KR20180116806A - Bio-reactor for sewage treatment and sewage treatment system comprising the same - Google Patents

Abstract

The present invention relates to a bioreactor for sewage treatment and a sewage treatment system comprising the same. In particular, the bioreactor for sewage treatment comprises an aerobic tank, a membrane bio reactor (MBR), and an aerobic tank. The aerobic tank comprises: an inlet which supplies sewage; a mixing cell which receives the sewage to mix the same with activated sludge; an aerobic reactor which is continuously connected to the mixing cell and allows the activated sludge to adsorb to organic matters; and an outlet which discharges the sewage containing the organic matters adsorbed to the activated sludge in the aerobic reactor. The MBR is configured to isolate the sludge including the organic matters adsorbed thereto from the sewage discharged through the outlet of the aerobic tank. The anaerobic tank is configured to conduct a denitrification process of treated water having passed through the MBR by using anaerobic ammonium-oxidizing bacteria (anammox). In particular, the MBR is configured to eliminate foreign materials attached to a separation membrane by reciprocating the separation membrane. By using the MBR after coagulating a large amount of organic matters contained in the sewage in an organic matter coagulator main body, a compact-type bioreactor for sewage treatment provided in the present invention can perform solid-liquid separation with a high efficiency, thereby reducing the treatment time, and can significantly reduce the amount of sludge being discharged by enabling the separated sludge to be reused.

Description

Technical Field [0001] The present invention relates to a bioreactor for sewage treatment and a sewage treatment system including the bioreactor,

The present invention relates to a bioreactor for sewage treatment and a sewage treatment system including the bioreactor. More particularly, the present invention relates to a bioreactor which is used in treating sewage, food waste or animal wastes, Sewage treatment system.

Conventional sewage treatment facilities mainly use the standard activated sludge process or an additional or modified method of the above method, and use A2 / O process, UCT process, VIP process, etc. in foreign countries, and the above- The A / O process is a biological treatment process for removing nitrogen and phosphorus by improving the A / O process. The reaction tank is an anaerobic tank, an anoxic tank, (Anoxic Tank) and Aerobic Tank. It consists of Nitrifer Recycle to remove nitrate nitrogen and settler sludge return. In anaerobic tank, it releases phosphorus in anaerobic condition, And the anoxic tank removes nitrogen and phosphorus by denitrifying nitrate in the aerobic tank's internal return water.

The A ₂ / O process removes nitrogen and phosphorus from the sewage to reduce nutrients in the sewage but focuses only on the removal of nitrogen and phosphorus in the sewage. In recent years, harmful bacteria and microorganisms There is a problem that it can not be removed.

The sewage treatment plant is operated as a biological treatment method using a method in which the pollutants are decomposed by microorganisms. The biological treatment method has proved its performance for a long time and is the most effective and safe method, but the problem is that excess sludge occurs.

Most of the excess sludge is a microbial mass, which is an organic matter, so it is easy to decay, which is a problem. So far, we have mainly relied on marine dumping and some have been landfilled or incinerated. The amount of surplus sludge generated is more than 10,000 tons per day in 2012, more than 3.65 million tons of sludge per year, and will continue to increase in the future.

As for the treatment of surplus sludge, since 2012, marine dumping has been banned and policies for promoting renewable energy conversion of organic wastes such as waste materialization, energy conversion and reduction have been promoted. Especially, in carrying out sludge treatment through anaerobic digestion tank, A pretreatment process for solubilization is carried out in order to increase the water content of the microorganisms. Examples of the pretreatment techniques include a biological method using high temperature aerobic microorganisms, a physical method using ultrasonic waves and hydrodynamic cavitation and thermal hydrolysis and ball milling apparatus, A chemical treatment method, a complex treatment method in which a plurality of the treatment methods are combined, and an electrical method using electrolysis are used, but they are expensive and have a problem in that they are difficult to be put to practical use due to their low cost.

Korean Patent No. 10-135458 discloses a sludge solubilization method for increasing the digestion efficiency of the anaerobic digestion tank, wherein the excess sludge generated in the wastewater treatment process is treated with an alkali catalyst and methanol to soften or destroy the cell membrane of biodegradable microorganisms in the sludge The difficulty of the operation management and the management cost of the anaerobic digestion efficiency by the anaerobic microorganism of the digester are problematic.

