WO2003051496A1

WO2003051496A1 - Rotary film separator and method for separation of film by rotary film separator

Info

Publication number: WO2003051496A1
Application number: PCT/JP2002/007527
Authority: WO
Inventors: Katsuyoshi Tanida; Yoshiya Kuide; Ryu Harada; Kazutaka Takada
Original assignee: Kobelco Eco-Solutions Co., Ltd.
Priority date: 2001-12-18
Filing date: 2002-07-25
Publication date: 2003-06-26
Also published as: TW550113B

Abstract

A rotary film separator, wherein a hollow rotating shaft (3) is disposed in a cylindrical container having a processed fluid supply inlet (1) so as to pass through the center part thereof, a large number of film bodies formed of plates having transmission films on both surfaces thereof are installed on the rotating shaft (3), the fluid transmitted through the transmission films is discharged from outlets (5) and (6), rectangular baffles (13) are disposed on both sides of the film bodies through clearances therebetween, a motor to rotate the film bodies together with the rotating shaft (3) is installed on the outside of the container, and a fluid flow passage (16) connected to the processed fluid supply inlet (1) is provided on the inner wall surface of the container.

Description

Description Rotary membrane separator and membrane separation method using rotary membrane separator [Technical field]

The present invention provides solid-liquid separation, ion removal, soluble organic matter removal, latex concentration, colloidal silica concentration, valuable resource recovery, waste liquid treatment, metal classification, tap water filtration, activated sludge treatment, tap water sludge treatment, food waste liquid The present invention relates to a rotary membrane separation apparatus and a membrane separation method using a rotary membrane separation apparatus that can be suitably used for processing, COD reduction, BOD reduction, slurry and colloid component filtration, and the like.

(Background technology)

A membrane separation device is used to separate liquids (substances to be treated) in which various substances are dissolved in water into clean water (permeate) and concentrated liquids with high particle concentrations. There are various types of membrane separation devices. For example, membrane separation by a cross-flow method is widely performed. As shown in FIG. 44, this cross-flow method is to pump the liquid to be treated by a supply pump 52 to a membrane module 51 having a function of separating a permeate and a concentrate, and The solution is removed from the membrane module 51 via the route 53, the concentrate is removed from the membrane module 51 via the route 54, and the concentrate is returned to the membrane module 51 via the route 55. In this method, 4 and 5 5 are circulated many times to increase the enrichment. However, in order to perform high concentration by the cross-flow method, it is necessary to circulate the liquid to be treated at a high flow rate in the supply pump 52 because the concentration polarization, the filling, and the blockage of the flow path are reduced. There is Therefore, a large supply pump is required, and the energy required for the pump increases. Moreover, although the energy of the pump is necessary, it is difficult to reduce the fermentation / concentration polarization due to the influence of the velocity boundary layer formed near the membrane surface, and as a result, high concentration cannot be achieved. In addition, even if the liquid to be treated is circulated at a high flow rate, the number of circulations must be increased in order to concentrate to a certain concentration or more because the permeation flow rate is small. The frequency of shearing of the treatment liquid on the pump blades may increase, and the treatment liquid may be altered.

It is also known to separate the liquid to be treated into clean water and concentrated liquid using an evaporating concentrator or a centrifugal separator. However, these methods require a large amount of energy to separate the liquid, The disadvantage is that separation is difficult and water cleanliness is low.

Therefore, a rotary membrane separator has been provided as a membrane separator that is not easily clogged, has a high permeation flux, and can be concentrated to a high concentration. Generally, in this rotary type membrane separation apparatus, a rotating shaft is arranged so as to penetrate the center of a container, and a number of membranes are mounted in a longitudinal direction of the rotating shaft. This is a method that performs membrane separation while rotating. The membrane has a porous structure with pores formed on the surface that prevent the passage of particles of a certain size or more, and a permeable membrane that has a path for transporting the permeated liquid is attached to both sides of the plate. With this structure, only a very fine substance in the liquid to be treated put into the container passes through the pores of the membrane, so that a permeated liquid can be obtained. In this case, the rotating shaft is rotated and mounted on the rotating shaft in order to prevent fouling in which particles of a certain size or more in the liquid to be treated block the pores of the film or adhere or deposit particles on the film surface. Rotating the attached film body is performed. However, just by rotating, the liquid to be treated co-rotates with the film body, and the rotation effect of the film body is reduced. As it is not fully exhibited, prevention of membrane pore blockage is insufficient. Therefore, as a means to more effectively prevent clogging of the membrane pores, turbulence is generated on the membrane surface to prevent co-rotation and to efficiently exchange the liquid to be treated on the membrane surface. Has been proposed. Also, by generating turbulence, concentration polarization can be reduced, thereby enabling high concentration. In addition, the performance of inhibiting the film can be improved.

For example, as shown in FIG. 45 (b), a hollow rotary shaft 63 is provided so as to penetrate the center of a cylindrical container 62 having a supply inlet 61 for a pressurized liquid to be treated. A number of membranes 64 having a structure capable of transferring the permeated liquid are mounted on the rotating shaft 63, and the liquid permeated by the membrane 64 is transferred from the membrane 64 to the rotating shaft 63. After passing through the hollow rotary shaft 63 through the small holes provided in the holes, the liquid is discharged from the outlets 65, 66, and the concentrated liquid is discharged from the outlet 67, and on both sides of the film 64, the film 64 There is known a rotary membrane separation apparatus having a structure in which a ring-shaped baffle 68 that covers almost the entire surface is fixed to a container 62 with a gap provided between the membrane body 64 and the baffle 68 (hereinafter referred to as “conventional”). Membrane separation device 1 ”). The same type as the conventional membrane separation device 1 is disclosed, for example, in Japanese Patent Application Laid-Open No. Hei 6-277645.

According to the conventional membrane separation apparatus 1, when the membrane 64 is rotated together with the rotating shaft 63 by a motor (not shown), the rotation between the surface of the rotating membrane 64 and the stationary ring-shaped baffle 68 is performed. A turbulent flow can be positively generated in the gap, and the effect of preventing pore clogging can be expected. However, the ring-shaped baffle 68 completely separates the membranes, the baffle 68 has a large area covering the membrane 64, and the liquid to be treated in the container 62 passes through the narrow and long flow path 69. As a result, the pressure loss increases, and it cannot be efficiently transmitted. Further, due to the pressure loss, the pressure applied to the membrane 64 becomes non-uniform. The deflection of the film body 64 increases, and the film body 64 and the ring-shaped baffle 6-8 come into contact with each other, and the relatively weak film body 64 may be damaged. Furthermore, when charging the container 62, it is necessary to alternately assemble the membrane body 64 and the ring-shaped baffle 68, which makes the assembly of the apparatus extremely complicated.

Therefore, as shown in FIG. 46 (a), a holed baffle 71 having a hole 70 formed in the periphery of a ring-shaped baffle has been proposed in order to reduce the pressure loss (hereinafter, referred to as “baffle”). “Conventional membrane separation device 2”). However, the conventional membrane separation device 2 requires a high processing cost for perforating the baffle, and, like the conventional membrane separation device 1, requires a membrane 64 and a hole when charged into the container 62. It is necessary to assemble the baffles 71 alternately, and there is a disadvantage that the device assembly is very complicated.

Further, in both of the conventional membrane separation devices 1 and 2, the baffles 68 and 71 uniformly cover the membrane surface, so that there is a disadvantage that the turbulence of the liquid to be treated is small.

Furthermore, with the conventional rotary membrane separators 1 and 2, the appropriate membrane separation conditions and equipment specifications that can effectively exhibit membrane separation performance are not clear, and economical and efficient operation of the membrane separator is guaranteed. Had not been.

SUMMARY OF THE INVENTION The present invention has been made in view of the above-mentioned problems of the prior art, and has as its object to reduce the time and labor required for assembling the device, to reduce the pressure loss, and to improve the efficiency. It is an object of the present invention to provide a rotary membrane separation apparatus and a membrane separation method using the rotary membrane separation apparatus, which can perform a permeation treatment on the membrane to effectively exhibit membrane separation performance.

[Disclosure of the Invention] In order to achieve the above object, the present invention provides a plurality of rectangular baffles provided with gaps on both sides of a membrane mounted on a rotating shaft of a rotary membrane separator, with a gap between the membrane and the membrane. Since a plurality of rectangular baffles are arranged parallel to each other from the vicinity of one inner wall of the container to the vicinity of the other inner wall of the container with the rotation axis interposed, the puffing covers the membrane surface unevenly, The turbulence is large, the concentration polarization and the effect of reducing fouling are large, so the permeation flux is extremely large, the pressure loss due to the presence of the baffle is small, and no special processing is required because the paffle has a simple shape. The baffle can be inserted after the membrane is mounted on the rotating shaft, making assembly of the device simple.

That is, the present invention relates to a rotary membrane separation device having a rotary shaft arranged so as to penetrate a container having a supply inlet for a liquid to be treated, wherein the liquid permeated in the container can be transferred. A membrane having a structure is mounted on the rotating shaft, has an outlet connected to the membrane to discharge the permeated liquid, and a plurality of rectangles provided with gaps between the membrane and the membrane on both sides of the membrane. Liquid baffle is provided, and a liquid flow path connected to the supply inlet of the liquid to be treated is provided on the inner wall surface of the container. It is characterized by being arranged parallel to each other up to the vicinity of the inner wall.

According to the membrane separation device of the present invention configured as described above, as shown in FIG. 7, when the membrane body 12 is rotated clockwise as shown by arrow A, the supply from the supply inlet into the container proceeds. On the left side of the rectangular baffle 13, the supplied and pressurized liquid to be treated flows from the flow path 16 along the inner wall 15 of the container along the rectangular paffle 13 as shown by an arrow B on the left side of the container. On the other hand, on the right side of the rectangular baffle 13, as shown by the arrow C, the liquid to be treated on the surface of the membrane body 12 is in the container. The liquid is discharged toward the flow path 16 along the wall 15. Due to the flow of the liquid to be treated formed between the surface of the membrane and the flow path along the inner wall of the container, the liquid to be treated does not stagnate on the surface of the membrane, and the liquid flowing outward in the container and The exchange of the liquid flowing to the side is performed smoothly. In addition, since the liquid to be treated generates turbulence due to a baffle which is unevenly mounted, fouling and concentration polarization are reduced, and membrane separation can be performed efficiently.

