JP2010184179A - Coagulation sedimentation equipment - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide coagulation sedimentation equipment capable of achieving the improvement of the rate of coagulation sedimentation treatment, uniformity of scattering of to-be-treated water into a tank, early formation of a slurry blanket layer during operation of the equipment, improvement of the solid concentration of the sludge drawn from the tank and securement of clear quality of treated water. <P>SOLUTION: The coagulation sedimentation equipment clarifies target water by sedimenting suspended matter and flocculation floc in the target water in the tank so as to form a slurry blanket layer and includes a chamber arranged in the tank and introduced with the target water, a distributer arranged at the lower end of the chamber in a rotatable way and having a blow-off tube which has a blow-off hole discharging the target water in the chamber toward the lower part of the tank and a baffle board arranged below the blow-off hole and rotating with the distributer. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

  The present invention relates to a coagulating sedimentation apparatus that settles and separates suspended substances and coagulated floc in water to be treated and forms a slurry blanket layer to clarify the water to be treated.

  When treating water to be treated that contains a lot of suspended solids in wastewater treatment or water treatment, add aluminum-based flocculants such as polyaluminum chloride and iron-based flocculants such as ferric chloride. Then, a coagulation sedimentation process is performed in which suspended substances in the water to be treated are flocked to perform sedimentation separation. In addition, when water to be treated containing an ionic substance such as fluorine is to be treated, it is reacted with a calcium agent to form calcium fluoride (solid matter), and then the flocculant is added. Then, a coagulation sedimentation process for performing sedimentation separation is performed.

  In the above coagulation sedimentation treatment method, in order to treat fluorine to a high degree, it is necessary to add a large amount of an inorganic coagulant such as an aluminum-based coagulant, but if a large amount of the coagulant is added, the sludge generated by the coagulation sedimentation treatment The dehydration property is poor, and there is a problem that the amount of cake after sludge dewatering becomes very large.

  Therefore, a method called a sludge circulation method has been adopted as a method for reducing the amount of cake after sludge dewatering. This is because part of the sludge after the coagulation sedimentation treatment is returned to the calcium reaction tank or inorganic flocculant reaction tank provided in the preceding stage, thereby increasing the sludge concentration and increasing the density, and improving the sludge cohesiveness and dewaterability. This is a method in which the moisture content is reduced (see, for example, Patent Documents 1 and 2).

  In addition, in the above sludge circulation method, in recent years, sludge regeneration treatment is performed by adding an alkali agent such as slaked lime or sodium hydroxide, or an acid agent such as sulfuric acid to the sludge to be returned in order to reduce the amount of inorganic flocculant added. Then, a method of returning to a calcium reaction tank, an inorganic flocculant reaction tank or the like is employed (see, for example, Patent Documents 3 and 4). By treating the sludge with an alkali or acid agent, the aluminum hydroxide derived from the flocculant in the sludge is dissolved, and the adsorbed fluorine is released. The released fluorine reacts with calcium in sludge, or calcium in slaked lime or calcium chloride added for pH adjustment during sludge regeneration to form calcium fluoride. The aluminum salt regenerated in this way is returned to the inorganic flocculant reaction tank and reused as the flocculant. As a result, the amount of the flocculant used can be significantly reduced, the quality of the treated water can be improved, the concentration and dewaterability of the generated sludge can be improved, and the processing equipment can be downsized.

  In the coagulation sedimentation process, a slurry blanket type sedimentation tank is often used for sedimentation separation of suspended substances in the water to be treated. The slurry blanket type sedimentation tank is an upflow type sedimentation tank, and a suspended and fluidized sludge layer called a slurry blanket layer is formed in the middle of the sedimentation tank, and the upward flow in the tank Accompanying fine flocs and other fine particles are captured by a slurry blanket layer to clarify the water to be treated. Such a slurry blanket type sedimentation tank can obtain better treated water quality than a normal upward flow type sedimentation tank that does not form a slurry blanket layer, and has a high linear velocity (LV) of 3 to 10 m / h. Have.

  For example, Patent Document 5 discloses a sludge blanket type that is connected to a chamber provided in a tank and is rotatable around a central axis of the chamber and has a distributor that discharges water to be treated from the chamber into the tank. A coagulating sedimentation device has been proposed.

  Further, for example, Patent Document 6 proposes a sludge blanket type coagulating sedimentation apparatus in which a distributor for discharging water to be treated is disposed in the vicinity of an interface position of a sludge zone formed by storing sludge at the bottom of a tank. ing.

  Further, for example, in Patent Document 7, an inflow water receiving tank is installed in a separation tank, and the upper part of the inflow water receiving tank is a first chamber and the lower part is a second chamber. The side wall is horizontally separated from the entire circumference, and a funnel-shaped flow straightening plate is installed below the inflow water receiving tank. The funnel-shaped flow straightening plate has an upper end in contact with the entire circumferential separation tank side wall, and a lower end is A coagulating sedimentation apparatus has been proposed in which the diameter is narrower than the upper end and is separated from the separation tank side wall.

Japanese Patent Publication No. 7-36911 JP 2001-9468 A JP 2005-296838 A Japanese Patent No. 2930594 Japanese Patent No. 2919462 Japanese Patent No. 3463493 Japanese Patent No. 3856314

  In the coagulation sedimentation apparatus of Patent Document 5, the water to be treated can be uniformly distributed in the tank, and clear treated water can be obtained even at a high LV. However, when the apparatus is in operation, it is stored at the bottom of the tank. It is difficult to form a slurry blanket layer early by floating the sludge immediately.

  Moreover, in the coagulation sedimentation apparatus of patent document 6, it is possible to form the slurry blanket layer at an early stage by immediately floating the sludge stored in the tank bottom during operation of the apparatus. However, when the apparatus is stopped, sludge accumulates on the distributor and the outlet of the distributor is blocked. Further, when the apparatus is in operation, the water to be treated is always sprayed onto the sludge at the bottom of the tank, the sludge is disturbed by the water to be treated, and the solid content concentration of the sludge drawn from the bottom of the tank becomes thin. In particular, when applied to a coagulation sedimentation process (for example, Patent Documents 3 and 4) involving a sludge circulation regeneration method, a sufficient coagulation effect may not be obtained at the return destination because the solid concentration of sludge is thin. In addition, in order to increase the coagulation effect, a circulation pump with a large capacity is required, which may increase the processing cost.

