KR101550216B1 - Hollow fiber membrane module and membrane bio reactor using hollow fiber membrane module - Google Patents

Abstract

The present invention relates to a hollow fiber membrane module including: a lower frame which has an open top and an open bottom and includes a plurality of fixated bars mounted at intervals thereon; a plurality of U-shaped hollow fiber membranes which are mounted on the fixated bars at intervals and have open upper ends; a fixated header which includes a plurality of through holes to allow the upper ends of the U-shaped hollow fiber membranes to penetrate the same; and a water collection header which is mounted on an upper portion of the fixated header and includes a treated water outlet which discharges treated water filtrated by the U-shaped hollow fiber membranes.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hollow fiber membrane module and a membrane separation bioreactor using the hollow fiber membrane module. 2. Description of the Related Art Hollow fiber membrane module,

The present invention relates to a hollow fiber membrane module capable of enhancing the membrane filtration efficiency and controlling the deposition of contaminants into the hollow fiber membrane to prolong its service life. The present invention relates to a hollow fiber membrane module having excellent energy efficiency, And a separation bioreactor.

Recently, due to population increase, urbanization and rapid development of industry, environmental pollution has rapidly progressed and damage to the water quality environment has become a serious problem. Furthermore, nutrients such as nitrogen and phosphorus are introduced into rivers and lakes, causing eutrophication, which causes problems such as destruction of aquatic ecosystem due to the death of fish species, decrease in water utilization value, and increase in water treatment cost.

In order to solve such problems, devices for simultaneously treating nitrogen and phosphorus, including organic matter, by physical, chemical, or biological unit processes have been developed.

Membrane bio reactors (MBRs) have been proposed as typical ones.

On the other hand, there are many examples of such devices in which a hollow fiber membrane module is used in a membrane separation vessel.

For example, in Japanese Unexamined Patent Publication (Kokai) No. 7-24264, air bubbling is continuously or continuously applied to hollow fibers by bubbles supplied from the acid pores of the acid substrate provided below the sheet-shaped flat hollow fiber module A method of filtrating a liquid while intermittently performing a filtration process in which a membrane module is disposed such that a sheet surface is in a vertical direction and a hollow fiber is in a horizontal direction and the hollow fiber membrane is vibrated by air bubbling to cause a swirling flow Method is disclosed.

However, even with the above-described technique, it is difficult to achieve sufficient microfibers efficiency, and it is not easy to remove contaminants deposited on the upper side of the hollow fiber yarn, so that the durability of the hollow fibers is short.

Japanese Patent Application Laid-Open No. 7-24264

Accordingly, it is an object of the present invention to provide a hollow fiber membrane module capable of controlling membrane contamination with excellent filtration efficiency, and a membrane separation bioreactor using the same.

The hollow fiber membrane module of the present invention comprises: a lower frame having upper and lower openings and a plurality of fixing bars installed at regular intervals; A plurality of U-shaped hollow fiber membranes mounted at predetermined intervals on the fixed bar and having open tops; A fixed header in which a plurality of through holes are formed through the upper end of the U-shaped hollow fiber membrane; And a collecting header formed on the fixed header and having a treated water outlet for discharging the treated water filtered through the U-shaped hollow fiber membrane.

As one example, the U-shaped hollow fiber membrane may be formed by adding 0.5 to 4 parts by weight of cellulose acetate, 1 to 5 parts by weight of manganese oxide, 1 to 3 parts by weight of catechin to the total weight of the polymer resin, Or a combination thereof.

As one example, a collection port is formed on the outside of the fixed header to extend downward to surround the U-shaped hollow fiber membrane from the outside, and the bubble is collected at the upper end of the U-shaped hollow fiber membrane.

For example, a conical guide space may be formed in the center of the water collecting header so as to communicate with the process water outlet, and the collecting header slides up and down in the fixed header.

