JP2000000405A - Flocculating and concentrating device and flocculating and concentrating method - Google Patents

Abstract

PROBLEM TO BE SOLVED: To improve the capacity and stability of the flocculating and concentrating device at the time of flocculating fine particles without using any flocculant, to miniaturize the device, to transfer the giantic floc formed in a flocculation tank to a solid-liq. separation chamber without releasing the small particles, to grow the flocs into a concd. sludge and to obtain a closed system without generating excess sludge by setting this flocculating downcomer in the existing solid-liq. separation chamber in an activated-sludge process. SOLUTION: A double hose consisting of a mixing pipe (outer pipe) and an injection pipe (inner pipe) is used, the discharge port of the injection pipe is opened in the mixing pipe, the double hose is spiraled, the discharge port 8 of the mixing pipe is opened in a volume increasing pipe, the discharge port 31 of the volume increasing pipe is opened in a flocculation tank 7, the residence time in the tank is controlled to several min to form the floc having 50 mm diameter, the flocs are transferred to a solid-liq. separation chamber 10 through a spiral downcomer 23 as the flocs easy to concentrate, and a sludge at >=13 kg/m3 is obtained from the bulking sludge.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION The present invention relates to a method in which fine particles are used as a flocculant without using a flocculant. This method separates and sediments at twice the speed to separate and concentrate fine particles into highly concentrated sludge and clear liquid that have grown further from giant flocs, and a device suitable for it.Examples include dredging, drilling, revetment, and opening of waterways. Separation and removal of sediment, clay, and sludge due to construction work, removal of sludge from dams, reservoirs, seas, lakes and marshes, removal of residual food and sludge from fish farms and cultivation fishing grounds,
Water and water pretreatment, removal of red tide, high-concentration activated sludge method / separation of activated bulking sludge, concentration and separation of animals and phytoplankton, removal of blue-green algae, recovery of valuable substances from wastewater, concentration and separation of fermentation liquor and valuable liquid , Other solid-liquid separation in the production process,
An apparatus and a method for economically separating and concentrating a clarified liquid and a solid matter with respect to solid-liquid separation of discharged water from a production process and the like can be mentioned.

[0002]

2. Description of the Related Art Conventional coagulation tubes include straight tubes (straight tubes).
Was used. The longer the coagulation tube, the higher the processing capacity (coagulation performance). However, there are many restrictions on installing on the site a number of coagulation tubes exceeding 4 m for processing a large amount of liquid. However, there is a drawback that the equipment cost increases when the number of units is increased.

In order to coagulate when the contaminated liquid is diluted, an inorganic coagulant is added to provide a reaction chamber in which high-speed stirring is performed in order to enhance the collision effect between the coagulated fine particles. If the solid-liquid separation performance is low, a method has been adopted in which a polymer flocculant is further added to form a huge floc by bridging the polymer flocculant between the fine flocs and then separated in a precipitation tank. The coagulated sludge of this method has a low coagulation concentration, cannot be used for living organisms, and has a great risk of causing environmental pollution.

The present inventor has previously proposed an aggregating apparatus for aggregating and separating fine particles [microorganisms (activated sludge), algae, minerals, plankton, etc.] from the brewery waste liquid, culture growth liquid, and water to be treated containing fine particles. An agglomeration method was invented (application number: 155624, 1988, 176579). In this aggregating apparatus, it is an absolute condition that two liquids having different electrolyte concentrations are brought into laminar flow contact in order to agglomerate fine particles of the injection liquid 16) and the water to be treated (dredge liquid). That is, in order to make laminar flow contact, the amount of the liquid to be treated supplied to one mixing tube had to be maintained at Re <10 ⁵ , but the increasing amount of liquid (= water to be treated) and the liquid containing the mixing tube floc were earlier. Although the processing capacity was improved by collision mixing with (1), it was desired to further reduce the concentration of the coagulated and concentrated sludge and reduce the size of the apparatus for improving the separation performance.

[0005]

Even if the performance of a coagulated tube (straight tube) exceeding 4 m (the longer the tube is, the higher the performance) is, the unevenness of the welding at the connection portion is not allowed to obtain laminar flow. There are many restrictions on installation, the length of time required for construction is long, the equipment cannot be moved, there is no mobility, there is a high demand for miniaturization that can be installed on mobile vehicles while maintaining cohesion performance, and the existing solid-liquid separation chamber The most important issue is the coagulation device that fits in the depth of the water.

The difference between the electrolyte concentrations of the two liquids, the injection liquid and the mixed liquid in the coagulation tube, which is the life of the apparatus, is adjusted to 1 mV or more.
The liquid is in laminar flow contact and the distance between the particles of the two liquids is 60 while maintaining the difference of the surface potential of the fine particles of the two liquids of 1 mV or more at the interface of the two liquids.
If sludge concentration within 〜80 ° (August Strong) is continuously maintained, it is an apparatus that instantaneously forms flocs by collision and aggregation. The disadvantage is that the laminar interface of the two liquids is destroyed by micro-vibration or the like of the device, and if the two liquids are mixed, no coagulation occurs. Preventing vibration to long coagulation tubes has been the biggest problem that cannot be avoided in outdoor equipment.

A large floc (30 to 40) which is taken out from the overflow weir (4) of the conventional floc forming tank by a straight pipe or an inclined plate method.
mm diameter), the falling speed is high, the resistance to still water is large, and there are many small particles that separate from the giant floc falling down the inclined plate. The clear liquid is the separated small particles that rise in the gap between the wall of the floc forming tank and the inclined plate, and the supernatant plate (21) on the floc forming tank suddenly becomes cloudy, and at the same time, the concentration performance at the bottom of the solid-liquid separation chamber is improved. There was also a drawback to lower. In an apparatus for the purpose of coagulation and separation for obtaining a clear liquid, a system for continuously treating the separated small particles is required.

