KR20160084360A - Air diffuser and membrane bio-reactor - Google Patents

Abstract

The present invention relates to a diffuser device, and a membrane bioreactor comprising the diffuser device. The diffuser device has a diffusing pipe comprising: a pore group containing at least two pores; and a side pore positioned to be separated from the pore group. The diffuser device reduces the amount of used air, and the amount of consumed electric power, and enhances an operating efficiency of the membrane bioreactor.

Description

TECHNICAL FIELD [0001] The present invention relates to an air diffuser and a membrane bioreactor,

The present invention relates to an anaerobic apparatus and a separation membrane bioreactor, and more particularly, to an apparatus and a method for separating and purifying biomass which are capable of effectively discharging and dispersing air or bubbles even with a small amount of air, Which is capable of reducing the amount of air and power consumed by the separation membrane bioreactor and increasing the operation efficiency of the separation membrane bioreactor, and a separator bioreactor including the above-described anaerobic reactor.

Membrane bioreactor (MBR) process is called activated sludge membrane separation process or membrane bound activated sludge process and is a method of sewage or wastewater treatment including high concentration organic or inorganic matter.

Such a membrane bioreactor can be used to culture a mixed liquor suspended solid (MLSS) by replacing solid-liquid separation by sedimentation, which is used in a previously known standard activated sludge process or standard activated sludge process, Accordingly, it is possible to greatly reduce the site area required for installation of the apparatus or the whole system, and it is possible to secure stable water quality while improving the treatment efficiency.

However, since the separation membrane bioreactor utilizes the inhalation action to conduct the solid-liquid separation in the separation membrane, in order to mitigate the contamination of the separation membrane or to remove contaminants from the separation membrane, an air diffuser for air injection is installed under the reaction vessel, .

Previously, there have been known methods for solving the problem of pressure distribution occurring in the operation of the air diffusers or methods for generating air bubbles more evenly in the air diffuser, but the use of a smaller amount of air, Or a method for removing contaminants has not been commercialized.

The present invention can effectively release air or bubbles even with a small air volume and can disperse the air or bubbles effectively, thereby achieving an excellent cleaning effect in applications such as separation membrane bioreactors, reducing the amount of air to be used and power consumption, The present invention is intended to provide an anaerobic device capable of improving the efficiency and cleaning the acid organs and controlling contamination of the separation membrane bioreactor.

Further, the present invention is to provide a separation membrane bioreactor including the above-described acidifier.

In this specification, a pore group containing two or more pores; And a side pore spaced from the pore group, wherein the pore groups are arranged in a line in a longitudinal direction of the air diffuser from a surface of the air diffuser, Is formed at a position corresponding to 1/5 to 1/3 of the entire circumference of the cross section perpendicular to the longitudinal direction of the diffuser.

Further, in the present specification, a bioreactor; At least one separation membrane module installed in the bioreactor; And a diffusion device installed at a lower end of the separation membrane module.

Hereinafter, the anaerobic device and the separation membrane bioreactor according to specific embodiments of the present invention will be described in detail.

According to one embodiment of the invention, a pore group comprising two or more pores; And a side pore spaced from the pore group, wherein the pore groups are arranged in a line in a longitudinal direction of the air diffuser from a surface of the air diffuser, Which is formed at a position corresponding to 1/5 to 1/3 of the entire circumference of the cross section perpendicular to the longitudinal direction of the diffuser, may be provided.

Previously known pneumatic devices, air purging pores are distributed at regular intervals or irregularly distributed. However, in such an air diffuser, it is not easy to control the shape and flow of the air discharged from the pores or the air bubbles generated from the air bubbles, and the apparatus applied due to the flow of air bubbles generated from the discharged air It was not easy to distribute the pressure in the separation membrane of the separation membrane bioreactor.

Therefore, the inventors of the present invention have conducted studies on an acidifier, and when a plurality of pore groups composed of two or more pores are formed on a plurality of air diffusers, air or bubbles can be effectively released and dispersed even with a small amount of air, Etc., it is possible to reduce the amount of air to be used and power consumption, and to increase the operation efficiency of the membrane bioreactor.

