WO2011152461A1

WO2011152461A1 - Solid-liquid separator device and operation method thereof

Info

Publication number: WO2011152461A1
Application number: PCT/JP2011/062610
Authority: WO
Inventors: 勝行矢ノ根; 朋樹川岸; 信也末吉
Original assignee: 三菱レイヨン株式会社
Priority date: 2010-06-01
Filing date: 2011-06-01
Publication date: 2011-12-08
Also published as: JPWO2011152461A1; CN203379815U; JP5982822B2; TWI462881B; TW201210948A

Abstract

A membrane separation device has multiple separation membrane modules arranged so as to be separated by an interval, and the separation membrane modules have multiple filtration membrane sheets arranged in parallel. Below the aforementioned separation membrane modules is disposed an aeration device provided with multiple aeration tubes which have a gas outlet and are arranged in parallel. Gas is supplied to the aforementioned aeration tubes, and in the solid-liquid separator device, which aerates the aforementioned separation membrane modules from the aforementioned gas outlets, the aforementioned aeration tubes are arranged in horizontal rows. Aeration tube groups, which comprise said multiple aeration tubes arranged in horizontal rows, are arranged so as to be stacked in multiple vertical levels, wherein the aeration tubes on neighboring levels are not vertically aligned. The solid-liquid separator device has a means for switching the supply of air to the different aeration tube groups.

Description

Solid-liquid separator and operation method thereof

The present invention relates to a solid-liquid separation apparatus that performs solid-liquid separation in water treatment and an operation method thereof.
This application claims priority based on Japanese Patent Application No. 2010-125927 filed in Japan on June 1, 2010, the contents of which are incorporated herein by reference.

Conventionally, sand filtration, gravity precipitation, and the like have been performed as methods for solid-liquid separation of water to be treated with high turbidity, such as water purification treatment, sewage treatment, or industrial wastewater treatment. However, solid-liquid separation by these methods has disadvantages that the quality of the treated water obtained may be insufficient, and that a large site is required for solid-liquid separation. Therefore, as a method for solving such inconvenience, various methods for performing solid-liquid separation of water to be treated using a separation membrane module provided with a separation membrane such as a microfiltration membrane and an ultrafiltration membrane have been recently studied. Yes. When water to be treated is filtered using a separation membrane, treated water with high water quality can be obtained.

When solid-liquid separation of water to be treated is performed using a separation membrane, the clogging of pores on the separation membrane surface due to suspended substances progresses as the filtration treatment continues, so the filtration flow rate decreases or the transmembrane pressure difference Rise. Therefore, in order to recover such a state, in a filtration process using a separation membrane, a diffusion tube is usually provided below the membrane module, air is diffused from the diffusion tube, and the separation membrane is swung. The method of peeling off the suspended substance on the surface of the membrane is performed.

However, even in the case of drainage filtration using a membrane module, it is difficult to keep the bubbles discharged from the air diffuser uniformly applied to the separation membrane when the operation is performed over a long period of time. However, there is a problem that frequent maintenance work is required to recover the reduced filtration flow rate because the pores on the membrane surface are blocked and the filtration flow rate is lowered.
In view of this, Patent Document 1 proposes to set the number of gas discharge ports of the diffuser according to the horizontal sectional area of the separation membrane module.

WO99 / 29630 pamphlet

However, when the number of gas discharge ports of the air diffuser is set according to the technique described in Patent Document 1, the number of gas discharge ports may be excessively increased, and the number of air diffuser tubes provided with the number of gas discharge ports increases. The ratio of the diffuser tube to the horizontal cross-sectional area of the separation membrane module becomes large, the flow path between the diffuser tubes must be narrowed, and aeration may become uneven and the separation membrane module may be blocked. There is.

The present invention has been made in view of such circumstances, and even when filtration is performed over a long period of time, there is little blockage of the gas discharge port of the diffuser tube, and as a result, there is little blockage of the pores on the membrane surface due to the suspension, and the stable An object of the present invention is to provide a solid-liquid separator capable of continuing the filtration for a long period of time and an operation method thereof.

As a means for solving the above problems, the present invention includes the following aspects.

[1] In the first aspect of the present invention, separation membrane modules (for example, separation membrane module 11 in the embodiment) in which a plurality of filtration membrane sheets (for example, the filtration membrane sheet 10 in the embodiment) are arranged in parallel are spaced apart. A diffuser tube (for example, a diffuser in the embodiment) having a gas discharge port (for example, the gas discharge port 16 in the embodiment) below the separation membrane module of a plurality of membrane separation devices (for example, the membrane separation device 3 in the embodiment). An air diffuser (for example, the air diffuser 4 in the embodiment) provided with a plurality of air tubes 13) and provided in parallel with each other is provided, gas is supplied to the air diffuser, and the separation membrane is supplied from the gas discharge port. In a solid-liquid separator that diffuses air to a module, a plurality of the diffuser tubes are arranged in a horizontal direction, and the plurality of diffusers arranged in the horizontal direction are arranged. A plurality of air diffusion tube groups (for example, the air

diffusion tube groups

13G and 14G in the embodiment) made of tubes are arranged in a plurality of layers in the vertical direction so that adjacent air diffusion tubes do not line up on the vertical line. It is a solid-liquid separator having means for switching supply air to the air diffusing tube group (for example, an automatic valve such as a valve in the embodiment).

