JP2008000637A - Flocculation reaction apparatus - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a flocculation reaction apparatus capable of ensuring a high flocculation reaction efficiency in a wide range of a flow rate and enlarging a range of a treatment amount. <P>SOLUTION: In the flocculation reaction apparatus having a transferring pipe 4 for pressure-feeding suspended water, a small diameter pipe 5 continued to the transferring pipe 4 and having a smaller diameter than the transferring pipe 4, a flocculant feeding means provided on the small diameter pipe 5 or the transferring pipe 4 in its upstream side, and a flocculation reaction tank directly opened with the small diameter pipe 5, an area varying means 7 (flap plate 8 having a spring function) for increasing/decreasing a cross section area of the small diameter pipe 5 in proportional to the pressure of the suspended water flowing in the small diameter pipe 5 is provided. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a coagulation reactor for coagulating suspended water such as excess sludge discharged from a biological treatment process of organic wastewater such as sewage, and in particular, ensuring high coagulation reaction efficiency over a wide flow rate range. The present invention relates to an agglomeration reactor that can be used.

  When the excess sludge discharged from the biological treatment process of organic wastewater such as sewage is dehydrated, the dehydration is generally performed after flocs are formed by adding a flocculant to the sludge and coagulating.

  FIG. 10 is a schematic cross-sectional view showing a conventional agglomeration reaction apparatus 101 that performs an agglomeration treatment by adding an inorganic flocculant to sludge (raw mud). In this agglomeration reaction apparatus 101, the raw mud is a raw mud pump 103. Is introduced into the agglomeration reaction tank 102, the inorganic flocculant is added to the raw mud in the agglomeration reaction tank 102, and both are agitated and mixed by the agitator 106 to discharge the agglomerated sludge.

  By the way, strong agitation is necessary to react sludge and inorganic flocculant efficiently. However, strong agitation consumes a lot of power and is contaminated in sludge like mixed raw sludge of sewage. In the case of raw mud containing things, impurities may get entangled with the stirring blades and smooth stirring may be hindered.

  Therefore, an agglutination reaction apparatus 201 as shown in FIGS. 11 and 12 has been proposed (see Patent Document 1).

  FIG. 11 is a front view of the agglomeration reaction apparatus, and FIG. 12 is a cross-sectional view taken along the line EE of FIG. 11. The illustrated agglomeration reaction apparatus 201 is a raw mud pump 203 that transfers sludge (raw mud) to the agglomeration reaction tank 202. A small-diameter pipe 205 having a diameter smaller than that of the transfer pipe 204 is connected to the transfer pipe 204 having a diameter, and the small-diameter pipe 205 is connected to the outer peripheral portion of the agglomeration reaction tank 202 in a tangential direction. Here, the agglomeration reaction tank 202 is formed in a cylindrical container shape, and a stirrer 206 is provided therein.

  Thus, while the sludge is introduced into the agglomeration reaction tank 202 via the transfer pipe 204 and the small diameter pipe 205 by the raw mud pump 203, the inorganic flocculant is formed in the vicinity of the connecting portion between the transfer pipe 204 and the small diameter pipe 205. Is injected. The injected inorganic flocculant is uniformly dispersed and mixed in the sludge by the sludge turbulent flow in the small-diameter fine pipe 205, and the high-speed sludge flow passing through the fine-diameter pipe 205 enters the coagulation reaction tank 202. The inorganic flocculant is effectively mixed and diffused by the jet stream flowing in the tangential direction.

  Then, the sludge flow that flows in the tangential direction from the small diameter pipe 205 into the agglomeration reaction tank 202 becomes a swirl flow in the agglomeration reaction tank 202, and the inorganic flocculant is mixed with the sludge in the agglomeration reaction tank 202. Mixing and diffusing more uniformly, and flocs grow by agitation by the agitator 206 in the agglomeration reaction tank 202, so that a good agglomeration treatment is performed.