When the side pores spaced apart from the pore group are formed at positions corresponding to 1/5 to 1/3 of the entire circumference of the cross section perpendicular to the length direction of the air diffusing pipe from the pore group, The air bubbles formed through the pore groups are bundled with the air bubbles discharged through the pore groups to form giant bubbles, and suspended matters remaining in the inside of the air diffuser are discharged through the side pores, And the contamination control of the separation membrane bioreactor becomes possible.

As described above, the side surface pores are formed so as to have a ratio of 1/5 to 1/3 of the entire circumference of the cross section perpendicular to the longitudinal direction of the air diffusions from the pore group, As shown in FIG. As shown in the drawing, the side pores are present at the outermost side of the upper engine plane on the plan view of the pore groups.

The side pores may be formed on the surface of the air diffusing tube, and two or more pairs of side pores may be formed on the surface of the air diffusing tube.

Although the number of the side pores is not limited to a large number, the side pores may be formed at two to ten equal parts in the longitudinal direction of the air diffusing pipe.

The maximum diameter of the side pores is not limited, but the maximum diameter of the side pores is preferably 5 mm to 20 mm, more preferably 5 mm to 20 mm, in order to more easily form large bubbles and to improve the cleaning performance and the contamination control performance of the separation membrane bioreactor. Lt; / RTI >

The maximum diameter of the side pores may be 1.5 to 3 times the maximum diameter of the pores included in each of the pore groups. Since the side pores have a larger diameter than the pores included in each of the pore groups, a flow occurs in the inside of the pore, thereby facilitating the inflow and outflow of the sludge and other debris into and from the large pores. The sludge adhered to each of the pores through a pressure increase or the like can be discharged in a larger amount into the side pores of the diffuser.

The 'pore group' means a group consisting of two or more pores formed on the acidifier, and the distance between the pores included in one pore group is smaller than the distance to the pores included in the other pore group Therefore, they can be divided into one group on the above-described diffuser.

In addition, as more than two pores are gathered to form one pore group, and as more than two of these pore groups are present in the above-mentioned air diffuser, the air bubbles released through the pores in the diffuser of the embodiment coalesce And such coalesced air bubbles form giant air bubbles and these giant air bubbles rise or flow in the apparatus (eg, membrane bioreactor) where the air diffuser is installed (slug flow). The air diffuser allows the giant foam to be uniformly formed in a uniform size.

The pore group may include two or more pores, specifically, two to six pores, or three to five pores.

The distance between adjacent pore groups formed in the air diffusing pipe may be 25 mm to 150 mm, or 30 mm to 120 mm, or 40 mm to 100 mm. If the distance between the neighboring pore groups is too small, the pores do not substantially form a group, and it is difficult to realize the above-described bubble coalescence or slug flow of macro air bubbles, It is not easy to do. In addition, if the distance between adjacent pore groups is too large, a slug flow can not be uniformly formed on the entire membrane, and the cross flow in a direction perpendicular to the permeated water on the membrane surface cross flow) or an upflow velocity formed upwardly from below may not be smoothly performed, thereby leading to localized separation membrane contamination and the efficiency of the acid catalyst may be reduced.

The pore groups may be arranged in a line in the longitudinal direction of the diffuser at the surface of the diffuser. The anaerobic device including the aeration orifice may be installed in the separation membrane bioreactor, and the pore groups formed in the aeration orifice may be formed to face the separation membrane module included in the separation membrane bioreactor.

Specifically, the pore groups formed on the surface of the diffuser can be arranged on a virtual straight line passing through them. Alternatively, all of the pore groups may exist in two hypothetical lines in which the width of the pore group including the two pores most widely distributed in the width direction of the diffuser is increased in the longitudinal direction of the diffuser.

The pore groups may be arranged in a line in the longitudinal direction of the air diffusing pipe from the surface of the air diffusing pipe, but not necessarily all have the same distribution pattern, and the arrangement of the above- For example, the positional error of the center of the pore group is less than 7%, which is seen as a substantial array of lines.

A schematic view of the diffuser included in the diffuser of an embodiment of the present invention is shown in Fig. However, FIG. 6 is merely an example of the air diffuser of the embodiment, and the details of the diffuser of an embodiment of the present invention are not limited thereto.