  Moreover, in the coagulation sedimentation apparatus of patent document 7, the sludge in a tank can be floated immediately at the time of operation of an apparatus, and a slurry blanket layer can be formed at an early stage. However, since there is only one outlet of the distributor and it is fixed, when the treatment flow rate of the treated water is large and the coagulation sedimentation tank becomes large, the uniform dispersibility of the treated water in the layer is Deteriorate. In particular, when applied to a coagulation sedimentation process (see, for example, Patent Documents 3 and 4) involving a sludge circulation regeneration method in which the flocs to be generated are heavy and the treated water SS is required to have a clear treated water quality of 10 mg / L or less. In the vicinity of the side wall, the floating of the floc is poor, and there are cases where a clear treated water quality cannot be obtained.

  Therefore, the purpose of the present invention is to improve the coagulation sedimentation treatment rate, the uniform dispersibility of the water to be treated in the tank, the early formation of a slurry blanket layer during the operation of the apparatus, the improvement of the solid matter concentration of the sludge drawn from the tank, An object of the present invention is to provide a coagulation sedimentation apparatus capable of ensuring a clear quality of treated water.

  (1) The present invention is a coagulation sedimentation apparatus for clarifying the water to be treated by settling and separating suspended substances and coagulated floc in the water to form a slurry blanket layer. A chamber into which the water to be treated is introduced, and a blowout hole that is rotatably disposed at the lower end of the chamber and discharges the water to be treated in the chamber downward in the tank. A distributor having a blowing pipe, and a baffle plate installed below the blowing hole and rotating together with the distributor.

  (2) In the coagulation sedimentation apparatus described in (1) above, sludge extraction means for extracting the sludge accumulated on the bottom of the tank to the outside of the tank, and water to be treated in which a part of the extracted sludge is introduced into the tank. Or the sludge return means which returns in the tank of a position higher than the said baffle plate is provided.

  (3) In the coagulation sedimentation apparatus described in (1) or (2) above, it is preferable to include a scraper that scrapes sludge accumulated on the bottom of the tank.

  (4) In the coagulation sedimentation apparatus according to any one of (1) to (3) above, an interfacial meter for detecting the interfacial position of the slurry blanket layer, and the sludge extraction means include: It is preferable to include an adjusting unit that adjusts the amount of sludge withdrawn from the bottom of the tank based on the detected value.

  (5) The treatment apparatus for fluorine-containing water shown in the present embodiment includes a calcium reaction tank that forms calcium fluoride by adding a calcium agent to fluorine-containing water to produce first treated water containing calcium fluoride, An inorganic agglomeration reaction tank for adding an aluminum salt to the first treated water to cause the calcium fluoride to flocculate and form a second treated water containing the aggregated flocked calcium fluoride; A flocculating sedimentation device that settles and separates suspended matter and flocculated calcium fluoride, forms a slurry blanket layer to clarify the water to be treated, and acid or alkali on the sludge deposited on the bottom of the flocculation sedimentation device And a recycle treatment tank that regenerates the sludge, and a circulation reactor that supplies the regenerated sludge to either the calcium reaction tank or the inorganic agglomeration reaction tank. And a down, the coagulating sedimentation apparatus is a coagulation-sedimentation apparatus according to any one of the above (1) to (4).

  According to the coagulation sedimentation apparatus of the present invention, the uniform dispersibility of the water to be treated in the tank, the early formation of a slurry blanket layer during the operation of the apparatus, the improvement of the solids concentration of the sludge drawn from the tank, the clear treated water quality Securement can be achieved.

It is a schematic diagram which shows an example of a structure of the processing apparatus of fluorine-containing water. (A) is a schematic side view illustrating an example of the configuration of the coagulation sedimentation apparatus according to the present embodiment, and (B) is a schematic top view illustrating an example of the configuration of the coagulation sedimentation apparatus according to the present embodiment. It is a side surface schematic diagram which shows another example of a structure of the coagulation sedimentation apparatus which concerns on this embodiment. (A) is a side surface schematic diagram which shows another example of the structure of the coagulation sedimentation apparatus which concerns on this embodiment, (B) is an upper surface schematic diagram which shows another example of the structure of the coagulation precipitation apparatus which concerns on this embodiment. FIG. It is a schematic diagram which shows the structure of the processing apparatus used by the Example and the comparative example.

  In the present embodiment, the coagulation sedimentation apparatus according to the present embodiment will be described based on the treatment of fluorine-containing water using the sludge circulation method. The coagulation sedimentation apparatus of this embodiment is an example for carrying out the present invention, and the present invention is not limited to the treatment of fluorine-containing water using a sludge circulation method.

  FIG. 1 is a schematic diagram illustrating an example of a configuration of a treatment apparatus for fluorine-containing water. As shown in FIG. 1, the treatment apparatus 1 for fluorine-containing water includes a calcium reaction tank 10, an inorganic flocculation reaction tank 12, a polymer flocculation reaction tank 14, a coagulation sedimentation apparatus 16, and a sludge regeneration tank 18.

  The calcium reaction tank 10 is connected to a fluorine-containing water supply line 20 that supplies fluorine-containing water, which is water to be treated, and a calcium agent supply line 22 that supplies calcium agent. Then, in the calcium reaction tank 10, the fluorine-containing water and the calcium agent react to form calcium fluoride. In this embodiment, the calcium reaction tank 10 is connected with a pH adjuster addition line 24 for supplying a pH adjuster such as caustic soda, and a stirring device 26 is installed in the calcium reaction tank 10. These are optional. In addition, even if it supplies to the calcium reaction tank 10 after providing the pH adjustment tank in the front | former stage of the calcium reaction tank 10, adjusting the pH of the liquid mixture of to-be-processed water and a calcium agent (for example, adjusting to pH7). Good.