More preferably, the fixed header has upper and lower flanges formed at upper and lower ends thereof, and a slide column portion is formed between the upper and lower flanges. The lower end of the water collecting header is opened to communicate with the guide space, And the lower end of the slide portion is formed with a hooking edge which is smaller in diameter than the slide portion, and the hooking edge of the catching header is engaged with the upper and lower flanges when the water collecting header is interlocked with the upper and lower flanges, respectively. do.

More preferably, the upper flange and the engaging rim are formed with teeth facing each other.

More preferably, the upper flange is equipped with a plurality of springs.

Meanwhile, the membrane separation bioreactor of the present invention comprises: an anaerobic tank for receiving raw water continuously or intermittently and maintaining the anaerobic environment; A shared tank which is adjacent to the anaerobic tank and which repeatedly forms anaerobic and aerobic environments; A membrane separation tank adjacent to the common tank and having the hollow fiber membrane module for removing solid matter of the influent water and discharging the treated water through the hollow fiber membrane module; And an automatic operation control panel for monitoring and controlling operation of the anaerobic tank, the common tank, and the membrane separation tank.

A first conveying means for conveying the treated water of the sharing tank to the anaerobic tank as an example and a second conveying means for conveying the treated water of the membrane separation tank to the shared tank, And a first transfer pipe connected to the first transfer pipe so that both the first transfer pipe and the second transfer pipe are communicated with each other to be openable and closable, And a second transfer pipe connected to the second transfer pipe, the second transfer pipe being connected to the first transfer pipe and the second transfer pipe so that both the first and second transfer pipes can be opened and closed.

As described in detail above, the hollow fiber membrane module of the present invention is excellent in filtration efficiency and has an advantage of extending the service life by controlling deposition of contaminants.

In addition, the membrane separation bioreactor of the present invention has an advantage that membrane filtration efficiency can be improved by using the hollow fiber membrane module.

1 is a perspective view of a hollow fiber membrane module according to the present invention,
FIG. 2 is an operational state diagram of the hollow fiber membrane module shown in FIG. 1,
3 is an operational state diagram showing an embodiment of the hollow fiber membrane module of the present invention,
4 is an operational state diagram showing another embodiment of the hollow fiber membrane module of the present invention,
FIG. 5 is an operational state diagram showing an embodiment of the hollow fiber membrane module shown in FIG. 4,
FIG. 6 is an operational state diagram showing another embodiment of the hollow fiber membrane module shown in FIG. 4,
FIG. 7 is an overall configuration diagram of the membrane-separation bioreactor of the present invention,
8 is another embodiment of the membrane-separation bioreactor of the present invention.

Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings.

1 and 2, the hollow fiber membrane module 100 of the present invention includes a lower frame 110 having upper and lower openings and a plurality of fixing bars 111 mounted at regular intervals; A plurality of U-shaped hollow fiber membranes (120) mounted at predetermined intervals on the fixed bar (111) and having open tops; A fixed header 130 in which a plurality of through holes 131 are formed through the upper end of the U-shaped hollow fiber membrane 120; And a collecting header 140 mounted on the fixed header 130 and formed with a treated water outlet 141 for discharging the treated water filtered through the U-shaped hollow fiber membrane 120.

Although the hollow fiber membrane module 100 of the present invention has a rectangular tube shape as a whole in FIG. 1 and the like, it is natural that the shape of the hollow fiber membrane module 100 may be variously changed according to a circular tube shape or other installation conditions.

6 and 7, bubbles are discharged from the lower part by the air diffuser 160 or the like so that the bubbles penetrate through the lower frame 110, So that contaminants deposited in the hollow fiber membrane 120 are removed.

1 and 2, the U-shaped hollow fiber membrane 120 is hooked to the fixing bar 111 at the lower part by mounting a fixing bar 111 parallel to the upper part of the lower frame 110 at a predetermined interval, To be fixed.

The U-shaped hollow fiber membrane 120 has hollows formed therein, and the material itself is made of a porous material. The waste water is filtered through the U-shaped hollow fiber membrane 120, To the top.

