JP2001121143A - Membrane separator - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a membrane separator having such constitution that the membrane washing efficiency of a backwashing liquid may be enhanced, the settlement of pollutants prevented and the treatment efficiency of the membrane separation treatment enhanced. SOLUTION: A tubular membrane module 90 of this membrane separator has the constitution exactly the same as the constitution of the conventional tubular membrane module except that a multiplicity of small moving/colliding bodies 91 are packed at a packing rate of about 50% into a liquid distributing chamber 30 and a liquid collecting chamber 34 and the inlet of the liquid distributing chamber and the outlet of the liquid collecting chamber are provided with batten plates 94 for preventing the outflow of the moving/colliding bodies 91. The moving/ colliding bodies are solids formed by providing plastic spherical bodies having a diameter of 20 mm and a specific gravity of 1.5 with a multiplicity of small conical projections. With this tubular membrane module, the moving/colliding bodies are freely moved around by the flow of the liquid to be treated or concentrated liquid and are brought into collision against the pollutants deposited on a lower end mirror plate 42 or an upper partition plate 28 or the gradually deposited pollutants, by which the pollutants are peeled or agitated. Since the pollutants are entrained in the liquid to be treated and the concentrated liquid at all times, the sudden and temporary inflow of a large amount of the pollutants into the tubular membranes and the occurrence of problems, such as closure, as experienced with the conventional devices do not occur.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a membrane separation apparatus using an internal pressure type tubular membrane as a membrane separation means, and more particularly, to a cross-flow type membrane separation apparatus capable of improving the processing efficiency of a membrane separation treatment. It is about. In the present invention, the term "tubular membrane" includes both those having an inner diameter of a tube generally called a tubular membrane of about 5 to 25 mm and those having an inner diameter of about 0.1 to 5 mm generally called a hollow fiber membrane. Collectively.

[0002]

2. Description of the Related Art Treated water having low turbidity or treated liquid is obtained by removing entrained suspended matter from treated water such as general water, power plant condensed water, industrial water, or industrial waste liquid. As means for obtaining the above, a membrane separation apparatus using a tubular membrane as a membrane separation means has been frequently used.

Here, the configuration of a conventional cross-flow type membrane separation apparatus will be described with reference to FIGS. 6 and 7. FIG. FIG.
Is a flow sheet showing the configuration of a conventional cross-flow type membrane separation apparatus, and FIG. 7 is a longitudinal sectional view showing the configuration of an internal pressure type tubular membrane module used in the conventional membrane separation apparatus.
As shown in FIG. 6, a conventional cross-flow type membrane separation apparatus 10 performs a membrane separation process on a liquid to be treated to flow out a processing liquid having a low turbidity and a part of the processing liquid as a concentrated liquid. Having a tubular membrane module 12 to be formed. Further, the membrane separation apparatus 10 includes a processing target liquid tank 14 that stores a processing target liquid to be subjected to membrane separation processing by the tubular membrane module 12, and a processing target liquid pipe 16 from the processing target liquid tank 14 to the tubular membrane module 12. A processing liquid tank 18 for storing a processing liquid flowing out of the tubular membrane module 12 via the processing liquid pipe 20, and a concentrated liquid from the tubular membrane module 12. It has a concentrate pipe 24 for returning to the tank 14.

[0004] As shown in FIG. 7, the tubular membrane module 12 is partitioned by a lower partition 26 and an upper partition 28 in order, and overlaps from bottom to top.
And a vertical container 36 having a concentrated liquid collecting chamber (hereinafter, simply referred to as a liquid collecting chamber) 34 and a number of internal pressure type tubular membranes 38 disposed in the processing liquid chamber 32. I have. The tubular membrane 38 has a lower end and an upper end fixed to the lower partition 26 and the upper partition 28 so as to communicate with the liquid distribution chamber 30 and the liquid collection chamber 34, respectively. Extend to. The tubular membrane 38 is a hollow fiber membrane formed of a usual filtration membrane, a microfiltration membrane, an ultrafiltration membrane, a nanofiltration membrane, or the like, or a tubular membrane.

