JP2024021327A - Coagulation granulator and water treatment device - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a coagulation granulator where water to be treated is agitated with smaller agitation power and a part of the water to be treated can be coagulated even when the treatment amount of the water to be treated is large.

SOLUTION: In a coagulation granulator comprising a pipe line, a coagulant injection part and a plurality of agitators,: the pipe line has an introduction port to introduce water to be treated and a discharge port to discharge the water to be treated; the coagulant injection part injects a coagulant into the water to be treated flowing in the pipe line: and the plurality of agitators are aligned in a direction crossing the flow direction of the water to be treated in the pipe line and generate the rotation flow of the water to be treated injected with the coagulant.

SELECTED DRAWING: Figure 1

COPYRIGHT: (C)2024,JPO&INPIT

Description

Embodiments of the present invention relate to an agglomeration granulation device and a water treatment device including the aggregation and granulation device.

Conventionally, in water treatment plants, industrial wastewater plants, power plants, etc., suspended solids (hereinafter also referred to as "turbid matter") such as metal ions, organic substances, and inorganic salts are removed from raw water using solid-liquid separators. separation and removal.
Typical technologies applied to this type of solid-liquid separation device include coagulation sedimentation processing technology and centrifugal separation technology.
In a solid-liquid separation device to which centrifugal separation technology is applied, after solids are floc-formed, raw water containing flocs is swirled by a centrifugal separator, and flocs larger than a predetermined particle size are separated by the action of centrifugal force. Separated from raw water. Since a centrifugal separator uses centrifugal force that has a higher acceleration than gravity, solids can be separated in a shorter time than when gravity is used, so the capacity of the sedimentation tank can be reduced.

However, when flocs with weak binding force are rotated at high speed in a centrifuge, the flocs once formed may break up and become fine. Therefore, when applying centrifugation technology, it is necessary to provide a floc formation tank in order to form flocs that are difficult to split or become fine. Furthermore, in order to form high-density and high-strength flocs, it is necessary to form a channel with shelf plates in the floc-forming tank so as to promote collision of the flocs with the wall surface.

In this way, solid-liquid separators to which centrifugal separation technology is applied can reduce the capacity of the settling tank, but since it is necessary to provide a floc-forming tank, it is not possible to downsize the entire device. difficult. Furthermore, since the floc formation tank has a complicated structure, it is not easy to manufacture.

Therefore, in order to downsize the entire device, an inorganic flocculant, a cationic polymer flocculant, and an anionic polymer flocculant are added to the raw water in a pipe-type mixer, and a high-speed (for example, 1000 (rpm) A solid-liquid separator is disclosed that has an aggregation and granulation function that aggregates and granulates suspended matter contained in raw water by stirring at a speed of 15,000 rpm).

Although a pipe-type mixer can be made compact, it is necessary to rotate stirring blades at high speed in the pipe for stirring. For this reason, when the throughput is large, the stirring power becomes large in order to rotate the large-diameter stirring blades at high speed, and the power consumption of the apparatus, that is, the running cost increases.

Patent No. 4875129 JP2010-214248A Patent No. 6805282

The problem to be solved by the present invention is that even when the amount of water to be treated is large, it is possible to stir the water with a smaller stirring power and coagulate and granulate a part of the water to be treated. An object of the present invention is to provide an agglomeration granulation device and a water treatment device including the aggregation and granulation device.

According to an embodiment, the agglomeration granulation device includes a flow path, a flocculant injection section, and a plurality of agitators. The pipe has an inlet through which the water to be treated is introduced, and an outlet through which the water to be treated is discharged. The flocculant injector injects a flocculant into the water to be treated flowing through the pipe. The plurality of agitators are arranged in parallel in a direction intersecting the flow direction of the water to be treated in the pipe, and generate a swirling flow in the water to be treated in which the flocculant has been injected.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a block diagram showing an aggregation granulation device and a solid-liquid separation device of a water treatment device according to an embodiment. 1 is a schematic diagram showing an aggregation granulation device and a solid-liquid separation device of a water treatment device according to an embodiment. FIG. 3 is a perspective view showing an agglomeration granulation device and a solid-liquid separation device of the water treatment device in FIG. 2; FIG. 4 is an exploded perspective view showing the agglomeration granulation device and solid-liquid separation device of the water treatment device in FIG. 3. FIG. FIG. 2 is a schematic perspective view showing an agitator module of the agglomeration and granulation device. FIG. 6 is an enlarged view of the area indicated by the symbol VI in FIG. 5; FIG. 2 is a schematic diagram showing the stirring blades and rotating shaft of the stirrer module of the agglomeration and granulation device. FIG. 8 is a schematic perspective view showing the stirring blades and rotating shaft of the stirrer module of FIG. 7; FIG. 2 is a schematic perspective view showing a channel assembly of a stirring plate unit of an agglomeration granulator. FIG. 2 is a schematic perspective view showing a stirring plate unit of the agglomeration and granulation device. 3 is a sectional view taken along the line XI-XI in FIG. 2. FIG. FIG. 3 is a vertical cross-sectional view of a gate valve unit of the solid-liquid separator. FIG. 3 is a schematic front view of a gate valve unit of a solid-liquid separator with an opening degree of 16%. FIG. 2 is a schematic front view of a gate valve unit of a solid-liquid separator with an opening degree of 50%. FIG. 2 is a vertical cross-sectional view of a solid-liquid separation unit of the solid-liquid separation device. A schematic diagram for explaining the mechanism of solid-liquid separation using a cyclone. The figure which shows an example of the analysis result of the pressure distribution in an inflow shell, a treated water shell, and a sludge recovery shell. FIG. 2 is a schematic front view of a solid-liquid separation unit of the solid-liquid separation device. 1 is a flowchart showing an example of the operation of the aggregation granulation system according to the embodiment. A schematic diagram showing the process from when an inorganic flocculant is injected into the water to be treated until the flocs grow. FIG. 21 is a schematic diagram following FIG. 20 showing the process from when the inorganic flocculant is injected into the water to be treated until the flocs grow. FIG. 22 is a schematic diagram following FIG. 21 showing the process from when an inorganic flocculant is injected into the water to be treated until the flocs grow. FIG. 23 is a schematic diagram following FIG. 22 showing the process from when an inorganic flocculant is injected into the water to be treated until the flocs grow. A table showing the stirring power for treating 1000 m ³ /day for the water treatment apparatuses according to the comparative example and the present embodiment. The schematic diagram which shows the stirring blade and rotating shaft of the stirrer module of the agglomeration granulation apparatus based on a modification. FIG. 26 is a schematic perspective view showing the stirring blades and rotating shaft of the stirrer module of FIG. 25;

Hereinafter, an agglomeration granulation system 1 according to an embodiment will be described with reference to the drawings.

As shown in FIG. 1, the aggregation granulation system 1 includes a water treatment device 2 and a water pump 3 that supplies raw water, that is, water to be treated W, to the water treatment device 2.

As shown in FIGS. 1 to 3, in this embodiment, the water treatment device 2 is preferably formed as a pipe type configured inside a cylindrical pipe 10, for example. The water treatment device 2 is preferably formed as straight as possible in order to prevent the water treatment device 2 from increasing in size. In this embodiment, each of the pipes 10 of the water treatment device 2 has a cylindrical shape and is formed by sequentially connecting a plurality of straight pipes 11 to 14, such as four. For example, each of the straight pipes 11 to 14 can be made of pressure-resistant 300A stainless steel. The lengths of the straight pipes 11 to 14 are set appropriately.

The water treatment device 2 includes an aggregation and granulation device 5 and a solid-liquid separation device 6 connected to the downstream side of the aggregation and granulation device 5. The agglomeration and granulation device 5 agglomerates and granulates suspended matter contained in the water to be treated W in plants such as water purification plants, industrial wastewater, power plants, and the like. In this embodiment, the agglomeration and granulation device 5 adds an appropriate flocculant (chemical) to raw water, stirs the water to be treated W that is a mixture thereof, and forms aggregates in the water to be treated. Grainy. The solid-liquid separator 6 separates aggregates from treated water W into which a flocculant has been injected into solid-liquid, returns some supernatant water from above as return water (blow water), and takes out sludge from below. At the same time, the treated water T is discharged from the discharge port 10b which is the terminal end of the pipe 10. Note that the returned water R is mixed with the water to be treated W, and is fed into the agglomeration and granulation device 5 again through the pipe 10 by the water pump 3, thereby being repeatedly treated.

In this embodiment, the aggregation and granulation device 5 has, for example, two straight pipes (pipe lines) 11 and 12. The solid-liquid separator 6 has, for example, two straight pipes (pipe lines) 13 and 14.

It is preferable that the straight pipes 11 and 12 of the agglomeration and granulation device 5 are connected straight in series. It is preferable that the straight pipes 13 and 14 of the solid-liquid separator 6 are connected straight in series. Moreover, it is suitable that the straight pipe 12 of the aggregation granulation device 5 and the straight pipe 13 of the solid-liquid separation device 6 are connected straight in series. At this time, it is preferable that the central axes of the straight pipes 11 to 14 coincide. The pipe 10 forms a flow path 15 for treating the water W to be treated by the straight pipes 11 to 14 between the inlet 10a and the outlet 10b of the pipe 10.

The aggregation and granulation device 5 has an introduction pipe 16 that introduces the water to be treated W into the straight pipe 11 . The introduction pipe 16 is, for example, directly fixed to the straight pipe 11.

In this embodiment, the water pump 3 is connected to the introduction pipe 16 at the front stage (upstream side) of the agglomeration and granulation device 5 . The water pump 3 introduces the water to be treated W into the flow path 15 of the agglomeration and granulation device 5 at an appropriate pressure.

In the present embodiment, in the water treatment device 2, the side where the water to be treated W is introduced into the agglomeration and granulation device 5 is referred to as the upstream side, and the side where the water to be treated W is discharged from the solid-liquid separation device 6 is referred to as the downstream side. . Further, the direction in which the water to be treated W sequentially flows through the pipes 11 to 14 is referred to as a flow direction L.

As shown in FIGS. 2 to 4, the agglomeration and granulation device 5 includes an aggregation and granulation unit 22 including a straight pipe 11 and a connection unit 24 including a pipe 12. In this embodiment, the agglomeration and granulation device 5 includes, for example, a gear train 26 and a motor 28 that drives the gear train 26. The drive of the motor 28 is controlled by a controller 30. The controller 30 may be included in the agglomeration and granulation device 5 or the water treatment device 2, or may be provided in a server located at an appropriate location. For this reason, it is also preferable that the motor 28 be remotely controlled.

Note that it is also suitable for the controller 30 shown in FIG. 1 to control the water pump 3. Moreover, it is also suitable for the controller 30 to control the upper and lower positions of a gate valve 71, which will be described later.

As shown in FIGS. 1 to 4, the aggregation granulation unit 22 includes straight pipes 11 and 16 as piping sections, an agitator module 34, and an agitator plate unit 36.

The straight pipe 11 is used as the main pipe of the agglomeration and granulation device 5. A stirrer module 34 and a stirring plate unit 36 are inserted into the main pipe 11 . The total length of the main pipe 11 is, for example, about 1200 mm, and the inner diameter is, for example, about 300 mm.