The agglomerated sludge obtained in the agglomeration reaction tank 202 as described above is discharged out of the agglomeration reaction tank 202 from the discharge pipe 209, and then an organic polymer flocculant is added and mixed to generate flock, and then To the dehydration process (not shown).
Japanese Patent No. 3539428

  Here, in the agglomeration reaction apparatus 201 shown in FIGS. 11 and 12, the flow rate Q and the injection speed v of the sludge injected into the agglomeration reaction tank 202 when a small diameter pipe (blow pipe) 205 having a diameter of 25 mm is used. The relationship is shown in FIG.

When the cross-sectional area of the small-diameter pipe 205 is S, the speed v is expressed by the following formula:
v = Q / S (1)
Therefore, it is apparent from FIG. 13 that the sludge injection speed v is directly proportional to the flow rate Q.

By the way, according to the knowledge of the present inventor, the reaction between the inorganic flocculant and the sludge is favorably performed when the sludge injection speed v is in the range of 2 to 5 m / sec. Therefore, from the relationship between the flow rate Q and the injection speed v shown in FIG. 13, the flow rate Q corresponding to the injection speed v = 2 to 5 m / sec is Q = 4 to 9 m ³ / h, and the processing amount within that range is desirable. I understand that. If the treatment amount is less than 4 m ³ / h, the stirring strength becomes weak and the reaction between the inorganic flocculant and the sludge becomes insufficient. Conversely, if the treatment amount exceeds 9 m ³ / h, the flocs formed tend to break down. In addition, there is a problem in that the pressure in the transfer pipe 204 and the small diameter pipe 205 becomes too high, which hinders the operation of the apparatus.

  However, in the conventional agglomeration reaction apparatus 201 shown in FIGS. 11 and 12, the diameter of the small-diameter pipe 205 is constant and the cross-sectional area S is also constant, so that the reaction between the inorganic flocculant and sludge is performed. There is a problem that the range of the processing amount (flow rate Q) for realizing the injection speed v that keeps good is narrow and the processing amount is limited.

  The present invention has been made in view of the above problems, and the intended treatment is to provide an agglomeration reaction apparatus capable of ensuring high agglomeration reaction efficiency in a wide flow rate range and expanding the range of throughput. There is to do.

In order to achieve the above object, the invention according to claim 1
A transfer pipe for pumping suspended water;
A smaller diameter pipe than the transfer pipe connected to the transfer pipe;
A flocculant supply means provided in the small-diameter pipe or the transfer pipe upstream thereof;
In an agglomeration reaction apparatus having an agglomeration reaction tank in which the small-diameter pipe opens directly,
An area variable means for increasing or decreasing the cross-sectional area of the small-diameter pipe in proportion to the pressure of the suspension water flowing through the small-diameter pipe is provided.

  A second aspect of the invention is characterized in that, in the first aspect of the invention, the area variable means is constituted by a flap plate having a spring function arranged in the small-diameter pipe.

  According to a third aspect of the present invention, in the first aspect of the present invention, the area variable means is screwed into a flap plate rotatably disposed in the small-diameter pipe so as to advance and retract. And the edge part was comprised including the volt | bolt connected with the said flap board.

  The invention according to claim 4 is characterized in that, in the invention according to claim 1, the area variable means is constituted by an elastically deformable taper tube whose diameter is reduced along the flow direction of the suspended water.

  According to a fifth aspect of the present invention, in the first aspect of the present invention, the area varying means is configured by a blow pipe partially configured by an elastic sheet that can be elastically deformed.

  A sixth aspect of the present invention is the invention according to any one of the first to fifth aspects, wherein a temporary retention part for agglomeration reaction having a larger cross-sectional area than the transfer pipe is provided at the downstream end of the small diameter pipe. The temporary retention portion is connected to the agglomeration reaction tank through a second transfer pipe and a second fine pipe having a smaller diameter than the second transfer pipe, and the second fine pipe is connected to the second fine pipe. An area variable means is provided.

