JPH09103609A - Flocculation apparatus and method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To enhance treatment capacity per one mixing pipe and the flocculation capacity of a flock forming tank by supplying a mixing soln. and an injection soln. certain in the concn. of an electrolite to the mixed soln. flowing through a mixing pipe from the discharge orifice of an injection pipe to bring them to a laminar contact state to perform flocculation in an increase pipe or the flock forming tank. SOLUTION: An injection soln. 16 is supplied to an injection pipe 19 and the discharge orifice of the injection pipe 19 (injection soln. 16) is turned toward the downstream direction of the polluted soln. flowing through a mixing chamber 17. The injection soln. 16 discharged from the discharge orifice of the injection pipe and the polluted soln. flowing through the mixing pipe 17 are brought to a laminar flow contact state to form a flock-containing sol. 28 which is discharge from the discharge orifice of the mixing pipe 8. The mixing pipe 17 is arranged in the increase pipe and the flock-containing soln. 28 discharge from the discharge orifice 8 of the mixing pipe and the increase pipe polluted soln. 34 flowing in the increase pipe 31 from an increase annular pipe part 37 are allowed to flow together and collides with other to form flock. Further, in the fluidized bed above the collision mixing part 20 of a flock forming bed 7, violent collision of medium and small flocks is repeated to form large flock.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for efficiently separating fine particles from a concentrated or dilute polluted liquid, separating and concentrating the fine particles into giant flocs and a clear liquid, and an apparatus suitable therefor. Regarding

[0002]

2. Description of the Related Art In order to agglomerate a polluted liquid when it is diluted, an inorganic flocculant is added to a flocculation chamber provided with a high-speed stirring reaction chamber in order to enhance the effect of collision between fine particles. However, if the solid-liquid separation performance is small, a method is adopted in which a polymer flocculant is further added to form huge flocs by bridging the polymer flocculant between fine flocs, and then separated in a precipitation tank. There is. The fine floc flocculation sludge formed by adding the flocculant of this method cannot be re-flocculated even if it is added to a dilute pollutant for repeated circulation.

The inventor of the present invention previously has an aggregating device and an aggregator for aggregating and separating fine particles [microorganisms (activated sludge), algae, minerals, plankton, etc.] from water to be treated containing fine particles such as brewing waste liquid, culture growth liquid and dredging. Invented the method (application number 1988, Japanese Patent Application No. 155624, 1988, Japanese Patent Application No. 176579). In this aggregating device, in order for the injection liquid and the fine particles of the water to be treated (dredge liquid) to agglomerate, it is an absolute condition that the two liquids having different electrolyte concentrations are brought into laminar flow contact. That is, the amount of liquid to be treated supplied to one mixing tube must be maintained at Re <10 ⁵ in order to make a laminar flow contact, so that the treatment capacity is low and it has been desired to further improve the treatment capacity.

[0004]

[Problems to be Solved by the Invention] (Application No. 155624 in 1988, Application No. 1 in 1988)
No. 76579) The flocs formed in the mixing pipe are in the flocculation tank (application number 1993, patent application No. 206793).
At that time, it collides with fine particles in the contaminated liquid to form flocs, but there is a restriction on the flow rate to make the injecting liquid and the water to be treated contact in a laminar flow, and the amount of the treating liquid per mixing tube is small, so a large amount. In order to process the liquid to be treated, it is necessary to increase the number of mixing tubes, which has a drawback that the equipment cost increases.

The present invention has a processing capacity per mixing tube,
To provide an aggregating and concentrating device and an aggregating and concentrating method capable of enhancing the aggregating performance of a floc forming tank and reducing the equipment cost.

[0006]

Means for Solving the Problems The present inventor has proposed a Japanese Patent Application No. 63-
Japanese Patent Application No. 5-2067 in the solid-liquid separation chamber of the flocculating device described in the specifications of No. 155624 and Japanese Patent Application No. 176579/1988.
A flocculating and concentrating device having a structure in which the flock forming tank described in No. 93 is provided and the discharge port of the mixing pipe is located inside the flock forming tank is We succeeded in obtaining concentrated sludge by colliding with flocs having cohesive force and flocculating flocs in a short time. It was discovered that the floc-containing liquid discharged from the mixing pipe had a sufficient flocculating ability to collide with the contaminated liquid of the increasing pipe to be fed to the floc forming tank and flocculate. In addition, the injection liquid in which fine particles with less electrolyte elution are added to the injection water or the condensed concentrated sludge and / or the injection water in the bottom of the solid-liquid separation chamber
Or a floc formed in the mixing tube by laminarly contacting an injecting solution to which the filtered residue and / or the filtered and washed residue is added with a contaminated solution (having a difference in electrolyte concentration from the injecting solution) in the mixing tube The contained liquid has a higher residual cohesive force than the floc-containing liquid formed by laminar flow contact between the injected water and the polluted liquid of Japanese Patent Application No. 63-155624, and is 1.5 to 25 times larger than the floc-containing liquid 1 It was found that the treatment capacity per mixing tube is improved by colliding the tube contaminated liquid in the increasing tube or / and further in the floc forming tank to form huge flocs. Since it is easy to collide between the small flocs of the floc-containing liquid and the small particles of the floc-containing liquid and the fine particles (5 × 10 ⁻⁴ mm or more) of the bulking pipe contaminant, the fine particles of the bulking pipe contaminant are It was found that the amount of polluted liquid in the increasing pipe can be increased as the concentration of the liquid containing flocs is small and the difference in specific gravity from the liquid is not so small.

The fine particles added to the mixed solution are a pollutant or a mixed solution containing fine particles added thereto and / or agglomerated concentrated sludge and / or a filter cake of the agglomerated condensed sludge and / or a filter cake washed by filtration. (Liquid having a large difference from the electrolyte concentration of the injection liquid was added to the mixed liquid, and the injection liquid was 1 p
(a difference of pm or more) is formed in the mixing tube by laminar flow contact with the water containing the flocs. The residual cohesive force is higher than that of the floc-containing liquid to be formed, and the amount of the pipe is 1.5 to 50 times larger than that of the floc-containing liquid (1-50 ppm or more of the electrolyte concentration difference from the floc-containing liquid), and the concentration is low. Increasing pipe contaminant (SS 1000ppm
It has been found that the processing capacity per mixing tube is improved by colliding 100 times with (in the following) and forming a huge floc in the increasing tube or in the floc forming tank.

[0008] The single pipe portion of the increasing pipe preferably has a thin pipe diameter and is equipped with a collision system in which one to several sets of weirs and mixers are arranged in the pipe, and a small floc of a liquid containing flock and a contaminated liquid of the increasing pipe. The small and medium floc groups in which the small flocs grow fine particles by repeatedly colliding, aggregating, concentrating and mixing with the fine particles of
Several times as large as No. 637, the aggregation performance was improved.

The aggregating apparatus used in the practice of the present invention supplies a contaminated liquid having a pollutant concentration sufficient for agglomeration and an injection liquid, and is provided with a dispersion chamber for dispersion and a mixing pipe open to the dispersion chamber, and the mixture is injected into the mixing pipe. Insert a pipe and supply the injection liquid with an electrolyte concentration difference of 1 ppm or more between the injection liquid and the mixed liquid in the downstream direction along the flow of the mixed liquid flowing in the mixing pipe from the injection pipe discharge port to form two liquid layers. The floc-containing liquid formed by flow contact is kept at a high concentration, the difference in electrolyte concentration from the contaminated liquid of the increasing pipe is kept at 1 ppm or more, and the liquid collides, aggregates, concentrates and mixes in the increasing pipe or in the floc forming tank.

In order to cause the small flocs having a concentration of the floc-containing liquid formed by the laminar flow contact of the mixed liquid and the injecting liquid to collide with and agglomerate with the fine particles of the increasing pipe pollutant, the number of the small flocs serving as the cores should be increased. Is. Therefore, it is necessary to increase the liquid concentrations of the mixed liquid and the injection liquid.

A) When fine particles are not added to the injected water:
The flow from the injection liquid discharge port and the flow of the contaminated liquid (electrolyte concentration difference from the injection liquid is 1.0 ppm or more) flowing from the mixing pipe annular portion 39 into the mixing pipe single pipe portion 40 (FIG. 1). In the laminar flow (10 <Re <1 × 10 ⁵ ) contact, there is a difference in the electrolyte concentration on the particle surface between the particles in contact with the injection liquid and the particles not in contact with the injection liquid in the fine particle group at the interface. Then, a potential difference occurs on the surface of the particles. For example, even if the potentials of the particle surfaces have the same sign, if the distance between particles is 100 Å (August strong) or less, attractive force acts, the repulsive force between particles decreases, and the diameter (1-5) × 10 ⁻⁴ Repetition of violent collisions between fine particles that are difficult to collide with mm, and supply the floc-containing liquid in which small flocs of 0.2 to 1 mm have been formed up to the discharge port of the mixing tube and the volume increasing pipe communicating with the distribution chamber or the floc formation tank. The flocculating tank 34 is collided with the incoming volume contaminated liquid 34 to form huge flocs in the flocculation tank, and the flocs concentrated in the solid-liquid separation chamber are separated. The contaminated liquid supplied to the dispersion chamber 18 from the contaminated liquid supply pump 15 from the primary mixing tank 5 into the dispersion chamber and the distribution chamber overflows from the upper edge of the mixing pipe in the dispersion chamber and is supplied to the mixing pipe. Is overflowed from the upper edge of the volume increasing liquid supply pipe and supplied to the volume increasing liquid supply pipe. Amount of liquid containing flock discharged from the mixing pipe outlet 1
On the other hand, since the amount of polluted liquid of the increasing pipe is 1.5 to 10 times, it may be in contact with the swirling flow, so that the discharge speed of the increasing pipe to the floc forming tank is 1 × 10 ⁶ >Re> 5 × 10 ² Will be selected. In general, 5x
It is desirable that 10 ⁵ >Re> 1 × 10 ³ . When fine particles are not added to the injected water, and when the mixed solution is supplied with Re corresponding to the diameter of the mixing tube, the area of the bottom of the flock forming tank is 50 to 400 times the total area 1 of the mixing tube discharge port, the flock forming tank. The horizontal area surrounded by the uppermost overflow weir is 10 to 3000 times. Example 2 Washing wastewater SS concentration 6400ppm (Ca +
+ 6.8ppm) of contaminated liquid 140l / hr to the mixing tube,
Injection liquid is groundwater (Ca ++ 1.1ppm) 15l / hr
Is continuously supplied to the increasing pipe, and the increasing pipe polluted liquid (AB) 1 m ³ /
There is no rolling up of fine particles in hr (supernatant is 10 ppm
In the following, (B) 2 m ³ / hr was observed to be wound up. The amount of the contaminated liquid in the increasing pipe was 6.45 times the amount of the floc-containing liquid (SS concentration was 5.8 g / l) (1). (A
B): is the amount of increasing pipe polluted liquid [(A) + (B)] / 2 = 1 m
³ / hr The area surrounding the overflow weir of the flock forming tank used in this experiment was 700 times the area of the mixing pipe discharge port, and the area of the tank bottom was 70 times.
The height of the tank was 1 m.