[2] In the solid-liquid separation device according to [1], the air diffusing device includes at least one air diffusing tube group (for example, the air diffusing tube group 13G in the embodiment) of the plurality of air diffusing tube groups, A plurality of air diffusers configured with at least one gas supply pipe header (for example, the gas supply pipe header 12A in the embodiment) that communicates with each of the air diffusion pipes of the air diffusion pipe group on the same plane and supplies gas to each of the air diffusion pipes. By configuring the apparatus and stacking the plurality of diffuser devices in a plurality of stages in the vertical direction, the diffuser tube group is arranged in the vertical direction so that adjacent diffuser pipes do not line up on the vertical line. It is preferable to arrange them in a stacked manner.

[3] In the solid-liquid separator according to [1] or [2], the filtration membrane sheet is preferably a filtration membrane sheet in which a number of hollow fiber membranes are arranged in parallel.

[4] The solid-liquid separator according to [1] to [3] is adjacent when the diffuser tube group arranged in a plurality of stages is viewed from the horizontal direction in the axial direction of the diffuser tube. , The distance between the axes of the diffuser tubes, which is the distance between the axes of the diffuser tubes of the pair of diffuser tubes,
A distance between an axis of one of the pair of air diffuser groups and a straight line obtained by projecting an axis of the other air diffuser onto a horizontal plane including the axis of the one air diffuser;
When the outer diameter of the air diffuser is D,
It is preferable that the air diffuser is disposed so as to satisfy d1 = 1.1 × d2 to 5.0 × d2 and d1> 1.3D.

[5] A second aspect of the present invention is a method for operating a solid-liquid separation device using the solid-liquid separation device according to any one of [1] to [4], wherein the plurality of aeration tubes A step of supplying air to one diffuser tube group, a step of stopping air supply to the diffuser tube group supplied with the air, and another diffuser tube different from the diffuser tube group stopped with the air supply. Supplying air to one of the trachea groups;
The operation method of the solid-liquid separator which repeats every fixed period. It is.

According to the present invention, even when filtration is performed over a long period of time, it is possible to suppress the blockage of the gas discharge port of the diffusing tube, and as a result, it is possible to suppress the blockage of the pores of the membrane surface due to the suspension, and to stabilize Filtration can be continued for a long time.

It is a schematic block diagram of the membrane separation activated sludge processing apparatus which concerns on embodiment of this invention. It is a perspective view of the aeration apparatus in a membrane separation activated sludge processing apparatus. It is a perspective view of the diffuser tube in an air diffuser. It is a perspective view explaining arrangement | positioning of a diffuser tube. It is the figure which looked at the diffuser tube in the horizontal direction (axial direction). It is a figure explaining arrangement | positioning of the diffuser tube of the membrane separation activated sludge processing apparatus which concerns on Example 1 of this invention. It is a figure explaining arrangement | positioning of the diffuser tube of the membrane separation activated sludge processing apparatus which concerns on Example 2 of this invention. It is a figure explaining arrangement | positioning of the diffuser tube of the membrane separation activated sludge processing apparatus which concerns on Example 3 of this invention. It is the figure which showed the driving | operation result of the membrane separation activated sludge processing apparatus which concerns on an Example.

Hereinafter, embodiments of the present invention will be described in detail with reference to the drawings.
FIG. 1 is a schematic configuration diagram of a membrane separation activated sludge treatment apparatus 1 which is a solid-liquid separation apparatus according to an embodiment of the present invention. The membrane separation activated sludge treatment apparatus 1 according to this embodiment includes a membrane separation apparatus 3 provided in a membrane separation tank 2 and an air diffuser 4 for membrane cleaning. A blower 5 is connected to the air diffuser 4, and a suction pump 6 is connected to the membrane separator 3. The membrane separation device 3 performs solid-liquid separation by suction filtration of the water 7 to be treated in the membrane separation tank 2 by the suction pump 6 to obtain treated water. In addition, a pressure gauge 8 is provided between the membrane separation device 3 and the suction pump 6, and during the operation of the membrane separation activated sludge treatment device 1, the transmembrane differential pressure in the membrane separation device 3 is caused by the pressure gauge 8. It has been measured.

The membrane separation device 3 has a plurality of separation membrane modules 11 arranged in parallel (assembled) with a plurality of filtration membrane sheets 10 in which a plurality of hollow fiber membranes 9 which are separation membranes are arranged in parallel. The hollow fiber membrane 9 is formed with a plurality of pores, and the water 7 to be treated passes through the pores, whereby solid-liquid separation is performed. The separation membrane mounted in the separation membrane module 11 is preferably a microfiltration membrane or an ultrafiltration membrane, and a flat membrane, a tubular membrane, a bag-like membrane, etc. may be used in addition to a hollow fiber membrane. A hollow fiber membrane capable of highly integrating the membrane area when compared at the base is preferable. Moreover, as a material of the separation membrane, polyethylene, cellulose, polyolefin, polysulfone, PVDF (polyvinylidene fluoride), PTFE (polytetrafluoroethylene (polytetrafluoroethylene)), ceramics, or the like can be applied.

The pore size of the pores of the separation membrane is not particularly limited, but a pore size of 0.001 to 0.1 μm, generally called an ultrafiltration membrane, or a pore size of 0.1, generally called a microfiltration membrane. Those having a pore size of ˜1 μm or larger can be used, and are selected according to the particle size of the substance to be subjected to solid-liquid separation. For example, if it is used for solid-liquid separation of activated sludge, the thickness is preferably 0.5 μm or less, and if sterilization is required, such as filtration of purified water, it is preferably 0.1 μm or less.