An object of the present invention is to provide a bioreactor for sewage treatment which has a simple structure and can minimize a site area, and is excellent in solid-liquid separation efficiency after aggregation of organic matter, thereby reducing sludge generation amount and treatment time.

Another object of the present invention is to provide a sewage treatment system capable of reducing the amount of by-products generated and the treatment time while minimizing site area through a simple structure including the bioreactor provided in the present invention, .

Other objects and advantages of the present invention will become more apparent from the following detailed description of the invention, claims and drawings.

The embodiments of the present invention are described in order to more fully explain the present invention to those skilled in the art, and the following embodiments may be modified into various other forms, It is not limited to the embodiment. Rather, these embodiments are provided so that this disclosure will be more faithful and complete, and will fully convey the scope of the invention to those skilled in the art.

In the drawings, the thickness and the size of each layer are assumed for convenience and clarity of description, and the same reference numerals denote the same elements in the drawings. As used herein, the term "and / or" includes any and all combinations of one or more of the listed items.

The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. As used herein, the singular forms "a," "an," and "the" include singular forms unless the context clearly dictates otherwise. Also, " comprise "and / or" comprising "when used herein should be interpreted as specifying the presence of stated shapes, numbers, steps, operations, elements, elements, and / And does not preclude the presence or addition of one or more other features, integers, operations, elements, elements, and / or groups.

According to an embodiment of the present invention, there is provided a sludge treatment system comprising: a mixing cell which receives an inlet for supplying sewage and sewage and mixes with an activated sludge; And an outlet for discharging sewage containing organic material adsorbed on the activated sludge in the exhalation reaction tank; A separation membrane bioreactor (MBR) for separating sludge that has adsorbed organic matter from sewage discharged through the discharge port of the oxic tank; And an anaerobic tank for carrying out a denitrification process using the anaerobic ammonium-oxidizing bacteria (Anammox), the treated water having passed through the membrane bioreactor (MBR), wherein the membrane bioreactor is configured to reciprocate the membrane, To a biological reaction tank for treatment of wastewater.

In the present invention, the membrane bioreactor (MBR) comprises a membrane support frame; A membrane module mounted on the membrane support frame; A reciprocating means connected to the membrane supporting frame and reciprocating the membrane supporting frame; And a sludge lifting unit disposed at a lower end of the membrane supporting frame and floating the sludge accumulated in the treatment tank.

In the present invention, the separation membrane module may include a plurality of hollow fiber membranes.

In the present invention, the separation membrane bioreactor may further include a sludge supply pipe for transferring the separated sludge to the oxic tank.

In the present invention, the activated sludge may include at least one selected from the group consisting of Ammonia Oxidizing Archaea (AOA), Ammonia Oxidizing Bateria (AOB) and Nitrite Oxidizing Bacteria (NOB).

In the present invention, the exhalation reaction tank may further include an air injection device for injecting air.

In one embodiment of the present invention, the present invention provides a sludge treatment apparatus comprising: a primary sedimentation tank for sedimenting sewage containing sludge to separate into raw sludge and sewage; The above compact bioreactor for adsorbing and separating the organic substances in the sewage separated from the primary settling tank and the activated sludge and conducting the denitrification process; A secondary settling tank for settling the excess sludge in the sewage that has decomposed organic matter in the aeration tank; A dehydrating tank for dehydrating the raw sludge recovered by being settled in the primary settling tank and the excess sludge recovered by precipitation in the secondary settling tank; A digester capable of anaerobically digesting raw sludge and excess sludge dehydrated in a dehydration tank to produce biogas; And an SBR reaction tank for removing nitrogen by reacting the ammonium-containing desalination solution generated in the digester with an anaerobic ammonium-oxidizing bacteria (Anammox).

In the present invention, the bioreactor may include a separation membrane bioreactor (MBR) for separating sludge adsorbing an organic substance.

In the present invention, the membrane bioreactor (MBR) comprises a membrane support frame; A membrane module mounted on the membrane support frame; A reciprocating means connected to the membrane supporting frame and reciprocating the membrane supporting frame; And a sludge lifting unit disposed at a lower end of the membrane supporting frame and floating the sludge accumulated in the treatment tank.

In the present invention, the separation membrane module may include a plurality of hollow fiber membranes.

In the present invention, the separation membrane bioreactor may further include a sludge supply unit for transferring the separated sludge to the oxic tank.

In the present invention, the activated sludge may include at least one selected from the group consisting of Ammonia Oxidizing Archaea (AOA), Ammonia Oxidizing Bateria (AOB) and Nitrite Oxidizing Bacteria (NOB).