(Application No. 1988 Patent Application No. 15562)
No. 4, application number 1988 Patent Application No. 176579) The floc formed in the mixing tube collides with the polluted fine particles in the floc forming tank (application number 1993 Patent Application No. 206793) to form floc. There is a restriction that the infused solution 16) and the mixed solution come into laminar flow contact, and the amount of the processing solution floc-containing liquid (1) per mixing tube is small. Even if the increasing liquid was increased to 10 times or more and 400 times the amount of the contained liquid (1), a huge floc was formed in the floc forming tank and a clear liquid was obtained on the upper surface of the forming tank, but overflowed from the upper edge of the floc forming tank. When the diameter of the floc during the transfer of the giant floc falling on the inclined plate to the solid-liquid separation chamber (10) becomes 25 mm or more, the detachment from the floc surface becomes severe, and the floc forming tank is formed by the detached small particles rolling up on the inclined plate. Up The diameter of the giant floc formed by collision mixing with an increasing amount of 10 to 20 times the amount of the floc-containing liquid (1) is 25 mm, which is the permissible limit of peeling. Was desired.

In the existing solid-liquid separation chamber, there is no system for recycling and recycling the activated sludge that has settled and separated, or a coagulant cannot be used for the settling and separation of fine-particle foodstuffs. A flocculant is used in a system that does not reuse settled sludge. There is a demand for a technical apparatus for obtaining high-concentration coagulated and concentrated sludge with little remodeling cost without using a coagulant.

[0010]

When a spiral tube (= convoluted tube) or a spiral tube is used as a coagulation tube, the critical Reynolds number for obtaining a laminar flow is more than 3 to 5 times more stable than a straight tube. The longer the pipe length, the greater the laminar flow stability.
In the United States, the flow-through processing capacity of the spiral tube and the spiral tube is increased to 10 to 25 times or more by increasing the tube length for the same straight tube diameter. From this, the number of spiral pipes and spiral condensing pipes can be greatly reduced as the number of straight pipe condensing pipes. Even if the condensing tube of the spiral tube and the spiral tube is lengthened to increase the liquid permeation performance, the device does not become high, but it becomes compact, and has high mobility that can be installed on a mobile vehicle and relocated as it is. Even if the liquid supply chamber, coagulation device and spiral downcomer are arranged in this order in the liquid separation chamber from the top, it can be set at the height that can be installed.

[0011] If a spiral tube (= convoluted tube) or a spiral tube is used, the laminar flow of the swirling flow is more stable and less turbulent than that in a straight tube. If the liquid is sent from below, it can be settled at a height of 1 m or less.
It can effectively cope with a range of m ^2. Spiral tube (=
If a spiral tube) or a spiral tube is used, the anti-vibration equipment becomes a conventional horizontal type 10
The installation area of a coagulation tube (straight pipe length 5 m, 8 tubes, width 1.8 m) for processing 00 m ³ days needs to correspond to a large area of 9 m ² , but the spiral tube coagulation tube must be installed. In a coagulation cylinder (45) having an area diameter of 1 m and a height of 1.5 m, two or three mixing tubes of a double tube (48) having a built-in injection tube can be wound and stored in a snake tube 1 m.

Assuming that the diameter of the condensing tube of the spiral tube is 1.9 m in the solid-liquid separation chamber loaded on the moving vehicle, the length of the spiral tube having the same diameter m is 5 m.
m ³ days can be processed. The height of the coagulation tube is 110
It fits in the coagulation tube frame (52) from the height of mm to the height of the conical rolled up +0.5 m. The end of the mixing pipe (sometimes a collision mixing section is connected to the mixing pipe discharge port) is connected to the branch pipe of the expanding pipe (in the coagulating pipe) flowing vertically through the flocculating cylinder, and is increased through the floc transfer pump (34). Since the pipe discharge port is supplied to the floc forming tank outside the coagulation tube, the vibration isolating equipment for the coagulation tube of the spiral tube is effectively attached to a small-area beam or column supporting the coagulation tube frame (52), There are no restrictions for selecting the installation location

The present inventor has disclosed Japanese Patent Application No. 63-155624,
A floc forming tank described in Japanese Patent Application No. 5-206793 is provided in a solid-liquid separation chamber of an aggregating apparatus described in Japanese Patent Application No. 63-176579, and a discharge port of a mixed liquid impingement mixing pipe is provided in an increasing pipe. The aggregating apparatus having a structure in which the discharge port of the expanding liquid impingement mixing pipe is located in the floc forming tank is provided with a floc having unagglomerated fine particles discharged from the expanding liquid impinging mixed liquid and residual cohesive force. When the residence time in the floc forming tank is 2 minutes to 50 minutes, the fluidized bed height after the operation is stopped is compared. When the bed height is low, the density of the floc is high, and the giant floc falling from the forming tank is high. Since it is difficult for the small particles to peel off, a residence time of about 2 to 30 minutes in the floc forming tank is sufficient.

The downcomer pipe for transferring the dense giant floc obtained in the floc forming tank is opened at the top of the floc forming tank, and spirally descends inside or outside the floc forming tank to form a solid liquid below the bottom of the floc forming tank. The outlet of the downcomer is opened in the separation chamber, and the spiral downcomer (23) has a gentle inclination angle of 5 to 45 degrees for activated sludge having a high fluidity, and an inclination angle of 10 to 60 for dredged sludge having a large specific gravity. By having a mechanism that can adjust and change the angle around the degree, it is possible to select a flow rate with little peeling in the downcomer pipe, the flocculation performance of the spiral flocculation pipe of the present invention is 400 times the amount of floc-containing liquid When giant flocs (30-55 mm in diameter) that have collided and mixed in the floc forming tank are moved as a continuous phase without voids that slowly descends in the spiral downcomer, almost no exfoliated small particles are generated. At the same time show a remarkably high performance, it has become possible to increase the concentration performance of the flock. The amount of the separated small particles deposited on the coagulated and concentrated sludge layer was extremely reduced, and the time for continuously treating the sludge was significantly reduced.

In the flocculation of a dredged contaminated liquid having a large specific gravity difference between the condensed condensed condensed sludge liquid and the contaminated liquid, the condensed liquid of the slightly separated small particle group deposited on the dredged condensed condensed sludge in the solid-liquid separation chamber is layered. Specific gravity shows 1.03 to 1.05. A pulling pump (1) is pulled out from the small particle suction port of the coagulated concentrated sludge layer (22).
2), the dispersion plate (1) in the re-coagulation tank (2) for storing the highly concentrated sludge layer (14) having a specific gravity of 1.10 or more.
If the particles are supplied and contacted at 1.5 m ³ / m ² min or less in 3), the small particle groups are completely captured by a huge concentrated sludge layer 14) having a specific gravity of 1.10. Supernatant (15)
The sludge is separated completely in the polluted state, and the highly concentrated sludge is not diluted.