  The fluorine-containing water in the present embodiment may be water of any origin as long as it contains fluorine. For example, wastewater discharged from the electronics industry including the semiconductor-related industry, the power plant, the aluminum industry, etc. However, it is not limited to these.

  The calcium agent is not particularly limited as long as it can generate calcium fluoride, and examples thereof include calcium hydroxide, calcium chloride, calcium carbonate, and the like, but are not limited thereto.

  After the formation of calcium fluoride, the first treated water containing calcium fluoride is supplied to the inorganic agglomeration reaction tank 12 via the first treated water supply line 28. An inorganic flocculant addition line 30 for supplying an inorganic flocculant such as an aluminum salt is connected to the inorganic agglomeration reaction tank 12. In the inorganic agglomeration reaction tank 12, the inorganic flocculant adsorbs the fluorine that remains without reacting with the calcium agent, and the calcium fluoride in the water to be treated is agglomerated and flocked. Moreover, although the stirring apparatus 32 is installed in the inorganic aggregation reaction tank 12, installation of this stirring apparatus 32 is arbitrary. Further, a sludge circulation line 34 is connected to the inorganic agglomeration reaction tank 12, and regenerated sludge described later is supplied to the inorganic agglomeration reaction tank 12 through the sludge circulation line 34. The sludge circulation line 34 may be connected to the calcium reaction tank 10 described above, and regenerated sludge may be added to the calcium reaction tank 10.

  As the inorganic flocculant such as an aluminum salt, any known flocculant can be used as long as it functions as a flocculant capable of aggregating and flocking calcium fluoride. For example, PAC, sulfate band However, it is not limited to these.

  Next, the second treated water containing coagulated flocked calcium fluoride is supplied to the polymer agglomeration reaction tank 14 via the second treated water supply line 36. A polymer flocculant addition line 38 for supplying a polymer flocculant is connected to the polymer flocculent reaction tank 14. The polymer flocculant supplied from the polymer flocculant addition line 38 is added to and mixed with the second treated water in the polymer flocculation reaction tank 14, so that the coagulability of calcium fluoride in the second treated water is increased. It can be further increased. Thereby, the fine calcium fluoride (suspended substance) that has not been aggregated in the inorganic aggregation reaction tank 12 is aggregated and flocked. Moreover, although the stirring apparatus 40 is installed in the polymer agglomeration reaction tank 14, the installation of the stirring apparatus 40 is optional.

  As the polymer flocculant, any polymer that further improves the flocculence of calcium fluoride generated by adding the inorganic flocculant in the inorganic flocculent reaction tank 12 can be used. For example, anionic polymer organic Examples thereof include, but are not limited to, a flocculant, a nonionic polymer organic flocculant, and a polymer organic flocculant having a cationic group.

  Examples of the anionic high molecular organic flocculant include alginic acid or a salt thereof, carboxymethylcellulose, a polymer of acrylic acid or a salt thereof, a copolymer of acrylic acid or a salt thereof and acrylamide, and the like. Is not to be done. Examples of nonionic high molecular organic flocculants include, but are not limited to, polymers of acrylamide. Examples of the polymer organic flocculant having a cationic group include, but are not limited to, cationic organic coagulants, cationic polymer organic flocculants, and amphoteric polymer organic flocculants. .

  The third treated water containing calcium fluoride coagulated and flocked in the polymer coagulation reaction tank 14 is supplied to the coagulating sedimentation device 16 via the third treated water supply line 42. Although the configuration and operation of the coagulation sedimentation device 16 will be described in detail later, in the tank, calcium fluoride in the third treated water is deposited on the tank bottom as sludge, and the third treated water is formed in the tank. After passing through the slurry blanket layer, it is clarified and becomes the final treated water. The final treated water is taken out from the treated water discharge line 44 connected to the coagulation sedimentation apparatus 16.

  A sludge extraction line 46 is connected to the bottom of the coagulation sedimentation device 16. The sludge extraction line 46 is provided with a sludge extraction pump 48. Then, by operating the sludge extraction pump 48, sludge containing calcium fluoride deposited on the bottom of the tank is extracted from the sludge extraction line 46. The sludge extraction line 46 is connected to the sludge storage tank 50, and a part of the sludge flowing through the sludge extraction line 46 is supplied to the sludge storage tank 50.

  As will be described in detail later, a sludge return line 47 is connected to the sludge extraction line 46, and a part of the sludge flowing through the sludge extraction line 46 passes through the sludge return line 47 and enters the coagulation sedimentation apparatus 16. Will be returned.

  Further, a sludge circulation line 34 is connected to the sludge extraction line 46, and a part of the sludge flowing through the sludge extraction line 46 passes through the sludge circulation line 34 and is regenerated in the sludge regeneration tank 18, and is regenerated as sludge. It is returned to the inorganic agglomeration reaction tank 12 (or the calcium reaction tank 10). A sludge regeneration tank 18 interposed in the sludge circulation line 34 is connected with a regenerated sludge agent addition line 52 for adding an acid or alkali regenerated sludge agent. Then, the regenerated sludge agent is added from the regenerated sludge agent addition line 52 to the sludge regeneration tank 18, and the sludge and the regenerated sludge agent are mixed and regenerated. In addition, although the stirring apparatus 54 is installed in the sludge reproduction | regeneration tank 18, installation of this stirring apparatus 54 is arbitrary.

  When an acid is used as the regenerated sludge agent used for the regeneration treatment, the acid to be used is not particularly limited, and examples thereof include hydrochloric acid, sulfuric acid, nitric acid and the like. In addition, when alkali is used as the regenerated sludge agent, the alkali to be used is not particularly limited, and examples thereof include sodium hydroxide, calcium hydroxide, etc., but calcium hydroxide is used for the regeneration treatment. Is preferred. This is because calcium hydroxide can be used as a calcium source, and fluorine released from dissolved aluminum can be converted into calcium fluoride by calcium hydroxide.

  In this way, the treatment of fluorine-containing water is performed, and the configuration and operation of the coagulation sedimentation apparatus will be specifically described below.