The air diffuser 4 is provided below the membrane separator 3 and includes gas supply pipe headers 12A to 12D, which are tubular bodies having a rectangular cross section in communication with the blower 5 with reference to FIG. 12A and 12B are arranged in parallel at a predetermined interval, and a first air diffuser 20 configured by arranging a plurality of air diffusers 13 between the gas

supply pipe headers

12A and 12B, a gas

supply pipe header

12C, 12D is arranged in parallel with a predetermined interval, and a second air diffuser 21 configured by disposing a plurality of air diffusers 14 between the gas

supply pipe headers

12C and 12D.

The gas supply pipe headers 12A to 12D are provided with air supply ports 15A to 15D to which air supplied from the blower 5 is supplied, respectively. Both ends of the air diffuser 13 are connected to the opposing inner surfaces of the gas

supply pipe headers

12A and 12B, and the inside of the air diffuser 13 communicates with the gas

supply pipe headers

12A and 12B. Both ends of the air diffuser pipe 14 are connected to the opposing inner surfaces of the gas

supply pipe headers

12C and 12D, and the inside of the air diffuser pipe 14 communicates with the gas

supply pipe headers

12C and 12D.

The plurality of air diffusion tubes 13 are arranged in parallel with each other at a predetermined interval in the horizontal direction, and one end portions thereof are respectively connected on the same plane of the gas supply tube header 12A, and the gas supply tube header 12B. The other ends are connected on the same plane. In addition, a plurality of diffuser tubes 14 are arranged in parallel with each other at a predetermined interval in the horizontal direction, and one end portions thereof are connected to the same plane of the gas supply tube header 12C, respectively. The other end is connected to the same plane of 12D.
As described above, the present invention is characterized in that a plurality of diffuser tube groups each composed of a plurality of diffuser tubes 13 arranged on the same horizontal plane are provided. Further, these diffuser tube groups are adjacent to each other. The diffusing tubes are stacked and arranged so as not to line up on the vertical line.
When adjacent diffuser tubes are arranged on the same plane in the vertical direction, the diffuser tubes vibrate as the gas passes through the diffuser tube during operation, etc. There are cases in which they approach each other or make the worst contact, so that a sufficient liquid flow path between the diffuser tubes cannot be secured, and there is a possibility that uniform aeration cannot be performed. On the other hand, it is not necessary to consider this point for non-adjacent diffuser groups. For example, diffuser tubes may be arranged in a staggered pattern when viewed from the side.

In the present embodiment, the first air diffuser 20 is disposed so as to be stacked above the second air diffuser 21, and the plurality of air diffusers arranged in the horizontal direction in the first air diffuser 20. The diffuser tube group 13G composed of 13 is arranged to be stacked above the diffuser tube group 14G composed of a plurality of diffuser tubes 14 arranged in the horizontal direction in the second air diffuser 21. The axial center of the diffusing tube 13 in the diffusing tube group 13G and the axial center of the diffusing tube 14 in the diffusing tube group 14G are spaced apart in the horizontal direction, and the diffusing tube group 13G and the diffusing tube group 14G are viewed from the vertical direction. In some cases, the diffuser tube 14 is positioned so as to be shifted between the adjacent diffuser tubes 13, and the diffuser tube 13 is positioned between the adjacent diffuser tubes 14. In this embodiment, the air diffuser group is arranged in two stages, and the first air diffuser and the second air diffuser are arranged so as to be located in a mountain and a valley. In this case, for example, the positions of the air diffuser groups in the positional relationship between the m-th stage and the n-th stage (mn ≧ 2) may be the same in the vertical direction.

Referring to FIG. 3, a plurality of gas discharge ports 16 and a plurality of gas discharge ports 17 are formed on the uppermost surfaces of the diffusion tube 13 and the diffusion tube 14, and sludge is formed on the lowermost surfaces of the diffusion tube 13 and the diffusion tube 14. A sludge flow discharge hole 18 for inflow and discharge is formed. The position of the sludge flow discharge hole 18 in the longitudinal direction to be opened with respect to the diffuser pipe 13 and the diffuser pipe 14 can be arbitrarily set, but in this embodiment, the gas

supply pipe headers

12A and 12B and gas on both sides are provided. Since air is supplied from the supply pipe headers 12 </ b> C and 12 </ b> D, a sludge flow discharge hole 18 is formed at the center of each of the air diffusion pipes 13 and the air diffusion pipes 14. Further, the number of the sludge flow discharge holes 18 in one aeration pipe is not particularly limited. Further, the sludge flow discharge hole 18 may not be formed in the air diffuser 13 but may be formed only in the air diffuser 14. Further, as the material used for the air diffuser 4, it is easy to manufacture and inexpensive to use a structure in which the

gas discharge ports

16 and 17 are opened in the air diffusion tube 13 and the air diffusion tube 14 made of metal, resin or the like. preferable.

In the first air diffuser 20 and the second air diffuser 21, the air supplied from the blower 5 is first supplied to the air supply ports 15A to 15D, and then sent to the gas supply pipe headers 12A to 12D. The gas is supplied to the air diffuser 13 and the air diffuser 14 and is discharged from the gas outlet 16 and the gas outlet 17. Thereby, the air bubbles continuously or intermittently diffused from the gas discharge port 16 and the gas discharge port 17 of the diffuser 4 reach the membrane separation device 3 through the liquid of the water 7 to be treated, and are further separated. It passes through the vicinity of the membrane surface of the membrane module 11 and is discharged from the water surface.