The straight pipe 16 is used as an introduction pipe for introducing the water W to be treated into the main pipe 11. The introduction pipe 16 has an introduction port 10a that introduces the water to be treated W into a flow path 15 formed continuously in the straight pipes 11 to 14. It is preferable that the center axis of the introduction pipe 16 and the center axis of the main pipe 11 be perpendicular to each other or intersect with each other. The center axis of the introduction pipe 16 and the center axis of the main pipe 11 may be in twisted positions.

The main pipe 11 has a flange portion 11A that projects radially outward at the upstream end, and a flange portion 11B that projects radially outward at the downstream end. An introduction pipe 16 is connected to the vicinity of the flange portion 11A of the main pipe 11. The inner diameter of the introduction pipe 16 is smaller than the inner diameter of the main pipe 11, and the introduction pipe 16 is fixed to the main pipe 11 so that the center axis of the introduction pipe 16 and the center axis of the main pipe 11 are perpendicular or intersect with each other. be done. The introduction pipe 16 communicates with the main pipe 11.

A first port 381 is provided in the introduction pipe 16 . The first port 381 is formed, for example, as a drug injection tube. For example, a pH adjuster Ma is injected into the introduction pipe 16 through the first port 381. The first port 381 is fixed to the introduction pipe 16 so that the center axis of the introduction pipe 16 and the center axis of the first port 381 are perpendicular to each other or intersect with each other. The center axis of the introduction pipe 16 and the center axis of the first port 381 may be in a twisted position.

A second port 382, a third port 383, and a fourth port 384 are provided near the flange portion 11A of the main pipe 11. The second port 382, the third port 383, and the fourth port 384 are formed, for example, as a drug injection tube. The second port 382, the third port 383, and the fourth port 384 extend from the upstream end of the main piping 11 to 1/6 to 1/6 of the total length of the main piping 11, for example. It is preferable to provide it at a position of about /3. The second port 382, the third port 383, and the fourth port 384 are provided at positions where necessary aggregation reaction time (residence time) can be secured after each flocculant is injected.

Inorganic flocculant Mb is injected into the main pipe 11 through the second port 382. A cationic polymer flocculant Mc is injected into the main pipe 11 through the third port 383. An anionic polymer flocculant Md is injected into the main pipe 11 through the fourth port 384. That is, different types of flocculants can be injected into the main pipe 11 in stages through the second port 382, the third port 383, and the fourth port 384.

Note that the pH adjusting agent Ma injected in the pH adjusting area 41 is appropriately determined depending on the type of the inorganic flocculant Mb injected in the mixing area 42. For example, in the mixing area 42, when an inorganic flocculant Mb used in a weakly acidic region or a neutral region, such as sulfuric acid and polyaluminum chloride, is added, in the pH adjustment area 41, for example, hydrochloric acid, sulfuric acid, etc. , carbonic acid is injected as a pH adjusting agent. Furthermore, if the water to be treated W is strongly acidic, caustic soda, baking soda, or the like may be injected as a pH adjuster. When an inorganic flocculant Mb used in an alkaline region such as ferrous sulfate is added in the mixing area 42, caustic soda, baking soda, etc. is injected as a pH adjuster Ma in the pH adjustment area 41. . Further, when the water to be treated W is strongly alkaline, for example, hydrochloric acid, sulfuric acid, or carbonic acid may be injected as the pH adjuster Ma.

Examples of the inorganic flocculant Mb include, but are not limited to, aluminum sulfate, polyaluminum chloride, ferrous sulfate, and ferric chloride. Sulfuric acid and polyaluminum chloride are used in acidic or neutral regions. Ferrous sulfate is used in alkaline areas. Ferric chloride is used in both acidic and alkaline regimes.

In this embodiment, for ease of explanation, the first port 381, the second port 382, the third port 383, and the fourth port 384 have the same diameter and have a communication portion with the main pipe 11. Let me explain using an example. Then, the second port 382, the third port 383, and the fourth port 384 are connected to the main pipe 11 so that the center axes of the main pipe 11 are perpendicular to each other or intersect with each other. Preferably, the third port 382, the third port 383, and the fourth port 384 are fixed.

It is preferable that the second port 382 is fixed to the main pipe 11 so that the central axis of the second port 382 and the central axis of the introduction pipe 16 are perpendicular to each other or intersect with each other. That is, it is preferable that the center axis of the introduction pipe 16 and the center axis of the second port 382 are not coaxial, but are arranged circumferentially offset from the center axis of the main pipe 11 by, for example, 90°. It is.

Among the second port 382, the third port 383, and the fourth port 384, the communicating portions with the main pipe 11 are arranged along the flow direction L that is parallel or substantially parallel to the central axis of the main pipe 11. is suitable.

The distance between the central axis of the second port 382 and the central axis of the third port 383 and the distance between the central axis of the third port 383 and the central axis of the fourth port 384 are the same. may be different.

Note that the connection unit 24 includes a pipe 12 having flange portions 12A and 12B. A flange portion 12A of a straight pipe (connection pipe) 12 is connected to a flange portion 11B of the main pipe 11. The inside of the flange portion 12B of the connection unit 24 is formed as an outlet of the agglomeration and granulation device 5.

As shown in FIGS. 4 and 5, the stirrer module 34 includes a disk (disc-shaped member) 341 as a base, and a plurality of stirrs 342a to 342g supported by the disk 341.

The disk 341 is fixed to the flange portion 11A of the main pipe 11 via a seal packing (not shown). The disk 341 and the flange portion 11A of the main pipe 11 are fixed with bolts and nuts, for example. The disc 341 closes the upstream opening of the main pipe 11.

In this embodiment, for example, seven stirrers 342a to 342g are rotatably supported on the disk 341. It is preferable that the stirrer 342a be arranged on the central axis of the disk 341 and on the central axis of the main pipe 11. It is preferable that the remaining six stirrers 342b to 342g be placed at the vertices of a regular hexagon with the center of the disk 341 as its centroid.

Each of the stirrers 342a to 342g has a rotating shaft 344 passing through the disk 341, and one or more stirring blades 346 provided on the rotating shaft 344.

The rotation shaft 344 passes through, for example, the center of the disk 341 and the apex of a regular hexagon whose centroid is the center of the disk 341. Therefore, in this embodiment, seven rotating shafts 344 penetrate the disk 341. Note that an O-ring (not shown) is disposed between the seven rotating shafts 344 and the through hole of the disk 341, and while the seven rotating shafts 344 can rotate with respect to the disk 341, fluid can not flow through the disk 341. Movement back and forth is prevented.
Note that the diameter of each rotating shaft 344 is, for example, 16 mm.

Among the rotating shafts 344, the rotating shafts 344 provided at the vertices of a regular hexagon with the center of the disk 341 as the centroid have a rotation direction that is similar to that of the rotating shafts 344 adjacent to the center of the disk 341 in the circumferential direction. The opposite is true. The rotational direction of the rotating shaft 344 passing through the center position of the disk 341 can be set as appropriate.

The seven rotating shafts 344 are connected to the gear train 26 shown in FIG. Further, a motor 28 is connected to the gear train 26 . The gear train 26 transmits the driving force generated by the rotation of the motor 28 to each rotating shaft 344 . At this time, the gear train 26 rotates the seven rotating shafts 344 in desired directions. It is preferable that the rotational speeds of the seven rotating shafts 344 be the same.

Note that the seven rotating shafts 344 may have a structure in which they are rotated in a predetermined direction via the gear train 26 using, for example, one motor 28, and each rotating shaft 344 or three rotating shafts rotated in the same rotational direction. Alternatively, a structure may be adopted in which each of the four rotating shafts 344 is rotated using one motor 28. Further, the seven rotating shafts 344 may be configured to be rotated individually using different motors 28. The controller 30 can control the drive (rotation) of one or more motors 28 .

As shown in FIGS. 5 and 6, in this embodiment, a plurality of stirring blades 346 are provided with respect to one rotating shaft 344 along the longitudinal direction of the rotating shaft 344, for example, at predetermined intervals or at appropriate intervals. It is also preferable that the plurality of stirring blades 346 be arranged at different intervals for each region (areas 41 to 44 to be described later) in the direction along the flow direction L with respect to one rotating shaft 344.

Note that when one (integral) stirring blade 346 is provided for one rotating shaft 344, it is preferable that the stirring blade 346 is formed continuously on the outer periphery of the rotating shaft 344, for example, in a spiral shape.

In this embodiment, for example, 24 stirring blades 346 are fixed to one rotating shaft 344. As shown in FIGS. 7 and 8, in this embodiment, each stirring blade 346 includes a fixed plate 3461 fixed to the rotating shaft 344, and six blades (blade portions) provided on the fixed plate 3461. 3462. Each blade 3462 is formed, for example, as a Rushton blade (disk turbine blade). Each blade 3462 is formed into a rectangular plate shape extending in the radial direction with respect to the central axis of the rotating shaft 344. Adjacent blades 3462 are arranged at intervals of, for example, 60° in the circumferential direction of the central axis of rotation shaft 344. Preferably, each blade 3462 has the same size and shape. The diameter of each stirring blade 346 (the distance from the distal end of the blade 3462 to the distal end of the blade 3462 on the opposite side with the center of the rotating shaft 344 in between) is, for example, 70 (mm). The diameter of each stirring blade 346 is appropriately small relative to the inner diameter of the main pipe 11, and is, for example, about 50 (mm) to 120 (mm) in order to generate a relatively strong swirling flow for the water W to be treated. It is preferable that
Note that each stirring blade 346 preferably has an outer diameter that is 1/2 or less of the inner diameter of the main pipe (pipe line) 11. Therefore, it is easy to arrange a plurality of stirring blades 346 in the direction perpendicular to the flow direction L within the main pipe 11. When each stirring blade 346 has an outer diameter of 1/2 of the inner diameter of the main pipe (pipe line) 11, the rotation angles are shifted so that the blades 3462 of the stirring blades 346 perpendicular to the flow direction L do not interfere with each other. It is preferable to do so.

As shown in FIGS. 5 and 6, the blades 3462 of the stirring blades 346 arranged in 24 pieces in the longitudinal direction of the rotating shaft 344 described above are connected to the stirring blades 346 adjacent to each other in the longitudinal direction according to the rotational direction planned by the rotating shaft 344. For example, the blades 3462 are shifted by 30° in a predetermined direction. Therefore, in each of the agitators 342a to 342g, the 24 blades 3462 of the stirring blades 346 arranged in the longitudinal direction generate a spiral flow between adjacent blades 3462.
Hereinafter, in this embodiment, an example will be described in which the blades 3462 of the stirring blades 346 are shifted in a predetermined direction by, for example, 30 degrees with respect to the blades 3462 of the stirring blades 346 adjacent in the longitudinal direction. Although not shown, the blades 3462 of the stirring blades 346 may be shifted in a predetermined direction by, for example, 10 degrees with respect to the blades 3462 of the stirring blades 346 adjacent in the longitudinal direction, depending on the rotational direction that the rotating shaft 344 is intended to rotate. suitable. In this case, each of the stirrers 342a to 342g is formed such that 24 blades 3462 of the stirring blades 346 arranged in the longitudinal direction are arranged in a spiral around the central axis of the rotating shaft 344.