Hereinafter, features and advantageous effects of the rotary membrane separation apparatus and the membrane separation method using the rotary membrane separation apparatus of the present invention will be described. (1) Baffle support and fixation

If both ends of the baffle are supported and fixed by a support independent of the container wall, assembly of the device becomes easy and cost can be reduced.

(2) Baffle shape

① Hook-shaped baffle, S-shaped baffle, and arc-shaped baffle A hook-shaped baffle is provided with a gap between the membrane on both sides of the membrane, and a plurality of hook-shaped baffles are sandwiched across the rotating shaft. It can also be arranged symmetrically with respect to the body diameter or symmetrically with respect to the axis of rotation. It is also possible to arrange an S-shaped paffle with a gap between the membrane and the membrane on both sides of the membrane, and to arrange a plurality of S-shaped paffles point-symmetrically with respect to the rotation axis with the rotation axis interposed therebetween. it can. In addition, an arc-shaped baffle is arranged on both sides of the membrane with a gap between the membrane and the arc-shaped baffle, and a plurality of arc-shaped baffles are arranged symmetrically with respect to the membrane diameter with the rotation axis interposed therebetween, or It can also be arranged point-symmetrically with respect to. The same effect as a rectangular baffle can be expected by using a hook-shaped baffle, S-shaped baffle, or arc-shaped baffle. In addition, hook-shaped, S-shaped or arc-shaped baffles can increase turbulence on the membrane surface. There is an effect that the membrane separation performance is improved. It also has the effect of promoting the exchange of fluid between the membranes.

② Radial baffle

If the baffle covers the membrane surface unevenly, the turbulence is large, and the concentration polarization and the effect of reducing fouling are large, so that the permeation flux is large and the pressure loss due to the presence of the baffle is small. For example, if a baffle having a configuration in which a plurality of baffles are arranged radially around the rotation axis toward the inner wall of the container (radial paffle) is used, the transmitted flux becomes large.

(3) Projected area of paffle against surface area of membrane

① In case of rectangular baffle, hook-shaped baffle, S-shaped baffle and arc-shaped baffle

In the case of a rectangular baffle, a hook-shaped baffle, an S-shaped baffle or an arc-shaped baffle, the projected area of the baffle with respect to the surface area of the membrane is preferably 1 to 90%. If it is less than 1%, the effect of promoting turbulence on the surface of the membrane is small, and if it exceeds 90%, the pressure loss of the liquid to be treated becomes too large. In addition, as shown in an example described later (see FIG. 22), even when the projected area of the baffle with respect to the surface area of the membrane is 1%, the permeation flux is significantly increased as compared with the case without the baffle, and 90% is reduced. If it exceeds, the decrease of the permeation flux becomes large.

Further, in the technical field to which the present invention is directed, a permeation flux of a certain value or more is required, depending on the properties of the liquid to be treated, the treatment purpose and the treatment cost, and the average permeation flux is 30 L (liter) / m. ^As shown in Fig. 22 below, in order to satisfy such a requirement for permeation flux, a rectangular baffle, hook-shaped baffle, S-shaped baffle or In the case of an arc-shaped baffle, the projected area of the baffle with respect to the surface area of the membrane is 10 to 9 More preferably, it is 0%, and in order to increase only the permeation flux without increasing the pressure loss in the apparatus, the projected area of the buffer with respect to the surface area of the membrane should be 26 to 70%. More preferred.

② In case of radial baffle

In the case of the radial baffle, if the projected area of the baffle with respect to the surface area of the membrane is less than 30%, the effect of promoting turbulence on the membrane surface is small, and

If it exceeds 0%, the pressure loss of the liquid to be treated becomes too large. Therefore, the projected area of the radial paffle on the surface area of the membrane is 30

~ 70% is preferred.

(4) Membrane diameter and membrane rotation speed

When a rectangular baffle, a hook-shaped baffle, an S-shaped baffle, or an arc-shaped baffle is used, the diameter of the membrane is preferably 200 to 110 wakes. If it is less than 200 mm, the number of membranes will be too large for a device with sufficient membrane separation capacity. The device and the rotating shaft will be too long, and those exceeding 110 mm will be manufactured. It is difficult, the production cost is greatly increased, and the power required for rotation is greatly increased. Further, as shown in an example to be described later (see FIG. 24), when the film body diameter is less than 20 O mm, when the rotation speed of the film body is low, the permeability is large enough to be practically used. If the overflux cannot be obtained and the membrane speed is low (eg.

This is because the permeation flux increases as the diameter of the membrane increases, but does not increase even if the diameter of the membrane exceeds 110 mm.

When a rectangular baffle, hook-shaped baffle, S-shaped baffle or arc-shaped baffle is used, the rotation speed of the membrane is as follows.

It is preferably between 20 and 180 rpm. At less than 20 rpm Has almost no pore blocking effect and concentration polarization reducing effect, and if it exceeds 180 rpm, the centrifugal force becomes too large, and as described above, the permeation efficiency decreases, and This is because the power greatly increases. Further, as shown in an example described later (see FIG. 25), when the rotation speed of the membrane is less than 20 rpm, the permeation flux is extremely small. The bundle does not rise.

② In case of radial baffle

In order to secure a predetermined permeation flux and to realize an industrial device having a practically required throughput, a membrane area of a certain value or more (for example, 10 m ² or more) is required. However, if the membrane diameter is less than 30 Omm, a very large number of membranes will be required to secure the required membrane area, and the equipment and the rotating shaft will be too long, making it a practical industrial device. It is difficult to be established. On the other hand, as the diameter of the membrane increases, the transmitted flux increases, and the rotation axis can be shortened.However, the power required for rotation increases in proportion to the fifth power of the diameter of the membrane, resulting in economical operation. There is an inconvenience that it cannot be done. Moreover, even when the diameter of the membrane is larger than a certain value, the amount of increase in the permeation flux is small.

Therefore, when a radial baffle is used, the diameter of the membrane is preferably in the range of 300 to 100 Omm, because an economical and efficient membrane separation device can be realized. When rotating a membrane having a diameter in this range, if the number of revolutions of the membrane is less than 50 rpm, the membrane pore blocking prevention effect, the fouling prevention effect, and the concentration polarization reduction effect are almost non-existent and can be used sufficiently. It is not possible to obtain a permeation flux of the order of magnitude. On the other hand, if the number of revolutions of the membrane exceeds l OOO r pm. The centrifugal force becomes too large, and the pressure effective for permeation applied to the pressurized liquid to be processed is canceled out, and the permeation efficiency decreases. Also, the power required for rotation is greatly increased. So, using radial baffles In this case, the rotation speed of the membrane is preferably in the range of 50 to 100 rpm.

(5) Number of notches

① Rectangular baffle, hook-shaped baffle, S-shaped baffle, and arc-shaped baffle

If the number of baffles provided on one side of the membrane is too large, there is a drawback that mounting becomes difficult. In addition, as shown in an embodiment described later (see FIG. 21), the number of baffles is set at 20. Since the permeation flux does not increase even if the number is increased to more than this, the number of rectangular baffles, hook-shaped baffles, S-shaped baffles or arc-shaped baffles is preferably set to 1 to 20.

② In case of radial baffle

When the number of radial baffles is small, the permeation flux is small, and when the number of puffles increases, the permeation flux increases. However, even if the number of radial baffles is increased beyond a certain level, the permeation flux does not increase. Therefore, the number of radial baffles is preferably 4 to 12 ((6) The gap between the membrane and the baffle)

In the case of a rectangular baffle, a hook-shaped baffle, an S-shaped baffle, or an arc-shaped baffle, the gap between the membrane and the baffle is preferably 2 to 18 bandages. If the thickness is less than 2 mm, the membrane and the baffle will contact each other, causing the membrane to be damaged, and the membrane may be damaged.If the length exceeds 18 mm, the rotation axis becomes longer, and the volume of the container containing the membrane becomes too large. And the distance between the membrane and the baffle is too large to reduce the turbulence promoting effect of the baffle. Also, as shown in the embodiment described later (see FIG. 26), If the gap between the membrane and baffle is less than 2 mm or more than 18 mm, This is because a permeation flux large enough to be practically used cannot be obtained.

② Radial baffle

In the case of a radial baffle, the gap between the membrane and the baffle is preferably 2 to 12 dragons. If less than 2 bandits, the membrane and the radial baffle may be easily in contact with each other, and the membrane may be damaged.If it exceeds 12 mm, the distance between the membrane and the radial baffle is too large, and This is because the effect of promoting turbulence cannot be expected, and the entire length of the device increases in order to secure the required film area, which is not economical.

(7) Rotation speed of membrane

In the case of a rectangular baffle, a hook-shaped baffle, an S-shaped baffle, an arc-shaped baffle, or a radial baffle, the rotation speed of the membrane on the outer periphery is preferably 1 to 30 m / sec. At low speeds of less than 1 mX sec, there is almost no effect of preventing pore clogging and concentration polarization reduction, and at more than 30 m / sec, the centrifugal force becomes too large and is added to the pressurized liquid to be treated. This is because the effective pressure for permeation is canceled out and permeation efficiency is reduced, and the power required for rotation is greatly increased. Further, as shown in an example to be described later (see FIG. 23), when the outer peripheral velocity of the film is less than lm / sec, it is not possible to obtain a sufficiently high permeation flux for practical use. This is because the permeation flux decreases when the peripheral velocity of the membrane exceeds 3 OmZ sec, regardless of whether the liquid has a high concentration or a high concentration.

(8) Baffle thickness

Regardless of whether a rectangular baffle, hook-shaped baffle, S-shaped baffle, arc-shaped baffle, or radial baffle is used, the baffle has a gap between the rotating membrane and the baffle. Should be installed and installed so that it does not come in contact with the membrane. You. On the other hand, it is preferable to reduce the thickness of the baffle as much as possible so as not to occupy a large volume. However, if the thickness is too small, the baffle should be at least lmm thick, since it is likely to bend and may come into contact with the membrane to damage the membrane. However, in order not to occupy too large a volume and to prevent the clearance between the membranes from becoming too wide and the equipment and rotating shaft from becoming long, the thickness of the paffle should be less than 20 bandages. Is preferred. In addition, in order to prevent deflection, the material of the baffle is not particularly limited, but various metals such as iron and stainless steel, plastics, ceramics, and glass fiber reinforced plastics are preferable. .