[0005] The lower diaphragm 26 and the upper diaphragm 28 are usually
The end portion of the tubular film 38 is formed as an adhesive layer which is fixed with an adhesive at a distance. The processing liquid chamber 32 is divided into a film inside and a film outside by a tubular film 38, and has a processing liquid port 39 connected to the processing liquid pipe 20 to allow the processing liquid to flow out. In the tubular membrane module 12, the liquid distribution chamber 3
0 and the liquid collection chamber 34 are formed by a lower head plate 40 and an upper head plate 42, respectively.
It communicates with 4. The lower head plate 40 and the upper head plate 42
The respective flanges 44 and 46 and the flanges 50 and 52 of the body 48 forming the processing liquid chamber 32 are flanged and connected to the body 48 to form an integral container 36.
Is composed.

In the tubular membrane module 12, the liquid to be treated is introduced into the membrane of the tubular membrane 38 through the liquid distribution chamber 30, and the membrane is separated by the tubular membrane 38 in a cross-flow system, and the treatment liquid is supplied to the treatment liquid chamber 32. The liquid is discharged from the upper processing liquid port 39,
0 is stored in the processing liquid tank 22. At the same time,
The liquid to be processed, which has passed through the tubular membrane 38 without passing through, is returned as a concentrated liquid to the liquid tank 14 via the liquid collecting chamber 34 and the concentrated liquid pipe 24.

In the present membrane separation apparatus 10, the flow rate of the liquid to be treated flowing in the tubular membrane 38 in the above-mentioned filtration step is increased, for example, at the outlet of the tubular membrane 38, that is, near the inlet of the liquid collecting chamber 34.
By setting the pressure in the range of 1 to 1.0 m / sec, most of the suspension adhered and deposited on the surface of the tubular membrane 38 by the hydraulic shear force of the liquid to be treated is peeled off, and discharged together with the concentrated liquid. ing.

After the above-described filtration step has been performed for a predetermined time, the tubular membrane 38 is backwashed in order to remove the suspended matter adhering to the membrane surface without peeling. In order to backwash the tubular membrane 38, the membrane separation device 10 uses a processing solution as a backwash solution. Therefore, as shown in FIG. 6, the processing liquid is supplied from the processing liquid tank 22 via the backwashing liquid pipe 54 connected to the processing target liquid pipe 20 and the processing liquid tank 22 via the backwashing liquid pipe 54 to the processing liquid chamber of the tubular membrane module 12. Backwash liquid pump 56 to be fed into
6 and a backwash drainage pipe 58 branching off. At the time of backwashing, the processing liquid is sent from the processing liquid tank 22 to the tubular membrane module 12 via the backwashing liquid pipe 54 and the processing liquid pipe 20 by the backwashing liquid pump 56 as a backwashing liquid, and the tubular film 38 is reversely washed. To the liquid distribution chamber 3 while washing the inner surface of the tubular membrane 38
0, the liquid is discharged to the outside via the liquid pipe 16 to be treated and the backwash drain pipe 58. Further, when the filtration step and the backwashing step are repeated to perform the filtration treatment of the liquid to be treated for a long period of time, even if the tubular membrane 38 is finally backwashed, the transmembrane pressure difference does not drop below a predetermined value. That is, since the filtration performance is not restored,
In such a case, the chemical cleaning of the tubular film 38 is performed using a chemical such as an acid, an alkali, or an oxidizing agent.

[0009]

However, the above-mentioned conventional membrane separation apparatus has the following problems. First, turbidity deposits on the upper diaphragm, which is the bottom of the liquid collection chamber, and eventually the outlet of the tubular membrane partially blocks, resulting in a decrease in membrane separation efficiency. Secondly, the membrane cleaning effect of the reverse cleaning of the tubular membrane is still lower, and the transmembrane pressure of the tubular membrane tends to increase.

SUMMARY OF THE INVENTION It is an object of the present invention to provide a membrane separation apparatus having a structure in which suspended matter is not deposited on an upper partition in a liquid collecting chamber and having a high membrane washing effect of back washing.

