JPH0252010A - Cohesion device and cohesion process - Google Patents

Abstract

PURPOSE:To enhance solid-liquid separation performance and cohesively remove fine particles without adding a cohesion agent by providing a dispersion chamber to disperse water to be treated and a mixing tube opened in the dispersion chamber and installing an injection tube for injection liquid in the mixing tube. CONSTITUTION:Water to be treated 2 such as biologically treated water or the like of soil waste water is fed into a dispersion chamber 3 of a liquid feeding chamber 1, and injection liquid 10 such as river water or the like is injected from an injection tube 6. The flow of injection liquid and the flow of water to be collected flow in contact with in a mixing tube 5, and violent impacts are repeated among the fine particles in the water to be treated at its interface to form mammoth flocks while passing through the mixing tube 5. The coherent flocks are discharged from a discharge outlet 15 of the mixing tube into a solid-liquid separation chamber 4 to carry out solid-liquid separation. Thus, high concentration treatment process utilizing active sludge can be carried out without a cohesion agent even when bulking phenomenon is generated. Also, botanical planktons or the like in lakes, swamps and waterways can be cohesively removed.

Description

[Detailed Description of the Invention] [Industrial Application Field] This invention is directed to the treatment of microorganisms (activated sludge) from water to be treated containing fine particles such as brewing waste liquid, culture growth liquid, and dredged sludge.
, algae, plankton, etc.] and a flocculation method.

[Prior Art] A sedimentation tank is used as a device for separating fine particles in water to be treated from water to be treated. The sedimentation tank allows fine particles to settle under the action of gravity while passing through the liquid supply cylinder where biologically treated water is supplied and reaching the overflow weir of the solid-liquid separation chamber. The bond is dependent on the local charge distribution.

In biological treatment of contaminated wastewater, activated sludge often flows out of the system together with treated water due to bulking.

As a result, the activated sludge concentration in the aeration tank decreases, often resulting in poor treated water quality.

The high-concentration activated sludge treatment method, which improves treated water quality, reduces excess sludge, and improves treatment capacity, tends to cause bulking in the sludge, which reduces the solid-liquid separation performance of activated sludge, so as a countermeasure, The biologically treated water m is reduced, the sludge 11 extracted from the settling tank is increased, and the activated sludge concentration is reduced. Therefore, it has been impossible to continue operating the high concentration treatment method.

For culture solutions and fermentation solutions that do not require the addition of flocculants, high-grade separators that require enormous equipment costs are used to separate microorganisms. In addition, vast areas of dredged sludge,
Conventional sedimentation tanks have too low performance to remove fine particles and phytoplankton from lakes and seawater, and no countermeasures have been taken.

[Problem to be solved by the invention:
LssIo, ooO*g/l or more]: The high concentration treatment method is
The object of the present invention is to provide a possible agglomeration device and agglomeration method.

In addition, the present invention improves solid-liquid separation performance by more than 1,000 times compared to the current level. 1 light M, it can not only be used as a newly installed sedimentation tank, but also be applied to existing sedimentation tanks with low performance. phytoplankton, etc.
The purpose is to provide a device with good performance for removing agglomerates at a low cost.

[Means for Solving the Problems] The agglomeration device according to claim 1 is provided with a dispersion chamber for dispersing the water to be treated and a mixing pipe opening into the dispersion chamber in the liquid supply chamber for supplying the water to be treated, and for mixing. An injection tube is inserted into the tube, and the flow of injected liquid into the mixing tube from the injection tube outlet comes into contact with the flow of the water to be treated flowing into the mixing tube, and electrolytes are formed between the fine particles at the interface. This causes a concentration difference, and the resulting drop in repulsion potential causes repeated violent collisions between fine particles of 1 to 5XIO'mm, which are difficult to collide with, and creates a huge floc of 05 to 1m111 by the mixing tube outlet. The formed liquid mixture is sent to a solid-liquid separation chamber to separate flocs of fine particles.

The flocculating method according to claim 13 is an invention of a method for separating treated water into fine particles and a clear liquid using the flocculating device according to claim 1, wherein The flow rate of the mixed liquid (treated water and injection liquid) is set to IQ<ne<10'',
The flow rate of the injection liquid in the injection tube is maintained at 5 < n c <10'', and the two liquids are brought into contact with each other in the mixing tube to almost complete the flocculation action.