In addition, the stirring blades 346 of the stirrers 342b and 342c adjacent to each other in the circumferential direction at the positions of the apexes of the regular hexagon, the stirring blades 346 of the stirrers 342c and 342d, the stirring blades 346 of the stirrers 342d and 342e, and the stirrer 342e. , 342f, and the stirring blades 346 of the stirrers 342f, 342g have different helical directions. For example, in the case of stirrers 342a, 342b, 342d, and 342f in which the rotating shaft 344 rotates clockwise when looking downstream from the disk 341 side, the spiral formed by the blades 3462 of the stirring blade 346 is similar to the spiral of a right-handed screw. It is formed. In the case of the stirrers 342c, 342e, and 342g in which the rotating shaft 344 rotates counterclockwise when looking downstream from the disk 341 side, the spiral formed by the blades 3462 of the stirring blade 346 is formed in the same manner as a left-handed spiral, for example. .

As shown in FIGS. 4, 9, and 10, the stirring plate unit 36 includes a channel assembly 361 and a stirring plate module (stirring plate) 362.

As shown in FIG. 9, the channel assembly 361 has disc bodies 363A, 363B and seven channels 364a to 364g.

The disk body 363A is formed to have an outer diameter that can be inserted into the main pipe 11. It is preferable that the outer edge of the disk body 363A and the inner circumferential surface of the main pipe 11 be sealed with, for example, an O-ring. Therefore, the water to be treated is prevented from flowing back and forth through the outside of the disc body 363A. Then, the water to be treated W is prevented from accumulating on the outside of the channels 364a to 364g between the outside of the disk body 363A and the disk body 363B.

The disk body 363B is formed in a size such that it can come into contact with the flange portion 11B of the main pipe 11. The disk body 363B and the flange portion 11B of the main pipe 11 are fixed via a seal packing. Note that the flange portion 11B of the main pipe 11, the disc body 363B of the channel assembly 361, and the flange portion 12A of the straight pipe 12 are fixed with bolts and nuts, for example. At this time, the central axes of the disc bodies 363A and 363B coincide with the central axis of the main pipe 11.

Each channel 364a-364g is formed, for example, as a cylinder. Preferably, each channel 364a-364g is the same size and length. Channels 364a to 364g are arranged at positions covering the outer sides of the downstream ends of agitators 342a to 342g. The central axis of the channel 364a is arranged on the central axis of the main pipe 11. Channels 364b-364g are arranged around the outer periphery of channel 364a. The channels 364b to 364g are centered at the vertices of a regular hexagon whose centroid is the center of the main pipe 11, and the centers thereof are arranged on the central axes of the rotating shafts 344 of the agitators 342b to 342g.

Note that channels 364a to 364g are between channels 364a and 364b to 364g, between channels 364b and 364c, between channels 364c and 364d, between channels 364d and 364e, between channels 364e and 364f, between channels 364f and 364g, and between channels 364a and 364g. It is preferable that 364g and 364b are arranged so as to be in contact with each other.
The inner diameter of each channel 364a to 364g is larger than the diameter (eg, 70 (mm)) of the stirring blade 346, and is, for example, 90 (mm).

When the disk body 363A is viewed from the upstream side to the downstream side, the outer edges of the seven channels 364a to 364g fit inside the outer edge of the disk body 363A. Furthermore, the upstream openings of each of the channels 364a to 364g are formed in the disk body 363A. The downstream opening of each channel 364a-364g is formed in disk body 363B.

As shown in FIG. 10, the stirring plate module 362 has seven assemblies 362a to 362g that are formed long along the longitudinal direction on the inner wall surfaces of seven channels 364a to 364g.

In each of the assemblies 362a to 362g, a plurality of stirring plates (rod-shaped members) 3621 parallel to the longitudinal direction of each channel 364a to 364g are arranged in the circumferential direction along the inner wall of each channel 364a to 364g. The stirring plates 3621 adjacent to each other in the circumferential direction are formed at appropriate intervals in the circumferential direction, such as in the range of 15° to 90° with respect to the central axis of each channel 364a to 364g. In this embodiment, 18 stirring plates 3621 are arranged at intervals of 20° in the circumferential direction of the central axis of the rotating shaft 344.
It is preferable that each stirring plate 3621 extends parallel to the central axis of the main pipe 11, for example. For this reason, each of the assemblies 362a to 362g is formed into a frame structure by a plurality of stirring plates 3621 as substantially tubular bodies spaced apart in the circumferential direction. The plurality of stirring plates 3621 are fixed, for example, to the inner peripheral surfaces of the plurality of toric bodies 3622.

The inner diameter of each of the assemblies 362a to 362g is larger than the diameter of the stirring blade 346. For example, the stirring plate 3621 of each assembly body 362a to 362g has a circumferential thickness of 1.5 (mm), a protrusion amount (height) of 10 (mm) from the inner peripheral surface of the channels 364a to 364g, and a length of 1200 mm. (mm).

Note that the inner diameter of each substantially tubular assembly body 362a to 362g made up of the plurality of stirring plates 3621 is formed at a position and size such that the stirring blades 346 of each of the stirring machines 342a to 342g do not come into contact with each other when rotating. The cross-sectional shape of the plurality of stirring plates 3621 is formed into an appropriate shape, such as a rectangular shape, for example.

The stirring plate unit 36 is fixed by inserting one corresponding assembly 362a to 362g of the stirring plate module 362 into each channel 364a to 364g. The upstream end of the stirring plate 3621 of the assembly bodies 362a to 362g of the stirring plate module 362 is arranged to protrude upstream from the disc body 363A. That is, the upstream end of the stirring plate 3621 of the stirring plate module 362 and the toric body 3622 are also arranged in a portion where the seven channels 364a to 364g are not present. It is preferable that the upstream end of the stirring plate 3621 of the stirring plate module 362 be close to or in contact with the disk 341 of the stirrer module 34 . The upstream end of the stirring plate 3621 of the stirring plate module 362 is preferably arranged in the pH adjustment area 41 or the mixing area 42.

Note that the downstream end of each stirring plate 3621 is arranged, for example, flush with the downstream end of the channels 364a to 364g. The downstream end of each stirring plate 3621 may be located upstream or downstream relative to the downstream ends of the channels 364a to 364g. In the latter case, it is preferable that the downstream end of each stirring plate 3621 be arranged upstream of the downstream surface of the disc body 363B (the surface that contacts the flange portion 12A of the straight pipe 12).

The agitator module 34 formed as described above is inserted into the main pipe 11 from the upstream side and fixed thereto, and the agitator plate unit 36 formed in this way is inserted and fixed from the downstream side.

Note that the position of the fourth port 384 is on the upstream side of the position of the disc body 363A of the stirring plate unit 36.

FIG. 11 shows a schematic cross section inside the main pipe 11 of the agglomeration and granulation device 5. As shown in FIG. Within the main pipe 11, between the fourth port 384 and the opening at the downstream end of the main pipe 11, seven stirrers 342a to 342g are connected to the corresponding channels 364a to 364g and the corresponding stirring plate modules 362. It is arranged inside the assemblies 362a to 362g.

The stirring plate module 362 has been described as an example in which a plurality of straight stirring plates (rod-shaped members) 3621 are arranged in the circumferential direction and formed into a cylindrical shape. It is also suitable to When each of the assemblies 362a to 362g of the stirring plate module 362 is formed in a cylindrical shape with a plurality of stirring plates 3621, the plurality of stirring plates 3621 are formed in a spiral shape in accordance with the rotation direction of the stirrers 342a to 342g. Good too. In this case as well, it is preferable that each of the assemblies 362a to 362g of the stirring plate module 362 is arranged in a cylindrical shape around the outer periphery of the stirrers 342a to 342g.

Although FIG. 11 shows an example in which the stirring plate 3621 has a substantially rectangular cross section, it is preferably formed into a flat plate shape like the blades 3462 of the stirring blades 346.

As shown in FIG. 1, in this state, the pH of the water to be treated W is adjusted between the first port 381 and the second port 382 in the introduction pipe 16 and the main pipe 11. A pH adjustment area 41 is formed. In the main pipe 11, a mixing area 42 is formed between the second port 382 and the third port 383 to mix the inorganic coagulant Mb into the pH-adjusted water W to be treated. In the main pipe 11, between the third port 383 and the fourth port 384, a cationic polymer flocculant Mc is mixed with the treated water W mixed with the inorganic flocculant Mb, A coagulation area 43 is formed that promotes coagulation of suspended solids contained in the water to be treated W. In the main piping 11, between the fourth port 384 and the opening at the downstream end of the main piping 11, an anionic polymer is placed between the fourth port 384 and the opening at the downstream end of the main piping 11. A granulation area 44 is formed in which the flocculant Md is mixed in and the aggregates contained in the water to be treated W are granulated and coarsened and densified.

Therefore, the aggregation and granulation unit 22 has a pH adjustment area 41, a mixing area 42, an aggregation area 43, and a granulation area 44 in order from the upstream side to the downstream side. That is, the aggregation and granulation unit 22 forms four areas with different phases regarding the treatment of the water to be treated W at the upstream end of the main pipe 11 and a position downstream from the vicinity thereof.

The flow path 15 on the upstream side of the pH adjustment area 41, mixing area 42, agglomeration area 43, and granulation area 44 is divided by channels (partition walls) 364a to 364g in a direction perpendicular to the central axis of the main pipe 11. The inside of the main pipe 11 is formed as one continuous flow path, rather than a continuous flow path. The flow path 15 on the downstream side of the granulation area 44 is formed as seven flow paths divided in a direction perpendicular to the central axis of the main pipe 11 by channels (partition walls) 364a to 364g.

The solid-liquid separation device 6 includes a gate valve unit 61 having a straight pipe 13 and a solid-liquid separation unit 62 having a straight pipe 14.

The flange portion 13A of the straight pipe 13 is connected to the flange portion 12B of the straight pipe 12 of the connection unit 24 via a seal packing. Note that the flange portion 12B of the straight pipe 12 and the flange portion 13A of the straight pipe 13 are fixed with bolts and nuts, for example.

As shown in FIGS. 12 to 14, the gate valve unit 61 includes a gate valve 71 provided halfway between the flange portions 13A and 13B of the straight pipe 13, and a gate valve 71 provided inside the straight pipe 13 on the downstream side of the gate valve 71. It has an inlet adjustment module 72 arranged therein.

The gate valve 71 is movable up and down in the middle between the flange portions 13A and 13B of the straight pipe 13 so as to cross the central axis of the straight pipe 13. The gate valve 71 is slidable on the upstream end surface of the inlet adjustment module 72. The gate valve 71 has a sealing structure (details not shown) so that the water to be treated W does not leak from the middle between the flange portions 13A and 13B of the straight pipe 13. The lower end of the gate valve 71 has a substantially arc shape and is formed in a shape along the inner circumferential surface of the straight pipe 13 .