The U-shaped hollow fiber membrane 120 is mounted on the fixing bar 111 at a predetermined interval and is not shown in the drawing, but a support frame is formed to define a gap between the U- It is proper to keep the gap between the first and second electrodes 120.

In the present invention, the U-shaped hollow fiber membrane 120 is manufactured using a porous polymer resin.

In the polymer resin, 0.5 to 4 parts by weight of cellulose acetate, 1 to 5 parts by weight of manganese oxide and 1 to 5 parts by weight of catechin are contained in the polymer resin, 1 to 3 parts by weight are added.

The cellulose acetate is added as a hydrophilic agent to improve the membrane fouling resistance of the U-shaped hollow fiber membrane 120 made of a polymer resin such as PVDF. The reason for limiting the above range is that if the amount is less than the above range, its functionality can not be expected, and if it exceeds the above range, compatibility with the polymer resin is lowered.

On the other hand, even if the U-shaped hollow fiber membrane 120 is made hydrophilic by adding cellulose acetate to the polymer resin, the microorganism used for the biological treatment, such as a high concentration MLSS (mixed liquer suspended solid) And the film is exposed to cause contamination of the film, thereby deteriorating the performance of the film.

In particular, microbial cells, colloidal materials EPS, SMP, and proteins, which are components of MLSS, have a weak negative charge due to the selective adsorption of anions, especially hydroxyl ions, in the medium. However, U-shaped hollow fiber membranes ) Has a weak positive charge as opposed to MLSS, so that there is a problem that the MLSS constituent material which is negatively charged on the surface of the membrane which is weakly positively charged due to an electrical stress adheres to the membrane, thereby increasing the membrane contamination. Accordingly, manganese oxide is added to the U-shaped hollow fiber membrane 120.

The manganese oxide exhibits a negative charge at pH 6 to 8 and generates MLSS and repulsive force, so that the membrane contamination can be controlled. The reason for limiting the manganese oxide to the above range is that if it is below the above range, its functionality can not be expected. If it exceeds the above range, the negative charge is excessively exhibited and rather the film contamination can be caused by adsorption of the metal component. .

Also, the catechin is added as an antioxidant to prevent the U-shaped hollow fiber membrane 120 itself from being oxidized by the contaminants deposited in the U-shaped hollow fiber membrane 120, so as to ensure durability.

The fixed header 130 corresponds to a structure in which a plurality of through holes 131 are formed through the upper end of the U-shaped hollow fiber membrane 120 to fix the U-shaped hollow fiber membrane 120 at the upper end.

The water collecting header 140 is installed on the fixed header 130 and has a treated water outlet 141 for discharging the treated water filtered through the U-shaped hollow fiber membrane 120. The U-shaped hollow fiber membrane 120 So that the treated water is collected through the treated water outlet 141 and discharged to the outside through the treated water outlet 141.

The suction force acting from a pump connected to the treated water outlet 141 is transmitted to the U-shaped hollow fiber membrane 120, respectively, although not shown in the drawing, and the suction force of each U Shaped hollow fiber membrane 120, and the waste water is filtered and sucked.

The treated water sucked into each U-shaped hollow fiber membrane 120 is guided to the collecting header 140 and discharged to the outside through the treated water discharging port 141.

Meanwhile, the hollow fiber membrane module 100 may be exposed to the problem of clogging due to deposition of contaminants on the upper end of the U-shaped hollow fiber membrane 120, respectively. Accordingly, the present invention proposes the respective embodiments in FIGS. 3 to 6. FIG.

3, a U-shaped hollow fiber membrane 120 is formed on the outside of the fixed header 130 to form a collecting hole 170 extending downward and surrounding the U-shaped hollow fiber membrane 120 from the outside. And the bubble is captured at the upper end.

As shown in FIG. 3, the collector 170 is fixed outside the fixed header 130 and has a frame that covers the U-shaped hollow fiber membrane 120 downward from the fixed header 130, .