The water to be treated by the flocculation device of the present invention includes culture growth liquid, brewing waste liquid, dredged sludge [algae (diatoms, blue-green algae, green algae,
(including microorganisms, their dead bodies, and other organic and inorganic substances), lake water and seawater with a lot of phytoplankton that are not susceptible to eutrophication, and lakes that contain actinomycetes that cause musty odors and red tide flagellates yil (water, seawater, settled sludge from fish farms, industrial wastewater (including livestock sewage)
and its biologically treated water, domestic wastewater and its biologically treated water, human waste and its biologically treated water, top water and/or sewage and its biologically treated water.

The injection liquid can be biological treatment supernatant, physicochemical treatment supernatant, low concentration contaminated industrial wastewater, seawater, tap water, distilled water, irrigation water and/or industrial water (lake water, river water, groundwater, etc.). It will be done. Furthermore, as the injection solution, an aqueous solution containing a flocculant, such as a total flocculant (aluminum salt, iron salt, activated silicic acid, magnesium salt, calcium salt) aqueous solution, alkali metal salt aqueous solution, or polymer flocculant aqueous solution, may be used. can.

The solid-liquid separation chamber of the present invention refers to a chamber for concentrating the sedimented flocs by sedimentation and a chamber for flotation concentration for flotation concentration.

The present invention will be explained below based on the accompanying drawings.

FIG. 1 shows the agglomeration device (vertical type) of the present invention. In the flocculation device, the room to which the water to be treated 2) is supplied is called the liquid supply chamber 1).
A dispersion chamber 3) is provided in the liquid supply chamber. One or more mixing tubes 5) (two are shown in FIG. 1) are provided in the dispersion chamber,
One end of the mixing tube 5) with both ends open in the dispersion chamber is provided as a supply port for the water to be treated, and the other end is provided as a mixing tube discharge port +5) for directly discharging the aggregates into the solid-liquid separation chamber 4). This is a diagram of a device in which one injection pipe 6) is provided in the mixing pipe, with their respective central axes aligned. The injection pipe discharge port 14) opens toward the downstream side of the mixing pipe. A partition wall 8) is provided between the dispersion chamber and the solid-liquid chamber, and the injection liquid 10 is supplied from the injection pipe outlet.
) flows in contact with the flow of the water to be treated flowing from the annular part 17) to the single pipe part l8) (see Figure 4), and at the interface, violent collisions occur between the fine particles of the water to be treated. It is repeated to form huge flocs while passing through the mixing tube. The water supply ports of the plurality of mixing pipes are maintained at the same water level to equalize the amount of water flowing into each mixing pipe. The number of mixing tubes is determined so that the total amount of the mixed liquid 7) of the amount of water to be treated and the amount of injection liquid is maintained at a flow rate of I O < Re < 105 passing through each mixing tube. The flow rate of the injection liquid in the injection tube is also maintained at 5 Re<105.

FIG. 2 shows the aggregation device EL (horizontal type) of the present invention. Similar to the vertical type, a dispersion chamber 3) is provided in the liquid supply chamber l), a mixing tube 5) is provided between the dispersion chamber and the solid-liquid separation chamber (), and a wall thickness g! 8) is penetrated by a mixing tube. The arrangement of the mixing pipe (water to be treated) and the injection pipe (injection liquid), the flow velocity in the mixing pipe, and the flow velocity in the injection pipe are in the same range as in the vertical type.

In the flocculation device shown in Fig. 3, a plurality of injection pipes 6) are evenly arranged in one liquid supply chamber l), and a dispersion chamber 3) into which the water to be treated 2) flows is divided into a partition fla (for mixing from the injection pipe outlet to Pipe diameter X0.
3m or more" second class o11), on the upstream side of the partition line. The downstream side of the partition line is defined as a mixing tube 5), the area from the partition line to the injection tube outlet 1a) is an annular section, and the area from the injection tube outlet to the mixing tube outlet 15) is an m-tube section.

The arrangement of the mixing tube and the injection tube with respect to the annular section and the lli tube section, the flow rate in the mixing tube, and the flow rate in the injection tube are in the same range as above.

Figure 4 shows the central axis 11) of the injection liquid supply pipe and the central axis 12 of the injection pipe.
) and the center axis of the mixing tube 13) are completely aligned, and the injection tube is loaded with the porous material 16). When the central axes are completely aligned, the length of the injection tube can be shortened and solid-liquid separation performance can be improved.