  According to the first aspect of the present invention, since the cross-sectional area of the small-diameter pipe can be increased or decreased in proportion to the pressure of the suspended water flowing through the small-diameter pipe, the diameter of the small-diameter pipe increases as the flow rate of the suspended water increases. The cross-sectional area of the piping is increased, and the rate of increase of the injection speed is kept low. For this reason, the injection rate does not increase linearly in proportion to the increase in flow rate, and the rate of increase in the injection rate with respect to the increase in flow rate becomes slow, realizing an injection rate that keeps the reaction between the flocculant and sludge well. Therefore, the range of the processing amount (flow rate) to be expanded can be secured, and high agglomeration reaction efficiency can be ensured in a wide flow rate range.

  According to the second aspect of the present invention, when the flow rate of the suspended water increases and the pressure increases, the flap plate automatically elastically deforms due to the pressure and the cross-sectional area of the small-diameter pipe increases. The increase rate of the injection speed becomes slow, and the range of the processing amount (flow rate) for realizing the injection speed that keeps the reaction between the flocculant and the sludge good is expanded.

  According to the third aspect of the present invention, the bolt can be turned in accordance with the flow rate of the suspended water to rotate the flap plate in the small diameter pipe to manually increase or decrease the cross sectional area of the small diameter pipe. The rate of increase of the injection speed with respect to the increase in the pressure becomes slow, and the range of the processing amount (flow rate) for realizing the injection speed that keeps the reaction between the flocculant and sludge good can be expanded.

  According to the invention described in claim 4, when the flow rate of the suspension water increases and the pressure increases, the taper tube expands due to the pressure and the cross-sectional area increases. It becomes slow, and the range of the processing amount (flow rate) for realizing the injection speed that keeps the reaction between the flocculant and sludge good is expanded.

  According to the fifth aspect of the present invention, when the flow rate of the suspension water increases and the pressure increases, a part of the elastic sheet of the blowing pipe expands due to the pressure, and the cross-sectional area of the blowing pipe increases. The increase rate of the injection speed with respect to the increase becomes slow, and the range of the processing amount (flow rate) for realizing the injection speed that keeps the reaction between the flocculant and the sludge good is expanded.

  According to the sixth aspect of the present invention, since the temporary retention portion for the agglomeration reaction having a cross-sectional area larger than that of the transfer pipe is provided at the downstream end of the small diameter pipe, the suspension water is uniformly dispersed by the turbulent flow in the small diameter pipe. Aggregation reaction by the aggregating agent dispersed in is promoted in the temporary residence part. Then, the cross-sectional area of the second small-diameter pipe is increased or decreased in proportion to the pressure of the suspension water by the area variable means provided in the second small-diameter pipe having a smaller diameter than the second transfer pipe connected to the temporary retention section. Therefore, the rate of increase of the injection speed with respect to the increase of the flow rate becomes slow, and the range of the processing amount (flow rate) for realizing the injection speed that keeps the reaction between the flocculant and the sludge good is expanded.

  Embodiments of the present invention will be described below with reference to the accompanying drawings.

<Embodiment 1>
1 is a front view of an agglomeration reaction apparatus according to Embodiment 1 of the present invention, FIG. 2 is a cross-sectional view taken along line AA in FIG. 1, FIG. 3 (a) is an enlarged cross-sectional view of a portion B in FIG. FIG. 4B is a diagram showing a change in the cross-sectional area of the small-diameter pipe in the direction of arrow C in FIG. 3A, and FIG.

  The agglomeration reaction apparatus 1 shown in FIGS. 1 and 2 is provided with a small-diameter pipe 5 smaller in diameter than the transfer pipe 4 in a transfer pipe 4 having a raw mud pump 3 for transferring sludge (raw mud) to the agglomeration reaction tank 2. The small-diameter pipe 5 is connected to the outer peripheral portion of the agglomeration reaction tank 2 in the tangential direction. Here, the agglomeration reaction tank 2 is formed in a cylindrical container shape, and a stirrer 6 is provided therein. Although not shown, the agglomeration reaction apparatus 1 is provided with a flocculant supply means for adding an inorganic flocculant to the sludge flowing through the transfer pipe 4.