  2A is a schematic side view showing an example of the configuration of the coagulation sedimentation apparatus according to the present embodiment, and FIG. 2B is a schematic top view showing an example of the configuration of the coagulation sedimentation apparatus according to the present embodiment. FIG. As shown in FIGS. 2 (A) and 2 (B), the sedimentation tank 56 of the coagulation sedimentation apparatus 16a is cylindrical, and the bottom of the sedimentation tank 56 is shaped like a hopper that becomes lower toward the center. A pit 58 for collecting sludge is provided in the center of the bottom. The shape of the sedimentation tank 56 is not limited to a cylindrical shape, and may be a polygonal shape or the like.

  A chamber 60 is provided in the sedimentation tank 56 of the coagulation sedimentation apparatus 16a. The chamber 60 is a cylindrical body and is disposed at the center of the settling tank 56. A third treated water supply line 42 is connected to the chamber 60.

  A distributor 64 fixed to a shaft 62 that passes through the chamber 60 is provided at the lower end of the chamber 60. The distributor 64 is rotated by driving the motor 66. The distributor 64 has a plurality of blow-out pipes 68, and a plurality of blow-out holes 70 for discharging the water to be treated in the chamber 60 downward in the settling tank 56 are formed at the bottom of each blow-out pipe 68. Has been.

  In the settling tank 56, a baffle plate 72 that is installed below the blowing hole 70 of the distributor 64 and rotates together with the distributor 64 is provided. This baffle 72 is suspended and fixed to the distributor 64 via a support 73 (FIG. 2B), and is disposed directly below the blowout hole 70.

  A sludge extraction line 46 is connected to a pit 58 provided at the center of the bottom. The sludge extraction line 46 is provided with a sludge extraction pump 48 as a sludge extraction means. Further, a sludge return line 47a as a sludge return means is connected between the sludge extraction line 46 and the sedimentation tank 56. However, the sediment tank 56 side end part of the sludge return line 47a is arrange | positioned in the tank of a position higher than a baffle plate.

  Next, operation | movement of the coagulation sedimentation apparatus 16a which concerns on this embodiment is demonstrated.

  First, third treated water (treated water) containing coagulated flocked calcium fluoride is supplied from the third treated water supply line 42 into the chamber 60 of the settling tank 56. And the 3rd process water in the chamber 60 is discharged on the baffle plate 72 (stage surface 72a) from the blowing hole 70 of the distributor 64 which rotates, and an upflow is generated. In the ascending flow of the third treated water, coarse aggregated flocs settle and separate by gravity and accumulate on the bottom of the settling tank 56 to form sludge. In addition, a suspended and fluidized slurry blanket layer A made of calcium fluoride or the like is formed in an intermediate portion of the settling tank 56. By the slurry blanket layer A, fine suspended substances contained in the upward flow of the third treated water are captured. And the 3rd treated water which passed the slurry blanket layer A turns into the clear supernatant water B from which the suspended substance and the aggregation floc were removed. And the supernatant water of the upper part of the sedimentation tank 56 is taken out from the treated water discharge line 44. In the present embodiment, the third treatment water discharged from the blowing hole 70 is blown against the sludge accumulated on the bottom of the tank by the baffle plate 72, and the sludge is prevented from being rolled up. It is possible to suppress the concentration reduction.

  Further, when the apparatus is stopped, the suspended matter forming the slurry blanket layer A accumulates as sludge on the baffle plate 72 (stage surface 72a). Therefore, when the apparatus is in operation, the third treated water discharged from the blowing hole 70 is sprayed on the sludge accumulated on the baffle plate 72 (stage surface 72a), so that the slurry blanket layer A can be formed at an early stage. It becomes possible. Thereby, clear supernatant water (final treated water) can be obtained at an early stage.

  Furthermore, in this embodiment, when the apparatus is in operation, the sludge extraction pump 48 is operated, the sludge accumulated at the bottom of the settling tank 56 is extracted from the sludge extraction line 46, and the on-off valve of the sludge return line 47a is opened. Then, the sludge is supplied into the tank above the baffle 72 from the sludge return line 47a. As a result, the sludge is transported to the upward flow of the water to be treated and contributes to the formation of the slurry blanket layer A. Therefore, the slurry is formed earlier than the formation of the slurry blanket layer A by only the sludge accumulated on the baffle plate 72. The blanket layer A can be formed.

  Next, the configuration of each unit will be described.

  The distributor 64 of the present embodiment is rotated by driving the motor 66. And when the distributor 64 rotates, the uniform dispersibility of the to-be-processed water in a tank is maintained. Therefore, the disturbance of the interface of the slurry blanket layer A formed in the tank is reduced, and it becomes possible to obtain good treated water quality.

  The outlet hole 70 of the distributor 64 of the present embodiment is preferably opened so that the water to be treated is discharged downward, and is thus less likely to be blocked by sludge in the sedimentation tank 56. The rotational speed of the distributor 64 is preferably in the range of 0.2 rpm to 2 rpm from the viewpoint of uniform dispersibility of the water to be treated in the settling tank 56. If the rotational speed of the distributor 64 is less than 0.2 rpm, the uniform dispersibility of the water to be treated may decrease. If it exceeds 2 rpm, the capacity of the motor 66 increases and the processing cost increases, or the motor 66 In some cases, an excessive load may be applied to cause damage.

  It is preferable that the number of the blow-out pipes 68 of this embodiment is at least two or more, and in order to balance the rotation, the number of the blow-out pipes 68 may be an even number that can be arranged at a symmetrical position around the distributor 64. More preferred. Specifically, although depending on the amount of treated water, 2 to 8 is preferable in that the treated water can be ejected vigorously from the blowing hole 70 and the sludge accumulated on the baffle 72 can be suspended. . Moreover, although the diameter of the blowing pipe 68 depends on the amount of treated water, if it is too thin, it is preferable that the diameter is 40 mm or more because the pipe may be blocked by a floc in the water to be treated and the pressure loss increases. Further, the horizontal length of the blow-out pipe 68 is not particularly limited, but when the sedimentation tank 56 has a large diameter, a plurality of blow-outs are provided so that the water to be treated is uniformly dispersed throughout the tank. Of the tubes 68, it is preferable to change the lengths of some of the blow-out tubes 68 in the horizontal direction.