FIG. 5 is adopted when a large amount of water to be treated is desired to be treated. Inside the mixing tube, insert a porous material into each of the two injection tubes (16).
It is a diagram in which the central axes of the mixing tube and two injection tubes are aligned with each other. Compared to when the injection tube is inserted into the mixing tube in parallel,
The agglomeration effect is large.

The solid-liquid separation performance improves when the fine particles in the water to be treated come into contact with the injection liquid, (0', 1-50)
m(7) A difference in electrolyte concentration occurs between fine particles, and the resulting drop in repulsion potential causes a strong agglomeration effect between the fine particles, and the mixing aggregation effect is repeated to form a huge floc toward the downstream of the mixing tube. . Therefore, even bulking sludge will form huge flocs. - When fishing by boat, when the electrolyte (ion) t5 degree difference between the two solutions is large, the bonding force between aggregated fine particles and floc particles seems to be strong. Preferably, the difference in electrolyte concentration between the injection solution and the water to be treated is 0.1 mg.
/1 or more, it becomes easier to form flocs, and IQm
When the ratio is g/1 or more, the floc-forming ability is strong. 2X lo
Although flocs can be formed even when the amount exceeds 'ag/1, the cost of the drug increases and it is not economical. When the water to be treated is seawater, if a polyvalent metal salt is used in the injection solution, the same coagulation effect can be achieved at a polyvalent metal salt concentration of lO to 1/200 of that of an alkali metal salt, so 2x IQ'mg/ It can be kept within 1.

If the flow rate in the mixing tube is Re>105, no flocs will be formed, and if Re<IO'l, flocs will be formed. If 10>Re, the amount of processing m per mixing tube will be small and the processing cost will be high. Even if the formed flocs are once destroyed when the flow velocity in the mixing tube becomes 105<Re<105, the flocs will still be formed if Re<105 is maintained. If the injection velocity of the injection liquid into or from the injection tube is Re>105, no flocs will be formed; Re<20'1. : If it is kept for 30 minutes, the growth of flocs will be promoted. If Re<5, the amount of injection tubes to be processed per tube will be small and the processing cost will be high.

The amount of injected liquid is 200 1/2 or less, preferably 30 to 1/2, relative to the water to be treated. Below 1z, the aggregation effect is low, 20
The floc formation ability remains unchanged even when the temperature exceeds 0, 2002
If it exceeds , the load on the solid-liquid separation chamber will be too large, and the effect of increasing the amount of injected liquid will not be observed.

When a partition is provided between the solid-liquid separation chamber above the dispersion chamber, the mixing tube is placed through the partition, and both ends of the mixing tube are connected to both chambers with a pressure of 1 iJ.
All the fine particles of the water to be treated pass through the mixing pipe, and if they are made to come into contact with the injection liquid discharged from one or more injection pipes in the mixing pipe, the VLT in the water to be treated will be reduced. Collision of the fine particles IJ becomes easier and flocs are formed within the mixing tube. When no partition is provided, the fine particles of the water to be treated flowing through the mixing tube and the injection liquid discharged from the plurality of injection tubes do not necessarily come into contact with each other. In addition, the injection liquid discharged from adjacent injection tubes interferes with each other to cancel out the formed electrolyte concentration difference, reducing collisions between @ fine particles, and the floc formation ability is lower than in the case where partition walls are provided. However, even without a partition wall, when the injection liquid is being supplied, the solid-liquid separation performance is much higher than when the injection liquid is stopped.

In the case where I or a plurality of injection tube discharge ports are opened in the mixing tube of the present invention, there are two cases in which a plurality of injection tubes are provided in parallel in one mixing tube as shown in FIG. An example of this is when the discharge port of an injection tube that is used in multiple stages inside the tube opens. Compared to the case where one injection pipe is provided in one mixing pipe, when multiple injection pipes are provided in multiple stages, for example,
As in the case where the injection liquid containing the metal salt flocculant is injected from the uppermost discharge port on the outermost side of the injection tube, and the injection liquid containing the metal salt flocculant or polymer flocculant is injected from the lowermost injection tube discharge port in the center, Suitable for injecting different types of injection liquids from different injection tube outlets. Furthermore, when multiple injection tubes are installed in parallel, the injection liquid discharged from adjacent injection tubes may interfere and cancel out the difference in electrolyte concentration on the fine particles once formed.
Floc-forming ability decreases.