FIG. 4 shows an enlarged view of the arrangement portion of the diffuser tube 13 and the diffuser tube 14 in the perspective view of the diffuser device, and FIG. 5 shows the arrangement portion of the diffuser tube 13 and the diffuser tube 14 in the perspective view of the diffuser device. The figure seen in the horizontal direction (axial direction) is shown. Here, the arrangement configuration of the air diffuser 13 and the air diffuser 14 in a state where the first air diffuser 20 and the second air diffuser 21 are laminated will be described. Adjacent when the first air diffuser 20 and the second air diffuser 21 (air diffuser tube group 13G and air diffuser tube group 14G) are viewed from the horizontal direction in the axial direction of the air diffusers 13 and 14 (in the direction of arrow H in FIG. 4). The distance between the axes (center distance) between the air diffuser 13 and the air diffuser 14 (first air diffuser axis distance) is d1, the axis of the air diffuser 13 and the axis of the air diffuser 14 are When d2 is the distance from the straight line projected onto the horizontal plane including the axis (sometimes referred to as the distance between the second air diffuser axes, see FIGS. 4 and 6), and D is the outer diameter of the air diffuser 13 and the air diffuser 14. In order to satisfy the relationship of d1 = 1.1 × d2 to 5.0 × d2, d1> 1.3D, 3 and the diffuser 14 are preferably arranged. Further, regarding the relationship between d1 and d2, it is more preferable that d1 = 1.2d2 to 2.5d2.

In addition, the 2nd air diffuser distance is the vertical direction (arrow of FIG. 5) of the 1st air diffuser 20 and the 2nd air diffuser 21 (air diffuser tube group 13G and air diffuser tube group 14G) which are arrange | positioned in multiple steps. It can be paraphrased as the inter-axis (center-to-center) distance between the air diffuser 13 and the air diffuser 14 adjacent when viewed from the (V direction).
Further, in the present invention, d1 and d2 do not have to be the same in all sets of air diffusers, and for example, air diffusers having different air diffuser pitches may be used.
At this time, it is preferable that d1 and d2 satisfy the relationship of d1 = 1.1 × d2 to 5.0 × d2 and d1> 1.3D in all the diffusers.
Further, the “adjacent diffuser tube” in the case of arranging three or more stages of diffusers is provided in the diffuser of the stage adjacent to the diffuser including the diffuser tube when viewed from a certain diffuser tube. Among the diffusing tubes, the diffusing tubes that are adjacent when viewed from the horizontal direction, that is, d2 is the smallest.
When d1 = 1.1d2 or less, there is no gap between adjacent diffuser tubes, the flow path between the diffuser tubes becomes narrow, and uniform aeration cannot be performed. On the other hand, when d1 is larger than 5.0d2, a gap between adjacent diffuser tubes becomes large, and uniform aeration cannot be performed. Further, when d1 <1.3D, the gap between the diffuser tubes becomes small, the flow path flowing between the diffuser tubes becomes narrow, and uniform aeration cannot be performed.

The outer diameters of the tubes used for the diffuser tube 13 and the diffuser tube 14 are preferably 5 <D <100 mm, and 20 <D <50 mm in consideration of the element clearance arranged at the top of the diffuser 4. Is more preferable. 2 or 3 again, the hole diameter of the gas discharge port 16 and the gas discharge port 17 in the diffuser tube 13 and the diffuser tube 14 is preferably 1 to 15 mm, considering the viewpoint of uniform aeration and hole blockage. In this case, the thickness is more preferably 4 to 6 mm.

Further, the hole pitch of the adjacent gas discharge ports 16 and the hole pitch of the adjacent gas discharge ports 17 are preferably 10 to 500 mm, and more preferably 50 to 200 mm in view of uniform aeration. . Further, the shape of the sludge flow discharge hole 18 in the air diffuser 13 and the air diffuser 14 can be arbitrarily set, such as a round hole or a long hole. When the diameters of the trachea 13 and the diffuser 14 are D, the hole diameter is 0.1D to 0.9D, and when sludge inflow and discharge are taken into account, 0.4D to 0. 6D is more preferable.

Next, an operation method of the membrane separation activated sludge treatment apparatus 1 according to this embodiment configured as described above will be described.

First, in order to supply oxygen necessary for biodegradation of pollutants such as organic substances present in the water to be treated 7 supplied to the membrane separation tank 2, oxygen is treated from the air diffuser 4 connected to the blower 5. Supply to water 7. Next, the water to be treated 7 is solid-liquid separated into permeated water that permeates the hollow fiber membrane 9 mounted on the membrane separation device 3 and activated sludge that does not permeate by operating the suction pump 6. Here, the permeation flow rate (LV) of the membrane separation device 3 is preferably 0.01 to 1.5 m ³ / m ² · day in the membrane separation activated sludge treatment. This permeation flow rate is an index indicating the permeation flow rate per day and per m ² (m ³ / m ² · day).

At this time, in the air diffuser 4, the air is supplied to one of the first air diffuser 20 and the second air diffuser 21, and the air diffuser supplied with air after a predetermined time has passed. Then, oxygen is supplied to the water to be treated 7 by repeating the step of supplying air to another air diffuser different from the air diffuser that stopped the air supply at regular intervals. That is, in the air diffuser 4, the air diffuser group 13G and the air diffuser group 14G are operated alternately.