[0011]

The inventors of the present invention have studied the cause of the low backwashing effect and the tendency of turbid matter to be easily deposited in the liquid collecting chamber, and have found the following. The first problem is that the collection chamber 3
In addition to the fact that the flow path in 4 is much wider than the flow path of tubular membrane 38, a part of the liquid to be treated that flows into liquid distribution chamber 30 passes through tubular membrane 38 and moves to the processing chamber side. Liquid collection chamber 3
This occurs because the amount of the liquid to be treated flowing into the liquid distribution chamber 4 is smaller than the amount of the liquid to be treated flowing into the liquid distribution chamber 30. That is, the liquid to be treated (hereinafter simply referred to as a concentrated liquid) that has passed without passing through the tubular membrane 38 enters the liquid collecting chamber 34 and has a flow rate of 1/10 to 1 of the flow rate in the tubular membrane 38. / 10
It drops to about 0. As a result, the tubular membrane 3
The suspension, particularly the suspension having a relatively large particle size, which has been peeled off and entrained from the membrane surface of No. 8, flows into the concentrate tube 24 together with the concentrate based on the difference in specific gravity from the liquid to be treated. Without settling, as shown in FIG. 8, they settle in the liquid collecting chamber 34, accumulate on the upper partition 28, and then deposit. The suspension gradually accumulates and accumulates on the upper diaphragm 28, and eventually falls into the tubular membrane 38 and reattaches to the membrane surface of the tubular membrane 38,
Further, the opening at the upper end of the tubular membrane 38 may be closed, causing an increase in the transmembrane pressure difference. As a result, chemical cleaning is required at a short frequency.

The second problem arises because the flow path in the liquid distribution chamber 30 is much wider than the flow path of the tubular membrane 38.
That is, since the flow path in the liquid distribution chamber 30 is much wider than the flow path of the tubular membrane 38, the flow rate of the liquid in the liquid distribution chamber 30 is
8 is about ２〜 to 1/10 of the flow rate of the liquid in FIG. Therefore, at the time of back washing, the turbid material that has peeled off from the inner surface of the tubular membrane 38 and entered the liquid distribution chamber 30 accompanying the back washing liquid settles in the liquid distribution chamber 30 as shown in FIG. It deposits on the bottom plate of the liquid distribution chamber 30. Then, along with the resumption of the filtration step, the liquid again accompanies the liquid to be treated and enters the tubular membrane 38 and is captured. By repeating this, the cleaning efficiency of the reverse cleaning is reduced, and the operation efficiency is reduced. Moreover, the turbid matter captured by the tubular membrane 38 is usually agglomerated on the membrane surface and easily aggregates in the liquid distribution chamber 30, so that the above-described phenomenon is promoted.

The first problem has a greater influence on the membrane separation efficiency of the tubular membrane module. Therefore, in order to increase the membrane separation efficiency of the tubular membrane module,
First, it was found through experiments that it was important to solve the first problem.

Therefore, the present inventor has proposed, as a first measure,
It has been considered that the flow path of the liquid collection chamber is narrowed, and preferably the flow path of the liquid distribution chamber is also narrowed to increase the flow rate of the concentrated solution, and further the flow rates of the backwashing liquid and the liquid to be treated. Also, as a second measure,
A small moving / colliding body that moves freely by the flow of the concentrated liquid or the liquid to be treated is placed in the collecting chamber, preferably also in the liquid distribution chamber, and the moving / colliding body is deposited on the suspended turbid matter and the turbid body being deposited. Colliding and peeling, or stirring, respectively,
The inventors of the present invention have completed the present invention through repeated experiments in consideration of entrainment with the concentrated liquid and the liquid to be treated.

