JP2013192974A - Membrane separation facility, and method of operating the membrane separation facility - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a membrane separation facility capable of forming stably and smoothly a circulation flow, and capable of enhancing a cleaning effect for a membrane face.SOLUTION: In this membrane separation facility 1, each of a plurality of membrane units 3a-3d in a treatment vessel 2 includes a plurality of membrane elements 8 arrayed with a space and serving as a flow channel of a circulation flow 4, a downward flow 20 flows in an inter-membrane-element flow channel of the membrane units 3a, 3c in at least one, and an upward flow 21 flows in an inter-membrane-element flow channel of the residual membrane units 3b, 3d, an area ratio D/R of total cross-sectional area D of the downward flow flow channel where the downward flow 20 flows to total cross-sectional area R of the upward flow flow channel where the upward flow 21 flows is within a range of 0.63 or more to 3.33 or less, in a horizontal-directional cross-section of the treatment vessel 2 in a portion arranged with the membrane elements 8, and a flow velocity of the downward flow 20 flowing in the inter-membrane-element flow channel is within a range of 0.15 m/sec or more to 0.25 m/sec or less.

Description

  The present invention relates to a reverse-aeration type membrane separation facility and a method for operating the membrane separation facility, for example, for solid-liquid separation of a liquid to be treated such as sewage wastewater or purified water. Note that the reverse aeration means that air bubbles are raised between the membrane elements by aeration from below the membrane elements in a state where a downward flow is flowing between the membrane elements.

  Conventionally, as this type of membrane separation equipment, for example, as shown in FIG. 26, a plurality of air diffusers 104 that generate an immersion type membrane unit 102 and a circulating flow 103 that circulates in the vertical direction inside a treatment tank 101. 109 are installed. The membrane unit 102 includes a box-shaped casing 105 that is open at the top and bottom, and a plurality of membrane elements 106 that are arranged vertically in the casing 105 and arranged in parallel at a predetermined interval.

The cleaning air diffuser 104 is disposed below the membrane element 106, and the circulating air diffuser 109 is disposed at the bottom of the treatment tank 101 and outside the membrane unit 102.
According to this, when the driving air is diffused from the circulating air diffuser 109 into the activated sludge mixed liquid in the treatment tank 101, an upward flow 107 is generated outside the membrane unit 102, and these upward air flows. The flow 107 is reversed near the liquid surface to become a downward flow 108, and this downward flow 108 flows from the upper part of the membrane unit 102 and flows through the membrane unit 102, and then reverses at the bottom of the processing tank 101. Then, it flows out from the lower part of the membrane unit 102 to the outside. By such an upward flow 107 and a downward flow 108, a circulating flow 103 is generated in the treatment tank 101.

  At this time, when a small amount of cleaning air is diffused from the cleaning air diffuser 104, an upward flow is generated in the membrane unit 102 by the air lift action of the small amount of air. A downward flow 108 is created in the membrane unit 102 because it is inferior to the downward flow 108 by the device 104. This downward flow 108 flows through the intermembrane flow path formed between the membrane elements 106. At this time, a small amount of air bubbles for the cleaning air supplied from the cleaning air diffuser 104 into the downward flow 108 rises in the opposite direction against the downward flow 108, so that the rising speed is reduced. While rising along the membrane surface of the filtration membrane, it drifts not only in the upward direction but also in the diagonal direction and the lateral direction. The presence of such bubbles disturbs the flow of the downward flow 108 and increases the amount of bubbles held in the liquid in the intermembrane flow path. Thereby, the membrane surface of the filtration membrane can be washed well and the total aeration amount can be reduced.

  Note that the reverse aeration type membrane separation equipment as described above is described in, for example, Patent Document 1 below.

JP2008-246357

  In the above conventional format, one immersion type membrane unit 102 is installed in the treatment tank 101 as shown in FIG. 26, but a plurality of membrane units 102 may be installed as shown in FIG. . In this case, depending on conditions such as the installation interval A between the membrane units 102 and the interval B between the membrane unit 102 and the wall surface 101a of the processing tank 101, the circulating flow 103 is not smoothly formed in the processing tank 101, and the membrane element 106 The cleaning effect of the membrane surface of the filter membrane may be reduced.

  In particular, when the processing tank 101 is large and the intervals A and B are large, the above-described reduction in the cleaning effect is remarkable. Conversely, the processing tank 101 is small and the distances A and B are small. Even if the flow rate is narrow, the circulating flow 103 may become unstable and the cleaning effect may be reduced.

  An object of the present invention is to provide a membrane separation facility and a method for operating the membrane separation facility in which a circulating flow is stably and smoothly formed, and a membrane surface cleaning effect is improved.

In order to achieve the above object, the first invention is provided with a plurality of immersion type membrane units and an air diffuser for generating a circulating flow circulating in the vertical direction in the treatment tank,
Each membrane unit has a plurality of membrane elements arranged with a space as a circulation flow path,
By diffusing from the diffuser below the membrane element, a downward flow flows in the flow path between the membrane elements of at least one membrane unit, and an upward flow flows in the flow path between the membrane elements of the remaining membrane units. A membrane separation facility,
The area ratio of the total cross-sectional area D of the downward flow channel and the total cross-sectional area R of the upward flow channel among the flow channels through which the circulating flow flows in the horizontal section of the treatment tank at the portion where the membrane element is disposed D / R is in the range of 0.63 or more and 3.33 or less, and the flow velocity of the downstream flow between the membrane elements is in the range of 0.15 m / second or more and 0.25 m / second or less. It is.

  According to this, a circulation flow is formed in the treatment tank by aeration by the aeration device, a downward flow flows in the flow path between the membrane elements of at least one membrane unit, and the membrane elements of the remaining membrane units An upward flow flows in the intermediate flow path. At this time, the area ratio D / R is in the range of 0.63 or more and 3.33 or less, and the flow velocity of the downward flow through the flow path between the membrane elements is 0.15 m / second or more and 0.25 m / second. By performing aeration so as to be within the following range, the circulating flow flows stably and smoothly, and the amount of bubbles retained in the downward flow increases and the disturbance of bubble movement increases, so The cleaning effect of the film surface is improved.

  The membrane separation facility in the second aspect of the present invention has an area ratio D / R in the range of 0.67 or more and 3.0 or less, and the flow velocity of the downward flow through the flow path between the membrane elements is 0.16 m / second or more. Is within the range of 0.22 m / sec or less.

According to this, the circulating flow flows more stably and smoothly, and the cleaning effect of the membrane surface of the membrane element is further improved.
In the membrane separation facility according to the third aspect of the present invention, the void ratio εd of the channel between the membrane elements in which the downward flow flows is 0.07 or more.

  According to this, the circulating flow flows more stably and smoothly, and the cleaning effect of the membrane surface of the membrane element is further improved. In addition, a void ratio means the volume ratio which the gas occupies in a certain area | region in a gas-liquid two-phase flow.

