JPH0441932Y2 - - Google Patents

Description

[Detailed description of the invention] (Field of industrial application) This invention uses SS coexisting liquids such as biological treatment liquids, industrial wastewater, and river water as the liquid to be treated, and the liquid to be treated is applied to the pipe wall of the hollow fiber membrane. This invention relates to an external pressure type hollow fiber membrane separator that allows SS to permeate from the outside surface and obtain a high flux of SS separated in the hollow part.

(Prior art) Conventionally, there has been a process in which the inside of a pressure-resistant container has a supply port for the liquid to be treated, a large number of hollow fiber membranes are arranged therein, and fine particles that are fluidized by the liquid to be treated are housed. and a liquid collecting chamber having an outlet for the processing liquid and in which at least one end of the hollow fiber membrane is opened, and the liquid to be processed is supplied under pressure into the processing chamber from the supply port to the hollow fiber. An external pressure type hollow fiber membrane separator in which the liquid permeates through the tube wall of the fiber membrane from the outside and collects the liquid from the hollow part of the hollow fiber membrane into a collection chamber is known from JP-A-57-167785.

This conventional external pressure type hollow fiber membrane separator fluidizes the fine particles in the chamber with the liquid to be treated, and the fluidized fine particles form a concentration polarized layer or gel on the outer surface of the hollow fiber membrane. The liquid to be treated is permeated from the outer surface to the inner surface of the pipe wall of the hollow fiber membrane while preventing the formation of layers, and the liquid to be treated is obtained in the liquid collection chamber.

(Problem that the invention aims to solve) However, in conventional equipment, when the operation is stopped, the fine particles settle at the bottom of the processing chamber, and some of the particles fall from the supply port to the outside of the processing chamber. The amount of fine particles in the room becomes insufficient. Therefore, when restarting operation, it is necessary to replenish the processing chamber with the insufficient amount of fine particles.

(Means for solving the problem) Therefore, the external pressure type hollow fiber membrane separation device of the present invention has the following features:
The present invention is characterized in that a repose angle nozzle having an angle of repose of the fine particles described above is attached to the end of the supply port for the liquid to be processed that opens into the processing chamber.

(Example) In each of the illustrated examples, 1 is a cylindrical pressure-resistant container, 2 is its top lid, 3 is also a bottom lid, 4 and 5 are a processing chamber and a liquid collection chamber formed in the container, and 6 is a hollow space. 7 is a thread membrane, 7 is a supply port for the liquid to be processed into the processing chamber, 8 is a port for taking out the processing liquid from the liquid collection chamber, 9 is a fine particle, and 10 is a repose angle nozzle.

The inner diameter of the pressure vessel 1 is larger in the lower half than in the upper half, and there is a step 1' between them.
Tighten with a nut to removably connect. Top lid 2
The bottom cover 3 has an outlet 2' for the concentrated liquid at the center, and an inlet 3' for the liquid to be treated at the center. The fine particles 9 are glass beads with a particle size of about 0.35 to 0.5 mm, and the angle of repose nozzle 10 is hollow as shown in FIG. It consists of a cylindrical part 11 that is erected on the supply port 7 with a male thread on the outer periphery, and a cap 12 that is fixed by closing the upper end of the cylindrical part and has a peripheral edge that extends from around the cylindrical part.
The angle θ of the line connecting the lower edge of 1′ and the outer edge of the shade 12 with respect to the horizontal is equal to or larger than the angle of repose of the grains used, and even if buried in the grains. It has a structure that prevents particles from entering the interior through the window hole 11'.

Now, in the embodiment shown in FIG. 1, each end of a large number of hollow fiber membranes 6 whose length is approximately equal to the length of the lower half of the pressure-resistant container is connected to two disc-shaped potting parts 13 with a distance maintained between them. , 14. The outer diameter of each of the potting parts 13 and 14 is equal to the inner diameter of the lower half of the pressure vessel 1, and can be fitted into the lower half of the pressure vessel.

As a result, one potting part 13 is fitted into the upper part of the lower half of the pressure container until it comes into contact with the step 1', and the other potting part 14 is fitted into the lower part of the lower half, fixed by, for example, adhesive or welding, and the hollow fiber The membrane 6 is made straight in the vertical direction.

In this way, a processing chamber 4 in which the hollow fiber membranes 6 are arranged in the axial direction is formed between the potting parts 13 and 14, and above the potting part 13, that is, the pressure vessel 1
The inside of the upper half is partitioned by the potting part 13,
A liquid collecting chamber 5 in which a hollow fiber membrane 6 is opened is formed on the upper surface of the potting part 13. For this reason, pressure vessel 1
A processing liquid outlet 8 is provided on the side surface of the upper half, and a processing liquid supply port 7 is provided in the center of the lower potting part 14, which communicates with the inlet 3' of the bottom cover. The nozzle 9 is attached and projected into the processing chamber.

Incidentally, an opening is also provided in the center of the upper potting part 13, and this is connected to the outlet 2' of the upper lid through a connecting pipe 15.