(9) Width of the notch

In the case of a rectangular baffle, hook-shaped baffle, S-shaped baffle, arc-shaped baffle or radial baffle, the width of the baffle is preferably 0.1 to 40% of the membrane diameter. If it is less than 0.1%, the effect of promoting turbulence on the surface of the membrane is small, and if it exceeds 40%, the pressure loss of the liquid to be treated becomes too large.

(10) Ratio of vessel inner diameter to membrane diameter

The ratio of the inner diameter of the vessel to the diameter of the membrane is preferably in the range of 1.03 to 3.00. If it is less than 1.03, the area occupied by the film is too large, and the pressure loss of the liquid to be treated becomes too large. On the other hand, if it exceeds 3.0000, the area occupied by the membrane is too small and the membrane separation efficiency is undesirably reduced.

(11) Pressure of liquid to be treated

When the pressure of the liquid to be treated introduced into the container exceeds 2 OMPa. There is an inconvenience that the pressure resistance of the container becomes difficult. The water level is less than 0.5 m.-There is a disadvantage that the membrane is not immersed in the liquid to be treated. The pressure of the liquid to be treated introduced into the tank is preferably 0.05 MPa to 20 MPa.

(1 2) Radial acceleration during membrane rotation

When the film body is rotated, the liquid to be treated near the film body that rotates together with the film body is subjected to radial acceleration toward the outside of the circle. According to the findings of the inventor, it has been found that this radial acceleration affects the membrane separation performance. That is, when the liquid to be treated is at a high concentration, the operation is performed in a range where the radial acceleration during rotation of the film is 200 mZsec ² or more, and when the liquid to be treated is at a low concentration, the radial acceleration during the film rotation is increased. By operating at a speed of 100 m / sec ² or more, a shearing force effective for permeation is applied to the liquid to be treated according to the viscosity of the liquid to be treated, and the permeation flux increases. .

(1 3) Thickness of membrane

The thickness of the film is preferably 1 to 20 mm. If it is less than 1, the strength is insufficient, and if it exceeds 20 dishes, the volume of the container for accommodating the membrane becomes too large.

(1 4) Shape of membrane

The shape of the film body may be a circle, but is not necessarily limited to a circular shape, and may be a pentagon or more polygonal shape.

(15) Making the equipment compact

The rotary shaft is hollow, and a small hole is formed in a portion where the membrane is mounted in the longitudinal direction of the membrane. The membrane has a structure in which a permeable membrane having a path through which a permeated liquid can be transferred is attached to both sides of the plate. If a configuration is adopted in which the permeated liquid transfer path of the permeable membrane communicates with the small hole provided in the rotating shaft. The rotating shaft can also be used as a means for discharging the permeated liquid. There is an advantage of becoming.

(1 6) Meaning of diameter

As used herein, "diameter" means "through the center of a circle or sphere. In addition to "a line segment having both ends on a circumference or a sphere," it also means "in a polygon, a line segment twice as long as the distance from its center to one vertex."

The rotary membrane separation apparatus and the membrane separation method using the rotary membrane separation apparatus of the present invention are configured as described above, and have the following effects.

(1) According to the rotary membrane separator according to claims 1, 2, 3, and 4, the baffle does not have a structure that completely separates the membranes, so that the baffle can be used for processing. Low liquid pressure loss and excellent membrane separation performance.

Also, there is no need to alternately assemble the membrane and the baffle. After assembling the rotating shaft and the membrane, the puffer can be inserted from the lateral direction of the laminated membrane, so that there is no need for installation.

Furthermore, since the paffle shape is simple, machining is easy and low cost.

Since the width, thickness and number of baffles can be arbitrarily changed according to the properties of the liquid to be treated, the type of liquid to be treated is not limited, and the applicability is excellent.

(2) In particular, the rotary membrane separator according to claims 2, 3, and 4 can increase turbulence generated on the membrane surface and improve membrane separation performance. There is an advantage. There is also an advantage that the exchange of fluid between the membranes is promoted.

(3) In particular, in the rotary membrane separator according to claim 5, the projected area of the baffle with respect to the surface area of the membrane is within an appropriate range. The permeation flux becomes extremely large.

(4) In particular, the rotary membrane separation device according to claims 6, 7, 8, and 9 may be a rectangular baffle, a hook-shaped baffle, an S-shaped baffle, or an arc-shaped baffle. Support both ends of Since it is held and fixed, it is easy to assemble the device and cost can be reduced.

(5) In particular, the rotary membrane separation device according to claim 10 has an advantage that the baffle can be easily attached.

(6) In particular, according to the rotary membrane separation apparatus described in Claims 11, 13, 13, 15, 17, 24, and 25, membrane separation There is an effect that the efficiency is extremely excellent.

(7) In particular, the rotary membrane separation device according to claim 12 has an advantage that the size of the device is appropriate and the production cost and running cost can be suppressed.

(8) In particular, the rotary membrane separator according to claims 14 and 16 has the advantage that the baffle is less likely to bend and the membrane is less likely to be damaged.

(9) In particular, the rotary membrane separation device described in claim 18 has an advantage that the device is compact.

(10) In particular, according to the inventions set forth in claims 19, 20, 21, 21, and 23, the membrane separation performance can be effectively exhibited. A rotary membrane separation device can be provided.

(11) In particular, according to the membrane separation method described in claims 26 and 27, the membrane is hardly clogged, has a high permeation flux, and can be concentrated to a high concentration. It is possible. In addition, since there is no need to supply the liquid to be treated at a high flow rate, there is no need for a pumping means such as a large pump, so energy costs are low, and it is not necessary to increase the number of circulations to increase the concentration. There is an effect that the liquid to be treated is less likely to be sheared by the feed blades and the like, and the quality of the liquid to be treated is not easily changed.

(12) In particular, according to the invention described in Claims 28, 29, and 30, the rotary type capable of effectively exhibiting the membrane separation performance is provided. Operating conditions of the membrane separation device can be provided.

[Brief description of drawings]

FIG. 1 is a perspective view of one embodiment of the rotary membrane separation device of the present invention.

FIG. 2 (a) is a cross-sectional view of one embodiment showing a rectangular baffle, a membrane, and a container of the rotary membrane separator of the present invention, and FIG. 2 (b) uses the rectangular baffle. FIG. 2 is a side view including a cross section of the rotary membrane separation apparatus, in which a rotating means is omitted, and FIG. 2 (c) is a cross-sectional view taken along the line II-II of FIG. 2 (a).

FIG. 3 (a) is a cross-sectional view of another embodiment showing a rectangular baffle, a membrane and a container of the rotary membrane separator of the present invention, and FIG. 3 (b) uses the rectangular baffle. FIG. 3 is a side view including a cross section of the rotating membrane separation apparatus, in which a rotating means is omitted, and FIG. 3 (c) is a cross-sectional view taken along the line III-III of FIG. 3 (a).

Fig. 4 (a) shows that a gap is provided between the membrane and the membrane on both sides of the membrane, and eight rod-shaped baffles are placed on each other from the vicinity of one inner wall of the container to the vicinity of the other inner wall across the rotation shaft. Sectional view of an example showing a rod-shaped paffle, membrane and container of a rotary membrane separator arranged in parallel. Fig. 4 (b) is a side view including a cross-section of a rotary membrane separator using the rod-shaped baffle. Yes, the rotating means is omitted, and FIG. 4 (c) is a diagram showing a method of fastening the rod-shaped paffle.

FIG. 5 (a) is an enlarged cross-sectional view showing a portion where the membrane is mounted on the rotating shaft in one embodiment of the rotary membrane separation apparatus of the present invention, and FIG. 5 (b) is FIG. 13 is an enlarged cross-sectional view showing a place where the film body of another embodiment is mounted on a rotating shaft.

FIG. 6 (a) is an enlarged cross-sectional view showing the membrane and the rectangular baffle near the inner wall of the vessel in one embodiment of the rotary membrane separator of the present invention. Fig. 6 (b) is an enlarged view of a permeated liquid transfer path in the permeable membrane.

FIG. 7 is a diagram showing a flow of the liquid to be treated in the rotary membrane separation device of the present invention.

FIG. 8 (a) is a cross-sectional view of one embodiment showing a radial membrane, a membrane and a container of the rotary membrane separation apparatus of the present invention, and FIG. 8 (b) is a VIII of FIG. 8 (a). -It is VIII arrow sectional drawing.

FIG. 9 is a sectional view of an embodiment showing an arc-shaped baffle, a membrane, and a container of the rotary membrane separator of the present invention.

FIG. 10 is a cross-sectional view of one embodiment showing a hook-shaped baffle, a membrane, and a container of the rotary membrane separator of the present invention.

FIG. 11 is a cross-sectional view of one embodiment showing an S-shaped profile, a membrane, and a container of the rotary membrane separator of the present invention.

FIG. 12 (a) is a cross-sectional view of one embodiment showing a wing-shaped baffle, a membrane and a container of the rotary type membrane separation device of the present invention, and FIG. 12 (b) is a wing-shaped baffle of the same. FIG. 12 is a side view including a cross section of the rotary membrane separator used, in which the rotating means is omitted. FIG. 12 (c) is a cross-sectional view taken along the line XII--XII in FIG. FIG. 4 is an enlarged view showing 0 and its vicinity.

FIG. 13 is a schematic configuration diagram showing one example of a membrane separation system, and FIG. 14 is a schematic configuration diagram showing another example of a membrane separation system.

FIG. 15 is a diagram showing the relationship between the concentration of the concentrated liquid and the permeation flux, and FIG. 16 is a diagram showing the relationship between the operating pressure and the permeation flux. FIG. 17 is a cross-sectional view of an example showing a rod-shaped baffle, a membrane, and a container of a rotary membrane separator.

FIG. 18 is another diagram showing the relationship between the operating pressure and the permeation flux, and FIG. 19 is a diagram showing a perforated plate-shaped baffle and membrane of a rotary membrane separator. FIG. 4 is a cross-sectional view of an example showing a container and a container.

FIG. 20 is yet another diagram showing the relationship between the operating pressure and the permeation flux.

FIG. 21 is a diagram showing the relationship between the number of rectangular baffles and the permeation flux.

FIG. 22 is a diagram showing the relationship between the projected area (%) of the rectangular paffle and the permeation flux with respect to the surface area of the membrane.