In the case of an activated sludge treatment liquid having a small specific gravity difference between the flocculated concentrated sludge liquid and the small particle contaminated liquid, the supernatant liquid (21) becomes turbid,
The supply speed is extremely reduced, which is not preferable.

In the initial stage of the operation in which a continuous moving layer of giant flocs cannot be formed in the spiral downcomer (23), small particles separated from the spiral downcomer are slightly discharged from the outlet of the spiral downcomer. When it is discharged as a continuous moving bed without gaps of huge flocs, a small particle group layer is formed on the flocculated and concentrated sludge layer (22) in the initial stage of operation, but the flocculated and concentrated lower layer is formed within one hour. If the small particles on the coagulated and concentrated sludge layer do not disappear, they are continuously supplied from the suction pipe to the expansion pipe and the distribution chamber (30) by the suction pump (26). To form flocs in the floc forming tank.

In the activated sludge method in which bulking sludge generated by filamentous microorganisms is frequently generated, or in a solid-liquid separation apparatus equipped with an existing solid-liquid separation chamber, the coagulation apparatus of the present invention is installed in the existing solid-liquid separation chamber. By installing a solid-liquid separation cylinder outside the existing solid-liquid separation chamber, supplying activated sludge subjected to biological treatment or coagulated sludge that has passed through the coagulation device of the present invention into the existing solid-liquid separation chamber. By staying in the chamber for several hours, bulking sludge that has not settled in the conventional solid-liquid separation chamber becomes 10,000 times or more the spontaneous sedimentation rate of the huge floc formed by the flocculation apparatus of the present invention. The concentration of the sludge drawn out of the liquid separation chamber is improved 2 to 8 times. In the activated sludge method, the amount of sludge in the aeration tank is increased. As a result, the processing capacity of the activated sludge method is increased, the BOD sludge load (= BOD load kg / sludge kg / day) is reduced, and the residual substrate in the discharged water is reduced. The concentration was reduced, the growth of microorganisms was suppressed, and the amount of excess sludge generated could be expected to be zero.

[0019]

Embodiment 1 Embodiment 1 will be described with reference to the drawings. In the embodiment shown in FIG. 1, the coagulation device includes a liquid supply chamber, a coagulation cylinder (45), and a solid-liquid separation chamber (10). The communication pipe (46) connects the coagulation cylinder (45) and the solid-liquid separation chamber.
And the water level of the flocculation cylinder is 3 from the liquid level in the solid-liquid separation chamber.
Adjust so that it can be maintained at ~ 50cm high, infusion solution (36)
The mixed liquid (55) and the supply of the increasing liquid are supplied quantitatively.
The treated water is discharged from the discharge pipe (47) of the aggregation tube. The coagulation tube is composed of an injection tube spiral (19), a mixing tube (32), and an extension tube (56). A double tube having an injection tube fixed to a support (39) inscribed in the mixing tube is inserted inside the coagulation tube. Tube (4
8) is wound in a snake tube. The flexible tube is fixed by a support fitting (50) fixed to the peripheral wall of the coagulation tube. The mixed liquid supply port (35) to the mixing pipe outside the flexible pipe penetrates the bottom of the dispersion chamber (18) of the liquid supply chamber and is located at a position higher than the overflow weir liquid level (38) at the discharge port of the coagulation cylinder. The outlet of the mixing pipe (8) is joined to the inlet of the collision mixing section (49), and the outlet of the collision mixing section is connected to the branch pipe (37) of an intensifier pipe flowing vertically through the condensation pipe (45) at the bottom of the condensation pipe. Are connected to each other and are opened to the expansion tube. A number of supports (39) inscribing the inner surface of the mixing tube are fixed to the outside of the injection tube, and are mounted so that the tube axes of the mixing tube and the injection tube merge as much as possible. The number of attachments varies depending on the diameter of the flexible tube and the diameter of the mixing tube.
Pieces / m. The injection liquid supply port (36) opens at a position higher than the supply port of the mixing pipe, and the injection liquid discharge port (20) opens downstream at a position 4 to 10D upstream of the mixing pipe diameter D from the mixing pipe discharge port. ing. The increasing pipe is opened to the distribution chamber (30) on the aggregating cylinder (45), and the liquid to be treated (extending liquid) 33 is supplied in an overflow manner, and collides and mixes with the mixed liquid in the branch pipe (37). The solid-liquid separation chamber (1) is transferred via the transfer pump (34).
It is fed into a floc forming tank 7) in 0) and separated into a giant floc and a clear solution.

In the embodiment shown in FIG. 2, a diagram is shown in which the solid-liquid separation chamber (10) and the aggregating device are relocated while loaded on the moving vehicle (41). The coagulation device conical-shaped a 3.5 m triple tube (53) in which a double tube (48) of an injection tube (inner tube) and a mixing tube (outer tube) was inserted into an increasing tube on a solid-liquid separation chamber. The height of the wound spiral tube (51) is 30 cm.
The connection pipe between the distribution chamber (30) and the expansion pipe (56), and the connection pipe between the dispersion chamber (18) and the mixing pipe (32) uses a highly flexible pipe, and is provided on the upper surface of the solid-liquid separation chamber. An accordion cylinder (44) that can expand and contract vertically is connected to adjust the water level of the distribution chamber / dispersion chamber with respect to the overflow discharge water level of the solid-liquid separation chamber. When moving, fold the accordion cylinder and place it in the distribution room. The dispersion chamber was separated from the coagulation tube and stored in the solid-liquid separation chamber, and the accordion cylinder was lowered to a height of 15 cm above the solid-liquid separation chamber to enhance the mobility. The coagulation tube frame is supported by a ladder (42) independent of the moving vehicle (41), and the ladder and the coagulation tube frame (5) are supported.
2) and the grounding part of the ladder (42)
By mounting 3), the rake (3) for discharging the coagulated sludge from the solid-liquid separation chamber (10) was prevented from vibrating, and no reduction in the coagulation performance was observed.

In the embodiment shown in FIG. 3, the branch pipe (37) of the expanding pipe and the mixing pipe end (the mixing pipe discharge port (8) and the collision mixing section (49) are connected, and the mixing pipe (32) FIG. 5 is a diagram showing the relationship between the liquid and the injection liquid discharge port (20).