Fine particles 9 are put into the processing chamber 4, but even if they are put into the pressure container, the top lid, the bottom lid, and the hollow fiber membrane bundled in the potting section when the device is assembled, they are not added to the liquid to be treated at the beginning of operation. They may be mixed and added as a slurry.

As a result, it is pressurized by the pump, passes through the inlet 3', the supply port 7, and the window hole 1 around the angle of repose nozzle 10.
The liquid to be treated that is supplied into the processing chamber 4 from 1' comes into contact with the outer surface of the hollow fiber membrane 6 as it flows upward while fluidizing the fine particles 9 in the chamber, and the liquid that can pass through the tube wall is removed from the outer surface. It passes through the pipe wall and enters the hollow part, where it is separated from SS, etc. The processing liquid that has entered the hollow part of each hollow fiber membrane in this way collects in the liquid collecting chamber 5 from the upper end of the hollow fiber membrane and is taken out from the outlet 8, while the concentrated liquid to be processed passes through the connecting pipe 15 and is discharged from the upper lid. It is discharged from outlet 2'. During operation, the fine particles 9 become fluidized and dance wildly in the processing chamber 4, suppressing the formation of a concentration polarized layer or a gel layer on the outer surface of the hollow fiber membrane 6.

Therefore, efficient membrane separation can be performed by supplying the liquid to be treated to the processing chamber at such an upward flow rate that the fluidized upper surface of the fine particles becomes the lower surface of the upper potting section 13.

Furthermore, when the operation is stopped, the fine particles are deposited on the upper surface of the lower potting part 14 which has the supply port for the liquid to be treated, but because the angle of repose nozzle 10 is attached to this supply port, they do not fall and are not deposited in the processing chamber. is maintained.

When the fine particles are to be taken out of the processing chamber for replacement, etc., they can be taken out from the inlet 3' together with the liquid contained in the processing chamber.

In the embodiment shown in FIG. 2, a large number of hollow fiber membranes 6 are each bent into an arch shape or an inverted U shape, and both ends of each are bent into an arch shape or an inverted U shape.
The hollow fiber membranes are fixed to one disk-shaped potting part 16 with a distance maintained between them, and both ends of each hollow fiber membrane are opened at the lower surface of the potting part 16. The outer diameter of the potting part 16 is also matched to the large-diameter lower half of the pressure container, and the potting part 16 is fitted into the lower half from below until it abuts against the step 1' inside the container 1 and is fixed.

As a result, a processing chamber 4 in which arch-shaped or inverted U-shaped hollow fiber membranes are arranged is formed in the upper half of the pressure-resistant container, and a liquid collection area with both ends of each hollow fiber membrane 6 opened under the potting section 16 is formed. A chamber 5 is formed. Therefore, the supply port 7 for the liquid to be treated is provided at the center of the potting section 16, and the angle of repose nozzle 10 is erected so as to protrude into the processing chamber 4. are connected by a communication pipe 17, and a processing liquid outlet 8 is provided on the side of the lower half of the pressure-resistant container.
The concentrated liquid is to be discharged from the discharge port 2' of the upper lid.

The fine particles 9 may be introduced into the processing chamber 4 at the time of assembling the apparatus, or may be mixed with the liquid to be processed and added to the slurry at the beginning of operation.

In this embodiment as well, the liquid to be treated is pressurized by a pump and supplied into the processing chamber 4 from the window hole 11' around the angle of repose nozzle 10 via the inlet 3', the connecting pipe 17, and the supply port 7. When the fine particles 9 are fluidized and flow upward in the chamber, those that come into contact with the outer surface of the hollow fiber membrane 6 and can pass through the tube wall pass through the tube wall from the outer surface and enter the hollow part, where they are separated from SS, etc. do. In this way, the processing liquid that has entered the hollow part of each hollow fiber membrane falls from both downward ends of the hollow fiber membrane into the liquid collecting chamber 5, collects therein, and is taken out from the outlet 8, while the concentrated liquid is discharged from the upper lid through the outlet 2'.
is discharged from. During operation, the fine particles 9 become fluidized and dance wildly in the processing chamber 4, suppressing the formation of a concentration polarized layer or a gel layer on the outer surface of the hollow fiber membrane 6.

Therefore, membrane separation can be carried out efficiently by supplying the liquid to be treated to the processing chamber at such an upward flow rate that the fluidized upper surface of the fine particles becomes the lower surface of the upper lid 2.

Furthermore, when the operation is stopped, the fine particles are deposited on the upper surface of the potting part 16 that has the supply port for the liquid to be treated, but because the angle of repose nozzle 10 is attached to this supply port, they do not fall and are retained in the processing chamber. be done.

When the fine particles are to be taken out of the processing chamber for replacement, etc., they can be taken out from the inlet 3' together with the liquid contained in the processing chamber.

Although two embodiments of the present invention have been described above, the amount of fine particles to be introduced into the processing chamber may be about 40 to 80% of the capacity of the processing chamber.