When the injection liquid supply tube center axis 11) and the injection tube center axis 12) are brought together, the injection tube center axis has two points, the injection tube inlet and the injection tube outlet, and two planes perpendicular to the center axis. , Extension line 3 (1) of the central axis of the injection liquid supply tube The two intersections are centered on the two intersections of the central axis of the injection tube and the two planes, and are drawn within two circles drawn at 0.2 times the inner diameter of the injection tube. refer to something When the center axis of the injection liquid supply tube and the center axis of the injection tube coincide with the intersections of the two planes perpendicular to the center axis of the injection tube mentioned above (hereinafter referred to as merging with Songquan), the length of the injection tube can be determined. It can be made shorter. The case where the central axis of the injection tube and the central axis of the mixing tube 13) meet means that the two intersections of the two points perpendicular to the central axis and the central axis of the injection tube are the two points of the inlet and outlet of the injection tube. Center, and the inner diameter of the injection tube is 0.
This indicates that there is an intersection between the center axis of the mixing tube and the above two planes in the two rivers drawn at double the angle. When the center axis of the injection tube and the center axis of the mixing tube coincide with the intersections of two planes perpendicular to the center axis of the injection tube (hereinafter referred to as complete union), the aggregation effect is large, and the length of the mixing tube is can be made shorter.

The length of the mixing pipe is the annular part 17) where the water to be treated comes into contact with the injection pipe.
and the length from the injection tube outlet to the mixing tube outlet,
In other words, it is the sum of the lengths of the single tubes ffi1g).

The length of the annular portion must be 0.3 to 80 times the inner diameter of the mixing tube, and the length of the single tube portion must be 0.1 to 20 times the inner diameter of the mixing tube. The length of the tube from the injection tube outlet to a point 20 times the inner diameter of the mixing tube (mixing tube outlet) to the solid-liquid separation chamber is called a connecting tube that connects the mixing tube outlet and the solid-liquid separation chamber. death,
Not included in mixing pipe length. The length of the original part is 0 of the inner diameter of the mixing pipe.
．． If the length is 3 times or less, or if the length of the tube portion is 0.1 times or less, no floc-forming ability is observed. If the annular length is 80 times or more the inner diameter of the mixing pipe, or if the length of the single pipe part is 20 times or more the inner diameter of the mixing pipe, it will depend on the shape of the mixing pipe population, the viscosity of the water to be treated, and the friction coefficient of the pipe. Although the influence is small and the flocculation ability is exhibited, the mixing tube becomes too long and is not economical.

The longer the length of the mixing tube, the less it will be affected by the diameter of the mixing tube, the shape of the population, the cohesive force of activated sludge, the quality of the water to be injected, and the injection method. The length is preferably 0.1 to 10 m.

The inner diameter of the mixing pipe must be 0.01 m to be able to aggregate within 0.1 m.
The following is required: If the inner diameter of the mixing tube is less than this, 1
The amount of processing per book is small, resulting in high costs. 10 more
There is no problem in agglomerating if the length is more than 10 m, but if it is more than 10 m, the aggregating device including the length of the injection pipe becomes huge and is not economical. The length of this mixing tube is preferably a straight tube.

The inner diameter of the mixing tube is 0.01 to 5 m. If the length is 0.01 m or less, if the amount of processing liquid is large, the pressure loss will be large and the cost will be high.

If the length exceeds 5 m, the length of the mixing pipe becomes too long, making the apparatus large and uneconomical.

Even if the mixing tube installed between the dispersion chamber and the solid-liquid separation chamber is connected horizontally or diagonally as shown in Fig. 2), or vertically as shown in Fig. However, there is no difference in solid-liquid separation performance even if the direction of the mixing tube is different.

The inlets of the water to be treated in the multiple mixing pipes opening into the dispersion chamber are
If they are provided at the same water level (vertical type), the amount of liquid flowing into the mixing tube will be equalized, the mixing tube will tend to have a permissible outflow of &, and it is possible to eliminate the mixing tube that deteriorates solid-liquid separation performance.

The diameter of the injection pipe is indicated by dm (outer diameter), and the diameter of the mixing pipe is indicated by Dm (inner diameter). If the width (D-d)m of the annular portion 17) is narrow, the amount of water to be treated flowing into the annular portion will be non-uniform, reducing floc formation ability and solid-liquid separation performance. The outer diameter of the injection tube must be 0.97 times or less than the inner diameter of the mixing tube to allow uniform inflow. If the outside diameter of the injection tube is 0.01 times or less than the inside diameter of the mixing tube, even if the injection liquid M to the water port to be treated is 35, the velocity of the injection tube discharge port 14) will be 330 times, and the flow rate will be Re > 105. , the ability to form flocs decreases, and the solid-liquid separation performance decreases.