B) When fine particles are added to the injected water, for example, as the fine particles added to the injected water, the flocculated condensed sludge 14 is added.
In the case of adding: The injection liquid 16 obtained by stirring and mixing the injection water 2 and the fine particles 6 with little electrolyte elution in the injection liquid stirring tank 36 in FIG. 1 and FIG. 2 is supplied by the injection liquid supply pump 35. In the case of adding the coagulated concentrated sludge 14, the coagulated concentrated sludge 14 supplied by the circulation pump 12 at the bottom of the solid-liquid separation chamber 10 or a filter residue obtained by filtering the filter, and a filter residue washed and filtered (electrolyte of the polluted liquid and the injection liquid) If the difference in concentration does not exceed several ppm, it is recommended to add a liquid with a large difference in electrolyte concentration to the filter cake before use.
The injection liquid 16 prepared by mixing the injection water 2 and the injection water 2 in the injection liquid stirring tank 36.
(SS concentration of 500 to 6 × 10 ⁴ is supplied to the injection liquid supply pump
When supplied by, the floc containing liquid concentration (SS concentration 100 to 6
× 10 ⁵ ppm) becomes high, and the aggregating performance with the increasing pipe contaminant becomes high. The injection liquid is discharged from the injection port of the injection pipe while maintaining the flow rate of 5 <Re <1 × 10 ⁴ to maintain a concentration at which fine particles of the mixture liquid of the injection liquid and the contaminant can collide. To do. As for the contaminated liquid, the flow of the contaminated liquid (mixed liquid) from the mixing pipe annular portion 39 in the mixing pipe to the mixing pipe single pipe portion 40 (FIG. 1) and the injection liquid are in laminar flow (10 <Re <1 × 10 ⁵ ) However, the difference in the electrolyte concentration between the injected liquid and the polluted liquid (mixed liquid) is 1 ppm.
If there is the above, there is a difference between the potentials of all the fine particles previously added to the injection liquid and the potentials of all the fine particles of the contaminated liquid flowing into the single tube portion of the mixing tube, and when the two liquids come into laminar contact. Instantly forms flock. When a square tube other than the circular shape (diameter = D) is used as the mixing tube, Re is calculated with the side length = b as the equivalent diameter (Deq). No difference is observed in the coagulation performance regardless of whether the mixing tube is circular or square. The concentration of fine particles added to the injection liquid is 1 x 10
^{4 to} 6 × 10 ⁵ ppm, preferably 1 × 10 ^{4 to} 6 × 10
It shall be ⁵ ppm.

B-1) When the polluted liquid is thin and fine particles are added to the injection water: Aggregated concentrated sludge 1 added as fine particles to the above-mentioned injection liquid 1
4 is a flocculation-concentrated sludge supplied by a circulation pump 12 at the bottom of the solid-liquid separation chamber 10 or a filtered filter residue is supplied to a stirring and mixing tank 5 and mixed with a polluted liquid 1 to form a mixed liquid 41 as a dispersion chamber 1
8 The concentration of the floc-containing liquid formed in the mixing pipe is gradually increased to achieve stable operation. Considering the case where the concentration of the contaminated liquid (mixed liquid) is 10 ppm, which is thinner than the injected liquid, the floc-containing liquid discharged from the mixing pipe discharge port formed from the fine particles added to the injected liquid and the fine particles of the contaminated liquid in the mixing pipe. When SS is 1000 ppm or more, it becomes possible to aggregate.
Using the same apparatus as in Example 2, the pollutant concentration was 0.31 g, which was the average of the pollutant that supplied the river water in the case of rain in Table 3 with a low pollutant concentration to the mixing pipe.
/L(Ca++2.1ppm)(C)(E)(F)14
5 l of diatomaceous earth (C) and 10 kg of (D) (E) were added to 0 l / hr and 100 l of infused liquid seawater, and 15 l / hr were continuously supplied to (C) (D) (E), respectively, and an increase pipe Intensifier pipe pollution liquid (C) 0, (D) 0, (E)
1.1 m3 / hr was supplied. In (C), a winding phenomenon was observed. (D) and (E) were not observed. , The amount of the floc-containing liquid (E) (SS concentration was 10 g / l) was 1 times, and the amount of the contaminated liquid in the expanding pipe was 7.1 times. In the flock forming tank, the overflow weir area was 700 times the mixing pipe discharge area and the tank bottom area was 70 times.

B-2) When the contaminated liquid is thick and fine particles are added to the injection water: All the fine particles added to the injection liquid are charged to a potential corresponding to the electrolyte of the injection liquid, and there is a difference between the injection liquid and the electrolyte concentration. There is a difference in the potential of all the fine particles of a certain mixed liquid, and when the two liquids come into contact with each other in a laminar flow, a violent collision between the fine particles from the two liquids from the injection liquid discharge port to a distance 1 to 3 times the diameter of the mixing pipe. The formation of small flocs is complete. The floc-containing liquid forming the small flocs is transferred from the mixing pipe discharge port to the single pipe part of the increasing pipe, and collides with the fine particles of the increasing pipe polluted liquid. Example 2
The amount of polluted liquid (AB) (D) SS 6.4 g / l, 14 which supplies the washing rice effluent of Table 2 with high concentration of polluted liquid to the mixing pipe
0 l / hr, injection liquid amount (ΛB) SS 0 g / l, 17.5
l / hr (D) SS 120 g / l, 60 l / hr, floc-containing liquid concentration (AB) 5.7 g / l, (D)
40.5 g / l Volume increase pipe contaminant supply amount is (AB) 1 m ³ /
The ratio of hr, (D) 8.3 m ³ / hr to the concentration of the floc-containing liquid is 7 times, and the ratio of the supply amount of the increasing pipe polluted liquid is 8 times.
The amount of the contaminated liquid in the increasing pipe is (ΛB) for the amount of liquid containing flock 1
6.3, (D) reached 41.5 times. (ΛB) indicates the average value of (A) and (B). The maximum amount of the amount of the contaminated liquid supplied to the increasing pipe, in which the phenomenon of rolling up of fine particles was not recognized, was a) 6.45 times b-1) 7.1 times b-2) 41.5 times the amount of the floc-containing liquid amount 1. The maximum concentration of flocculent liquid supplied when no phenomenon was observed The concentration SS of the floc-containing liquid when it was obtained was a) 5.8 g / l, b-1) --- [Different in specific gravity between starch and mud] b -2) It was 40.5 g / l.
Concentration of liquid containing flocs The concentration of liquid containing flocs is increasing, and the amount of polluted liquid in the increasing pipe is increasing.

C) In the case of adding fine particles to the injection water and the mixing pipe: The injection liquid and the mixed solution are adjusted by adjusting the injection water 2 and / or the pollutant liquid 1 and / or the condensed concentrated sludge 14 and / or the fine particles 6. It is adjusted in the tank 36 and supplied as the injection liquid 16. When the polluted liquid 1 is thick, it is supplied to the dispersion chamber 18 and the distribution chamber 30. When the polluted liquid 1 is thin, the coagulated concentrated sludge 14 and / or the primary mixing tank 4 is added with the injected water 2 and the fine particles 6 and stirred, and the mixture is supplied to the stirring and mixing tank 5 and supplied from the pollutant supply pump 15 to the dispersion chamber 18 And to the distribution chamber 30. The supplied contaminated liquid (mixed liquid 41) overflows from the dispersion chamber and is supplied to the mixing pipe, and the contaminated liquid 1 is supplied to the distribution chamber 30 and overflows from the distribution chamber and is supplied to the increasing liquid supply pipe. When the contaminated liquid supplied to the distribution chamber is thin, a concentrated mixed liquid 41 may be supplied from the contaminated liquid supply pump 15 to correct the concentration of the contaminated liquid. The fine particles to be added to the injection water are the injection liquid. Fine particles with little electrolyte elution into the injection water or the coagulated concentrated sludge at the bottom of the solid-liquid separation chamber and / or the sludge of the coagulated concentrated sludge and / or the coagulated concentrated sludge are filtered. All the fine particles added with the washed filter and the fine particles added to the mixed solution are the pollutant liquid or the polluted liquid added with the fine particles and / or the coagulated concentrated sludge and / or the coagulated concentrated sludge filter and And / or all the fine particles in the liquid added with the filtered and washed filter cake (a liquid having a large difference from the electrolyte concentration of the injection liquid was added to the mixed liquid to make a difference of 1 ppm or more from the injection liquid). Then, all the fine particles added to the injecting liquid are charged to a potential corresponding to the injecting liquid, and the fine particles added to the mixed liquid are charged to a potential corresponding to the mixed liquid. The difference in electrolyte concentration between the two solutions is 1p
If there is a difference of pm or more, when the injection liquid discharged from the injection pipe discharge port and the contaminated liquid (mixed liquid) flowing through the mixing pipe are brought into laminar contact, flock is instantaneously formed. This floc-containing liquid 28
Is discharged from the mixing pipe discharge port 8 into the increasing pipe, and if the difference in the electrolyte concentration with the increasing pipe pollutant is 1 ppm or more, they collide and aggregate. 2
Since the fine particles added to the liquid can be added up to about 1 × 10 ⁵ , the concentration of the floc-containing liquid is increased, and the amount of the polluted liquid in the increasing pipe can be increased. In Fig. 1, the area of the bottom of the floc formation tank is 70 times the total area 1 of the mixing pipe discharge port, but 5 to 4
The horizontal area surrounded by the uppermost overflow weir of the floc formation tank is preferably 000 times, but it is 10 times to 15,000 times (the mixed solution and the injection solution are not supplied to the pipe diameter to the full, and the amount of the increase pipe contaminant is Corresponding to the increased amount of) is desirable. The tank height is 40 times the diameter of the mixing tube, but it is desirable to increase it to 30 to 60 times to apply a static pressure to the inside of the volume increasing tube. It is easy for the small flocs of the floc-containing liquid to collide with each other and for the small particles of the liquid for increasing pipe contamination to collide with each other, but it is difficult for the fine particles to collide with each other. It is clear in Example 2.3 that small flocs can be increased by increasing the concentration of the floc-containing liquid.
Example 2 Contaminated liquid SS 6.4 g / l. 140 l / hr
(Λ) (D) is supplied to the mixing tube, and the injection liquid SS0g / l
(A), 120g / l (D) into the injection tube 15l / hr
(A), the concentration of the floc-containing liquid formed by supplying 20 l / hr (D) is 5.8 g / l (A), 20.6 g / l
In contrast to (D), the supply amount of the increasing pipe pollutant is 1 m ³ / hr (A
B), 8.3 m ³ / hr. Example 3 Contaminated liquid SS
Average 307 ppm. 140 l / hr (C) (D) (E)
Is supplied to the mixing tube, and the injection liquid SS 50 g / l (C), 10
The concentration of the floc-containing liquid formed by supplying 0 g / l (D) (E) to the injection tube at 15 l / hr was 5.1 g / l (C), 1
To 0g / l (D) (E ), supply amount of bulking tube polluted liquid was ^{0m 3 /hr(C)(D),1.1m 3 / hr (E} ). As the concentration of the floc-containing liquid increases, the supply amount of the amount of the increasing pipe polluted liquid also increases. Fine particles may be added to either or both of the injection liquid and the mixed liquid to increase the concentration of the floc-containing liquid. In Example 5 (using the collision system), 6400 ppm of washing rice drainage was added to the mixed solution at 30 l / hr.
(B), 3 l / hr (D), injection liquid 6 × 10 ⁴ ppm,
With a floc of 3 l / hr (B) and 30 l / hr (D) (concentration: 11.3 g / l (B), 55.1
g / l) It was possible to verify the increase pipe pollution amount 45 times and 151 times with respect to the amount 1. In Example 6, the concentration of the floc-containing liquid when diatomaceous earth (specific gravity 2.1) was added to the injection liquid was the same in both cases where the injection liquid and the mixed liquid were activated sludge (specific gravity 1.01). The number of small flocs formed from the two liquids, the injection liquid and the mixed liquid, is considered to be halved when diatomaceous earth is added. The amount of supply of the expansion pipe pollutant is 2 m ³ for the one to which diatomaceous earth is added.
/ Hr, the value without diatomaceous earth showed 4 m ³ / hr. The fine particles to be added for the purpose of forming the floc-containing liquid should be selected so that the difference in specific gravity from the fine particles in the expanding pipe polluted liquid is not too large and not too small. It is assumed that the ideal specific gravity difference is 0.2 to 0.6.