In the embodiment shown in FIG. 4, the support (39) adhered to the injection pipe is made of a 1.2 mm-thick metal plate of the support (39) A inscribed at three places of the mixing pipe. The radius of the inscribed surface at the tip of A is 1.5 to 2 mm, and the length in the tube axis direction is the width of the hard core of the mixing tube and the width of the hard core (2 to 6) +4.
mm, and the area of the product of the length of 45 to 55% of the outer circumference of the injection tube and the length of 25 mm in the tube axis direction is bonded. One example of a supporter having an inner diameter of a mixing tube of 63 mm and an outer diameter of 33 mm of an injection tube is shown. The support (39) provided on the mixing tube and the extension tube is made of a synthetic resin, and the support B inscribed at three places of the extension tube is a flat plate having a thickness of 25 to 6 mm. The length is 0.5 to 1.5 mm in order to reduce the size, the axial length of the tip is 30% to 2 times the diameter of the mixing tube, and in order to prevent the generation of a vortex toward the upstream and downstream of the flow, FIG. Sharp off the shoulder of the flat plate and sharpen the tip as shown in ()). FIG. 4A shows a combination of the support A fixed to the injection tube and the support B fixed to the mixing tube. The combination of fixing the support A to the injection tube and fixing the support A to the mixing tube, and the support A combination in which B is fixed to the injection tube and the support B is fixed to the mixing tube, or a combination in which the support A is fixed to the mixing tube and the support B is fixed to the injection tube.

Embodiment 2

Activated sludge treatment liquid in an activated sludge treatment facility for treating rice washing wastewater generates filamentous microorganisms, and the activated sludge cannot be coagulated and concentrated at a natural sedimentation rate of 1 cm / day and a concentration of 12,000 ppm. ing. This filamentous bulking sludge is used as an injection liquid 16) at 0.05 l / min.
And a mixed solution of the activated sludge 3 and tap water 1 as a mixed solution.
The floc-containing liquid (1) (0.15 l / min) discharged from the mixing pipe in which laminar flow of 1 l / min is contacted with the bulking liquid in the bulking pipe, and the discharge port of the bulking liquid collision mixing pipe is connected to the floc forming tank. (Volume of 150 l). Injection tube inner diameter 8 mm, mixing tube inner diameter 19 mm, increasing tube inner diameter 65 mm
And a spiral downcomer of 125 mm was used. The apparatus of FIG. 5 was used. A) The floc-containing liquid (1) was supplied at a rate of 0.15 l / min and a quantity of the increasing liquid of 4.85 l / min to the floc forming tank at a residence time of 30 minutes. B) The floc-containing liquid (1) amount of 0.15 l / min and the increasing liquid amount of 29.85 l / min were supplied to the same floc forming tank with a residence time of 5 minutes. Result: When the supply of the bulking liquid was stopped, the height of the fluidized bed in the floc formation tank was lower in B than in A, and the sedimentation speed of both sludges pumped from the tank was higher in B than in A. C) Floc-containing liquid (1) 0.15 l / min and an increasing amount of 74.85 l / min were supplied to the same floc forming tank with a residence time of 2 minutes. Result: The height of the fluidized bed in the floc forming tank was not different from B). D) The floc-containing liquid (1) in an amount of 0.15 l / min and a bulking liquid of 37.35 l / min were supplied to the same floc forming tank with a residence time of 4 minutes. Result: Fluidized tank height in the floc forming tank was lower in D) than in B). It is determined that B) has a higher fluidized bed height than D) because the floc growth is slow because the amount of the liquid to be supplied per unit time is small. It is determined that the reason why C) is higher than that of D) is that the residence time in the floc forming tank is as short as 2 minutes. Three hours after the treatment under the operating conditions of B) and C), the concentrations of the coagulated and concentrated sludge in the solid-liquid separation chamber were 11,600 ppm and 11,000 ppm. The flocculent concentrated sludge of the huge floc in the solid-liquid separation chamber, which was treated under the operating conditions of D) and supplied from the floc formation tank to the solid-liquid separation chamber by a spiral downcomer pipe for 3 hours, had a supplied concentrated liquid concentration of 12,000 ppm. The activated sludge (natural sedimentation rate = 1 cm / day) was concentrated to 13,000 ppm.
No peeling phenomenon was observed during continuous operation. It has been considered impossible to concentrate high-concentration activated sludge of filamentous microorganisms. However, under the operating conditions of D) using the flocculation and concentration device having a spiral downcomer according to the present invention, the concentration can be reduced in a short time. Has been demonstrated to be possible. In the floc formation tank, it collides with a larger amount of the increasing amount of liquid, and a dense giant floc (3
(5 to 55 mm diameter), it is desirable to form a fluidized bed of highly concentrated sludge in the formation tank and the residence time in the floc formation tank is 4 minutes or more.

[0024]