Even if the dispersion chamber and the solid-liquid separation chamber are two independent chambers separated by a layer, they can be connected by a mixing tube and a connecting tube.

When loading the porous material 16) into the injection tube 6), the loading position is located upstream from the injection tube outlet, at a point 1 of the injection tube diameter.
The rectification effect is greater when the distance is more than twice that, and it has a large effect on improving the flocculation performance. By providing an appropriate porous material at an appropriate position, it is not necessary to unite the center axis of the injection liquid supply pipe with the center axis of the injection pipe, and the amount of injection liquid can be reduced, and the length of the injection pipe and the mixing pipe can be shortened. Furthermore, when a porous material is used, even if the flow velocity in the mixing tube is increased to 10 times the Re when no porous material is used, that is, Re=105, giant flocs are formed.

The porous material is made of antibacterial polymer fibers and inorganic fibers, and has a thickness of 100 to 10 mm when the thickness is 10 mm. (100g/
*” non-woven fabric, antibacterial 0.01~: polymeric resin sponge made of Js (continuous fine bubbles), 0.01~
Powder and granular materials with a diameter of 5 ■, metal, inorganic, and polymeric resin porous plates with a hole diameter of 0, O1 to 3, woven fabrics, knitted fabrics, nets, membranes,
These: +: Materials can be used alone or in combination in layers. Loading height of porous bamboo material from 0.1 to 5
00m5, average speed in the tap water pipe sx 10-'m/se
It is desirable that the pressure loss at e is within 10 to 10,000 mm. If the pressure R1 loss is less than I0ratn, there is no rectifying effect, and if it is more than 10,000aIII, the required power is large and uneconomical.

Example 1 Using the flocculation apparatus shown in FIG.
g/l) was separated. Sedimentation tank water area load 12I++'
/ ta'' day, the liquid supply chamber (=dispersion chamber pipe diameter 11.7 m, pipe length 0.3 m, mixing pipe diameter 0.7 m, pipe length 1.5 m) had a diameter of 0.
．． Thirty injection tubes with a length of 1.05 m and a length of 075 m5 were inserted. Water to be treated when no injection liquid is injected (@activated sludge in air tank) (7) MLSSA 880 mg/l, SV+t.

=98. At that time, the activated sludge interface in the solid-liquid separation chamber was 0.35 m below the water surface, and the overflow water sludge concentration was 4 to 18+
*g/l. On the other hand, 14.5 m of infusion solution was added for 7 days.
After continuous injection for 4 hours, the interface of activated sludge is 1.
7 m, and the overflow water sludge concentration was 2 to 5 B/l. The flow of the mixed liquid in the mixing tube during that time is Re1580~1
It was maintained at 780. The injection solution is river water (COD2mg/
L NaCl content fft1.2mg/l) IQ (1g
'1J7JL'ri.

Example-2 A flocculating device of the same type as in Fig. 1 (mixing tube diameter 9 cm, length Igocm, injection tube diameter 7.5 cm, length 160 cm)
A slight bulking phenomenon is observed in the activated sludge obtained by biologically treating udon processing wastewater using a sludge (inserted and completely combined to form an annular length of 120 cm). Sodium chloride 36a+g/l of treated water (@activated sludge in air tank) 11Lss4] 30mg/l, SV+to” 97
Met. Water area load for solid-liquid separation chamber 12II15/
1! The interface of the activated sludge in the solid-liquid separation chamber when the injection liquid is not injected is 0.77 m1 below the water surface.
The concentration was 14 B/l. River water (COD) as injection liquid
Add sodium chloride to 2mg/I) and its content f
it 70mg/! 10% of the amount of water to be treated is 24
Flow rate Re = 1750 in the mixing tube, continuously injected for a period of time
1840, when treated with a water area load of 25 m'/+'' days in the solid-liquid separation chamber, the sludge concentration in the overflow water was less than 2 mg/l, and the returned sludge when the activated sludge interface was maintained at 1.7 m below the water surface. The concentration was 19,850 IAg/l.While keeping the above conditions the same, injection of the injection solution into the mixing tube was stopped,
2 o'clock IX'', the sludge concentration of the overflow water after J is 23g+sg/l
The interface of the active 1'5 mud floated 0.5 m below the water surface, making continuous operation impossible, but 2 hours after injecting the injection liquid, the mud r degree of the bath water was 4 mg/l. He had recovered. In this way, complete solid-liquid separation was possible even with tη mud, which only shows a bulking phenomenon.