In order to increase the concentration of the floc-containing liquid, the contaminated liquid is mixed with the mixing pipe annular portion 39 in the mixing pipe (round pipe. Square pipe).
Flow of the contaminated liquid (mixed liquid) from the mixing tube to the mixing pipe single pipe section 40 (FIG. 1) and the injected liquid are in laminar flow (10 <Re <1 × 10 ⁵ ), and the injected liquid and the contaminated liquid (mixed liquid) If the difference in the electrolyte concentration with) is 1 ppm or more, there will be a difference between the potential of all the fine particles added to the injection liquid in advance and the potential of all the fine particles of the contaminated liquid flowing in the single pipe part of the mixing tube. When the two liquids come into contact with each other in a laminar flow, flock is instantly formed. The small flock number in the floc-containing liquid formed in the mixing pipe by laminarly contacting both the injection liquid containing the fine particles and the mixed liquid is found in Japanese Patent Application No. 63-
The number of small flocs in the floc-containing liquid in which the two liquids of the injection liquid containing no fine particles and the mixed liquid containing fine particles of 155624 are in laminar contact to form flocs is much larger.
A sufficient flocculating ability remains so that the amount of the floc-containing liquid collides with the amount-increasing pipe contaminant in the amount-increasing pipe or the amount-increasing pipe contaminant supplied to the flock forming tank to cause aggregation.

The residual cohesive force of the floc-containing liquid that is in laminar contact with the two liquids containing fine particles in both the injecting liquid and the mixed liquid has a high residual cohesive force. 200 times as much expansion pipe pollutant (electrolyte concentration difference is 1 ppm or more as compared with the floc-containing liquid), and low-concentration flow pipe pollution liquid (SS 1000 ppm or less) 1
It has been found that the processing capacity per one increasing tube is improved by colliding with 00 times or more in the increasing tube or the floc forming tank to form a huge floc.

It is easy for the small flocs of the liquid containing the flocs to collide with each other and for colliding the small flocs with the fine particles of the metering pipe contaminated liquid, but it is difficult for the fine particles to collide with each other. To efficiently collide with and 1) increase the number of small flocs that are the core of the floc-containing liquid,
2) The floc-containing liquid and the contaminated liquid of the expansion pipe are efficiently collided and mixed in the expansion pipe. 3) The distance between particles is narrowed (compressed and concentrated). 4) Concentrating and mixing fine particles and small flocs of the floc-containing liquid to grow into a small floc group, and 5) Collision between small flocs and concentrating to grow into medium flocs. The means for that are a) increasing the number of small flocs serving as the core, and increasing the liquid concentration of the injection liquid and the mixed liquid. (B) An electrolyte concentration difference is created between the small flocs of the floc-containing liquid and the fine particles of the expansion pipe pollutant. C) Collision / aggregation / concentration between small flocs and fine particles of the expanding liquid
A collision system is provided to increase the frequency of mixing. ,

It has been described above that (a) the concentration of the injecting liquid and the mixed liquid is increased to increase the number of small flocs of the floc-containing liquid in order to enhance the aggregation performance of the present invention. There is a limit to increasing the concentration of the floc-containing liquid (the liquid cannot be retained) in order to further increase the amount of the volume-inclusion liquid, and it is necessary to improve the performance of collision and aggregation between the floc-containing liquid and the volume-inclusion liquid. Is becoming. (B) Adjust by adding, to either the mixed solution or the injecting solution, the increase pipe contaminated liquid and groundwater (tap water) seawater having a large difference in electrolyte concentration. C) Collision, coagulation, concentration and mixing of the fine particles of the volume increasing tube and the small flocs of the floc-containing liquid are repeated in the volume increasing tube to grow a group of small flocs without fine particles.

(A) b) should be solved in the preceding step of the volume increasing tube. B) is as already explained. In (4), the concentration of the floc-containing liquid is the same in Examples-4 (D), (E), and (F), and it can be understood that the floc-containing liquid is agglomerated because there is no SS in the cleaning liquid. The difference in the electrolyte concentration between the contained liquid and the expanding pipe polluted liquid was Na + 100 ppm or more (E) and (F) was 1 ppm calculated as Na +. Flock growth in the impingement system with the floc-containing liquid in the extender tube is barely observed in (F). In (D), the higher the concentration of the floc-containing liquid, the more the small flocs, the difference of 5 ppm from the electrolyte concentration of the expanding pipe contaminant.
It has been shown that the small flocs of the floc-containing liquid and the fine particles of the expanding pipe polluted liquid can easily collide with each other, and it is possible to supply a group of small and medium flocs having almost no fine particles in the floc formation tank. Floc containing liquid concentration SS
When it is possible to supply a large amount of 30 parts by weight or more of the SS of the increasing pipe contaminant to 1 part by weight, the difference in the electrolyte concentration between the floc-containing liquid and the increasing pipe contaminant is preferably 5 ppm or more, and the fine particle diameter of the increasing pipe contaminant is At 5 × 10 ⁻⁴ mm or more, the specific gravity difference between the fine particles of the polluted liquid and the floc-containing liquid is 0.3.
The following is desirable. As a method of increasing the electrolyte concentration between the floc-containing liquid and the increasing pipe pollutant to 1 ppm or more, for example, the injection liquid and the increasing pipe pollutant are used as the contaminated liquid, and the coagulated concentrated sludge is used as the mixed liquid, and a liquid with a large difference in the electrolyte concentration ( 1-10% (for example seawater or tap water) is added only to the mixture. The method of controlling the difference in electrolyte concentration between the mixed solution, the injecting solution, and the contaminated liquid of the increasing pipe to be 1 ppm or more is easy to manage. It is not easy to collide small flocs having an electrolyte concentration difference of 1 ppm or less between the floc-containing liquid and the increasing pipe contaminant with fine particles having a fine particle concentration of 400 ppm or less in the increasing pipe contaminant.

(C) was solved by providing a collision system in the increasing pipe. The following equipment a) The diameter of the expansion tube is reduced, b) The weir (Oris plate, nozzle, collision plate, screen) is provided, c) Combination plate of collision plate and collision plate-13, Combination diagram of collision plate and weir 14. Combination of mixing blades The static mixer shown in FIG. 12 is provided. D) The floc formation tank height is increased in order to apply static pressure to the small floc group to concentrate and grow it. Part or all of the equipment in (c) works intricately intertwined with each other to act as a plurality of the above means. Therefore, collision, coagulation, concentration and mixing immediately after the mixing pipe discharge port in the volume increasing pipe or the floc forming tank. As an example of the instrument device for the purpose of FIG. 10, a collision system in which FIGS. 10, 11, 13, 14 and the like are mounted (as an example, FIG. 12 and the like will be referred to) will be incorporated. Figure-12 is explained. It is an example of a collision system. a) The diameter of the increasing tube is reduced to narrow the distance between particles of the contaminated liquid in the tube. b) The weir has a function that the nozzle 45-1 in FIG. 12 collides with the contaminated liquid flowing from the annular portion of the increasing pipe into the single pipe of the increasing pipe and the floc-containing liquid from the discharge port of the mixing pipe, and mixes the mixture to the static mixer. There is. c)
It has the function of causing small flocs to grow by colliding and mixing the small flocs of the floc-containing liquid with the fine particles of the increasing pipe polluted liquid by a static mixer. d) The nozzle 45-2 is in the mixer,
The nozzle 45-3 has a function of narrowing the distance between the fine particles of the polluted liquid and the particles of the small flocs in the increasing pipe to enhance the effect of collision-aggregation mixing (the difference in the electrolyte concentrations of the two liquids is also large). This a)
b) Arrange the devices having the functions of c) and d) and mount them in the expansion tube. This is called a collision system. With this system, small and medium floc groups, in which small floc groups without fine particles have grown, are supplied to the floc forming tank, and stable operation is always possible. By providing this system for strengthening the collision mixing, the supply amount of the increasing pipe contaminant when the collision system is not provided is improved several times when the results of Example 2 and Example 5 are compared. I understand. Even if a plurality of mixing pipes (round pipes or square pipes) are arranged in one expansion pipe (round pipes or square pipes), if the collision system is incorporated, no reduction in cohesive performance is observed. In Example 2, a floc-containing liquid (concentration 40.
5 g / l (D) 1 to 44 times the amount of the expanding pipe polluted liquid, while Example 5 (B) (D) was 11.3 g / l of the floc-containing liquid
(B), the concentration is 55.1 g / l (D) 1, and the amount of the amount-increasing pipe contaminant is 45.5 times (B) and 150 times (D). It is considered that the effect of the installed collision system is that the same system as in Example 2 was equipped with the collision system Fig. 12 in the single pipe portion of the increasing pipe in Example 5, and the same rice washing wastewater was treated to make a large difference. The performance is exhibited without installing all the equipment and devices of the collision system (a) to (e). Since the collision system provided in the single tube of the increasing tube repeats collision, coagulation, concentration and mixing using the flow of the polluted liquid, the pressure loss due to the vortex in the tube is large,
When it is set to 1 to 50 mm, preferably 5 to 40 mm, it is easy to balance the pressures when a large number of increasing tubes are installed in the flock forming tank. If it is smaller than 5 mm, the performance is low.

Even if the type of the injection water to which the fine particles are added is a pollutant, it is sufficient that the difference between the electrolyte concentration of the injectate and the electrolyte concentration of the pollutant to be supplied to the mixing tube is 1 ppm. It will be selected in consideration of the purpose of using the treated liquid. For example, tap water, industrial water, agricultural water, lake water, river water, groundwater (underflow water), biologically treated water, physicochemically treated water, seawater, brackish water, liquid containing alkali metal salt or alkaline earth metal salt, polluted liquid ( Examples include activated sludge), coagulated concentrated sludge (returned sludge), and coagulated concentrated sludge of treated sludge.

The SS concentration of the fine particles added to the injected water or the mixed liquid 41 is preferably 1 × 10 ³ ppm or more. The fine particles added to the injection water or the mixed solution have a particle diameter of 1 × 1.
It is 0 ^{−4 to} 0.5 mm. Desirably 1 × 10 ⁻³
0.1 mm is suitable. The specific gravity of the fine particles is higher than 1, and it does not differ much from the specific gravity of the pollutant, and may be inexpensive. When the treated water is used as tap water, it is desirable that the electrolyte hardly elutes in the fine particles added to the injected water or the mixed solution. When it comes to removing marine pollutants, it is desirable that the electrolytes have no impact on the ecosystem. Generally, fine particles are diatomaceous earth, (acidic) clay, bentonite, shirasu, coke powder, anthracite powder, coal powder, lignite powder, charcoal powder,
Cristobal stone powder, feldspar powder, talc, kaolin, clay, zeolite powder, quartz powder, foamed rock powder, ceramic raw material powder, slag powder, fiber powder, circulation of coagulated concentrated sludge 14 in activated sludge or treated polluted liquid It can be reused.