The reason why the collecting port 170 is formed is that the bubble is discharged to the upper U-shaped hollow fiber membrane 120 by the diffuser 160 at the lower portion of the lower frame 110 as shown in FIG. So that the bubbles are collected in the trapping space formed by the collecting tool 170 so that the contact time with the foreign matter deposited on the upper end of the U-shaped hollow fiber membrane 120 is prolonged.

As described above, the contact time between the foreign matter deposited on the upper end of the U-shaped hollow fiber membrane 120 and the bubble is prolonged so that the foreign matter is directly oxidized and decomposed or the foreign matter is separated from the U- .

More preferably, the collecting port 170 is formed so that a portion extending downward from the fixed header 130 has a larger diameter in a downward direction, so that more bubbles are received, and a bubble It is reasonable to let it easily escape to the outside.

4, a conical guide space 142 is formed in the center of the collecting header 140 so as to communicate with the treated water discharging port 141, and the collecting header 140 Are slid up and down in the fixed header 130. In the example of FIG.

The guide space 142 serves to collect and guide the treated water introduced through the U-shaped hollow fiber membrane 120 to the treated water outlet 141. The water collecting header 140 is configured to slide up and down in the fixed header 130 because the treated water discharged through the U-shaped hollow fiber membrane 120 by pumping hits the conical guide space 142, The water collecting header 140 is slid upward in the fixed header 130 so that the collecting header 140 strikes the fixed header 130 by the constitution described below, The vibration due to the impact is generated in the vibration isolator 130.

These vibrations cause each of the U-shaped hollow fiber membranes 120, especially the pollutants deposited at the upper end thereof to be separated by vibration, and the separated pollutants are decomposed or suspended by the bubbles to be removed.

To this end, upper and lower flanges 132 and 133 are formed on the upper and lower ends of the fixed header 130, a slide post 144 is formed between the upper and lower flanges 132 and 133, Is formed with a slide portion 143 which is opened at the lower end and communicates with the guide space 142 and surrounds the outer periphery of the slide column portion 144. The slide portion 143 has a diameter smaller than that of the slide portion 143 The lower end flange 132 and the lower flange 133 may be engaged with the catching header 140 when the collecting header 140 is coupled to the upper and lower flanges 132 and 133, respectively.

That is, when the collecting header 140 slides upward in the fixed header 130 by the discharge pressure of the treated water from the U-shaped hollow fiber membrane 120, the catching rim 144 hits the upper flange 132, And when the discharge pressure of the treated water from the U-shaped hollow fiber membrane 120 is small or does not exist, the raised collecting header 140 slides downward from the fixed header 130 so that the engaging rim 144 ) Strikes the lower flange 133 so that the fixed header 130 generates vibration.

By this operation mechanism, it is possible to remove the contaminants deposited on the upper end portion of the U-shaped hollow fiber membrane 120 during the operation, thereby improving the operation efficiency. In addition, the U-shaped hollow fiber membrane 120 can be durable It is possible to control the degradation.

Further, in the present invention, two schemes for doubling the efficiency of the above-mentioned operating mechanism are proposed.

5 shows an example in which teeth 135 and 145, which are opposite to each other, are formed on the upper flange 132 and the engaging rim 144, respectively.

The reason why the teeth 135 and 145 are further configured is that the collecting head 140 is moved from the U-shaped hollow fiber membrane 120 to the slide part 134 The rotation of the collecting header 130 in the process of engaging the teeth 145 of the engaging rim 144 with the teeth 135 of the upper flange 132 is generated So that the hooking edge 144 strikes the upper flange 132.

That is, due to the action of the teeth 135 and 145, longitudinal vibration as well as longitudinal vibration are simultaneously generated in the fixed header 130, so that the removal efficiency of contaminants from the U-shaped hollow fiber membrane 120 can be further increased .