In order to achieve the above object, a membrane separation apparatus according to the present invention (hereinafter, referred to as a first invention) is provided with a liquid distribution chamber and a processing liquid chamber partitioned by a crossing lower partition and an upper partition. And a vertical container having a concentrated liquid collecting chamber at a lower part, a central part, and an upper part. The vertical container has a lower part at a lower end and an upper end so as to communicate with the liquid distribution chamber and the concentrated liquid collecting chamber, respectively. A tubular membrane module having an internal pressure type tubular membrane fixed to the plate and the upper partition and extending in the processing liquid chamber in the longitudinal direction is provided.The liquid to be treated is introduced into the liquid distribution chamber, and the membrane is separated by a cross flow method. In a membrane separation device in which the processing liquid flows out from the processing liquid chamber and the concentrated liquid flows out through the concentrated liquid collecting chamber, the flow rate of the concentrated liquid in the concentrated liquid collecting chamber is increased in the processing target flowing through the tubular membrane. 0.5 to 2.0 times the flow rate of the liquid, more preferably 0.5 to 2.0 times. To be in the range of 1.0, it is characterized in that the concentrate collection liquid chamber flow paths are formed.

Preferably, in addition, the flow rate of the liquid to be treated in the liquid distribution chamber is in the range of 0.5 to 2.0 times, more preferably 0.5 times, the flow rate of the liquid to be treated flowing in the tubular membrane. The flow path of the liquid distribution chamber is formed so as to be in a range of 1.0 to 1.0 times.

In the present invention, there is no limitation on the flow path forming means as long as the flow paths in the liquid distribution chamber and the concentrated liquid collecting chamber are formed so as to have the flow velocity specified in the present invention. For example, the liquid distribution chamber and the concentrated liquid collecting chamber may be designed and manufactured so as to have the flow rate specified by the present invention, and may be manufactured. A plastic filler is filled in the liquid distribution chamber and the concentrated liquid collecting chamber, or a flow path forming body described later in the embodiment is provided in the liquid distribution chamber and the concentrated liquid collecting chamber to narrow the flow path. You can also. At this time, a flow path is formed so as to minimize the flow velocity distribution in the liquid distribution chamber and the concentrated liquid collection chamber.

Another membrane separation apparatus according to the present invention (hereinafter referred to as a second
The invention comprises a vertical container having a liquid distribution chamber, a processing liquid chamber, and a concentrated liquid collecting chamber partitioned by a crossing lower partition and an upper partition at the lower, center, and upper portions. An inner pressure type tubular membrane fixed to a lower partition and an upper partition at lower and upper ends so as to communicate with the liquid distribution chamber and the concentrated liquid collecting chamber, respectively, and extending in the processing liquid chamber in the vertical direction. The treatment liquid is introduced into the liquid distribution chamber, the membrane is separated by a cross-flow method, the treatment liquid flows out from the treatment liquid chamber, and the concentrated liquid flows out through the concentrated liquid collecting chamber. The membrane separation apparatus is characterized in that a solid movement / collision body that freely moves by the flow of the concentrated liquid in the concentrated liquid collecting chamber is accommodated in the concentrated liquid collecting chamber.

Preferably, in addition, a solid motion / collision body which freely moves by the flow of the liquid in the liquid distribution chamber is accommodated in the liquid distribution chamber.

The shape of the solid moving / colliding body used in the second invention can be freely moved by the flow of the liquid to be treated in the liquid distribution chamber or the flow of the concentrated liquid in the concentrated liquid collecting chamber. wall,
There is no restriction as long as it has a shape that collides with the lower partition, the wall of the liquid collecting chamber, the upper partition, etc., for example, a sphere, an ellipsoid, a cylinder,
Various objects such as a rectangular object, a polyhedron, a cone, and the like, and those having grooves, projections, fins, and the like provided on the surface of the shaped object can be used. Moreover, a ribbon-shaped thing may be used. Specific examples of the moving / colliding body include a granular material such as sand or granular activated carbon, or a plastic molded product molded into the above shape. The size of the motion / collision body is
When a hollow fiber having an inner diameter of about 0.1 to 0.8 mm, which is about 2 to 100 times the inner diameter of the tubular membrane, is used as the tubular membrane, it also depends on the size of the liquid distribution chamber or the liquid collection chamber. However, the range may be 2 mm or more and 50 mm or less.