The inlet adjustment module 72 sequentially connects a flow path 72a, flow paths 72b1, 72b2, flow paths 72c1, 72c2, flow paths 72d1, 72d2, flow paths 72e1, 72e2, and flow paths 72e1, 72e2 in the circumferential direction of the piping 10. 72f. The flow path 72a is formed, for example, at the lowest position. The flow path 72a is preferably formed larger than the other flow paths 72b1, 72b2, 72c1, 72c2, 72d1, 72d2, 72e1, 72e2, and 72f. The flow path 72f is formed, for example, at the uppermost position. These channels 72a, 72b1, 72b2, 72c1, 72c2, 72d1, 72d2, 72e1, 72e2, and 72f are formed symmetrically with respect to a plane that crosses the top and bottom of the pipe 10 along the central axis of the pipe 10. Each flow path 72a, 72b1, 72b2, 72c1, 72c2, 72d1, 72d2, 72e1, 72e2, 72f is continuous along the flow direction L from the upstream end to the downstream end of the inlet adjustment module 72. The upstream openings of these channels 72a, 72b1, 72b2, 72c1, 72c2, 72d1, 72d2, 72e1, 72e2, and 72f can be opened and closed by a gate valve 71. The downstream openings of these channels 72a, 72b1, 72b2, 72c1, 72c2, 72d1, 72d2, 72e1, 72e2, 72f correspond to the inflow shells 812 of the solid-liquid separation module 81, which will be described later, of the solid-liquid separation unit 62. It is connected to shells (channels) 81a, 81b1, 81b2, 81c1, 81c2, 81d1, 81d2, 81e1, 81e2, and 81f.

When the gate valve 71 is moved upward and downward, for example, the opening amount of the inflow port adjustment module 72, that is, the size of the flow passage cross-sectional area inside the straight pipe 13 is adjusted. FIG. 13 is a schematic diagram of a state where the opening degree of the gate valve 71 is 16%. FIG. 14 is a schematic diagram of the gate valve 71 in a state where the opening degree is 50%. Therefore, the gate valve unit 61 can select the flow path through which the water to be treated W containing the aggregates obtained by agglomerating the solids and granulating them flows. In this case, the inlet adjustment module 72 is selected in the following order: flow path 72a, flow paths 72b1, 72b2, flow paths 72c1, 72c2, flow paths 72d1, 72d2, flow paths 72e1, 72e2, and flow path 72f. Therefore, the inlet adjustment module 72 inserted into the gate valve unit 61 adjusts the amount of water to be treated W flowing into the solid-liquid separation module 81 depending on the opening degree of the gate valve 71.

As shown in FIG. 15, the solid-liquid separation unit 62 includes a solid-liquid separation module 81 disposed inside the straight pipe 14, a sludge recovery pipe 82, and a blow pipe 83.

The flange portion 14B of the straight pipe 14 is open in this embodiment. A discharge port 10b is formed inside the flange portion 14B of the straight pipe 14.

The solid-liquid separation module 81 includes a plurality of solid-liquid separators (cyclone assemblies) 811 , an inflow shell 812 , a treated water shell 813 , a sludge recovery shell 814 , and a flange portion 815 .

The solid-liquid separation module 81 is formed into a substantially cylindrical or cylindrical shape, and the flange portion 815 is formed at the upstream end of the solid-liquid separation module 81. The flange portion 815 of the solid-liquid separation module 81 is sandwiched between the flange portion 13B of the straight pipe 13 and the flange portion 14A of the straight pipe 14. Seal packing is provided between the flange portion 13B of the straight pipe 13 and the flange portion 815 of the solid-liquid separation module 81, and between the flange portion 815 of the solid-liquid separation module 81 and the flange portion 14A of the straight pipe 14. Concatenated. The flange portion 13B of the straight pipe 13, the flange portion 815 of the solid-liquid separation module 81, and the flange portion 14A of the straight pipe 14 are fixed with bolts and nuts, for example.

Further, the inflow shell 812 of the solid-liquid separation module 81 is in common spatial communication with an inlet pipe 86a of the plurality of solid-liquid separators 811, which will be described later. The treated water shell 813 of the solid-liquid separation module 81 is in common spatial communication with all the discharge ports 10b of the plurality of solid-liquid separators 811 at the treated water shell opening 813a. The sludge recovery shell 814 of the solid-liquid separation module 81 is in common spatial communication with all of the sludge discharge pipes 86c, which will be described later, of the plurality of solid-liquid separators 811.

In this embodiment, the solid-liquid separation module 81 includes five solid-liquid separators 811 arranged in the flow direction L. In the example shown in FIGS. 16 and 17, three solid-liquid separators 811 are arranged in the flow direction L. These are all examples, and the number of solid-liquid separators 811 arranged in parallel is not limited.

As shown in FIG. 15, each solid-liquid separator 811 includes, for example, a plurality of approximately cone-shaped cyclones (centrifugal separators) 85. The plurality of cyclones 85 are arranged in the circumferential direction with respect to the central axis of the straight pipe 14. The central axis of each cyclone 85 extends in the radial direction with respect to the central axis of the straight pipe 14.

In the cyclone 85, a hollow conical portion 85a on the central axis side of the straight pipe 14 and a cylindrical portion 85b spaced apart from the central axis of the straight pipe 14 are integrated or joined.

The cyclone 85 is connected to the cylindrical portion 85b and has an inlet through which the water to be treated W containing the aggregate g sent from the granulation area 44 flows into the cyclone 85 from the tangential direction of the inner wall of the cylindrical portion 85b. A tube 86a is provided. The cyclone 85 is connected to the center of the closed surface that closes the cylindrical portion 85b, and uses the solid-liquid separation action of the cyclone 85 to move the treated water T, which is the water to be treated W from which aggregates g have been separated, in a direction perpendicular to the tangential direction. An outlet pipe 86b for discharging from the cyclone 85 is provided (in the axial direction of the cylindrical portion 85b). The cyclone 85 is provided at the tip of the hollow conical part 85a, and discharges from the cyclone 85 the sludge S containing the aggregates g separated from the water to be treated W containing the aggregates g by the solid-liquid separation action of the cyclone 85. A sludge discharge pipe 86c is provided for this purpose. In addition, in FIG. 15, the sludge discharge pipes 86c of the plurality of cyclones 85 are arranged at positions equidistant from the central axis of the straight pipe 14.

The inner diameter size of the cylindrical portion 85b is, for example, 20 (mm) or more, and more preferably 30 (mm).

In the cyclone 85, the smaller the inner diameter of the cylindrical part 85b, that is, the maximum inner diameter of the hollow conical part 85a, the larger the swirling force becomes, and the solid-liquid separation performance improves. On the other hand, the inner diameter of the inlet pipe 86a and the sludge discharge pipe 86c of each cyclone 85 needs to be larger than the size of the aggregates contained in the water to be treated W sent from the granulation area 44. The size of the aggregates contained in the water to be treated W sent from the granulation area 44 is, for example, several tens (μm) to several (mm). Therefore, it is necessary to make the inner diameter of the inlet pipe 86a and sludge discharge pipe 86c of each cyclone 85 larger than this. Therefore, the inner diameter size of the cylindrical portion 85b needs to be at least 20 (mm), and preferably 30 (mm).

As shown in FIGS. 15 and 18, the inflow shell 812 of the solid-liquid separation module 81 is partitioned in the flow direction L by a wall. The inflow shell 812 has shells (channels) 81a, 81b1, 81b2, 81c1, 81c2, 81d1, 81d2, 81e1, 81e2, and 81f in this order in the circumferential direction of the straight pipe 14. Note that the shells 81a, 81b1, 81b2, 81c1, 81c2, 81d1, 81d2, 81e1, 81e2, 81f are the flow paths 72a, 72b1, 72b2, 72c1, 72c2, 72d1, 72d2 of the inlet adjustment module 72 of the gate valve unit 61. , 72e1, 72e2, and 72f.

In this embodiment, the flow path 72a of the inlet adjustment module 72 includes four cyclones 85 of the solid-liquid separator 811 in front of the lower side of the solid-liquid separation module 81, and five stages along the depth (flow direction L). It communicates with the inlet shell 81a to the four cyclones 85 of the solid-liquid separator. That is, the flow path 72a of the inlet adjustment module 72 communicates with 20 (4×5 stages) cyclones 85. The flow paths 72b1 and 72b2 communicate with the two cyclones 85 of the solid-liquid separator 811 on both sides of the inflow shell 81a in the circumferential direction, and the inflow shells 81b1 and 81b2 with a depth of five stages. That is, the flow paths 72b1 and 72b2 of the inlet adjustment module 72 communicate with ten cyclones 85 (2×5 stages). The flow paths 72c1 and 72c2 communicate with the two cyclones 85 of the solid-liquid separator 811 on the circumferentially outer side of the inflow shells 81b1 and 81b2, and the inflow shells 81c1 and 81c2 with a depth of five stages. That is, the flow paths 72c1 and 72c2 of the inlet adjustment module 72 communicate with ten cyclones 85 (2×5 stages). The flow paths 72d1 and 72d2 communicate with the two cyclones 85 of the solid-liquid separator 811 on the circumferentially outer side of the inflow shells 81c1 and 81c2, and the inflow shells 81d1 and 81d2 with a depth of five stages. That is, the flow paths 72d1 and 72d2 of the inlet adjustment module 72 communicate with ten (2×5 stages) cyclones 85. The flow paths 72e1 and 72e2 communicate with the two cyclones 85 of the solid-liquid separator 811 on the circumferentially outer side of the inflow shells 81d1 and 81d2, and the inflow shells 81e1 and 81e2 with a depth of five stages. That is, the flow paths 72e1 and 72e2 of the inlet adjustment module 72 communicate with ten (2×5 stages) cyclones 85. The flow path 72f communicates with the four cyclones 85 of the solid-liquid separator 811 on the upper side of the solid-liquid separation module 81 and the inflow shell 81f with a depth of five stages. That is, the flow path 72f of the inlet adjustment module 72 communicates with 20 (4×5 stages) cyclones 85.

The treated water shell 813 spatially communicates with the downstream side of the solid-liquid separation area 92 at the treated water shell opening 813a.

The sludge recovery shell 814 has a barrel shape. In the sludge recovery shell 814, a plurality of cyclones 85 are arranged so as to rotate 360° around the shell, with the sludge discharge pipes 86c facing the sludge recovery shell 814 side.

Near the downstream end of the sludge recovery shell 814, there is a region 814a (see FIGS. 16 and 17) that is not circulated by the cyclone 85. This region 814a contains aggregates discharged from the tip of the cyclone cone on the opposite side to the inlet pipe 86a, and from the sludge discharge pipe 86c extending in the direction of the central axis of the cyclone. A sludge recovery pipe 82 for recovering sludge S, which is the sludge of material g, is connected. That is, this area 814a has a sludge recovery system for recovering only the sludge-rich wastewater that has settled due to gravity in the space (downstream side) of the sludge recovery shell 814 where the cyclone 85 of the solid-liquid separation module 81 is not loaded. A tube 82 is connected.

Further, a blow pipe 83 is connected to the sludge recovery shell 814 of the solid-liquid separation module 81 via a blow pipe connection part 816b. The blow pipe 83 is a pipe for returning the supernatant liquid of the water to be treated W discharged together with the aggregates g from the sludge discharge pipe 86c to the inlet 10a side as return water (blow water) R. .

As shown in FIG. 1, in the pipe 10, a pH adjustment area 41, a mixing area 42, an aggregation area 43, and a granulation area 44 are arranged in the flow path 15 in order from the inlet 10a side to the outlet 10b side. Continuous. Then, in a solid-liquid separator 6 for solid-liquid separation after the granulation area 44, that is, on the downstream side, an inlet adjustment area 91 and a solid-liquid separation area 92 are continuous.

Next, an example of a series of flows of water treatment using the aggregation granulation system 1 of the embodiment as described above will be explained.

FIG. 19 is a flowchart showing an example of the operation of the agglomeration granulation device 5 and the solid-liquid separation device 6 of the water treatment device 2 of the embodiment.