FIG. 23 is a diagram showing a relationship between a membrane peripheral velocity and a permeation flux. FIG. 24 is a diagram showing the relationship between the diameter of the membrane and the permeation flux. FIG. 25 is a diagram showing the relationship between the number of revolutions of the membrane and the permeation flux (FIG. 26 is a diagram showing the relationship between the gap between the membrane and the baffle and the permeation flux).

FIG. 27 is a diagram showing a time change of a permeation flux of the rotary membrane separation device of the present invention.

FIG. 28 is a diagram showing the concentration polarization reducing effect of the rotary membrane separation device of the present invention.

FIG. 29 is another diagram showing the concentration polarization reducing effect of the rotary membrane separation device of the present invention.

FIG. 30 is a diagram showing the relationship between the number of revolutions of the membrane and the permeation flux, with the membrane diameter as a parameter, when the low-concentration latex is subjected to membrane separation using a radial baffle.

FIG. 31 is a diagram showing the relationship between the number of rotations of the membrane and the permeation flux with the membrane diameter as a parameter when the high-concentration latex is subjected to membrane separation using a radial baffle.

FIG. 32 is a diagram showing the relationship between the permeation flux and the gap between the membrane and the baffle when the membrane is separated using a radial baffle.

Fig. 33 uses a ring-shaped baffle or a radial baffle. FIG. 4 is a diagram showing a relationship between a transmembrane pressure and a permeation flux when performing membrane separation by using the method shown in FIG.

FIG. 34 is a diagram showing the relationship between the number of radial baffles and the permeation flux when membrane separation is performed using a radial baffle.

FIG. 35 is a diagram showing the relationship between the projected area (%) of the radial baffle and the permeation flux with respect to the surface area of the membrane when performing membrane separation using a radial baffle.

Fig. 36 shows the relationship between the permeation flux and the radial acceleration when the membrane rotates, with the transmembrane pressure (operating pressure) as a parameter in the case of membrane separation using a ring-shaped paffle. FIG. Fig. 37 shows the relationship between the permeation flux and the radial acceleration during rotation of the membrane, using the transmembrane pressure (operating pressure) as a parameter in the case of membrane separation using a ring-shaped paffle. FIG. 36 is different from FIG.

Fig. 38 shows the relationship between the permeation flux and the radial acceleration during rotation of the membrane, using the transmembrane pressure (operating pressure) as a parameter in membrane separation using a ring-shaped baffle. FIG. 36 is different from FIGS. 36 and 37.

Fig. 39 shows the relationship between the permeation flux and the radial acceleration when the membrane rotates when the membrane transmembrane pressure (operating pressure) is set as a parameter in the case of membrane separation using a ring-shaped baffle. FIG. 36 is a view different from FIG. 37 and FIG.

FIG. 40 is a diagram showing the relationship between the radial acceleration and the radial flux during rotation of the membrane when the membrane is separated using a ring-shaped baffle, with the latex concentration as a parameter.

Fig. 41 shows the relationship between the radial flux and the radial flux during rotation of the membrane when the membrane is separated using a ring-shaped baffle, with the latex concentration as a parameter. Different from FIG.

Fig. 42 shows the relationship between permeate flux and radial acceleration during rotation of the membrane, using latex concentration as a parameter in the case of membrane separation using a ring-shaped paffle. FIG. 41 is different from FIG.

FIG. 43 (a) is a plan view showing an example in which a large number of punched holes are provided in the paffle, and FIG. 43 (b) is a cross-sectional view showing an example in which the front and back surfaces of the baffle are etched. FIG. 43 (c) is a cross-sectional view showing an example in which the front and back surfaces of the baffle are embossed. FIG. 44 is a diagram showing a schematic configuration of a membrane separation device using a cross flow method.

FIG. 45 (a) is a cross-sectional view showing a ring-shaped baffle, a membrane and a container of a conventional rotary type membrane separation apparatus, and FIG. 45 (b) is a rotary type using the ring-shaped baffle. FIG. 2 is a side view including a cross section of the membrane separation device, omitting a rotating unit.

FIG. 46 (a) is a cross-sectional view showing a perforated ring-shaped baffle, a membrane and a container of a conventional rotary membrane separator, and FIG. 46 (b) is a diagram showing the perforated ring-shaped baffle used. FIG. 4 is a side view including a cross section of the rotating membrane separation apparatus, in which a rotating means is omitted.

[Best mode for carrying out the invention]

Hereinafter, embodiments of the present invention will be described with reference to the drawings. However, the present invention is not limited to the following embodiments, and those skilled in the art will be able to perform the present invention without departing from the technical scope of the present invention. If so, it can be changed or modified as appropriate. Further, in a comparative investigation experiment on membrane separation characteristics described later, as an embodiment of the present invention, a case where a rectangular baffle and a radial baffle were mainly used was shown, but the same effect was obtained. Within the technical scope of the present invention, it is possible to point out baffles having other shapes described in the claims, and the invention is not limited to the baffles having the shapes used in the experiments.

FIG. 1 is a perspective view of a rotary membrane separation device of the present invention. Reference numeral 1 denotes a supply inlet for the liquid to be treated. A hollow rotary shaft 3 is arranged so as to pass through the center of the cylindrical container 2, and a number of membranes mounted on the hollow rotary shaft 3 (number 1 in FIG. 2). The liquid permeated in 2) passes through the hollow rotary shaft 3 and is discharged from outlets 4 and 5, and the concentrated liquid is discharged from outlet 6. Reference numeral 7 denotes a motor that rotates the membrane together with the rotating shaft 3, and the torque of the motor 7 is transmitted to the rotating shaft 3 by a belt 8. The transmission of rotational force is not limited to this, and it is also possible to use a motor-direct connection type, a gear reducer, or a wrapping transmission device.

As shown in FIGS. 5 (a) and 5 (b), the membrane used in this example is a polyether sulfone permeate through woven fabric cloth 10 on both sides of a polypropylene plate 9. This is the structure to which the conductive film 11 is attached. In addition, a metal plate or a ceramic plate other than the plastic plate used in this embodiment can be used as a plate on which the permeable membrane is attached, and it is preferable to use a material that does not easily deform and is resistant to breakage. .

In this specification, a permeable membrane has a porous structure, and is capable of transporting permeated liquid by passing through a porous portion (by connecting the porous portions to each other). A channel formed therein means a channel formed inside, and as long as it has such a function, a ceramic film or a metal film other than the above-mentioned organic film can be adopted.

The spacer cloth 10 can also transfer the permeated liquid, and the flow path of the permeated liquid in the spacer cloth 10 is larger in diameter than the permeated liquid transfer path 27 of the permeable membrane 11 described later. The liquid is a single sacro It is easy to flow through the 10

As shown in FIG. 2 (b), a film body 12 composed of a plastic plate body 9, a cross cloth 10 and a permeable membrane 11 is mounted on the rotating shaft 3 as shown in FIG. The two stainless steel rectangular baffles 13 are parallel to each other from the vicinity of one inner wall of the container 2 to the vicinity of the other inner wall of the container 2 with the rotating shaft 3 interposed therebetween. It is arranged (see FIG. 2 (a)), and both ends of the plurality of rectangular baffles 13 are supported and fixed by through bolts 14 connecting the surfaces 2a and 2b of the container 2. Further, a liquid flow path 16 connected to the supply inlet 1 of the liquid to be treated is formed along the inner wall surface 15 of the container 2.

The rotating shaft 3 is hollow, and as shown in Fig. 5 (a), a small hole 17 is provided in the mounting portion of the membrane member 12 in the longitudinal direction of the shaft, and the permeable membrane 1 forming the membrane member 12 is provided. The permeated liquid transfer path of No. 1 and the permeated liquid transfer flow path of the spacer cloth 10 communicate with the small holes 17. Reference numeral 18 denotes a rotating shaft mounting portion of the membrane body 12, which is a spacer interposed between the vertically adjacent membrane bodies 12 and 12. In addition, as shown in FIG. 5 (b), a plurality of slits 19 are provided in a longitudinal direction of a portion where the spacer 18 and the film body 12 are mounted on the rotating shaft 3, and the slits 19 are provided. A small hole 17 is provided at the end of the rotating shaft 3 using 9 as the permeate liquid transfer passage. The permeate liquid transfer passage of the permeable membrane 11 and the permeate liquid transfer passage of the spacer cloth 10 are provided. A configuration that leads to the small hole 17 through the slit 19 can also be adopted. Although omitted in FIG. 5 (b), small holes 17 are provided at arbitrary positions of the rotating shaft 3.

Fig. 3 shows that four stainless steel rectangular paffles 20 are placed on one side of a container 2 with a rotating shaft 3 interposed between them. An example is shown where they are arranged parallel to each other from the vicinity of the inner wall to the vicinity of the other inner wall. The material of the baffle is It is also possible to use plastic or ceramic besides the above-mentioned metal.

Either supply the pressurized liquid to be treated into the container 2 of the membrane separation apparatus configured as described above (at a pressure of about 0.1 MPa or more) or fill the container 2 with the liquid to be treated, When the pressure is reduced or sucked through the rotating shaft 3 and the rotating shaft 3 is rotated, as shown by an arrow 24 in FIG. 6 (a), a flow is generated radially outward due to centrifugal force. In addition, since baffles 13 are present on both sides of the membrane 12, a flow 25 that prevents the action of particles that try to block the pores of the membrane 12 and concentration polarization occurs, and As shown in Fig. (B), the membrane pores 26 are not closed, and pass through the passages in the spacer cloth 10 from the passages 27 formed by connecting the porous portions. The permeate is discharged from the small holes 17 shown in Figs. 5 (a) and (b) via the hollow rotary shaft 3 and the outlets 4 and 5 shown in Fig. 1, while the concentrated solution is discharged at the outlet 6 Is discharged from Since the permeated liquid flows more easily through the wide passage in the spacer cloth 10 than the narrow permeated liquid transfer path 27 in the permeable membrane, the permeate flows directly from the permeated liquid transfer path 27 directly to the small holes 17. The amount of the liquid is small, and the amount of the permeated liquid reaching the small holes 17 via the wide flow passage in the space cloth 10 is larger. At this point, it is also possible to form a flow path for the permeate in the plate 9 in order to secure a flow path through which the permeate flows easily. In this case, the spacer cloth 10 is unnecessary. . However, forming a permeate flow path in the plate body 9 is costly, so it is preferable to use spacer cloth 10 from the viewpoint of economy.