  By providing the baffle plate 72 below the blowout hole 70 as in the present embodiment, the water to be treated discharged from the blowout hole 70 hits the baffle plate 72 to create an upward flow that is dispersed throughout the tank. Therefore, the number of the blow pipes 68 can be reduced and the diameter of the blow pipe 68 can be increased. As a result, the blowout hole 70 is hardly blocked by the sludge in the settling tank 56. Further, with the above configuration, when the apparatus is stopped, the water to be treated discharged from the blow-out hole 70 immediately floats the sludge accumulated on the stage surface 72a of the baffle 72 and forms the slurry blanket layer A at an early stage. Therefore, it is possible to obtain good treated water quality immediately after restarting. Moreover, in this embodiment, the to-be-processed water discharged from the blowing hole 70 by the baffle plate 72 is suppressed from being directly injected by the sludge deposited on the tank bottom part. As a result, it becomes possible to improve the solid content concentration of the sludge deposited on the tank bottom.

  The shape of the baffle plate 72 is preferably a shape such as a circle or a square because the water to be treated discharged from the blowout hole 70 is all in contact with the shape and the manufacturing is easy. Further, it is preferable that the baffle plate 72 is disposed at a predetermined interval downward from the blowing hole 70 so that the water to be treated discharged from the blowing hole 70 becomes an upward flow dispersed throughout the tank. For example, it is preferable that the cross-sectional area of the blowout hole 70 is arranged with an interval of 1 to 5 times.

  Further, the area of the baffle plate 72 is not particularly limited as long as the water to be treated discharged from the blowout hole 70 is of a size that can be prevented from being directly injected into the sludge accumulated at the bottom of the tank. Is preferably at least equal to or greater than the cross-sectional area of the blow-out hole 70, and more preferably at least twice the cross-sectional area of the blow-out hole 70. However, if the area of the baffle plate 72 is too large, the aggregated floc in the tank is blocked by the baffle plate 72 and cannot move to the tank bottom without delay. Therefore, the area of the baffle plate 72 is preferably 50% or less with respect to the horizontal sectional area of the settling tank 56.

  In the present embodiment, a part of the sludge accumulated at the bottom of the tank is put on the upward flow of the water to be treated to form the slurry blanket layer A at an early stage, and a part of the extracted sludge is higher than the baffle 72. When returning to the tank at the position, as shown in FIG. 2, the tank inner end of the sludge return line 47a is disposed above the baffle 72, and the sludge is supplied directly from the sludge return line 47a into the tank. Alternatively, for example, the tank inner end of the sludge return line 47a may be connected to the chamber 60, and sludge may be supplied into the tank from the sludge return line 47a via the chamber 60. Even in such a configuration, since the returned sludge is carried upward by the rising flow of the water to be treated, the slurry blanket layer A can be formed at an early stage during operation of the apparatus. In particular, when the apparatus is in operation, the slurry blanket layer A is formed only by the sludge accumulated on the baffle plate 72, but the extracted sludge is returned from the sludge return line into the settling tank 56 to form the slurry blanket layer A. The slurry blanket layer A can be formed more quickly.

  In addition, as shown in FIG. 2, when supplying sludge directly from the sludge return line into the tank, it is preferable that the tank inner end of the sludge return line 47 a be disposed above the baffle plate 72. Thereby, contamination of the final treated water by sludge can be suppressed.

  In the present embodiment, an example in which a part of the extracted sludge is returned into the tank at a position higher than the baffle plate 72 has been described. However, a part of the sludge accumulated at the bottom of the tank is placed on the upward flow of the water to be treated. In order to form the slurry blanket layer A at an early stage, a part of the extracted sludge may be returned to the water to be treated introduced into the tank. One example will be described below.

  FIG. 3 is a schematic side view showing an example of the configuration of a coagulation sedimentation apparatus according to another embodiment of the present invention. In the coagulation sedimentation apparatus 16b shown in FIG. 3, about the structure similar to the coagulation precipitation apparatus 16a shown in FIG. 2, the same code | symbol is attached | subjected and the description is abbreviate | omitted. In the coagulation sedimentation apparatus 16b of this embodiment, the sludge return line 47b is connected from the sludge extraction line 46 to the third treated water supply line 42. Therefore, the sludge extraction pump 48 is operated, and the sludge extracted from the tank bottom is supplied from the sludge extraction line 46 to the third treated water supply line 42 through the sludge return line 47b. The sludge is supplied into the tank through the chamber 60 together with the water to be treated. And sludge becomes an upward flow with to-be-processed water, and the slurry blanket layer A is formed. Even with such a configuration, the slurry blanket layer A can be formed faster than the slurry blanket layer A is formed by only the sludge accumulated on the baffle plate 72 during operation of the apparatus.

  In the present embodiment, it is preferable that a scraper 76 that scrapes the sludge accumulated on the bottom of the settling tank 56 is provided at the bottom of the settling tank 56. In particular, when the diameter of the sedimentation tank 56 is large, the sludge can be discharged at a high concentration without delay by installing the scraper 76. The scraper 76 is fixed to the shaft 62 and rotates together with the distributor 64. Then, as the scraper 76 rotates, the sludge accumulated at the bottom of the settling tank 56 is scraped to the pit 58 at the center of the tank.

  FIG. 4A is a schematic side view illustrating another example of the configuration of the coagulation sedimentation apparatus according to the present embodiment, and FIG. 4B illustrates another example of the configuration of the coagulation sedimentation apparatus according to the present embodiment. FIG. Until now, as shown in FIG. 2 or 3, the distributor 64 includes a blowing pipe 68 extending in the horizontal direction and a blowing hole 70 formed along the longitudinal direction of the blowing pipe 68. Although described as an example, it is not necessarily limited thereto. For example, like the coagulation sedimentation apparatus 16c shown in FIG. 4, the blowing hole 84 is provided in the end surface of the blowing pipe 82, and the blowing pipe 82 is arranged so that the blowing hole 84 and the baffle plate 72 face each other (that is, The distributor 80 may be configured to extend downward from the lower end portion of the chamber 60 toward the baffle plate 72 (stage surface 72a) so that the blowing hole 84 and the stage surface 72a face each other. In addition, in this embodiment, although the blower tube 82 is bent, it is not restricted to this. The distributor 80 configured as shown in FIG. 4 is less likely to accumulate sludge on or in the distributor 80 than the distributor 64 configured as shown in FIG.

