JP2001129368A - Gas-liquid separation module - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a gas-liquid separation module wherein a crack or a pinhole does not occur in a hollow fiber membrane, or very difficult to occur, and a life of the hollow fiber membrane is long. SOLUTION: A gas-liquid separation module comprises an annular body part 1 which has an inflow opening 1a of a liquid to be treated and its outflow opening, and contains a hollow fiber membrane; and a first header 5 being a flow speed attenuating room which attenuates a flow speed of the supplied liquid to be treated and communicates with the inflow opening 1a of the liquid to be treated of the annular body part 1 are provided.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

The present invention relates to a method for reducing the pressure in a hollow fiber membrane tube, filling the outside of the hollow fiber membrane with a liquid to be treated, and taking in the gas in the liquid to be treated into the hollow fiber membrane tube. The present invention relates to a gas-liquid separation module that performs liquid separation, a hollow fiber membrane suitably used for the gas-liquid separation module, and a hollow fiber membrane module.

[0002]

2. Description of the Related Art Conventionally, a liquid containing a gas (liquid to be treated) is passed through a tube of a hollow fiber membrane, and the outside of the tube of the hollow fiber is evacuated or evacuated to remove the gas in the liquid to be treated. 2. Description of the Related Art There is known an internal reflux type gas-liquid separation module of a type in which a gas-liquid separation is performed by taking it out of a pipe. For example, one using a hollow fiber membrane made of a tetrafluoroethylene-based resin or the like is known (Japanese Patent No. 2140818).

As a module or apparatus for separating gas from a liquid to be treated, for example, the liquid to be treated is contained by flowing the liquid to be treated outside the tube of the hollow fiber membrane and reducing the pressure inside the tube of the hollow fiber membrane. There is known an external recirculation type deaeration module that separates a generated gas into a hollow fiber membrane.

[0004]

However, the conventional external reflux type deaeration module has a problem that cracks and pinholes are liable to occur in the hollow fiber membrane as the module is used.
Further, when the pressure inside the hollow fiber membrane is reduced to a predetermined pressure or less, there is a problem that the hollow fiber membrane is crushed and the inner walls of the hollow fiber membrane come into contact with each other, making it difficult to use. further,
There is a problem that the hollow fiber membrane comes into contact with the hollow fiber membrane and the degassing ability of the hollow fiber membrane is reduced.

[0005] An object of the present invention is to provide a gas-liquid separation module in which cracks and pinholes are hardly generated or extremely hardly generated in the hollow fiber membrane and the life of the hollow fiber membrane is long.
Another object of the present invention is to provide a hollow fiber in which the inner walls of the hollow fiber membrane do not contact each other even when the inside of the hollow fiber membrane is decompressed to such an extent that the hollow fiber membrane is crushed and the inner walls of the hollow fiber membrane contact each other. Is to provide a membrane. Further, another object of the present invention is to provide a hollow fiber membrane or a hollow fiber membrane module which prevents the hollow fiber membrane from coming into contact with the hollow fiber membrane to reduce the degassing ability of the hollow fiber membrane.

[0006]

Means for Solving the Problems The present inventors have found the following contents and have completed the present invention. In the case where the liquid flow to be treated with the reduced flow velocity is supplied to the outside of the hollow fiber membrane, it is possible to prevent cracks and pinholes from being generated in the hollow fiber membrane. When a crush prevention device or a crush prevention portion for preventing crushing of the hollow fiber membrane is provided in the hollow fiber membrane tube, the inside of the hollow fiber membrane is crushed until the inner wall of the hollow fiber membrane comes into contact with the crushed hollow fiber membrane. Even when the pressure is reduced, the pressure inside the tube of the hollow fiber membrane can be reduced without bringing the inner walls of the hollow fiber membrane into contact with each other. Further, by providing a projection or a thick part (particularly, a thick part at the end of the hollow fiber membrane) outside (outer peripheral surface) of the tubular hollow fiber membrane, a gap is formed between adjacent hollow fiber membranes. In the case where the hollow fiber membrane is provided, the contact area between the hollow fiber membrane and the hollow fiber membrane can be reduced, so that the degassing ability of the hollow fiber membrane can be prevented from being reduced. Furthermore, in the case where a gap is provided between adjacent hollow fiber membranes by making the shape of the contour of the outer periphery of the radial cross section into a polygon, the contact area between the hollow fiber membrane and the hollow fiber membrane can be reduced. Therefore, it is possible to prevent the degassing ability of the hollow fiber membrane from decreasing.

That is, according to a first aspect of the present invention, a hollow fiber membrane-containing chamber having an inlet and an outlet for a liquid to be treated and containing a hollow fiber membrane therein, and a flow rate of the supplied liquid to be treated is reduced. The above object can be achieved by a gas-liquid separation module having a flow rate relaxation chamber communicating with the inflow port of the liquid to be treated in the hollow fiber membrane built-in chamber.

According to a second aspect of the present invention, the above object can be attained by a crush prevention device or a hollow fiber membrane having a crush prevention portion in a tube of the hollow fiber membrane for preventing the crush of the hollow fiber membrane. . In a third aspect, the present invention can achieve the above object by a hollow fiber membrane having a projection on the outside of the tube or a thick portion at the end of the tube. Further, according to a fourth aspect of the present invention, there is provided a hollow fiber membrane module comprising a plurality of tubular hollow fiber membranes, wherein the end of the hollow fiber membrane has a thickness other than the end. The above object can be achieved by a hollow fiber membrane module having a thickness larger than the thickness of the hollow fiber membrane module.

The gas-liquid separation module of the present invention can be operated as follows. The hollow fiber membrane-containing chamber is divided into two or more gas-liquid separation chambers, and the two or more gas-liquid separation chambers can communicate with each other so that the flow path of the liquid to be treated in the hollow fiber membrane-containing chamber becomes long. With this configuration, the liquid to be treated can be brought into contact with the hollow fiber membrane for a longer time to perform gas-liquid separation more efficiently. Therefore, even if the liquid to be treated is a large amount (large flow rate), it can be obtained after the treatment. The concentration of the gas contained in the processing liquid can be made lower.

The hollow fiber membrane-containing chamber has a tubular shape, and the tubular hollow fiber membrane-containing chamber has two or more gas-liquid separation chambers defined by partition walls extending in the axial direction of the tube. At least one set of two gas-liquid separation chambers communicating with each other via a header portion provided on the outer peripheral portion of the hollow fiber membrane built-in chamber can be provided. With this configuration, the liquid to be treated can be efficiently contacted with the hollow fiber membrane for a longer time to perform gas-liquid separation efficiently. Therefore, even if the liquid to be treated is a large amount (large flow rate), the treatment obtained after the treatment can be performed. The concentration of gas contained in the liquid can be made lower.

The hollow fiber membrane-containing chamber may have two or more inlets for the liquid to be treated. In the hollow fiber membrane built-in chamber, the inflow port of the liquid to be treated can be partitioned by a partition plate. With this configuration, the flow rate of the liquid to be treated can be further reduced. The partition may have a thickness gradient.

[0012] The hollow fiber membrane built-in chamber has an inlet area for the liquid to be processed in the hollow fiber membrane built-in chamber that increases as the distance from the supply port of the liquid to be processed supplied to the flow velocity relaxation chamber increases. A plurality of inlets for the processing liquid can be arranged.
With this configuration, the flow rate of the liquid to be treated can be further reduced. The processing of the hollow fiber membrane-containing chamber is performed such that the area of the inlet of the liquid to be processed in the hollow fiber membrane-containing chamber increases as the distance from the supply port of the liquid to be processed supplied to the flow velocity relaxation chamber increases. The shape of the liquid inlet can be set. With this configuration, the flow rate of the liquid to be treated can be further reduced.

The shape of the hollow fiber membrane-containing chamber can be set so that the hollow fiber membrane does not come into contact with the hollow fiber membrane-containing chamber. With this configuration, it is possible to prevent the hollow fiber membrane from being in contact with the hollow fiber membrane built-in chamber and being damaged during gas-liquid separation. The hollow fiber membrane can be a substantially non-porous (non-porous) silicone hollow fiber membrane. With this configuration, when the inside of the hollow fiber membrane tube is decompressed or evacuated,
As compared with a hollow fiber membrane using a porous membrane, the degree of vacuum in the tube can be made higher, so that the degassing performance can be further enhanced.

In the hollow fiber membrane, a crush prevention device for preventing crush of the hollow fiber membrane can be incorporated in the tube.
A crush prevention portion for preventing crushing of the hollow fiber membrane can be provided in the tube, and further, a portion having a large outer diameter can be provided on the outside of the tube of the hollow fiber membrane at the projection or at the end of the tube. Each of these configurations can prevent the degassing ability of the hollow fiber membrane from decreasing.