Although not shown in the figure, the inner diameter of the slide portion 134, the upper rim 132, the inner rim of the latching rim 144, the inner diameter of the slide pillar 144, the inner diameter of the guide space 142 The cross section of the back should be circular. That is, it is necessary to mount the collecting header 140 in the fixed header 130 so as to be rotatable.

Another example shows an example in which a plurality of springs 136 are mounted on the upper flange 132 as shown in FIG.

A plurality of springs 136 may be mounted on the lower surface of the upper flange 132 so that the catching header 140 hits the upper flange 132 by the upward slider in the fixed header 130, The vibration generated by the striking is multiplied through the spring 136 by the plurality of springs 136 formed on the upper flange 132 so that the vibration transmitted to the fixed header 130 It is doubled. In other words, due to the larger vibration energy, the desorption efficiency of contaminants from the U-shaped hollow fiber membrane 120 can be further increased.

As shown in FIGS. 7 and 8, the membrane separation bioreactor of the present invention comprises an anaerobic tank 20 containing raw water continuously or intermittently introduced therein and maintaining the anaerobic environment; A shared tank adjacent to the anaerobic tank (20) for repeatedly forming anaerobic and aerobic environments; A membrane separation tank (40) adjacent to the common tank (30) and provided with the hollow fiber membrane module (100) to remove solid matter of influent water, and discharging treated water through the hollow fiber membrane module (100); And an automatic operation control panel (80) for monitoring the operation of the anaerobic tank (20), the sharing tank (30), and the membrane separation tank (40).

The anaerobic tank 20 and the common tank 30 or the common tank 30 and the membrane separation tank 40 are connected to the aeration, 1102536, etc.), it is possible to carry out the feeding and returning of the treated water repeatedly depending on the presence or absence of the aeration, that is, the anaerobic or aerobic environment, so that the wastewater is circulated continuously .

In this case, the circulation of the MLSS (mixed liquor suspended solid) between the anaerobic tank 20 and the common tank 30 or the common tank 30 and the membrane separation tank 40 is time- The circulating means is constituted by an aeration (liquid transfer) means which functions as the aeration, stirring and liquid transfer device 10, and as the transfer means, the first transfer means 50 and the second transfer means 60).

The sharer 30 communicates with the membrane separation tank 40 due to the aeration action of the aeration, stirring, and liquid transfer device 10 at the expiration time, and circulates the treated water to perform the exhalation process. Conversely, in the anaerobic time zone, the anaerobic process is interrupted by the stirring operation of the aeration, stirring, and liquid transfer device 10, and the anaerobic process is performed by communicating with the anaerobic tank 20 to circulate the process water .

In this way, according to the anaerobic condition and the expiratory condition, the two adjacent baths are simultaneously subjected to the anaerobic condition and the exhalation condition, so that the reaction treatment time can be shortened.

First, the anaerobic tank 20 receives raw water continuously or intermittently, which may be determined depending on the quantity of the influent raw water and whether or not the flow rate adjusting tank is installed on the upstream side of the anaerobic tank 20. In addition, although the inflow point of the sewage from the sewer pipe can be the upper part of the anaerobic tank 20, it is natural that the height of the sewage inflow point can be different according to the depth of the sewer pipe installed.

The anaerobic tank 20 is connected to the common tank 30 and the aeration, mixing and liquid transfer device 10 and the first transfer means 50 as the common tank 30 is operated in the anaerobic environment, The MLSS included in the MLSS is circulated.

The anoxic tank 20 and the common tank 30 communicate with each other at the bottom by the action of the aeration, stirring and liquid transfer device 10 installed at the lower part of the common tank 30, The first conveying pipe 51 and the first conveying valve 52 for opening and closing the first conveying pipe 51 are constituted by the first conveying means 50 So that the anaerobic tank 20 and the common tank 30 communicate with each other at the upper part.

At this time, the first transfer pipe 51 is configured to be relatively smaller than the inner diameter D2 of the other side to which the inner diameter D1 of the one side to be discharged flows, so that the sludge is stirred It is desirable to be able to help.