In the membrane separation facility according to the fourth aspect of the invention, the downward flow flows only in the flow path between the membrane elements in the horizontal cross section of the treatment tank at the portion where the membrane elements are arranged.
In the fifth invention, a plurality of submerged membrane units and an air diffuser for generating a circulating flow circulating in the vertical direction are provided in the treatment tank,
Each membrane unit has a plurality of membrane elements arranged with a space as a circulation flow path, and generates an upward flow and a downward flow by varying the amount of air diffused by the air diffuser. A method for operating a membrane separation facility,
By adjusting the amount of air diffused, in the horizontal cross section of the treatment tank at the portion where the membrane element is arranged, the total cross-sectional area D of the downward flow channel through which the downward flow flows among the flow channels through which the circulating flow flows A circulating flow is generated within an area ratio D / R with the total cross-sectional area R of the upward flow channel through which the upward flow flows is 0.63 or more and 3.33 or less. The counter flow velocity is adjusted within a range of 0.15 m / second or more and 0.25 m / second or less.

  As described above, according to the present invention, the circulation flow stably and smoothly flows, the amount of bubbles held in the downward flow increases, and the disturbance of the movement of the bubbles increases. improves.

It is sectional drawing of the membrane separation equipment in the 1st Embodiment of this invention. It is a top view of a membrane separation equipment. It is a XX arrow line view in FIG. It is a graph which shows the relationship between the area ratio of a membrane separation equipment, and the transmembrane flow rate. It is a graph which shows the relationship between the operation | movement elapsed days of a membrane separation equipment with respect to several area ratio, and a membrane | film | coat dirt ratio. It is a graph which shows the relationship between the operation | movement elapsed days of a membrane separation equipment with respect to several area ratio, and a membrane | film | coat dirt ratio. It is a graph which shows the relationship between the area ratio of the membrane separation equipment in the 2nd Embodiment of this invention, and an intermembrane void ratio. It is a graph which shows the relationship between the operation | movement elapsed days of a membrane separation installation with respect to the several void rate of the flow path between membrane elements through which a downward flow flows, and a membrane | film | coat dirt ratio. It is sectional drawing of the membrane separation equipment in the 3rd Embodiment of this invention. It is a top view of a membrane separation equipment. It is sectional drawing of the membrane separation equipment in the 4th Embodiment of this invention. It is a top view of a membrane separation equipment. It is sectional drawing of the membrane separation equipment in the 5th Embodiment of this invention. It is a top view of a membrane separation equipment. It is a XX arrow line view in FIG. It is sectional drawing of the membrane separation equipment in the 6th Embodiment of this invention. It is sectional drawing of the membrane separation equipment in the 7th Embodiment of this invention. It is a top view of a membrane separation equipment. It is sectional drawing of the membrane separation equipment in the 8th Embodiment of this invention. It is a top view of a membrane separation equipment. It is sectional drawing of the membrane separation equipment in the 9th Embodiment of this invention. It is a top view of a membrane separation equipment. It is sectional drawing of the membrane separation equipment in the 10th Embodiment of this invention. It is sectional drawing of the membrane separation installation in the 11th Embodiment of this invention. It is sectional drawing of the membrane separation equipment in the 12th Embodiment of this invention. It is sectional drawing of the conventional membrane separation installation. It is sectional drawing of another conventional membrane separation installation.

Hereinafter, embodiments of the present invention will be described with reference to the drawings.
(First embodiment)
The reverse aeration type membrane separation equipment of the present invention is used for water treatment such as sewage waste water and purified water, and in the first embodiment, the membrane separation equipment used for membrane separation activated sludge treatment will be described.

As shown in FIGS. 1 to 3, the membrane separation equipment 1 includes a treatment tank 2, a plurality of submerged membrane units 3 a to 3 d, and an air diffusion equipment 5 that generates a circulating flow 4 that circulates in the vertical direction. Have.
Each of the membrane units 3a to 3d has a square box type membrane case 7 installed in the processing tank 2 and open at both upper and lower ends, and a plurality of membrane elements 8 provided in the membrane case 7. Yes. Each membrane element 8 has a filter plate 9 made of resin and a filtration membrane 10 attached to both surfaces of the filter plate 9. Each of these membrane elements 8 communicates with a permeated liquid derivation system 12 that derives a permeated liquid that has permeated through the filtration membrane 10.

  The membrane elements 8 are arranged in parallel in the membrane case 7 with a predetermined interval C (generally about 5 to 8 mm) along the membrane surface of the filtration membrane 10 in the vertical direction. Between the membrane surfaces of the filtration membranes 10 of the membrane elements 8 adjacent in the thickness direction of the membrane element 8, an inter-membrane element flow path 11 is formed.

  The air diffusion equipment 5 is diffused to the air diffuser case 13 installed at the bottom of the treatment tank 2, the plurality of air diffusers 14a to 14d installed in the air diffuser case 13, and the air diffusers 14a to 14d. An air supply device (not shown) for supplying air. The membrane units 3 a to 3 d are provided in the upper part of the diffuser case 13, and the lower ends of the respective membrane cases 7 communicate with the diffuser case 13. Each of the air diffusers 14a to 14d is disposed below each of the membrane units 3a to 3d, and includes a plurality of air diffusers and the like. The air supply device includes a blower, a valve that adjusts the amount of air diffused (air ejection amount) of each of the air diffusers 14a to 14d, and the like.

  Further, the inside of the diffuser case 13 is partitioned by a plurality of partition plates 15 into a plurality of draft portions 17a to 17d. A communicating portion 16 is formed between the lower end of each partition plate 15 and the bottom surface of the processing tank 2, and the draft portions 17 a to 17 d adjacent to each other via the partition plate 15 communicate with each other via the communicating portion 16. doing.

As shown in FIG. 2, when the inner vertical dimension inside the membrane case 7 of each membrane unit 3a-3d is L1, and the inner lateral dimension is L2, the inner transverse area S of one membrane case 7 is L1 × L2. It becomes. Assuming that E% of the inner cross-sectional area S is occupied by the inter-membrane element flow path 11 (hereinafter, E is referred to as the inter-membrane element flow rate), the flow between the membrane elements per one of the membrane units 3a to 3d. The flow path cross-sectional area S1 of the path 11 is expressed by the following equation.
S1 = S × E / 100 = L1 × L2 × E / 100
For example, if the inner longitudinal dimension L1 = 2000 mm and the inner lateral dimension L2 = 500 mm, the inner transverse area S is 2000 mm × 500 mm = 1 m ² . Assuming that 50% of these are the flow passages 11 between the membrane elements, the flow passage cross-sectional area S1 per one of the membrane units 3a to 3d is 0.5 m ² .