[0015] The hollow fiber membrane can be built in the hollow fiber membrane housing chamber by providing a gap enough to ensure a sufficient flow rate of the liquid to be treated. With this configuration, the flow rate of the liquid to be treated flowing through the hollow fiber membrane built-in chamber can be sufficiently ensured.

In the form of a hollow fiber membrane module formed by binding the ends of a hollow fiber membrane having a tube wall at an end portion having a thickness larger than the thickness of the tube walls other than the end portion, the hollow fiber membrane is connected to the hollow fiber membrane module. It can be built into the fiber membrane chamber. With this configuration, it is possible to prevent the degassing ability of the hollow fiber membrane from being reduced, further increase the strength and binding force of the hollow fiber membrane module, and prolong the life of the hollow fiber membrane module. And a sufficient resistance to the flow of the liquid to be treated.

The hollow fiber membrane of the present invention having a crush prevention device or a crush prevention portion for preventing the crush of the hollow fiber membrane in the tube of the hollow fiber membrane has a projection on the outside of the tube or a thick portion at the end of the tube. Can have. In the hollow fiber membrane module of the present invention, the thickness of the tube wall at the end of the hollow fiber membrane may be larger than the thickness of the tube wall other than the end.

[0018]

DESCRIPTION OF THE PREFERRED EMBODIMENTS [Gas-Liquid Separation Module] The gas-liquid separation module of the present invention has at least a hollow fiber membrane built-in chamber and a flow rate relaxation chamber. The hollow fiber membrane built-in chamber has an inlet and an outlet for the liquid to be treated and houses the hollow fiber membrane. The inside of the hollow fiber membrane tube is communicated with a reduced pressure source such as a vacuum pump (suction pump). be able to.

The flow velocity relaxation chamber relaxes the flow velocity of the supplied liquid to be treated, and communicates with the inlet of the liquid to be treated in the hollow fiber membrane built-in chamber. In the flow velocity relaxation chamber, for example, an inlet for the liquid to be treated into the flow velocity relaxation chamber can be provided at a position where the supplied liquid to be treated does not directly flow into the inlet for the liquid to be treated in the hollow fiber membrane built-in chamber.

The chamber containing the hollow fiber membrane can be divided into two or more chambers by partition walls. Although a hollow fiber membrane can be provided in at least one of the two or more chambers, a hollow fiber membrane module or a hollow fiber membrane module in which a plurality of hollow fiber membranes are bundled is arranged in all chambers in order to efficiently perform gas-liquid separation. Can be set up. The hollow fiber membrane-containing chamber can be formed in a tubular shape having a radial cross section of various shapes, for example, a circle, a substantially circle, an ellipse, a square, a rectangle, and the like.

The hollow fiber membrane-containing chamber is a tubular hollow fiber membrane-containing chamber having an inlet and an outlet for the liquid to be treated on the outer peripheral surface of the tube, preferably in two regions near the end of the tube. An inlet for the liquid to be treated is provided on one side, and an outlet for the liquid to be treated is provided on the other side at a distance.

The gas-liquid separation module has an inflow port and an outflow port for the liquid to be treated at the outer periphery of the tubular hollow fiber membrane built-in chamber, and the tubular hollow section communicates with the inflow port for the liquid to be treated. An annular flow rate mitigation chamber (having an annular internal space) may be provided in a circumferential direction of an outer peripheral portion of the thread film built-in chamber. An annular chamber (having an annular internal space) may be provided in a circumferential direction of an outer peripheral portion of the tubular hollow fiber membrane built-in chamber. The inflow port and the outflow port of the liquid to be treated are preferably provided apart from each other, and more preferably, the inflow port of the liquid to be treated is provided in one of two regions near the end of the tube, and the liquid to be treated is provided in the other one. Outlet is provided.

As the hollow fiber membrane, hollow fiber membranes of various materials can be used as long as the inside of the tube can be decompressed. Preferably, a substantially hollow silicone hollow fiber membrane is used. Used.

[First Hollow Fiber Membrane] The first hollow fiber membrane of the present invention is a crush prevention device for preventing crushing of the hollow fiber membrane and a crush prevention portion for preventing crush of the hollow fiber membrane. At least one is in the tube. The crush prevention device can be formed separately from the tubular hollow fiber membrane, for example, and can be provided by inserting the crush prevention device into the tube of the tubular hollow fiber membrane.
Further, the crush prevention portion for preventing crushing of the hollow fiber membrane can be provided, for example, in a tube of the tubular hollow fiber membrane by integrally molding with the tubular hollow fiber membrane.

The hardness of the crush prevention device or the crush prevention portion in the hollow fiber membrane of the present invention can be made equal to or less than the hardness of the built-in hollow fiber membrane so as not to damage the built-in hollow fiber membrane. . Usually, the material of the crush prevention device can be the same as the material of the hollow fiber membrane to be incorporated. In the hollow fiber membrane of the present invention, the tubular hollow fiber membrane main body and the crush prevention part do not necessarily need to be formed of the same material (for example, a material such as a resin). The tubular main body portion and the crush prevention portion can be formed of the same material (for example, a material such as resin).

The crush prevention device can be formed into a shape that can be manufactured by an extrusion molding method for extruding a molten resin so that it can be easily manufactured. For example, when the hollow fiber membrane is built in the hollow fiber membrane, the cross section in the radial direction of the hollow fiber membrane can be made uniform (for example, the cross section is cross-shaped). The dimension of the crush prevention device in the radial direction of the hollow fiber membrane is preferably equal to or less than the inner diameter of the hollow fiber membrane to be incorporated. In addition, the crush prevention device can be inserted into the internal space of the tubular hollow fiber membrane to insert the crush prevention device into the internal space of the tubular hollow fiber membrane.

The hollow fiber membranes can be bundled into a hollow fiber membrane module. An adhesive can be used to bundle a large number of hollow fiber membranes. As an adhesive,
An appropriate adhesive is used depending on the type of the hollow fiber membrane to be used. For example, in the case of a silicone hollow fiber membrane, preferably, an adhesive of a resin of the same material as the membrane, an epoxy resin, or a polyamide resin can be used, and a hollow fiber membrane module is formed using these resins as an adhesive. If 250
Up to about ° C, the silicone hollow fiber membranes have heat resistance of being bonded with sufficient adhesive strength.

[Second Hollow Fiber Membrane] A large number of hollow fiber membranes are usually bundled and built in the gas-liquid separation module. For this reason, a state in which the hollow fiber membrane and the hollow fiber membrane are pulled and adhered to each other due to the evacuation in the tube always occurs. In addition, since a large number of hollow fiber membranes are bound, they are naturally in contact with each other. When the intervals between the hollow fiber membranes are not present or narrow, the hollow fiber membranes cannot exhibit sufficient degassing performance and the flow rate of the liquid to be treated cannot be sufficiently ensured. The interval between the hollow fiber membranes can be increased by reducing the number of the hollow fiber membranes to be built in, but in this case, the degassing efficiency deteriorates.
Therefore, in the second hollow fiber membrane of the present invention, in order to prevent such a state of contact or sticking, a portion having a large outer diameter is provided on the outer periphery of the hollow fiber membrane at the end of the projection or tube. With such a configuration, the flow rate of the liquid to be treated can be ensured, and the degassing performance can be sufficiently exhibited to efficiently degas.

That is, the second hollow fiber membrane of the present invention has a projection on the outside (outer peripheral surface) of the tube or a portion having a large outer diameter at one end (at least one of the two ends) of the tube. It is characterized by the following. The shape or arrangement position of the protrusion may be any shape or arrangement position capable of preventing the state of contact or sticking as described above, and preferably,
Select a shape or arrangement position that is easy to form. The portion having a large outer diameter in the hollow fiber membrane having a portion having a large outer diameter at the end of the tube is preferably formed by increasing the thickness of the tube wall at the end of the tube.

The difference between the height of the projections or the length of the portion where the outer diameter of the end of the tube is large and the diameter of the portion where the outer diameter is small other than the end of the tube is said to be in contact or sticking as described above. The height or the difference is such that the state can be prevented, and the height or the difference is appropriately set according to the diameter of the hollow fiber membrane. In a normal case, the height of the projection or the difference can be set so that the interval between the hollow fiber membranes and the hollow fiber membrane can be secured, for example, 0.5 mm or more. For example, the height of the projections is 0.5 mm or more. Can be

When the inner diameter of the hollow fiber membrane is small, for example, when the inner diameter of the hollow fiber membrane is small, the projection may be of a raised type in which the inner wall surface is depressed and raised outward. Also,
When the outer diameter of the hollow fiber membrane is large, a projection is formed on the outer wall surface (outer peripheral surface) of the hollow fiber membrane, and a hump type in which the inner wall surface (inner peripheral surface) does not have a depression is used. it can.