Here, the bubbles due to oxygen from the diffuser 4 move upward to the water surface through the water 7 to be treated, so that an upward gas-liquid mixed flow composed of the water 7 to be treated and bubbles is generated. Thereby, in the membrane separation activated sludge treatment apparatus 1, the gas-liquid mixed flow is prevented from adhering to the membrane surface of the solid content by scrubbing the membrane surface of the separation membrane module 11, and the membrane surface is rapidly clogged. Can be prevented.
Then, as described above, the first air diffuser 20 and the second air diffuser 21 are operated alternately, and the first air diffuser 20 and the second air diffuser 21 are continuously operated from different positions. By performing a good aeration, it is possible to supply oxygen uniformly to the separation membrane module 11 with a high density.
The aeration condition of the aeration device 4 is preferably aeration in the range of 50 to 300 m ³ / m ² / hr at the aeration linear velocity. This aeration linear velocity is an index indicating the amount of air (m ³ / hr.) Diffused per 1 m ² of the membrane separation device projection area of the amount of air diffused from the diffuser 4. In addition, in this embodiment, although the 1st air diffuser 20 and the 2nd air diffuser 21 operate | move alternately, you may operate both and may supply oxygen.

Further, the MLSS (biological reaction tank suspended solids) concentration of the water to be treated 7 in the membrane separation tank 2 is preferably set to 3000 to 15000 mg / L. MLSS concentration is an alternative indicator of microbial concentration. By setting the MLSS concentration to 3000 mg / L or more, the biodegradation of microorganisms proceeds sufficiently, and the effect of suppressing the progress of membrane fouling by undegraded organic substances is enhanced. Moreover, the effect which suppresses the membrane fouling resulting from the viscosity raise of the to-be-processed water 7 becomes high by making MLSS density | concentration into 15000 mg / L or less. The MLSS concentration is more preferably 7000 to 12000 mg / L.

As described above, in this embodiment, the membrane separation device 3 and the air diffuser 4 connected to the blower 5 are provided in the membrane separation tank 2, and the membrane separation device 3 sucks and filters the water 7 to be treated by the suction pump 6. Thus, the water 7 to be treated is subjected to solid-liquid separation. At this time, the transmembrane pressure difference is measured by the pressure gauge 8 installed between the membrane separation device 3 and the suction pump 6, and the value of the pressure gauge 8 is monitored. Thus, the operation management of the membrane separation device 3 is possible.
In the present embodiment, the first air diffuser 20 and the second air diffuser 21 are stacked in two stages, that is, the air diffuser group 13G and the air diffuser group 14G are stacked in two stages and adjacent to each other. It arrange | positions so that the diffuser pipes (13, 14) of the stage to line up may not line up on a perpendicular line. That is, it arrange | positions so that the gas jet nozzle in the diffuser pipe | tube of an adjacent diffuser may not overlap, when it sees from a perpendicular direction. According to this, the number of the

gas discharge ports

16 and 17 is prevented while preventing the number of the

diffusion tubes

13 and 14 from being excessively increased in the diffusion tube group 13G and the diffusion tube group 14G and reducing the diameter of the

diffusion tubes

13 and 14. As a result, the non-uniformity of aeration can be eliminated, and even if filtration is performed over a long period of time, the gas outlet of the air diffuser can be kept from clogging. Therefore, stable filtration can be continued for a long time.

In the above-described embodiment, the mode in which the first air diffuser 20 and the second air diffuser 21 are stacked and arranged in two stages has been described. There may be. As a method of operating the air diffuser in this case, air is supplied to one of the air diffusers, and the air supply to the air diffuser that has supplied air after a predetermined time has elapsed is stopped. Thereafter, the step of supplying air to one of the other air diffusers different from the air diffuser that has stopped supplying air can be repeated at regular intervals. Thus, by using a plurality of diffusers one by one, oxygen can be uniformly supplied to the separation membrane module 11 with high density.

Moreover, in the said embodiment, the diffuser tube group 13G is provided in the 1st diffuser 20, and the diffuser tube group 14G is provided in the 2nd diffuser 21, and the diffuser tube group 13G and the diffuser tube group 14G are laminated | stacked and arrange | positioned. However, a plurality of air diffuser groups are stacked in a single air diffuser in a plurality of stages in the vertical direction so that adjacent air diffuser tubes are not aligned on the vertical line, for example, a staggered arrangement Good. In other words, on the same plane of the gas supply pipe header, a plurality of diffuser tubes are arranged side by side in the horizontal direction, and a plurality of diffuser tube groups composed of the plurality of diffuser tubes arranged in the horizontal direction are arranged in a plurality of stages in the vertical direction. The gas supply pipe header may be arranged so as to supply gas to each air diffuser through a single air supply port of the gas supply pipe header. In this case, in addition to providing a partition inside, a means for switching the flow path of the gas supplied into the gas supply pipe header such as a valve is provided, so that the air is diffused by a group of diffused pipes stacked vertically. You may make it comprise so that change is possible.

In the above-described embodiment, a plurality of air diffusers 13 are disposed between the gas

supply pipe headers

12A and 12B, and a plurality of air diffusers 14 are disposed between the gas

supply pipe headers

12C and 12D. Although the aspect which comprises the 2nd air diffuser 21 was demonstrated, it is the aspect which provides a gas supply pipe header only in the one side of the air diffuser 13 and the air diffuser 14 of the 1st air diffuser 20 and the 2nd air diffuser 21. It doesn't matter.

Examples of the present invention will be described below.
<Example 1>
In Example 1, specific dimensions were set in the membrane separation activated sludge treatment apparatus 1 described above, and operation was performed under predetermined conditions.