Note that a radial baffle as shown in FIG. 8 can be used as the baffle. Fig. 8 shows that eight baffles 28 are arranged radially toward the inner wall surface 15 of the container 2 with the rotation axis 3 as the center, with a gap provided between the film body 12 and the film body on both sides. For example, The end of the notch 28 is supported and fixed by a through bolt 14 connecting the surfaces 2 a and 2 b of the container 2. Furthermore, an arc-shaped baffle 29a shown in Fig. 9, a hook-shaped baffle 29b shown in Fig. 10, and an S-shaped baffle 29c shown in Fig. 11 should be used. Can also. Even if these baffles 29a, 29b and 29c are used, the same effect as that of the rectangular baffle can be expected. In addition, the arc-shaped baffle 29a, hook-shaped baffle 29b, and S-shaped baffle 29c can increase turbulence on the membrane surface and improve membrane separation performance. This has the effect. It also has the effect of promoting the exchange of fluid between membranes. As shown in FIGS. 9 and 10, the arc-shaped baffle 29 a and the hook-shaped baffle 29 b have a plurality of arc-shaped baffles 29 a or a plurality of arc-shaped baffles 29. The hook-shaped baffle 29 b should be arranged symmetrically with respect to the diameter of the membrane 12, or a plurality of arc-shaped baffles 29 a or a plurality of hook-shaped baffles 29 b should be Can be arranged point-symmetrically. Regarding the S-shaped baffle 29c, as shown in Fig. 11, a plurality of S-shaped baffles 29c can be arranged point-symmetrically with respect to the rotation axis 3 with the rotation axis 3 interposed therebetween. . Although not shown in FIGS. 9 to 11, the same number of baffles 29 a, 29 b, and 29 c are similarly arranged on the other side of the membrane 12, and the baffle shape is Except for the differences, the other configuration is basically the same as in FIG. Also, both ends of the arc-shaped notch 29a, the hook-shaped baffle 29b, and the S-shaped baffle 29c connect the surfaces 2a and 2b (see Fig. 2) of the container 2, respectively. It is supported and fixed by through bolts 14.

Further, as shown in FIG. 12 (c), it is also possible to employ a knotle 30 having a cross section similar to that of the wing. This baffle 3 0 According to this, there is an advantage that it is difficult to contact with the film body. Furthermore, there is an advantage that the rotation power can be reduced. The cross-section in the longitudinal direction of the rectangular baffle 13 shown in FIG. 2 and the rectangular baffle 20 shown in FIG. 3 are as shown in FIG. 2 (c) or FIG. 3 (c). The cross-sectional dimensions do not change. The rectangular baffle of the present invention is not limited to those exemplified here.

Next, the membrane separation device of the present invention and a conventional membrane separation device were compared and examined for various characteristics, and will be described. The inner diameter of the cylindrical container 2 used in each of the following experiments was 350 thighs, and the diameter of the membranes other than those particularly indicated was 300 mm. It is common.

(1) Membrane separation system

First, a membrane separation system to which the membrane separation device according to the present invention can be applied will be described.

That is, as shown in FIG. 13, the liquid to be treated 33 stored in the storage tank 32 for the liquid to be treated via the path 31 is stirred by the stirrer 34, and the liquid to be treated is reduced to about 0 by the pump 35. It is pressurized to 0.05 to 20 MPa and sent to the membrane separation device 37 via the path 36. Reference numeral 38 denotes a strainer for removing foreign matter in the liquid to be treated. The permeate separated by the membrane in the membrane separation device 37 is discharged through the route 39, the concentrated solution is returned to the storage tank 32 again through the routes 40 and 41, and the route 36 is further removed. After that, it is supplied again to the membrane separation device 37 to be subjected to membrane separation. By repeating such a membrane separation operation, the concentration of the concentrated solution is gradually increased. When the concentration reaches a predetermined concentration, the concentrated solution is taken out through the path 42. 43 is a valve, and 44 is a motor. The concentrated liquid does not necessarily need to be circulated, and the liquid separated by membrane in the membrane separation device 37 can be directly discharged through the path 42, or a part of the liquid can be returned to the storage tank to be partially recycled. Discharge You may. After the membrane separation of the liquid to be treated 33 stored in the storage tank 32 is completed, another liquid to be treated is stored in the storage tank 32 via the path 31 and the membrane separation is performed by the same operation. FIG. 14 shows a configuration in which a pump 35 is installed in the permeate discharge path 39 of the membrane separation device 37, and the pump 35 sucks the liquid to be treated in this manner. When supplying to the membrane separation device 37, the membrane separation device 37 can be opened, and the number of auxiliary equipment of the membrane separation device can be reduced, so that the entire device becomes compact. This has the effect. In the case of the membrane separation system shown in Fig. 14, the pressure of the liquid to be treated supplied to the membrane separation device 37 is relatively small, so that an effect that fouling hardly occurs can be expected.

(2) Influence of permeation flux by paffle shape and presence or absence of rotation during membrane separation

A membrane separation was performed using the membrane separation system shown in Fig. 13 and the result of investigating the relationship between the concentration of the concentrated solution and the permeation flux is shown in Fig. 15. As shown in FIG. 2, a membrane having two rectangular baffles on one side and the other side is used as a conventional membrane separation apparatus. A membrane separation device of the type and a cross-mouth type membrane separation device shown in FIG. 44 were used. Are as follows. B. Common conditions

a Membrane U F membrane (ultrafiltration membrane, diameter 2 65 mm)

b Temperature 25 ° C

c Liquid to be treated Latex, initial concentration 3.3% by weight d Operating pressure 450 kPa

Mouth. Rotational condition of rotary membrane separator

a Peripheral velocity of the membrane 1 2 mZ seconds In FIG. 15, the symbols “”, “▲”, and “拿” mean the membrane separation method according to the present invention (using the rotary membrane separation device in FIG. 2) and FIG. The membrane separation method using a rotary membrane separation device and the cross-flow type membrane separation method (in which the membrane separation device 37 in the membrane separation system of FIG. 13 is a non-rotation type) shown in Fig. 13 are shown. As shown in FIG. 15, the membrane separation method of the present invention (symbol 〇) shows a much larger permeation flux than that of the cross-flow method (symbol parable), and is shown in FIG. It shows an excellent permeation flux compared to the membrane separation method using a rotary membrane separator (symbol ▲). That is, in the rotary membrane separator shown in Fig. 45, the ring-shaped baffle 68 completely separates the membranes, the baffle 68 has a large area covering the membrane 64, and the inside of the vessel 62 Since the liquid to be processed passes through the narrow and long flow path 69, the pressure loss increases, and the permeation flux cannot be increased. In addition, in the rotary membrane separation apparatus shown in FIG. 45, since the baffle 68 uniformly covers the membrane surface, there is a disadvantage that the turbulence of the liquid to be treated is small.

In the cross-flow method, the permeation flux at a concentration of 22.6% is almost zero, and it is impossible to further concentrate. However, the membrane separation method of the present invention employs a concentration of 22.6%. Even at%, the permeation flux exceeds 30 L (liter) m ² Zhr, and further high concentration is possible.

(3) Effect of baffle shape on pressure loss

Using the membrane separation system shown in Fig. 13 and the rotary membrane separator shown in Fig. 2 and the rotary membrane separator shown in Fig. 45, the membrane is a UF membrane (diameter of 26.5 mm). A latex having a temperature of 25 ° C and an initial concentration of 3.3% by weight is supplied to each of the above-mentioned membrane separation devices at 1 m ³ / lir and 0.2 MPa, and the outer peripheral velocity of the membrane is set to 12 mZ seconds. The flow rate of the permeate, the flow rate of the concentrate, and the pressure of the concentrate. Inspected. The results are shown in Table 1 below.

【table 1】

As shown in Table 1, the rotary membrane separator of Fig. 2 has substantially no pressure drop of the concentrated solution, while the rotary membrane separator of Fig. 45 using all partition baffles However, the outlet pressure of the concentrated liquid is reduced to 1/4 of the supply pressure of the liquid to be treated. The flow rate of the permeate in the rotary membrane separator of the present invention is larger than that in FIG. 45 using the all-partitioned paffle, and conversely, the flow rate of the concentrate in the rotary membrane separator of the present invention Is half that of Fig. 45 using all-partitioned paffles. That is, according to the membrane separation method of the present invention, the concentration can be increased five-fold, but with the membrane separation device shown in FIG. 45, the concentration can be performed only 2.5-fold. Thus, according to the membrane separation method of the present invention, it is possible to concentrate to a high concentration at a high permeation flow rate, and to provide a membrane separation method with extremely small pressure loss.

(4) Influence on operation pressure and permeation flux due to difference in paffle shape (a) For rectangular and ring baffles

Using the membrane separation system shown in FIG. 13, the membrane separation device of the present invention has two rectangular paffles on one side and the other side of the membrane as shown in FIG. The conventional membrane separation device having a ring-shaped paffle was used as shown in Fig. 45, and the result of investigating the relationship between operating pressure and permeation flux is shown in Fig. 16. The operating pressure is the effective pressure obtained by subtracting the centrifugal force from the supply pressure of the liquid to be treated. Is the pressure used for the permeation of

As shown in FIG. 16, at any of the peripheral speeds of the membrane of 8 m / sec, 16 m / sec, and 24 mZsec, the membrane separation device of the present invention having a rectangular baffle (symbol △, port) , 〇) have a higher permeation flux than conventional membrane separation devices with a ring-shaped baffle (signs ▲, 酾, ·).

(b) Rectangular and bar baffles

Using the membrane separation system shown in FIG. 13, the membrane separation device of the present invention has four rectangular baffles on one side and the other side of the membrane as shown in FIG. As shown in Fig. 17, a membrane separator having four rod-shaped baffles 21 on one side of the membrane 12 was used as the membrane separator having rod-shaped baffles. Fig. 18 shows the results of investigation of the relationship between permeation flux. Although not shown in FIG. 17, the same number of rod-shaped baffles are arranged in the same manner on the other side of the membrane 12, except for the difference in the number of rod-shaped baffles. The configuration is basically the same as that shown in Fig. 4. The rod-shaped paffle 21 connects the two surfaces 2a and 2b of the container 2, and the recess of the stepped fastener 22 shown in Fig. 4 (c). 2 and 3 are engaged.