The specific gravity of the motion / collision body is determined by the motion / collision body freely moving in the liquid distribution chamber or the liquid collection chamber, and the walls of the liquid distribution chamber, the lower partition, the wall of the liquid collection chamber, the upper partition, etc. In the liquid distribution chamber, the solid material adhered to the liquid distribution chamber side plate surface of the lower partition plate is efficiently peeled off. Considering the efficient removal of solids deposited on the plate, the specific gravity of the moving / colliding body to be placed in the liquid distribution chamber is 1.0 or less, more preferably 0.1%.
A range of 9 to 1.0 is suitable, and the specific gravity of the moving / colliding body to be put into the liquid collecting chamber is 1.0 or more, more preferably 1.
Those having a range of 0 to 3.0 are preferred. Also, the specific gravity is reduced for a large motion / collision object, and the specific gravity is increased for a small motion / collision object. The number of moving / colliding objects is
One or a plurality of moving / colliding bodies are preferably accommodated to increase the number of collisions with walls such as a liquid distribution chamber and a liquid collection chamber. The filling rate of the movement / colliding body with respect to the volume of the liquid distribution chamber or the collection chamber is 90% or less, preferably 40% or more.
0% or less.

In the second aspect of the present invention, preferably, the solid movement / free movement freely performed by the flow of the concentrate in the concentrate collecting chamber is provided.
By storing the colliding body in the concentrated liquid collecting chamber, the flow rate of the concentrated liquid in the concentrated liquid collecting chamber is in the range of 0.5 to 2.0 times the flow rate of the liquid to be treated flowing in the tubular membrane. Preferably, the flow path in the concentrated liquid collecting chamber is narrowed so as to be in the range of 0.5 to 1.0. More preferably, a solid motion / collision body that freely moves by the flow of the liquid in the liquid distribution chamber and the flow of the concentrated liquid in the concentrated liquid collecting chamber is accommodated in the liquid distribution chamber and the concentrated liquid collecting chamber, respectively. Thereby, the flow rate of the liquid to be treated in the liquid distribution chamber, and the flow rate of the concentrated liquid in the concentrated liquid collecting chamber are in the range of 0.5 to 2.0 times the flow rate of the liquid to be treated flowing in the tubular membrane. Preferably, the flow path in the liquid distribution chamber and the flow path in the concentrated liquid collecting chamber are each narrowed so as to be in the range of 0.5 to 1.0 times. Accordingly, the flow velocity can be increased by narrowing the flow path, and the deposited suspended matter and the suspended suspended matter can be agitated by the moving / colliding body to be accompanied by the liquid to be treated or the concentrated liquid. .

The membrane separation apparatus according to the present invention can be applied without being limited to the properties of the liquid to be treated. For example, not only raw water for industrial and water supply such as river water, well water and lake water, but also public sewage, industrial effluent, etc. In particular, it can be optimally applied to raw water having a turbidity ranging from several degrees to several hundred degrees or a liquid to be treated.

[0024]

Embodiments of the present invention will be described below in detail with reference to the accompanying drawings. Embodiment 1 This embodiment is an example of an embodiment of a membrane separation device according to the first invention, and FIG. 1 is a cross-sectional view showing a configuration of a tubular membrane module provided in the membrane separation device of this embodiment. FIG. In the membrane separation device of the present embodiment, the tubular membrane module 60 provided in the membrane separation device of the embodiment is different from the conventional membrane separation device 10.
Except that the configuration is different from the tubular membrane module 12 of
It has the same configuration as the conventional membrane separation device 10.

As shown in FIG. 1, the tubular membrane module 60 has the same configuration as the conventional tubular membrane module 12 except that the configurations of the liquid distribution chamber 62 and the liquid collection chamber 64 are different. In the liquid distribution chamber 62 and the liquid collection chamber 64 of the present tubular membrane module 60, the flow rate of the liquid in the liquid distribution chamber 62 and the liquid collection chamber 64 is, for example, about 0.6 times the flow rate of the liquid in the tubular membrane 38. In addition, the flow paths of the liquid distribution chamber 62 and the liquid collection chamber 64 are made of a plastic material attached to the liquid distribution chamber 62 and the liquid collection chamber 64 so that the flow velocity in each part of the room is uniform and the flow velocity distribution is not generated as much as possible. Are narrowed by the flow path forming bodies 66 and 68 formed by the hollow bodies.