[0032] The second hollow fiber membrane of the present invention can have projections on its outer peripheral surface that are continuous in a direction perpendicular to the radial direction (normally, the longitudinal direction of the hollow fiber membrane). Such a hollow fiber membrane has a gap between the hollow fiber membranes even when the hollow fiber membranes are in contact with each other, such as when a plurality of hollow fiber membranes are bundled and used. Therefore, the liquid to be treated can sufficiently flow outside the hollow fiber membrane, a stable flow rate of the liquid to be treated can be ensured, and the projections act as a reinforcing material for the hollow fiber membrane. It is hard to be crushed when the inside of the tube is used under reduced pressure.

The projections may be, for example, one or more curved or linear projections, but preferably one or more spiral projections formed so as to spirally surround the outer periphery of the hollow fiber membrane. It is. The helical projection may be a projection that rotates clockwise or counterclockwise on the outer peripheral surface of the hollow fiber membrane, but a projection that has at least one counterclockwise part in the clockwise part, The projection may have at least one clockwise portion.

A certain interval (for example, an interval necessary for changing the direction of rotation) can be provided between the clockwise portion and the counterclockwise portion. As such a protrusion, for example, there is a protrusion in which a clockwise portion and a counterclockwise portion alternately appear. The height of the projections can be appropriately set within a range such that a stable flow rate of the liquid to be treated can be secured outside the hollow fiber membrane when a plurality of hollow fiber membranes are bundled and used. it can.

A hollow fiber membrane having a tubular hollow fiber membrane having projections continuous in the longitudinal direction on the outer peripheral surface can be produced, for example, by integrally molding the same material (eg, resin) in a mold.
The hollow fiber membrane of the present invention may have a portion having a large outer diameter at an end (at least one of the two ends). A combination of at least two or more of the first and second hollow fiber membranes of the present invention (preferably, a type in which as many gaps as possible are formed between the hollow fiber membranes), The ends can be bound with, for example, an adhesive to form a hollow fiber membrane module.

[Hollow Fiber Membrane Module] The hollow fiber membrane module of the present invention is preferably a hollow fiber membrane module formed by binding ends of a plurality of tubular hollow fiber membranes with, for example, an adhesive. The thickness of the end portion of the fiber membrane is a hollow fiber membrane module that is thicker than the thickness other than the end portion, and more preferably, the thickness of the tube wall at the end portion of the hollow fiber membrane is the thickness of the tube wall other than the end portion. Thicker than the thickness.

A hollow fiber membrane having a tube wall at an end portion having a thickness larger than the thickness of the tube wall other than the end portion is, for example, a tube member having a tubular cross section having a uniform sectional area. It can be manufactured by surrounding and bonding with an adhesive if necessary. In that case, the end of the hollow fiber membrane can be easily surrounded by making a cut in the longitudinal direction of the tubular member.
The tubular member may be the same as the material of the surrounding hollow fiber membrane.

[0038]

[Embodiment 1] An embodiment of the present invention will be described with reference to the drawings. FIG. 1 is a schematic perspective view of one embodiment of the gas-liquid separation module of the present invention. FIG. 2 is a cross-sectional view in a direction perpendicular to the longitudinal direction of the gas-liquid separation module of FIG.
Appear on the cut surface. FIG. 2 is a cross-sectional view as viewed in the direction of the end of the gas-liquid separation module.

FIG. 3 is a cross-sectional view of the gas-liquid separation module of FIG. 1 in a direction perpendicular to the longitudinal direction, in which the second header 7 to which neither the water supply joint nor the degassing water joint is connected is cut. Is what appears. FIG. 3 is a cross-sectional view as viewed in the direction of the center of the gas-liquid separation module.

The gas-liquid separation module of FIG. 1 includes a partition plate 2 in a hollow portion inside a tubular body 1. Partition plate 2
Divides the cavity in the longitudinal direction to define two supply water treatment chambers. The supply water treatment chamber contains the hollow fiber membrane 10. Both ends of the supply water treatment chamber are formed as vacuum cover joints K having a large number of hollow fiber membranes and an adhesive filling portion filled with an adhesive for bonding the outer peripheral portions thereof, so that supply water does not leak. . Open ends at both ends of the hollow fiber membrane are open at end faces of the joint K for vacuum cover. Therefore, for example, a cap member communicating with a vacuum source (for example, a vacuum pump or the like) by a pipe or the like is hermetically covered with the vacuum cover joint K at both ends of the tubular body portion 1, and the inside of the hollow fiber membrane pipe is formed. Can be reduced in pressure. FIG. 11 is a schematic perspective view of a gas-liquid separation module in which a cap member 120 is air-tightly covered on the vacuum cover joint K at both ends of the tubular body 1.
In the first embodiment, the gas in the tube is sucked from both open ends of the hollow fiber membrane. However, one open end of the hollow fiber membrane can be sealed with an adhesive.

As shown in FIG. 2, the supply water (liquid to be treated) supplied from the supply water joint 3 collides with the header partition plate 4a at a substantially right angle so that the supply water (the liquid to be treated) is supplied to the first header 5 which is the flow rate reduction chamber. It flows into the internal space 5a, and flows into the first supply water treatment chamber 6 from the plurality of inlets 1a into the first supply water treatment chamber. A large number of inflow ports 1a are formed penetrating the body wall of the body portion 1 (however, excluding the vicinity of the partition plate 4a and the feed water coupling (inflow port to the internal space 5a) 3).

By providing the first header 5 so as to surround the plurality of inlets 1a to the first supply water treatment chamber, the flow rate of the supply water can be reduced, and further, the pressure of the supply water can be reduced. And the flow rate can be reduced.
The first header 5 is provided at the body 1 around the inlet 1a.
Is provided so that the supply water does not leak. For example, the first header 5 is provided on the body 1 around the inflow port 1a with an adhesive.

The treated water flowing into the first supply water treatment chamber 6 is
It flows from the first header 5 side to the second header 7 side in FIG. As described above, since the plurality of hollow fiber membranes that reduce the pressure in the hollow fiber membrane tube from at least one of the open ends is built in the first feed water treatment chamber 6, the first feed water treatment chamber 6 is During the passage, the gas contained in the feed water is sucked into the hollow fiber membrane and separated from the feed water.

As shown in FIG. 3, the supply water supplied to the first supply water treatment chamber 6 flows out from one large outlet 1b of the tubular body 1 on the side of the second header 7, and the second supply water is supplied to the second supply water treatment chamber 6.
It flows into the internal space 7a of the header 7. In FIG. 1, the position at which the supply water flows into the internal space 7 a of the second header 7 is indicated by reference symbol E. The second header 7 is formed in an annular shape so as to surround the outer periphery of the tubular body 1. The internal space 7
a is an annular space surrounding the outer periphery of the tubular body 1. The supply water flowing into the internal space 7a is supplied to the second header 7
Flows along the inner peripheral surface of
c and flows into the second supply water treatment chamber 8.

The treated water flowing into the second supply water treatment chamber 8 is
The second feed water treatment chamber 8 flows from the second header 7 side to the first header 5 side. As described above, the second supply water treatment chamber 8 contains a plurality of hollow fiber membranes in which the inside of the hollow fiber membrane tube is depressurized from at least one by a decompression source (not shown) such as a vacuum pump. The gas contained in the feed water is sucked into the hollow fiber membrane and separated from the feed water.

As shown in FIG. 2, the supply water from the second supply water treatment chamber 8 is supplied to the tubular body 1 on the first header 5 side.
Out of the outlet 1d of the first header 5
b and further out of the degassed water joint 9. In addition,
The internal space 5a and the internal space 5b of the first header 5 are partitioned by the header partition plates 4a, 4b and are not directly communicated.

FIG. 18 shows another preferred embodiment of the outlet of the tubular body inside the second header and the vicinity of the outlet. FIG. 18 is a cross-sectional view in a direction perpendicular to the longitudinal direction of a gas-liquid separation module according to another embodiment of the present invention,
FIG. 4 is a cross-sectional view at a position corresponding to FIG. 3, in which a second header to which neither a supply water coupling nor a degassing water coupling is connected appears on a cut surface.

As shown in FIG. 18, one outlet 1b and one inlet 1c of the tubular body shown in FIG. 3 are formed as a plurality of outlets 1b 'and a plurality of inlets 1c', respectively. can do. The plurality of outlets 1b ′ and the plurality of inlets 1c ′ are, for example, provided with a plurality of plate-shaped members M at one large outlet as in the case of the inlet 1a and the outlet 1d in FIG. It can be formed by partitioning, or can be formed by providing a plurality of small independent through holes. FIG.
As shown in FIG. 5, a partition plate N for partitioning the internal space 7a 'of the second header 7' can be provided. When the partition plate N is provided, the outlet of the outlet in a region relatively far from the partition plate N can be provided. The area can be made smaller or the number of outlets can be made smaller, and the area of the outlet in a region relatively close to the partition plate N can be made larger or the number of outlets can be made larger. That is, as the distance from the partition plate N increases, the area of each outlet can be gradually reduced and the number of outlets (distribution density of outlets) can be gradually reduced.