EXAMPLE 3 The coagulation device of the present invention was used with the downcomer diameter of 60% of the device of FIG. 5 used for the activated sludge, and the recoagulation tank (2) of FIG. 6 was installed. In order to collide and coagulate the 80-600 ppm river water MLSS polluted water for the purpose of service water, fine particles of Kibushi clay (specific gravity: 2.6, tap water is taken in a 1-liter cylinder, 100 g of a specimen is added, and 24 hours later 248 ml of the sedimentation interface, and 22% for the sample particle size accumulation curve of 1 micron or less) and a test contaminant MLSS 110,000 having a sufficient contaminant concentration for collisional aggregation.
It adjusted to 1.082 ppm specific gravity. Inject the contaminated liquid,
Separate into a mixed liquid and a bulking liquid, add 20% of the polluted liquid with tap water with low electrolyte concentration to the injection liquid, provide a difference of 1 ppm or more in the electrolyte concentration with the mixed liquid, and provide a mixing pipe that opens into the dispersion chamber. Then, the injection pipe is inserted into the mixing pipe with its pipe axis united, and 0.05 l / min of the injection liquid (16) is downstream from the discharge outlet of the injection pipe along the flow of 0.1 l / min of the mixed liquid flowing through the mixing pipe. In the direction, 0.05 l / min is supplied at a laminar flow rate. The MLSS 110,0 is added to the extension tube that incorporates or connects the mixing tube.
200 ppm of 200 ppm floc-containing liquid (1) 2
9.85 l / min was supplied from the distribution chamber. The speed of passing through the opening (diameter: 45 cm) at the top of the tank in the floc forming tank 150 l for a residence time of 5 min is 0.315 cm / sec.
Met. In the initial stage of the operation, the separated small particle-containing liquid shown in FIG. 6 is drawn out from the suction port of the coagulation-concentrated sludge layer (22) by the suction pump (26), and the re-coagulation tank storing the water-grained clay having a specific gravity of 1.13 or more ( In 2), it was supplied and captured at a speed of 0.4 m / min, but after 1 hour, the discharge port of the downcomer pipe was buried in the sediment sludge in the solid-liquid separation chamber, and then the separated small particles were observed on the coagulated and concentrated sludge layer. The operation to the re-coagulation tank was stopped, but the trapping effect was expected. Table 1 shows the SS, specific gravity, and supernatant MLSS of the coagulated and concentrated sludge for 30 minutes, 1 hour, and 3.5 hours after the start of the operation for pulling out from the bottom of the solid-liquid separation chamber. Table 1 Extraction time SS Specific gravity Supernatant MLSS 30 min 145 g / l 1.102 18 ppm 1 hour 180 １．１ 1.122 12 〃 3.5 hours 270 １．１ 1.158 9 〃 Water area load of Kibushi clay 0. At 01 m / day, the concentration of raw water is 100 g / l and the concentration of residual water is 0.1 g / l. The apparatus of the present invention supplied 30 l / m to the solid-liquid separation chamber (0.6 m diameter). The water area load at that time was 152 m ² / m ² days, and the difference in performance was 15,200 times. 152 m / day / 0.01 m / day = 15,200 times For the purpose of collecting a clear supernatant from a dilute contaminant, a large amount of Kibushi clay, fly ash, diatomaceous earth, etc. is added and collisional coagulation is performed. After the coagulation, concentration, and separation, a supernatant 21) was obtained as in the above example, and the coagulation aid was added to the added water (diluted contaminant), circulated and reused to clarify the dilute contaminated liquid. Can be achieved.

[0025]

Embodiment 4 A liquid absorption chamber, a spiral coagulation tube, and a floc forming tank are provided outside a solid-liquid separation chamber having a diameter of 3 m and a depth of 4 m which is treating the bulking activated sludge of Example 2 (sedimentation velocity: 2.3 cm / day). Solid-liquid separation tube with built-in spiral downcomer (5
4) is installed, the spiral downcomer of the solid-liquid separation tube penetrates the side wall of the solid-liquid separation chamber, and the enlarged pipe nozzle at the end thereof is joined as the discharge port of the huge floc. As shown in FIG. 0.15 l / m of a mixed solution obtained by laminar flow contact of 0.05 l / m of the injection solution and 0.1 l / m of the mixture of activated sludge 3 tap water 1
m collides with the bulking liquid in the bulking pipe, and
The giant floc formed by collision mixing for 4 minutes in 1 was transferred to the solid-liquid separation chamber through a magnifying tube by a spiral downcomer tube opened on the tank. The coagulation tube has an inner diameter of the injection tube of 8 mm, an inner diameter of the mixing tube of 19 mm, an inner diameter of the increasing tube of 65 mm, and a 150 mm inside the spiral downcomer. Example 2
(D) Operating conditions The floc-containing liquid (0.15 l / min) and the increasing pipe (37.35 l / min) were placed in the floc forming tank 150.
to the solid-liquid separation chamber from the floc forming tank with a spiral downcomer 150 mm in diameter.
After 10 hours had passed from the supply to the solid-liquid separation chamber at mm / sec, the concentrated sludge obtained 16,400 ppm of bulking activated sludge having a bulking liquid concentration of 3200 ppm. It is concentrated 5.13 times. The MLSS of the effluent from the solid-liquid separation chamber is 5 to 5.
13 ppm.

[0026]

Since the present invention is configured as described above, it has the following effects.

When a spiral tube or a spiral tube is used, the stability of laminar flow is higher and the flow-through capacity is 3 to 5 times higher than that of a straight tube. The size can be reduced to 3 to 1/10. Therefore, it is possible to install a coagulation-downcomer pipe in most existing solid-liquid separation chambers, and it is possible to load on a mobile vehicle, and it is easy to move and relocate for long-term and short-term treatment of polluted liquid. Became.

The above-mentioned laminar flow stability and liquid passing capacity are 3 to 5 times higher than those of the straight pipe type, and the cost of the coagulation equipment can be reduced to 20 to 50%.

The agglomerator to 3000 m ³ days per group is manufactured in the factory, facility construction becomes principal construction piping connection around the site becomes short as environmental facilities, in a short time undesired outage Can be completed.

By using the spiral downcomer from the floc forming tank, it is possible to adjust the descending speed of the giant floc with the inclination angle in accordance with the properties of the floc, and to continuously move without the floc gap between the giant flocs. As a result of continuous discharge as a layer, the peeling phenomenon of fine particles almost disappeared.

The interface between the coagulated concentrated sludge deposited in the solid-liquid separation chamber and the supernatant (21) is referred to as the coagulated concentrated sludge layer 22) surface. The liquid containing the separated small particles on the surface of the sludge layer is sucked by a suction pump (26), returned to the filler supply pipe, and continuously supplied to a system for re-aggregation in the floc forming tank. The reduction in the transfer speed in the tube resulted in a decrease in peeling, and a favorable result was obtained in preventing the supernatant from being polluted by the peeled small particles.

The outlet of the downcomer pipe of the solid-liquid separation chamber is opened two to several times below the diameter of the downcomer pipe from the surface of the coagulated and concentrated sludge layer (22), and the properties of the coagulated and concentrated sludge (specific gravity, concentration, friction coefficient) The position of the discharge port rises and falls according to the length of the inclined downcomer and the amount of sludge. However, when the surface of the coagulated and concentrated sludge layer rises and the discharge from the downcomer stops, the pulling pump (1) at the bottom of the solid-liquid separation chamber is used.
2) is operated to discharge the coagulated concentrated sludge, and when the surface of the coagulated concentrated sludge reaches a position twice the diameter of the downcomer pipe from the outlet of the downcomer pipe, the operation of the drawing pump (12) is stopped. If the required residence time of the coagulated and concentrated sludge is always ensured in the volume of the solid-liquid separation chamber below the discharge port, stable continuous operation without discharge of separated small particles can be performed.