  By adjusting the amount of air diffused by each of the air diffusers 14 a to 14 d, the treatment target liquid 19 in the treatment tank 2 flows, and a vertical circulation flow 4 is generated in the treatment tank 2. At this time, the total cross-sectional area of the downward flow path through which the downward flow 20 flows among the flow paths through which the circulating flow 4 flows is D, and the total cross-sectional area of the upward flow path through which the upward flow 21 flows is R. Then, the area ratio D / R between the total cross-sectional area D and the total cross-sectional area R is in the range of 0.63 or more and 3.33 or less, and the flow velocity of the downward flow 20 flowing through the inter-membrane element flow path 11 is 0. The amount of air diffused by each of the air diffusers 14a to 14d is adjusted so as to be within a range of 15 m / second or more and 0.25 m / second or less.

  In addition, the flow velocity of the downward flow 20 flowing through the flow path 11 between the membrane elements is measured by measuring the downward flow velocity in a specific horizontal section of each draft portion 17a to 17d in the diffuser case 13 with an electromagnetic current meter or the like. The flow rate can be obtained by multiplying the ratio of the horizontal cross-sectional area of each draft portion 17a to 17d and the total cross-sectional area of the inter-membrane-element flow path 11 through which the downward flow 20 flows. Further, the flow velocity of the upward flow 21 can be obtained in the same manner.

  For example, as shown in FIG. 1, the amount of air diffused by the first and third air diffusers 14a and 14c is reduced to a small amount of air, and the amount of air diffused by the second and fourth air diffusers 14b and 14d is reduced. By increasing the amount of air diffused from the first and third air diffusers 14a and 14c to a large aeration amount, the circulation flow is caused to flow between the membrane elements in the second and fourth membrane units 3b and 3d. 4 is generated, and the upward flow 21 is reversed near the liquid surface to become the downward flow 20, and the downward flow 20 is generated by the first and third membrane units 3a and 3c. After flowing through each inter-membrane element flow path 11, the first and third draft parts 17 a and 17 c pass through the bottom communication part 16 and flow into the adjacent second and fourth draft parts 17 b and 17 d for circulation. To do.

The area ratio D / R at this time is as follows.
Area ratio D / R = (channel sectional area S1 of the first membrane unit 3a + channel sectional area S1 of the third membrane unit 3c) / (channel sectional area S1 of the second membrane unit 3b + fourth membrane) Channel cross-sectional area S1 of unit 3d) = (0.5 m ² +0.5 m ² ) / (0.5 m ² +0.5 m ² ) = 1
As described above, the area ratio D / R = 1, which satisfies the condition of 0.63 ≦ D / R ≦ 3.33. Further, for example, when the downward flow 20 is generated in the first, third, and fourth membrane units 3a, 3c, and 3d and the upward flow 21 is generated in the second membrane unit 3b, the area ratio D / R = 3.

  In the present embodiment, the downward flow generated in the space 22 between the membrane units 3a to 3d and the downward flow generated in the space 23 between the membrane units 3a to 3d and the side wall surface 2a of the treatment tank 2 are used. Since the flow is interrupted by the diffuser case 13 on the way, it does not communicate with the lower side of each of the membrane units 3 a to 3 d and does not become the circulating flow 4. The spaces 22 and 23 in which such downward flow that does not become the circulation flow 4 is generated are not regarded as downward flow paths and are not included in the total cross-sectional area D. The same applies to the upward flow.

  In the actual operation of the membrane separation facility 1, an operation of switching between the downward flow 20 and the upward flow 21 may be performed every predetermined time. For example, after a predetermined time has elapsed, the first, second, and fourth membrane units 3a, 3b, and 3d are switched to the operation in which the downward flow 20 is generated and the upward flow 21 is generated in the third membrane unit 3c. Further, after a predetermined time has elapsed, the operation is switched to the operation in which the downward flow 20 is generated in the first, second, and third membrane units 3a, 3b, and 3c and the upward flow 21 is generated in the fourth membrane unit 3d. After a predetermined time has elapsed, the operation is switched to the operation in which the downward flow 20 is generated in the second, third, and fourth membrane units 3b, 3c, and 3d and the upward flow 21 is generated in the first membrane unit 3a. Repeated operation can also be performed.

Hereinafter, the operation of the above configuration will be described.
By making the area ratio D / R in the range of 0.63 or more and 3.33 or less and the flow velocity of the downward flow 20 in the range of 0.15 m / second or more and 0.25 m / second or less, the first And the rising speed of the bubbles released from the third air diffusers 14a and 14c is slowed down, and the bubbles flow in the downward flow 20 flowing through the inter-membrane-element channel 11 of the first and third membrane units 3a and 3c. Is raised at a low speed while swinging laterally. Due to the presence of such bubbles, the flow of the downward flow 20 is disturbed, and the amount of bubbles held in the processing target liquid 19 in the inter-membrane-element flow path 11 of the first and third membrane units 3a and 3c increases, resulting in voids. The rate increases. Further, since the bubbles are brought into contact with each other and the bubble diameter is appropriately increased, the opportunity of contact between the membrane surface and the bubbles is increased, and the membrane surface of the filtration membrane 10 of the first and third membrane units 3a and 3c is good. To be washed. Such an effect is remarkably generated by reverse aeration.

  If the flow velocity of the downward flow 20 exceeds 0.25 m / sec, some of the bubbles released from the first and third air diffusers 14a and 14c do not rise, and the downward flow Therefore, the cleaning efficiency of the membrane surface of the filtration membrane 10 of the first and third membrane units 3a and 3c is lowered.

  On the contrary, when the flow velocity of the downward flow 20 is lower than 0.15 m / sec, the rising speed of the bubbles released from the first and third air diffusers 14a and 14c is not so slow, and the downward flow Since the bubbles in the flow 20 are not sufficiently oscillated in the lateral direction, the amount of bubbles held in the liquid 19 to be processed in the inter-membrane-element flow path 11 of the first and third membrane units 3a, 3c is reduced, and the first In addition, the cleaning efficiency of the membrane surface of the filtration membrane 10 of the third membrane units 3a and 3c is lowered.

Further, the membrane surfaces of the filtration membranes 10 of the second and fourth membrane units 3b and 3d are sufficiently cleaned by a large amount of bubbles in the upward flow 21.
In the above embodiment, the area ratio D / R is in the range of 0.63 to 3.33, and the flow rate of the downward flow 20 is in the range of 0.15 m / sec to 0.25 m / sec. However, as a more preferable range, the area ratio D / R is in the range of 0.67 or more and 3.0 or less, and the flow rate of the downward flow 20 is 0.16 m / second or more and 0.22 m / second or less. It may be within the range. As a result, the film surface is better cleaned.

  The graph shown in FIG. 4 shows the relationship between the area ratio D / R and the intermembrane flow velocity (m / sec) of the membrane units 3a to 3d. The graph Gd is the intermembrane flow velocity of the downward flow 20, and the graph Gr. Indicates the transmembrane flow rate of the upward flow 21. The intermembrane flow velocity of the downward flow 20 is the flow velocity of the downward flow 20 flowing in the inter-membrane element flow path 11, and the inter-membrane flow velocity of the upward flow 21 is the upward flow flowing in the inter-membrane element flow path 11. A flow rate of 21.