The structure of the flocculating and concentrating device of the present invention will be described with reference to the explanatory view shown in FIG.
In the aggregating device consisting of the solid-liquid separation chamber 10 provided with the floc forming tank 7, the number of mixing tubes is one or more (one in FIG. 1) depending on the amount of treatment liquid. An injection pipe 19 for injecting the injection liquid 16 is provided in the mixing pipe 17. One injection tube is provided for each mixing tube. (In FIG. 1, one injection pipe is provided for each mixing pipe.) The discharge port of the injection pipe (injection liquid) is directed in the downstream direction of the contaminated liquid flowing in the mixing pipe. Injected water 2 and / or polluted liquid 16 and / or agglomerated condensed sludge 14 and / or fine particles 6 are injected into an injecting pipe 19 into an injecting liquid stirring tank 3
It is supplied as the injecting liquid 16 from the injecting liquid supply pump 35 while being adjusted in 6. When the polluted liquid 1 is thick, it is supplied to the dispersion chamber 18 and the distribution chamber 30. Further, in order to increase the concentration of the floc-containing liquid, as an example, the mixed liquid 41 obtained by adding the coagulated concentrated sludge to the polluted liquid 1 may be supplied to the dispersion chamber 18 and the polluted liquid 1 to the distribution chamber. When the polluted liquid 1 is thin, the coagulated concentrated sludge 14 and / or the primary mixing tank 4 is added with the injected water 2 and the fine particles 6 and stirred, and the slurry pump 3 supplies it to the stirring and mixing tank 5 to supply the polluted liquid supply pump 15 The mixed liquid 41 is supplied to the dispersion chamber 18 and the distribution chamber 30 from. Further, as an example, the mixed liquid 41 may be supplied to the dispersion chamber and the flocculated concentrated sludge 14 and the contaminated liquid may be supplied to the distribution chamber. The supplied mixed liquid 41 overflows from the upper edge of the mixing pipe in the dispersion chamber and is supplied to the mixing pipe, and the contaminated liquid 1 is supplied to the distribution chamber 30 and overflows from the upper edge of the increasing liquid supply pipe in the distribution chamber. It is supplied to the increasing liquid supply pipe. Contaminant supply pump 1 when the contaminated solution supplied to the distribution chamber is diluted 1
The concentration of the contaminated liquid may be corrected by supplying a mixed liquid 41 having a concentration higher than 5. One end of the distribution chamber 30 and the flock forming tank communicate with the distribution chamber, and the other end communicates with the flock forming tank 7 by a volume increasing liquid supply pipe 33 having an opening (a volume increasing pipe discharge port 32). Flock-containing liquid 28 formed by laminar contact between the injection liquid discharged from the injection pipe discharge port and the contaminant flowing in the mixing pipe 28
Is discharged from the mixing pipe discharge port 8. A plurality of mixing pipes are arranged in the increasing pipe 31 (circular pipe or square pipe) (one mixing pipe is provided in FIG. 1), and the floc-containing liquid 28 discharged from the mixing pipe discharge port 8 and the increasing amount From pipe annular part 37 to increasing pipe 31
And the flow-increasing pipe contaminant 34 flowing into the cylinder collide with each other to form a floc. There is an electrolyte concentration difference of 1 ppm or more between the two liquids containing the floc-containing liquid and the expansion pipe pollutant. In addition, if the collision system shown in FIG. 30 to 150 times is possible. A flock forming tank 7 is provided in the solid-liquid separation chamber 10 of this apparatus, and the above-mentioned increasing pipe discharge port is provided so as to be located in the flock forming tank.

The structure of the flocculating and concentrating device will be described with reference to the explanatory view shown in FIG. 2. In the flocculating device comprising the dispersion chamber 18, the distribution chamber 30, and the floc forming tank 7 provided in the solid-liquid separation chamber 10, a mixing pipe is provided. An injection pipe 19 is provided in the injection pipe 17, and the injection water 2 and / or the contaminated liquid and / or the condensed concentrated sludge and / or the fine particles and / or the injection liquid to which the fine particles are added are supplied to the injection pipe 19 as the injection liquid 16. To be done. The outlet of the injection pipe faces the downstream direction of the contaminated liquid flowing in the mixing pipe. The discharge port 8 of the mixing tube is provided so as to be located in the floc forming tank. The dispersion chamber 18 and the flock forming tank 7 communicate with each other through a mixing pipe 17 having one end open to the dispersion chamber and the other end opening to the flock forming tank. One to a plurality of mixing tubes are provided depending on the amount of processing liquid. The mixed liquid 41 supplied to the dispersion chamber is the polluted liquid 1 and / or the condensed concentrated sludge 1
4 or the contaminated liquid and the condensed concentrated sludge are diluted, the fine particles 6 are added to the respective liquids, and one end of the distribution chamber 30 and the floc formation tank is the distribution chamber and the other end is the bottom of the floc formation tank. A plurality of metering pipe discharge ports 32 are opened and communicated with a metering liquid supply pipe 33. The polluted liquid 1 supplied to the distribution chamber overflows from the upper edge of the volume increasing liquid supply pipe 33 and is supplied to the volume increasing liquid supply pipe. The position of the outlet of the increasing pipe was provided at a position separated from the bottom of the tank by 1 to 10 times the diameter of the mixing pipe. The position of the discharge port of the mixing tube is located at a distance of 1.5 to 15 times the length of the diameter of the mixing tube from the bottom of the flock forming tank. It seems that unaggregated fine particles that did not form flocs in the companion mixing pipe in which the position of the mixing pipe discharge port is more than 15 times the diameter of the mixing pipe from the bottom of the floc forming tank do not decrease and the collision effect is small. The cross-sectional area of the bottom 26 of the collision mixing section 20 in the flock forming tank has an area of 5 to 400 times the total area of the mixing pipe discharge port, and from the bottom to a position (distance) about 10 times the diameter of the mixing pipe, Area where unaggregated fine particles form small flocs (collision mixing section 2
Although it is 0), there is a wide space in which the floc-containing liquid discharged from the discharge port of the mixing pipe and the polluted liquid discharged from the increase liquid supply pipe collide with each other, and a collision system diagram for enhancing the collision in the single pipe of the increase pipe. As compared with FIG. 1 in which −12 is mounted, small flocs and medium flocs without fine particles cannot be formed, and the aggregation performance of FIG. 2 is low.

In the flocculating and concentrating apparatus of the present invention (FIGS. 1 and 2), a floc forming tank is provided in the solid-liquid separation chamber, and the mixing pipe discharge port or the expansion pipe discharge port 32 is located in the floc forming tank. The present invention is characterized in that the flocculated flocs are concentrated in the solid-liquid separation chamber and used as a floc concentration chamber in which the solid-liquid separation chamber is formed. The supernatant liquid 11 is discharged from the uppermost part of the solid-liquid separation chamber.

In FIGS. 1 and 2, a fluidized bed section 21 is provided above the collision mixing section 20 of the flock forming tank, and the horizontal cross-sectional area of the flock forming tank increases as the height rises along the axis of the mixing tube. The height of the fluidized bed portion 21 is 7 to 20 times as large as the diameter of the mixing tube from the bottom of the vessel. In the fluidized bed portion 21, violent collisions are repeated between medium and small flocs to form large flocs. It is difficult to form large flocs unless the fine particles discharged from the discharge port of the mixing tube up to this region form small flocs. The decisive difference in performance between Fig. 1 and Fig. 2 is that Fig. 2 does not collide small flocs of the floc-containing liquid with fine particles of the contaminated liquid of the extender pipe in a floc formation tank that is 10 times wider than the inside of the extender pipe. On the other hand, in Fig. 1, it is considered that the collision system is mounted in the increasing pipe and also in the pipe having a reduced diameter to repeat collision, aggregation, concentration and mixing.

The large locks form a huge floc at the uppermost moving layer portion 22 of the floc formation tank by gentle collision between the large flocs. The tank height of the moving bed section is set to a range of 3 to 15 times the mixing tube diameter above the fluidized bed section. The giant flocs overflow from the overflow weir, slide down the inclined plate, and fall into the coagulated concentrated sludge layer of the solid-liquid separation chamber. The horizontal cross-sectional area surrounding the overflow weir is 10 to 40,000 times the total area of the mixing pipe discharge port because the supply amount of the increasing pipe contaminant increases.

In the coagulating and concentrating apparatus of the present invention, the distance between the side wall 25 of the floc forming tank and the inclined plate 23 becomes larger as the scale and performance are improved. Horizontal cross-sectional area surrounded by the flock forming tank overflow weir and the sloping plate formed by cutting along the horizontal plane surrounded by the upper edge of the flock forming tank uppermost overflow weir 9 (Fig. 9-B).
Is the area surrounded by the overflow weir of the floc formation tank (Fig. 9-
It is better to keep it at 120 to 5% of A). When cut along the horizontal plane of the bottom plate 26 of the flock forming tank, the outer circumference of the tank bottom and the inclined plate 2
The horizontal cross-sectional area (Fig. 9-D) surrounded by 3 is 100 to 5 of the area (Fig. 9-A) surrounded by the overflow weir 9 of the flock formation tank.
%, And the area in FIG. 9-D is distributed to the area where the outer circumference of the tank bottom and the inclined plate are evenly spaced. The coagulated sludge overflowing from the overflow weir is slid down between the side wall 25 of the flocculation tank and the inclined plate, and is transferred and accumulated in the coagulated concentrated sludge at the bottom of the solid-liquid separation chamber 10. In the solid-liquid separation chamber of the apparatus of the present invention, the sludge discharged from the discharge port of the increasing pipe provided with the collision system has no disturbance and concentrated sludge can be obtained in an extremely short time. If a collision system is installed in the floc formation tank and the expansion pipe, the concentration of activated sludge will be 20 kg / m even if a high concentration liquid of about 10 kg / m ³ is treated.
Highly concentrated sludge of around ³ can be obtained. The solid-liquid separation chamber 10
At the bottom of the chamber, a filter 13 is installed at the flocculation tank discharge port 24 for taking out flocculated sludge (sludge) for disposal. If necessary, flocculated sludge (sludge) is returned to the stirring and mixing tank 5 by the circulation pump 12 and mixed with the contaminated liquid,
Alternatively, it is returned to the injection liquid stirring tank 36 and is used in the present flocculating and concentrating device.

The flock forming tank 7 has a shape of cylinder, square tube,
It is a truncated cone shape or a truncated pyramid shape, and they are joined up and down, and the one with the larger horizontal cross-sectional area opens up. 26
There is.

The frusto-conical flock forming tank shown in FIG.
A container having a large circle diameter (R) and a small circle diameter (r) as the tank bottom, and the upper opening edge and the bottom edge of the tank bottom surrounded by side walls. The uppermost edge (overflow weir 9) of the side wall of the flock forming tank is kept horizontal, and the uppermost edge of the inclined plate 23 is higher than that of the flock forming tank. The mixing pipe discharge port 8 is opened to each of the two increasing pipes, and the increasing pipe discharge ports of the two increasing pipes are opened to the collision mixing section 20 toward the tank bottom.

FIG. 4 shows a pyramid-shaped flock forming tank in which the truncated pyramidal bottom surface and the opening surface are square, rectangular, and 5 to polygonal pyramid shapes, and the truncated opening surface and the tank bottom surface are square. The truncated pyramid is a container in which a large square opens upward, the small square serves as the tank bottom, and the upper opening edge and the bottom edge of the tank bottom are surrounded by side walls. The uppermost edge of the side wall of the flock forming tank is horizontal and serves as an overflow weir, and the uppermost edge of the inclined plate 23 is higher than that of the flock forming tank. It is provided on the outside of a truncated pyramid-shaped side wall that opens vertically with a space between the inclined plate 23 and the pyramid side wall of the flock forming tank. The mixing pipe discharge port is open to one increasing pipe, and one increasing pipe discharge port is opened toward the bottom of the tank.