  By the way, in the present embodiment, as shown in FIG. 3, the small-diameter pipe 5 is formed into a rectangular cross section, and the fine-diameter pipe 5 has an opening area of sludge (accurately flowing through the fine-diameter pipe 5). Is provided with an area variable means 7 for increasing or decreasing in proportion to the pressure of the sludge and the inorganic flocculant mixture. In the present embodiment, the area varying means 7 is constituted by a flap plate 8 having a spring function disposed in the small-diameter pipe 5, and the flap plate 8 is bent up and down around the starting point 8a. .

  Thus, while the sludge is introduced into the agglomeration reaction tank 2 through the transfer pipe 4 and the small diameter pipe 5 by the raw mud pump 3, it is not shown in the vicinity of the connection portion between the transfer pipe 4 and the small diameter pipe 5. An inorganic flocculant is injected by the flocculant supply means. The injected inorganic flocculant is uniformly dispersed and mixed in the sludge by the sludge turbulent flow in the small-diameter fine pipe 5, and the high-speed sludge flow passing through the fine-diameter pipe 5 is agglomerated reaction tank 2. The inorganic flocculant is effectively mixed and diffused by the jet flow when flowing in the tangential direction.

  The agglomerated sludge obtained in the agglomeration reaction tank 2 as described above is discharged out of the agglomeration reaction tank 2 from the discharge pipe 9, and then the organic polymer flocculant is added and mixed to generate flocs. To the dehydration process (not shown).

  Here, in the present embodiment, as described above, the opening area of the small diameter pipe 5 is proportional to the pressure of the sludge flowing through the small diameter pipe 5 (more precisely, the mixture of sludge and inorganic flocculant). Since the flap plate 8 having a spring function is provided as the area varying means 7 to be increased or decreased, the flap plate 8 bends and deforms vertically around the starting point 8a in proportion to the sludge pressure flowing through the small diameter pipe 5. As the cross-sectional area S of the diameter pipe 5 increases and decreases, the sludge flow rate Q increases and the pressure P in the small diameter pipe 5 increases, the cross-sectional area S of the small diameter pipe 5 increases and the rate of increase of the sludge injection speed v ( dv / dQ) can be kept small.

Specifically, when the sludge flow rate Q is low and the pressure P is low, the tip of the flap plate 8 is at the solid line position a1 in FIG. 3 and the cross section of the small-diameter pipe 5 is narrowed by the flap plate 8. Since the cross-sectional area S of the small-diameter pipe 5 is reduced to S1 (see FIG. 3B), the sludge injection speed v is expressed by the following formula based on the small cross-sectional area S1:
v = Q / S1 (2)
Indicates the value obtained by.

Next, when the flow rate Q of sludge increases and the pressure P increases, the flap plate 8 is automatically bent upward about the starting point 8a by the pressure P, and the tip moves to the chain line position a2 in FIG. Since the flap plate 8 is opened, the cross-sectional area S of the small-diameter pipe 5 increases from S1 to S2 (see FIG. 3B). Thus, when the cross-sectional area S of the small-diameter pipe 5 increases from S1 to S2, the sludge injection speed v is expressed by the following formula:
v = Q / S2 (3)
The increase rate (dv / dQ) of the injection speed v with respect to the increase in the flow rate Q becomes slow.

  In the above, the relationship between the sludge flow rate Q (pressure P), the injection speed v, and the cross-sectional area S of the small-diameter pipe 5 when the flap 8 is at the positions indicated by a1 and a2 in the drawing has been described. The tip of the plate 8 moves to any position other than the illustrated a1 and a2 in accordance with the sludge flow rate Q (that is, the pressure P). It can be continuously changed to any value other than S2.