This is because the cross sectional area of one inner diameter D1 is smaller than the other inner diameter D2 due to the Bernoulli theorem and the pressure of the one inner diameter D1 is lowered and the flow rate of the conveyed liquid to be conveyed becomes relatively faster . Thus, the agitation of the sludge, which is moved from the anaerobic tank 20 to the common tank 30, can be performed together with the aeration, stirring, and liquid transfer device 10 by the carrier liquid having a high flow rate.

In this manner, in the anaerobic tank 20, the anaerobic environment is maintained together with the common tank 30 to perform hydrolysis and removal of organic substances contained in the influent raw water, and denitrification (NO 3 → N 2) of nitrate in the influent and return water Leading to phosphorus release by phosphorus removal microorganisms.

In this anaerobic environment, in the present invention, the liquid is transferred from the anaerobic tank 20 to the common tank 30 by the action of the aeration, stirring and liquid transfer device 10, and the liquid is transferred to the anaerobic tank 20 and the shared tank 30 ) Is used for stirring the sludge agitatingly for the sake of brewing, and it is intended to increase the chance of contact between organic matter and microorganisms due to the stirring action.

The membrane separation tank 40 is in contact with one side surface of the common tank 30 and is connected to the aeration, mixing and liquid transfer unit 10 and the second transfer unit 60 The circulation of the MLSS contained in the treated water of the sharing tank 30 is performed. The communication between the two vessels by the second conveying pipe 61 and the second conveying valve 62 as the aeration, stirring and liquid conveying device 10 and the second conveying means 60 is performed by the above-mentioned anaerobic tank 20, Liquid transfer device 10 and the first tank 30 between the aeration / liquid transfer device 10 and the first transfer means 50, the description thereof will be omitted.

The function of the membrane separation unit 40 is to receive the treated water to be treated and circulated from the sharing tank 30 according to the breath environment of the sharing tank 30 and to perform the breathing process together with the sharing tank 30 The solid material contained in the treated water is removed. At this time, in the exhalation process of the common tank 30 and the membrane separation tank 40, the phosphorus released in the anaerobic process in the previous stage is absorbed by the phosphorus removal microorganisms, and the final removal is discharged to the outside together with the sludge.

Accordingly, according to a preferred embodiment of the present invention, there is provided a sludge discharging means 70 for discharging surplus sludge containing microorganisms generated in the circulation process of the membrane separation tank 40 and the sharing tank 30.

Specifically, the sludge discharging means 70 includes a sludge discharge pipe 71. When the load of the microorganisms in the raw water flowing into the anaerobic tank 20 is low, a part of excess sludge containing microorganisms is discharged to the anaerobic tank 20 20 to the sludge return pipe 72 to be treated.

The sludge discharge pipe 71 is connected to the lower portion of the common tank 30 to be opened and closed. The sludge discharge pipe 71 is connected to the sludge discharge pipe 71, 30) and discharges the excess sludge through the sludge discharge pipe (71).

The sludge return pipe 72 is connected to the lower sludge discharge pipe 71 of the anaerobic tank 20 so as to be opened and closed so that part of the surplus sludge containing microorganisms discharged through the sludge discharge pipe 71 is re- 20), it is possible to control the amount of microorganisms to be loaded in the anaerobic tank 20.

Referring to the membrane separation tank 40, the membrane separation tank 40 performs solid-liquid separation, and the hollow fiber membrane module 100 is provided. The membrane separator (40) includes a discharge pipe (150) for discharging treated water from the hollow fiber membrane module (100) to the outside.

7, in order to prevent clogging of the hollow fiber membrane module 100, the membrane separation tank 40 is connected to the aeration / The vortex in which the air is dissolved by the aeration, stirring, and liquid transfer device 10 is scattered from the lower portion of the hollow fiber membrane module 100. In addition, as shown in FIG. 8, the air diffuser (40) can separately constitute the air diffuser (160) to control clogging.