FIG. 7 schematically shows a plan view of an air diffuser included in the diffuser of an embodiment of the present invention. 7 is a plan view of the air diffuser included in the diffuser of the embodiment and an example of the content of the air diffuser included in the diffuser, and the specific details of the diffuser of the embodiment of the present invention are limited thereto It is not.

As shown in Fig. 8, in the case where previously known acid organs, for example, simply, one pore on the acid orifice are formed in one column or two columns at regular intervals, the above-described bubble coalescence or giant It is difficult to realize a slug flow of the air bubbles, so that it is not easy to achieve the above-mentioned effect.

As the pore groups include two to six or three to five pores, the air bubbles emitted through the pores can easily be combined into one, and the flow of large air bubbles (slug flow, slug flow) can be stably and balancedly formed.

9 schematically shows the formation of the flow of the macro air bubbles, and a schematic diagram of a phenomenon in which the flow of the macro air bubbles ascends or flows in the membrane bioreactor is shown in As shown in Fig.

The distance between the pores included in the one pore group may be 1 mm to 20 mm, or 4 mm to 12 mm, or 5 mm to 10 mm. The distance between pores included in the one pore group may be defined as a distance between a center point of each pore and a center point of the adjacent pore. The center point of the pores may be a center point of the circle including the entire surface of the pores.

As the distance between the pores included in the one pore group is specified in the above range, the air bubbles emitted through the pores can be easily combined into one, and the large air bubbles can be stably and balanced .

The maximum diameter of the pores may be 0.5 mm to 10 mm, or 1 mm to 5 mm. If the size of the pores is too small, the pressure applied to the air generated through the pores is increased to increase the energy loss, and the size of the air bubbles released from the pores becomes too small to form large air bubbles, The bubbles may not be able to make the above-mentioned slug flow. In addition, if the pore size is too large, the air at the air diffuses suddenly from the pores close to the injection port, thereby causing a problem in the pressure distribution of the air diffuser as a whole, and is likely to become unevenly distributed. In addition, if the pore size is too large, the action and effect of forming the pore group can be reduced, and it is difficult to realize the bubble coalescence or the slug flow of the large air bubble. It is not easy to achieve.

The cross-section of the pores on the surface of the diffuser may be a circle, an ellipse, or a polygon having 3 to 30 internal angles.

Meanwhile, the specific shape and size of the air diffusing pipe may vary depending on the apparatus to be actually used, but the diffusing pipe may be in the form of a pipe having an outer diameter of 10 mm to 100 mm or an inner diameter of 1 mm to 90 mm.

The shape of the cross section perpendicular to the longitudinal direction of the air diffusing pipe is not particularly limited, but may be, for example, a circle, an ellipse or a polygon having 3 to 30 internal angles.

The material of the air diffuser is not limited to a specific material. For example, thermoplastic plastic or metal such as PVC can be used for the production of the air diffuser.

As described above, the aeration apparatus of one embodiment can be used in a membrane bioreactor (MBR).

In addition, the anatalizing device of one embodiment may further include other components commonly known to be other than the aerosol for use in a membrane bioreactor.

For example, the diffuser of the embodiment may further include a gas injection unit connected to the diffuser and injecting gas into the upper organ. The gas injection unit may include a motorized valve for ensuring the safety of air injection and a change in the operation method, a solenoid valve for intermittent injection or pulp injection, and the like. The gas injection unit may be provided outside the separation membrane bioreactor, .

In addition, the diffuser of the embodiment may further include a gas distributor for distributing the gas injected from the gas injector to the air diffuser.

According to another embodiment of the present invention, there is provided a bioreactor; At least one separation membrane module installed in the bioreactor; And a diffusion device installed at a lower end of the separation membrane module.

As described above, by using the air diffuser of the embodiment, it is possible to effectively discharge and disperse air or bubbles even with a small amount of air, and it is possible to realize an excellent cleaning effect in application fields such as a membrane bioreactor, It is possible to reduce the amount of air and power consumption, and to increase the operation efficiency of the membrane bioreactor.