In the gas-liquid separation module of the present invention, the structure (shape, number, formation position from the supply water joint, area, etc.) of the inflow port of the annular body 1 through which supply water flows into the first supply water treatment chamber ), The flow of the supply water can be adjusted, and the supply water can be uniformly and stably supplied to the hollow fiber membrane built-in chamber (particularly, the first supply water treatment chamber). It is possible to prevent an excessive rate or amount of supply water that adversely affects the hollow fiber membrane from flowing through the hollow fiber membrane built-in chamber. Hereinafter, the first embodiment based on FIGS.
Examples of inlets to the first supply water treatment chamber other than those shown in FIG.

Embodiment 2-1 FIG. 4 shows another example of the feed water coupling, the first header, and the inlet to the first feed water treatment chamber. FIG. 4 shows a tubular body 41 near the first header 45.
It is a schematic perspective view of. The tubular body 41 has a band-shaped opening 41a having a substantially constant width in the circumferential direction, and a plurality of plate-like members 42 that partition the opening are provided in the opening. The plurality of plate members 42 can be provided such that the surface directions of the respective plate members substantially coincide with the radial direction of the tubular body 41. That is, the tubular body 4
The plate-like member 42 can be provided so that the surface including the central axis of the one and the surface of the plate-like member 42 coincide with each other. Further, the plate members can be provided so that the distance between the plate members increases as the distance from the feed water coupling 43 increases.

The shape of the plate member 42 can be a plate having a uniform thickness as shown in FIG.
(B), the thickness increases from one end to the other end, that is, the end face can be widened. The plate-like member shown in FIG. 5 (b) has a thicker end having a tubular body portion 41.
The opening 41a can be provided so as to be located on the outer peripheral side of the tubular body portion or such that the thicker end portion is located on the center side of the tubular body portion 41.

Embodiment 2-2 FIG. 6 shows another example of the feed water coupling, the first header, and the inlet to the first feed water treatment chamber. FIG. 6 is a cross-sectional view in the radial direction of the tubular body 61, and shows a section of the tubular body 61 and the vicinity thereof. In the case where a plurality of plate-like members 62 are provided in the opening 61a of the tubular body 61, in FIG. 6 including the radial cross section of the tubular body 61 and its vicinity, it communicates with the internal space 65a of the first header 65. The water supply coupling 63 is provided near a header partition plate 64a that partitions the internal space 65a and the internal space 65b of the first header. More specifically, the pipe axial direction of the tubular water supply coupling 63 is the longitudinal direction of the cross section of the partition plate 66 provided in the hollow portion inside the tubular body 61 in the radial section of the tubular body 61. It is provided so as to be substantially parallel to. The header partition plate 64b partitions the internal space 65a and the internal space 65b of the first header together with the header partition plate 64a.

In the sectional view of FIG. 6, the center of the central axis A of the tubular body 61 is
Is defined as a reference position (0 °) for measurement of a central angle of a sector having a center axis A as a center and an outer circumference of the tubular body portion 1 as an arc. Tubular body part 61 in the region where the central angle is 0 to 90 °
In the outer peripheral surface of the main body 61, an opening having a length of 10 mm in the circumferential direction and a length of 100 mm in the longitudinal direction of the body 61
Twenty can be provided. In the same case as above, the tubular body 6 in the region where the central angle is 90 to 180 °.
In the outer peripheral surface of No. 1, an opening having a length of the body 61 in the circumferential direction of 20 mm and a length of the body 61 in the longitudinal direction of 100 mm
Fifteen can be provided.

Third Embodiment FIG. 7 shows another example of the inlet to the first supply water treatment chamber. FIG. 7 is a schematic perspective view of the tubular body 71 near the first header 75. The tubular body 71 has three inlets 7 which open in a belt shape in the circumferential direction.
0a, 70b, and 70c. The inflow port 70b is formed such that the circumferential length of the tubular body is longer than the inflow ports 70a and 70c and is closest to the feed water coupling 73. Therefore, the total area of the inflow port gradually increases as the distance from the feed water coupling 73 increases.

Fourth Embodiment FIG. 8 shows another example of the inlet to the first supply water treatment chamber. FIG. 8 is a schematic perspective view of the tubular body 81 near the first header 85. The tubular body portion 81 has two rows of openings (a plurality of openings are provided in ascending order of area) formed of a plurality of openings in the circumferential direction. The first group of openings includes eight openings from the smallest opening 80a to the largest opening 80b. The second group of openings includes the smallest opening 80c to the largest opening 8c.
Consists of eight openings up to 0d. Therefore, the feed water coupling 8
3, the total area of the inlets gradually increases.

Embodiment 5 In the gas-liquid separation module of the present invention, a partition plate is provided at the inlet of the tubular body or a plurality of holes are provided as inlets. In the vicinity of the inflow port on the peripheral surface, the partition plate and the perforated surface are prevented from directly contacting the hollow fiber membrane. For example, as shown in FIG. 9, the vicinity of the inlet 91 a on the inner peripheral surface of the tubular body 91 is not in contact with the hollow fiber membrane 90, and the vicinity of the inlet 91 a is another inner peripheral surface of the tubular body. Lower than the gap 92
Can be provided. Further, a coating layer may be provided on the surface of the hollow fiber membrane near the inflow port 91a, or the periphery of the hollow fiber membrane or a bundle thereof may be covered with a belt-shaped cover.

[Embodiment 6] In a gas-liquid separation module of the present invention, as shown in FIG. 10, a partition plate 102 having a cross section in a direction perpendicular to the longitudinal direction is formed inside a tubular body 101. Provided, the body part is divided in the longitudinal direction to 4
One supply water treatment chamber 106, 107, 108 and 109 can be defined.

FIG. 10 is a cross-sectional view in a direction perpendicular to the longitudinal direction of the gas-liquid separation module of the present invention, in which the first header 105 to which the supply water joint and the deaeration water joint are connected appears on the cut surface. It is. The first header 105 is provided in an annular shape so as to define an annular internal space on the outer peripheral surface of the tubular body portion 101. In FIG. 10, the annular internal space is partitioned by header partition plates 104a, 104b, and 104c, and internal spaces 105a, 105b, and 105c that are not directly communicated with each other are defined.
FIG. 10 is a cross-sectional view taken in the direction of the center of the gas-liquid separation module.

The supply water flows into the internal space 105a of the first header 105 from the tubular supply water joint 103, and flows into the first supply water treatment chamber 106 from the inlet 101a of the tubular body. The supply water that has flowed into the first supply water treatment chamber 106 passes through a second header (not shown) provided at the end of the tubular body opposite to the end where the first header 105 is provided. Flows into the second supply water treatment chamber 107 via the second supply water treatment chamber 107.

As shown in FIG. 10, the supply water flowing into the second supply water treatment chamber 107 is supplied to the outlet 101 of the tubular body.
b flows out into the internal space 105b of the first header 105, and further flows into the third supply water treatment chamber 108 from the inflow port 101c of the tubular body. Third supply water treatment chamber 108
Is supplied to the fourth feed water treatment via a second header (not shown) provided at the end of the tubular body opposite to the end at which the first header 105 is provided. Room 1
09.

The supply water in the fourth supply water treatment chamber 109 is shown in FIG.
As shown in FIG. 0, the gas flows out from the outflow port 101d of the tubular body into the internal space 105c of the first header 105, and further flows out of the deaerated water joint 119. Each of the four supply water treatment chambers 106, 107, 108 and 109 has a built-in hollow fiber membrane 110 whose pressure in the pipe is reduced, so that the treated water is removed when passing through the four supply water treatment chambers. I'm bothered.

The hollow fiber membranes housed in each of the four supply water treatment chambers are open at both ends, and vacuum suction is performed from both open ends of the first header side and the second header side. The feed water is passed through the four feed water treatment chambers, and
Degassed times. In addition, when sucking the gas in the hollow fiber membrane tube built in the four supply water treatment chambers, the opening on the first header side and the opening on the second header side are connected to the suction port of one vacuum pump. It is possible to perform suction while the first suction is preferably performed only from the opening on the first header side.
A vacuum pump and a second vacuum pump that sucks only from the opening on the second header side are used.

As described above, in FIG. 10, the partition wall is provided in the hollow fiber membrane built-in chamber to define four supply water treatment chambers and to make their cross-sectional areas substantially uniform.
One or more feedwater treatment chambers can be defined and their cross-sectional areas or volumes substantially uniform, or
Three or four or more supply water treatment chambers are defined and their cross-sectional areas or volumes are made uneven (for example, the cross-sectional area of the first supply water treatment chamber into which the liquid to be treated first flows in). Or maximize the volume).