The flow path forming body 66 has a lower curved surface 70 having the same shape as the inner surface of the lower end plate 42, and has an upper curved surface 72 formed so as to suppress the flow velocity distribution, as shown in FIG. It has the same shape as a rotating body whose section is rotated. On the other hand, the flow path forming body 68 has an upper curved surface 74 having the same shape as the inner surface of the upper end plate 40, and has a lower curved surface 76 formed so as to suppress the flow velocity distribution. It has the same shape as a rotating body formed by rotating. The flow path forming bodies 66 and 68 are respectively provided with the lower head plate 42 and the upper head plate 4.
It is fixed to 0 by a usual fixing means, for example, bonding with an adhesive, fastening with an embedded bolt, or the like.

In this embodiment, the flow paths of the liquid distribution chamber 62 and the liquid collection chamber 64 are about 0.6 times the flow velocity of the liquid in the tubular membrane 38, and the flow velocity distribution in the chamber is suppressed as much as possible. As a result, the turbidity in the backwashing liquid is deposited in the liquid distribution chamber 62 as in the prior art, reducing the membrane cleaning effect of the backwashing, and the turbidity in the concentrated liquid is collected. There is no possibility that the filtration efficiency is lowered by depositing in the liquid chamber 64.

Modification of Embodiment 1 This modification is a modification of the tubular membrane module of Embodiment 1, and FIG. 2 shows the configuration of the tubular membrane module provided in the membrane separation apparatus of this modification. It is sectional drawing. The configuration of the tubular membrane module 80 of this modified example is the same as that of the tubular membrane module 60 of Embodiment 1 except that the configurations of the flow path forming bodies 86 and 88 attached to the liquid distribution chamber 82 and the liquid collection chamber 84 are different. It has. The flow path forming bodies 86 and 88 of this modification example
As shown in FIG. 2, it has a short columnar shape penetrating many through holes 89, and the total cross-sectional area of the through holes 89 is
Is approximately twice as large as the total cross-sectional area. The diameter of the through hole 89 is about twice the diameter of the tubular membrane 38. Further, the distance between the flow path forming body 86 and the lower partition plate 26 and the flow path forming body 88
And the distance between the upper partition plate 28 and the upper partition plate 28 are determined such that the flow rate of the backwash liquid and the flow rate of the concentrated liquid are, for example, about 0.6 times or less of the flow rate of the liquid in the tubular membrane 38. Similarly, the space above the flow path forming body 86 and the space above the flow path forming body 88 respectively have a flow rate of the backwash liquid and a flow rate of the concentrated liquid that are approximately equal to, for example, about the flow rate of the liquid in the tubular membrane 38. It is determined to be 0.6 times.

Embodiment 2 This embodiment is an example of the embodiment of the membrane separation apparatus according to the second invention. FIG. 3 shows the configuration of the tubular membrane module provided in the membrane separation apparatus of this embodiment. FIG. 4 is a perspective view showing the structure of the moving / colliding body. The membrane separation apparatus of the present embodiment is different from the conventional membrane separation apparatus except that the tubular membrane module 90 provided in the membrane separation apparatus of the embodiment is different from the tubular membrane module 12 of the conventional membrane separation apparatus 10. It has the same configuration as the device 10.

As shown in FIG. 3, in the tubular membrane module 90, the liquid distribution chamber 30 and the liquid collection chamber 34 are each filled with a large number of small motion / colliding bodies 91 at a filling rate of about 50%. And an inlet and a liquid collecting chamber 3 in the liquid distribution chamber 30.
4 is provided with a baffle 94 for preventing the movement / impingement body 91 from flowing out at the outlet of the conventional tubular membrane module 12.
It has the same configuration as. As shown in FIG. 4, the motion / collision body 91 is a solid material having a plastic sphere 92 having a diameter of 20 mm and a specific gravity of 1.5 and a plurality of small conical projections 93 provided on a plastic sphere 92.