In the present invention, the compact aeration tank may further include an air injection device capable of injecting air for adsorption of organic substances in the sewage and activated sludge.

In the present invention, the anaerobic ammonium-oxidizing bacteria (Anammox) may be Planctomycetes.

In the present invention, the anaerobic ammonium-oxidizing bacteria (Anammox) may be a planktonomyces granule.

In the present invention, the SBR reaction tank may include a membrane bioreactor (MBR) for selectively separating activated sludge.

In the present invention, the SBR reaction tank is connected to a treated water storage tank, and the treated water storage tank may include a separation membrane bioreactor for selectively separating activated sludge.

In the present invention, the biogas collector may further include a biogas collector for collecting the biogas generated in the digester.

The biological treatment tank for sewage treatment provided in the present invention is characterized in that a large amount of organic matter contained in the sewage is agglomerated in the organic matter aggregation body and the solid-liquid separation is carried out with high efficiency using a membrane bioreactor, As the sludge is reused, the sludge emission can be significantly reduced. As a result, sewage treatment efficiency per site area can be further improved while minimizing site area.

1 schematically shows the structure of a biological treatment tank for sewage treatment according to an embodiment of the present invention.
2 schematically shows the structure of a biological treatment tank for sewage treatment including conventional MBR.
3 schematically shows the structure of a sewage treatment system according to an embodiment of the present invention.
4 schematically shows the structure of a sewage treatment system according to an embodiment of the present invention.
5 schematically shows the structure of a sewage treatment system according to an embodiment of the present invention.
6 is a perspective view of a separation membrane bioreactor according to an embodiment of the present invention.
7 is a view illustrating a structure of a separation membrane module in a separation membrane bioreactor according to an embodiment of the present invention.
8 is a diagram illustrating a method of calculating the looseness of the present invention.
10: Primary settling tank
20: Bioreactor
21: arousal trough
22: Mixed cell
23: Exhalation reaction tank
24: Membrane bioreactor
25: Anaerobic
26: air injection device
30: the second settling tank
40: dehydration tank
50: digester
60: SBR reactor
61: Treatment tank
62: Membrane bioreactor
63: treated water storage tank
64: treated water supply piping
65: Granule transfer pipe
100: membrane bioreactor
200: round trip means
250: reciprocating frame
300: Treatment tank 310: Inlet port
320: Outlet
400: sludge lifting portion
500: Sliding means
600: membrane support frame
700: separator module 710: upper frame
711: collecting part 720: lower frame
712, 722: spacing portion 730: hollow fiber membrane
900:
1000:

Hereinafter, preferred embodiments of the present invention will be described. However, the embodiments of the present invention can be modified into various other forms, and the scope of the present invention is not limited to the embodiments described below. Further, the embodiments of the present invention are provided to more fully explain the present invention to those skilled in the art.

The sewage treatment bioreactor and sewage treatment system of the present invention will be described with reference to the drawings.

FIG. 1 schematically shows a structure of a bioreactor for sewage treatment according to an embodiment of the present invention. The bioreactor 20 for a sewage treatment of the present invention is a bioreactor for adsorbing organic materials contained in sewage An aerobic tank 21; A separation membrane bioreactor (MBR) 24 for separating sludge adsorbing organic material; And an anaerobic tank 25 for the denitrification process.

In more detail, the bioreactor bioreactor 20 comprises a mixing cell 22 for receiving an inlet for supplying sewage and sewage and mixing the activated sludge with the activated sludge, An aerobic tank (23) for adsorbing the activated sludge and an aerobic tank (20) containing an outlet for discharging sewage containing organic matter adsorbed on the activated sludge in the aerobic tank (23);

A separation membrane bioreactor (24) for separating sludge that has adsorbed organic matter from the sewage discharged through the discharge port of the oxic tank; And

And an anaerobic tank 25 for carrying out a denitrification process using the anaerobic ammonium-oxidizing bacteria (Anammox) as the treated water that has passed through the membrane bioreactor (MBR).

In the present invention, the sewage to be treated is supplied through the inlet of the bioreactor 20, and the activated sludge is mixed and reacted to adsorb the organic substances contained in the sewage. The activated sludge is composed of at least one selected from the group consisting of Ammonia Oxidizing Archaea (AOA), Ammonia Oxidizing Bateria (AOB) and Nitrite Oxidizing Bacteria (NOB), and adsorbs organic substances through activated sludge.