  The precipitation tank 56 is provided with an interface level meter 78 that can detect the interface position (height of the interface) of the slurry blanket layer A formed in the tank. The interface level meter 78 and the sludge extraction pump 48 provided in the sludge extraction line 46 are electrically connected. The interface level meter 78 is not particularly limited as long as the interface level of the slurry blanket layer A formed in the settling tank 56 can be detected, but the ultrasonic wave is emitted to the target object. It is preferable that the ultrasonic interface level meter measures the interface level of the slurry blanket layer A in the sedimentation tank 56 based on the time from reflection to return to the sensor.

  Next, operation | movement of the coagulation sedimentation apparatus 16c which concerns on this embodiment is demonstrated. In the coagulation sedimentation apparatus 16c shown in FIG. 4, the process of causing the suspended solids and coagulation flocs to settle and separating and forming the slurry blanket layer A to clarify the water to be treated is based on the coagulation sedimentation apparatus 16a of FIG. This is the same as the processing described above. Here, a means for adjusting the amount of sludge withdrawn on the bottom of the tank according to the interface position of the slurry blanket layer A will be described.

  In this embodiment, when the apparatus is in operation, the sludge extraction pump 48 is operated, and the sludge accumulated on the bottom of the settling tank 56 is extracted from the sludge extraction line 46. However, the sludge extraction pump 48 of the present embodiment determines the amount of sludge that has accumulated at the bottom of the settling tank 56 based on the interface level (interface height) of the slurry blanket layer A detected by the interface level meter 78. It has a function that can be adjusted. Thereby, the interface position of the slurry blanket layer A can be maintained in a certain range, and a stable treated water quality can be obtained. Specifically, when the interface level meter 78 detects that the interface level of the slurry blanket layer A in the settling tank 56 has reached a predetermined height, the sludge extraction pump 48 is operated for a predetermined time, The sludge extraction pump 48 is operated until the interfacial position is lowered to a height, or the operation / stop cycle of the sludge extraction pump 48 is repeated until the interfacial position is lowered to a predetermined height. Further, an on-off valve may be installed in the sludge extraction line 46, and the sludge extraction amount may be adjusted by changing the opening of the on-off valve instead of operating the sludge extraction pump 48. That is, when the interface level meter 78 detects that the interface level of the slurry blanket layer A in the settling tank 56 has reached a predetermined height, the on-off valve is opened for a predetermined time, or the interface level is reduced to a predetermined level. The on-off valve may be opened until it drops, or the open / close cycle of the on-off valve may be repeated until the interface level drops to a predetermined height.

  Here, the height of the interfacial position of the slurry blanket layer A formed in the settling tank 56 varies depending on the properties of the substance to be removed in the water to be treated, but to obtain a good quality of treated water (SS, turbidity). Is preferably 0.7 m or more from the baffle plate 72. The upper limit of the height of the interface position of the slurry blanket layer A is not particularly limited. However, if the height of the interface position of the slurry blanket layer A is made higher than necessary, the precipitation tank 56 needs to be made higher by that amount. Therefore, the height of the interface position of the slurry blanket layer A is preferably 2 m or less from the baffle plate 72.

  Hereinafter, although an example and a reference example are given and the present invention is explained more concretely in detail, the present invention is not limited to the following examples.

  FIG. 5 is a schematic diagram illustrating the configuration of the processing apparatus used in the examples and comparative examples. The treatment apparatus shown in FIG. 5 is obtained by an inorganic agglomeration reaction tank 86 in which water to be treated, polyaluminum chloride (PAC), and sodium hydroxide are mixed to agglomerate and flock calcium fluoride, and an inorganic agglomeration reaction tank 86. A polymer agglomeration reaction tank 88 in which treated water and an organic polymer (anionic polyacrylamide) are mixed to grow flocs, and a coagulation sedimentation apparatus for subjecting the treated water obtained by the polymer agglomeration reaction tank 88 to settling and separation. Prepare. In the coagulation sedimentation apparatus, the coagulation sedimentation apparatus 90 of Example 1, the coagulation sedimentation apparatus 92 of Comparative Example 1, and the coagulation sedimentation apparatus 94 of Comparative Example 2 are installed in parallel at the subsequent stage of the polymer coagulation reaction tank 88 to polymer coagulation. The treated water obtained from the reaction tank 88 was distributed and supplied to each coagulation sedimentation apparatus. The coagulation sedimentation apparatus 90 of Example 1 is the same apparatus as the apparatus shown in FIG. The coagulation sedimentation apparatus 92 of Comparative Example 1 is the same apparatus as shown in FIG. 2 except that the baffle plate 72 is not installed and the sludge return line 47a is not installed. The coagulation sedimentation apparatus 94 of Comparative Example 2 is the same apparatus as that of Comparative Example 1 except that the distributor 64 and the scraper 76 that scrapes the sludge accumulated on the bottom of the tank are integrated.

  In the sludge extraction line 46 of the coagulation sedimentation apparatus of Example 1 and Comparative Examples 1 and 2, an ultrasonic sludge concentration meter 96 that detects the solid matter concentration of the extracted sludge, and an integrated flow meter 98 that detects the amount of sludge extraction. Intervened. Further, the interface position of the slurry blanket layer formed in the tank was measured by an interface level meter 78, and the sludge accumulated on the tank bottom was drawn out so that the interface position was maintained at a height of 2 m from the center of the tank bottom. .