As shown in Fig. 18, the membrane separation device of the present invention having a rectangular paffle (symbol △, mouth) has a rod-shaped baffle regardless of whether the membrane peripheral speed is 8 m / sec or 16 m / sec. The permeation flux is much higher than that of a membrane separation device with a symbol (▲, Peng).

(c) Rectangular baffle and perforated plate baffle

Using the membrane separation system shown in Fig. 13, the membrane separation device of the present invention has four rectangular baffles on one side and the other side of the membrane as shown in Fig. 3. As a membrane separation device having a perforated plate-shaped baffle, as shown in FIG. Fig. 20 shows the results of an investigation of the relationship between operating pressure and permeation flux using a perforated plate-like baffle 45 installed from the inner wall 15 of the container to the vicinity of the rotating shaft 3. . Although not shown in FIG. 19, the same number of perforated plate-like baffles are similarly arranged on the other side of the membrane 12, except that the shape of the baffles is different. The other configuration is basically the same as FIG.

As shown in FIG. 20, the membrane separation device of the present invention having a rectangular paffle (symbols △, 、, 〇) at any of the membrane peripheral speeds of 8 mZsec, 16 m / sec, and 24 m / sec. ) Has a much higher permeation flux than a membrane separator with perforated plate-shaped baffles (signs ▲, 酾,).

(5) Number of rectangular baffles and flux

Using the membrane separation system shown in Fig. 13 and when the projected area of the baffle with respect to the surface area of the membrane is fixed at 50%, one side of the membrane and the other Figure 21 shows the results of an investigation of the relationship between the number of rectangular baffles arranged from the vicinity of the inner wall to the vicinity of the other inner wall and the permeation flux.

As shown in Fig. 21, when the outer peripheral speed of the film is 8 mZsec (△) or 24 m / sec (〇), the presence of one rectangular baffle makes it possible to reduce The permeation flux increases significantly, and the permeation flux increases as the number of rectangular baffles increases. However, the permeation flux does not increase even if the number of rectangular paffles is increased beyond 20.

Therefore, it is preferable that the number of baffles is 1 to 20 in order to avoid the complicated mounting of the baffle and to obtain a sufficient permeation flux.

(6) Projected area and permeation flux of the baffle with respect to the surface area of the membrane using the membrane separation system shown in Fig. 13 and as shown in Fig. 2 In addition, when the number of rectangular baffles provided on one side and the other side of the membrane is two, the relationship between the projected area (%) of the rectangular baffle and the permeation flux with respect to the surface area of the membrane is shown. shows the result of investigation into the second 2 figures, the numerical value of the flux (L (liters) Bruno m ² Bruno hr) to the projected area of each Paffuru second FIG. 2 (%), Makugaishu speed is 8 m Table 2 below shows the case of / m, and Table 3 below shows the case of 24 m / sec.

[Table 2]

As shown in Fig. 22, when the outer peripheral velocity of the film is 8 mZsec (△) or 24 mZsec (〇), the projected area of the paffle with respect to the surface area of the film body is 1%, compared to the case without the rectangular paffle. As a result, the permeation flux increases significantly, and the permeation flux increases as the projected area of the paffle increases. However, it can be seen that when the projected area of the paffle exceeds 90%, the permeation flux is greatly reduced. The reason for the baffle projection area exceeding 90% is that, like the above-mentioned conventional ring-shaped baffle, the baffle has a large area covering the membrane and the pressure loss of the liquid to be treated is large. This is because the transmission efficiency decreases.

In Fig. 22, the permeation flux is larger at 24 m / sec when the outer peripheral velocity is 8 mZ sec, but the power required for rotation increases when the outer peripheral velocity increases (necessary for rotation). Power is approximately rotation speed However, the power required for rotation does not become excessive at a membrane peripheral speed of about 8 m / sec. Furthermore, in the technical field targeted by the present invention, an average permeation flux of 30 LZm ² / hr or more is often required, so that it is necessary for economic efficiency and the technical field targeted by the present invention. In order to satisfy both requirements of the permeation flux, it is preferable from FIG. 22 and Table 2 that the projected area of the baffle with respect to the surface area of the membrane is 10 to 90%. Further, in order to increase only the permeation flux without increasing the pressure loss in the apparatus, the projected area of the baffle with respect to the surface area of the membrane is more preferably 26 to 70%.

(7) Peripheral velocity and permeation flux

When the membrane separation system shown in Fig. 13 is used and the number of rectangular paffles provided on one side and the other side of the membrane is two as shown in Fig. 2 (based on the surface area of the membrane) Fig. 23 shows the results of an investigation of the relationship between the membrane peripheral velocity and the permeation flux when the projection area of the paffle was 50%).

In FIG. 23, symbols “Hata”, “△”, “Jiyu”, and “◊” indicate that the concentration of the liquid to be treated is 10%, 20%, 30%, and 50%, respectively. As shown in FIG. 23, if the outer peripheral velocity of the film is less than 1 m / sec, it is not possible to obtain a sufficiently high permeation flux for practical use. In particular, at a high concentration exceeding 30%, the permeation flux becomes extremely low when the peripheral speed of the membrane is low. This is because in order to perform high-concentration liquid membrane separation, sufficient kinetic energy to overcome the high viscosity is required, and the kinetic energy is proportional to the square of the velocity. This is because sufficient energy for membrane separation cannot be supplied at the membrane rotation speed.

At a low concentration of 20% or less, the permeation flux is almost constant when the membrane peripheral speed exceeds 15 mZsec, but at a high concentration of 30% or more, The permeation flux increases up to a membrane peripheral velocity of 30 m / sec. However, when the peripheral speed of the membrane exceeds 30 m / sec, the permeation flux decreases at both low and high concentrations.

Therefore, in order to obtain a sufficient permeation flux from a low concentration to a high concentration, the outer peripheral velocity of the membrane is preferably set to 1 to 30 mZsec.

(8) Diameter of membrane and flux

When the membrane separation system shown in Fig. 13 is used and the number of rectangular paffles provided on one side and the other side of the membrane is two as shown in Fig. 2 (based on the surface area of the membrane) Figure 24 shows the relationship between the diameter of the membrane and the permeation flux when the projected area of the baffle was 50%).

In FIG. 24, the symbols “parable”, “▲”, “garden”, “♦”, and “V” indicate that the rotational speed of the membrane is 200 rpm, 600 rpm, and 10 rpm, respectively. 0 0 rpm> 1400 rpm and 1800 rpm. At a very high rotation speed of 180 rpm, the permeation flux increases very little even if the membrane diameter increases. The membrane separation energy is proportional to the square of the rotation speed, and the effect of the rotation speed greatly contributes. Therefore, at ultra-high speed rotation, the difference in the diameter of the membrane body does not matter much.

On the other hand, when the rotation speed is 140 rpm or less, the permeation flux increases as the membrane diameter increases, but the permeation flux increases when the membrane diameter exceeds 110 mm. Does not increase. If the diameter of the membrane is less than 200 mm, the permeation flux cannot be sufficiently large for practical use at a low rotation speed of less than 600 rpm.

Therefore, in order to suppress a large increase in the power required for rotation and to obtain a sufficient permeation flux from low speed to high speed rotation, the membrane diameter should be 200 mm: L100 mm. Is preferred. (9) Rotation speed and flux of membrane

When the membrane separation system shown in Fig. 13 is used and the number of rectangular paffles provided on one side and the other side of the membrane is two as shown in Fig. 2 (based on the surface area of the membrane) Figure 25 shows the results of an investigation of the relationship between the membrane rotation speed and the permeation flux when the projected area of the baffle is 50%).

In FIG. 25, the symbols “see”, “▲”, “sphere”, “instruction”, and “T” indicate that the diameters of the membranes are 110 mm, 7500 mm, and 450 mm, respectively. , 3 000 mm and 2 000 mm. If the rotation speed is less than 20 rpm, it is not possible to obtain a sufficiently high permeation flux with any membrane diameter. The permeation flux increased as the rotation speed increased from 20 rpm, but at 180 rpm, the permeation flux was almost the same for all membrane diameters, and the rotation speed was increased to 180 rpm. Larger values do not increase the permeation flux any further.

Therefore, in order to suppress a large increase in the power required for rotation and to obtain a sufficient permeation flux regardless of the size of the membrane diameter, the rotation speed of the membrane is set to 20 to 180 rpm. It is preferred that

(10) Interval between membrane and baffle and flux

When the membrane separation system shown in Fig. 13 is used and the number of rectangular paffles provided on one side and the other side of the membrane is two as shown in Fig. 2 (based on the surface area of the membrane) Figure 26 shows the results of an investigation of the relationship between the distance between the membrane and the baffle and the permeation flux when the projected area of the baffle is 50%).

As shown in FIG. 26, even if the distance between the membrane and the baffle is less than 2 mm or more than 18 mm, it is not possible to obtain a sufficiently high permeation flux for practical use.

Therefore, it is necessary to obtain a sufficient permeation flux without damaging the membrane. For this purpose, the distance between the membrane and the baffle is preferably 2 to 18 mm.

(11) Stability of permeation flux

Using the membrane separation system shown in Fig. 13 as the membrane separation device of the present invention, as shown in Fig. 2, having two rectangular baffles on one side and the other side of the membrane, respectively. Fig. 27 shows the results of an investigation of the change in permeation flux with respect to the operating time using the. As shown in FIG. 27, the permeation flux (A) does not change even after performing the membrane separation for 8 hours, which indicates that the membrane separation device of the present invention is excellent in the stability of the permeation flux.

(1 2) Concentration polarization reduction effect

(a) M g S 0 ₄ rejection

Using the membrane separation system shown in FIG. 13 and a membrane separation device of the present invention, as shown in FIG. 3, having four rectangular paffles on one side and the other side of the membrane, respectively. Fig. 28 shows the results of an investigation into the effect of reducing the concentration polarization on the outer peripheral velocity of the membrane by using. The MgS C rejection is defined by the following equation.

M g S C rejection = [1-1 (permeate concentration) Z (stock solution M g S C concentration)] X 100 (%)

That is, as the value of Mg SC rejection is high, indicates the superiority of the concentration polarization reducing effect, membrane separation apparatus of the present invention, have a high degree of M g S 0 ₄ rejection for practical use ten minutes are doing.