A hollow fiber membrane module as a separation membrane module 11 (trade name: SADF membrane, manufactured by Mitsubishi Rayon Co., Ltd .: hollow fiber) in which a polyethylene hollow fiber membrane for microfiltration with an average pore size of 0.1 μm is developed and fixed as a separation membrane in a screen shape. The module length in the fiber axis direction of the membrane is 125 cm; the membrane area is 25 m 2, and the 11 modules are arranged in the horizontal direction so that the center distance between adjacent modules is 4.5 cm, and the length is 130 cm, the width is 75 cm, and the height is 210 cm. The membrane separation device 3 placed in a frame was immersed in the water 7 to be treated.

In the air diffuser 4 disposed below the membrane separator 3, four gas supply pipe headers 12A to 12D having four air supply ports 15A to 15D are prepared, and the gas

supply pipe headers

12A and 12B are respectively provided. The first air diffuser 20 is formed by branching and providing six air diffuser tubes 13 installed on the same plane of the gas

supply pipe headers

12A and 12B (in addition, a plurality of gas diffuser tubes arranged in the horizontal direction are arranged in six lines). A diffuser tube group 13G is constituted by the diffuser tube 13). Moreover, the 2nd air diffuser 21 was comprised by branching from each of the gas

supply pipe headers

12C and 12D, and providing the six air diffusion pipes 14 installed on the same plane of the gas

supply pipe headers

12C and 12D. A diffuser tube group 14G is composed of six diffuser tubes 14 arranged side by side in the horizontal direction).
The diameters of the air supply ports 15A to 15D were 32 mm, and air was supplied evenly to the gas supply pipe headers 12A to 12D, respectively. As the gas supply pipe headers 12A to 12D, square pipes having an outer diameter of 50 mm were used, and the gas supply pipe headers facing each other were connected by a diffuser pipe.

Then, referring to FIG. 6, the first diffuser between the

adjacent diffuser tubes

13 and 14 when viewed from the horizontal direction when the first diffuser 20 and the second diffuser 21 are stacked and installed. The distance d1 between the trachea axes is set to 4.8 cm, and when the first air diffuser 20 and the second air diffuser 21 are stacked and installed, the air diffuser 13 and the air diffuser 14 adjacent to each other when viewed from the vertical direction are set. The distance between the second air diffuser tubes is set to 2.7 cm, and the air diffuser 13 and the air diffuser 14 are made of stainless steel having an outer diameter of 2.7 cm, an inner diameter of 2.4 cm, and a length of 114.5 cm. Twelve pipes were used and arranged so that the longitudinal direction thereof was parallel to the longitudinal direction of the hollow fiber membrane. The diffuser pipe 13 and the diffuser pipe 14 each have 22 circular

gas discharge ports

16 and 17 each having a diameter of 0.4 cm on the uppermost surface and an interval of 5 cm between the discharge ports, and a sludge flow discharge hole 18 on the lowermost surface. As described above, one elongated hole having a width of 1.5 cm and a length of 5 cm was provided in the central portion.

At this time, d1 = 1.78D between the outer diameter D of the air diffuser 13 and the air diffuser 14, the distance d1 between the first air diffuser axes, and the distance d2 between the second air diffuser axes, and d1> 1 .3D, d1 = 1.78d2, and d1 = 1.1 × d2 to 5.0 × d2.

As the aeration conditions, the blower 5 was used to supply the aeration tube 13 and the aeration tube 14 at 140 L / min and aeration linear velocity of 150 m ³ / m ² / hr. Filtration conditions were as follows: activated sludge having an MLSS concentration of 8000 to 12000 mg / L, using a suction pump 6 at a membrane permeation flow rate LV = 0.8 m ³ / m ² / d, and filtration time / stop time = 7 minutes / 1. The filtration process was continued for one month with intermittent operation for 1 minute. And the continuous operation was performed for one month, measuring the transmembrane differential pressure at the time of suction filtration with the pressure gauge 8 installed between the membrane separator 3 and the suction pump 6.

FIG. 9 shows the operation results of the membrane separation activated sludge treatment apparatus 1 according to Example 1. The diamond-shaped plots in the figure show the operation results of Example 1. As is clear from the figure, in the membrane separation activated sludge treatment apparatus 1 according to Example 1, no increase in transmembrane pressure difference was observed, and stable operation was possible while maintaining the initial differential pressure of 6 kPa. Further, when the membrane separation device 3 was pulled up and visually confirmed, the separation membrane mounted on the membrane separation device 3 was maintained at the initial level without adhesion of sludge.

<Example 2>
Next, in Example 2, the dimension setting of each part is changed from Example 1 above, and the membrane separation device 3 is immersed in activated sludge under the same conditions as in Example 1 for the aeration condition and filtration condition, and the suction pump 6 was used for driving. The separation membrane module 11 used in the membrane separation device 3 was the same as that used in Example 1.