In addition, in the present invention, the mixing cell 22 further includes at least one stirrer to facilitate the mixing process of the sewage and the activated sludge.

In the present invention, the shape of the stirrer is not particularly limited, but may be an impeller type having a blade. Although the shape of the impeller-type agitator is not particularly limited, according to a preferred embodiment of the present invention, the impeller-type agitator is formed such that the outer wing portion is bent toward the lower direction of the inner wing portion, By pushing as much water as possible in the desired direction as if pushing water strongly, it is possible to maximize the stirring effect.

In the present invention, when there are a plurality of stirrers, the blades of the plurality of stirrers may have the same or different diameters, but preferably, the plurality of stirrers having different blade diameters is arranged so as to have a smaller diameter from the upper portion of the chamber toward the lower portion of the chamber The inflow water can be moved from the upper part of the chamber to the lower part to maintain a faster mixing speed.

In this case, the number of revolutions (G-value) of the stirrer blade is not particularly limited and may be appropriately selected according to the size of the agglomeration and agglomeration scale and the size of the chamber, but it may preferably be 30 to 110 sec ^-1 .

The present invention further includes an air injector 26 at the lower end of the exhalation reaction tank 23, so that the activated sludge in the exhalation reaction tank 23 can promote the adsorption of the organic substances contained in the sewage.

Further, in the present invention, an auxiliary agent may be added together with the activated sludge, wherein the auxiliary agent may be selected from the group consisting of clay, calcium hydroxide, a cation flocculant, an anionic flocculant and a non-ion flocculant.

In the present invention, when the organic matter contained in the sewage is grown into floc in the exhalation reaction tank 23 as described above, the treated sewage is supplied to the separation membrane bioreactor 24 connected to the exhalation reaction tank 23. The activated sludge adsorbed by the organic substances contained in the sewage can not pass through the separation membrane bioreactor 24 and remains as a solid sludge. Accordingly, in the present invention, the sewage containing flocs can be separated into the primary sludge and the liquid primary treated water through the separation membrane bioreactor (24).

In the present invention, the membrane bioreactor 24 comprises a membrane support frame; A membrane module mounted on the membrane support frame; A reciprocating means connected to the membrane supporting frame and reciprocating the membrane supporting frame; And a sludge lifting unit disposed at a lower end of the membrane supporting frame and floating the sludge accumulated in the treatment tank.

In the present invention, the separation membrane module may include a plurality of hollow fiber membranes.

In the present invention, the separation membrane bioreactor 24 can remove foreign substances adhering to the separation membrane by reciprocating the separation membrane. Accordingly, FIG. 2 relates to a bioreactor including a conventional membrane bioreactor, wherein the membrane bioreactor can separate the sludge contained in the sewage as a separation membrane, but at this time, the membrane that the foreign matter adsorbs on the separation membrane may be occluded have. In order to prevent clogging of the membrane, an air injection device for cleaning the separation membrane is separately required as shown in Fig. However, in the present invention, the separation membrane bioreactor 24 is configured to reciprocate so that no separate air injection device for cleaning the separation membrane is required. For this reason, compared with the conventional separation membrane bioreactor shown in FIG. 2 So that the power consumption can be minimized.

In addition, in the present invention, the separation membrane bioreactor 24 further includes a sludge supply pipe for transferring the separated sludge to the biological reactor, so that the separated solid sludge can be transferred to the biological reactor 20 again.

3 schematically shows the structure of a sewage treatment system according to an embodiment of the present invention. As shown in FIG. 1, the sewage sludge is sedimented in the primary sedimentation tank 10, the liquid wastewater is separated and transferred to the bioreactor 20, 21); A membrane bioreactor 24; And the anaerobic tank 25, the organic material removal and denitrification process proceeds.

The bioreactor 20 is the same as that shown in FIG. 1, so detailed description will be omitted.

The second treated water from which the nitrogen has been removed in the anaerobic tank 25 stays in the second settling tank 30, the excess sludge is settled and removed, and then discharged through a disinfection process.

The raw sludge and the excess sludge separated and precipitated by the primary settling tank and the secondary settling tank are transferred to the dewatering tank 40, and the dewatering process is performed. The concentrated sludge after the dewatering process is transferred to the digester 50.

In the present invention, the anaerobic digestion process may be performed on the excess sludge and raw sludge using anaerobic microorganisms.

