KR0173996B1 - Apparatus for dissolving a gas into and mixing the same with a liquid - Google Patents

Abstract

The present invention relates to a gas-liquid dissolving mixing method and apparatus therefor for mixing and dispersing bubbles in a liquid or dissolving gas in a liquid efficiently. This gas-liquid dissolution mixing method and apparatus include an throttling portion 12 provided in a liquid flow path, and a gas inlet 18 formed slightly downstream of the throttling portion 12, and an enlarged portion continuous from the throttling portion 12. It is provided downstream of (16), and the mixing part 20 which mixes the liquid in a flow path and the gas which flowed in from the gas inlet 18, and the nozzle part 24 provided in the exit of this mixing part 20 are provided.

This gas dissolving mixing method and apparatus are used for dissolving gas such as ozone in a liquid, or dispersing bubbles in water to form fine bubbles or to float fine particles by the bubbles.

Description

Gas-liquid dissolution mixing method and apparatus

1 is a longitudinal sectional view of the mixer of the first embodiment of the gas-liquid dissolution mixing apparatus of the present invention.

2 is a pipeline diagram of an apparatus for producing gas-dissolved water using the gas-liquid dissolving mixing apparatus of this embodiment.

3 is a schematic refinement of the mixer of the second embodiment of the gas-liquid dissolution mixing apparatus of the present invention.

4 is a partial longitudinal sectional view of the mixer of the third embodiment of the gas-liquid dissolution mixing apparatus of the present invention.

5 is a pipeline diagram of an apparatus for producing gas-dissolved water using the gas-liquid dissolving mixing apparatus of Embodiment 4 of the present invention.

6 is a schematic pipeline diagram of a fifth embodiment of the gas-liquid dissolution mixing apparatus of the present invention.

7 is a longitudinal sectional view of the mixer of the gas-liquid dissolution mixing apparatus of the fifth embodiment of the present invention.

8 is a longitudinal sectional view of the redistribution apparatus and nozzle portion of the fifth embodiment of the gas-liquid dissolution mixing apparatus of the present invention.

9 is a schematic pipeline diagram of a sixth embodiment of the gas-liquid dissolution mixing apparatus of the present invention.

FIG. 10 is a schematic sectional view of a part of the seventh embodiment of the gas-liquid dissolution mixing apparatus of the present invention.

Fig. 11 is a longitudinal sectional view showing the gas-liquid dissolving mixing apparatus in Embodiment 8 of the present invention.

12 is a schematic pipeline diagram of the gas-liquid dissolution mixing apparatus of the ninth embodiment of the present invention.

13 is a longitudinal cross-sectional view of the gas-liquid mixing mixer of the tenth embodiment of the present invention.

14 is a view showing the floating particles floating by the tenth embodiment of the present invention.

15 is a view showing the floating particles floated by the present embodiment.

16 is a schematic diagram of the floating particle floating separator of the tenth embodiment of the present invention.

17 is a schematic diagram of an eleventh embodiment of the present invention.

18 is a schematic diagram of a floating particle floating separator according to the twelfth embodiment of the invention.

19 is a longitudinal sectional view of the floating particle floating separator of the twelfth embodiment.

20 is a longitudinal sectional view showing the mixer of the thirteenth embodiment of the gas-liquid dissolution mixing apparatus of the present invention.

Fig. 21 is an enlarged cross-sectional view of a part of the mixer of the gas-liquid dissolution mixing apparatus of the thirteenth embodiment of the present invention.

22 is a longitudinal sectional view of the mixing vessel of the gas-liquid dissolution mixing apparatus of the fourteenth embodiment of the present invention.

FIG. 23 is a partial longitudinal sectional view of the nozzle portion of the gas-liquid dissolution mixing apparatus of the fifteenth embodiment of the present invention.

24 is a partial longitudinal cross-sectional view of the middle nozzle portion of the gas-liquid dissolution mixing apparatus of the fifteenth embodiment of the present invention.

25 is a longitudinal sectional view of the mixer of the gas-liquid dissolution mixing apparatus of the fifteenth embodiment of the present invention.

Fig. 26 is a longitudinal sectional view showing the excess gas separation type gas-liquid mixing apparatus of the sixteenth embodiment of the present invention.

FIG. 27 is a longitudinal sectional view of a portion showing an example of use of the excess gas separation type gas-liquid mixing apparatus of the sixteenth embodiment described above.

Fig. 29 is a schematic diagram showing the microcellular end cell manufacturing apparatus of Example 17 using the gas-liquid dissolving mixing apparatus of the present invention.

30 is a longitudinal sectional view of the mixer of the seventeenth embodiment of the present invention.

Fig. 31 is a longitudinal sectional view of another mixer of the microblastoma preparation device of the seventeenth embodiment.

32 is a longitudinal cross-sectional view of a part of another mixer of the microcellular powder producing apparatus of this embodiment.

33 is a longitudinal sectional view of a gas-liquid mixing tank of another micron cell preparation apparatus of the seventeenth embodiment of the present invention.