The water to be treated W discharged from plants such as water purification plants, industrial wastewater, power plants, etc. is pressurized by the water pump 3 and flows through the inlet 10a of the piping 10 to the flow path 15 of the agglomeration and granulation device 5. is introduced (step S1). Therefore, the controller 30 of the water treatment device 2 uses the water pump 3 to introduce the water to be treated W into the flow path 15 in the main pipe 11 through the introduction port 10a of the introduction pipe 16, and rotates the motor 28. The plurality of agitators 342a to 342g rotate around their axes by inputting driving force. Therefore, the rotation shafts 344 of the stirrers 342a, 342b, 342d, and 342f rotate clockwise, for example, when viewed from the upstream side of the main pipe 11, and the stirrers 342c, 342e, and 342g rotate through the gear train 26. The shaft 344 rotates counterclockwise when viewed from the upstream side of the main pipe 11. The stirrers 342a to 342g stir the water to be treated W in the main pipe 11 of the agglomeration and granulation unit 22. The water to be treated W is agitated in the main pipe 11 by the stirrers 342a to 342g, and is sent spirally through the channel 15 in the pipe 10 from the upstream side to the downstream side.

When introducing the water W to be treated into the flow path 15 in the main pipe 11 through the introduction pipe 16, the aggregation granulator 5 injects the pH adjuster Ma into the water W to be treated through the first port 381 of the introduction pipe 16. (Step S2).

The water to be treated W is stirred according to the rotation of the stirrers 342a to 342g (step S3). The water to be treated W into which the pH has been injected is sent through the flow path 15 in the main pipe 11 from the upstream side (first port 381 side) to the pH adjustment area 41 on the downstream side (second port 382 side). It will be done. Therefore, the pH of the water to be treated W is adjusted in the pH adjustment area 41.

The aggregation and granulation device 5 injects an inorganic flocculant Mb into the pH-adjusted water W to be treated through the second port 382 of the main pipe 11 (step S4).

The water to be treated W is stirred according to the rotation of the stirrers 342a to 342g (step S5). The water to be treated W, whose pH has been adjusted and the inorganic flocculant Mb has been injected and stirred, flows through the flow path 15 in the main pipe 11 from the upstream side (second port 382 side) to the downstream side (third port 382 side). port 383 side) to the mixing area 42.

The agglomeration and granulation device 5 feeds the water to be treated W, which has been pH-adjusted, injected with the inorganic flocculant Mb, and agitated, through the third port 383 of the main pipe 11 to give it a cationic content. A molecular flocculant Mc is injected (step S6).

The water to be treated W is stirred according to the rotation of the stirrers 342a to 342g (step S7). The water to be treated W is stirred according to the rotation of the stirrers 342a to 342g. The water to be treated W, whose pH has been adjusted and the inorganic flocculant Mb and the cationic polymer flocculant Mc have been injected and stirred, passes through the flow path 15 in the main pipe 11 on the upstream side (third port 383). side) to the aggregation area 43 on the downstream side (fourth port 384 side). That is, the water to be treated W containing the aggregates g is sent to the aggregation area 43 on the downstream side of the mixing area 42 . In the aggregation area 43, the aggregates g in the water to be treated W grow large.

The aggregation and granulation device 5 supplies the water W to be treated, the pH of which has been adjusted and the inorganic flocculant Mb and the cationic polymer flocculant Mc have been injected and stirred, through the fourth port 384 of the main pipe 11. An anionic polymer flocculant Md is injected into the water to be treated W (step S8).

The water to be treated W is stirred according to the rotation of the stirrers 342a to 342g (step S9). The water to be treated W is stirred according to the rotation of the stirrers 342a to 342g. The water to be treated W, whose pH has been adjusted and the inorganic flocculant Mb, cationic polymer flocculant Mc, and anionic polymer flocculant Md have been injected and stirred, flows through the flow path 15 in the main pipe 11. It is sent from the upstream side (the fourth port 384 side) to the granulation area 44 on the downstream side (the channel assembly 361 side). In the granulation area 44, the aggregates g in the water to be treated W grow larger and are granulated.

In this way, the aggregation granulation device 5 supplies the inorganic flocculant Mb, the cationic polymer flocculant Mc, and the anion to the water W flowing through the flow path 15 in the flow direction L in the main pipe 11. The system polymer flocculant Md is injected in order while stirring.

Here, FIGS. 20 to 23 are schematic diagrams showing the process from when the inorganic flocculant Mb is injected into the water W to be treated until the aggregates (agglomerated flocs) g grow. FIG. 20 is a schematic diagram showing the relationship between the inorganic flocculant Mb and the suspended matter e at the moment when it is injected into the water W to be treated.

In the mixing area 42, the inorganic flocculant Mb neutralizes the surface potential of the suspended solids e, which are solids in the water to be treated W, and the suspended solids e, which are more likely to coagulate, are strongly stirred by the agitators 342a to 342g. Collision due to stirring force. As shown in FIGS. 20 and 21, an aggregate f is formed, and then, as shown in FIG. 22, the surface of the aggregate f becomes spherical. Furthermore, as shown in FIG. 23, the particle size distribution of the aggregates f becomes uniform. As a result, fine aggregates g with minimum size, narrow particle size distribution, high density and high strength are obtained.

On the upstream side of the disc body 363A, on the outer periphery of at least one of the plurality of stirrers 342a to 342g of the stirrer module 34, a stirring plate unit 36 is arranged parallel to the flow direction L of the flow path 15. One or more elongated assemblies 362a to 362g of the stirring plate module 362 are provided, for example, in a cylindrical shape. The swirling flow generated by the rotation of each of the stirrers 342a to 342g hits the assemblies 362a to 362g of the stirring plate module 362. Therefore, vortices are generated on the surfaces of the assemblies 362a to 362g of the stirring plate module 362. The vortex becomes a shear flow due to the flow velocity difference between the assemblies 362a to 362g of the stirring plate module 362, and the coagulation and granulation reaction rate of the water to be treated W can be improved. At this time, the assemblies 362a to 362g of the stirring plate module 362 only surround the outer periphery of the stirrers 342a to 342g. Therefore, the assemblies 362a to 362g of the stirring plate module 362 can prevent the aggregation and granulation device 5 from increasing in size while improving the aggregation and granulation reaction rate of the water W to be treated.

In this way, the water to be treated W is continuously moved in the order of pH adjustment area 41, mixing area 42, aggregation area 43, and granulation area 44 while being stirred in the flow path 15 in the main pipe 11. The aggregates contained in the water to be treated W are coarsened and densified while being granulated in the granulation area 44 by the injection and stirring of the flocculants Mb, Mc, and Md.

The stirring force by the stirrer module 34 will be explained. The stirring force is expressed as G(1/S) in the following equation (1).

G=(P/(V・μ)) ^1/2 ...(1)
Here, P is the energy (W) input into the aggregation and granulation device 5, V is the capacity (m ³ ) of the pH adjustment area 41, mixing area 42, aggregation area 43, and granulation area 44, and μ is the viscosity of water. coefficient (kg/m·s).

The stirrer module 34 has a stirring force G in the range of, for example, 5000 (1/S)≦G≦25000 (1/S), and contains a pH adjuster Ma, an inorganic flocculant Mb, a cationic polymer flocculant Mc, The water to be treated W into which the anionic polymer flocculant Md is sequentially injected is stirred. The water to be treated W into which the pH adjuster Ma, the inorganic flocculant Mb, the cationic polymer flocculant Mc, and the anionic polymer flocculant Md have been injected is heated to 5000 (1/ S)≦G≦25000 (1/S).
Further, when V is the capacity (m ³ ) of only the mixing area 42, the inorganic flocculant Mb is injected into the mixing area 42 with a stirring force G of 750 (1/S)≦G≦5500 (1/S). The treated water W is stirred. In order to achieve these stirring forces G, the aggregation and granulation device 5 rotates the stirrers 342a to 342g at a rotational speed of 500 (rpm) or more and 15,000 (rpm) or less, for example, 1000 (rpm). let As a result, the treated water W into which the inorganic flocculant Mb has been injected generally has a temperature of 750 (1/S)≦G≦5500 (1/S) while passing through the mixing area 42 for 0.1 seconds to 1 second. The mixture is stirred with a stirring force G in the range of .

If the mixture is stirred in the mixing area 42 for 0.1 seconds to 1 second with a stirring force G of 500 (1/S)≦G≦5500 (1/S), the binding force is strong and the specific gravity is, for example, 1. A dense agglomerate f of .1 to 1.5 is produced. Furthermore, by making the surface of the aggregate f spherical and narrowing the particle size distribution, a fine and high-density aggregate g is formed from the aggregate f.

In the case of this embodiment, a plurality of agitators 342a to 342g, for example seven, are housed inside the main pipe 11, and agitation is performed by the plurality of agitators 342a to 342g. In addition, in the granulation area 44, assemblies 362a to 362g of the stirring plate modules 362 arranged in a cylindrical shape around the outer periphery of each of the stirring machines 342a to 342g, and assemblies 362a to 362g of the stirring plates 342a to 342g and the stirring plate modules 362. 362g is installed inside the cylindrical channels 364a to 364g. As a result, for each of the stirrers 342a to 342g, a large stirring force can be obtained with a smaller stirring power, and the shear rate of the flow that contributes to the agglomeration rate is increased.

Note that on the downstream side of the disc body 363A, the latter granulation area 44 in the aggregation granulation device 5 has channels 364a to 364g in addition to the seven first to seventh assembly bodies 362a to 362g. .

A wall is provided in the form of cylindrical channels 364a to 364g on the outer periphery of the assemblies 362a to 362g of the stirring plate module 362, which are arranged in a cylindrical manner on the outer periphery side of the stirrers 342a to 342g. The aggregation and granulation device 5 not only uses the assemblies 362a to 362g of the stirring plate module 362, but also uses channels 364a to 364g to generate vortices on the surfaces of the assemblies 362a to 362g, and Generates a vortex on the wall. Therefore, the aggregation and granulation device 5 can further improve the aggregation and granulation reaction rate of the water to be treated W. At this time, the channels 364a to 364g only surround the outer peripheries of the stirrers 342a to 342g and the assemblies 362a to 362g of the stirring plate module 362, so that the aggregation and granulation reaction speed of the water W to be treated is increased. Enlargement of the granulation device 5 can be suppressed.

The water to be treated W containing the aggregates g thus granulated is discharged from the aggregation and granulation unit 22 to the connection unit 24 . The connection unit 24 discharges to the solid-liquid separator 6 the water to be treated W containing the suspended matter e that has been aggregated and granulated in the aggregation and granulation unit 22 . At this time, the connection unit 24 converts the flow path 15 separated into seven by the channel assembly 361 at the downstream end of the agglomeration granulation unit 22 into one flow path 15, and transfers the water to be treated W to the solid-liquid separator 6. Discharge.

Therefore, the water to be treated W is sent to the inlet adjustment area 91 in the gate valve unit 61 of the solid-liquid separator 6 on the downstream side of the agglomeration and granulation device 5 (step S10).

The gate valve unit 61 adjusts the degree of opening and closing of the gate valve 71. For this reason, the opening/closing degree of the gate valve 71 of the gate valve unit 61 is adjusted to select the inflow shell 812 into which the water to be treated W flows. For this reason, the number of cyclones 85 that separate solid-liquid aggregates g contained in the water W to be treated is adjusted every time the flow rate of the water W to be treated changes.