Here, the anaerobic digestion process is also referred to as "methane fermentation", and is a series of processes for converting organic substances contained in the excess sludge into methane by decomposition of various anaerobic microorganisms. More specifically, solid organic matter is liquefied , The process of hydrolysis, the process of producing lower fatty acids (VFA) that produce vinegar acid, propionic acid, and butanoic acid, decomposing them with vinegar acid and H ₂ gas, .

In the present invention, in the digester 50, energy can be recovered by the biogas called methane simultaneously with the treatment of the concentrated sludge. Therefore, in the present invention, it is possible to further include a biogas collector (not shown) for collecting the biogas generated in the digester 50, and if necessary, biogas, which separates methane and carbon dioxide contained in the biogas, And may further include a separator.

In the present invention, when the anaerobic digestion process is performed in the digestion tank 50, digested sludge and desolvation solution, which can not be recycled any more, are generated. In the case of the extinguished sludge, it can be discarded, and the desorbing liquid can be supplied to the SBR reaction tank 60.

The SBR reactor (60) is a sequential batch reactor, which uses a continuous batch activated sludge process. In the conventional SBR process, the reaction and the precipitation of the mixed solution, the drainage of the representative water, and the discharge process of the settled sludge are repeatedly performed by making the reaction tank and the secondary settling tank function in one batch tank.

In the conventional sewage treatment system, after the anaerobic digestion process is carried out using the concentrated sludge in the digestion tank 50, the generated desorption liquid is transferred again to the primary settling tank for reprocessing. However, in this case, the desorbing liquid generated in the digester 50 contains NH ^{4 +} or NO ^{2 -,} and if the sewage treatment is performed in a continuous process, the concentration of nitrogen continuously increases, ) / N (nitrogen) exceeds 1, resulting in a problem that energy production efficiency in the digester 50 is remarkably low.

In order to prevent the above-mentioned problem, the present invention provides a method for removing NH ^{4 +} and NO ² contained in the desalination liquid by transferring the desorbed liquid generated in the digester 50 to the SBR reaction tank 60 and reacting with the anaerobic ammonium-oxidizing bacteria (Anammox) ^- can be converted to N ₂ to remove nitrogen.

In the present invention, the anaerobic ammonium-oxidizing bacteria may be planctomycetes. In general, the AOB bacteria used as the activated sludge in the bioreactor 20 can convert about 50% of NH ^{4 +} to NO ^{2 -} . However, in the present invention, planktonic acid Planctomycetes) may be converted to N ₂ and all of the NH ⁴⁺ NO ^2-. In addition, in the present invention, the planctomycetes adsorb to surrounding organic materials to form granules, wherein the particle size of granules is relatively large compared to AOA, AOB and NOB bacteria And can be selectively separated according to the particle size in the membrane bioreactor 62 as described later.

In the present invention, as described above, when the nitrogen contained in the desorption liquid is removed in the SBR reaction tank 60, the final treated water generated in the SBR reaction tank 60 is transferred to the first settling tank 10 to perform the sewage treatment process The ratio of C (carbon) / N (nitrogen) in the bioreactor 20 can be maintained at 1, and energy production efficiency can be maintained even in a continuous process for sewage treatment.

4 is a schematic view illustrating the structure of a sewage treatment system according to an embodiment of the present invention. Specifically, the SBR reaction tank 60 of the present invention may include a treatment tank 61 and a separation membrane bioreactor 62 .

In the present invention, the desorbed liquid transferred to the SBR reaction tank (60) can be received in the treatment tank (61). In addition, in the present invention, the separation membrane bioreactor 62 includes a separation membrane module, and the separation membrane module may include a plurality of hollow fiber membranes.

In the present invention, the desorbed liquid transferred to the treatment tank (61) is anaerobically digested by the anaerobic ammonium-oxidizing bacteria to form granules.

In the present invention, the pore of the hollow fiber membrane included in the separation membrane module is controlled to have a diameter of 50 to 150 탆, so that the granule can not pass through the separation membrane module, while the activated sludge AOA, AOB and NOB Of the bacteria can again pass through the membrane module.

In the present invention, the purified effluent and the bacteria such as AOA, AOB and NOB contained therein may be separately recovered and re-supplied to the first settling tank 10 through the treated water supply pipe 64.

5 schematically illustrates the structure of a sewage treatment system according to an embodiment of the present invention. Specifically, the SBR reaction tank 60 of the present invention comprises a treatment tank 61; A process water reservoir 63 and a separation membrane bioreactor 62.