  In the graph of FIG. 4, 5 to 8 membrane units are provided in the treatment tank 2, and the ratio between the number of membrane units through which the downward flow 20 flows and the number of membrane units through which the upward flow 21 flows is expressed as follows. By switching to 2 to 3, 3 to 3, 4 to 2, 6 to 2, and 4 to 1, the area ratio D / R was set to 0.67, 1, 2, 3, and 4.

  Also, the total aeration amount (total aeration amount) of each aeration amount is made the same so that the small aeration amount and the large aeration amount corresponding to the area ratio D / R = 0.67, 1, 2, 3, 4 When the ratio was 13:87, 19:81, 32:68, 39:61, 49:51, the inter-membrane flow velocity of the downward flow 20 of the graph Gd was 0.2 to 0.08 m / sec. . For example, when the area ratio D / R is 0.67 (that is, the number ratio is 2 to 3) and the ratio of the small aeration amount to the large aeration amount is 13 to 87, two membrane units through which the downward flow 20 flows The aeration amount per unit is 6.5 (= 13/2), and the aeration amount per unit of the three membrane units through which the upward flow 21 flows is 29 (= 87/3).

  In addition, when the area ratio D / R is 4 (that is, the number ratio is 4 to 1) and the ratio of the small aeration amount to the large aeration amount is 49 to 51, the per unit of membrane unit through which the upward flow 21 flows is per unit. The aeration amount is 51, and the propulsive force of the flow is increased, so that the flow velocity of the upward flow 21 is expected to increase. However, in the experiment, a tendency that the flow velocity becomes slow was observed. This is thought to be due to the fact that when the void ratio increases, the number of bubbles staying at the inflow portion from the draft portion to the flow path between the membrane elements increases and the resistance increases. And since the flow velocity of the upward flow 21 fell, the flow velocity of the downward flow 20 also fell as a result.

  The graph shown in FIG. 5 and FIG. 6 shows the relationship between the number of days (days) of operation of the membrane separation equipment 1 and the membrane contamination ratio (kPa / kPa) of the membrane element 8. The membrane dirt ratio is the ratio of the transmembrane differential pressure of the membrane element 8 that has been operated for a predetermined number of days to the transmembrane differential pressure of the clean new membrane element 8.

  In the graph shown in FIG. 5, the first graph G1 has an area ratio D / R of 1, the flow rate of the downward flow 20 is 0.22 m / sec, and the second graph G2 has an area ratio D / R of 1. The flow velocity of the downward flow 20 is 0.08 m / second, the third graph G3 has an area ratio D / R of 0.67, the flow velocity of the downward flow 20 is 0.19 m / second, and the fourth graph G4 has an area. A case where the ratio D / R is 0.67 and the flow rate of the downward flow 20 is 0.08 m / sec is shown. Further, the fifth graph G5 shows a case where the aeration amount for all the membrane units is set to a large aeration amount, and the upward flow operation for generating the upward flow 21 in all the membrane units is performed.

  In addition, in the graph shown in FIG. 6, the sixth graph G6 has an area ratio D / R of 2, the flow rate of the downward flow 20 is 0.2 m / sec, and the seventh graph G7 has an area ratio D / R of 3 In the eighth graph G8, the area ratio D / R is 3, the flow velocity of the downward flow 20 is 0.16 m / sec, and the ninth graph G9 has an area. The ratio D / R is 3 and the downward flow 20 has a flow velocity of 0.12 m / second, and the tenth graph G10 is operated with an area ratio D / R of 4 and the downward flow 20 has a flow velocity of 0.14 m / second. Shows the case. Further, the fifth graph G5 is the same as the graph shown in FIG. 5, and the upward flow for generating the upward flow 21 in all the membrane units by setting the aeration amount for all the membrane units to a large aeration amount. The case where operation was performed is shown.

  In the graph of FIG. 5, the first and third graphs G1 and G3 are in the condition of 0.63 ≦ area ratio D / R ≦ 3.33 and 0.15 m / s ≦ downward flow velocity ≦ 0.25 m / s. The film contamination ratio of the first and third graphs G1 and G3 is lower than the film contamination ratio of the second and fourth graphs G2 and G4, and the film contamination ratio of the fifth graph G5. Is kept almost the same.

  In the graph of FIG. 6, the sixth to eighth graphs G6 to G8 are also 0.63 ≦ area ratio D / R ≦ 3.33 and 0.15 m / s ≦ downward flow velocity ≦ 0.25 m / s. The film contamination ratio of the sixth to eighth graphs G6 to G8 is lower than the film contamination ratio of the ninth and tenth graphs G9 and G10, and the film of the fifth graph G5 It is kept almost the same as the dirt ratio. Thus, it is clear that satisfying the above conditions, the circulating flow stably and smoothly flows, and the cleaning effect of the membrane surface of the membrane element is improved.

(Second Embodiment)
In the second embodiment, by adjusting the amount of air diffused by each of the air diffusers 14a to 14d, 0.63 ≦ area ratio D / R ≦ 3.33 and 0.33 in the first embodiment. While satisfying the condition of 15 m / s ≦ downward flow velocity ≦ 0.25 m / s, the void ratio εd of the inter-membrane-element channel 11 through which the downward flow 20 flows is set to 0.07 or more. The void ratio εd can be measured by installing a gas-liquid flow measurement system (optical fiber void ratio meter) manufactured by Nippon Kanomax in the channel 11 between the membrane elements.

Hereinafter, the operation of the above configuration will be described.
For example, as in the first embodiment, as shown in FIG. 1, the first and third air diffusers 14a and 14c have a small aeration amount, and the second and fourth air diffusers. With the amount of air diffused by the devices 14b and 14d as a large aeration amount, an upward flow 21 is generated in the channel 11 between the membrane elements of the second and fourth membrane units 3b and 3d, and the first and third membrane units. A downward flow 20 is generated in the flow path 11 between the membrane elements 3a and 3c.

  When the void ratio εd of the inter-membrane-element flow path 11 through which the downward flow 20 flows is 0.07 or more, the bubble having an appropriately increased diameter and the filtration membrane 10 of the first and third membrane units 3a and 3c are in contact with each other. Opportunities increase, and the opportunity for bubble disturbance to act on the film surface increases, so that the cleaning effect on the film surfaces of the first and third film units 3a and 3c is improved.

  In addition, when the void ratio εd of the inter-membrane element flow path 11 through which the downward flow 20 flows decreases to less than 0.07, the action of bubbles on the membrane surface of the filtration membrane 10 of the membrane element 8 decreases. The cleaning effect on the film surfaces of the first and third film units 3a and 3c is reduced.

  The graph shown in FIG. 7 shows the relationship between the area ratio D / R and the inter-membrane void ratio of the membrane units 3a to 3d, and the graph Gd shows the void ratio of the inter-membrane flow path 11 through which the downward flow 20 flows. εd and graph Gr indicate the void ratio εr of the inter-membrane element flow path 11 through which the upward flow 21 flows. The graph shown in FIG. 7 is obtained under the same conditions as the graph shown in FIG.