The degree of opening and closing of the gate valve 71 of the gate valve unit 61 is adjusted, and the water to be treated W containing the aggregates g reaches the solid-liquid separation area 92 from the inlet adjustment area 91. Therefore, the water to be treated W containing the aggregates g is sent to a plurality of solid-liquid separators 811 connected in parallel in the axial direction of the flow direction L along the central axis of the pipe 10 within the solid-liquid separation module 81 . In these solid-liquid separators 811, aggregates g are separated from the water to be treated W by the solid-liquid separation effect caused by the centrifugal force of the cone-shaped cyclone 85 (step S11).

In the case of this embodiment, only the flow path 72a below the straight pipe 13 is connected to the other flow paths 72b1, 72b2, 72c1, 72c2, 72d1, 72d2, 72e1, 72e2, 72f with respect to the central axis of the straight pipe 13. The position of the outer edge (width in the radial direction) is expanded toward the inner peripheral surface side (outer peripheral side (lower side)) of the straight pipe 13. Therefore, when the opening degree of the gate valve 71 is 16% as shown in FIG. It flows only into channel 72a. At this time, the water to be treated W flows only into the shell 81a of the inflow shell 812 of the solid-liquid separation module 81, which communicates with the flow path 72a.

Further, as shown in FIG. 14, when the opening degree of the gate valve 71 is 50%, the water to be treated W flows into the flow paths 72a, 72b1, 72b2, 72c1, 72c2, and the flow paths 72d1, 72d2, 72e1, 72e2, 72f shielded. At this time, the water to be treated W flows only into the shells 81a, 81b1, 81b2, 81c1, 81c2 of the inflow shell 812 of the solid-liquid separation module 81, which communicate with the channels 72a, 72b1, 72b2, 72c1, 72c2.

Inlet shell 812, treated water shell 813, and sludge recovery shell 814 are separated by multiple cyclones 85. This makes the pressures inside each of the inflow shell 812, the treated water shell 813, and the sludge recovery shell 814 uniform.

The treated water W from which the aggregates g have been separated is discharged from the cyclone 85 as treated water T through the discharge port 10b. The treated water T joins in the treated water shell 813, moves from the solid-liquid separation module 81 in the flow direction L into the solid-liquid separation device 6 (straight pipe 14), and then flows through the discharge port 10b of the solid-liquid separation device 6. (Step S12).

On the other hand, the sludge S containing aggregates g separated from the water to be treated W is collected in the sludge recovery shell 814 from the cyclone 85 via the sludge discharge pipe 86c, and the sludge S containing a large amount of aggregates g is collected in the sludge recovery shell 814. Solid-liquid separation is performed into (precipitate) and supernatant water R (step S13). The sludge S (sediment) separated into solid and liquid by the sludge recovery shell 814 is discharged from the sludge recovery pipe 82 to the outside of the solid-liquid separator 6 through the sludge recovery pipe connection part 816a (step S14). The supernatant water is discharged as blow water (return water R) from the blow pipe 83 to the outside of the solid-liquid separator 6 through the blow pipe connecting portion 816b. The blow water (return water) R is then returned to the treated water W on the inlet side of the water pump 3 (step S15).

16 and 17 are diagrams showing an example of analysis results of pressure distribution in the inflow shell 812, the treated water shell 813, and the sludge recovery shell 814. 16 and 17, the pressure inside each shell becomes uniform in the inflow shell 812, the treated water shell 813, and the sludge recovery shell 814, and as a result, the inlet pipe 86a, outlet pipe 86b, and sludge of each cyclone 85 The pressure difference in the discharge pipe 86c is equalized, and the treated water W is evenly distributed in each cyclone 85 arranged in parallel (that is, the amount of treated water W flowing into each cyclone 85 is equalized, and the separation performance is equalized). Realize.

In this way, the aggregation and granulation system 1 adjusts the pH of the water to be treated W while stirring the water to be treated in the aggregation and granulation device 5, and then aggregates the suspended matter contained in the water to be treated. The aggregate g can be granulated, and the treated water W containing the granulated aggregate g can be discharged to the solid-liquid separator 6. In addition, the aggregation and granulation system 1 can separate and discharge treated water, sludge, and return water from the pipe 10 in the solid-liquid separator 6 on the downstream side of the aggregation and granulation device 5 . Therefore, according to the water treatment device 2, after the turbidity e contained in the water to be treated W is grown into large aggregates g by the aggregation granulation device 5, the large aggregates g are grown by the solid-liquid separation device 6. By applying centrifugation to the treated water W containing g, the aggregate g is separated from the treated water W, and the treated water W from which the aggregate g has been separated is recovered as treated water T. be able to.

Since the large aggregates g contained in the water to be treated W have a strong binding force and a high density, they are difficult to be destroyed by centrifugal force even if centrifugal separation is performed. Therefore, in the water treatment device 2 of the embodiment, a flocculation tank and a settling tank are not required. As a result, the area required for installing the flocculation tank and the settling tank can be reduced, so that the overall size of the water treatment device 2 can be reduced.

In the case of this embodiment, assuming that the amount of water to be treated W to be treated is 1000 (m ³ /day), the main pipe 11 made of stainless steel is 300A in size and has a length of 1200 (mm). Agitators 342a to 342g having two (plural) rotating shafts 344 were prepared. The outer diameter of each of the stirrers 342a to 342g is 70 (mm). Generally, the flow rate of the fluid flowing inside the piping 10 is designed to be a maximum of 2 (m/s), and when the water to be treated W flows at this maximum flow rate, in order to stir it for 0.1 seconds to 1 second, In the flow direction L, it is necessary to ensure that the total length of the pH adjustment area 41, mixing area 42, aggregation area 43, and granulation area 44 is 0.2 (m) to 2 (m). In this embodiment, the main pipe 11 having a length of 1200 (mm) was used. In this case, while moving each of the stirrers 342a to 342g, flocculants Mb, Mc, and Md are sequentially injected from ports 382, 383, and 384 as flocculant injection parts, and the water to be treated W is flocculated and granulated, and the solid-liquid The total driving force for stirring to reach a separable state was, for example, 6 (kW).
Note that the energy P (W) input to the stirrers 342a to 342g can be confirmed by the wattmeter of the motor 28 that rotates the rotating shaft 344 of the stirrers 342a to 342g.
As an example, assuming that the amount of treated water W to be treated is 1000 (m ³ /day), a 250A size pipe (outside diameter 200 (mm)) made of stainless steel material, which is different from this embodiment, and a , one (not more than one) rotating shaft stirrer was prepared on the central axis of the piping. The stirring blade of the stirrer in this case has an outer diameter several times larger than the stirring blade 346 of the stirrers 342a to 342g according to the embodiment. The diameter of the stirring blade of this stirrer is 200 (mm). The length of the piping in this case is, for example, 1200 (mm). In this case, the driving force for injecting the flocculant from the flocculant injection part while moving the stirrer, flocculating and granulating the water W to be treated, and stirring it to a state where solid-liquid separation is possible is as follows: For example, the total power was 46 (kW).
Therefore, when using the agglomeration granulation device 5 according to the present embodiment, a pipe of a different size (outer diameter 200 (mm)) and one (not plural) rotating shaft on the central axis of the pipe are used. Compared to the case of using a stirrer, it is possible to greatly reduce the stirring power required to aggregate and granulate the suspended matter e in the water to be treated W into aggregates g of a required size. Therefore, by using the agglomeration and granulation device 5 having a plurality of agitators 342a to 342g in the main pipe 11 according to the present embodiment, the power consumption when treating the water W to be treated, that is, the running cost can be reduced. can be lowered.
The agglomeration granulation device 5 having a plurality of agitators 342a to 342g according to the present embodiment uses a small agitation power P and agitation force G with appropriate power consumption to control the cyclone type solid-liquid separation device 6. Aggregates g that can be separated into solid and liquid without being broken by centrifugal force can be created. The agglomeration granulation device 5 according to the present embodiment has a bonding force comparable to that when using a 250A size stainless steel pipe (outer diameter 200 (mm)) and a stirrer with one (not plural) rotating shaft. It is possible to produce a high-density aggregate g with a strong specific gravity of, for example, 1.1 to 1.5.

Therefore, according to the present embodiment, even if the amount of treated water W to be treated is appropriately large, the treated water W is stirred with a smaller stirring power, a part of the treated water W is aggregated, It is possible to provide an agglomeration granulation device 5 capable of granulation, and a water treatment device 2 having the aggregation granulation device 5.

According to the aggregation and granulation device 5 of such an embodiment, the intersecting channel cross section, such as orthogonal to the flow direction L in the pipe 10, is divided into a plurality of sections, and a swirling flow is generated in each divided channel section. By providing the agitators 342a to 342g each having a plurality of small-diameter agitating blades 346, the agitation required for agglomeration and granulation is more effective than using a single agitator having a large-diameter agitation blade close to the flow path size in the pipe 10. The stirring power can be reduced while maintaining a sufficient stirring power.

In the agglomeration and granulation device 5 according to the present embodiment, an example using seven agitators 342a to 342g has been described, but it is preferable to use three or more agitators. In this case, in the aggregation and granulation device 5, the rotating shaft 344 is arranged at the vertex of an equilateral triangle with respect to the disk 341, for example.
In the agglomeration and granulation device 5, two agitators installed in parallel may be used. In this case, in the aggregation and granulation device 5, the rotating shaft 344 is arranged at a predetermined distance from the disk 341, for example.
In the aggregation and granulation device 5, a plurality of agitators, such as eight agitators or nine agitators, may be used.
The agitator module 34 of the agglomeration and granulation device 5 according to this embodiment is preferably arranged at a point-symmetrical or rotationally symmetrical position with respect to the center of the main pipe 11.

Further, each of the plurality of agitators 342a to 342g has one or more agitation blades 346 that generate a swirling flow in the water to be treated W in the flow path 15 of the main pipe 11. For example, when one stirring blade 346 is attached to one rotating shaft 344, the blades 3462 of the stirring blade 346 are formed, for example, in a spiral shape. Due to the pressure of the water to be treated W flowing in the flow path 15 at a maximum value of, for example, 2 (m/s), the spiral blades 3462 cause the plurality of agitators 342a to 342g to rotate around the rotation shaft 344. Whether or not the water to be treated W is used, a swirling flow can be generated.
In the aggregation and granulation device 5, by attaching a plurality of relatively small-diameter stirring blades 346 to each of the stirrers 342a to 342g in parallel to the flow direction L of the flow path of the pipe 10, the to-be-treated material flowing in the main pipe 11 is The water W to be treated can be stirred while maintaining the necessary stirring force with low power. In the aggregation and granulation device 5, the inside of the main pipe 11 is injected into the flow path 15 in this order by injecting the pH adjuster Ma, the inorganic flocculant Mb, the cationic polymer flocculant Mc, and the anionic polymer flocculant Md. can be stirred while maintaining the stirring power necessary for agglomerating and granulating the suspended matter e into aggregates g. In the aggregation and granulation device 5, a cyclone-type solid-liquid separator 6 converts the turbidity e, which is a solid substance contained in the water to be treated W, into aggregates g, which are difficult to break up by centrifugal force and can be separated into solid-liquid. , the water to be treated W can be aggregated and granulated.