Coagulation in solid-liquid separation chamber of existing activated sludge equipment
In the experiment in which a downcomer was installed, the natural settling velocity of the activated sludge of 12,000 ppm of activated sludge was 0.012 m ³ / m ² days of bulking sludge was converted to a floc forming tank diameter of 0.45 m, a volume of 0.15 m ^{3 and a} residence time of 4 m.
in, the amount of liquid supplied to the floc forming tank 0.0375 m ³ /
min. 1) Floc forming tank load 340 m ³ / m ² days Natural sedimentation velocity 0.012 m ³ / m ² days The performance of the apparatus of the present invention is 340 / 0.012 = 28.333 times that of a general sedimentation tank 2) Solid-liquid separation chamber (Area of 0.6 m × 2.5 m) Water area load 191 m ³ / m ² days The performance of the apparatus of the present invention is 191 / 0.012 = 15,923 times that of a general sedimentation tank. The diameter of the floc that has descended to the natural settled floc diameter is 15,923 ^0.5 =
That is, it is 126 times larger. The removal of small particles from the spiral downcomer was successfully eliminated, and for the first time it was possible to evaluate the water area load performance on the solid-liquid separation chamber.

A floc-containing liquid (1) in which the sedimentation rate of 12,000 ppm of bulking activated sludge, which had been considered impossible to be concentrated, at 1 cm / day was adjusted to two different potentials of bulking sludge, and the two liquids were brought into laminar flow contact. And a giant floc formed by flowing and contacting 250 times the amount of the floc-containing liquid in a 150-liter floc forming tank for 4 minutes, and forming a continuous floc without a floc gap in the solid-liquid separation chamber with a spiral downcomer. After forming a moving layer and discharging the giant floc without exfoliation of small particles, the giant floc was retained in the solid-liquid separation chamber for 3 hours and could be concentrated to 13,000 ppm.

Since the separation from the giant floc having a diameter of 40 to 55 mm was eliminated by the spiral downcomer pipe (23) from the floc forming tank, an increased amount of the liquid that is 400 times or more the amount of the floc-containing liquid (1) was transferred to the floc forming tank. Can be supplied, and the number of aggregation tubes is reduced to 1/10 to 1/20.
By adjusting the angle of inclination of the spiral downcomer and gently transporting the inside of the tube with a moving layer without voids, the solution of the generation of small particles peeled off enhances the aggregating performance of the aggregating device, brings downsizing, and reduces the existing solidification. The coagulation-downcomer can be easily installed inside and outside the liquid separation chamber, and the countermeasures against micro-vibration of the coagulation device are facilitated. If this equipment is installed, the BOD ₅ sludge load will be 0.06 kg / kg day or less, the disposal and disposal cost of excess sludge which has been required for 70 years since the development of the activated sludge method will be eliminated, and the treated water quality will be the BOD ₅ removal rate. Achieve 99%,
The contaminated liquid turned into a clarified liquid, and the apparatus became a complete apparatus only for discharging CO ₂ and N ₂ . Naturally, the coagulation (agent) device, sludge thickening tank, filtration device, incineration facility, sludge dumping site and its workers are not required.

[Brief description of the drawings]

FIG. 1 is a longitudinal sectional view of an aggregating device provided with a flexible tube.

FIG. 2 is a longitudinal sectional view of an aggregating device provided with a spiral tube.

FIG. 3 is a diagram showing a connection between a discharge port of a mixing pipe and a branch pipe of an increasing pipe, and a relation between a discharge port of a mixing pipe and a discharge port of an injection pipe.

FIG. 4 is an example of a support for unifying the respective tube axes of the support for the mixing tube and the injection tube (A) and the support for the extension tube and the support for the mixing tube (B).

FIG. 5 is a longitudinal sectional view of a coagulating and concentrating apparatus having a spiral downcomer outside a floc forming tank.

FIG. 6 includes a spiral downcomer in a floc forming tank,
It is a partial longitudinal section of the coagulation concentration apparatus equipped with the recoagulation tank.

FIG. 7 is a longitudinal sectional view of a coagulating and concentrating apparatus for transferring coagulated sludge from a floc forming tank in a solid-liquid separation cylinder outside a solid-liquid separation chamber to a solid-liquid separation chamber by a spiral downcomer.

[Explanation of symbols]

 REFERENCE SIGNS LIST 1 floc-containing liquid 2 reagglomeration 3 rake 4 overflow weir 5 exfoliated small-particle-containing liquid 6 penetrating side wall of floc forming tank 7 floc forming tank 8 discharge port of mixing tube 9 floc forming tank bottom 10 solid-liquid separation chamber 11 expansion nozzle 12 drawing pump DESCRIPTION OF SYMBOLS 13 Perforated plate 14 Highly concentrated sludge layer 15 Reconcentration tank supernatant liquid 16 Injection liquid 17 Spiral mixing pipe 18 Dispersion chamber 19 Spiral injection pipe 20 Injection liquid discharge port 21 Supernatant liquid 22 Coagulated concentrated sludge layer 23 Spiral downcomer 24 Spiral descent Pipe inlet 25 Suction port 26 Suction pump 27 Volumetric liquid collision mixing pipe 28 Spiral volumetric pipe 29 Volumetric liquid supply pipe 30 Distribution chamber 31 Volumetric pipe discharge port 32 Mixing pipe 33 Liquid to be treated 34 Floc transfer pump 35 Mixed liquid supply port 36 Injected liquid Supply port 37 Increasing pipe Branch pipe 38 Overflow weir (discharge water) 39 Supporting tool 40 Supporting blade 41 Transfer Car 42 ladder 43 anti-vibration rubber 44 accordion cylinder 45 coagulation cylinder 46 communication pipe 47 discharge pipe 48 double pipe 49 collision mixing unit 50 support fitting 51 spiral tube 52 coagulation pipe frame 53 triple pipe 54 solid-liquid separation cylinder 55 mixed liquid 56 Extension tube

Claims (13)