In the tubular membrane module 90 of this embodiment, a plurality of small motion / colliding bodies 91 placed in the liquid distribution chamber 30 and the liquid collection chamber 34 move freely around by the flow of the liquid to be treated or the concentrated liquid. The turbidity deposited on the lower head plate 42 or the upper partition plate 28 and the turbidity being deposited are collided with and peeled off or agitated, so that they are always entrained in the liquid to be treated and the concentrated liquid, respectively. Thus, a large amount of turbidity does not suddenly flow into the tubular membrane and cause problems such as blockage.

The shape of the moving / colliding body is not limited to this, and may be, for example, a simple sphere, or a sphere 95 provided with a spiral groove 96 as shown in FIG. ,
As shown in FIG. 5B, there are various types such as a type in which a spiral fin 98 is provided on a cylindrical body 97. FIG.
The moving / colliding body shown in (a) and (b) has a spiral groove 9.
By providing the fins 6 or the spiral fins 98, they can move freely while rotating by the flow of the liquid to be treated or the concentrated liquid. FIGS. 5A and 5B are perspective views of the moving / colliding body, respectively.

[0033]

According to the structure of the present invention, the flow rate of the concentrated liquid in the concentrated liquid collecting chamber and the flow velocity of the liquid to be treated in the liquid distribution chamber are set to be less than the flow velocity of the liquid to be treated flowing in the tubular membrane. By forming the flow path in the concentrated liquid collecting chamber or the flow path in the liquid distribution chamber so as to be in the range of 5 to 2.0 times, or in the concentrated liquid collecting chamber or the liquid distribution chamber, By accommodating a solid movement / collision body that freely moves by the flow of the concentrated liquid in the liquid chamber or the flow of the liquid in the liquid distribution chamber, the membrane cleaning effect of the backwash liquid is improved as compared with the conventional membrane separation device. hand,
The efficiency of the membrane separation treatment can be improved.

[Brief description of the drawings]

FIG. 1 is a cross-sectional view illustrating a configuration of a tubular membrane module provided in a membrane separation device according to a first embodiment.

FIG. 2 is a cross-sectional view illustrating a configuration of another tubular membrane module provided in the membrane separation device of the first embodiment.

FIG. 3 is a cross-sectional view illustrating a configuration of another tubular membrane module provided in the membrane separation device of Embodiment 2.

FIG. 4 is a perspective view showing a configuration of a moving / colliding body.

FIGS. 5A and 5B are perspective views each showing a configuration of another moving / colliding body.

FIG. 6 is a flow sheet showing a configuration of a conventional membrane separation device.

FIG. 7 is a cross-sectional view showing a configuration of a tubular membrane module provided in a conventional membrane separation device.

FIG. 8 is a schematic view showing a problem of a tubular membrane module provided in a conventional membrane separation device.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 10 Conventional cross-flow type membrane separation apparatus 12 Tubular membrane module 14 Liquid tank to be processed 16 Liquid pipe to be processed 18 Liquid pump to be processed 20 Processing liquid pipe 22 Processing liquid tank 24 Concentrated liquid pipe 26 Lower diaphragm 28 Upper diaphragm 30 Liquid distribution chamber 32 Processing liquid chamber 34 Concentrated liquid collecting chamber 36 Vertical container 38 Internal pressure type tubular membrane 39 Processing liquid port 40 Upper head plate 42 Lower head plate 44, 46, 50, 52 Flange 48 Body 54 Backwashing liquid pipe 56 Reverse Washing pump 58 Backwash drainage pipe 60 Tubular membrane module of Embodiment 1 62 Liquid distribution chamber 64 Collection chamber 66, 68 Flow path forming body 70 Lower curved surface 72 Upper curved surface 74 Upper curved surface 76 Lower curved surface 80 First embodiment Modified tubular membrane module 82 Liquid distribution chamber 84 Liquid collection chamber 86, 88 Flow path forming body 89 Through hole 90 Tubular membrane module 91 of Embodiment 2 91 Movement / colliding body 92 Plastic-made balls 93 small conical projections 94 batten 95 sphere 96 grooves 97 cylinder 98 spiral fins