In the air diffuser 4, four gas supply pipe headers 12A to 12D having four air supply ports 15A to 15D are prepared and branched from the gas

supply pipe headers

12A and 12B, respectively. The first diffuser 20 is configured by providing six diffuser tubes 13 installed on the same plane of 12B (in addition, the diffuser tube group 13G is composed of six diffuser tubes 13 arranged side by side in the horizontal direction. Configured). Moreover, the 2nd air diffuser 21 was comprised by branching from each of the gas

supply pipe headers

Referring to FIG. 7, the first diffuser tube axis between the

diffuser tubes

13 and 14 adjacent to each other when viewed from the horizontal direction when the first diffuser device 20 and the second diffuser device 21 are stacked and installed. When the distance d1 is set to 11 cm and the first air diffuser 20 and the second air diffuser 21 are stacked and installed, the second distance between the adjacent air diffuser 13 and the air diffuser 14 seen from the vertical direction is shown. The distance d2 between the diffuser tubes is set to 4.5 cm, and the diffuser tube 13 and diffuser tube 14 are 12 stainless steel pipes having an outer diameter of 2.7 cm, an inner diameter of 2.4 cm, and a length of 114.5 cm. They were used so that their longitudinal directions were parallel to the longitudinal direction of the hollow fiber membrane. The diffuser pipe 13 and the diffuser pipe 14 each have 22 circular

gas discharge ports

At this time, between the outer diameter D of the diffusion tube 13 and the diffusion tube 14, the distance d1 between the diffusion tube axes, and the distance d2 between the diffusion tube axes, d1 = 4.07D, and d1> 1.3D is satisfied. D1 = 2.44d2 and d1 = 1.1 × d2 to 5.0 × d2.

FIG. 9 shows the operation results of the membrane separation activated sludge treatment apparatus 1 according to Example 2. The plots with square marks in the figure show the operation results of Example 2. As is clear from the figure, in the membrane separation activated sludge treatment apparatus 1 according to Example 2, no increase in transmembrane pressure difference was observed, and stable operation was possible while maintaining the initial pressure difference of 6 kPa. Further, when the membrane separation device 3 was pulled up and visually confirmed, the separation membrane mounted on the membrane separation device 3 was maintained at the initial level without adhesion of sludge.

<Example 3>
Next, in Example 3, the dimension setting of each part was changed from the said Example 1, the membrane separation apparatus 3 was immersed in activated sludge on the conditions similar to Example 1 for aeration conditions and filtration conditions, and a suction pump was used. Used to drive.

supply pipe headers

Referring to FIG. 7, the first diffuser tube axis between the

diffuser tubes

13 and 14 adjacent to each other when viewed from the horizontal direction when the first diffuser device 20 and the second diffuser device 21 are stacked and installed. When the tube distance d1 is set to 5.1 cm and the first air diffuser 20 and the second air diffuser 21 are stacked and installed, the distance between the adjacent air diffuser 13 and the air diffuser 14 seen from the vertical direction is set. The distance d2 between the second air diffuser tubes is set to 1.2 cm. As the air diffuser 13 and the air diffuser 14, the stainless steel pipe 12 having an outer diameter of 2.7 cm, an inner diameter of 2.4 cm, and a length of 114.5 cm is used. The books were used and arranged so that the longitudinal direction thereof was parallel to the longitudinal direction of the hollow fiber membrane. The diffuser pipe 13 and the diffuser pipe 14 each have 22 circular

gas discharge ports

At this time, between the outer diameter D of the diffusion tube 13 and the diffusion tube 14, the distance d1 between the diffusion tube axes, and the distance d2 between the diffusion tube axes, d1 = 1.89D, and d1> 1.3D is satisfied. D1 = 4.25d2 and d1 = 1.1 × d2 to 5.0 × d2.

The operation result of the membrane separation activated sludge treatment apparatus 1 according to Example 3 is shown in FIG. The triangle marks in the figure show the operation results of Example 3. As is clear from the figure, in the membrane separation activated sludge treatment apparatus 1 according to Example 3, a slight increase in the transmembrane pressure difference was observed, and after 30 days, a 3 kPa increase was observed from the initial pressure difference. Stable operation was possible. Further, when the membrane separation device 3 was pulled up and visually confirmed, the separation membrane mounted on the membrane separation device 3 did not adhere to sludge and maintained the initial level.

<Example 4>
Next, in Example 4, the dimension setting of each part was changed from Example 1 above, and the membrane separation device 3 was immersed in activated sludge under the same conditions as in Example 1 for the aeration condition and filtration condition, and the suction pump 6 Driving was performed using.

The air diffuser 4 is arranged below the membrane separation device 3, and four gas supply pipe headers 12A to 12D having four air supply ports 15A to 15D are prepared and branched from the gas

supply pipe headers

12A and 12B, respectively. Thus, the six air diffusers 13 installed on the same plane of the gas

supply pipe headers

12A and 12B are provided to form the first air diffuser 20 (note that a plurality of diffusers arranged in the horizontal direction are arranged in parallel. The trachea 13 constitutes a diffuser tube group 13G). Moreover, the 2nd air diffuser 21 was comprised by branching from each of the gas

supply pipe headers

And with reference to FIG. 8, when the 1st air diffuser 20 and the 2nd air diffuser 21 are laminated | stacked and installed, the air diffuser 13 and the 2nd air diffuser of the 1st air diffuser 20 which adjoins seeing from the horizontal direction. The vertical distance when the first air diffuser axis distance d1 between the air diffuser 14 and the air diffuser 14 is set to 3.8 cm and the first air diffuser 20 and the second air diffuser 21 are stacked and installed. The distance d2 between the second air diffuser axes between the air diffuser 13 of the first air diffuser 20 and the air diffuser 14 adjacent to the second air diffuser 21 is set to be 2.7 cm. As the trachea, twelve stainless steel pipes having an outer diameter of 3.0 cm, an inner diameter of 2.4 cm, and a length of 114.5 cm were used and arranged such that the longitudinal direction thereof was parallel to the longitudinal direction of the hollow fiber membrane. Each air diffuser has 22 circular gas outlets with a diameter of φ0.4 cm on the uppermost surface, the interval between the outlets is 5 cm, and the lowermost surface is a sludge flow discharge hole 18 with a width of 1.5 cm and a length of 5 cm. One long hole was provided at the center.