Particularly, by using the air diffuser of the embodiment, the air bubbles emitted through the pores of the diffuser can coalesce, and the air bubbles thus formed form a large air bubble, Such large air bubbles rise or flow in the membrane bioreactor of this embodiment (slug flow). The air diffuser allows the giant foam to be uniformly formed in a uniform size.

According to the cyclic flow of the macro air bubbles, contaminants that can be generated in the separation membrane of the separation membrane bioreactor can be easily removed even with a smaller amount of air, and the accumulation of contaminants in the separation membrane can be minimized .

The detailed description related to the air diffusing apparatus includes all of the above-mentioned contents in the above embodiment.

The bioreactor is a part that performs biological purification using microorganisms in the treatment of sewage or wastewater. The part where the separation membrane is immersed is called an aeration tank, aeration tank or aerobic tank, and serves as a decomposition part of organic matter. Or circular shape. The size of such a bioreactor is not limited, but may be on the order of 100 m 3 to 20,000 m 3 per unit of an aeration tank, for example.

The one or more separation membrane modules installed in the biological reaction tank are installed in an aeration tank or in the form of an air lift in a separating membrane tank or outside the tank in a bioreactor represented by a standard activated sludge method or a standard activated sludge process modification method, Called liquid-solid separation in which purified water is separated. Depending on the installation position of the separation membrane, the operation method, etc., it may be in the form of an immersion type or a pressure type. In addition, such a membrane module consists of a constituent part of a unit comprising a membrane, an element (including a panel or a spacer), a module and a module in the form of a flat membrane.

The separator module may include a hollow fiber membrane, and the material of the membrane and the hollow fiber membrane is not particularly limited. Typically, polyvinylidene fluoride (PVDF), which is a hydrophobic material, is subjected to surface treatment, hydrophilization, And a hydrophilic modification may be used. In addition to PVDF, it is also possible to use aromatic polymer materials such as polysulfone (PSf) or polyethersulfone (PES), polyacrylonitrile (PAN), cellulose acetate (CA) or cellulose triacetate , CTA) can be used. The flat membrane and the hollow fiber membrane may have a plurality of pores having a size of 5 mu m to 0.0005 mu m.

The separator module may be installed in an upper space between the pore groups included in the diffuser. Specifically, the separation membrane module may be formed variously according to the designing method of the manifold and the air injection direction perpendicularly or horizontally to the direction of the diffuser of the diffuser.

Meanwhile, a distance between the separation membrane module and the diffusion device may be 5 mm to 400 mm. If the distance between the separator module and the acid generator is too small, the air bubbles released through the pores of the air diffuser may be difficult to accumulate, or the bubble growth due to the foam coalescence may provide a space over the entire separator It is possible to increase the number of installation places of the device for dissipating heat and to lower the energy consumption efficiency. If the distance between the separation membrane module and the acid generator is too large, the stability of the large air bubbles formed by the aggregation of the air bubbles discharged through the pores of the air diffuser may be reduced, or the large air bubbles may flow into the separator module It may not be easy to penetrate. As a result, the effect of large and strong bubble aggregates formed by controlling the ratio of air / water is halved, which hinders the formation of smooth slug flow.

Meanwhile, the separation membrane bioreactor of the embodiment includes an injection unit for injecting wastewater into the bioreactor; An air injection unit for injecting outside air into the bioreactor; An injecting portion of washing air or washing liquid to be introduced for washing the air diffuser; A discharge unit for discharging treated water treated in the bioreactor; A conveying unit for conveying in the bioreactor; As shown in FIG.