The present invention has been described with reference to a vertical apparatus in which a dispersion chamber 18 and a solid-liquid separation chamber 10 are vertically connected by a mixing pipe 17 as shown in FIG. 1, but Japanese Patent Application No. 63-15562.
Also in the horizontal agglomerating device in which the mixing tube is horizontal or inclined as described in No. 4, the mixing tube and the injection tube have a distance from the injection tube discharge port to the mixing tube discharge port as shown in FIG. After that, the mixing pipe is bent from a vertical direction to a horizontal plane in a direction of 20 degrees with respect to the horizontal plane, its discharge port is opened to the collision mixing section 20 in the floc forming tank, and the extended liquid supply pipe 33 is connected to the collision mixing section 20. By opening it, 5 times the amount of the contaminated liquid of the increasing pipe can be flowed with respect to 1 of the floc-containing liquid. If the impact mixing section is replaced with an extender pipe of the impact system, and the impact plates are arranged and a static mixer is used, it is possible to further increase the contaminated liquid of the extender pipe several times. In a horizontal flocculating device in which the pipe axes of the injection pipe, the mixing pipe, and the bulking liquid supply pipe are united, the flocs of the floc-containing liquid flow down from the mixing pipe discharge port to the bottom of the bulking pipe as a layered accumulation flow, while the bulking pipe Even if the contaminated liquid flows into the single tube of the volume increasing pipe, it does not collide with the small flocs of the floc-containing liquid and flows over the sediment flow, and if only the vertical bend vortex flow and the flocculation tank collide, the small flocs can be Since the collision with the fine particles of the metering pipe polluted liquid is insufficient, the coagulation performance is further improved several times when the collision system Fig. 12 is installed in the single tube part of the metering pipe.

As an embodiment of the flock forming tank of the present invention, in addition to this, as shown in FIG. 6, the lowermost cylindrical portion of the cylindrical flock forming tank in which large and small cylindrical shapes are combined by an expansion pipe 27 is a collision mixing section. is there. The floc-containing liquid that is supplied by opening the mixing pipe discharge port to the collision mixing part collides with the increasing pipe polluted liquid that is supplied from the increasing liquid supply pipe 33 from the increasing pipe discharge port 32 that opens to the side wall of the cylindrical portion of the collision mixing part. It is arranged to do.

FIG. 7 shows a structure in which a discharge port 29 is provided in the fluidized bed portion of the floc forming tank, and a discharge port of the increasing pipe is opened to the collision mixing section in the flock forming tank to treat a contaminated liquid containing coarse particles. Then, when it is difficult for the coarse particles to be discharged from the overflow weir, the discharge port 29 is provided.

As shown in FIG. 8, the flock forming tank has a structure in which a truncated cone shape having a bottom and a truncated pyramid shape are combined.

FIG. 9 shows an arrangement in which a huge floc descends from the overflow weir 9 of the flock forming tank to the inclined plate 23 and slides down the inclined plate to determine the distance between the side wall and the inclined plate required to reach the concentration tank. The larger the processing amount, the wider.

FIG. 10 shows a situation in which three collision mixing plates 42 are mounted in the metering pipe, and the floc-containing liquid and the contaminated liquid of the metering pipe flow by collision mixing, and are fixed to the wall of the metering pipe by the fixing band 43. Suitable for mounting on a horizontal type expansion tube.

FIG. 11 shows an example of a static mixer in which the cutting surfaces of the mixing blades 44 are mounted so that vertical and horizontal sections are alternately crossed with the tube axis as an intersection, and the liquid flow is first
A static mixer is shown in which the second blade is divided into 1/2 and stirred, the second blade is divided into 1/4 and stirred, and the third blade is divided into 1/8 and stirred. The small flocs of the floc-containing liquid are uniformly mixed with the extender tube contaminated liquid, and the small flocs are grown to form medium flocs having the same particle diameter. Suitable for mounting on a vertical type expansion tube.

FIG. 12 shows an example of the collision system. In the horizontal agglomerator, the pipe axes of the injection pipe, the mixing pipe, and the bulking liquid supply pipe are united laterally, and small flocs of the liquid containing flocs flow down from the mixing pipe discharge day 8 as a layered deposition flow to the bottom of the bulking pipe. On the other hand, the fine particles of the metering pipe polluted liquid flow over the sediment flow without colliding with the small flocs of the floc-containing liquid in the metering pipe, so that the aggregation performance is low. Mixing pipe discharge port in the increasing pipe The liquid containing flock and the large amount of increasing pipe contaminated liquid flowing out from the bottom of the pipe are blocked by the first nozzle, and the inside of the pipe is filled upstream, and the sludge pushed out from the first nozzle port is Immediately after that, the diameter of the increasing pipe becomes thin (the diameter of the expanding pipe does not have to be thin), and the mixing blade 44
With a static mixer equipped with three sheets and a second nozzle provided immediately after the mixer, the inside of the mixer is filled with sludge, and the filled fine particles (bulk pipe contaminated liquid) and small flocs (fluc-containing liquid) The sludge from the second nozzle port to the third nozzle day provided at the discharge port of the increasing pipe is homogeneously stirred and mixed, and the sludge is compressed by the pressure of the tank height where huge flocs are accumulated in the floc formation tank, The inter-particle distance is further narrowed by the compression by the nozzle port, and while growing into medium flocs, it is sent to the floc forming tank as medium flocs by the nozzle of the discharge pipe discharge port. The amount of the floc-containing liquid of 1 is improved several times as much as the amount of the pollutant of the increasing pipe before the collision system is installed.

FIG. 13 shows an example of a static mixer. An annular plate is arranged on the wall surface of a circular pipe, and a disk is arranged alternately on the pipe axis perpendicularly to the pipe axis.

FIG. 14 shows that the liquid flows from a large mouth of a nozzle (funnel) type to a small mouth, a disk is arranged in front of the small mouth, and the central axis of the nozzle (funnel) and the disk are united with the tube axis. They are arranged alternately.

Even if the dilute pollutant and the injection liquid are in laminar contact, the flocs formed are small, and even if the floc-containing liquid and the dilute pollutant collide with each other in the increasing pipe or the floc forming tank, the collision effect is small. , The interparticle distance between the flocs and the fine particles is narrow, and it cannot be expected to improve the solid-liquid separation performance. In order to increase the supply amount of the volume increasing pipe contaminant, fine particles are added to the injection liquid and the mixing pipe, and the high concentration injection liquid and the thickened contamination liquid are brought into laminar contact in the mixing pipe to adjust the concentration of the floc-containing liquid. By increasing the electrolyte concentration difference between the floc-containing liquid and the expansion pipe pollutant to 1 ppm or more, and equipping the expansion pipe with a collision system Figure-12, even if a dilute expansion pipe pollutant is supplied, fine particles of flocs and pollutants will be generated. The inter-particle distance between particles becomes narrower, and the ability to form flocs with a small amount of fine particles increases,
The supply amount of the dilute amount-increasing pipe contaminant liquid before mounting the collision system to the floc-containing liquid 1 can be increased from 1.5 to 10 times to several times or more to wait 5 to 150 times.

The injection liquid stirring tank 36 for mixing fine particles having a low solute content with the diluted injection water or the diluted polluted liquid, the primary mixing tank 4 and the stirring / mixing tank 5 also discharge a large amount of flocs from the solid-liquid separation device. A circulation system including a circulation pump 12 for returning the coagulated concentrated sludge to a diluted polluted liquid for circulation is required. If fine particles are added to the diluted injection liquid to make a laminar flow contact with the diluted pollutant to increase the concentration of the floc-containing liquid and form a condensed concentrated sludge, an extra condensed concentrated sludge is sequentially added to the diluted contaminated liquid by a circulation pump. Then, as the concentration of the floc-containing liquid in the mixing pipe gradually increases by supplying the mixed liquid to the dispersion chamber 18, the effect of collision between the dilute pollutant liquid and the increasing pipe or the floc forming tank is improved, and the solid-liquid separation performance is also improved. It is possible to improve and increase the supply amount of the expansion pipe pollutant. The SS concentration of the dilute pollutant is 50 ppm or less, and when used as water after SS removal or as clean water, purified diatomaceous earth 5 × 10 ³ pp
By adding m or more to the injection liquid and adding the flocculated concentrated sludge at the bottom of the solid-liquid separation chamber to the suspension liquid and supplying it to the dispersion chamber as a mixed liquid, the concentration of the floc-containing liquid gradually increases and the solid-liquid separation performance improves. It is possible to increase the supply amount of the contaminated liquid.

[0045]

Example 1 Using the coagulation-concentration apparatus of the present invention shown in FIG. 2, river water (diluted pollutant 1 in FIG. 2) SS concentration 18-
An example of processing 25 ppm (Ca ++ 6.8 ppm) is shown. Mixing pipe (diameter 4 cm, pipe length 3 m) and injection pipe (diameter 2 c
m pipe length 2.7 m) and the pipe axes are united to install so that the mixing pipe annular portion is 2.5 m, and the mixing pipe single pipe portion is 0.5 m,
The mixing pipe opens to the upper dispersion chamber, and the discharge port of the mixing pipe opens to a position 30 cm from the bottom of the flock forming tank. The discharge port of the volume increasing liquid supply pipe that opens into the distribution chamber is located 6 cm above the bottom of the flock forming tank and has a diameter of 7.5 cm at two opposite side walls of the flock forming tank. The increasing-tube contaminated liquid supplied to the floc formation tank collides and aggregates in the floc formation tank. The flock forming tank has a bottom area of 230 times the mixing pipe discharge area and a horizontal area of 2000 times for the overflow weir, and the position of the inclined plate is the area surrounded by the inclined plate and the overflow weir. The width is 27% of the enclosed area (S), and the position of the lower inclined plate is 16% of the area (S) enclosed by the outer periphery of the bottom of the flock forming tank and the inclined plate. 5 × 10 ³ ppm of concentrated pollutant obtained by adding fine particles 6 (purified diatomaceous earth cake) to 1 m ³ of dilute pollutant in the agitation mixing tank 5 and distributing chamber 30 and dispersion chamber 18 with pollutant feed pump 15 Supplied to.
Thick polluted liquid 0 m ^{3 /} hr (A) (B), 1.7 m ^{3 /} h
^{r (C), 2.1m 3 /hr(D),1.6m} 3 / hr
(E) 1.8 m ³ / hr (F) was supplied from the distribution chamber 30 to the bottom of the flock forming tank as a thickening pipe contaminant. To the mixing pipe, 0.14 m ³ / hr (A) to (D) of dilute polluted liquid was supplied from the dispersion chamber 18, and 0.14 m ³ / hr of concentrated polluted liquid was supplied.
(E) to (F) were supplied from the dispersion chamber 18 to the mixing tube. On the other hand, the injected water (reference numeral 2 in Fig. 2) is (Λ) (E)
In the case of (F), it is used as the injection liquid 16 as it is, and 20 l /
Each hr was supplied to the injection pipe 19. On the other hand, in the case of (B), (C) and (D), the injection liquid 16 was prepared by mixing 1 m ³ of injected water (tap water) with 100 Kg of fine particles (purified diatomaceous earth cake average capillary diameter 0.8 × 10 ⁻³ mm). 20 l / hr each
Was supplied to the injection tube.

The flow of the injection liquid and the flow of the contaminated liquid flowing down in the mixing pipe 17 are in laminar contact, and at the interface (A).
In (E) and (F), there is a difference in electric potential between the fine particles in contact with the injecting liquid and the fine particles in the polluted liquid.
In (F), the interparticle distance was predicted to be 1 × 10 ⁻⁵ mm or less, and aggregation occurred between the particles to form flocs,
In (A), flock formation was impossible. Also (B)
In (C) and (D), there is a difference in the electric potential between the fine particles added to the injected water and the fine particles in the mixing tube polluted liquid due to the difference in the electrolyte concentration of the two liquids, and instantaneously between the particles in the mixing tube. Aggregation occurred and flocs were formed. The floc-containing liquid discharged from the mixing pipe discharge port and the increasing pipe polluted liquid collide with each other in the floc-forming tank and coagulate to form huge flocs, which are separated in the solid-liquid separation chamber. Table 1 shows the SS concentration of the supernatant 11 and the SS concentration at the outlet of the bottom circulation pump 12 of the solid-liquid separation chamber.