4, the separation membrane bioreactor 62 is not contained in the treatment tank 61 of the SBR reaction tank 60 and the separation membrane bioreactor 62 is disposed in the treatment water reservoir 63 connected to the treatment tank 61 . Therefore, in the treatment tank 61 of the SBR reaction tank 60, the anaerobic digestion reaction is carried out by the anaerobic ammonium-oxidizing bacteria in the desolvation solution, and the purified desalted solution subjected to the anaerobic digestion reaction is transferred to the treatment water reservoir 63, The membrane bioreactor 62 can be used to separate granules produced by anaerobic ammonium-oxidizing bacteria and bacteria such as AOA, AOB and NOB. That is, the granules can not pass through the membrane module of the membrane bioreactor 62, while bacteria such as AOA, AOB, and NOB are again passed through the membrane module, and the purified desolvation solution containing the passed bacteria And the granules are transferred to the treatment tank 61 of the SBR reaction tank 60 through the granule transfer pipe 65. The granules are supplied to the first settling tank 10 through the supply pipe 64,

Hereinafter, the separation membrane bioreactor (24, 62) of the present invention will be described in more detail.

6, the separation membrane bioreactor 24 and 62 of the present invention basically comprises a treatment tank 300, a membrane supporting frame 600, a separation membrane module 700, a reciprocating means 200, a sludge lifting unit 400, A slide means 500, and a filtered water discharge portion.

Further, according to a further embodiment, it is possible to further include a configuration such as a length adjusting unit 740, a gap measuring unit 810, a gap adjusting unit 860, and a controller 1000.

The treatment tank 300 may be provided in the form of a tank and may include an inlet 310 through which wastewater (or sewage) flows and an outlet 320 through which treated wastewater (or sewage) is discharged.

At this time, it is preferable that the inflow port 310 is formed so that inflow water can flow to the upper side of the treatment tank 300, so that a flow that flows upward from the inlet of the treatment tank 300 is generated, It is possible to prevent stagnation at the lower side of the treatment tank 300 and more effective filtration can be performed. The inlet 310 may be formed on the upper surface of the processing tank 300 or may be formed as a pipe bent from the lower side to the upper side when the lower side is easier to design.

The membrane support frame 600 is disposed inside the treatment tank 300 and is a portion where a membrane type membrane module 700 is mounted. As described later, the membrane supporting frame 600 is connected to the reciprocating means 200, and the membrane supporting frame 600 reciprocates integrally with the separating membrane module 700 by the reciprocating means 200 .

The reciprocating means 200 may be connected to the membrane support frame 600 and may be provided to reciprocate the membrane support frame 600. The reciprocating unit 200 may include a reciprocating frame 250 and a driving unit 205.

The reciprocating frame 250 may be connected to the membrane supporting frame 600 and may support the membrane supporting frame 600. The driving unit 205 may be disposed in the treatment tank 300 and may be connected to one side of the reciprocating frame 250 to move the reciprocating frame 250. The driving unit 205 may include a motor 210, a first pulley 211, a second pulley 213, a rotor 230, and a link rod 220.

7, the separation membrane module 700 includes an upper frame 710 and a lower frame 720, and the upper frame 710 and the lower frame 720 are connected to each other. A plurality of hollow fiber membranes 730 may be bundled and fixed.

At this time, the upper frame 710 and the lower frame 720 are symmetrically formed in the same shape, and may be formed in various shapes. In the present embodiment, the upper frame 710 and the lower frame 720 have a long rectangular shape.

The hollow fiber membrane 730 is fixed at both ends to the upper frame 710 and the lower frame 720. The hollow fiber membrane 730 has a collecting part 711 formed inside the upper frame 710 and a hollow fiber membrane 730 The hollow fiber membrane 730 may be inserted into the hollow fiber membrane 730 to communicate with the hollow fiber membrane 730. Accordingly, the filtered water that is sucked from the outside to the inside of the hollow fiber membrane and collected may be collected in the collecting part 711. In this regard, the following section will be discussed in detail.

In the above description, both ends of the hollow fiber membrane are fixed to the upper frame and the lower frame, but according to another embodiment, the hollow fiber membrane is fixed between the upper frame and the lower frame, and both ends of the hollow fiber membrane are fixed And may be wound in a U-shape through a fixing bar provided in the lower frame. For example, the fixing bar may be a rod having a space through which the hollow fiber membrane can pass.