In other words, in the present embodiment, the cross-sectional area S of the small-diameter pipe 5 is not constant as in the prior art, but is a variable S (P) that changes according to the pressure P.
v = Q / S (P) (4)
The injection speed v obtained in step (3) does not change linearly in direct proportion to the flow rate Q as in the prior art (see FIG. 13), and the rate of increase (dv / dQ) with respect to the increase in the flow rate Q becomes slow. As shown, it changes in a quadratic curve with respect to the flow rate Q. For this reason, the range of the processing amount (flow rate Q) for realizing the injection speed v that keeps the reaction between the inorganic flocculant and sludge good can be expanded, and high agglomeration reaction efficiency can be secured in a wide flow rate range. Become.

  By the way, as described above, it has been found that the reaction between the inorganic flocculant and the sludge is favorably performed when the injection speed v is in the range of 2 to 5 m / sec.

FIG. 4 shows the relationship between the injection speed v and the flow rate Q obtained when the cross section of the small-diameter pipe 5 is □ 30 mm. As is clear from the figure, the agglomeration reaction apparatus 1 according to the present embodiment is shown in FIG. Accordingly, the flow rate Q corresponding to the injection speed v = 2 m / sec is Q = 2 m ³ / h, the flow rate Q corresponding to the injection speed v = 5 m / sec is Q = 16 m ³ / h, and the injection speed v = 2−2. The range of throughput (flow rate Q) for realizing 5 m / sec can be expanded to Q = 2-16 m ³ / h compared to the conventional Q = 4-9 m ³ / h (see FIG. 13). High agglomeration reaction efficiency can be secured in a wide flow rate range.

  Further, according to the agglomeration reaction apparatus 1 according to the present embodiment, even when the tip of the small diameter pipe 5 is clogged with impurities, the pressure P in the small diameter pipe 5 rises and the flap plate 8 Since it is deformed in the opening direction, the effect that the clogged impurities are blown along with the sludge flow is also obtained.

  By the way, there is a tendency for scale (scale) to adhere to the inside of the small-diameter pipe 5, and when the scale adheres, the cross-sectional area S of the fine-diameter pipe 5 is reduced, so that the sludge injection speed v increases (see FIG. 4 and FIG. 4). The characteristic curve shown in FIG. 13 moves to the small flow rate side (left side in the figure)).

  Therefore, conventionally, it was necessary to remove the scale by cleaning at a certain frequency. However, in the agglomeration reaction apparatus 1 according to the present invention, the rate of increase of the injection speed v with respect to the increase of the sludge flow rate Q (dv / dQ), Since the slope of the characteristic curve shown in FIG. 4 becomes slow, the frequency of cleaning can be kept low.

<Embodiment 2>
Next, a second embodiment of the present invention will be described with reference to FIGS.

  FIG. 5 is a front view of the coagulation reaction apparatus according to the present embodiment, and FIG. 6 is a cross-sectional view taken along the line DD of FIG. 5. In these figures, the same elements as those shown in FIGS. The same reference numerals are given, and description thereof will be omitted below.

  The agglomeration reaction apparatus 1 according to the present embodiment is provided with a temporary staying part 10 for agglomeration reaction having a cross-sectional area larger than that of the transfer pipe 4 at the downstream end of the small diameter pipe 5, and the temporary staying part 10 is transferred. The second transfer pipe 11 having the same diameter as the pipe 4 and the second fine pipe 12 having a smaller diameter (same diameter as the fine pipe 5) than the second transfer pipe 11 are connected to the aggregation reaction tank 2. In addition, the second variable diameter pipe 12 is provided with the same area variable means 7 (see FIG. 3) as in the first embodiment, and the other configuration is the same as that in the first embodiment. .