 ────────────────────────────────────────────────── ─── Continuing on the front page (72) Inventor Satoshi Nemoto 1-2-8 Shinsuna, Koto-ku, Tokyo Organo Corporation F-term (reference) 4D006 GA03 GA06 GA07 HA02 HA18 HA27 JA27A JA27B JA30A JA30B JA30C JA36A JA36B JA36C JA37A JA37B JA37C KA45 KA63 KC03 KC13 KC17 KC18 MA01 MA02 PA01 PB04 PB05 PB08

Claims (6)

[Claims] 1. A liquid distribution chamber, a processing liquid chamber and a concentrated liquid collecting chamber which are defined by a lower partition and an upper partition that cross each other.
A vertical container having a center and an upper portion is provided.In the vertical container, a lower partition and an upper partition are fixed to a lower partition and an upper partition at a lower end and an upper end so as to communicate with a liquid distribution chamber and a concentrated liquid collecting chamber, respectively.
A tubular membrane module having an internal pressure type tubular membrane extending in the processing liquid chamber in the longitudinal direction is provided, and the liquid to be treated is introduced into the liquid distribution chamber,
In a membrane separation device in which a membrane is separated by a cross-flow method and a processing liquid flows out of the processing liquid chamber and a concentrated liquid flows out through the concentrated liquid collecting chamber, the flow rate of the concentrated liquid in the concentrated liquid collecting chamber is reduced. 0.5 of the flow rate of the liquid to be treated flowing in the tubular membrane
A membrane separation apparatus, wherein a flow path in a concentrated liquid collecting chamber is formed so as to be in a range of 2 to 2.0 times. In addition, the flow rate of the liquid to be treated in the liquid distribution chamber is set to be 0.5 to 2.0 times the flow rate of the liquid to be treated flowing in the tubular membrane. The membrane separation device according to claim 1, wherein a passage is formed. 3. A liquid distribution chamber, a processing liquid chamber and a concentrated liquid collecting chamber which are defined by a lower partition and an upper partition that cross each other.
A vertical container having a center and an upper portion is provided.In the vertical container, a lower partition and an upper partition are fixed to a lower partition and an upper partition at a lower end and an upper end so as to communicate with a liquid distribution chamber and a concentrated liquid collecting chamber, respectively.
A tubular membrane module having an internal pressure type tubular membrane extending in the processing liquid chamber in the longitudinal direction is provided, and the liquid to be treated is introduced into the liquid distribution chamber,
In a membrane separation apparatus in which a membrane is separated by a cross-flow method and a processing liquid is caused to flow out of the processing liquid chamber and a concentrated liquid is caused to flow out through the concentrated liquid collecting chamber, the flow of the concentrated liquid in the concentrated liquid collecting chamber A membrane separation device, wherein a solid moving / colliding body that freely moves is accommodated in a concentrated liquid collecting chamber. 4. The membrane separation apparatus according to claim 3, wherein a solid motion / collision body that freely moves by the flow of the liquid in the liquid distribution chamber is accommodated in the liquid distribution chamber. 5. A flow rate of the concentrated liquid in the concentrated liquid collecting chamber is reduced by accommodating a solid movement / collision body that freely moves by the flow of the concentrated liquid in the concentrated liquid collecting chamber in the concentrated liquid collecting chamber. The flow path in the concentrated liquid collecting chamber is narrowed so as to be in a range of 0.5 to 2.0 times the flow rate of the liquid to be processed flowing in the tubular membrane. Membrane separation equipment. 6. A solid motion / collision body that freely moves by the flow of liquid in the liquid distribution chamber and the flow of concentrated liquid in the concentrated liquid collection chamber is accommodated in the liquid distribution chamber and the concentrated liquid collection chamber, respectively. Thereby, the flow velocity of the liquid to be treated in the liquid distribution chamber and the flow velocity of the concentrated liquid in the concentrated liquid collecting chamber are in the range of 0.5 to 2.0 times the flow velocity of the liquid to be treated flowing in the tubular membrane. The membrane separation device according to claim 4, wherein the flow path in the liquid distribution chamber and the flow path in the concentrated liquid collection chamber are each narrowed.