facility of an immersion type MBR system according to the present invention.
3a to 3b show a plan view and a side view, respectively, of a U-shaped inline mixer according to the present invention.
4 to 9 are diagrams illustrating an embodiment of sewage treatment using the immersion type MBR system according to the present invention.
4 shows the appearance of raw water applied to the embodiment.
Figure 5 shows the application conditions of the immersion type MBR system according to the present invention applied to the embodiment.
6 shows jar test results for determining flocculant input concentration.
7 is a table showing experimental results, and FIGS. 8 and 9 are graphs showing experimental results.

Hereinafter, the present invention will be described in detail with reference to the accompanying drawings. It is noted that a valve or a flow path irrelevant to the core idea of the present invention is not separately mentioned, and any configuration according to the related art is applicable.

Description of Submerged MBR System According to the Present Invention

Immersion type MBR system according to the present invention, the collection tank 100, drum screen 200, anoxic tank 300, anaerobic tank 400, membrane separation tank 500, disinfection tank 600, concentration tank 700 and the control unit 800 ), In particular with a U-shaped inline mixer (590).

Raw water flowing into the immersion-type MBR system according to the present invention is first stored in the sump tank 100, and then screened through the drum screen 200 is introduced into the oxygen-free tank (300).

A sensor (not shown) associated with the control unit 800 is positioned in the water collecting tank 100 to sense the phosphorus concentration of raw water flowing into the immersion type MBR system and transmit the same to the control unit 800 to control the pump operation.

On the other hand, the anaerobic tank 300, the anaerobic tank 400, the membrane separation tank 500 is in turn in fluid communication is processed raw water is delivered.

The anaerobic bath 300 is effective for denitrification. Nitrogen is first removed by passing raw water through the anaerobic tank 300 before the anaerobic tank 400, thereby minimizing the inhibitory effect in the phosphorus removal process of the latter stage due to nitrogen. The denitrification treatment of the oxygen-free tank 300 may use any method according to the prior art.

Raw water that has passed through the anaerobic tank 300 is introduced into the anaerobic tank 400 is made biological release. The dephosphorization treatment of the anaerobic tank 400 may use any method according to the prior art. Raw water from which biological release has been made flows into the membrane separation tank 500.

Membrane separation tank 500 is a flocculant in a separation membrane (not shown) capable of filtration treatment, a circulation pump 510 for pumping raw water therein to the U-shaped inline mixer 590, and a U-shaped inline mixer 590. Is mixed with a membrane separation suction pump (not shown) to remove the phosphorus by pumping the raw water re-sent to the membrane separation tank 500 to pass through the separation membrane, the filtered treated water is transferred to the disinfection tank 600 and the sludge concentration tank 700 It includes a transfer pump 520 for transferring to. Operation of the pumps may be controlled by the controller 800.

In the case of a separation membrane (not shown), any membrane used in the MBR process can be used. Depending on the site conditions or the characteristics of the wastewater, any membrane can be used, such as hollow fiber membranes, flat membranes, tubular membranes.

Raw water introduced into the membrane separation tank 500 by the operation of the circulation pump 510 is transmitted to the U-shaped inline mixer 590. Coagulant may be introduced into the U-shaped in-line mixer 590 from the coagulant tank 550.

The U-shaped inline mixer 590 will be described in detail with reference to FIGS. 3A and 3B.

U-shaped in-line mixer 590 is the first venturi tube (591). Preferably, the second venturi tube 593 and one U-shaped connecting tube 592 are formed. More preferably, each of the venturi tubes 591 and 593 is provided with valves 591a and 593a capable of controlling inflow and outflow.

The raw water transferred by the circulation pump 510 and the coagulant transferred by the first pump 570 of the coagulant tank 550 flow into the U-shaped inline mixer 590 and are mixed.

Each of the venturi tubes 591 and 593 has a small cross-sectional area in the middle, thereby increasing the speed of the introduced raw water or flocculant and lowering the pressure. In addition, the first venturi tube 591 and the second venturi tube 593 is located up and down, the U-shaped connecting pipe 592 connects it. Through this, the U-shaped connecting pipe 592 inside the vortex is generated, the incoming raw water and the flocculant and rapid, slow mixing process is effectively performed.

That is, in the prior art, since there is no structure such as a U-shaped connector, there is no step, and in the present invention, the venturi tubes 591 and 593 are positioned up and down by using the U-shaped connector 592. Multistage is applied and the bend is located. Through this, the vortex is effectively generated without a separate stirrer, so that flocculant and raw water can be efficiently mixed. The inventors have confirmed that the mixing effect is more effective when the length of the venturi tubes (591, 593) is 2m or more through a number of experiments.

The mixed flocculant and the raw water are transferred back to the membrane separation tank 500.

When the raw water mixed with the flocculant is re-introduced into the membrane separation tank 500, the controller 800 operates a membrane separation suction pump (not shown) after giving a predetermined mixing time. When the membrane separation suction pump (not shown) is operated, raw water mixed with the flocculant may be filtered through the separation membrane (not shown) and phosphorus may be removed to separate the treated water and the sludge. Thereafter, when the transfer pump 520 is operated, the treated water and the sludge are transferred to the disinfection tank 600 and the concentration tank 700, respectively.