At this time, the hollow fiber membrane 730 is formed like a curtain along the longitudinal direction of the frame, and the hollow fiber membrane 730 is formed as a bundle for each predetermined length, and the hollow fiber membrane 730 may be spaced apart by a certain distance for each bundle. This is because if the membrane is formed too tightly along the longitudinal direction, the water will stagnate and the fouling may become worse, so that the water can flow well by giving a little of the separation distance.

As described below, a plurality of the separation membrane modules 700 may be disposed inside the membrane support frame 600. In this case, since the air purification process is not used, The water between the modules may become stagnant and the fouling may become worse. Therefore, the density of the membrane module 700 should be lowered so that the water can flow well between the modules.

At this time, it is preferable that the interval between the modules is 2 cm or more in order to allow the water to flow without stagnation between the membrane modules 700. However, if the interval is too wide, the installation space of the membrane module becomes large, Is preferably 4 cm or less.

An inertial force acting on the separator module 700 is generated due to the reciprocating motion of the separator module 700 by the reciprocating means 200. This causes the attachment of contaminants to the surface of the separator membrane 700 Or remove contaminants from the surface of the separator.

At this time, in order to maximize the effect of preventing or removing the foreign matter by inertial force, the looseness of the separation membrane should be maintained at an appropriate level.

This is because if the separation membrane module 700 does not sag, the separation membrane module 700 is reciprocated integrally due to the reciprocating motion of the membrane support frame 600, but inertia is hardly imparted and the separation membrane module 700 is broken or damaged This is because it is difficult to impart inertia even when the distance is too much, and the reciprocating distance of the membrane module 700 is increased, which results in a large installation space.

Accordingly, the length of the hollow fiber membrane 730 is formed by adding the length of from 0% over 10% or less of the distance (L _o) to the distance (L _o) between the upper frame 710 and lower frame 720 . That is to say, the length of the hollow fiber membrane 730 connected to the upper frame 710 and the lower frame 720 is not more than 10% of the maximum length (hereinafter referred to as the 'minimum separation membrane length) But it is particularly desirable to provide an allowance of 5% to 10%.

8, the length L _f of the maximum separation membrane that can generate inertia in the separation membrane due to the reciprocating motion is determined by the length of the minimum separation membrane, that is, the distance between the upper frame 710 and the lower frame 720 (L _o ) of the minimum separation membrane and the reciprocating distance a of the separation membrane module, and the degree of slackness of the separation membrane module 700 can be calculated by dividing the length L _f of the maximum separation membrane by the length L _o ). That is, the looseness of the separation membrane module 700 should be more than 1 and less than 1.1, and more preferably 1.05 or more and 1.1 or less.

For example, the length L _o of the minimum separation membrane, that is, the vertical distance between the upper frame 710 and the lower frame 720 is 500 mm, based on the reciprocation distance a of the separation membrane module 700 being 100 mm, 8, the length L _f of the maximum separation membrane can be calculated as 538.5 mm according to the nature of the triangle, and 1.08 (exactly 1.077) is obtained when the looseness is calculated . However, at this time, if the reciprocating distance is 150 mm, the length L _f of the maximum separator becomes 583.1 mm, which indicates that the degree of sagging is about 1.17 (exactly 1.166) . In this case, the reciprocating motion distance can be reduced or the minimum separation membrane length can be increased.

When the distance L _o of the separation membrane module 700 is 100 mm and the length L _o of the minimum separation membrane is 750 mm, the maximum separation membrane length L _f is calculated to be 776.2 mm and the degree of sagging is 1.03, If the length (Lo) of the minimum separation membrane is 1000 mm, the length (L _f ) of the maximum separation membrane is calculated as 1019.8 mm, and the degree of sagging is approximately 1.02.

However, when the reciprocating distance of the separator module 700 is 100 mm, when the length L _o of the minimum separator is 1500 mm, the length L _f of the maximum separator is calculated as 1513.3 mm, It is difficult to impart inertia to the separation membrane. In this case, the reciprocation distance of the separation membrane module 700 must be further increased or the length L _o of the minimum separation membrane must be reduced.

Hereinafter, the present invention will be described more specifically by way of specific examples. The following examples are provided to aid understanding of the present invention, and the scope of the present invention is not limited thereto.