An example in which the water to be treated is degassed using an example of a gas-liquid separation module having four supply water treatment chambers having a structure similar to that shown in FIG. 10 will be described below.

The material of the gas-liquid separation module is iron (SGP
Material, STPG material), stainless steel, vinyl chloride, etc., and the material of the gas-liquid separation module of this embodiment was stainless steel. The total length of the gas-liquid separation module in the longitudinal direction (that is, the longitudinal direction of the tubular body 101) is 5000 mm, and the diameter of the gas-liquid separation module (that is, the diameter of the tubular body 101) is 1000 mm. is there.

The tubular hollow fiber membrane built in the gas-liquid separation module is a hollow fiber membrane made of silicone resin having an outer diameter of 0.8 mm and an inner diameter of 0.5 mm. Both ends are bonded with an adhesive so as to be 4500 mm and bound, so that the gas in the tube can be removed by suction from the open ends on both sides. In addition, the number of all hollow fiber membranes built in the gas-liquid separation module is about 1.4 million,
A substantially equal number of hollow fiber membranes are built in each of the four supply water treatment chambers, and the degree of vacuum in the hollow fiber membrane tube is -750 mm.
/ Hg (10 Torr).

The water to be treated before being supplied to the gas-liquid separation module was a water temperature of 13.0 ° C. and a dissolved oxygen concentration (D
O) 10.2 ppm of water to be treated was used. The amount of treated water supplied to the gas-liquid separation module for treatment is 200
m ³ / hour.

The dissolved oxygen concentration after passing through the first supply water treatment chamber was 0.93 ppm, and the dissolved oxygen concentration after passing through the second supply water treatment chamber was 0.15 ppm. The dissolved oxygen concentration after passing through the chamber is 0.02pp
m, and the dissolved oxygen concentration after passing through the fourth supply water treatment chamber was 0.009 ppm.

As described above, the gas-liquid separation module has high degassing performance (degassing capability) and can efficiently process a large amount (large flow rate) of supply water (water to be treated). The air does not adversely affect the hollow fiber membrane. That is, the gas-liquid separation module can efficiently process a large amount (large flow rate) of supply water (water to be treated) without adversely affecting the hollow fiber membrane, and can reduce the supply water (water to be treated). Even if the amount is large (large flow rate), the concentration of the gas contained in the treated water obtained after the treatment can be extremely reduced.

Embodiment 7 FIGS. 12 to 14 show embodiments of the first hollow fiber membrane of the present invention.

<Example 7-1> An example of a hollow fiber membrane in which a plurality of branches are branched from a central axis, and a crush prevention device having a sphere at the tip of the branched branch is built in a hollow fiber membrane tube. Figure 12
(1a) and (1b).

Example 7-2 FIGS. 12A and 12B show an example of a hollow fiber membrane in which a helical spring is incorporated in a hollow fiber membrane tube as a crush prevention device.

Embodiment 7-3 FIGS. 12 (3a) and (3b) show an example of a hollow fiber membrane in which a crush prevention device having a plurality of warp-shaped projections on the central axis is incorporated in a hollow fiber membrane tube. Indicated by

<Example 7-4> An example of a hollow fiber membrane in which a crush prevention device formed by forming three plate-like members around the center axis at approximately 120 ° intervals is incorporated in a hollow fiber membrane tube. Figure 1
3 (4a) and (4b). This hollow fiber membrane can be manufactured by separately forming a tubular hollow fiber membrane main body and a crush prevention device and inserting the crush prevention device into the tubular hollow fiber membrane main body.

The crush prevention device has a shape that can be manufactured by an extrusion molding method in which a molten resin is extruded from a mold and molded, and thus can be manufactured by an extrusion molding method. FIG. 13 (5b) shows a radial cross-sectional view of another example of the hollow fiber membrane of the present invention in which the crush prevention device can be easily formed by an extrusion molding method. FIG. 13 (5b) shows a cross section in the hollow fiber membrane radial direction in the case where the cross section in the hollow fiber membrane radial direction is a “10” shape and the cross sectional shape is uniform in the hollow fiber membrane longitudinal direction. It is shown.

Further, a hollow fiber membrane obtained by integrating the above-mentioned crush prevention device and a tubular hollow fiber membrane, that is, a crush prevention portion having the same shape as the above-mentioned crush prevention device is integrated into the hollow fiber membrane tube. May be used as the hollow fiber membrane. This hollow fiber membrane can be manufactured by simply integrating the tubular hollow fiber membrane main body and the crush prevention portion having the above-mentioned shape by extrusion molding. In particular, when manufacturing a hollow fiber membrane having a thin tubular hollow fiber membrane main body, it is preferable to manufacture the hollow fiber membrane integrally by extrusion.

<Example 7-5> An example of a hollow fiber membrane having a plurality of warp-shaped projections provided on the inner wall surface (inner peripheral surface) inside the tube of the hollow fiber membrane is shown in FIG. 14 (6a). And (6b). The wart-like protrusions are provided at intervals of about 120 ° in the circumferential direction of the inner wall surface of the tube so that three wart-like protrusions can be seen in a radial cross section of the tubular hollow fiber membrane. The hollow fiber membranes shown in (6a) and (6b) of FIG. 14 are formed, for example, by a method in which a resin melted by heating (having elasticity enough to be taken out of the mold at room temperature) is molded in a mold. It can be obtained by integrating the fiber membrane and the wart-like projections, and is particularly suitable for a hollow fiber membrane having a thin tube.

<Example 7-6> An example of a hollow fiber membrane in which a plurality of ring-shaped projections, which are crush prevention portions, are provided at intervals on the tube wall in the longitudinal direction of the hollow fiber membrane is shown in FIG. 14 (7a). (7
Shown in b). The hollow fiber membranes shown in (7a) and (7b) of FIG. 14 are formed, for example, by a method in which a resin melted by heating (having elasticity enough to be removed from the mold at room temperature) is molded in a mold. It can be obtained by integrating the fiber membrane and the ring-shaped projection, and is particularly suitable for a hollow fiber membrane having a thin tube.

Embodiment 8 FIG. 15 shows an embodiment of the second hollow fiber membrane of the present invention. FIG. 15 is a longitudinal sectional view of the hollow fiber membrane.

<Embodiment 8-1> FIG. 15A shows a projection 150a in which the inner wall surface of the hollow fiber membrane is depressed and raised to the outside, which is suitable when the inner diameter of the membrane is small. 1 shows a hollow fiber membrane. This hollow fiber membrane can be produced, for example, by a method of molding a resin melted by heating (having enough elasticity at room temperature to be able to be removed from the mold) in a mold.

<Embodiment 8-2> In FIG. 15B, a projection 150b having no internal space is formed on the outer wall surface of the hollow fiber membrane, which is suitable when the inner diameter of the membrane is large. The inner wall surface shows a hollow fiber membrane that remains flat. This hollow fiber membrane
For example, it can be manufactured by a method of molding a resin melted by heating in a mold.

Embodiment 9 FIG. 16 shows another embodiment of the gas-liquid separation module of the present invention, that is, the vicinity of the inlet and outlet of the liquid to be treated in the hollow fiber membrane-containing chamber containing the hollow fiber membrane. 3 shows another embodiment. FIG. 16 is a longitudinal sectional view of the gas-liquid separation module of the present invention, showing the vicinity of the first header.

In the conventional gas-liquid separation module, since the distance between the inlet and the hollow fiber membrane and the distance between the outlet and the hollow fiber membrane are narrow, the required flow rate of the liquid to be treated could not be secured. On the other hand, in the gas-liquid separation module according to the embodiment of the present invention shown in FIG. 16, the end portions of a large number of hollow fiber membranes are bound with an adhesive (crossing at about 90 ° in FIG. 16). By providing an adhesive portion between the innermost wall of the tubular body and the end of the tubular body, the inner wall of the tubular body and the outer surface of the hollow fiber membrane module are provided. Since there is a gap between it and the water flow path,
A sufficient flow rate of the liquid to be treated can be secured.

The gap between the inner wall surface of the tubular body and the outer surface of the hollow fiber membrane module (the length of the gap in the direction perpendicular to the direction in which the liquid to be treated flows) is preferably
The length should be at least 1% of the diameter of the tubular body. For example, when the diameter of the tubular body is 1000 mm, it is preferable that the diameter of the body be 10 mm in the direction perpendicular to the direction in which the liquid to be treated flows.
A gap of at least mm is provided.

Example 10 FIG. 17 shows an example of the second hollow fiber membrane of the present invention and an example of the hollow fiber membrane module of the present invention. FIG. 17 is a diagram showing a schematic appearance of a hollow fiber membrane module of the present invention using the second hollow fiber membrane of the present invention. The inner diameter of the tubular hollow fiber membrane constituting the hollow fiber membrane module in FIG. 17 is constant in the longitudinal direction of the hollow fiber membrane, and the end of the hollow fiber membrane has a tube wall thickness at the end other than the end. Since the thickness is larger than the thickness of the wall, the diameter of the end portion is larger than the diameter of the hollow fiber membrane other than the end portion.