According to the present invention, it is possible to effectively discharge and disperse air or bubbles even with a small amount of air, thereby realizing an excellent cleaning effect in applications such as separation membrane bioreactors, etc., A separator bioreactor including the anaerobic device and the anaerobic device capable of cleaning the acid ore and controlling contamination of the separation membrane bioreactor can be provided.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a photograph showing the operation of a separation membrane bioreactor according to Example 1. FIG.
FIG. 2 is a photograph showing the operation of the separation membrane bioreactor of Example 2. FIG.
FIG. 3 is a photograph of the operation of the separation membrane bioreactor of Examples 3 to 6. FIG.
FIG. 4 is a photograph of the operation of the separation membrane bioreactor of Examples 7 to 10 observed. FIG.
FIG. 5 is a photograph showing the operation of the separation membrane bioreactor of Comparative Example 1 observed. FIG.
6 schematically shows an air diffuser included in the diffuser of an embodiment of the invention.
Fig. 7 schematically shows a plan view of an aerodrome included in the anomaly device of an embodiment of the invention. Fig.
Fig. 8 schematically shows a plan view of a conventional diffuser.
FIG. 9 is a schematic view briefly showing the flow of air bubbles generated in the diffuser and the conventional diffuser included in the diffuser of the embodiment of the invention. FIG.
FIG. 10 is a schematic view showing a flow pattern of air bubbles in a separator bioreactor using an acid diffuser and a conventional diffuser, which are included in the diffuser of an embodiment of the present invention.
FIG. 11 is a graph showing changes in pressure applied to the vacuum pump according to time when a flow rate of 20 L / min is injected into the separation membrane bioreactor of Example 11 and Comparative Example 2, respectively, in Experimental Example 2. FIG.
12 is a graph showing changes in pressure applied to the vacuum pump according to time when a flow rate of 30 L / min is injected into the separation membrane bioreactor of Example 11 and Comparative Example 2 in Experimental Example 2, respectively.
13 is a graph showing the measurement results of the cross-flow velocity measured in Experimental Example 3. FIG.
14 schematically shows a plan view of an aerodynamic tube included in a diffuser of Example 12. Fig.
FIG. 15 is a photograph of the operation of the air diffuser of the twelfth embodiment in different amounts of air to be injected.
16 is a photograph of the sludge discharged from the aeration engine of the twelfth embodiment.

The invention will be described in more detail in the following examples. However, the following examples are illustrative of the present invention, and the present invention is not limited by the following examples.

< Example 1 to  10 and Comparative Example 1 : Air diffuser and separator Bioreactor  Driving>

In a bioreactor having a volume of 200 liters, four separation membranes each having a size of 150 mm x 300 mm (width x length) were arranged at intervals of 8 mm on both sides, and a total of 8 surfaces were provided, and a diffuser was installed at a predetermined distance from the separation membrane.

As the separator, a polyacrylonitrile (PAN) ultrafiltration membrane (pore size of about 0.07 μm) was used. The longest diameter of each pore formed on the surface of the diffuser included in the diffuser was changed to a pore group The number of pores included, the distance between the pores in the pore group, the distance between the pore groups, and the distance between the membrane module and the diffusion device are as shown in Table 1 below.

The operation was carried out by filling the tap water with 10 L / min (10 L / min) and 10 L / min (unit), and the formation of slug flow and the behavior of bubbles dispersed throughout the membrane And observed with a high-speed camera.

Formation of pores on the air diffuser of Examples and Comparative Examples Pore
Longest diameter Number of pores contained in the pore group Spacing between pores within the pore group Distance between groups Distance between membrane module and diffuser Example 1 About 2 mm 3 7 mm 37.5 mm 40 mm Example 2 About 2 mm 4 7 mm 37.5 mm 40 mm Example 3 About 2 mm 3 8 mm 37.5 mm 40mm Example 4 About 2 mm 3 7 mm 37.5 mm Example 5 About 2 mm 4 8 mm 37.5 mm Example 6 About 2 mm 4 7 mm 37.5 mm Example 7 About 4 mm 3 10 mm 83.3 mm 160 mm Example 8 About 4 mm 3 9 mm 83.3 mm Example 9 About 4 mm 4 10 mm 83.3 mm Example 10 About 4 mm 4 9 mm 83.3 mm Comparative Example 1 About 2 mm 4 No group spacing [pores arranged in series at intervals of 7 mm] No group spacing 120mm

< Experimental Example 1 : Example 1 to  10 and Comparative Example 1  Membrane Bioreactor  Driving observation>

(1) As shown in FIG. 1 and FIG. 2, as the separation membrane bioreactor of Example 1 and Example 2 is operated, the phenomenon of coalescence of air bubbles generated in the air diffuser can be observed (Coalescence) of the air bubbles, and thus, a slug flow occurs in which the large air bubbles formed by the air bubbles are transferred to the membrane module.