At this time, d1 = 1.27D and d1> 1.3D are satisfied between the outer diameter D of the air diffuser, the first air diffuser axis distance d1, and the second air diffuser axis distance d2. Not. On the other hand, d1 = 1.41d2, and d1 = 1.1 × d2 to 5.0 × d2 is satisfied. A pressure gauge was installed between the membrane separator and the suction pump, and continuous operation was performed for one month while measuring the transmembrane pressure difference during suction filtration.

FIG. 9 shows the operation result of the membrane separation activated sludge treatment apparatus according to Example 4. The x-marked plot in the figure shows the operation result of Example 4. As is clear from the figure, in the membrane separation activated sludge treatment apparatus according to Example 3, the transmembrane pressure difference gradually increased from the past 20 days, and after 30 days, the pressure difference increased by 30 kPa from the initial pressure difference. Observed. Further, when the membrane separator was pulled up and visually confirmed, some sludge was observed on the separation membrane mounted on the membrane separator.

In the operation results and observation results of Examples 1 to 4 described above, it was confirmed that the increase in the transmembrane pressure difference was suppressed over a relatively long period for Example 3, but Examples 1 and 2 and 3 confirmed that it was possible to suppress the increase in the transmembrane pressure difference over a longer period than in Example 4.
From this result, when the first air diffuser 20 and the second air diffuser 21 arranged in a plurality of stages are viewed from the horizontal direction in the axial direction of the

air diffusers

13 and 14, The inter-axis distance between the diffuser tube 14 (first diffuser tube distance) is d1, the axis of one of the pair of diffuser tubes and the axis of the other diffuser tube are the one diffuser tube. D1 = 1.1 × d2-5. Where d2 is the distance from the straight line projected onto the horizontal plane including the axis of (diffusion tube distance) d2 and the outer diameters of the diffusion tube 13 and the diffusion tube 14 are D. It was confirmed that stable filtration can be continued for a longer period when the diffuser 13 and the diffuser 14 are arranged so as to satisfy the relationship of 0 × d2, d1> 1.3D.

The solid-liquid separation device of the present invention has less obstruction of the gas discharge port of the air diffuser even after long-term filtration. Since it can be continued, it is useful, for example, as a membrane separation activated sludge treatment apparatus.

1 Membrane separation activated sludge treatment equipment (solid-liquid separation equipment)
DESCRIPTION OF SYMBOLS 3 Membrane separator 4 Air diffuser 9 Hollow fiber membrane 10 Filtration membrane sheet 11 Separation membrane module 12 Gas

supply pipe header

13, 14

Air diffuser

13G, 14G

Air diffuser group

16, 17 Gas outlet 20 First air diffuser (diffuse Qi device)
21 2nd air diffuser (air diffuser)

Claims

A plurality of diffusion tubes having gas discharge ports are provided below the separation membrane module of the membrane separation device in which a plurality of separation membrane modules in which a plurality of filtration membrane sheets are arranged in parallel are arranged at intervals. In a solid-liquid separation device that provides an air diffuser provided in parallel with each other, supplies gas to the air diffuser, and diffuses air from the gas discharge port to the separation membrane module,
A plurality of the diffuser tubes are arranged side by side in the horizontal direction, a plurality of diffuser tube groups composed of a plurality of diffuser tubes arranged in the horizontal direction are arranged in a plurality of levels in the vertical direction, and the diffuser tubes in adjacent stages are arranged on the vertical line. A solid-liquid separation device having means arranged so as to be stacked so as to switch the air supply to each of the diffuser tube groups.
The air diffuser is connected to at least one air diffuser group of the plurality of air diffuser tube groups and the air diffuser tubes of the air diffuser tube group on the same plane, and supplies at least one gas to each air diffuser tube. Consists of a plurality of air diffusers composed of a gas supply pipe header,
By arranging the plurality of air diffusers in a plurality of stages in the vertical direction, the air diffuser groups are arranged in a vertical direction so that adjacent stages of the air diffusers do not line up on the vertical line. The solid-liquid separator according to claim 1.
The solid-liquid separation device according to claim 1 or 2, wherein the filtration membrane sheet is a filtration membrane sheet in which a large number of hollow fiber membranes are arranged in parallel.
When the diffuser tube group arranged in a plurality of stages is viewed from the horizontal direction in the axial direction of the diffuser tube, the adjacent distance between the diffuser tubes is the interaxial distance between the diffuser tubes of the pair of diffuser tube groups D1,
A distance between an axis of one of the pair of air diffuser groups and a straight line obtained by projecting an axis of the other air diffuser onto a horizontal plane including the axis of the one air diffuser;
When the outer diameter of the air diffuser is D,
4. The air diffuser according to claim 1, wherein the air diffuser is arranged so as to satisfy d1 = 1.1 × d2 to 5.0 × d2 and satisfy d1> 1.3D. Solid-liquid separator.
A method for operating a solid-liquid separator using the solid-liquid separator according to any one of claims 1 to 4,
Supplying air to one of the plurality of air diffuser groups;
Stopping air supply to the group of air diffusers that supplied the air;
Supplying air to one of the other diffusing tube groups different from the diffusing tube group that has stopped the air supply;
The operation method of the solid-liquid separator which repeats every fixed period.