[0047]

[Table 1]

From these results, (B), (C) and (D) are the cases where the injection liquid containing fine particles and the dilute contaminated liquid are in laminar flow contact, and (E) and (F) are the concentrated contaminated liquid supplied to the mixing pipe. The flocculating and concentrating device of the present invention in which the amount of the contaminated liquid supplied from the increasing pipe is greatly increased with respect to the floc-containing liquid obtained by directly using
Clearly, compared with the conventional aggregating device, the coagulating and concentrating function of fine particles in the polluted liquid did not deteriorate, and the mixing pipe processing capacity was significantly improved. Although the flocculation performance was better when added to the injection liquid of (C) than that of (E), the concentration of the floc-containing liquid of (C) of 12.5 g / l was 4.4 g / l of (E). From 2.
Because it is 9 times higher.

[0048]

[Embodiment 2] In the flocculating and concentrating apparatus of the present invention shown in FIG. 1, the mixing pipe annular portion 2 is formed by uniting the pipe axes of the mixing pipe (diameter 4 cm, pipe length 3 m) and the injection pipe (diameter 2 cm, pipe length 2.7 m). .5
The mixing tube has a structure in which it is installed so that the mixing tube has a single tube portion of 0.5 m, and the mixing tube is opened to the upper dispersion chamber. The mixing pipe is integrated with the pipe axis of the increasing pipe (diameter 12.5 cm, pipe length 4 m), the mixing pipe discharge port 8 is opened in the increasing pipe, and the increasing pipe discharge port 32 is opened 1 m ahead to form a flock. 2 from the bottom of the layer
There is an opening at a position 0 cm above. On the other hand, the expansion pipe is open to the upper distribution chamber. The area surrounding the overflow weir of the floc formation tank is 700 times the area of the mixing pipe discharge port (0.88
m ² ) 1.06 m in diameter, the area of the bottom of the tank is 70 times the area of the outlet of the mixing pipe (0.088 m ² ) 0.33 m in diameter, and the height of the tank is frustoconical side wall and overflows. An inclined plate is provided at an outer periphery of the weir with an interval of 15 cm and an outer periphery of the tank bottom is provided with an interval of 20 cm, and is fixed to the bottom of the solid-liquid separation chamber having a water depth of 5.6 m. Using this device, SS concentration 640
0 ppm of washed rice water (Ca ++ concentration 6.8 ppm) was supplied from the stirring and mixing tank 5 to the dispersion chamber 18 by using the supply pump 15, and continuously supplied from the same chamber to the mixing pipe at a rate of 0.14 m ³ / hr. (Λ) ground water (water for brewing Ca ++ concentration 1.1 ppm) 15 l / hr, (B) injection liquid (ground water)
20 l / hr, fine powder of rice aggregated as fine particles into ground water was added to adjust to 1.2 × 10 ⁵ ppm (C).
Injection liquid is 20 l / hr, (D) (E) injection liquid 60 l / h
r was continuously supplied to the injection tube, and then was supplied into the mixing tube of the flocculation concentrating device of FIG. Rice rinsing drainage 0m ³ / hr (A), Rice rinsing drainage 2.0m ³ / hr (B) Rice rinsing drainage 2.8m ³ / hr
(C), washed rice effluent 8.3 m ³ / hr (D), and washed rice effluent 8.8 m ³ / hr (E) are supplied to the increasing pipe through the increasing liquid supply pipe, and each is subjected to a collision coagulation treatment in the increasing pipe ( B) ~
The same floc forming tank as in (E) and the floc forming tank in which (A) in which the supply of the rice rinsing wastewater to the distribution chamber was stopped was treated by the aggregating device were used.

In the flocculating and concentrating apparatus shown in FIG. 1, when the flocculating liquid of the injecting liquid and the mixing pipe contaminated liquid is coagulated in the floc forming tank (Λ), the mixed liquid of the floc containing liquid and the increasing pipe contaminated liquid is When the flocculation treatment is carried out in the volume increasing pipe and in the floc forming tank (B) and (C), the mixed solution of the floc-containing liquid formed by the injection liquid containing the fine particles and the flow increasing pipe contaminated liquid is added in the volume increasing pipe and the flock forming tank. At the time of coagulation treatment (D) and (E), the sludge plate 23 is slid down over the overflow weir, and the concentrated sludge accumulated on the bottom of the solid-liquid separation chamber is discharged to the SS concentration of the circulation pump 12 and the solid-liquid separation chamber. Table 2 shows the SS concentration of the supernatant 11 of the above.

[0050]

[Table 2]

From these results, it is found that the concentration of the floc-containing liquid (D), in which the injection liquid added with the fine particles and the contaminated liquid are in contact with each other in a laminar flow, is as high as 40.5 g / l. The method of the present invention in which the floc-containing liquid and the polluted liquid collide and agglomerate in the increasing pipe at a high concentration, the water quality, the treatment amount (increase pipe contaminated liquid amount / flock-containing liquid amount = 41.5 times, increasing pipe contaminated liquid SS / The floc-containing solution SS = 6.4) is also satisfactory.

[0052]

Example 3 Using the coagulation concentrating device of the present invention in FIG. 1, the circular tubes were replaced by square tubes for the mixing tube and the expanding tube, and the river water (dilute polluted liquid) SS concentration in rainy weather was 238 to 375 ppm (C
a ++ 2.1 ppm) is an example of using seawater as an injecting liquid. Mixing tube (1 side 4 cm square tube, tube length 3 m), injection tube (diameter 2 cm tube length 2.7 m) and tube axis are combined so that mixing tube ring part 2.5 m, mixing tube single tube part 0.5 m. The mixing tube is attached to the mixing tube, the mixing tube opens in the upper dispersion chamber, the mixing tube and the metering tube (12 cm on a side, square tube length 4 m) are united, and the mixing tube discharge port opens in the metering tube. However, the discharge port of the metering pipe opens 1 m ahead of the mixing pipe discharge port, the metering pipe discharge port opens 30 cm from the bottom of the flock forming tank, while the metering pipe opens in the upper distribution chamber. ing. The same floc forming tank as in Example 2 is used. The diluted contaminated liquid was supplied to the distribution chamber and the dispersion chamber by the contaminated liquid supply pump 15. 0 m ³ / hr (A) to distribution tube from distribution chamber
^{(D), 1.1m 3 /hr(E),1.7m 3} / hr
(F) Supply the diluted pollutant 0.14 from the dispersion chamber to the mixing tube.
m ³ / hr (A) to (F) were supplied. Tap water or seawater is used as injection water, and tap water is (Λ) 15 l / hr,
Seawater supplied to (B) 15 l / hr to the injection pipe,
An injection liquid of 15 l / hr in which m ³ was mixed with fine particles (diatomaceous earth cake average capillary diameter 9.5 microns) at a ratio of 50 Kg (C) and 100 Kg (D) (E) (F) was supplied to the injection pipe. Table 3 shows the SS concentration of the supernatant 11 of the solid-liquid separation chamber and the SS concentration of the concentrated sludge at the outlet of the circulation pump 12.

[0053]

[Table 3]

From these results, (B) in Table 3 in which sea water (high electrolyte concentration) was used as the injected water had higher aggregation performance than (A). The river water polluted liquid supply amount was 7 times (E) with respect to the floc-containing liquid amount of 1 and there was no winding phenomenon, and 11 times (F) was with the winding phenomenon. Laminar contact was made between a dilute pollutant of river water and an injecting solution containing diatomaceous earth having a fine particle average capillary diameter 10 times larger (9.5 micron of Example 3 / 0.8 micron of Example 1). It is considered that, since the number of flocs of the formed floc-containing liquid is not much different from that in Example 1, there is no difference in the collision aggregation performance in the increasing pipe and the floc forming tank. It is not recognized that there was a difference in the coagulation performance regardless of whether a circular tube or a square tube was used as the mixing tube.

[0055]

[Embodiment 4] The same apparatus is used for the flocculation apparatus and the floc formation tank of Example 2. The extender tube was equipped with the collision system of Figure-12. Opening ratio 1/3 at 3 cm downstream of mixing pipe outlet
Nozzle opened to the inside of the metering tube, and 5 mixing vanes were placed 6 cm downstream of the mixing tube discharge port in the metering tube that narrowed the diameter of the metering tube annular part from 12.5 cm to 10 cm of the metering tube single tube part. Five nozzles were arranged, a nozzle opening having an opening ratio of 1/2 was provided at the outlet 5 cm of the fifth mixing blade, and a nozzle having an opening ratio of 1/2 was provided at the outlet of the increasing tube. Dredging (25 years later) sludge in the reclaimed land (1 in Fig. 1 of polluted liquid) S with tap water
S concentration 810-1200ppm (Solute Ca ++ 0.2p
pm) 1000 ppm on average from the distribution chamber to the volume increasing pipe with a pollutant supply pump, 1 m ³ / hr = SS1 Kg / hr (A),
3m ³ / hr = SS3Kg / hr (B), 5m ³ / hr
^{= SS5Kg / hr (C),} 7m 3 / hr = SS7Kg
/ Hr (D) is supplied. 3. As for the injecting solution, 2 kg of fine particle diatom cake (average capillary tube diameter: 0.8 micron) was added to 100 l of seawater and 100 l of tap water, respectively, to the injecting solution stirring tank 36, and the mixture was stirred into the injecting tube by the injecting solution supply pump 35 (seawater). 5
l / hr (Λ) (B) (C) (D) and (tap water) 4.5
l / hr (E) (F) is supplied. The coagulated concentrated sludge 14 at the bottom of the solid-liquid separation chamber is fed from the circulation pump 12 to the injection liquid stirring tank 3
Return to No. 6 and supply to the injection tube as an injection liquid. Diluted liquid 45l / hr (A) (B) (C) (D) into the mixing tube
(E) and (F) were supplied from the dispersion chamber 18 to the mixing tube.

The flow of the injection liquid (seawater) and the contaminated liquid in the mixing pipe 17 make laminar contact to form flocs, and there is a large difference in the potential based on the difference in the electrolyte concentrations of the two liquids, and the flocs are formed. . The SS concentration of the floc-containing liquid is 2,727
ppm, the weight of SS supplied for 1 hour is 5 Kg / hr. Table 4 shows the SS concentration of the supernatant 11 of the solid-liquid separation chamber, and the ratio of the weight of the increasing pipe polluted liquid SS to the weight of the floc-containing liquid.

[0057]

[Table 4]

As a result, since seawater and tap water were used as the injection liquid, the electrolyte concentration of the floc-containing liquid had a difference of Na + 100 ppm (C) or more with the electrolyte concentration of the dredging sludge liquid, but (C ) It is possible to supply 37 times the weight of the flocculating liquid SS with respect to the weight of the floc-containing liquid SS 1. (E)
(F) The electrolyte concentration difference between the injectate and the mixture is Ca ++ 0.2.
ppm (Na + conversion 12 ppm) The difference in electrolyte concentration between the small flocs of the formed floc-containing liquid and the contaminated liquid of the increasing pipe is Ca
The formation of ++ 002 ppm (Na + conversion of 1 ppm) flocs is recognized, but small flocs have not yet grown by colliding with fine particles. The difference in electrolyte concentration between the floc-containing liquid and the contaminated liquid of the expanding pipe must be 1 ppm, and 5 ppm or more is desirable for the growth of small flocs. Controlled by the difference in specific gravity between fine particles, the particle size, and the difference in electrolyte concentration between liquids, the amount of the contaminated liquid in the increasing pipe of (C) reaches about 80 times the volume of the floc-containing liquid (1). The collision system installed in the metering pipe has a large electrolyte concentration difference of 100 ppm or more between the small flocs of the floc-containing liquid and the fine particles of the contaminated liquid of the metering pipe. It is thought that the flocs grow into medium flocs without fine particles and are supplied to the floc formation tank.