  In the reverse aeration, the aeration amount of the membrane unit that forms the downward flow 20 is smaller than the aeration amount of the membrane unit that forms the upward flow 21, but the void in the channel 11 between the membrane elements in which the downward flow 20 flows. The rate is characterized by being equivalent to the void rate of the channel 11 between the membrane elements in which the upward flow flows. The void ratio of the flow path 11 between the membrane elements through which the upward flow 21 flows is influenced by factors such as the flow velocity of the upward flow 21 and the bubble diameter, and the amount of aeration is large as when the area ratio D / R is 4. It has been found that the void ratio may also decrease as the flow velocity of the upward flow 21 decreases.

Moreover, the graph shown in FIG. 8 shows the relationship between the operation elapsed days (days) of the membrane separation equipment 1 and the membrane dirt ratio (kPa / kPa) of the membrane element 8.
In this graph, the first graph G1 has a void rate εd of 0.1 and the flow velocity of the downward flow 20 is 0.25 m / sec, and the second graph G2 has a void rate εd of 0.075 and a downward flow. The flow rate of 20 is 0.2 m / second, the third graph G3 has a void rate εd of 0.07, the flow rate of the downward flow 20 is 0.15 m / second, and the fourth graph G4 has a void rate εd of 0. It is 05 and the case where it drive | operates with the flow velocity of the downward flow 20 at 0.1 m / sec is shown. Further, the fifth graph G5 shows that the void ratio εr is 0 when the upward flow operation in which the upward flow 21 is generated in all the membrane units is performed with the large aeration amount for all the membrane units. The case of 06 is shown.

  In the graph shown in FIG. 8, the first to third graphs G1 to G3 are 0.63 ≦ area ratio D / R ≦ 3.33 and 0.15 m / s ≦ downward in the first embodiment. The flow velocity ≦ 0.25 m / s is satisfied, and the void ratio εd ≧ 0.07 is satisfied. The film contamination ratio of the first to third graphs G1 to G3 is lower than the film contamination ratio of the fourth graph G4. In particular, the first graph G1 is almost the same as the film contamination ratio of the fifth graph G5. Kept the same. Thereby, by satisfying the above conditions, the circulation flow stably and smoothly flows, the bubble retention amount increases, and the disturbance of the bubble movement increases, so the cleaning effect of the membrane surface of the membrane element is improved. Is clear.

(Third embodiment)
In the first embodiment, as shown in FIG. 1, one common diffuser case 13 is provided below each membrane unit 3 a to 3 d, but in the third embodiment, FIG. 9 is used. As shown in FIG. 10, a plurality of diffuser cases 13a to 13d are provided for each of the membrane units 3a to 3d. Each air diffuser 14a-14d is installed in each air diffuser case 13a-13d. The membrane units 3a to 3d are provided on the upper sides of the diffuser cases 13a to 13d, and the lower ends of the membrane cases 7 communicate with the diffuser cases 13a to 13d.

  The lower part of the membrane units 3 a to 3 d adjacent to each other is shielded by the upper shielding plate 26. A communication port 27 is formed at the lower end of each of the diffuser cases 13a to 13d. Among these, the communication ports 27 other than the communication ports 27 on the surfaces where the adjacent diffuser cases 13 a to 13 d face each other are closed by the lower shielding plate 28.

According to this, the same operation and effect as the first and second embodiments can be obtained.
(Fourth embodiment)
The fourth embodiment is a modification of the third embodiment. As shown in FIGS. 11 and 12, the upper shielding plate 26 shields the lower portions of the membrane units 3 a to 3 d adjacent to each other. Furthermore, the upper shielding plate 26 also shields the space between the lower part of each of the membrane units 3a to 3d and the wall surface 2a of the processing tank 2.

According to this, the same operation and effect as the first and second embodiments can be obtained.
(Fifth embodiment)
In the fifth embodiment, as shown in FIGS. 13 to 15, the membrane separation facility 1 includes a treatment tank 2, a plurality of submerged membrane units 3 a to 3 d, and a circulating flow 4 that circulates in the vertical direction. A diffuser 5 for generating

  The membrane units 3a to 3d are adjacent to each other, and the upper region and the lower region of the membrane units 3a to 3d communicate with each other in the processing tank 2. Each of the membrane units 3 a to 3 d has a membrane case 32 installed in the treatment tank 2 and a plurality of membrane elements 8 provided in the membrane case 32. In the membrane case 32, the upper region forms a membrane filling portion and the lower region forms a draft portion. The membrane elements 8 are arranged in parallel at a predetermined interval C in the membrane filling portion with the membrane surface of the filtration membrane 10 along the vertical direction.

  The air diffuser 5 includes a plurality of air diffusers 14a to 14d installed below the membrane elements 8 of the respective membrane units 3a to 3d, and an air supply for supplying air for air diffused to the air diffusers 14a to 14d. And a device (not shown).

  According to this, for example, the amount of air diffused by the first and third air diffusers 14a and 14c is set as a small amount of air, and the amount of air diffused by the second and fourth air diffusers 14b and 14d is set as a large amount of air. As a result, an upward flow 21 is generated in the flow path 11 between the membrane elements of the second and fourth membrane units 3b, 3d, and the upward flow 21 is reversed near the liquid surface to become a downward flow 20. The downward flow 20 flows from the upper region of the second and fourth membrane units 3b and 3d to the upper region of the first and third membrane units 3a and 3c, and the first and third membrane units 3a and 3c. After flowing through each of the membrane element flow paths 11, it flows from the lower region of the first and third membrane units 3 a, 3 c to the lower region of the second and fourth membrane units 3 b, 3 d for circulation. In this case, in the horizontal cross section of the treatment tank 2 at the portion where the membrane element 8 is disposed, the downward flow 20 flows into the channel 11 between the membrane elements of the first and third membrane units 3a and 3c, and the upward flow The flow 21 flows into the inter-membrane element flow paths 11 of the second and fourth membrane units 3b and 3d.

At this time, when the inner vertical dimension L1 of each membrane unit 3a to 3d is 1500 mm, the inner lateral dimension L2 is 500 mm, and the flow rate E between the membrane elements of each membrane unit 3a to 3d is 50%, the area ratio D / R is as follows.
D / R = (0.75 m ² × 0.5 + 0.75 m ² × 0.5) / (0.75 m ² × 0.5 + 0.75 m ² × 0.5) = 1
As described above, by setting the area ratio D / R within the range of 0.63 or more and 3.33 or less, the same operation and effect as the first and second embodiments can be obtained.

(Sixth embodiment)
The sixth embodiment is a modification of the fifth embodiment, and as shown in FIG. 16, a plurality of membrane units 3 a to 3 d and 34 a to 34 d are arranged in two upper and lower stages in the treatment tank 2. It is installed in (multi-stage) stacking.