  Thus, in the agglomeration reaction apparatus 1 according to the present embodiment, since the temporary residence part 10 for the agglutination reaction having a larger cross-sectional area than the transfer pipe 4 is provided at the downstream end of the small diameter tube 5, the small diameter Aggregation reaction by the inorganic flocculant uniformly dispersed in the sludge by the turbulent flow in the pipe 5 is promoted in the temporary retention part 10. Then, the cross-sectional area S of the second small-diameter pipe 12 is provided by the area variable means 7 (see FIG. 3) provided in the second small-diameter pipe 12 having a smaller diameter than the second transfer pipe 11 connected to the temporary retention section 10. Is increased or decreased in proportion to the sludge pressure, the increase rate (dv / dQ) of the injection speed v with respect to the increase in the sludge flow rate Q becomes slow as in the first embodiment, and the flocculant and sludge The range of the processing amount (flow rate Q) for realizing the injection speed (v = 2 to 5 m / sec) that keeps the reaction favorable is expanded.

  In addition, in the present embodiment, the same effects as those of the first embodiment such as prevention of clogging of foreign substances and reduction of the cleaning frequency can be obtained.

<Other forms of area variable means>
In the above-described first and second embodiments, the configuration using the flap plate 8 having the spring characteristics as the area varying means 7 is adopted. However, the area varying means 7 has, for example, the structures shown in FIGS. Conceivable.

  That is, FIG. 7 is a sectional view of the transfer pipe 4 and the small diameter pipe 5, and the area variable means 7 is provided in the small diameter pipe 5. The area variable means 7 includes a flap plate 13 rotatably disposed in the small diameter pipe 5, a nut 14 attached to the upper portion of the small diameter pipe 5, and a small diameter screwed to the nut 14. The bolt 15 is inserted into the pipe 5 so as to be movable up and down, and a handle 16 is attached to the head of the bolt 15. The lower end of the bolt 15 facing the narrow pipe 5 is the flap plate. 13 is connected to the tip.

  In the above configuration, the handle 16 is rotated according to the sludge flow rate Q, the bolt 15 is turned, and the bolt 15 is moved up and down with respect to the small-diameter pipe 5, whereby the tip portion is connected to the bolt 15. The plate 13 can be turned up and down in the small diameter pipe 5. Thus, by rotating the flap plate 13 up and down in the small-diameter pipe 5, the cross-sectional area S of the small-diameter pipe 5 can be manually increased / decreased. The increase rate (dv / dQ) of the injection speed v with respect to the increase in the flow rate Q of the engine becomes slow. For this reason, the range of the processing amount (flow rate Q) for realizing the injection speed (v = 2 to 5 m / sec) that keeps the reaction between the flocculant and the sludge good can be expanded, and is high in a wide flow rate range. Aggregation reaction efficiency can be ensured.

  FIG. 8 is a perspective view of a taper tube 17 serving as the area variable means 7. The taper tube 17 is an elastically deformable tube that is reduced in diameter along the sludge flow direction (the arrow direction in the figure). For example, it is comprised with elastic bodies, such as rubber | gum.

  Thus, when the taper pipe 17 is used as a small-diameter pipe of the coagulation sludge device, when the sludge flow rate Q increases and the pressure P in the taper pipe 17 increases, the pressure P causes the taper pipe 17 to become in FIG. Since the diameter is increased and the cross-sectional area (opening area) S is increased as indicated by the chain line, the rate of increase of the injection speed v with respect to the increase in the sludge flow rate Q (dv /) as in the first and second embodiments. dQ) becomes slow, and the range of the throughput (flow rate Q) for realizing the injection speed (v = 2 to 5 m / sec) that keeps the reaction between the flocculant and the sludge good can be expanded. High aggregation reaction efficiency can be ensured in a range.

  Further, FIG. 9 is a cross-sectional view of the blowing pipe 18 as the area varying means 7. The blowing pipe 18 is composed of elastic sheets 19 whose upper and lower walls are elastically deformable, and the left and right side walls are rigid bodies such as metal. It is configured. Note that a rubber sheet or the like is used as the elastic sheet 19.