<Processing conditions>
Water to be treated: Groundwater in which calcium fluoride particles are suspended at 200 mg / L (SS: 200 mg / L)
Processed water flow rate: 16.5m ³ / h (adjusted by pump)
Treated water flow rate to the coagulating sedimentation device: 5.5 m ^{3 /} h (LV 5.0 m / h)
PAC added to the inorganic agglomeration reactor: 300 mg / L
Inorganic agglomeration reactor pH: 7.0
Addition amount of anionic polyacrylamide to polymer aggregation reaction: 2.5 mg / L

  In Example 1 and Comparative Examples 1 and 2, the 12-hour water flow for 12 hours and the 12-hour stop were taken as 1 cycle, and 10 cycles were performed. Even after the water flow was stopped, the scraper was kept rotating as much as possible so as not to impair the fluidity of the sludge. Furthermore, in Example 1, sludge was returned from the sludge return line into the tank for 3 minutes after the start of water flow in each cycle under the processing conditions of the water flow cycle.

<Test equipment>
Inorganic agglomeration reactor size: 1.5 m ³
Polymer agglomeration reactor size: 1.5 m ³
Coagulating sedimentation apparatus tank Size: φ1.2m × 4.0m (4.5m ^3, the effective precipitation area 1.1 m ²⁾

  Table 1 summarizes the average values of the solid matter concentration and the amount of extraction of sludge extracted from each coagulation sedimentation apparatus when the water to be treated was passed. As can be seen from Table 1, the solid concentration of the sludge extracted from the coagulation sedimentation apparatus of Example 1 is the highest at 28000 mg / L, and the solid concentration of the sludge extracted from the coagulation sedimentation apparatus of Comparative Example 1 is 25000 mg / L. The solid concentration of sludge extracted from the coagulating sedimentation apparatus of Comparative Example 2 was 17000 mg / L, which was considerably lower than that of Example 1. Along with this, the amount of sludge withdrawn was the smallest in the coagulating sedimentation apparatus of Example 1, followed by the few coagulating sedimentation apparatuses in Comparative Example 1, and the most coagulating sedimentation apparatus in Comparative Example 2.

  Like the coagulation sedimentation apparatus of Example 1, by providing a baffle plate directly under the distributor, the sludge accumulated at the bottom is concentrated almost without being disturbed by the jet of water to be treated discharged from the distributor. Therefore, the solid matter concentration of the sludge extracted from the coagulation sedimentation apparatus of Example 1 becomes high. On the other hand, in the coagulation sedimentation apparatus of Comparative Example 1, since the distributor is separated from the bottom of the tank but no baffle plate is provided, the sludge accumulated on the bottom is disturbed by the jet of water to be treated discharged from the distributor. Receive a little. Therefore, the solid matter concentration of the sludge of Comparative Example 1 is lower than that of Example 1. In the coagulation sedimentation apparatus of Comparative Example 2, since the distributor is near the bottom of the tank, the sludge accumulated on the bottom is wound up by the jet of water to be treated discharged from the distributor. Therefore, in the coagulation sedimentation apparatus of Comparative Example 2, the concentration of sludge does not proceed sufficiently, and the solid matter concentration of sludge becomes the lowest value. From these things, the coagulation sedimentation apparatus of Example 1 can fully concentrate sludge more than the coagulation sedimentation apparatus of the comparative examples 1 and 2, and can extract at high concentration, and can also reduce the amount of extraction sludge accordingly. Therefore, it becomes possible to reduce the capacity of the sludge storage tank installed in the subsequent stage.

  Table 2 summarizes the SS and turbidity average values of the supernatant water (final treated water) obtained from each coagulation sedimentation apparatus when the treated water was passed. This average value is an average value excluding the value for 1 hour after the start of water flow. The SS and turbidity of the supernatant water obtained from the coagulation sedimentation apparatus of Example 1 were comparable to those of Comparative Examples 1 and 2. That is, it was shown that the coagulation sedimentation apparatus of Example 1 has the same SS removal performance as that of the conventional coagulation sedimentation apparatus.

  Table 3 shows the maximum turbidity of the treated water and the time taken for the turbidity to decrease to 0.3 degrees (average value of 9 cycles) at the time of restarting after stopping for 12 hours. The highest turbidity of the treated water was 1.7 degrees at the lowest in the coagulation sedimentation apparatus of Example 1, and then 1.8 degrees of the coagulation sedimentation apparatus in Comparative Example 2. And the coagulation sedimentation apparatus of the comparative example 1 was the highest and was 3.2 degree | times. The time required for the treated water turbidity to drop to 0.3 degrees was 3 minutes, the shortest for the coagulating sedimentation apparatus of Example 1, and then 5 minutes for the coagulating sedimentation apparatus of Comparative Example 2. And the coagulation sedimentation apparatus of the comparative example 1 was 12 minutes longest.

  In the coagulation sedimentation apparatus of Example 1 and Comparative Example 2, the sludge near the distributor (the sludge accumulated on the baffle plate in the coagulation sedimentation apparatus of Example 1, the comparative example 2) by the jet of water to be treated discharged from the distributor. In the coagulating sedimentation apparatus, sludge accumulated on the bottom of the tank is immediately rolled up, and a slurry blanket layer is quickly formed. Therefore, even at the time of restarting, the SS / turbidity removal performance by the slurry blanket layer is exhibited early. In particular, in the coagulation sedimentation apparatus of Example 1, the sludge supplied from the sludge return line contributes to the formation of the slurry blanket layer, so that the slurry blanket layer is formed more quickly than the coagulation sedimentation apparatus of Comparative Example 2. Is possible. On the other hand, in the case of the coagulation sedimentation apparatus of Comparative Example 1, the sludge forming the slurry blanket layer has been sunk in the bottom of the tank away from the distributor due to the stop for a long time. Can not form. For this reason, the turbidity is temporarily high, and the time required for the turbidity to decrease to 0.3 degrees is also increased.

  Next, after 10 cycles of the water flow cycle, the state of blockage of the outlet holes of the distributor in each coagulation sedimentation apparatus was confirmed. As a result, in the coagulation sedimentation apparatus of Example 1 and the coagulation sedimentation apparatus of Comparative Example 1, the blowout holes were not blocked, but in the coagulation sedimentation apparatus of Comparative Example 2, the blowout holes were easily buried in sludge when the water flow was stopped. Of the 16 blowout holes, 2 blowout holes were closed.