[0059]

[Embodiment 5] The same device as that of Embodiment 2 is used, and a drawing is made on the extending pipe.
Twelve collision systems were fitted. Downstream of mixing pipe outlet 3
A nozzle having an opening ratio of 1/3 to 1 cm is provided in the metering tube, and 5 mixing blades are provided downstream of the mixing tube discharge port in the metering tube which is thinned from the diameter of the metering tube annular portion of 12.5 cm to the metering tube single tube diameter of 10 cm. Five nozzles were arranged from 6 cm as shown in FIG. 11, a nozzle opening having an opening ratio of 1/2 was provided at the outlet 5 cm of the fifth mixing blade, and a nozzle having an opening ratio of 12 was provided at the discharge port of the increasing tube. Washing waste water (Ca ++ concentration 6.
6 ppm) to 6400 ppm, and a mixed solution of 0.
03m ³ / hr (A) (B) (C) with 3 as injection liquid
L / hr (D) (E) was continuously supplied, and fine powder of rice washed and agglomerated with tap water was added to a liquid mixed with a ratio of tap water amount 5 to wash water amount 5 to adjust to 6 × 10 ⁴ ppm. The obtained liquid was continuously supplied to 0.03 m ³ / hr (D) (E) as a mixed liquid and 3 l / hr (Λ) (B) (C) as an injection liquid. Washing rice drainage 1m ^{3 /} hr (A), 1.5m ³
/ Hr (B), 3m ³ hr (C), 5m ³ / hr
Table 5 shows the results of supplying (D) and 6 m ³ / hr (E).

[0060]

[Table 5]

By providing a static mixer and a nozzle at the outlet of the metering pipe before and after the static mixer,
The distance between the particles was narrowed, and the impingement and mixing were effectively caused by the mixing blades. The concentration of the floc-containing liquid in (D) was 5 times higher than that in (B), and the difference in the floc-containing liquid concentration caused a difference in the aggregation performance. Think (D) Electrolyte concentration Ca of the expanding pipe polluted liquid
C + + of the floc-containing liquid of (D) against 6.6 ppm
a ++ is 3.3 ppm or less, and Ca + in the floc-containing liquid of (Λ) is 6.3 ppm in the electrolyte concentration difference (D) of 1
ppm or more is secured, but (A) is 0.3 ppm
Is 1 ppm or less. Limiting aggregation concentration Na +: Ca ++
= 1/1 / ⁶ : From the law of 1/2 ⁶ , Ca ++ is 1 of Na +
/ 64 ppm is sufficient. Therefore, the difference in electrolyte concentration is 1 ppm
The above is secured. In the present example, the amount of the (D) expanding pipe polluted liquid reached 150 times the amount of the floc-containing liquid of 1. On the other hand, in Example 2, the amount of liquid containing flock was 44 times.
Comparing this example with Example 2, (D) of Example 2
The floc-containing liquid concentration of (E) is 40.5 g / l,
(D) and (E) of Example 5 are not different from 55.1 g / l.
It is considered that the flocculation performance is greatly different because the concentrating and mixing function of the collision system of the present embodiment supplies medium flocs to the floc forming layer in which fine particles do not exist. If the floc-containing liquid in the initial stage of operation reaches the metering pipe from the nozzle port provided immediately before the mixing pipe discharge port, and if the metering pipe polluted liquid is supplied to the metering pipe, the phenomenon of rolling up of fine particles in the floc forming tank is observed. No, continuous operation is possible.

[0062]

[Sixth Embodiment] The same apparatus as in the fifth embodiment is used.
(A) (B) (C) (D) equipped with two collision systems
About (E) Activated sludge (treated sludge) SS6500pp
m (Ca ++ 6.3ppm) to 100l and 1kg of diatom cake (average capillary diameter 0.8micron specific gravity 2) to the injecting liquid stirring tank 36 and stirring, and 4.5l / hr (A) to the injecting pipe by the injecting liquid supply pump The activated sludge liquid SS (16.5 g / l (D) (E)) to which (B) (C) and the returned sludge filter are added is supplied to the injection pipe. Return sludge SS to mixing tube (10.5g
/ L) 100 l of tap water with stirring and mixing (C
a ++ 1.5 ppm) 45 m ³ / hr was fed from the dispersion chamber to the mixing tube. Activated sludge (m ³ / hr) 1 (A), 2
(B), 3 (C), 4 (D), 5 (E) were fed to the extender tube.

The electrolyte concentration difference between the injecting liquid and the mixed liquid was large, and flocs were formed. Floc containing liquid concentration 6.3g
/ L is the same as (A) to (E), the electrolyte concentration is Ca
++ 1 ppm or more. Table 6 shows the amount of activated sludge supplied (contamination liquid for increasing pipes) and the supernatant liquid.

[0064]

[Table 6]

From these results, (A), (B) and (C) to which diatomaceous earth having a high specific gravity is added have a worse aggregation performance than (D) and (E). This is because even if the concentration of the floc-containing liquid is the same, the number of small flocs in the floc-containing liquid is small. I think that there would be some difference in performance without the collision system.

[0066]

EFFECTS OF THE INVENTION The present invention exhibits the following effects because it exerts its performance in aggregation / separation / concentration without using a chemical as described above.

Since the present invention is a method of utilizing the electrolyte in the contaminated liquid as the coagulant without adding the coagulant, the contaminants and the clear liquid can be separated instantaneously while preventing environmental pollution and clear liquid contamination. Since it can be removed, there is no need for a transportation facility to the flocculation facility, and the clarified liquid can be discharged near the work site (coagulation removal of bottom mud and red tide from aquaculture fisheries, dredging, water purification plants, fish farms). Even if microbial growth and coagulation separation are repeated, chemical damage due to the accumulation of coagulant should not occur (activated sludge method). Filamentous bulking sludge and low sludge load sludge that cannot grow can be coagulated and settled 100%, so that stable operation can be performed for many years with zero generation of excess sludge (active sludge method).

When the injecting liquid and the contaminated liquid come into contact with each other in a laminar flow, they are instantly aggregated. Therefore, a chemical agent / reaction chamber for aggregation is unnecessary. Compared with conventional flocculation methods and equipment, it is possible to select fine particles with large flocs and high density, which can be reduced to 1/2 to 1/10 of the scale of sedimentation separation facility (thickener) when using conventional flocculants. Is excellent. A cleaning method for tap water in which tap liquor is added to tap water, a mixture of coagulated concentrated sludge is added to biologically treated water, and biologically treated water is supplied to an expanding pipe.

Fine particles with little elution or recovered fine particles are added to the dilute pollutant and / or injecting water to increase the pollutant concentration. If the electrolyte concentration difference is 1 ppm or more, flocculation and separation are likely to occur. (EN) A method and an apparatus for coagulating and concentrating, for example, recycling and reusing the supernatant as purified water. Specifically, in addition to the above, pulverized coal (coal, lignite, graphite, activated carbon, bone charcoal, a liquid containing carbon black (including lamp black, acetylene black), or separation from the waste liquid containing them, Recovery.

Separation from other sedimentable particles / sedimentable fine particles / microorganisms without contaminating oils and fats with blood and protein from the processing liquid of fish, birds and beasts and its meat processing liquid and its effluent, Recovery.

Industrial wastewater, urine and urine, sewage, and their biologically treated water, brewing waste liquid, brewing liquid, and concentration and separation / recovery of sedimentable fine particles / microorganisms of fermentation liquid.

Separation of sand and fine particles from dredging liquid, dredging bottom mud, accumulated sludge in dam reservoirs, etc. Separation of sand and fine particles from spring water containing sediment in the excavation site, contaminated water from revetment works and landfill sites, leachate from waste landfill sites, waste liquid from non-combustible building materials factories, etc.

Separation of fine particles and separation of supernatant liquid from tap water / industrial water sampling water, washing drainage from a filter basin of a water purification plant, sludge discharged from a high-speed coagulation sedimentation basin, sludge discharged from a chemical sedimentation basin, and the like.

Further, the present invention provides a method / apparatus capable of significantly increasing the amount of processing liquid per mixing tube. In the coagulating and concentrating device of the present invention, both the injection liquid and the mixed liquid are fine particle-containing liquids, and as the concentration of the floc-containing liquid increases due to laminar contact in the mixing pipe, the floc-containing liquid collides with the expansion pipe polluted liquid in the expansion pipe. Collision, aggregation, concentration and mixing are repeated in the system,
Alternatively, by forcibly colliding in the floc forming tank, the residual flocculation ability of the floc-containing liquid is large, unaggregated fine particles are eliminated, and the flocs become huge. The processing capacity per mixing tube is Japanese Patent Application No. 63-155624.
It is 5 to 200 times higher than that of the aggregating apparatus described in Japanese Patent Application No. 63-176579, and the equipment cost is greatly reduced. Moreover, even if the mixing pipe is horizontal and inclined, if a floc formation tank is provided, concentrated sludge can be obtained in a short time at a shallow water depth. If the water depth is 5 m in the dredging of sludge, 60 extension pipes with a diameter of 12.5 cm are placed in a water area of 1.5 m ² and treated at 10000 m ³ / day, the solid-liquid separation tank is 1/3 of the conventional one. The water quality of the supernatant liquid is uniform without SS and the maintenance is easy.

When a collision system is incorporated in the volume increasing pipe and the floc forming tank (precipitation tank), the effects of collision, coagulation, concentration and mixing are enhanced, and the distance between particles from the mixing pipe discharge port to the expansion pipe discharge port becomes narrow, Stable operation can be performed even if the concentrations of the injection liquid and the mixed liquid are constantly changed.

As the number of nozzles mounted in the metering tube increases, the small flocs of the floc-containing liquid and the fine particles are compressed immediately after the mixing tube discharge port, the interparticle distance becomes narrower, and the fine particles decrease and move in the metering tube. Therefore, full operation can be performed in a short time, and operation management becomes easy.

In mounting the collision system in the volume increasing pipe, the diameter of the single pipe of the volume increasing pipe corresponding to the amount of the polluted liquid is determined, and the flow of small flocs and fine particles is blocked in the volume increasing pipe by a nozzle or orifice so as to be statically operated. By installing a collision system that concentrates and mixes with a mixer, etc., the cohesive performance before installation was improved several times.

Small flocs grow in a volume increasing pipe equipped with a collision system to form medium flocs without fine particles, which are supplied to the floc forming tank and easily become huge flocs in the tank. The area of the surrounding overflow weir can be reduced, and the floc formation tank has been further downsized.

When the collision system is provided, even if the concentration of the fine particles contained in the injecting liquid / mixed liquid is reduced to 1/10, from the upper surface of the flock forming tank, it is as much as when the collision system is not provided. It has been found that the performance due to the winding phenomenon of does not deteriorate.

If the collision system is not installed, the floc-containing liquid is supplied to the floc forming tank so that the small floc group forms the fluidized bed in the tank and then the increasing pipe pollutant is supplied. If provided, if the floc-containing liquid concentration is 2000 ppm or more in the activated sludge, the operation can be performed from the initial stage. Depending on the concentration of the floc-containing liquid, the performance is sufficiently exhibited without providing all of the collision system means a) to e).

[Brief description of the drawings]

FIG. 1 is an explanatory diagram of an apparatus in which a floc-containing liquid 28 in which an injection liquid 16 containing fine particles is formed and a metering tube contaminated solution collide with each other in a metering tube 31 and a flock forming tank to coagulate and concentrate.

FIG. 2 is an explanatory view of an apparatus in which a floc-containing liquid 28 in which an injection liquid 16 containing fine particles is formed and a volume increasing pipe polluted liquid collide with each other in a floc forming tank to coagulate and concentrate.

FIG. 3 is an explanatory diagram of an apparatus in which a mixing pipe discharge port 8 located in the expansion tube is opened in the frustoconical flock formation tank, and the discharge port of the expansion tube is opened to the collision mixing section of the flock formation tank. Is.