  Thus, when the blowing pipe 18 is used as a small-diameter pipe of the coagulation sludge apparatus, when the flow rate Q of the sludge increases and the pressure in the blowing pipe 18 increases, the elastic sheet 19 becomes a chain line in FIG. As shown in FIG. 2, since the cross-sectional area (opening area) S of the blow-in pipe 18 expands to the outside, the increase rate of the injection speed v with respect to the increase in the sludge flow rate Q (as in the first and second embodiments) dv / dQ) becomes slow, and the range of the throughput (flow rate Q) for realizing the injection speed (v = 2 to 5 m / sec) that keeps the reaction between the flocculant and sludge good can be expanded. High aggregation reaction efficiency can be secured in a wide flow rate range.

  In addition, although the above demonstrated the coagulation reaction apparatus which performs the coagulation process of sludge, this invention is used for the coagulation process of suspension water with high suspended solids density | concentration like the excess sludge discharged | emitted from a biological treatment process. In addition to the agglomeration reaction apparatus, the present invention can be similarly applied to an agglomeration sludge apparatus used for agglomeration treatment of polluted water having a relatively low solid matter concentration such as factory waste water and sewage.

It is a front view of the aggregation reaction apparatus which concerns on Embodiment 1 of this invention. It is the sectional view on the AA line of FIG. (A) is the B section expanded sectional view of Drawing 1, and (b) is a figure of the arrow C direction of (a) showing change of the cross-sectional area of small diameter piping. It is a figure which shows the relationship between the flow volume of sludge and the injection speed in the aggregation sludge apparatus which concerns on this invention. It is a front view of the aggregation reaction apparatus which concerns on Embodiment 2 of this invention. It is the DD sectional view taken on the line of FIG. It is sectional drawing of the transfer pipe and thin diameter piping which show the other form of an area variable means. It is a perspective view of the taper tube which shows the other form of an area variable means. It is a cross-sectional view of the blowing pipe which shows the other form of an area variable means. It is sectional drawing of the conventional agglutination reaction apparatus. It is a front view of the conventional aggregation reaction apparatus. It is the EE sectional view taken on the line of FIG. It is a figure which shows the relationship between the flow volume of sludge and the injection speed in the conventional coagulation sludge apparatus.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Coagulation reaction apparatus 2 Coagulation reaction tank 3 Raw mud pump 4 Transfer piping 5 Thin diameter piping 6 Stirrer 7 Area variable means 8 Flap plate 8a Starting point of flap plate 9 Discharge piping 10 Temporary retention part 11 Second transfer piping 12 2nd Small-diameter pipe 13 Flap plate 14 Nut 15 Bolt 16 Handle 17 Tapered pipe 18 Blow-in pipe 19 Elastic sheet

Claims (6)

A transfer pipe for pumping suspended water;
A smaller diameter pipe than the transfer pipe connected to the transfer pipe;
A flocculant supply means provided in the small-diameter pipe or the transfer pipe upstream thereof;
An agglomeration reaction tank in which the small-diameter pipe opens directly;
In an agglutination reactor having
An agglomeration reaction apparatus comprising an area variable means for increasing or decreasing the cross-sectional area of the small-diameter pipe in proportion to the pressure of the suspended water flowing through the small-diameter pipe.   2. The coagulation reaction apparatus according to claim 1, wherein the area variable means is constituted by a flap plate having a spring function arranged in the small-diameter pipe.   The area variable means includes a flap plate rotatably disposed in the small-diameter pipe, and a bolt that is threadably engaged with the small-diameter pipe and whose end is connected to the flap plate. The agglomeration reaction apparatus according to claim 1, comprising:   2. The agglomeration reaction apparatus according to claim 1, wherein the area variable means is constituted by an elastically deformable taper tube whose diameter is reduced along the flow direction of the suspended water.   2. The agglomeration reaction apparatus according to claim 1, wherein the area variable means is constituted by a blowing tube partly constituted by an elastic sheet that can be elastically deformed.   A temporary retention part for agglomeration reaction having a larger cross-sectional area than the transfer pipe is provided at the downstream end of the small diameter pipe, and the temporary retention part is smaller in diameter than the second transfer pipe and the second transfer pipe. The second variable diameter pipe is connected to the agglomeration reaction tank, and the area variable means is provided in the second small diameter pipe. Aggregation reactor.

Images