[Claims] 1. An aggregating apparatus for forming a huge floc of fine particles from a liquid to be treated (33) containing fine particles, comprising: a) a liquid supply chamber for supplying and distributing the liquid to be treated; The liquid supply chamber includes a dispersion chamber (18) for dispersing the liquid to be treated (33) containing fine particles and a distribution chamber (30) for distributing the liquid to be treated. C) One end of the distribution chamber (30) An expanding pipe (29) is provided at the other end, and an expanding branch pipe (37) for receiving the mixing pipe is provided in the middle thereof. D) One end of the dispersion chamber (18) is provided. ) Is provided with a spiral mixing tube (17) having the other end opened in the volume increasing tube, and a double tube (47) having the mixing tube on the outside and an injection tube on the inside is a spiral tube = a serpentine tube (26) and a spiral tube (51). E) Injecting the injection liquid (16) into the spiral mixing tube (32) Liquid to be treated containing fine particles, characterized in that the liquid injection port (20) of the spiral injection pipe (19) has a structure opened toward the downstream of the liquid to be treated (33) flowing in the mixing pipe. An aggregating device that separates into giant flocs of finer particles and clear liquid. 2. An aggregating apparatus for forming giant flocs of fine particles from a liquid to be treated (3) containing fine particles, comprising: a) a liquid supply chamber for supplying and distributing the liquid to be treated; The liquid supply chamber is composed of a dispersion chamber (18) for dispersing the liquid to be treated (33) containing fine particles and a distribution chamber (30) for distributing the liquid to be treated. C) One end is connected to the distribution chamber (30). A spiral volume increase pipe (28) is provided which is open and the other end is open to the floc forming tank 7). D) One end is open to the dispersion chamber (18) and the other end is the distribution chamber (3).
0) a mixing pipe 2) having a mixing pipe discharge port (8) opening downstream from the inlet of the spiral pipe (29) extending along the pipe axis of the pipe, and e) outside the mixing pipe. A spiral mixing tube in which the respective tube axes of a triple tube (53) having an injection tube on the inside are merged = a serpentine tube (26) and a spiral tube 51). F) The spiral mixing The supply port of the spiral injection pipe (19) for injecting the injection liquid into the pipe (17) has a higher water level than the inlet of the mixing pipe, and the injection liquid discharge port (20) is located downstream of the liquid to be treated (33) flowing through the mixing pipe. An aggregating apparatus for separating a liquid to be treated into a giant floc of fine particles and a clear liquid from a liquid to be treated containing fine particles, wherein the flocculant has a structure opened toward the direction. 3. Spiral mixing pipe (17) The spiral injection pipe (19) has a smooth inner wall surface, the injection pipe and the mixing pipe have smooth outer walls, and the injection pipe has a support (39) inscribed on the inner surface of the mixing pipe. 3. The aggregating apparatus according to claim 1, wherein the aggregating apparatus is fixed to maintain a structure in which the axis of the mixing tube and the axis of the injection tube are united. 4. A structure in which a double pipe (6) having a spiral (= convoluted) mixing pipe on the outside and a spiral injection pipe on the inside is wound along the side wall of the cylinder. 4. The coagulation device according to claim 3. 5. A spiral tube (51) having a structure formed by winding a double tube (48) having a spiral mixing tube on the outside and a spiral injection tube on the inside along a conical side surface, and a double tube (4).
The aggregating apparatus according to claim 1, wherein the coagulating apparatus has a structure formed by winding 8) from the inside to the outside on a plane. 6. A double pipe (4) consisting of a spiral mixing pipe and a spiral injection pipe, with the spiral expanding pipe (28) being the outermost.
8) Inserting, winding a triple tube having united tube axes to form a spiral (= convoluted tube), spiral tube (51) structure.
The coagulation apparatus according to claim 3, wherein 7. A metal plate having a thickness of 0.5 to 6 mm for a support (39) for joining the axis of the spiral injection pipe and the axis of the spiral mixing pipe and also joining the axis of the mixing pipe and the extension pipe. Alternatively, using a synthetic resin, a support (39) inscribed at three or four locations is provided on the inner surface of the mixing tube and the extension tube, and the tip of the support (39) inscribed in the mixing tube or the extension tube is 0.5 to A curved surface having a radius of 3 mm, and the length in the axial direction of the tube is 20% to 100% of the diameter of the mixing tube or the expanding tube, and 35 to 100% of the outer circumference of each of the injection tube and the mixing tube. The area obtained by multiplying the length by the length of 0.3 to 3 times the diameter of the injection tube and the mixing tube is adhered and held on the outside of each of the injection tube and the mixing tube. Claim 1, Claim 2, Claim 3, Claim 4, Claim 4
The aggregating device according to claim 5, claim 5, or claim 6. 8. An apparatus for preventing fine particles in a contaminated liquid from separating small particles in a spiral downcomer (23) from giant flocs grown in a floc forming tank (7), comprising the steps of: A dispersion chamber (18) for storing and dispersing, a distribution chamber (30) for distributing the contaminated liquid, and a solid-liquid separation chamber (10) for separating fine particles from the contaminated liquid; and b) inside the solid-liquid separation chamber (10). Is provided with a floc forming tank (7) which is open upward, c) between the distribution chamber (30) and the floc forming tank (7), one end of which opens into the distribution chamber. A spiral volume increase pipe (2) having a volume increase pipe discharge port (31) having an opening for introducing the contaminated liquid and the other end opened in the floc forming tank (7).
8) and d) a mixing tube discharge port (one end of which has an opening opening into the dispersion chamber (18) to introduce the contaminated liquid and the other end opening into the volume expansion pipe (28)). 8) a spiral mixing tube (17) having an injecting liquid outlet (20) in the spiral injecting tube (19) for injecting an injecting tube (16) into the mixing tube downstream of the contaminated liquid flowing through the mixing tube; F) a flocculation device having a structure opened toward the direction; f) a spiral downcomer inlet (24) for guiding a huge floc to the solid-liquid separation chamber is opened at the top of the floc forming tank (7); When a spiral downcomer is installed in the solid-liquid separation chamber, a spiral downcomer is introduced to penetrate the bottom (9) of the floc forming tank, and an enlarged nozzle (11) is opened at the end thereof. H) or floc forming Spiral drop tube to the outside (2
When 3) is provided, penetrate the side wall of the flock forming tank (6)
The spiral downcomer that wraps around the outside of the flock forming tank prevents small particles from separating in the downcomer from the huge floc with a grooved structure with an enlarged nozzle at the end of the spiral downcomer that guides the huge floc to the solid-liquid separation chamber The coagulating and concentrating apparatus according to claim 1, claim 2, claim 3, claim 4, claim 5, claim 6, or claim 7. 9. Separation of fine particles from a giant floc from a contaminated liquid containing fine particles into a highly concentrated sludge grown further and a clear liquid by using the coagulating / concentrating apparatus according to claim 8) Injection liquid (liquid to be treated) (16) discharged from the spiral injection pipe (9) of the apparatus and a spiral mixing pipe (17)