Using the apparatus shown in Figures 1 and 2, we conducted experiments in which fine particles were placed in the processing chamber 4 and the liquid was passed through it, and in which the liquid was passed without it.The following results were obtained. was gotten. In addition, the liquid to be treated is SS.
The activated sludge mixture contains 100PPM, the pressure container has an inner diameter of 100mm and a height of 800mm, and the height of the processing chamber is 600mm.
The fine particles were glass beads with a particle size of 0.35 to 0.5 mm, which accounted for about 60% of the capacity of the processing chamber.

Experimental example 1 When fine particles are added, the upward flow linear velocity L/V1.5
The liquid was passed at a rate of cm/sec, and permeated water was obtained at 140 mm/min, and operation continued smoothly for 500 hours.

Experimental example 2 When the liquid was passed at the same upward linear velocity without adding fine particles, the same amount of permeated water could be obtained for up to 10 hours after the start of operation, but after that, the amount of permeated water obtained decreased. The amount of permeated water gradually decreased to 14 mm/min 100 hours after the start of operation.

Experimental example 3 Even after 500 hours had passed since the start of operation without adding fine particles, in order to obtain the same permeated water of 140 mm/min as at the beginning of operation, the upward linear water velocity had to be increased to 1.5 m/sec. .

As a result, the running cost of electricity required to drive the pump was 0.06KW/hour/m ³ in Experimental Example 1 and 6.0KW/hour/m ³ in Experimental Example 3, making it possible to perform the membrane separation in Experimental Example 1 with much lower energy. Ta.

Further, each of the illustrated embodiments is a single stage, but the same device may be connected in multiple stages in the vertical direction and used in multiple stages such that the concentrated liquid discharged from the lower stage is further subjected to membrane separation at the upper stage. good. In this case, in the apparatus shown in FIG.
Although it is not necessary when the hollow fiber membrane is buried inside and is blocked, when the lower end of the hollow fiber membrane is open on the lower surface of the potting section 14, the partition plate 18 that closes the upper surface of the liquid collection chamber 5 is moved as shown by the broken line. The potting section 14 of the upper device is placed on top of the potting section 14, and the opening at the lower end of the hollow fiber membrane is closed with a partition plate. Further, in the apparatus shown in FIG. 2, a partition plate 18 is provided to close the upper surface of the processing chamber 4, and the upper apparatus is stacked on the partition plate 18, so that the upper liquid collection chamber and the processing chamber of the lower apparatus are separated by the partition plate 18.

(Effect of the invention) According to the invention, fine particles are deposited at the bottom of the processing chamber where the supply port for the liquid to be treated is opened when the operation is stopped, but the repose angle nozzle is installed at the supply port opened in the processing chamber. is installed, the fine particles are retained in the processing chamber without falling into the supply port. Therefore, the necessary amount of fine particles can always be maintained in the processing chamber without using any special means such as a fine particle replenishment device. Therefore,
The concentration polarized layer or gel layer generated on the outer surface of the hollow fiber membrane can always be efficiently removed, and stable membrane separation can be performed with low energy.

Generally speaking, membrane separators have ON-OFF switching due to their characteristics.
I usually drive. ON-OFF like this
If fine particles were supplied into the processing chamber each time the operation was performed, work efficiency and operational efficiency would decrease. Furthermore, if a means for replenishing fine particles is added, both the apparatus itself and the control system for operation become complicated, making the operation complicated and increasing the cost. The present invention completely eliminates the above-mentioned inconveniences by having a simple configuration in which an angle of repose nozzle is provided at the supply port of the water to be treated that opens into the treatment chamber.

[Brief explanation of the drawing]

FIG. 1 is a sectional view of one embodiment of the present invention, FIG. 2 is a sectional view of another embodiment, and FIG. 3 is a sectional view of a repose angle nozzle. In the figure, 1 is a pressure-resistant container, 2 is a top lid, 2' is a concentrated liquid outlet, 3 is a bottom lid, 3' is an inlet for a liquid to be treated, 4 is a processing chamber, 5 is a liquid collection chamber, and 6 is a hollow space. 7 is a thread membrane, 7 is a supply port for a liquid to be treated, 8 is an outlet for a processing liquid (flux), 9 is a fine particle, and 10 is a repose angle nozzle.

Claims (1)

[Scope of claim for utility model registration] The inside of the pressure-resistant container has a supply port for the liquid to be treated,
In addition to arranging a large number of hollow fiber membranes inside,
A processing chamber containing fine particles to be fluidized by the liquid to be treated, and a liquid collection chamber having an outlet for the treatment liquid and in which at least one end of the hollow fiber membrane is opened inside, A liquid to be treated that is pressurized and supplied into the treatment chamber is permeated through the tube wall of the hollow fiber membrane from the outside surface,
In the external pressure type hollow fiber membrane separator that collects liquid from the hollow part of the hollow fiber membrane into a liquid collecting chamber, a repose having an angle of repose of the fine particles at an end of a supply port for the liquid to be treated opened in the processing chamber. An external pressure hollow fiber membrane separation device featuring a square nozzle.