In this hollow fiber membrane module, the end (thick portion) of the hollow fiber membrane having a large diameter is further bonded with an adhesive to form an adhesive portion (a net-like shape crossing at about 90 ° in FIG. 17). Are formed and bound, so that in the portion of the hollow fiber membrane other than the large-diameter end portion, a gap (flow path of the liquid to be treated) is formed between adjacent hollow fiber membranes. Can be formed, the flow rate of the liquid to be treated can be sufficiently secured when the hollow fiber membrane is housed in the hollow fiber membrane built-in chamber, and a decrease in the degassing ability of the hollow fiber membrane can be sufficiently prevented. further,
In this hollow fiber membrane module, the end of the hollow fiber membrane having a large diameter is bonded and bound with an adhesive, so that the strength of the bound portion can be increased.

Further, in the hollow fiber membrane module of FIG. 17, the vicinity of the region indicated by reference numeral 170 of the portion where the ends (thick portions) of the hollow fiber membranes having a large diameter are bound (not bonded with an adhesive) Even if the flow of the liquid to be treated from the inflow port collides with the region, the hollow fiber membrane can be protected since the wall thickness of the hollow fiber membrane is larger.

As described above, by increasing the wall thickness of the tube wall at the end of the hollow fiber membrane, the strength of the hollow fiber membrane can be increased, and the life of the hollow fiber membrane can be extended. As a result, the binding force of the binding portion of the hollow fiber membrane module can be increased, and the flow of the liquid to be treated can be maintained.

[Embodiment 11] FIG. 19 shows an example of a hollow fiber membrane having spiral projections on the outer peripheral surface, which is an example of the second hollow fiber membrane of the present invention. FIG. 19A is a schematic external view of a hollow fiber membrane having a spiral projection 190 on the outer peripheral surface that spirally surrounds the outer peripheral surface of the tubular hollow fiber membrane in the longitudinal direction of the hollow fiber membrane. (B) of FIG. 19 is a diagram showing only the end face of the hollow fiber membrane of (a) of FIG. (C) of FIG.
An outline of a hollow fiber membrane having spiral projections 191 surrounding the outer peripheral surface of a tubular hollow fiber membrane in a spiral manner in the longitudinal direction of the hollow fiber membrane on the outer peripheral surface, and having outer diameters at both ends larger than other portions. It is an external view. In addition, on the outer peripheral surface of these hollow fiber membranes, one or more linear or substantially linear projections extending in the longitudinal direction of the hollow fiber membrane can be further provided. The linear or substantially linear projection has an action of reinforcing the spiral projection.

The linear or substantially linear projections can be provided at substantially equal intervals in the outer circumferential direction of the outer peripheral surface of the hollow fiber membrane, but need not necessarily be provided at substantially equal or equal intervals. The number of such linear projections is preferably 3
Or more, and more preferably 4 or more (for example, 6 to 8 or the like). Incidentally, the hollow fiber membrane of the present invention,
Only one or more (for example, three or more, preferably four or more, more preferably six to eight, etc.) linear projections may be provided on the outer peripheral surface.

Embodiment 12 FIG. 20 shows another example of the second hollow fiber membrane of the present invention having a spiral projection on the outer peripheral surface. FIG. 20 is a schematic external view of a hollow fiber membrane having a plurality of spiral projections 200 on its outer peripheral surface that spirally surround the outer peripheral surface of a tubular hollow fiber membrane in the longitudinal direction of the hollow fiber membrane. The pitch (length in the longitudinal direction of the tubular hollow fiber membrane) until one spiral projection makes one round of the outer periphery of the hollow fiber membrane is:
For example, twice or more (preferably 4 to 5 times or more, more preferably 4 to 1) times the outer diameter of the hollow fiber membrane (outer diameter excluding protrusions).
About 0 times). Such a hollow fiber membrane can be manufactured, for example, by integrally molding the same material (eg, resin) with a mold.

Embodiment 13 FIG. 21 shows another example of the second hollow fiber membrane of the present invention. FIG. 21 shows a hollow fiber membrane in which the outer peripheral shape of the radial cross section at the center is a substantially regular hexagon, and the outer diameter of both ends is larger than that of the other part (center). FIG. 4 is a schematic external view of a hollow fiber membrane in which the shape of the outer periphery of the radial cross section is substantially a regular hexagon and the shape of the inner periphery of the radial cross section is substantially a regular hexagon.

The hollow fiber membrane may have another polygonal shape (eg, a triangle, a quadrangle, a pentagon, or a heptagon or more polygon) in the outer periphery of the radial cross section of the central portion having a small diameter. Can be. The polygon may be an equilateral polygon or an unequal polygon. The central portion of the hollow fiber membrane having a small diameter can be formed in a prism shape other than a hexagonal prism, for example, in a prism shape of a triangular prism or more (triangular prism, quadrangular prism, pentagonal prism, or heptagonal prism or more).

The shape of the inner peripheral contour of the radial cross section of the hollow fiber membrane may be the same as or different from the outer peripheral contour of the radial cross section. For example, in the case of a hollow fiber membrane in which the shape of the outer periphery of the radial cross section is hexagonal, the shape of the inner periphery of the radial cross section can be hexagonal, and other polygons You can also make a circle.

FIG. 22 shows an adhesive (not shown) in which both ends of the hollow fiber membrane 220 are substantially the same as the hollow fiber membrane shown in FIG.
It is a schematic external view of the hollow fiber membrane module bound by (1). Since this hollow fiber membrane module has gaps at portions other than both ends, the liquid to be treated can flow evenly between the hollow fiber membranes.

The hollow fiber membrane shown in FIG. 21 is provided with spiral projections on the outer peripheral surface, so that the hollow fiber membrane has spiral projections 230 on the outer peripheral surface as shown in FIG. it can. In addition, the hollow fiber membrane shown in FIG. 21 has a cylindrical shape at a portion of the hollow fiber membrane other than both ends having a large outer diameter, and has spiral projections on an outer peripheral surface thereof, whereby the hollow fiber membrane shown in FIG.
The hollow fiber membrane can be a hollow fiber membrane having a cylindrical outer portion except for both ends having a large outer diameter as shown in FIG. Each of the hollow fiber membranes shown in FIGS. 23 and 24 can be manufactured by, for example, integrally molding using a mold. Further, the hollow fiber membrane shown in FIG. 23 or FIG. 24 can be bound into a hollow fiber membrane module by bonding both ends with an adhesive as shown in FIG.

Each of the hollow fiber membranes shown in FIGS. 19 to 24 has a hollow space even when a plurality of hollow fiber membranes are used in a bundle, since there is a sufficient gap between the hollow fiber membranes. The flow of the liquid to be treated outside the yarn membrane is always constant, and a stable flow rate of the liquid to be treated can be secured. Also, when the inside of the tube of the hollow fiber membrane is used under reduced pressure, it is hardly crushed.

Embodiment 14 FIG. 25 shows another example of the gas-liquid separation module of the present invention. FIG. 25A is a schematic external view of the gas-liquid separation module viewed from a direction perpendicular to the longitudinal direction, and arrows 250 indicate positions and directions in which the liquid to be treated flows into the gas-liquid separation module. . (B), (c), and (d) of FIG. 25 show a schematic cross section in a direction perpendicular to the longitudinal direction of the gas-liquid separation module at the central portion where the diameter of the gas-liquid separation module is small. In FIGS. 25B, 25C, and 25D, the thickness of the partition partitioning each flow path is shown in a simplified manner.

FIG. 25 (b) shows a case where the gas-liquid separation module has six flow paths in one direction in the longitudinal direction. For example, a cylindrical pipe is provided in each of three pipes having a fan-shaped cross section. Can be formed. FIG. 25 (c) shows a case where there are twelve one-way channels in the longitudinal direction. For example, in each of six tubes having a fan-shaped cross-section, a tube having a substantially triangular cross-section in the radial direction is provided. It can be formed by providing. FIG. 25 (d) shows a case in which eight one-way channels are provided in the longitudinal direction. For example, tubes each having a substantially square cross-section in the radial direction are provided in each of four tubes having a fan-shaped cross-section. Can be formed. The gas-liquid separation module of the present embodiment has a length in the longitudinal direction substantially equal to the length of the gas-liquid separation module of the first embodiment in the longitudinal direction, and has an average cross-sectional area per one flow path. The hollow fiber membrane module is provided in the flow path of the gas-liquid separation module of Example 1 by providing the flow path with substantially the same total cross-sectional area (total cross-sectional area in the direction perpendicular to the direction in which the liquid to be treated flows). As compared with the gas-liquid separation module of Example 1, a very large amount of liquid to be treated can be treated.