(b) N a C 1 rejection

Using the membrane separation system shown in FIG. 13 and a membrane separation device of the present invention having four rectangular baffles on one side and the other side of the membrane as shown in FIG. Figure 29 shows the results of an investigation of the effect of reducing the concentration polarization on the peripheral velocity of the membrane using Shown in The NaCl rejection rate (Hata) is defined by the following equation.

N a C 1 rejection rate 2 [1 (permeate concentration) / (stock solution N a C 1 concentration)] X 100 (%)

In other words, the larger the numerical value of the NaC 1 rejection ratio, the better the concentration polarization reduction effect. The membrane separation device of the present invention has a high Na C 1 rejection ratio sufficient for practical use. have.

(13) Effects of membrane diameter and membrane rotation speed on permeation flux with radial paffle

Fig. 30 shows the difference between the transmembrane pressure (the pressure obtained by subtracting the pressure on the permeate side from the pressure on the inflow side of the membrane) using the membrane separation system shown in Fig. 13 and using latex with a concentration of 1% by weight. The pressure actually used for permeation of the liquid to be treated is 200 kPa, the temperature is 25 ° C, the membrane is an ultrafiltration membrane (UF membrane), and the baffle is shown in Fig. 8. With the radial baffle shown (the number of baffles is 8) and the projected area of the baffle is 40% of the surface area of the film, the diameter of the film is changed in the range of 300 to 125 It is a result of investigating the relationship between the membrane rotation speed and the permeation flux.

Fig. 31 shows the results obtained by using the membrane separation system shown in Fig. 13 and using latex at a concentration of 30% by weight, at a transmembrane pressure of 400 kPa and at a temperature of 25 ° C. When the membrane is a UF membrane, the baffles are radial baffles (the number of baffles is 8) shown in Fig. 8, and the projected area of the baffle is 40% of the surface area of the membrane, the diameter of the membrane is 3 This is the result of investigating the relationship between the membrane rotation speed and the permeation flux in the range of 0 to 1250. In other words, Fig. 30 shows the membrane separation performance under low pressure and low concentration and low load conditions, and Fig. 31 shows the membrane separation performance under high pressure and high concentration and high load conditions. . As shown in Fig. 30, under a low load condition, the permeation flux sharply increases when the rotational speed reaches 50 rpm, when the membrane diameter is between 300 and 125 mm. Although increasing, the amount of increase in the permeation flux when the rotation speed is increased to 50 rpm or more is small.

As shown in Fig. 31, under high load conditions, the rate of increase of the permeation flux with respect to the increase in the number of revolutions when the membrane diameter increases is large, but the membrane diameter is 1 It can be seen that the permeation flux does not increase so much even if the force increases from 250 mm to 1250. Also, the maximum value of the permeation flux in the membrane diameter range of 300 to 125 mm is almost the same, and the permeation flux of the membrane with a diameter of 300 mm is also obtained at the rotation speed of 100 rpm. The bundle has reached a maximum.

Considering that a realistic number of membranes should be provided so that the machine would not be too long, and that the power required for rotation in proportion to the membrane diameter should not be too large, From Fig. 0 and Fig. 31, when the radial baffle is used, the diameter of the membrane is appropriate in the range of 300 to 100 mm, and the rotation speed of the membrane is 50 to 100 It can be seen that r pm is an economical and efficient operating range.

(14) Gap between the membrane and radial paffle on the permeation flux Fig. 32 shows the transmembrane pressure using the membrane separation system shown in Fig. 13 and latex with a concentration of 20% by weight. Is 400 kPa, the temperature is 25 ° C, the membrane is a UF membrane, the baffle is a radial baffle (eight baffles shown in Fig. 8), and the baffle is projected on the surface area of the membrane. In the case where the area is 40% and the rotation speed of the membrane is 550 rpm, the relationship between the flux and the gap between the membrane and the radial baffle is examined.

As shown in Fig. 32, there is no significant change in the permeation flux up to a gap of 12 mm between the membrane and the radial baffle. Above 12 mm, the flux decreases sharply.

If the gap between the membrane and the baffle is less than 2 mm, the membrane and the baffle may be easily contacted and the membrane may be damaged.If the gap between the membrane and the radial baffle exceeds 12 mm, the thirty-two As shown in the figure, the permeation flux is greatly reduced. Moreover, if the membrane and the baffle are too far apart, the overall length of the device will be long in order to secure the required membrane area, making it difficult to establish a real industrial device. Therefore, it is preferable that the gap between the film body and the radial baffle be in the range of 2 to 12 mm.

(15) Membrane Separation Performance of Radial Baffle and Ring Baffle Fig. 33 shows the use of the membrane separation system shown in Fig. 13 and the use of latex with a concentration of 30% by weight at a temperature of 25 ° C. When the membrane is a UF membrane and the rotation speed of the membrane is 550 rpm, the ring baffle 68 shown in FIG. 45 is used, and the radial baffle 28 shown in FIG. 8 is used. (The number of baffles is 8, and the projected area of the baffle is 40% with respect to the surface area of the membrane.) The result of investigating the relationship between the transmembrane pressure and the permeation flux is shown.

In FIG. 33, the symbol “〇” indicates a radial baffle, and the symbol “letter” indicates a ring-shaped baffle. As shown in Fig. 33, when the transmembrane pressure increases, the radial baffle has a higher permeation flux than the ring baffle, and the radial baffle has better membrane separation performance than the ring baffle. I understand.

(16) Number of radial baffles and flux

Fig. 34 shows the results obtained using the membrane separation system shown in Fig. 13 using latex at a concentration of 20% by weight, a transmembrane pressure difference of 400 kPa and a temperature of 25 ° C. When the membrane is a UF membrane, the baffle is a radial baffle shown in Fig. 8, the projected area of the baffle is 40% of the surface area of the membrane, and the rotation speed of the membrane is 550 rpm. It is the result of investigating the relationship between the number of projectile baffles and the permeation flux. As shown in Fig. 34, when the number of baffles is less than four, the transmission flux is small, and when the number of baffles increases, the transmission flux increases, but when the number of baffles increases, the transmission flux no longer increases. You can see that it does not grow.

Thus, it can be seen that the number of radial baffles is between 4 and 12 within the range where membrane separation can be performed efficiently.

(17) Projected area and transmission flux of radial baffle with respect to surface area of membrane

Fig. 35 shows the results obtained by using the membrane separation system shown in Fig. 13 and using latex at a concentration of 20% by weight, at a transmembrane pressure of 400 kPa and at a temperature of 25 ° C. When the membrane is a UF membrane, the baffle is a radial baffle shown in Fig. 8 (the number of paffles is eight), and the rotational speed of the membrane is 550 rpm, the radial baffle with respect to the surface area of the membrane is This is the result of investigating the relationship between the projected area (%) and the transmitted flux.-As shown in Fig. 35, the transmitted flux rapidly increases when the projected area of the radial buffer relative to the surface area of the membrane is 30% or more. It can be seen that when the projected area increases and the projected area exceeds 70%, the permeation flux decreases.

Thus, it can be seen that the projected area of the radial baffle with respect to the surface area of the membrane is in the range of 30 to 70% in which the membrane can be efficiently separated.

(18) Radial acceleration and flux during membrane rotation

Using the membrane separation system shown in Fig. 13, the results of investigating the relationship between the permeation flux and the radial acceleration during rotation of the membrane are shown in Figs. 36-42.

Fig. 36 to 42 show that the temperature is 25 ° C, the membrane is a UF membrane, the baffle is a ring-shaped baffle 68 shown in Fig. 45, and the transmembrane pressure (operating pressure) is a parameter. As the radial acceleration when the membrane rotates. Fig. 36, Fig. 37, Fig. 38, Fig. 39 show the latex concentration of 1% by weight, 10% by weight, and 20% by weight, respectively. , 30% by weight. As is clear from Figs. 36 to 39, almost constant proportionality is observed between the radial acceleration and the permeation flux under all operating conditions regardless of the latex concentration. The higher the pressure, the higher the permeation flux. Also, the permeation flux increases as the radial acceleration increases, but as the latex concentration decreases, the relationship in the low acceleration range becomes more pronounced. Than the third 7-3 9 figure, in the high concentration of latex concentration of 1 0% by weight or more, if the radius Direction acceleration and 2 0 Om / sec ² or more, can not be obtained to some extent transparent flux, From FIG. 36, it can be seen that at a low latex concentration of less than 10% by weight, a practically sufficient permeation flux can be obtained in a radial acceleration range of 100 mZsec ² or more.

Figs. 40 to 42 show the results of Figs. 36 to 39 with different parameters arranged at different temperatures.The temperature is 25 ° C, the membrane is UF membrane, and the puffer is Fig. 45. Fig. 40, Fig. 41, and Fig. 42 show the results of a study of the relationship between the radial flux during rotation of the membrane and the permeation flux with the latex concentration as a parameter in the ring-shaped baffle 68 shown in Fig. 40. The figures show the cases where the transmembrane pressure (operating pressure) is 200 kPa, 300 kPa, and 400 kPa, respectively. As is evident from Figs. 40 to 42, there is a nearly constant proportional relationship between the radial acceleration and the flux under all operating conditions, regardless of the operating pressure. The lower the concentration, the higher the permeation flux.

In addition, as shown in Fig. 43 (a), a number of holes with a predetermined shape are punched out, or as shown in Fig. 43 (b), the baffle is etched by etching. The back side Alternatively, as shown in Fig. 43 (c), the baffle can be pressed against a roll with an uneven pattern (by embossing), and the baffle can be used with an uneven pattern on the front and back surfaces. . Although FIG. 43 (a) shows the case of a radial baffle, it is also possible to provide a punched hole in a paffle of another shape, and it is possible to use the etching process shown in FIG. The embossing in Fig. (C) can be applied to all shapes of baffles. The turbulence promoting effect of the baffle is increased by etching or embossing of these punched holes, and the permeation flux is increased.

The container 2 may have a shape other than a cylindrical shape, for example, a quadrangle or more polygon, or a tank without an upper lid.

In this embodiment, an example in which the apparatus is used horizontally is described. However, the present invention is not limited to this, and the apparatus can be used vertically. When the device is placed vertically, the load of the membrane is not directly applied to the rotating shaft, so that the rotating shaft can be made longer than the device placed horizontally, and a large-sized membrane separation device can be manufactured.