FIG. 4 is an explanatory view in which a mixing pipe discharge port 8 located in the expansion pipe is opened in the truncated pyramid type flock formation tank, and a discharge port of the expansion pipe 32 is opened in a collision mixing portion of the flock formation tank.

FIG. 5 is an explanatory view showing the relationship when the mixing pipe discharge port 8 and the discharge pipe 32 of the increasing pipe polluted liquid are opened at the collision mixing section in the floc formation tank of the flocculation device (horizontal type).

FIG. 6 is an explanatory diagram showing a relationship when the mixing pipe discharge port and the discharge port of the increasing amount pipe polluted liquid are opened in the collision mixing section in the cylindrical flock forming tank.

FIG. 7 is an explanatory diagram of an apparatus in which a mixing pipe discharge port is opened in the metering pipe and a discharge port of the metering pipe is opened to the collision mixing section in the truncated cone type flock forming tank.

FIG. 8: In a flock forming tank composed of a truncated cone shape with a bottom (bottom) and a truncated pyramid shape (top), a mixing tube discharge port opens in the metering tube, and the metering tube discharges into the collision mixing section. It is explanatory drawing of the apparatus which an outlet opens.

FIG. 9 is an explanatory diagram for determining the distance between the side wall of the flock forming tank and the inclined plate.

FIG. 10 is an explanatory view in which a collision mixing plate is mounted in the increasing pipe.

FIG. 11 is an explanatory view showing a static mixer by arranging several mixing blades in the increasing tube.

FIG. 12 is an explanatory diagram of an example of a collision system in which a static mixer is attached to an extender pipe having a small diameter from an annular portion of the extender pipe, and a nozzle and a nozzle are attached to the outlet of the extender pipe before and after the mixer.

FIG. 13 is an explanatory view showing a static mixer by arranging collision plates in the increasing pipe.

[Explanation of symbols]

 1 Polluted Liquid 2 Injection Water 3 Slurry Pump 4 Primary Mixing Tank 5 Stirring Mixing Tank 6 Fine Particles 7 Flock Forming Tank 8 Mixing Pipe Discharge Port 9 Overflow Weir 10 Solid-Liquid Separation Chamber 11 Supernatant Liquid 12 Circulation Pump 13 Filter 14 Coagulation Concentration Sludge 15 Contamination liquid supply pump 16 Injection liquid 17 Mixing pipe 18 Dispersion chamber 19 Injection pipe 20 Collision mixing part 21 Fluidized bed part 22 Moving bed part 23 Inclined plate 24 Flock formation tank discharge port 25 Flock formation tank side wall 26 Flock formation tank bottom 27 Expansion pipe 28 Flock-containing liquid 29 Discharge port 30 Distribution chamber 31 Volume increase pipe 32 Volume increase pipe discharge port 33 Volume increase liquid supply pipe 34 Volume increase pipe pollutant 35 Injection liquid supply pump 36 Injection liquid stirring tank 37 Volume increase pipe ring 38 Volume increase pipe Single pipe Part 39 Mixing pipe annular part 40 Mixing pipe Single pipe part 41 Mixed liquid 42 Collision mixing plate 43 Fixed band 44 Mixing blade 45 Nozzle 45-1 First nozzle 45-2 Second nozzle 45-3 Third nozzle 46 Outlet port

────────────────────────────────────────────────── ───

[Procedure amendment]

[Submission date] May 21, 1996

[Procedure amendment 2]

[Document name to be amended] Statement

[Correction target item name] FIG.

[Correction method] Added

[Correction contents]

FIG. 14 is an example of an explanatory diagram of a static mixer in which nozzles 45 and collision plates 47 are alternately arranged in the increasing pipe.

Claims (13)

[Claims] 1. A flocculating and concentrating device for separating a contaminated liquid containing fine particles into huge flocs of fine particles and a clear liquid. A) A dispersion chamber 18 for storing and dispersing the contaminated liquid, and the contaminated liquid. And a solid-liquid separation chamber 10 for separating fine particles from the contaminated liquid. B) Inside the solid-liquid separation chamber 10, there is provided a flock forming tank 7 that opens upward. , C) and a floc forming tank 7 at the bottom of the solid-liquid separation chamber 10.
Has a take-out port for taking out the huge flocs that have overflowed and dropped from the overflow weir 9, and d) one end between the distribution chamber 30 and the floc forming tank 7 opens into the distribution chamber to collect the contaminated liquid. An opening for introducing and an increasing pipe 31 having an increasing pipe discharge port 32 whose other end is opened in the flock forming tank 7; A mixing pipe 17 having a portion and the other end having a mixing pipe discharge port 8 which is opened in the volume increasing pipe 31, and f) an injection pipe 1 for further injecting an injection liquid 16 into the mixing pipe.
9 has a structure in which the discharge port of the injecting liquid has an opening toward the downstream direction of the contaminated liquid flowing through the mixing pipe, and separates the contaminated liquid containing fine particles into giant flocs of fine particles and a clear liquid. Coagulation concentrator. 2. A flocculating and concentrating device for separating a flocculate liquid containing fine particles into giant flocs of fine particles and a clear liquid, which comprises: a) a dispersion chamber 18 for storing and dispersing the pollutant liquid and the pollution. It is composed of a distribution chamber 30 for distributing a liquid and a solid-liquid separation chamber 10 for separating fine particles from the contaminated liquid. B) Inside the solid-liquid separation chamber 10, a flock forming tank 7 having an upward opening is provided. C) and at the bottom of the solid-liquid separation chamber 10 there is a take-out port for taking out giant flocs that have overflowed and dropped from the overflow weir 9 of the floc formation tank 7, and d) the distribution chamber 30 and the floc formation tank. 7 and one end is opened in the distribution chamber to introduce the pollutant and the other end is opened in the floc forming tank 7 to introduce the pollutant into the floc forming tank 7. A metering tube 31 having a metering tube outlet 32, and e) one end A mixing pipe 17 having an opening for introducing the polluted liquid in the dispersion chamber 18 and a mixing pipe discharge port 8 having the other end opened in the floc forming tank 7; and f) further injecting the injection liquid into the mixing pipe. The injection pipe 19 has a structure in which the outlet of the injecting liquid is opened toward the downstream direction of the contaminated liquid flowing through the mixing pipe. Condensation concentrator that separates into two. 3. The shape of the flock forming tank is such that its cross-sectional area increases upward from the tank bottom and opens at the top of the tank, and the opening edge is a horizontal overflow weir 9, The flocculating and concentrating device according to claim 1 or 2, wherein the giant flocs generated inside are overflowed and deposited on the bottom of the solid-liquid separation chamber 10. 4. When separating from a contaminated liquid containing fine particles into giant flocs of fine particles and a clear liquid by using the flocculating and concentrating device according to claim 1, a) discharging from an injection pipe 19 of the device. By making laminar flow contact between the injection liquid and the contaminated liquid flowing in the mixing pipe 17, fine particles in the contaminated liquid are formed into flocs, and To form a floc group by colliding with the contaminated liquid flowing in the volume increasing pipe 31 in the volume increasing pipe 31, c) Next, the floc group discharged from the volume increasing pipe discharge port 32 into the floc forming tank 7 is aggregated to form a huge floc. A method for aggregating and concentrating, wherein a contaminated liquid containing fine particles is separated into giant flocs of fine particles and a clear liquid. 5. When separating from a contaminated liquid containing fine particles into huge flocs of fine particles and a clear liquid by using the flocculating and concentrating device according to claim 2, a) discharge from an injection pipe 19 of the device By making laminar flow contact between the injecting liquid and the contaminated liquid flowing in the mixing pipe 17, fine particles in the contaminated liquid are formed into flocs, and (2) the floc containing discharged from the discharge port 8 of the mixing pipe 17 of the device. The liquid and the polluted liquid discharged from the discharge port 32 of the increasing pipe 31 are collided in the floc forming tank 7 to form a floc group, and c) The floc group is then aggregated in the floc forming tank to form a huge floc. A method for aggregating and concentrating, wherein a contaminated liquid containing fine particles is separated into giant flocs of fine particles and a clear liquid. 6. The coagulating and concentrating method according to claim 4, wherein an injection liquid prepared by adding fine particles to injection water is used as the injection liquid. 7. Flocculated concentrated sludge of giant flocs accumulated on the bottom of a solid-liquid separation chamber as fine particles to be added to injected water and / or a filter residue obtained by filtering this sludge and / or a filter residue obtained by washing and filtering this sludge. The method for coagulating and concentrating according to claim 4, 5 or 6, wherein 8. When the fine particles added to the injected water are the same as or different from the fine particles of the polluted liquid, the difference between the electrolyte concentration of the polluted liquid and the electrolyte concentration of the injected liquid is at least 1 ppm. Item 8. The method of aggregation and concentration according to Items 4 to 7. 9. The difference in the electrolyte concentration between the floc-containing liquid and the increasing-tube contaminated liquid is set to 1 ppm or more, and the contaminated concentration in the floc-containing liquid is increased to 10 ^{2 to} 6 × 10 ⁵ ppm and supplied to the expanding-pipe contaminated liquid. The method according to any one of claims 4 to 8, characterized in that: 10. The coagulating and concentrating method according to claim 4, wherein a mixed liquid prepared by adding fine particles to the contaminated liquid is used. 11. A flocculated concentrated sludge of giant flocs accumulated on the bottom of a solid-liquid separation chamber as fine particles to be added to a polluted liquid and / or a filter residue obtained by filtering the sludge and / or a filter residue obtained by filtering the sludge. 5. Use according to claim 4.
11. The aggregation / concentration method according to any one of 1 to 10. 12. A flocculating and concentrating device for separating a contaminated liquid containing fine particles into huge flocs of fine particles and a clear liquid, comprising: a) a cross-sectional area of a single pipe portion of a volume increasing pipe and an increase of an annular portion of the volume increasing pipe. The ratio to the cross-sectional area of the increasing pipe calculated from the pipe diameter is called the opening ratio, and the diameter of the single pipe portion of the increasing pipe is desirably reduced to an opening ratio of 85% or less, and b) the increasing pipe immediately before the outlet of the mixing pipe. A weir that opens like a funnel from the annular part to the single pipe of the increasing pipe is provided at the inlet of the single pipe of the increasing pipe. C) A mixer is provided immediately after the weir of the single pipe of the increasing pipe, and a weir is provided downstream of the mixer. ) 1 to several sets are arranged with the mixer and the weir as one set, e) a weir is provided at the outlet of the increasing pipe, and f) 1 to 50 from the outlet of the mixing pipe to the outlet of the thinning pipe.
A coagulation / concentration device for separating a large floc of fine particles into a clear liquid from a contaminated liquid containing fine particles, which is characterized by providing a collision system in which weirs and mixers each having a pressure loss of cm are arranged. 13. When separating a contaminated liquid containing fine particles into giant flocs of fine particles and a clear liquid by using the flocculation device according to claim 1, a) a weir is provided immediately after the outlet of the mixing pipe. (2) A weir arranged in the narrow single tube of the increasing pipe by collision-mixing the increasing pipe polluted liquid flowing into the single pipe of the increasing pipe from the annular portion of the increasing pipe with the floc-containing liquid discharged from the discharge port of the mixing pipe. The small flocs of the floc-containing liquid and the fine particles of the expansion pipe polluted liquid repeatedly collide, agglomerate, and mix with one to several sets with a mixer, and c) concentrate the upstream mixed sludge at the weir of the expansion pipe discharge port. ) Collision, concentration and mixing of concentrated small flocs and fine particles with a mixer to form small floc groups, and e) Next, the static pressure of the giant flocs in the floc formation tank is received to increase the density in the volume increasing pipe. And a little grown small flow in the expansion tube How aggregation concentration for separating the massive floc and clear liquid polluted liquid finer particles containing fine particles, characterized in that agglomerating the middle floc click group.