Embodiment 15 FIGS. 26 to 28 show another example of the gas-liquid separation module of the present invention. FIG. 26 is a schematic external view of the gas-liquid separation module viewed from a direction perpendicular to the longitudinal direction. FIG. 27 is a cross-sectional view of the gas-liquid separation module shown in FIG. FIG. 28 is a cross-sectional view of the gas-liquid separation module shown in FIG.

The gas-liquid separation module has a header 2
61 to 266, hollow fiber membrane built-in chambers 267 to 272, and a liquid quality improving member built-in chamber 273 in which a member for improving the quality of the liquid to be treated is built. Each of the header portions 261 to 266 has a pentagonal cross section in a direction perpendicular to the direction in which the liquid to be treated flows. Each of the hollow fiber membrane built-in chambers 267 to 272 and the liquid quality improving member built-in chamber 273 is a tubular body having a regular hexagonal cross section in a direction perpendicular to the direction in which the liquid to be treated flows.

The header 261 is provided in the hollow fiber membrane built-in chamber 26.
Communicate with 7. The hollow fiber membrane built-in chamber 267 is
It communicates with the hollow fiber membrane built-in chamber 268 via 62. The hollow fiber membrane built-in chamber 268 communicates with the hollow fiber membrane built-in chamber 269 via the header portion 263. The hollow fiber membrane built-in chamber 269 communicates with the hollow fiber membrane built-in chamber 270 via the header 264. The hollow fiber membrane built-in chamber 270 communicates with the hollow fiber membrane built-in chamber 271 via the header 265. Hollow fiber membrane built-in room 2
Reference numeral 71 denotes a hollow fiber membrane built-in chamber 27 through a header 266.
Communicate with 2. The hollow fiber membrane built-in chamber 272 communicates with the liquid quality improving member built-in chamber 273.

Therefore, first, the liquid to be treated, which has flowed into the header portion 261 which is the flow velocity relaxation chamber,
Gas-liquid separation is performed sequentially through 7 to 272, and the liquid to be treated is improved after passing through the liquid quality improvement member built-in chamber 273 and discharged from the gas-liquid separation module. As a member for improving the quality of the liquid to be treated, there are a filter, a filter, a spherical ceramic, and the like. This gas-liquid separation module is particularly suitable when the liquid to be treated is a liquid to be treated such as for chemicals, chemicals, and medical use, or drinking water. The gas-liquid separation module has seven one-way tubular flow paths in the longitudinal direction of the gas-liquid separation module, and a flow path at the center is provided with a member for improving the quality of the liquid to be treated. However, the member for improving the liquid quality of the liquid to be treated is not only the last one of the seven flow paths but also the last four (or the last three or two). Can be provided in the flow path.

The hollow fiber membranes (not shown) housed in the hollow fiber membrane built-in chambers of the gas-liquid separation module of this embodiment are evacuated from both ends. Further, even when the number of the hollow fiber membrane built-in chambers in the gas-liquid separation module of this embodiment increases or decreases, the hollow fiber membranes built in each hollow fiber membrane built-in chamber can be evacuated from both ends. it can.

Embodiment 16 FIGS. 29 to 31 show another example of the gas-liquid separation module of the present invention. FIG. 29 is a schematic external view of the gas-liquid separation module viewed from a direction perpendicular to the longitudinal direction. 30A is a cross-sectional view of the gas-liquid separation module shown in FIG. 29 taken along the line aa, and FIG. 30B is a cross-sectional view of the gas-liquid separation module shown in FIG. 29 taken along the line bb.
(C) of FIG. 30 is an arrow c of the gas-liquid separation module of FIG.
It is -c sectional drawing. FIG. 31 is a schematic perspective view of a portion between the aa section and the cc section of the gas-liquid separation module in FIG. 29.

This gas-liquid separation module has a flow velocity relaxation chamber 301 into which the liquid to be treated flows, header sections 302 to 306, an outflow chamber 307 into which the liquid to be treated flows out, and a chamber with a built-in hollow fiber membrane. Each of the header portions 302 to 306 has a pentagonal cross section in a direction perpendicular to the direction in which the liquid to be treated flows. The flow mitigation chamber 301 and the outflow chamber 307
The liquid to be treated before and after the treatment is separated by a partition so as not to mix. Each of the hollow fiber membrane containing chambers is a tubular body having a regular hexagonal cross section in a direction perpendicular to the direction in which the liquid to be treated flows.

[0107] The flow velocity relaxation chamber 301 communicates with the hollow fiber membrane built-in chamber. The hollow fiber membrane-containing chamber communicates with the hollow fiber membrane-containing chamber via the header section 302. The hollow fiber membrane-containing chamber communicates with the hollow fiber membrane-containing chamber via the header section 303. The hollow fiber membrane-containing chamber communicates with the hollow fiber membrane-containing chamber via the header section 304. The hollow fiber membrane-containing chamber communicates with the hollow fiber membrane-containing chamber via the header section 305.
The hollow fiber membrane-containing chamber communicates with the hollow fiber membrane-containing chamber via the header section 306. The hollow fiber membrane built-in chamber is the outflow chamber 3
07.

Therefore, first, the liquid to be treated, which has flowed into the flow velocity relaxation chamber 301, passes through the hollow fiber membrane built-in chambers 1 to 3 and is separated into gas and liquid, and flows out from the outflow chamber 307. The hollow fiber membrane built-in chamber of the gas-liquid separation module has a hexagonal cross section in a direction perpendicular to the longitudinal direction of the gas-liquid separation module, but may have an octagonal or decagonal shape.

[0109]

The gas-liquid separation module of the present invention has a hollow fiber membrane built-in chamber having an inlet and an outlet for a liquid to be treated and containing a hollow fiber membrane, and a flow rate of the supplied liquid to be treated is reduced. Since there is a flow rate relaxation chamber communicating with the inflow port of the liquid to be treated in the hollow fiber membrane built-in chamber, it is possible to prevent cracks and pinholes from being generated in the hollow fiber membrane and to remove a large amount (large flow rate) of the liquid to be treated. It can be processed efficiently.

The hollow fiber membrane built-in chamber is divided into two or more gas-liquid separation chambers, and the two or more gas-liquid separation chambers communicate with each other so that the flow path of the liquid to be treated in the hollow fiber membrane built-in chamber becomes long. The gas-liquid separation module of the present invention having the constitutional requirements of
The hollow fiber membrane-containing chamber is tubular, and the tubular hollow fiber membrane-containing chamber has two or more gas-liquid separation chambers defined by partition walls extending in the axial direction of the tube. The gas-liquid separation module according to the present invention, which has a constitutional requirement of having at least one set of two gas-liquid separation chambers that communicate with each other via a header portion provided on the outer peripheral portion of the thread film built-in chamber, further comprises: Even if the liquid is a large amount (large flow rate), the concentration of the gas contained in the processing liquid obtained after the processing can be further reduced.

The first hollow fiber membrane of the present invention has a crush prevention device or a crush prevention part for preventing crushing of the hollow fiber membrane in the tube of the hollow fiber membrane. Even when the inside of the hollow fiber membrane is decompressed to such an extent that the inner walls come into contact with each other, it is possible to prevent the hollow fiber membrane from being crushed to such an extent that the inner walls of the hollow fiber membrane come into contact with each other, and to always maintain the deaeration function. Therefore, since the degree of vacuum in the tube of the hollow fiber membrane can be increased (the pressure in the tube can be further reduced), the degassing performance (degassing ability) of the hollow fiber membrane can be increased, and a large amount (large) Flow rate) can be efficiently processed.

Further, since the second hollow fiber membrane of the present invention has a projection on the outside of the tube or a thick portion at the end of the tube, the hollow fiber membrane comes into contact with the hollow fiber membrane to form the hollow fiber membrane. It is possible to prevent the degassing ability from being reduced.

[Brief description of the drawings]

FIG. 1 is a schematic perspective view of one embodiment of a gas-liquid separation module of the present invention.

FIG. 2 is a cross-sectional view taken along a line II-II of the gas-liquid separation module of FIG. 1 taken in a direction perpendicular to the longitudinal direction, and shows a first header 5 in which a supply water coupling and a degassing water coupling are connected. Appear on the cut surface.

FIG. 3 is a sectional view taken along line III-III of the gas-liquid separation module shown in FIG. 1 in a direction perpendicular to the longitudinal direction, and shows a second embodiment in which neither the feed water coupling nor the degassing water coupling is connected. The header 7 appears on the cut surface.

FIG. 4 is a schematic perspective view of a tubular body 41 near a first header 45. FIG.

FIGS. 5A and 5B are schematic perspective views each showing an example of a plate-shaped member.

FIG. 6 is a radial cross-sectional view of the tubular body portion 61, showing the tubular body portion 61 and a cross section in the vicinity thereof.