  As described above, the coagulation sedimentation apparatus of Example 1 has the same processing performance as the conventional coagulation sedimentation apparatus such as the coagulation sedimentation apparatuses of Comparative Examples 1 and 2, while the conventional coagulation sedimentation apparatus has a problem. In other words, it was possible to solve problems such as a decrease in the solid content concentration of sludge, early securing of good treated water quality at the time of restart, blockage of the blowout holes, and the like.

  In Example 2, the treatment of fluorine-containing water was performed using an apparatus similar to the treatment apparatus shown in FIG. 1 (the coagulation sedimentation apparatus is shown in FIG. 4). Moreover, in Comparative Example 3, the treatment of fluorine-containing water was performed in the same manner as in Example 2 except that the coagulating sedimentation apparatus used in Example 2 was changed to the coagulating sedimentation apparatus used in Comparative Example 2.

<Processing conditions>
Water to be treated: water in which fluoride ions are suspended at 100 mg / L (SS <1 mg / L)
Processed water flow rate: 5.5 m ³ / h
LV of the coagulation sedimentation device: 5.0 m / h
Sludge circulation rate through the sludge circulation line: 0.5m ³ / h
Calcium chloride added to the calcium reaction tank: 1300 mg / L
PAC addition amount to the inorganic agglomeration reaction tank: 200 mg / L
Inorganic agglomeration reactor pH: 7.0
Anionic polyacrylamide added to the polymer agglomeration reactor: 2.0 mg / L
Polymer aggregation reactor pH: 7.0
Extraction of sludge accumulated at the bottom of the coagulation sedimentation apparatus: The sludge was extracted so that the height of the interface of the slurry blanket layer formed in the tank was maintained at 2 m from the bottom of the tank.

  In Example 2 and Comparative Example 3, the 12-hour water flow for 12 hours and the 12-hour stop were taken as one cycle, and this was performed for 10 cycles. Even after the water flow was stopped, the scraper was kept rotating as much as possible so as not to impair the fluidity of the sludge. Furthermore, in Example 2, sludge was returned from the sludge return line into the tank for 3 minutes after the start of water flow in each cycle under the processing conditions of the water flow cycle.

<Test equipment>
Calcium reaction tank size: 1.5m ³
Inorganic agglomeration reactor size: 1.5 m ³
Polymer agglomeration reactor size: 1.5 m ³
Coagulation sedimentation apparatus tank size: φ1.2 m × 4.0 m (4.5 m ³ , effective precipitation area 1.1 m ² )
Sludge regeneration tank: 0.3m ³
Sludge storage tank: 3m ³

  The solid matter concentration of the sludge extracted from the coagulation sedimentation apparatus of Example 2 and Comparative Example 3, the fluorine ion concentration remaining in the supernatant water (final treated water) obtained from the coagulation sedimentation apparatus of Example 2 and Comparative Example 3, and SS is summarized in Table 4. As can be seen from Table 4, the solid concentration of the sludge extracted from the coagulation sedimentation device of Example 2 is 59000 mg / L, whereas the solid concentration of the sludge extracted from the coagulation sedimentation device of Comparative Example 3 is It was 33000 mg / L. Accordingly, in Example 2, the concentration of aluminum whose coagulation ability has been regenerated by the sludge regeneration tank is inevitably higher than that of Comparative Example 3. As a result, the fluorine ion concentration of the supernatant water obtained from the coagulation sedimentation apparatus of Comparative Example 3 was 7.8 mg / L, whereas the fluorine ion concentration of the supernatant water obtained from the coagulation sedimentation apparatus of Example 2 was It was lower than Comparative Example 3 and reduced to 4.2 mg / L. In addition, SS of supernatant water was comparable in Example 2 and Comparative Example 3.

  DESCRIPTION OF SYMBOLS 1 Treatment apparatus, 10 Calcium reaction tank, 12,86 Inorganic coagulation reaction tank, 14,88 Polymer coagulation reaction tank, 16, 16a, 16b, 16c, 90, 92,94 Coagulation sedimentation apparatus, 18 Sludge reproduction tank, 20 Fluorine Contained water supply line, 22 Calcium agent supply line, 24 pH adjuster addition line, 26, 32, 40, 54 Stirrer, 28 First treated water supply line, 30 Inorganic flocculant addition line, 34 Sludge circulation line, 36 2 treated water supply line, 38 polymer flocculant addition line, 42 3rd treated water supply line, 44 treated water discharge line, 46 sludge extraction line, 47, 47a, 47b sludge return line, 48 sludge extraction pump, 50 sludge storage tank , 52 Recycled sludge additive line, 56 Sedimentation tank, 58 pits, 60 chambers, 62 shafts, 64 80 Distributor, 66 Motor, 68, 82 Blowout pipe, 70,84 Blowout hole, 72 Baffle plate, 72a Stage surface, 73 Support body, 76 Scraper, 78 Interface level meter, 96 Ultrasonic sludge concentration meter, 98 Integrated flow rate Total.

Claims (4)

In the tank, the suspended solids in the water to be treated, the aggregated floc is settled and separated, a slurry blanket layer is formed to clarify the water to be treated,
A chamber disposed in the tank and into which the water to be treated is introduced, and a blower that is rotatably disposed at the lower end of the chamber and discharges the water to be treated in the chamber downward in the tank. A coagulation sedimentation apparatus comprising: a distributor having a blowing pipe in which a hole is formed; and a baffle plate installed below the blowing hole and rotating together with the distributor.   It is a coagulation sedimentation apparatus of Claim 1, Comprising: The sludge extraction means which draws out the sludge accumulated in the bottom part in the said tank out of a tank, The to-be-processed water introduced into the said tank, or a part of the extracted sludge, or the said And a sludge return means for returning the sludge to a tank higher than the baffle.   The coagulation sedimentation apparatus according to claim 1 or 2, further comprising a scraper for scraping the sludge accumulated on the bottom of the tank.   It is a coagulation sedimentation apparatus of any one of Claims 1-3, Comprising: Based on the interface level meter which detects the interface level of the said slurry blanket layer, and the detected value of the said interface level meter, in the said tank A coagulating sedimentation apparatus comprising: adjusting means for adjusting an amount of sludge accumulated on the bottom.

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