[Possibility of industrial use]

Since the present invention is configured as described above, there is no need for assembling the apparatus, the cost is low, the pressure loss is small, the permeation process is performed efficiently, and the membrane separation performance is effectively improved. It is suitable for use as a rotary type membrane separation device that can be used in various applications.

Claims

In a rotary membrane separation device having a rotary shaft arranged so as to penetrate a container having a supply inlet for a liquid to be treated, it is possible to transfer the liquid that has passed through the container. A membrane having a structure is mounted on the rotating shaft, and has an outlet connected to the membrane to discharge a permeated liquid. A plurality of gaps are provided between the membrane and the membrane on both sides of the membrane. A rectangular paffle is arranged, and a liquid flow path connected to the supply inlet of the liquid to be treated is provided on the inner wall surface of the container, and a plurality of rectangular baffles are sandwiched across the rotation axis from near one inner wall of the container to the other. Rotary membrane separation devices arranged parallel to each other up to the vicinity of the inner wall. In a rotary membrane separation device having a rotary shaft arranged so as to penetrate a container having a supply inlet for a liquid to be treated, a membrane having a structure capable of transferring the liquid that has passed through the container. Is mounted on the rotating shaft, and has an outlet connected to the membrane for discharging the permeated liquid.Hook-shaped baffles are provided on both sides of the membrane with gaps between the membrane and the membrane. A liquid flow path connected to the supply inlet of the liquid to be treated is provided on the inner wall surface of the container, and a plurality of hook-shaped baffles are arranged symmetrically with respect to the diameter of the film body with the rotation axis interposed therebetween; or Rotary membrane separation device arranged symmetrically with respect to the rotation axis. In a rotary membrane separation device having a rotary shaft arranged so as to penetrate a container having a supply inlet for a liquid to be treated, a membrane having a structure capable of transferring the liquid that has passed through the container. Is mounted on the rotating shaft, has an outlet connected to the membrane, and discharges a permeated liquid, and an S-shaped baffle is provided on both sides of the membrane with a gap between the membrane and the membrane. A liquid passage connected to the supply inlet of the liquid to be treated is provided on the inner wall surface of the container, and a plurality of S-shaped baffles are arranged point-symmetrically with respect to the rotation axis with the rotation axis interposed therebetween. Inverted membrane separation equipment.

In a rotary membrane separation device having a rotary shaft arranged so as to penetrate a container having a supply inlet for a liquid to be treated, a membrane having a structure capable of transferring the liquid that has passed through the container. Is mounted on the rotating shaft, has an outlet connected to the membrane, and discharges the permeated liquid, and provides an arc-shaped paffle with a gap between the membrane and the membrane on both sides of the membrane. A liquid flow path connected to the supply inlet of the liquid to be treated is provided on the inner wall surface of the container, and a plurality of arc-shaped baffles are arranged line-symmetrically with respect to the diameter of the film body with respect to the rotation axis, or the rotation axis is Rotary membrane separation device arranged symmetrically with respect to point.

5. The rotary membrane separator according to claim 1, wherein the projected area of the baffle with respect to the surface area of the membrane is 10 to 90%.

6. The rotary membrane separator according to claim 1, wherein both ends of the rectangular baffle are supported and fixed by supports independent of the container wall.

7. The rotary membrane separator according to claim 2, wherein both ends of the hook-shaped baffle are supported and fixed by supports independent of the container wall.

8. The rotary membrane separator according to claim 3, wherein both ends of the S-shaped baffle are supported and fixed by supports independent of the vessel wall.

9. The rotary membrane separator according to claim 4, wherein both ends of the arc-shaped baffle are supported and fixed by supports independent of the vessel wall.

10. The number of paffles provided on one side of the film body is 20 or less. Claims 1, 2, 3, 4, 5, 6, 9 A rotary membrane separator according to paragraph 7, paragraph 8, or paragraph 9

1. The rotation speed of the film body is 1 to 30 m / sec on the outer circumference. Claims 1, 2, 3, 4, 5, 6, and Rotary type according to paragraph 7, paragraph 8, paragraph 9 or paragraph 10 Membrane separation device.

1 2. Claims 1, 2, 3, 3, 4, 5, 6, and 7 in which the diameter of the membrane is 200 to 110 , Clause 8, Clause 9, Clause 10 or Clause 11;

1 3. The rotation speed of the membrane is 20 to 180 rpm. Claims 1, 2, 3, 4, 5, 5, 6, The rotary membrane separator according to any one of Items 7, 8, 9, 9, 10, 11, and 12.

1 4. Claim 1 wherein the thickness of the baffle is 1 to 2 Omm. Clause 2, Clause 3, Clause 4, Clause 5, Clause 6, Clause 7, Clause 8. Item 9. The rotary membrane separation device according to Item 9, Item 10, Item 11, Item 12, or Item 13.

1 5. The width of the baffle is 0, 1 to 40% of the diameter of the membrane body. Claims 1, 2, 3, 4, 5, 6, 7 Item 15. The rotary membrane separation device according to Item 8, Item 9, Item 10, Item 11, Item 11, Item 12, Item 13, or Item 14.

1 6. The gap between the membrane and the baffle is 2 to 18 mm. Claims 1, 2, 3, 3, 4, 5, 6, and 7. Clause 8, Clause 9, Clause 10, Clause 11, Clause 12, Clause 13, Clause 13. The rotary membrane separator according to clauses 14 or 15.

17. The ratio of the inner diameter of the container to the diameter of the membrane is 1.03 to 3.00. Clause 6, Clause 7, Clause 8, Clause 9, Clause 10, Clause 11, Clause 12, Clause 13, Clause 14, Clause 15, Clause 15 or Clause 16 Rotary membrane separation device.

1 8. The rotating shaft is hollow and a small hole is provided in the shaft. Claims 1 and 2, wherein the permeated liquid transfer path of the permeable membrane is configured to communicate with a small hole provided in the rotation shaft. Clauses 5, 6, 7, 7, 8. Clause 9, Clause 10, Clause 11, Clause 12, Clause 13, Clause 14, Clause 15, Clause 15, Rotary membrane separation as described in Paragraph 16 or 17. 9. A rotating shaft is arranged so as to penetrate the container having the supply inlet for the liquid to be treated, and the permeated liquid in the container is transferred. A rotary type membrane separation device, comprising: a membrane having a structure capable of performing the above-mentioned operation, mounted on the rotating shaft, and a baffle provided with a gap between the membrane and the membrane on both sides of the membrane. treatment liquid radial acceleration at the time of the film body rotating at high concentrations operated Te ² 0 0 m / sec 2 or more ranges smell, radial acceleration at the time of the film body rotating when the liquid to be treated lightly 1 0 0 mZsec ² or more Rotary membrane separation device, characterized by operating in the range.

0. A rotating shaft is provided so as to penetrate a container having a supply inlet for the liquid to be treated, and a film having a structure capable of transferring the permeated liquid in the container is provided on the rotating shaft. A rotating membrane separation device which is mounted and has a gap between the membrane body on both sides of the membrane body and a plurality of baffles arranged radially toward the inner wall of the container around the rotation axis, A rotary type membrane separation apparatus characterized in that the membrane has a diameter of 300 to 100 mm and operates at a rotation speed of the membrane of 500 to 1000 rpm.

1. The rotary membrane separation device according to claim 20, wherein the number of radial baffles is 4 to 12.

2. The rotary membrane separator according to claim 20, wherein a projected area of the radial baffle with respect to a surface area of the membrane is 30 to 70%.

23. The rotary membrane separation according to claim 20, 20 or 21, wherein the gap between the membrane and the radial baffle is 2 to 12 thighs.

24. The rotating membrane separation according to claim 20, wherein the rotation speed of the membrane at the outer periphery is l to 30 m / sec. apparatus.

25. The width of the radial paffle is 0.1 to 40% of the diameter of the film body, and the width of the radial paffle is 0.1 to 40% of the diameter of the film body. Item 8. The rotary membrane separation device according to Item 1.

2 6. A rotating shaft is arranged so as to penetrate the container having the supply inlet for the liquid to be treated, and the film having a structure capable of transferring the permeated liquid in the container is connected to the rotating shaft. A rectangular baffle, a hook-shaped baffle, and an S-shape having an outlet connected to the membrane and discharging the permeated liquid by being connected to the membrane, and providing a gap between the membrane and the membrane on both sides of the membrane A method in which a baffle or an arc-shaped baffle is arranged, and a membrane is separated using a rotary membrane separation device having a liquid flow path connected to a supply inlet of a liquid to be treated on an inner wall surface of the container. While introducing the liquid to be treated into the container and lowering the pressure of the permeated liquid side from the liquid to be treated side of the membrane, rotating the rotating shaft and replacing the liquid to be treated between the membranes, The permeate that has passed through is drained from the container outlet, and the liquid to be treated is permeated and concentrated. How to membrane separation.

27. The membrane separation method according to claim 26, wherein the pressure of the liquid to be treated introduced into the container is 0.05 MPa or more.

2 8. A rotating shaft is arranged so as to penetrate the container having the supply inlet for the liquid to be treated, and the film having a structure capable of transferring the permeated liquid in the container is rotated by the rotating shaft. And a baffle is provided on both sides of the membrane with a gap between the membrane and the membrane. This is a method of performing membrane separation using a rotary membrane separation apparatus.When the liquid to be treated is at a high concentration, the radial acceleration during rotation of the membrane is operated within a range of 200 mZsec ² or more. There membrane separation method according to the rotary membrane separation device, wherein the radial acceleration at the time of the film body rotating at low concentration is operated at 1 0 O m / sec ² or more ranges.

9. A rotating shaft is provided so as to penetrate the container having the supply inlet for the liquid to be treated, and a film having a structure capable of transferring the permeated liquid in the container is provided on the rotating shaft. The membrane is mounted using a rotary membrane separation device in which a plurality of baffles are arranged radially toward the inner wall of the container around the rotation axis with a gap provided between the membrane and the membrane on both sides of the membrane. A method for separating a membrane, wherein the membrane has a diameter of 300 to 100 mm and the rotation speed of the membrane is in a range of 50 to 100 rpm. Separation method using the device.

0. The method of claim 29, wherein the gap between the membrane and the baffle is operated as 2 to 12 bandages.