The mixed liquid flowing through the inside (a liquid obtained by adding a liquid having a different electrolyte concentration to the liquid to be processed) (32) is brought into laminar flow contact, whereby fine particles in the contaminated liquid form flocs. ) The amount of the contaminated liquid 3 to 3 flowing through the expanding liquid collision mixing pipe in the spiral expanding pipe (28) with respect to the amount of the floc-containing liquid (1) discharged from the discharge port (8) of the spiral mixing pipe of the apparatus.
A floc group is formed by colliding with a 400-fold amount. C) Then, a fluidized bed is formed by discharging the floc from the discharge pipe (31) into the floc formation tank (7) and violently between the floc groups. The collision is repeatedly agglomerated for a short time of 0.5
It grows into a huge floc that becomes strong with a residence time of ６０60 minutes, and most of the feed solution is released as a supernatant (21) from the surface of the fluidized bed of the floc forming tank. D) A giant floc formed in the floc forming tank The floc group flows down the edge of the spiral downcomer opening (24) at the upper part of the forming tank as an overflow weir (4), and the inclination angle of the downcomer is 5 to 60.
And the outlet of the downcomer pipe is an expansion nozzle (11) with an expansion angle of 5 to 20 degrees. E) The discharge speed of the expansion pipe nozzle is preferably equal to or lower than the opening passage speed of the uppermost surface of the floc forming tank. Agglomerated and concentrated sludge layer (2) of huge flocks deposited in the solid-liquid separation chamber
2) When the giant floc that is held below the interface and descends in the downcomer is moved as a continuous moving layer of flocs with few air gaps, there are no small particles to be separated. F) The coagulated concentrated sludge layer deposited in the solid-liquid separation chamber. If the interface rises and comes to a position 3 to 7 times the diameter of the downcomer pipe from the outlet of the downcomer pipe, and the downward movement of the sludge in the downcomer pipe stops, the coagulated concentrated sludge scraped to the rake (3) will When the drawing pump (12) is operated and the coagulated and concentrated sludge layer interface is discharged to a depth twice the diameter of the spiral downcomer (23), the moving pump of the huge floc in the spiral downcomer is stopped by stopping the drawing pump. The coagulation / concentration apparatus and the coagulation / concentration method according to claim 8, wherein the coagulation / concentration apparatus is moved as a continuous phase without voids to eliminate exfoliated small particles. 10. A coagulation-concentrated sludge layer (2) in a solid-liquid separation chamber.
2) Above the separated small particle-containing liquid (5), which is separated from the giant floc and slightly deposited in a layer form, is sucked from the suction port (25) by the suction pump (26). Is returned to the distribution chamber (30) or the supply pipe of the bulk liquid and reaggregated in the floc forming tank through the bulk liquid impingement mixing pipe (27). The coagulating / concentrating apparatus and the coagulating / concentrating method according to claim 8 or 9, wherein the coagulating / concentrating sludge grown on the giant floc is separated into a supernatant liquid 21). 11. A suction for sucking a separated small particle-containing liquid (5) that separates from giant flocs and deposits in layers on the coagulated and concentrated sludge (22) having a specific gravity of 1.1 or more in the solid-liquid separation chamber. The suctioned small particles are sucked from the mouth (25) by the suction pump (26). B) The sucked exfoliated small particles are supplied to the re-coagulation tank (2). Perforated plate (13) with pores formed on the entire bottom of the tank
To the tank at a speed of 1.5 m ³ / m ³ min or less to cause the detached small particles to adhere to the highly concentrated sludge of the giant floc, and discharge the re-coagulation tank supernatant (15) from the tank. The coagulation / concentration apparatus and the coagulation / concentration method according to claim 8, claim 9, or claim 10. 12. The method according to claim 1, wherein the coagulation device, the liquid supply chamber and the spiral downcomer (hereinafter referred to as coagulation-downcomer) are installed in an existing solid-liquid separation chamber. The flocculated concentrated sludge grown on the giant floc is separated into a supernatant and a supernatant liquid.
2. The coagulation concentration device and coagulation concentration method according to 1. 13. A solid-liquid separation chamber (1) comprising a coagulation apparatus, a liquid supply chamber and a spiral downcomer (hereinafter referred to as a coagulation-downcomer) according to the present invention.
0) When there is no space for installing the coagulation-downcomer, the solid-liquid separation cylinder (54) incorporating the coagulation-downcomer is installed outside the existing solid-liquid separation chamber, and the side wall of the existing solid-liquid separation chamber is provided. Alternatively, when the outlet of the spiral downcomer is opened in the existing solid-liquid separation chamber on the bottom plate, in separating the highly coagulated sludge into highly concentrated sludge and a clear liquid in the existing solid-liquid separation chamber in which the sludge stays for a long time, B) The overflow weir (4) of the spiral downcomer pipe (23) is opened on the floc forming tank in the solid-liquid separation cylinder, and the huge floc descending from the overflow weir (4) is a series of flocs with few voids. B) The discharge port of the downcomer is an expansion pipe nozzle with an expansion angle of 5 to 40 degrees. C) The discharge speed of the expansion pipe nozzle is preferably equal to or lower than the opening passage speed of the uppermost surface of the floc formation tank. D) The interface of the coagulated and concentrated sludge layer deposited in the solid-liquid separation chamber is When the ascending concentrated sludge is stopped and the descending movement of the sludge in the descending pipe is stopped at a position 3 to 7 times higher than the diameter of the descending pipe from the outlet of the enlarged pipe nozzle, the drawing pump (12) is operated, and the flocculated concentrated sludge is operated. If the interface discharges to a depth of twice the diameter of the spiral downcomer, stop the extraction pump. E) Continuously move the moving bed of huge flocs in the tube from the spiral downcomer connected to the solid-liquid separation tube without voids. Phase, and transfer the flocculated sludge without separated small particles to the solid-liquid separation chamber. F) The concentration of the flocculated sludge from the floc formation tank to the existing solid-liquid separation chamber is high, It is impossible to collect accumulated sludge within a specified time (no denitrification occurs), and the total floor area of the existing solid-liquid separation chamber is 40 to 20.
%, Wherein the slant angle of the central floor area is set to a steep angle of 25 to 55 degrees to discharge the highly concentrated sludge downhill on the inclined surface. Equipment and coagulation concentration method.