According to this, the same operation and effect as the first and second embodiments can be obtained.
In the sixth embodiment, the membrane units 3a to 3d and 34a to 34d are installed in two upper and lower stages, but may be three or more stages. In addition, although four upper membrane units 3a to 3d and four lower membrane units 34a to 34d are installed, a plurality of units other than four may be installed.

(Seventh embodiment)
The seventh embodiment is a modification of the third embodiment shown in FIG. 9 and eliminates the upper and lower shielding plates 26 and 28 in the third embodiment. As shown in FIGS. 17 and 18, a flow passage 37 having a predetermined interval is formed between the membrane units 3 a to 3 d adjacent to each other and between the diffuser cases 13 a to 13 d. In addition, a flow passage 38 having a predetermined interval is formed between each of the membrane units 3 a to 3 d and each of the diffuser cases 13 a to 13 d and the wall surface 2 a of the treatment tank 2.

The inside of each of the diffuser cases 13 a to 13 d communicates with the outside of the diffuser cases 13 a to 13 d via the communication port 27.
According to this, for example, the amount of air diffused by the second air diffuser 14b is a small amount of aerated air, and the amount of air diffused by the first, third, and fourth air diffusers 14a, 14c, and 14d is a large amount of aerated air. In this case, an upward flow 21 is generated in the flow path 11 between the membrane elements of the first, third, and fourth membrane units 3a, 3c, and 3d, and the first, third, and fourth units 3a, 3c, and 3d are generated. The upward flow 21 that has passed through the inside reverses in the vicinity of the liquid surface to become the downward flow 20, and the downward flow 20 flows through the communication port 27 after flowing through the second unit 3 b and the flow passages 37 and 38. Then, the air flows into the first, third, and fourth aeration cases 13a, 13c, and 13d and circulates.

At this time, if the inner vertical dimension L1 of each membrane unit 3a to 3d is 2000 mm, the inner horizontal dimension L2 is 500 mm, the inner vertical dimension L3 of the treatment tank 2 is 2200 mm, and the inner horizontal dimension L4 is 2500 mm, the downward flow The total cross-sectional area D of the downward flow channel through which 20 flows is a value obtained by adding the channel cross-sectional area S2 (cross-sectional area) of each of the flow passages 37 and 38 to the channel cross-sectional area S1 of the second unit 3b. That is, when the flow rate E between the membrane elements is 50%, the area ratio D / R is as follows.
Area ratio D / R = (channel cross-sectional area S1 of the second unit 3b + channel cross-sectional area S2 of the flow passages 37 and 38) / (flow cross-sectional area S1 of the first unit 3a + flow of the third unit 3c) Road cross-sectional area S1 + channel cross-sectional area S1 of the fourth unit 3d) = (1 m ² × 0.5 + (5.5 m ² −4 m ² )) / (1 m ² × 0.5 × 3) = 1.33
As described above, by setting the area ratio D / R within the range of 0.63 or more and 3.33 or less, the same operation and effect as the first and second embodiments can be obtained.

  In addition, the downward flow 20 flowing through the flow passages 37 and 38 flows into the first, third, and fourth aeration cases 13a, 13c, and 13d through the communication port 27, and the first, third, and third flows. The four membrane units 3a, 3c, 3d communicate with each other below and circulate up and down. Thus, the flow passages 37 and 38 through which the downward flow 20 that is a part of the circulation flow 4 flows are regarded as the downward flow passages and are included in the total cross-sectional area D.

(Eighth embodiment)
The eighth embodiment is a modification of the third embodiment, and as shown in FIGS. 19 and 20, a flow for promoting the flow at the bottom of each flow passage 37, 38, respectively. A promoting air diffuser 41 (an example of a flow promoting device) is installed.

  According to this, for example, the amount of air diffused by the first, third, and fourth air diffusers 14a, 14c, and 14d is a small amount of air diffused, and the amount of air diffused by the second air diffuser 14b and the air diffused for flow promotion When the aeration amount of the device 41 is a large aeration amount, the upward flow 21 is generated in the inter-membrane-element flow path 11 and the flow passages 37 and 38 of the second unit 3b, and the upward flow 21 is generated. It reverses in the vicinity of the liquid surface to become a downward flow 20, and the downward flow 20 flows through the first, third, and fourth membrane units 3 a, 3 c, and 3 d, and then passes through the communication port 27 to form the second diffused air. It flows into the case 13b and the bottom of each flow passage 37, 38 and circulates.

At this time, the total cross-sectional area R of the upward flow path through which the upward flow 21 flows is a value obtained by adding the flow path cross-sectional area S2 of each of the flow paths 37 and 38 to the flow path cross-sectional area S1 of the second unit 3b. . That is, the area ratio D / R is as follows.
Area ratio D / R = (channel cross-sectional area S1 of first unit 3a + channel cross-sectional area S1 of third unit 3c + channel cross-sectional area S1 of fourth unit 3d) / (flow of second unit 3b) Road cross-sectional area S1 + flow path cross-sectional area S2 of the flow passages 37 and 38) = (1 m ² × 0.5 × 3) / (1 m ² × 0.5 + (5.5 m ² −4 m ² )) = 0.75
As described above, by setting the area ratio D / R within the range of 0.63 or more and 3.33 or less, the same operation and effect as the first and second embodiments can be obtained.

  The upward flow 21 flowing through the flow passages 37 and 38 is reversed near the liquid surface, flows into the first, third, and fourth membrane units 3a, 3c, and 3d from above and circulates up and down. Thus, the flow passages 37 and 38 through which the upward flow 21 that is a part of the circulation flow 4 flows are regarded as the upward flow passage and included in the total cross-sectional area R.

(Ninth embodiment)
The ninth embodiment is a modification of the fifth embodiment shown in FIG. 13, and as shown in FIGS. 21 and 22, the first and second films are disposed in the treatment tank 2. Units 3a and 3b, first and second air diffusers 14a and 14b, and a flow promoting air diffuser 41 (an example of a flow promoting device) are installed. A flow passage 44 having a predetermined interval is formed between the first membrane unit 3a and the second membrane unit 3b, and the flow promoting air diffuser 41 is installed at the bottom of the flow passage 44. Yes.

  Further, the lower region of the flow passage 44 communicates with the lower regions of the first and second membrane units 3a and 3b, and the upper region of the flow passage 44 and the upper portions of the first and second membrane units 3a and 3b. It communicates with the area.

  As an example, the inner vertical dimension L1 of each membrane unit 3a, 3b is 2000 mm, the inner horizontal dimension L2 is 500 mm, the width W of the flow passage 44 is 150 mm, and the flow rate E between the membrane elements is 50%.

Hereinafter, the operation of the above configuration will be described.
For example, as shown in FIG. 21, in the first operation, the amount of air diffused by the first and second air diffusers 14a and 14b is set to a small amount of air, and the amount of air diffused by the flow promoting air diffuser 41 is set to a large amount of air. By setting the amount, the upward flow 21 is generated in the flow passage 44, and the upward flow 21 is reversed in the vicinity of the liquid level in the upper region of the flow passage 44 to become the downward flow 20. The downward flow 20 flows through the flow path 11 between the membrane elements of the first and second membrane units 3a and 3b, and then flows from the lower region of the first and second membrane units 3a and 3b to the flow passage 44. It flows into the lower area and circulates.