For example, when a plurality of stirring blades 346 are attached to one rotating shaft 344 at a distance in the flow direction L, the blades 3462 of the stirring blades 346 as a whole are formed, for example, in a spiral shape. That is, the blades 3462 of the stirring blades 346 adjacent to each other along the axial direction of the rotating shaft 344 are shifted by appropriate angles in the circumferential direction of the rotating shaft 344. Therefore, depending on the pressure of the water to be treated flowing through the channel 15, the spiral blades 3462 are rotated regardless of whether or not the plurality of agitators 342a to 342g are rotating around the rotating shaft 344. , it is possible to generate a swirling flow in the water W to be treated.
In these cases, by rotating the plurality of stirrers 342a to 342g around the rotating shaft 344, a larger stirring force can be obtained in the main pipe 11.

It is preferable that the rotation shafts 344 of the plurality of stirrers 342a to 342g are arranged in parallel. Therefore, interference between adjacent stirrers 342a to 342g is suppressed.

Among the plurality of agitators 342a to 342g, stirring between two adjacent agitators 342b and 342c, between agitators 342c and 342d, between agitators 342d and 342e, between agitators 342e and 342f, and between agitators 342f and 342g. Preferably, one of the rotating shafts 344 between the machines 342g and 342b is clockwise when viewed from a predetermined direction, and the other is counterclockwise when viewed from the predetermined direction. In that case, the outer flows of adjacent swirling flows are oriented in the same direction at the contacting portions of the respective swirling flows. Therefore, the plurality of agitators 342a to 342g of the agitator module 34 can maintain a vortex by rotating each of the agitators 342a to 342g without interfering with and disrupting the swirling flow of the water to be treated W.

In FIGS. 5 and 6, the plurality of stirring blades 346 in each of the plurality of stirrers 342a to 342g are equidistantly spaced along the flow direction L of the flow path 15. The plurality of stirring blades 346 attached to the rotating shafts 344 of the plurality of stirrers 342a to 342g may be appropriately shifted at intervals along the flow direction L of the flow path 15, and may be arranged at different distances. For example, in the main pipe 11, the density of the stirring blades 346 may be increased in areas where a relatively high stirring force is desired, and the density of the stirring blades 346 may be decreased in areas where a relatively low stirring force is required. . The density of the stirring blades 346 may be changed for each of the above-mentioned pH adjustment area 41, mixing area 42, aggregation area 43, and granulation area 44. Further, it may be changed within each area 41, 42, 43, 44. That is, the spacing of the plurality of stirring blades 346 in each of the plurality of stirrers 342a to 342g along the flow direction L of the main pipe 11 differs depending on the areas 42, 43, and 44 along the flow direction L.
The plurality of stirring blades 346 in each of the plurality of stirrers 342a to 342g are arranged in the injection region of the flocculants Mb, Mc, Md and the vicinity thereof, and the flocculants Mb, Mc, Md in the flow direction L of the main pipe 11. It is also preferable that the number (density) per unit length is different between the injection region and its vicinity and downstream. For example, when comparing the flocculant Md injection area and its vicinity with the flocculant Md injection area and its vicinity downstream, it is found that the stirring blade 346 is more downstream than the flocculant Md injection area and its vicinity. It is preferable that the density is high. In this case, the density of the stirring blades 346 can be lowered in the flocculant Md injection region and its vicinity, so that the flocculant Md can be easily distributed from the port 384 to the distal position in the circumferential direction of the main pipe 11. By increasing the density of the stirring blades 346 in the injection region of the flocculant Md and on the downstream side in the vicinity thereof, the flocculant Md can be more reliably stirred with the water to be treated W in the granulation area 44.

In FIGS. 7 and 8, an example will be described in which each blade (blade portion) 3462 of the plurality of stirring blades 346 is arranged parallel to the flow direction L of the water to be treated W in the flow path 15. did. As shown in FIGS. 25 and 26, the blades (blade portions) 3462 of the stirring blades 346 may be offset from each other with respect to the flow direction L of the water to be treated W in the flow path 15. It is preferable that the plurality of blades 3462 of at least one stirring blade 346 of the plurality of stirring blades 346 are inclined at an appropriate angle θ with respect to the flow direction. For example, it is preferable that the angle θ be inclined at an angle of −20° to +20°. The blades 3462 of the stirring blade 346 are fixed to the stirring blade 346 at an angle θ of -20° to +20° with respect to the flow direction L, so that the rotation direction of the stirring blades 342a to 342g is on the upstream side of the main pipe 11. If it is clockwise when viewed from the center, it should be attached at a negative angle, and if it is to be rotated counterclockwise, it should be attached at a plus angle (see Figures 25 and 26). Therefore, each of the stirrers 342a to 342g including the stirring blades 346 rotates inside the main pipe 11, so that the water to be treated W received from the inlet 10a of the pipe 10 flows through the flow path inside the main pipe 11. The liquid is sent spirally from the upstream side to the downstream side along the line 15. The power of the water pump 3 can be reduced by making the angle of the blades 3462 of the stirring blades 346 attached to the stirrers 342a to 342g into a shape and angle that allows the water to be treated W to be fed and pressurized. . Alternatively, the water pump 3 can be omitted.

The rotation shafts 344 of the plurality of stirrers 342a to 342g are supported by one disc 341 so that the rotation shafts 344 of the stirrers 342a to 342g each rotate around the respective axes. The disk 341 is fixed to the flange portion 11A at one end of the main pipe 11, which becomes the flow path 15. Therefore, the stirrer module 34 can be easily pulled out from the main pipe 11, and maintenance of the stirrer module 34 and position adjustment of the stirring blades 346 are easy.

On the outer periphery of at least one of the plurality of stirrers 342a to 342g of the stirrer module 34, a long one of the stirring plate module 362 of the stirring plate unit 36 is arranged parallel to the flow direction L of the flow path 15. Alternatively, a plurality of assembly bodies 362a to 362g are provided in a cylindrical shape, for example. The rotation of each of the stirrers 342a to 342g causes the generated swirling flow to hit the assemblies 362a to 362g of the stirring plate module 362, further generating vortices on the surfaces of the assemblies 362a to 362g of the stirring plate module 362. The vortex becomes a shear flow due to the flow velocity difference between the assemblies 362a to 362g of the stirring plate module 362, and the coagulation and granulation reaction rate of the water to be treated W can be improved. As a result, the turbidity e, which is a solid substance contained in the water to be treated W, is not broken by the centrifugal force of the cyclone-type solid-liquid separator 6, and is agglomerated and granulated into aggregates g that can be separated into solid-liquid. It is possible to obtain the strong stirring power necessary for At this time, since the assemblies 362a to 362g of the stirring plate module 362 only surround the outer periphery of the stirrers 342a to 342g, the aggregation and granulation device 5 It is possible to suppress the increase in size.

Channels 364a to 364g as cylindrical walls are provided on the outer periphery of the plurality of assemblies 362a to 362g of the stirring plate module 362. A wall is provided on the outer periphery of the assembly body 362a to 362g of the stirring plate module 362 arranged in a cylindrical shape on the outer periphery side of the agitator 342a to 342g, and a vortex is generated on the wall surface. Thereby, the aggregation and granulation reaction rate of the water to be treated W can be further improved. As a result, the turbidity e, which is a solid substance contained in the water to be treated W, is not broken by the centrifugal force of the cyclone-type solid-liquid separator 6, and is agglomerated and granulated into aggregates g that can be separated into solid-liquid. It is possible to obtain the stronger stirring power required for At this time, since the channels 364a to 364g only surround the outer peripheries of the stirrers 342a to 342g and the assemblies 362a to 362g of the stirring plate module 362, the aggregation and granulation reaction speed of the water W to be treated can be improved. Enlargement of the agglomeration and granulation device 5 can be suppressed.

The channels 364a to 364g are fixed to one disc body 363B having a downstream opening for the flow path 15 of the main pipe 11, and the disc body 363B is connected to a flange at the other end of the main pipe 11 which becomes the flow path 15. It is fixed to part 11B. Further, the plurality of assemblies 362a to 362g of the stirring plate module 362 are fixed to one disk body 363B, and the disk body 363B is fixed to the flange portion 11B at the other end of the main pipe 11 that becomes the flow path 15. . By doing so, the plurality of assemblies 362a to 362g of the stirring plate module 362 can be easily inserted into the interior of the aggregation and granulation device 5, that is, into the main piping 11 without interfering with the stirrers 342a to 342g. .

The agglomeration granulation device 5 according to the present embodiment includes a second port 382 for injecting the inorganic flocculant Mb into the flow path 15 as a flocculant injection part, and a second port 382 downstream of the flow path 15 from the second port 382. A third port 383 and a fourth port 384 are provided on the side and for injecting polymer flocculants Mc and Md. In this case, the turbidity e, which is a solid substance contained in the water to be treated, is stirred to the extent necessary for agglomerating and granulating the turbidity e, which is a solid substance contained in the water to be treated, inside the main pipe 11, and It is possible to agglomerate and granulate the solid-liquid separable aggregates g without destroying the particles e by the centrifugal force of the cyclone-type solid-liquid separator 6.

In this embodiment, the aggregation and granulation device 5 includes three or more ports 382, 383, and 384 as a flocculant injection part along the flow path 15 from the upstream side to the downstream side. The interval along the flow direction L of the flow path 15 between three or more ports 382, 383, 384 is determined by the speed at which the water to be treated W can reach the ports 382, 383, 384, and the stirring time by the plurality of stirrers 342a to 342g. It is preferable that it be shifted according to the following. That is, the intervals between the three or more ports 382, 383, and 384 along the flow direction L of the main pipe 11 are arranged in a size corresponding to the stirring time by the plurality of stirrs 342a to 342g. The intervals between the three or more ports 382, 383, and 384 can be set as appropriate.
In other words, the intervals between the ports 382, 383, and 384 connected to the flow path 15 in the main pipe 11 are shifted in accordance with the flow velocity along the flow direction L of the water to be treated W, so that each aggregation By injecting the flocculant, the stirring time after the flocculant injection can be adjusted. After injecting the inorganic flocculant Mb, in order to provide sufficient stirring force and stirring time necessary to advance the aggregates g from FIG. 20 to FIG. The distance to the port 382 into which the coagulant Mc is injected is long. By doing so, it is possible to stir with a stirring force G in the range of 750≦G≦5500 (1/S) for a passage time of 0.1 seconds to 1 second through the mixing area 42. In addition, the length of the flow path 15 after injecting the cationic polymer flocculant Mc and the anionic polymer flocculant Md from ports 383 and 384, respectively, and the latter half of the stirrers 342a to 342g are lengthened, and the stirring blades are By increasing the number of stirrers 346, stirring can be carried out for a long time of 0.2 seconds to 4 seconds or more using the stirrers 342a to 342g while maintaining the stirring power. Therefore, each of the flocculants Mb, Mc, and Md evenly spreads through the water to be treated W in order. As a result, the turbidity e, which is a solid substance contained in the water to be treated W, can be granulated into aggregates g that can be separated into solid and liquid without being broken by the cyclone type solid-liquid separator 6. Although not shown in the figures, in the aggregation and granulation device 5 according to the present embodiment, by changing the interval between the stirring blades 346, areas where the stirring blades 346 have a short interval can be stirred for a long time with a weaker stirring force, for example. In the aggregation and granulation device 5 according to the present embodiment, depending on the quality of the water to be treated W, if it is necessary to agitate for a long time with a small stirring force for aggregation or granulation, unnecessary stirring power is added. Necessary stirring can be achieved without the need for

In this embodiment, the plurality of stirring blades 346 provided in the stirrers 342a to 342g are arranged in the flow direction L in the main pipe 11, as shown in FIG. The blades (blade portions) 3462 of the front and rear stirring blades 346 are fixed to the rotating shafts 344 of the stirrers 342a to 342g with their positions shifted. Therefore, even if the distance between the stirring blades 346 along the flow direction L in the main pipe 11 is short, a strong stirring force can be obtained.