As shown in FIGS. 3 and 4, the above phenomenon was also confirmed in the operation of the separation membrane bioreactors of Examples 3 to 10.

(2) On the other hand, when the separation membrane bioreactor of Comparative Example 1 (FIG. 5) was operated, it was hard to observe the accumulation of air bubbles generated in the air diffuser, And it was possible to observe the passage between the membrane modules.

< Example 11  And Comparative Example 2 >

In a bioreactor having a volume of 200 liters, four separation membranes each having a size of 150 mm x 300 mm (width x length) were arranged at intervals of 8 mm on both sides, and a total of 8 surfaces were provided, and a diffuser was installed at a predetermined distance from the separation membrane.

As the separation membrane, a polyacrylonitrile (PAN) ultrafiltration membrane (pore size of about 0.07 m) was used, and the maximum diameter of each pore formed in the acidifier, the number of pores contained in the pore group, The distance between the pore groups, and the distance between the membrane module and the diffusion device are as shown in Table 2 below.

Artificial wastewater containing artificial organic contaminants such as insoluble organic matter, sugar, and lipids was filled in the separation membrane bioreactor and air was injected at a rate of 30 L / min. The pressure applied to the vacuum pump used in the separation membrane , And trans membrane pressure (TMP).

[Operation condition]

(1) Flux: 15.4 LMH (L / m ² / h)

(2) Operation mode: 9 min.

(3) Organic matter concentration (wt%): 0.035

Formation of pores on the acidifier of Example 11 and Comparative Example 2 [Length of the acidifier: 150 mm] Pore
Longest diameter Number of pores contained in the pore group Spacing between pores within the pore group Distance between groups Distance between membrane module and diffuser Example 11 About 2 mm 3
[Total 4 groups] 7 mm 37.5 mm 40 mm Comparative Example 2 About 2 mm - No group spacing [23 pores arranged in series] - 120 mm

< Experimental Example 2 : Example  11 and Comparative Example 2  Membrane Bioreactor  Driving observation>

Experiments were conducted by flowing a flow rate of 20 L / min and 30 L / min into the separation membrane bioreactor of Example 11 and Comparative Example 2, respectively.

1. At a flow rate of 20 L / min

As shown in FIG. 11, when the flow rate of 20 L / min was introduced into the separation membrane bioreactor of Comparative Example 2, the rate of increase of the differential pressure was relatively high, and it was confirmed that the borrowing continuously increased for a relatively long time.

On the other hand, the separation membrane bioreactor of Example 11 showed that the differential pressure was relatively slow and the differential pressure was maintained at 0.4 Kg / cm 2 or less even after prolonged use of more than 1000 minutes.

2. At the flow rate of 20 L / min

As shown in FIG. 12, the separation membrane bioreactor of Comparative Example 2 was an experiment conducted for 100,000 seconds

The trans membrane pressure (TMP) is continuously increased to 0.2 Kg / ㎠ or more.

On the contrary, in the membrane bioreactor of Example 11, even when the same flow rate of 30 L / min was introduced and the experiment was carried out at the same time, the differential pressure increase rate was gentle and the differential pressure was maintained within about 0.2 Kg / And the time to reach the limit differential pressure (when the average is about 0.5 or more) is relatively long. Thus, it was confirmed that the cycle of washing the separation membrane of Example 11 can be greatly improved, and an economical operating condition of the separation membrane bioreactor can be formed.

< Experimental Example 3 : Measurement of cross-flow velocity by an aeration device>

When a water tank of 400 mm × 500 mm × 700 mm (WXLXH) was filled with clean water and air of 15 to 30 L / min was fed into the air diffuser, the air diffuser was introduced into the air diffuser of Example 11 and Comparative Example 2, The cross-flow velocity was measured by comparing the formed water / air flow rate.

Specifically, the measurement of the flow velocity was carried out by providing four sheets of separators each having a size of 150 mm × 300 mm (width X length) at 8 mm intervals on both sides, a total of 8 surfaces were provided, and a diffuser was installed at a predetermined distance from the separator, The flow velocity was measured indirectly by analyzing the moving distance of the bead per frame with the ultra-high speed camera floating the upward flow rate generated by sodium alginate bead.