Table-1 Volume of 71 human fluids to be treated None 0.1 None 0.1 Example-3 Biological treatment after neutralization of chip heated extract (NaCIZ8
7mg/l), a bulking phenomenon (SV,...;99) due to the generation of filamentous bacteria is clearly observed. Sludge concentration of the water to be treated at this time (@air tank sludge concentrated overflow liquid sludge 0 degrees 14o+g/1 2〃F 238!) 4 〃 12aA'/mTl 25 〃 25 〃 25 〃 Water area C'J 6: j degree) is 2.49Kg/m3. Solid-liquid separation chamber (
When treated with a water area load of 61 m'/lIl' day, the sludge interface in the solid-liquid separation chamber (settling tank) with a depth of 3.5 m is 0.65 m below the water surface, and the overflow water is 5 Sct degree. was 28 mg/l. This same water to be treated was collected using a flocculation device of the same type as shown in Figure 1 (mixing pipe diameter 12 cm, length 18 cm).
Insert an injection tube with a diameter of 9 cm and a length of IgOc- into the
6% of the water to be treated is supplied with the injection liquid (seawater) to the wall (the length of the wall is 120 cm), the flow rate in the mixing pipe is Re = 2340, and the water area load is 35 m'/m' day. When treated, the sludge concentration in the overflow water was 2 mg/l or less, and when the activated sludge interface was maintained at 1.7 m below the water surface, the returned sludge concentration was 9570 mg/l. In this way, complete solid-liquid separation was possible even with bulking sludge caused by filamentous bacteria. The supply of injection liquid 6z was stopped while this water area load remained at 35I11311f days, and the SS concentration in the overflow water after 1 hour showed 580 to 640 mg/l.

When the injection liquid was supplied again at 6% of the water to be treated while the water area load remained at 35 m'/m'' day, the 5S15 degree of the overflow water after 4 hours was restored to 2 mg 7'l or less.

Table-2 Injected liquid/Water to be treated Water area load 113/day/m'/day II'J/lm' day None 60.06 35 None 350.06 3
5 Example 4 Dredged sludge from a marsh was treated using the same type of flocculation device as shown in Figure 1. In one mixing tube (diameter?, 5c+n),
One injection tube diameter (6 cm) was inserted, and the center axis of the mixing tube and the center axis of the injection tube were completely aligned. A) Porous material [propylene nonwoven fabric (thickness 10 mm, l080 g/m
A rectifying layer was provided by filling 50 cm upstream from the injection tube outlet with three sheets of 15+ nm thick layered to make a total of 45+ am. B) There was no rectifying layer in the injection tube. The injection tube had a total length of 160 cm and was inserted into the mixing tube. The mixing tube had a single tube length of 80 cm, an annular portion length of 120 cm, and a total length of 200 cm, and was installed between the dispersion chamber and the solid-liquid separation chamber. Dredged sludge moisture (dry m group 1) ato3, ignition loss 31%, TOCI
A mixed solution of 30 mg/g dry mud, filtrate Cl-1.6 mg/l] and injection liquid was added to each mixing pipe for 56 m'7 days (overflow water sludge concentration mg/12 or less 580 to 640 2 or less Re = 1. Supply 1X IO″') to the dispersion chamber, and use one injection pipe: 1) River water (COD 2mg/1) using 816'/[3 as injection water l: Fe (trivalent) S
tag/I was added and fed. C) Pa (trivalent)2
0.11 of the 5 mg/l injection solution was added to 0.61 of the dredged sludge, a force of 90 G/sec was applied for 4 minutes in a coagulation tank, and flocs were removed by filtration. Filtration was carried out at a filtration speed of 18 m/hour through a filter bed filled with sand grains having a particle size of 0.8 mm to a thickness of 12 cm. Table 3 shows the SS5 degree in the filtrate, the concentration of dredged sludge concentrated in the solid-liquid separation chamber, and the SS concentration in the overflow supernatant.