In this embodiment, as described above, the second port 382, the third port 383, and the fourth port 384 are connected to each other from the upstream end of the main pipe 11, for example, within the entire length of the main pipe 11. However, it is provided at a position of about 1/6 to 1/3. For this reason, the distance from the fourth port 384 to the most downstream opening of the main pipe 11 is lengthened, that is, the flow path 15 after injecting the cationic polymer flocculant Mc and the anionic polymer flocculant Md. can be made longer. By lengthening the channel 15, the area stirred by the stirrers 342a to 342g after the cationic polymer flocculant Mc and the anionic polymer flocculant Md are injected can be lengthened. Therefore, it is possible to increase the number of stirring blades 346 through which the water W to be treated after injecting the cationic polymer flocculant Mc and the anionic polymer flocculant Md passes. At this time, the water to be treated W can be stirred by the stirrers 342a to 342g for a relatively long time, for example, 0.2 seconds to 4 seconds or more. Therefore, by using the aggregation and granulation device 5 according to the present embodiment, it is possible to stir the inside of the flow path 15 while maintaining the stirring force G to the water W to be treated. As a result, the suspended matter e, which is a solid substance contained in the water to be treated W, can be granulated into aggregates g that can be separated into solid and liquid without being broken by the centrifugal force of the solid-liquid separator 6.

In this embodiment, the agitator module 34, which has a plurality of small-diameter agitators 342a to 342g fixed to one disk 341 so that each agitator 342a to 342g rotates, is connected to the main pipe of the aggregation and granulation unit 22. 11 from the upstream side, and is fixed with bolts and nuts across the flange portion 11A of the agglomeration and granulation unit 22 and a seal packing (not shown). Thereby, the agitator module 34 can be easily pulled out from the piping 10, and the aggregation and granulation unit 22 can be assembled while maintaining the agitator module 34 and adjusting the position of each of the agitators 342a to 342g. At this time, the stirring blades 346 of each of the stirrers 342a to 342g are adjusted so that the blades 3462 of the stirring blades 346 of each of the stirrers 342a to 342g have a spiral shape along the flow direction L, and the stirring blades 346 of the main piping 11 are adjusted. The arrangement of the stirrers 342a to 342g arranged in a direction perpendicular to the central axis can be adjusted.

The solid-liquid separator 6 uses centrifugal force to separate the aggregates from the water to be treated W containing the aggregates g granulated in the granulation area 44 having the first to seventh assembly bodies 362a to 362g of the channel assembly 361. A plurality of solid-liquid separators 811 are connected in parallel to perform solid-liquid separation by separating water W from which aggregates g have been separated. Further, the water to be treated W containing the aggregates granulated in the granulation area 44 having the first to seventh assembly bodies 362a to 362g of the channel assembly 361 is combined at the connection unit 24, and then connected to the gate valve unit. The flow path can be selected again in step 61 to adjust the number of solid-liquid separators 811 that perform solid-liquid separation.

Note that the large aggregates g contained in the water to be treated W treated using the agglomeration and granulation device 5 according to this embodiment have a strong binding force and a high density, so even if centrifugal separation is applied, the large aggregates g contained in the water to be treated W are Destruction by force is prevented. Therefore, when using the agglomeration and granulation device 5 according to this embodiment, the solid-liquid separation device 6 connected to the aggregation and granulation device 5 can be used, and an aggregation tank and a settling tank are not required. As a result, the area required for installing the flocculation tank and the settling tank can be reduced, and the water treatment device 2 can be made smaller.

The assemblies 362a to 362g of the stirring plate module 362 are fixed to one disk body 363B so that the agitator module 34 fits inside the assembly bodies 362a to 362g of the corresponding stirring plate module 362, and the aggregation and granulation unit is assembled. 22 from the downstream side of the main pipe 11. The disk body 363B integrated with the assemblies 362a to 362g of the stirring plate module 362 is placed between the flange portion 11B of the agglomeration and granulation unit 22 and the flange portion 12A of the connection unit 24 with sealing packing (see FIG. (not shown) and then fix it with bolts and nuts. By doing so, the stirrer module 34 can be easily inserted into the main pipe 11 of the agglomeration and granulation unit 22, in other words, into the pipe 10, without interfering with the stirrers 342a to 342g.

On the other hand, in this embodiment, the channels 364a to 364g into which the assemblies 362a to 362g of the stirring plate module 362 are inserted are fixed to the stirring plate unit 36 sandwiched between the disc bodies 363A and 363B, and the channels 364a to 364g are fixed to each other. The assemblies 362a to 362g of the stirring plate module 362 are loaded and inserted into the aggregation and granulation unit 22 from the downstream side. Seal packing (not shown) is inserted between the flange portion 11B of the agglomeration granulation unit 22 and the flange portion 12A of the connection unit 24 to sandwich the disk body 363B of the stirring plate unit 36, and then bolts and nuts are fixed. There is. By doing so, the stirrer module 34 can be easily inserted into the main pipe 11 of the agglomeration and granulation unit 22, in other words, into the pipe 10, without interfering with the stirrers 342a to 342g.

According to the agglomeration and granulation device 5 of at least one embodiment described above, even when the amount of treated water W to be treated is appropriately large, the to-be-treated water W can be stirred with a smaller stirring power, and the treated water W can be stirred with a smaller stirring power. A part of the water W can be aggregated and granulated.

Although several embodiments of the invention have been described, these embodiments are presented by way of example and are not intended to limit the scope of the invention. These novel embodiments can be implemented in various other forms, and various omissions, substitutions, and changes can be made without departing from the gist of the invention. These embodiments and their modifications are included within the scope and gist of the invention, as well as within the scope of the invention described in the claims and its equivalents.

DESCRIPTION OF SYMBOLS 1...Aggregation granulation system, 2...Water treatment device, 3...Water pump, 5...Agglomeration granulation device, 6...Solid-liquid separation device, 10...Piping, 10a...Inlet, 10b...Outlet, 11-14... Straight pipe, 11A, 11B, 12A, 12B, 13A, 13B, 14A, 14B...flange section, 15...flow path, 16...introduction piping, 22...agglomeration granulation unit, 24...connection unit, 26...gear train, 28 ...Motor, 30...Controller, 34...Stirrer module, 341...Disc, 342a-342g...Stirrer, 344...Rotating shaft, 346...Stirring blade, 3461...Fixed plate, 3462...Blade, 36...Stirring plate unit, 361 ...Channel assembly, 362...Stirring plate module, 362a-362g...Assembly body, 3621...Stirring plate, 3622...Torus, 363A, 363B...Disc body, 364a-364g...Channel, 381-384...Port, 41...pH Adjustment area, 42...Mixing area, 43...Agglomeration area, 44...Pelletization area.

Claims (20)

a pipe line having an inlet through which the water to be treated is introduced and an outlet through which the water to be treated is discharged;
a coagulant injection unit that injects a coagulant into the water to be treated flowing in the pipe;
a plurality of agitators arranged in parallel in a direction intersecting the flow direction of the water to be treated in the pipe line and generating a swirling flow in the water to be treated in which the flocculant has been injected; Grain device. Each of the plurality of stirrers has one or more stirring blades that generate the swirling flow in the water to be treated in the pipe line.
The agglomeration granulation device according to claim 1. The aggregation and granulation device according to claim 2, wherein each of the one or more stirring blades has an outer diameter that is 1/2 or less of the inner diameter of the pipe line. Each of the plurality of stirrers has a plurality of stirring blades spaced apart from each other in the flow direction.
The aggregation granulation device according to claim 2 or claim 3. The plurality of stirring blades in each of the plurality of stirrers have an interval along the flow direction of the pipe line that differs depending on an area along the flow direction.
The agglomeration granulation device according to claim 4. The plurality of stirring blades in each of the plurality of stirrers are arranged in the flocculant injection region and its vicinity, and the downstream side of the flocculant injection region and its vicinity with respect to the flow direction of the pipe line. and the number is different,
The agglomeration granulation device according to claim 4. The agglomeration and granulation apparatus according to claim 4, wherein the blades of the front and rear stirring blades of the plurality of stirring blades are shifted from each other with respect to the flow direction. At least one of the plurality of stirring blades has a plurality of blades,
The plurality of blades are inclined at an angle of −20° to +20° with respect to the flow direction.
The agglomeration granulation device according to claim 4. Each of the plurality of stirrers is provided with the one or more stirring blades and has a rotation shaft that rotates around the shaft by input of driving force,
The rotation axes of the plurality of stirrers are arranged in parallel,
The aggregation granulation device according to claim 2 or claim 3. One of the rotating shafts of two adjacent agitators among the plurality of agitators is clockwise when viewed from the predetermined direction, and the other is counterclockwise when viewed from the predetermined direction.
The agglomeration granulation device according to claim 9. The plurality of agitators each have a rotating shaft supported by a single disc-shaped member so that the rotating shafts of the agitators each rotate around the respective axes,
The disc-shaped member is fixed to a flange at one end of the pipe serving as the pipe line,
The agglomeration granulation device according to claim 9. One or more elongated stirring plates are provided on the outer periphery of at least one of the plurality of stirrers in parallel to the flow direction.
The agglomeration granulation device according to claim 1. The plurality of stirring plates are arranged in a cylindrical shape around the outer periphery of the stirrer,
The agglomeration granulation device according to claim 12. A cylindrical wall is provided on the outer periphery of the plurality of stirring plates,
The agglomeration granulation device according to claim 12. The cylindrical wall is fixed to a disc body having an opening for the conduit,
The disk body is fixed to a flange at the other end of the pipe constituting the pipe line.
The agglomeration granulation device according to claim 14. The stirring plate is fixed to a disc body,
The disk body is fixed to a flange at the other end of the pipe constituting the pipe line.
The agglomeration granulation device according to claim 12. The flocculant injector injects a different type of flocculant selected from the flocculants along the flow direction of the pipe at a position where the plurality of agitators generate the swirling flow in the water to be treated. can be injected in stages,
The agglomeration granulation device according to claim 1. The flocculant injection part includes a first port for injecting an inorganic flocculant into the pipe line, and a second port for injecting a polymer flocculant, which is provided on the downstream side of the pipe line from the first port. Equipped with ports of
The agglomeration granulation device according to claim 17. The flocculant injection part includes three or more ports along the upstream side to the downstream side of the pipe line,
The intervals between the three or more ports along the flow direction of the pipe line are arranged in a dimension according to the stirring time by the plurality of stirrers,
The agglomeration granulation device according to claim 1. The agglomeration granulation device according to claim 1;
a solid-liquid separation device connected to the downstream side of the agglomeration and granulation device, which performs solid-liquid separation of aggregates from the water to be treated into which the flocculant has been injected, takes out sludge, and discharges treated water. Water treatment equipment.