As shown in FIG. 13, when the same amount of air of 15 to 30 L / min was injected, when the air diffuser of Example 11 was used, the cross-flow velocity ) By about 10% to 20%.

Accordingly, when the acidifier of Example 11 is used, it can be higher than the cross-flow velocity even when the same energy is used as compared with the case of using the acidifier of Comparative Example 2, It is expected that it will save the energy required and extend the cleaning cycle of the membrane.

< Example 12 >

In a bioreactor having a volume of 200 liters, four separation membranes each having a size of 150 mm x 300 mm (width x length) were arranged at intervals of 8 mm on both sides, and a total of 8 surfaces were provided, and a diffuser was installed at a predetermined distance from the separation membrane.

As the separation membrane, a polyacrylonitrile (PAN) ultrafiltration membrane (pore size of about 0.07 m) was used, and the maximum diameter of each pore formed in the acidifier, the number of pores contained in the pore group, The distance between the pore groups, the distance between the membrane module and the diffusion device, the maximum diameter of the side pores, and the number and spacing of the side pores are as shown in Table 3 below.

Artificial wastewater containing artificial organic contaminants such as insoluble organic matter, sugar, and lipids was filled in the separation membrane bioreactor and air was injected at a rate of 30 L / min. The pressure applied to the vacuum pump used in the separation membrane , And trans membrane pressure (TMP).

[Operation condition]

(1) Flux: 15.4 LMH (L / m ² / h)

(2) Operation mode: 9 min.

(3) Organic matter concentration (wt%): 0.035

Formation of pores on the acidifier of Example 12 [Length of acidifier: 150 mm] Of the pores contained in the pore group
Longest diameter Number of pores contained in the pore group Spacing between pores within the pore group Distance between groups Distance between membrane module and diffuser Longest diameter of side pore Number and spacing of side pores Example 12 About 3 mm 3
[Total 6 groups] 7 mm 37.5 mm 40 mm About 6 mm 2 pairs
/
75 mm

As shown in Figs. 15 (a) to 15 (d), when the separation membrane bioreactor including the anaerobic apparatus of the twelfth embodiment was operated, it was found that when the operation was performed with the amount of air injected into the anaerobic tank set at 4 to 5 m3 / hr The air bubbles released through the pore group can coalesce, and the air bubbles thus formed can generate larger air bubbles, which can be higher than the cross-flow velocity using the same energy.

In addition, when the amount of air to be injected into the air diffuser is increased to about 10 m 3 / hr, air bubbles are generated from the side air holes formed in the air diffuser, so that generation and action of the air air bubbles can be more smoothly performed. Suspended matter or other debris remaining in the engine was discharged through the side pores.

Specifically, as shown in FIG. 15C, when the amount of air to be injected into the air diffuser is 6 m 3 / hr, the air bubbles generated in the side air bubbles form air bubbles If the amount of air to be injected into the air diffuser is 9 m &lt; 3 &gt; / hr as shown in Fig. 15D, air bubbles generated in the side air holes are combined with air bubbles emitted through the air hole group, It was confirmed that bubbles were formed.

Accordingly, when the amount of air injected into the air diffuser is changed, for example, the amount of air to be injected into the air diffuser is maintained at 4 to 5 m &lt; 3 &gt; / hr, 6 to 10 m3 / hr, flow occurs in the acid furnace, and the sludge adhered to the sludge by the inflow and outflow of the sludge such as sludge into the large pore and the pressure to the small pore, Of the pore size. FIG. 16 shows the discharge of the sludge.