In addition, according to a preferred embodiment of the present invention, the aeration, stirring and liquid transfer device 10 is configured in the shared bath 30 to supply the air necessary for the bath, and the aeration, So that the vortex in which the air is dissolved is scattered from the lower portion of the sharing tank 30. [

Also, in the present invention, the automatic operation control panel 80 can be configured to automatically monitor and control the above-described operating conditions of the present invention. That is, the anaerobic tank 20, the common tank 30, and the membrane separation tank 40, and automatically controls operation.

7, the automatic operation control panel 80 is provided in the membrane separation tank 40 in cooperation with the pressure gauge in the hollow fiber membrane module 100, The control of the amount of air and the like can be performed. In FIG. 8, the air amount of the air diffuser 160 is adjusted to perform smooth operation automatically.

It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit or scope of the invention. Therefore, the technical scope of the present invention should not be limited to the contents described in the detailed description of the specification, but should be defined by the claims.

100: hollow fiber membrane module

Claims (9)

A lower frame having upper and lower openings and equipped with a plurality of fixing bars at regular intervals;
A plurality of U-shaped hollow fiber membranes mounted at predetermined intervals on the fixed bar and having open tops;
A fixed header in which a plurality of through holes are formed through the upper end of the U-shaped hollow fiber membrane; And
And a water collecting header mounted on the fixed header and having a treated water outlet for discharging the treated water filtered through the U-shaped hollow fiber membrane,
Wherein the water collecting header has a conical guide space formed therein to communicate with the process water outlet at a central portion thereof, and slides up and down in the fixed header.
The method according to claim 1,
The U-shaped hollow fiber membrane is formed by mixing 0.5 to 4 parts by weight of cellulose acetate, 1 to 5 parts by weight of manganese oxide, and 1 to 3 parts by weight of catechin, based on the total weight of the polymer resin forming the porous structure Wherein the hollow fiber membrane module is fabricated from a hollow fiber membrane module.
The method according to claim 1,
And a bubble collecting unit for collecting bubbles at the upper end of the U-shaped hollow fiber membrane. The hollow fiber membrane module according to claim 1, wherein the U-shaped hollow fiber membrane has a U-shaped hollow fiber membrane.
delete The method according to claim 1,
The fixed header includes upper and lower flanges at upper and lower ends, a slide post is formed between the upper and lower flanges,
The water collecting header includes a slide portion having a lower end opened and communicating with the guide space and surrounding the outer periphery of the slide column portion, and a lower end of the slide portion is formed with an engagement protrusion having a smaller diameter than the slide portion, And the hooking edge is hooked on the upper and lower flanges, respectively.
6. The method of claim 5,
And wherein teeth of the hollow fiber membrane module are mutually opposed to each other in the upper flange and the hooking rim.
6. The method of claim 5,
And a plurality of springs are mounted on the upper flange.
An anaerobic tank for receiving continuous or intermittently introduced raw water and maintaining the anaerobic environment;
A shared tank which is adjacent to the anaerobic tank and which repeatedly forms anaerobic and aerobic environments;
The hollow fiber membrane module according to any one of claims 1 to 3, wherein the hollow fiber membrane module is provided adjacent to the shared bath to remove solid matter of the influent water, Membrane separation tank; And
And an automatic operation control panel for monitoring the anaerobic tank, the common tank, and the membrane separation tank and controlling the operation of the membrane separation bioreactor.
9. The method of claim 8,
A first transporting means for transporting the treated water of the sharing tank to the anaerobic tank and a second transporting means for transporting the treated water of the membrane tank to the sharing tank,
Wherein the first conveying means comprises:
A first conveying pipe installed on the side of the upper portion of the tank and connected to the anaerobic tank so as to be openable and closable, and a first conveying valve connected to the first conveying pipe,
The second conveying means
A second transfer pipe provided on the upper side of the membrane separation tank and communicating with both the first transfer pipe and the second transfer pipe so as to be opened and closed; and a second transfer valve connected to the second transfer pipe.

Images