Table-3 Condensation sludge concentration Supernatant liquid SS concentration Filtrate SS concentration Δ 32.400 to 41,600 mg/l I~
3111g/lB 21 , 300-30.600
mg/l I 8-23 (la+g/ICI
, 5a+g/1 Example-5 Allantoic syneresis (COD2060n+g/l, BOD525
CI 150
Diluted 6 times with 0 mg/l dilution water (river water including seawater),
Biologically treated water (MLSS5600mg/l, C
0D180+ag/l, BODISOmg/l) as the first
The flocculation device f1!2 shown in the figure (mixing pipe inner diameter 9ca+, 1
An injection tube of 6 cm and a 150 cm diameter were added to the 80 cm length, and the center axes of the injection tube and the mixing tube were aligned to make an annular portion of length 12 cm. Porous material for injection pipe (average diameter 0.2 m)
6C11 filled with sand grains of 0.6 mm on the upstream side of the discharge port.
Loaded into m. Injection liquid: tap water, dilution water C115001
75 injections of 1 g/l each of the water to be treated were made. The flow rate of the mixed liquid was Re = 4510 to 4B (10). Table 4 shows the SS concentration of the overflow water and the returned sludge concentration when treated with an average water area load of 35 fflff/llt day for the solid-liquid separation chamber A.

Table-4 Injected liquid Returned sludge concentration Overflow water SS concentration Tap water
12600mg/l 1 country/1 selected water 12
300 mg/l I to 2 mg/l [Effect of the invention J This invention is constructed as described above.

When the water to be treated comes into contact with the injection liquid flowing out from the injection pipe outlet in the mixing pipe, the particle size is 1 to 5 x 10" am at the interface.
Collision aggregation occurs between fine particles that are difficult to collide with, and further collisions occur to form huge flocs of 0.5 to 1+mm in size within the mixing tube within a few seconds. Its solid-liquid separation capacity is large, and when compared in terms of water area load, bulking sludge, which is processed in a conventional settling tank at 5 ml/l' day, can be solid-liquid separated in more than 100 h+'/C day. Furthermore, since the flocculating apparatus of the present invention is small and light, it is easy to install and can be installed in an existing settling tank to improve the solid-liquid separation performance several times.

The liquid supply cylinder of an existing settling tank that cannot handle the bulking sludge that occurs frequently, or between the outside of the liquid supply cylinder and the weir.
Even if the flocculation device of the present invention is installed and bulking sludge is treated with the same water area load as normal (20 to 30 m'/m per day), the SS concentration in the treated effluent is 2 tag/l or less, the return sludge concentration is 10, 000mg/l, it became possible to adopt the high-concentration activated sludge method.

Since the flocculating apparatus of the present invention can utilize the electrolyte in the water to be treated as a flocculating liquid for fine particles in the water to be treated, the cost of chemicals can be reduced.

Since the coagulation device of the present invention can use an injection solution containing an alkali metal salt as a coagulant, it is possible to coagulate and separate microorganisms that dislike polyvalent metal salts and microorganisms that are difficult to separate by sedimentation.

Furthermore, when using an injection solution containing a polyvalent metal salt as a flocculant, the concentration of the injection solution injected into the mixing tube is approximately a fraction of the concentration of the flocculant added using the flocculant addition method of a conventional flocculation device. It exhibits solid-liquid separation performance and requires less flocculant cost.

Conventional flocculation equipment required a high-speed stirring chamber for collision, but the flocculation equipment of the present invention simply brings the injected liquid and the water to be treated into contact in the mixing pipe, and collisions of fine particles occur, resulting in huge flocs. From forming the power for collision, high-speed stirring chamber,
A flock growth chamber is not required.

Dispersion chamber and solid-liquid molecules: Even if chamber a is connected horizontally, diagonally, or vertically with a mixing tube, the dispersion chamber and solid-liquid separation performance can be separated independently using a mixing tube and a connecting tube. Even if the connection is made, the formation of giant flocs will be completed in the mixing tube, so if the flow rate in the mixing tube and connecting tube is Re<105, the flocs will not be destroyed, so regardless of the connection direction or connection method, solid-liquid No difference was observed in separation performance.

The interface between the sludge and the supernatant liquid in the solid-liquid separation chamber is clearly defined13; the center axis of the mixing tube allows the inflowing sludge to be automatically drawn out at a speed commensurate with its sedimentation rate, making it easier to operate. Easy to manage.