FIG. 7 is a schematic perspective view of a tubular body 71 near the first header 75.

FIG. 8 is a schematic perspective view of a tubular body 81 near the first header 85.

FIG. 9 is a longitudinal sectional view of an example of the gas-liquid module of the present invention.

FIG. 10 is a cross-sectional view in a direction perpendicular to the longitudinal direction of an example of the gas-liquid separation module of the present invention, in which a first header 105 to which a feed water coupling and a degassing water coupling are connected has a cut surface. It appears in the.

FIG. 11 is a schematic perspective view of one embodiment of a gas-liquid separation module of the present invention in which a cap member is covered on a joint for a vacuum cover.

12 (1a), (2a) and (3a) show the structure of the crush prevention device in the hollow fiber membrane of the present invention, respectively. FIG. 12 (1b), (2b) and (3b) The figure which looked at the crush prevention tool in the hollow fiber membrane of this invention from the opening end side of the tube of the hollow fiber membrane, respectively is shown.

13 (4a) shows the structure of the crush prevention device in the hollow fiber membrane of the present invention, and FIGS. 13 (4b) and (5b) show the structure of the crush prevention device in the hollow fiber membrane of the present invention, respectively. The figure which looked at from the opening end side of the tube of a thread membrane is shown.

FIGS. 14 (6a) and (7a) show the structure of the hollow fiber membrane having the crush preventing portion of the present invention, and FIGS. 14 (6b) and (7b) show the structure of the crush preventing portion of the present invention, respectively. The figure which looked at the hollow fiber membrane which has from the opening end side of the tube of a hollow fiber membrane is shown.

FIGS. 15 (a) and (b) are longitudinal sectional views of the hollow fiber membrane of the present invention each having a projection on the outer peripheral surface of the tubular hollow fiber membrane.

FIG. 16 is a longitudinal sectional view of one embodiment of the gas-liquid separation module of the present invention, showing a vicinity of a first header.

FIG. 17 is a view schematically showing the appearance of one embodiment of the hollow fiber membrane module of the present invention.

FIG. 18 is a cross-sectional view of one example of the gas-liquid separation module of the present invention, and is a cross-sectional view showing another example of a cross section corresponding to the cross section shown in FIG.

FIG. 19 (a) is a schematic external view of a hollow fiber membrane according to one embodiment of the present invention. (B) of FIG. 19 is a diagram showing only the end face of the hollow fiber membrane of (a) of FIG. FIG.
(C) is a schematic external view of a hollow fiber membrane according to another embodiment of the present invention.

FIG. 20 is a schematic external view of a hollow fiber membrane of one embodiment of the present invention.

FIG. 21 is a schematic external view of a hollow fiber membrane according to one embodiment of the present invention.

FIG. 22 is a schematic external view of the hollow fiber membrane module according to one embodiment of the present invention, as viewed from a direction perpendicular to the longitudinal direction of the hollow fiber membrane constituting the hollow fiber membrane module.

FIG. 23 is a schematic external view of a hollow fiber membrane according to one embodiment of the present invention.

FIG. 24 is a schematic external view of a hollow fiber membrane according to one embodiment of the present invention.

FIG. 25 (a) is a schematic external view of a gas-liquid separation module according to an embodiment of the present invention as viewed from a direction perpendicular to a longitudinal direction. (B), (c) and (d) of FIG.
FIG. 3 is a diagram showing a schematic cross section in a direction perpendicular to a longitudinal direction of the gas-liquid separation module at a central portion of the gas-liquid separation module having a small diameter.

FIG. 26 is a schematic external view of the gas-liquid separation module according to one embodiment of the present invention as viewed from a direction perpendicular to a longitudinal direction.

FIG. 27 is a cross-sectional view of the gas-liquid separation module shown in FIG. 26, taken along the line AA.

28 is a cross-sectional view of the gas-liquid separation module shown in FIG. 26, taken along the line BB.

FIG. 29 is a schematic external view of the gas-liquid separation module viewed from a direction perpendicular to the longitudinal direction.

30A is a cross-sectional view of the gas-liquid separation module taken along line aa of FIG. 29, and FIG.
FIG. 3 is a sectional view taken along line bb of FIG.
0 (c) is an arrow cc of the gas-liquid separation module of FIG.
It is sectional drawing.

FIG. 31 is a diagram showing a of the gas-liquid separation module of FIG. 29;
It is a schematic perspective view of the part between -a cross section and cc cross section.

 ──────────────────────────────────────────────────続 き Continued on the front page F term (reference) 4D006 GA32 HA02 JA02A JA13A JA15A JA16A JA17A JA18A JA25A JA29A JA51A JA52A JA70A JB04 MA01 MC65 PC80 4D011 AA17

Claims (19)

[Claims] 1. A hollow fiber membrane built-in chamber having an inlet and an outlet for a liquid to be treated and containing a hollow fiber membrane therein, and a flow rate of the supplied liquid to be treated is relaxed so that the hollow fiber membrane built-in chamber is processed. A gas-liquid separation module having a flow velocity relaxation chamber communicating with a liquid inlet. 2. The hollow fiber membrane-containing chamber is divided into two or more gas-liquid separation chambers, and the two or more gas-liquid separation chambers communicate with each other so that the flow path of the liquid to be treated in the hollow fiber membrane-containing chamber becomes long. The gas-liquid separation module according to claim 1, wherein: 3. The hollow fiber membrane-containing chamber is tubular, and the tubular hollow fiber membrane-containing chamber has two or more gas-liquid separation chambers defined by partition walls extending in the axial direction of the tube. The gas-liquid separation chamber according to claim 1, further comprising at least one pair of two gas-liquid separation chambers that communicate with each other via a header provided on an outer peripheral part of the tubular hollow fiber membrane built-in chamber. 4. Gas-liquid separation module. 4. The gas-liquid separation module according to claim 1, wherein the hollow fiber membrane built-in chamber has two or more inlets for the liquid to be treated. 5. The gas-liquid separation module according to claim 1, wherein the hollow fiber membrane built-in chamber has an inlet for the liquid to be treated partitioned by a partition plate. 6. The gas-liquid separation module according to claim 5, wherein the partition plate has a thickness gradient. 7. The hollow-fiber-membrane-containing chamber such that the area of the inflow port of the liquid to be treated in the hollow-fiber-membrane-containing chamber increases as the distance from the supply port of the liquid to be supplied to the flow-rate relaxation chamber increases. The gas-liquid separation module according to any one of claims 1 to 6, wherein a plurality of inlets for the liquid to be treated are arranged. 8. The hollow-fiber-membrane-containing chamber so that the area of the inflow port of the liquid to be treated in the hollow-fiber-membrane-containing chamber increases as the distance from the supply port of the to-be-processed liquid supplied to the flow velocity relaxation chamber increases. The gas-liquid separation module according to any one of claims 1 to 7, wherein the shape of the inlet of the liquid to be treated is set. 9. The air chamber according to claim 1, wherein a shape of the hollow fiber membrane-containing chamber is set so that the hollow fiber membrane does not contact the hollow fiber membrane-containing chamber. Liquid separation module. 10. The gas-liquid separation module according to claim 1, wherein the hollow fiber membrane is a substantially nonporous silicone hollow fiber membrane. 11. The gas-liquid separation according to claim 1, wherein the hollow fiber membrane has a crush prevention device or a crush prevention part for preventing the hollow fiber membrane from being crushed. module. 12. The gas-liquid separation module according to claim 1, wherein the hollow fiber membrane has a projection outside the tube or a portion having a large outer diameter at an end of the tube. . 13. The hollow fiber membrane is housed in the hollow fiber membrane-containing chamber with a gap provided to ensure a sufficient flow rate of the liquid to be treated. A gas-liquid separation module according to item 1. 14. A hollow fiber membrane module comprising a hollow fiber membrane module formed by binding said ends of a hollow fiber membrane in which the thickness of a tube wall at an end is larger than the thickness of a tube wall other than said end. The hollow fiber membrane built-in chamber is built in the hollow fiber membrane built-in chamber.
The gas-liquid separation module according to any one of the above. 15. A hollow fiber membrane comprising a crush prevention device or a crush prevention part for preventing the crush of the hollow fiber membrane in a tube of the hollow fiber membrane. 16. The hollow fiber membrane according to claim 15, wherein the hollow fiber membrane has a projection on the outside of the tube or a thick portion at the end of the tube. 17. A hollow fiber membrane having a projection on the outside of a tube or a thick portion at an end of the tube. 18. A hollow fiber membrane module comprising ends of a plurality of tubular hollow fiber membranes, wherein the thickness of the end of the hollow fiber membrane is larger than the thickness of the other end. Features hollow fiber membrane module. 19. The hollow fiber membrane module according to claim 18, wherein the thickness of the tube wall at the end of the hollow fiber membrane is larger than the thickness of the tube wall other than the end.