In this case, the area ratio D / R is as follows.
Area ratio D / R = (channel cross-sectional area S1 of the first unit 3a + channel cross-sectional area S1 of the second unit 3b) / (channel cross-sectional area S2 of the flow path 44) = (1 m ² × 0.5 + 1 m ² × 0.5) / (0.3 m ² ) = 3.33
After performing the first operation for a predetermined time, the first operation is switched to the second operation as follows.

  By setting the aeration amount of the first aeration device 14a as a small aeration amount, and the aeration amount of the flow promotion aeration device 41 and the aeration amount of the second aeration device 14b as a large aeration amount, An upward flow 21 occurs in the flow path 44 and the flow path 11 between the membrane elements of the second membrane unit 3b, and the upward flow 21 is reversed near the liquid surface to become a downward flow 20, and the downward flow 20 is After flowing through the inter-membrane-element flow paths 11 of the first membrane unit 3a, it flows from the lower region of the first membrane unit 3a into the lower region of the flow path 44 and the lower region of the second membrane unit 3b. Circulate.

In this case, the area ratio D / R is as follows.
Area ratio D / R = (channel cross-sectional area S1 of first unit 3a) / (channel cross-sectional area S1 of second unit 3b + channel cross-sectional area S2 of flow path 44) = (1 m ² × 0.5 ) / (1 m ² × 0.5 + 0.3 m ² ) = 0.63
After performing the second operation for a predetermined time, the second operation is switched to the following third operation.

  By setting the aeration amount of the second aeration device 14b to a small aeration amount, and the aeration amount of the flow promotion aeration device 41 and the aeration amount of the first aeration device 14a to a large aeration amount, An upward flow 21 is generated in the flow path 44 and the flow path 11 between the membrane elements of the first membrane unit 3a, the upward flow 21 is reversed near the liquid surface to become a downward flow 20, and the downward flow 20 is Then, after flowing through each membrane element flow path 11 of the second membrane unit 3b, it flows from the lower region of the second membrane unit 3b into the lower region of the flow path 44 and the lower region of the first membrane unit 3a. Circulate.

In this case, the area ratio D / R is the same as that in the second operation and is 0.63.
When the first operation to the third operation are performed by switching at predetermined time intervals, in each operation, the area ratio D / R is set within a range of approximately 0.63 or more and 3.33 or less. In addition, operations and effects similar to those of the second embodiment can be obtained.

(Tenth embodiment)
The tenth embodiment is a modification of the ninth embodiment. As shown in FIG. 23, the first and second film units 3a and 3b described in the ninth embodiment are used. When the first and second air diffusers 14a and 14b, the flow promoting air diffuser 41 (an example of a flow promoting device), and the flow passage 44 are used as the membrane separation unit 46, such a membrane separation unit 46 can perform processing. A plurality of units are installed in the tank 2.

According to this, the same operation and effect as in the ninth embodiment can be obtained.
In the tenth embodiment, three membrane separation units 46 are installed in the processing tank 2, but a plurality of units other than three may be installed.

  In the eighth to tenth embodiments, the flow promoting air diffuser 41 is used as an example of the flow promoting device. However, instead of the flow promoting diffuser 41, a stirring device or the like is provided to allow the flow to flow. May be promoted.

(Eleventh embodiment)
In the eleventh embodiment, as shown in FIG. 24, in the membrane separation tank 55 which is an example of the processing tank, the membrane units 3a to 3d and the aeration equipment 5 shown in the first embodiment are provided. Is provided. A biological treatment tank 56 (an example of an upstream tank) is installed on the upstream side of the membrane separation tank 55, and a sludge storage tank 57 (an example of a downstream tank) is installed on the downstream side of the membrane separation tank 55. The biological treatment tank 56 is an aeration tank, a nitrification tank, an anaerobic digestion tank, or the like. Further, although the sludge storage tank 57 is provided as an example of the downstream tank, a sludge concentration tank may be provided instead of the sludge storage tank 57.

  The upper part of the biological treatment tank 56 and the upper part of the membrane separation tank 55 communicate with each other via a supply port 59, and the treatment target liquid 19 in the biological treatment tank 56 overflows from the supply port 59 and is supplied into the membrane separation tank 55. The Further, the inside of the diffuser case 13 of the diffuser facility 5 and the lower part of the sludge storage tank 57 communicate with each other via the discharge pipe 60. In addition, the sludge storage tank 57 is provided with a drawing pump 61 and a return path 64 for drawing the processing target liquid 19 (sludge) in the tank and returning it to the biological treatment tank 56. The supply port 59, the discharge pipe 60, the extraction pump 61, and the return path 64 constitute a flow promoting device that promotes the downward flow in the membrane separation tank 55.

Hereinafter, the operation of the above configuration will be described.
For example, the amount of air diffused by the first and third air diffusers 14a and 14c is reduced to a small amount of air, and the amount of air diffused by the second and fourth air diffusers 14b and 14d is changed to the first and third air diffusers. By increasing the amount of air diffused from the air devices 14a and 14c to a large aeration amount, an upward flow 21 is generated in the channel 11 between the membrane elements of the second and fourth membrane units 3b and 3d. The counterflow 21 is reversed near the liquid surface to become the downward flow 20, and the downward flow 20 flows through the channel 11 between the membrane elements of the first and third membrane units 3a, 3c, The third draft parts 17a and 17c flow through the communication part 16 into the second and fourth draft parts 17b and 17d to circulate.

  At this time, the processing target liquid 19 in the biological treatment tank 56 overflows from the supply port 59 by driving the extraction pump 61 to extract the processing target liquid 19 in the sludge storage tank 57 and returning it to the biological processing tank 56. After being supplied into the membrane separation tank 55 and flowing downward in the membrane separation tank 55, it is discharged into the sludge storage tank 57 through the discharge pipe 60 and returned to the biological treatment tank 56 by the drawing pump 61. . Thereby, the process target liquid 19 circulates over each tank 55,56,57.

  At this time, since the discharge pipe 60 is lower than the supply port 59, the processing target liquid 19 supplied from the supply port 59 into the membrane separation tank 55 becomes a downward flow and becomes the first and third membranes. It flows through the flow paths 11 between the membrane elements of the units 3a and 3c. As a result, in addition to the downward flow generated by aeration, a downward flow flows from the supply port 59 toward the discharge pipe 60 in the first and third membrane units 3a and 3c. For this reason, the flow rate of the downward flow 20 flowing through the first and third membrane units 3a, 3c is increased, and the downward flow flowing through the inter-membrane element flow paths 11 of the first and third membrane units 3a, 3c. A flow rate of 20 increases. Thereby, even if it reduces the aeration amount (large aeration amount) of the 2nd and 4th diffuser 14b, 14d, the flow velocity of the downward flow 20 is 0.15 m / sec or more and 0.25 m / sec or less. The power consumption can be saved by reducing the total amount of aeration of the diffuser 5.