Claims (20)

A mixing cell for mixing an inlet for supplying sewage and sewage and mixing the activated sludge with the activated sludge, an aerobic reactor connected continuously to the mixed cell, the activated sludge absorbing organic matter, and an organic material adsorbed on the activated sludge in the aerobic reactor An aerobic tank including an outlet for discharging sewage;
A separation membrane bioreactor (MBR) for separating sludge that has adsorbed organic matter from sewage discharged through the discharge port of the oxic tank; And
And an anaerobic tank for carrying out the denitrification process using the anaerobic ammonium-oxidizing bacteria (Anammox) in the treated water that has passed through the MBR,
Wherein the separation membrane bioreactor is capable of removing foreign matter adhered to the separation membrane by reciprocating the separation membrane. The method according to claim 1,
The membrane bioreactor (MBR) comprises a membrane support frame;
A membrane module mounted on the membrane support frame;
A reciprocating means connected to the membrane supporting frame and reciprocating the membrane supporting frame; And
And a sludge lifting unit disposed at a lower end of the membrane support frame for lifting sludge accumulated in the treatment tank. 3. The method of claim 2,
Wherein the separation membrane module comprises a plurality of hollow fiber membranes. The method of claim 3,
Wherein the hollow fiber membrane comprises pores having a diameter of 50 to 150 占 퐉. 3. The method of claim 2,
Wherein the separation membrane bioreactor further comprises a sludge supply pipe for transferring the separated sludge to the aerobic tank. The method according to claim 1,
Wherein the activated sludge comprises at least one selected from the group consisting of Ammonia Oxidizing Archaea (AOA), Ammonia Oxidizing Bateria (AOB) and Nitrite Oxidizing Bacteria (NOB). The method according to claim 1,
Wherein the exhalation reaction tank further comprises an air injection device for injecting air. A primary settling tank for settling the sewage containing the sludge into raw sludge and sewage;
The bioreactor according to claim 1, wherein the organic material in the sewage separated from the primary settling tank and the activated sludge are adsorbed and separated, and the denitrification process is performed.
A second settling tank for settling the excess sludge in the sewage having adsorbed the organic material in the aeration tank;
A dehydrating tank for dehydrating the raw sludge recovered by being settled in the primary settling tank and the excess sludge recovered by precipitation in the secondary settling tank;
A digester capable of anaerobically digesting raw sludge and excess sludge dehydrated in a dehydration tank to produce biogas; And
And an SBR reaction tank for removing nitrogen by reacting the ammonium-containing desalination solution generated in the digester with an anaerobic ammonium-oxidizing bacteria (Anammox). 9. The method of claim 8,
Wherein the bioreactor includes a separation membrane bioreactor (MBR) for separating sludge adsorbing an organic substance. 10. The method of claim 9,
The membrane bioreactor (MBR) comprises a membrane support frame;
A membrane module mounted on the membrane support frame;
A reciprocating means connected to the membrane supporting frame and reciprocating the membrane supporting frame; And
And a sludge floatation unit disposed at a lower end of the membrane support frame for flooding the sludge accumulated in the treatment tank. 11. The method of claim 10,
Wherein the separation membrane module comprises a plurality of hollow fiber membranes. 12. The method of claim 11,
Wherein the hollow fiber membrane comprises pores having a diameter of 50 to 150 占 퐉. 10. The method of claim 9,
Wherein the separation membrane bioreactor further comprises a sludge supply unit for transferring the separated sludge to the oxic tank. 9. The method of claim 8,
Wherein the activated sludge comprises at least one selected from the group consisting of Ammonia Oxidizing Archaea (AOA), Ammonia Oxidizing Bateria (AOB) and Nitrite Oxidizing Bacteria (NOB). 9. The method of claim 8,
Wherein the bioreactor further comprises an air injection device capable of injecting air for adsorption of an organic material in the sewage and an activated sludge. 9. The method of claim 8,
Wherein the anaerobic ammonium-oxidizing bacteria (Anammox) is Planctomycetes. 9. The method of claim 8,
Wherein the anaerobic ammonium-oxidizing bacteria (Anammox) is a planktonicide granule. 9. The method of claim 8,
Wherein the SBR reactor comprises a membrane bioreactor (MBR) for selectively separating activated sludge. 9. The method of claim 8,
The SBR reaction tank is connected to the treated water storage tank,
Wherein the treated water reservoir comprises a membrane bioreactor for selectively separating activated sludge. 9. The method of claim 8,
And a biogas collector for collecting the biogas generated in the digester.

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