The treated water transferred to the disinfection tank 600 is discharged to the outside after the chemical treatment.

The sludge conveyed to the concentration tank 700 is discharged to the outside after reacting with the coagulant pumped by the second pump 570 from the coagulant tank 550.

That is, the coagulant tank 550 may be mixed with the raw water by pumping the coagulant through the first pump 560 to the U-shaped in-line mixer 590, and the coagulant is concentrated through the second pump 570. Can be mixed with the sludge.

The controller 800 may control the circulation pump 510, the transfer pump 520, and the membrane separation suction pump (not shown) in the membrane separation tank 500, and the first pump 560 of the flocculant tank 550. And a second pump 570.

On the other hand, raw water or treated raw water or sludge is collected directly in the collecting tank 100, anoxic tank 300, anaerobic tank 400, membrane separation tank 500, disinfection tank 600 and concentration tank 700 in a separate medium-large treatment tank However, except for the coagulant tank 550 and the pumps 560 and 570 connected thereto, the U-line in-line mixer 590 and the control unit 800 are located as separate facility facilities, as shown in FIGS. 2A to 2C. The space can be minimized.

That is, the first pump 560 and the second pump 570 are located in parallel to one side of the coagulant tank 550, the U-shaped in-line mixer 590 is adjacent to the other side of the coagulant tank 550 The controller 800 may be located on the side surfaces of the first pump 560 and the second pump 570 and above the U-shaped inline mixer 590 to minimize the space occupied by the facility.

Description of Immersion Type MBR System Control Method According to the Present Invention

Raw water flows into the sump 100.

Raw water introduced into the sump tank 100 is introduced into the anaerobic tank 200 after the coarse solids are screened on the drum screen 200.

Next, the raw water introduced into the anaerobic tank 300 is denitrified and introduced into the anaerobic tank 400, and the anaerobic tank 400 is biologically treated and introduced into the membrane separation tank 500.

The controller 800 may detect a phosphorus concentration of raw water introduced through a sensor (not shown) located in the water collecting tank 100, and operate the pump when the predetermined concentration is reached.

When the predetermined concentration is reached, the controller 800 operates the circulation pump 510 of the membrane separation tank 500 for a predetermined mixing time to feed the raw water introduced into the membrane separation tank 510 into the U-shaped inline mixer 590. And simultaneously operating the first pump 560 to transfer the coagulant from the coagulant tank 550 to the U-shaped inline mixer 590.

The raw water and the flocculant introduced into the U-shaped in-line mixer 590 are effective for rapid and slow mixing due to the vortices generated in the unique U-shaped in-line mixer 590 according to the present invention.

Next, the flocculant and the raw water mixed in the U-shaped in-line mixer 590 are transmitted to the membrane separation tank 500 again.

Next, the controller 800 stops the circulation pump 510 and the first pump 560, and then operates a membrane separation suction pump (not shown) of the membrane separation tank 500 to perform a membrane separation process. Filtration by the membrane separation process produces treated water and slurry.

The treatment water is introduced into the disinfection tank 600 by the transfer pump 520 and then discharged to the outside, and the slurry is introduced into the concentration tank 700. A flocculant pumped by the second pump 570 may flow into the concentration tank 700. The slurry is then discharged to the outside in the concentration tank (700).

In the controller 800, the mixing time and the membrane separation time may be set according to a user's selection. Admixture time and membrane separation time may be set differently according to site conditions, sewage type and the like.

In addition, the membrane separation suction pump (not shown) is preferably not operated together with the circulation pump 510 / first pump 560. This is because when the two are simultaneously operated, chemical and biological treatments are performed together, and fouling occurs in a separator (not shown) in the membrane separator 500 to reduce the lifetime of the separator and lower treatment efficiency.

To this end, the control unit 800 may be programmed to control the operation of the membrane separation suction pump (not shown) of the circulation pump 510 / first pump 560.

For example, when the control unit 800 attempts to operate the circulation pump 510 and the first pump 560 due to a preset mixing time, and the membrane separation suction pump (not shown) is in operation, the controller 800 After waiting for the operation of the circulation pump 510 and the first pump 560 and even starting the membrane separation suction pump (not shown), after the operation of the membrane separation suction pump (not shown) is finished, the circulation pump ( 510 and the first pump 560 may be operated.

For another example, when the control unit 800 attempts to operate the membrane separation suction pump (not shown) due to the preset membrane separation time, the control unit 800 currently operates the circulation pump 510 and the first pump 560. ) Stops the operation of the circulation pump 510 and the first pump 560, and then completely operates the membrane separation suction pump (not shown) for a predetermined membrane separation time, and then the operation of the membrane suction pump (not shown) When it is finished, the circulation pump 510 and the first pump 560 may be operated again. The operation time may be controlled to be the remaining time remaining of the mixing time at which the circulation pump 510 and the first pump 560 should operate.

By such a control method, the life of the separator can be extended and more effective treatment can be achieved.