(Twelfth embodiment)
The twelfth embodiment is a modification of the eleventh embodiment, and as shown in FIG. 25, the sludge storage tank 57 is not installed. Further, the membrane separation tank 55 is provided with a drawing pump 61 and a return path 64 for drawing out the processing target liquid 19 in the diffuser case 13 and returning it to the biological treatment tank 56. The supply port 59, the drawing pump 61, and the return passage 64 constitute a flow promoting device that promotes the downward flow in the membrane separation tank 55. The drawing pump 61 is connected to the bottom of the membrane separation tank 55 through a drawing tube 61a.

Hereinafter, the operation of the above configuration will be described.
For example, the amount of air diffused by the first and third air diffusers 14a and 14c is reduced to a small amount of air, and the amount of air diffused by the second and fourth air diffusers 14b and 14d is changed to the first and third air diffusers. Increasing the amount of air diffused by the air devices 14a and 14c to a large aeration amount causes the upward flow 21 to occur in the second and fourth membrane units 3b and 3d, and the first and third membrane units 3a. , 3c, a downward flow 20 is generated.

  At this time, the processing target liquid 19 in the biological treatment tank 56 overflows from the supply port 59 by driving the extraction pump 61 to extract the processing target liquid 19 in the diffuser case 13 and returning it to the biological treatment tank 56. Then, it is supplied into the membrane separation tank 55 and returned to the biological treatment tank 56 from the membrane separation tank 55 by the drawing pump 61. Thereby, the process target liquid 19 circulates through the tanks 55 and 56.

  At this time, the processing target liquid 19 supplied into the membrane separation tank 55 from the supply port 59 flows downward and flows through the inter-membrane element flow paths 11 of the first and third membrane units 3a and 3c. . As a result, in addition to the downward flow generated by aeration, a downward flow flows from the supply port 59 toward the extraction pipe 61a in the first and third membrane units 3a and 3c. For this reason, the flow velocity of the downward flow 20 flowing through the channel 11 between the membrane elements of the first and third membrane units 3a and 3c is increased, and thereby the second and fourth air diffusers 14b and 14d Even if the aeration amount (large aeration amount) is reduced, the flow velocity of the downward flow 20 can be within the range of 0.15 m / second or more and 0.25 m / second or less. The amount of aeration can be reduced to save power consumption.

  In the eleventh and twelfth embodiments, the membrane units 3a to 3d and the diffuser 5 shown in the first embodiment are provided in the membrane separation tank 55. In addition, you may provide what was shown in the said 2nd-10th embodiment.

  In the first embodiment, as shown in FIG. 1, a downward flow 20 is generated in the first and third membrane units 3a and 3c, and an upward flow is generated in the second and fourth membrane units 3b and 3d. Although the flow 21 is generated, the flow 21 may be switched so that the downward flow 20 and the upward flow 21 are reversed. Moreover, you may change suitably the combination of the downward flow 20 and the upward flow 21. FIG. The same applies to other embodiments.

  In each said embodiment, although the four film | membrane units 3a-3d were installed in the processing tank 2, multiple units other than four may be installed. In this case, it is sufficient that the downward flow 20 flows in the flow path between the membrane elements of at least one membrane unit and the upward flow flows in the flow path between the membrane elements of the remaining membrane units.

In each of the above embodiments, the membrane element 8 is a flat membrane type, but may be a hollow fiber type membrane element 8.
In many cases, the capacity (cross-sectional area) and shape of the water tank in which the membrane separator is installed cannot give priority to the layout of the membrane separator. That is, when combined with a biological treatment tank, the tank capacity is determined by conditions such as BOD-MLSS load, BOD volume load, total nitrogen-MLSS load, etc., and the shape of the tank may be restricted by the site shape where the equipment is installed. . Moreover, although the remodeling work of the existing plant has been increasing recently, the existing remodeling work will install a membrane separation device in the existing water tank, and there is no degree of freedom. The present invention can meet the expectation while it is desired to develop a membrane separation apparatus that can be installed without being constrained by the capacity of the water tank or the shape of the water tank.

DESCRIPTION OF SYMBOLS 1 Membrane separation equipment 2 Processing tank 3a-3d, 34a-34d Membrane unit 4 Circulating flow 8 Membrane element 11 Flow path 14a-14d between membrane elements Diffuser 20 Downstream flow 21 Upstream flow 55 Membrane separation tank (processing tank)

Claims (5)

In the treatment tank, a plurality of immersion type membrane units and an air diffuser for generating a circulating flow circulating in the vertical direction are provided,
Each membrane unit has a plurality of membrane elements arranged with a space as a circulation flow path,
By diffusing from the diffuser below the membrane element, a downward flow flows in the flow path between the membrane elements of at least one membrane unit, and an upward flow flows in the flow path between the membrane elements of the remaining membrane units. A membrane separation facility,
The area ratio of the total cross-sectional area D of the downward flow channel and the total cross-sectional area R of the upward flow channel among the flow channels through which the circulating flow flows in the horizontal section of the treatment tank at the portion where the membrane element is disposed D / R is in the range of 0.63 or more and 3.33 or less, and the flow velocity of the downstream flow between the membrane elements is in the range of 0.15 m / second or more and 0.25 m / second or less. A membrane separation facility. The area ratio D / R is in the range of 0.67 or more and 3.0 or less, and the downward flow velocity in the flow path between the membrane elements is in the range of 0.16 m / second or more and 0.22 m / second or less. The membrane separation equipment according to claim 1, wherein The membrane separation facility according to claim 1 or 2, wherein a void ratio εd of the flow path between the membrane elements in which the downward flow flows is 0.07 or more. The membrane separation according to any one of claims 1 to 3, wherein the downward flow flows only in the flow path between the membrane elements in the horizontal cross section of the treatment tank at the portion where the membrane elements are arranged. Facility. In the treatment tank, a plurality of immersion type membrane units and an air diffuser for generating a circulating flow circulating in the vertical direction are provided,
Each membrane unit has a plurality of membrane elements arranged with a space as a circulation flow path, and generates an upward flow and a downward flow by varying the amount of air diffused by the air diffuser. A method for operating a membrane separation facility,
By adjusting the amount of air diffused, in the horizontal cross section of the treatment tank at the portion where the membrane element is arranged, the total cross-sectional area D of the downward flow channel through which the downward flow flows among the flow channels through which the circulating flow flows A circulating flow is generated within an area ratio D / R with the total cross-sectional area R of the upward flow channel through which the upward flow flows is 0.63 or more and 3.33 or less. A method for operating a membrane separation facility, characterized by adjusting a countercurrent flow velocity within a range of 0.15 m / sec or more and 0.25 m / sec or less.

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