Claims (28)

A pore group containing two or more pores; And
And a side pore spaced apart from the pore group,
Wherein the pore groups are arranged in a line in the longitudinal direction of the diffuser at the surface of the diffuser,
Wherein the side pores are formed at positions corresponding to 1/5 to 1/3 of the entire periphery of the cross section perpendicular to the longitudinal direction of the air diffusing pipe from the pore group.
The method according to claim 1,
Wherein at least one pair of side pores opposite to each other is formed on the surface of the diffuser.
The method according to claim 1,
And the side pores are respectively formed at positions which are divided into 2 to 10 in the longitudinal direction of the air diffuser.
The method according to claim 1,
And the maximum diameter of the side pores is 5 mm to 20 mm.
The method according to claim 1,
Wherein the maximum diameter of the side pores is 1.5 to 3 times the maximum diameter of the pores contained in each of the pore groups.
The method according to claim 1,
Wherein a distance between neighboring pore groups of said pore groups is 25 mm to 150 mm.
The proliferation device according to claim 1, wherein a maximum diameter of the pores contained in each of the pore groups is 0.5 mm to 10 mm.
2. The diffuser as claimed in claim 1, wherein the pore groups are arranged in a line in the longitudinal direction of the diffuser at the surface of the diffuser.
The apparatus of claim 1, wherein the pore group comprises two to six pores.
The proliferation device according to claim 1, wherein a distance between the pores included in the one pore group is 1 mm to 20 mm.
The diffusing device according to claim 1, wherein the cross-section of the pores included in each of the pore groups is a polygon having a circle, an ellipse, or 3 to 30 internal angles.
The method according to claim 1,
Wherein the pore groups are formed at positions which are equally divided into 4 to 25 in the longitudinal direction of the diffuser.
The air diffuser device according to claim 1, wherein said diffuser is in the form of a pipe having an outer diameter of 10 mm to 100 mm.
The diffuser as claimed in claim 1, wherein the diffuser is in the form of a pipe having an inner diameter of 1 mm to 90 mm.
2. The diffuser as claimed in claim 1, wherein the cross-section of the diffuser is a polygon having a circle, an ellipse or an interior angle of 3 to 30 angles.
The apparatus according to claim 1, wherein the material of the diffuser is thermoplastic plastic or metal.
2. The air diffuser according to claim 1, further comprising a gas injection unit connected to the air diffuser and injecting gas into the upper organ.
18. The air diffusing device according to claim 17, further comprising: a gas distribution section for distributing the gas injected from the gas injection section to the air diffuser.
Bioreactor;
At least one separation membrane module installed in the bioreactor; And
The separator bioreactor according to claim 1, wherein the separator module is installed at the lower end of the separator module.
20. The method of claim 19,
Wherein the separation membrane module is installed in an upper space between pore groups included in the anaerobic device.
20. The method of claim 19,
Wherein the separation membrane module comprises a hollow fiber membrane.
20. The method of claim 19,
Wherein a distance between the separation membrane module and the anaerobic device is 5 mm to 400 mm.
20. The method of claim 19,
An injector injecting wastewater into the bioreactor;
An air injection unit for injecting outside air into the bioreactor; or
And a discharge part for discharging the treated water treated in the bioreactor.
Bioreactor;
At least one separation membrane module installed in the bioreactor; And
And a diffusion device installed at a lower end of the separation membrane module,
Wherein the separator module is installed in an upper space between the pore groups included in the diffuser, the distance between the separator module and the diffuser is 5 mm to 400 mm,
Wherein the air diffuser comprises a pore group comprising at least two pores; And a side pore spaced apart from the pore group,
Wherein said air diffusing pipe is in the form of a pipe having an outer diameter of 10 mm to 100 mm and an inner diameter of 1 mm to 90 mm,
Wherein the pore groups are arranged in a line in the longitudinal direction of the diffuser at the surface of the diffuser,
Wherein said pore group comprises two to six pores,
Wherein the side pores are formed at positions corresponding to 1/5 to 1/3 of the entire circumference of the cross section perpendicular to the longitudinal direction of the air diffusing pipe from the pore group,
Membrane bioreactor.
25. The method of claim 24,
Wherein at least one pair of side pores opposite to each other is formed on the surface of the acid diffuser.
The method according to claim 24,
Wherein the side pores are respectively formed at 2 to 10 equal parts in the length direction of the air diffusing pipe.
25. The method of claim 24,
And the maximum diameter of the side pores is 5 mm to 20 mm.
25. The method of claim 24,
Wherein the maximum diameter of the side pores is 1.5 to 3 times the maximum diameter of the pores contained in each of the pore groups.

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