EXAMPLES Explanation of Effects of Immersion MBR System According to the Present Invention

The actual sewage with the properties shown in FIG. 4 was applied to the immersed MBR system according to the invention. The CODmn and TP concentrations of raw water were 69 mg / L and 3.8 mg / L, respectively, higher than those of general public sewage treatment plants. The difference between the concentrations of TP and SP was 3.5 mg / L. there was.

Application conditions of the immersion type MBR system according to the present invention are as shown in FIG. The condition shown in FIG. 5 is a numerical range that enables the inventors to secure optimum processing efficiency through a number of experiments. In particular, a number of jar tests were conducted to determine the flocculant input concentration, as shown in FIG. 6.

Generally, aluminum salts such as aluminum sulfate and polyaluminum chloride or iron salts such as ferrous chloride and ferric chloride are used as flocculants, but aluminum salts with less effect of a separator are used here.

Application results of the immersion type MBR system according to the present invention are shown in FIGS. 7 to 9.

As shown, it was confirmed that the treatment efficiency by the immersion-type MBR system according to the present invention is superior to the prior art, in particular, it can be lowered to TP below 0.2ppm when added 5 days a week.

For this reason, the inventors have found that, according to a number of experiments, the economic and efficient amount of flocculant injection is 9-11 L, preferably about 10 L per day. Conventionally, the preferred amount of flocculant injection was 30L per day, resulting in about 67% of flocculant savings.

Although the preferred embodiments of the present invention have been described, the present invention is not limited to the specific embodiments described above. That is, those skilled in the art to which the present invention pertains can make many changes and modifications to the present invention without departing from the spirit and scope of the appended claims, and all such appropriate changes and modifications are possible. Equivalents should be considered to be within the scope of the present invention.

100: sump
200: drum screen
300: anoxic
400: anaerobic tank
500: membrane separation tank
510: circulation pump
520: transfer pump
550: flocculant tank
560: the first pump
570: second pump
590 U-shaped inline mixer
591, 593: Venturi Hall
591a, 593a: Venturi tube valve
592: U-shaped connector
600: disinfectant
700: thickening tank
800: control unit

Claims (11)

Anaerobic bath;
An anaerobic tank in fluid communication with the anoxic tank;
A membrane separation tank in fluid communication with the anaerobic tank; And
U-shaped inline mixer in fluid communication with the membrane separator
An immersion type MBR (membrane bioreactor) system comprising:
The U-shaped in-line mixer comprises one or more venturi tubes and U-shaped connectors, and
The membrane separation tank may pump raw water into the U-shaped inline mixer, and the coagulant tank may pump the coagulant into the U-shaped inline mixer.
Immersion MBR System.
The method of claim 1,
At least one venturi tube of the U-shaped in-line mixer consists of a first venturi tube and a second venturi tube, and
The first venturi tube and the second venturi tube is characterized in that connected by being located up and down by the U-shaped connecting pipe,
Immersion MBR System.
The method of claim 2,
The length of the first venturi tube and the second venturi tube, characterized in that more than 2m,
Immersion MBR System.
The method of claim 1,
The immersed MBR system further comprises a thickening tank in fluid communication with the membrane separation tank, and
Coagulant in the coagulant tank is introduced into the U-shaped in-line mixer through a first pump and into the thickening tank through a second pump, and
Sludge is discharged from the thickening tank, characterized in that
Immersion MBR System.
The method of claim 4, wherein
The submerged MBR system further comprises a sump, and
Raw water introduced through the sump is screened through a drum screen, characterized in that the inflow into the anoxic tank,
Immersion MBR System.
The method of claim 5, wherein
The immersed MBR system further comprises a disinfection tank, and
Raw water treated in the membrane separation tank is characterized in that the flow into the disinfection tank,
Immersion MBR System.
The method according to claim 6,
The membrane separation tank, characterized in that it comprises a circulation pump for pumping the raw water to the U-shaped in-line mixer and a membrane separation suction pump for the membrane separation process,
Immersion MBR System.
The method of claim 7, wherein
The immersion type MBR system further includes a control unit, and
The control unit is characterized in that the control to be made only one of the operation of the operation of the first pump and the circulation pump or the membrane separation suction pump,
Immersion MBR System.
The method of claim 8,
Adjacent to one side of the coagulant tank the first pump and the second pump are located in parallel,
The U-shaped inline mixer is located adjacent to the other side of the flocculant tank, and
The control unit is located on the side of the first pump and the second pump, and above the portion of the U-shaped in-line mixer,
Immersion MBR System.
A first venturi tube in fluid communication with the membrane separation tank;
A second venturi tube positioned below or above the first venturi tube and in fluid communication with the coagulant tank; And
It comprises a U-shaped connecting pipe connecting the first venturi tube and the second venturi tube,
Characterized in that the raw water introduced from the membrane separation tank and the flocculant introduced from the flocculant tank are mixed while generating a vortex therein,
U-shaped inline mixer for submerged MBR systems.
11. The method of claim 10,
The length of the first venturi tube and the second venturi tube, characterized in that more than 2m,
U-shaped inline mixer for submerged MBR systems.

Images