[Brief explanation of the drawing]

FIG. 1 is a sectional view of the agglomeration device (vertical type) of the present invention. FIG. 72 is a sectional view of the aggregation device (horizontal type) of the present invention. FIG. 3 is a sectional view of a condensing device in which a large number of injection tubes according to the present invention are provided in a mixing tube. FIG. 4 is a cross-sectional view in which the central axis of the injection liquid supply tube, the central axis of the injection tube, and the central axis of the mixing tube of the present invention are completely merged. FIG. 5 is a cross-sectional view showing a mixing tube filled with a porous material and a discharge port of an injection tube opened in multiple stages. 1: Liquid supply chamber 2: Water to be treated 3: Dispersion chamber 4: Solid-liquid separation chamber 5: Mixing pipe 6: Injection pipe 7: Mixed liquid 8: Partition wall
9: Injection liquid supply pipe 10: Infusion liquid 11: Injection liquid supply pipe center axis 12: Injection pipe center axis 15: Mixing pipe outlet 18: Single pipe part

Claims (1)

[Claims] 1) Consisting of a liquid supply chamber 1) and a solid-liquid separation chamber 4), a dispersion chamber 3) for dispersing the water to be treated in the liquid supply chamber, one end serving as the dispersion chamber, and the other end serving as the dispersion chamber. Fine particles characterized by having a structure in which one or more mixing tubes 5) are provided that open to a solid-liquid separation chamber, and one or more injection tubes 6) are further provided for injecting an injection liquid into the mixing tubes. A flocculation device that separates treated water containing fine particles and supernatant liquid. 2) The flocculation apparatus according to claim 1, having a structure in which the dispersion chamber 3) and the solid-liquid separation chamber 4) are arranged horizontally, diagonally, and vertically, and a mixing tube 5) is provided between them. 3) The flocculation device according to claim 1 or 2, wherein the dispersion chamber 3) and the solid-liquid separation chamber 4) are connected by a mixing tube 5) and a connecting tube. 4) A structure according to any one of claims 1 to 3, characterized in that a partition wall 8) is provided between the dispersion chamber 3) and the solid-liquid separation chamber 4), and a mixing pipe 5) is provided through the partition wall. Flocculation device. 5) The aggregation device according to any one of claims 1 to 4, further comprising a supply pipe 9) for supplying the injection liquid to the injection pipe 6). 6) The aggregation device according to claim 5, wherein the central axes of the injection liquid supply pipe 9) and the injection pipe 6) are aligned. 7) The aggregation device according to claim 1, wherein the central axes of the injection pipe 6) and the mixing pipe 5) are aligned. 8) The aggregation device according to claim 1, having a structure in which the injection pipe 6) is loaded with a porous material 16). 9) Mixing tube inner diameter 0.01~5m, mixing tube length 0.1~
The agglomerating device according to claim 1, which is within a range of 10 m. 10) Request that the length of the annular portion 17) of the mixing tube 5) is 0.3 to 80 times the inner diameter of the mixing tube, and the length of the single tube portion 18) is 0.1 to 20 times the inner diameter of the mixing tube. The agglomeration device according to item 1. 11) The injection pipe diameter (outer diameter) is 0.0 of the mixing pipe diameter (inner diameter).
The aggregation device according to claim 1, wherein the agglomeration device is 1 to 0.97 times. 12) The flocculation device according to claim 1, wherein the inlets of the water to be treated flowing into the plurality of mixing pipes are set at the same water level. 13) When separating fine particles and supernatant liquid from water to be treated containing fine particles using the flocculation device according to claim 1, the flow of the mixed liquid in the mixing tube is 10<Re<10^5,
A coagulation method for separating fine particles from water to be treated, characterized in that the flow of the injection liquid in the injection pipe is maintained in the range of 5<Re<10^4. 14) The flocculation method according to claim 13, wherein the amount of injected liquid is 1 to 200% of the amount of water to be treated. 15) The flocculation method according to claim 13, wherein the difference between the electrolyte concentration in the injection solution and the electrolyte concentration in the water to be treated is in the range of 0.1 mg/l to 2×10^5 mg/l. 16) The aggregation method according to claim 15, wherein the electrolyte concentration in the injection liquid is lower than the electrolyte concentration in the water to be treated. 17) The aggregation method according to claim 15, wherein the electrolyte concentration in the injection liquid is higher than the electrolyte concentration in the water to be treated.