* Explanation of symbols for main parts of the drawings

10: mixer 12,206,422,528: throttle

16,122,210,426: Magnification 18,123,226,428: Gas inlet

20,124,430 Mixing part 24,54,115,434 Nozzle part

30: liquid supply part 38: liquid receiving part

44 gas supply unit 52 body part

56: pipeline 113,134: liquid pipeline

117: nozzle hole 120: first throttle

130: second throttle 133: branch point

213: pressurized mixing flow passage 216: intermediate bridge

220 nozzle nozzle 250 pressure measuring means

427: gas inlet 512: flow path

516: gas separation flow path 520: nozzle

522, 524: sensor 530: solenoid valve

The present invention relates to a mixing method and apparatus for mixing and dispersing bubbles in a liquid or dissolving gas efficiently in a liquid.

Conventionally, as an apparatus for dispersing and dissolving gas in a large amount in a liquid, a so-called ejector bubble generator is used. This passes the liquid jet stream injected from the nozzle into the gas to be mixed once, and draws the surrounding gas into the jet stream. Then, a gas-mixed jet flow is injected into the liquid from a throttle having a diameter substantially the same as the jet stream provided coaxially with the nozzle, thereby producing a liquid containing fine bubbles. In addition, by injecting the jet flow in which the fine bubbles are dispersed by the above method into the lower part of the tank in which the bubbles rise, the large amount of bubbles are dissolved in the liquid while the fine bubbles rise in the liquid in the tank. There is also an apparatus for producing a liquid in which gas is dissolved.

In addition, the gas and the liquid are sent into the pressure pump, the liquid and the gas are pressurized in the pressure pump to dissolve the gas in the liquid, thereafter, the liquid in which the gas is dissolved is decompressed, and the dissolved gas is precipitated to bubble into the liquid. There is also a device for forming.

When the ejector type bubble generator according to the prior art is used, the center of the liquid jet nozzle and the center of the throttling portion must be coincident, so that the structure of the device is complicated and assembly is difficult.

In addition, the gas dissolving device using the bubble tank had a long time required to obtain a liquid in which gas was sufficiently dissolved, resulting in poor manufacturing efficiency.

In addition, when the pressure pump according to the related art is used, since gas and liquid are sent together inside the pressure pump, there is a problem that the material and structure of the pump are limited.

In addition, when bubbles are generated by this pressure dissolution, the bubbles to be precipitated are only gases that have been dissolved in the pressurized state, and thus it is impossible to generate bubbles above the solubility limit to the liquid of the gas by depressurization. In order to generate bubbles, the pressure must be considerably high pressure. Therefore, there is a problem that the apparatus is enlarged and cavitation is more easily generated.

SUMMARY OF THE INVENTION The present invention has been made in view of the above-described problems in the prior art, and has a simple structure, capable of forming fine bubbles in a liquid with continuous and good efficiency, and capable of mixing and dissolving gas in a liquid in large quantities. It is an object to provide a mixing method and a mixing device.

According to the present invention, a part of the liquid flow path is throttled by a venturi tube, an orifice, or the like, and gradually expands the conduit on the downstream side of the throttling portion, while gas is introduced into the liquid flowing in the conduit slightly downstream from the throttling portion. It is a gas-liquid melt mixing method which flows in and mixes this gas and the liquid in a pipe on the downstream side of the said expanded part, and ejects gas-liquid mixture stream from the nozzle part provided in the outlet.

In addition, the present invention relates to a throttling portion such as a venturi tube or an orifice provided in a liquid flow path, an enlarged portion continuously extending from the throttle portion, and a gas inlet provided in an enlarged portion slightly downstream from the throttle portion. And a gas-liquid dissolving-mixing device which is provided downstream of the above-mentioned expansion part, and comprises a mixing part for mixing the liquid in the flow path and the gas introduced from the gas inlet, and a nozzle part provided at the outlet of the mixing part.

In the gas-liquid dissolution mixing method and apparatus of the present invention, a mixing portion in which gas is introduced into a liquid flow from a negative pressure portion slightly downstream from a throttle portion such as a neck portion of a venturi tube, and the flow is slowed to increase static pressure. Pressurizes and melts the gas introduced into the gas, and accelerates the gas-liquid mixture flow by the nozzle part of the outlet, and shears and breaks up the mixed bubbles by using the disturbance of the flow. By vaporizing the gas into a micro bubble, bubbles are generated. Moreover, this invention provides the liquid supply part which delivers the liquid which melt | dissolves a gas to a predetermined pressure, the mixer which mixes the liquid conveyed from this liquid supply part, and predetermined gas, and is installed in this liquid flow path in this mixer. A throttling portion formed by a venturi tube or an orifice, a gas inlet provided slightly downstream of the throttling portion, and an enlarged portion gradually expanding the conduit continuous from the throttling portion; A mixing section which is provided, and which mixes the liquid in the flow path and the gas introduced from the gas inflow water, and a nozzle section provided at the outlet of the mixing section, in the above-described mixer, and a gas supply section connected to the gas inlet of the mixer, A liquid-liquid mixing plant in which the nozzle portion of the mixer is connected, and a liquid-receiving portion into which liquid in which gas is dissolved flows in the mixing portion is provided. A.

In addition, the present invention provides a first throttling portion such as a venturi tube or an orifice in a part of the liquid flow passage, and forms an enlarged portion that is continuously extended to the downstream side of the first throttling portion, wherein the first throttling portion is formed. A gas inlet is formed in an enlarged portion slightly downstream, and a mixing portion for mixing the gas flowing from the liquid in the flow path and the gas inlet is provided downstream of the expansion portion, and the nozzles held by the plurality of nozzle holes downstream of the mixing portion. A gas-liquid dissolution mixing apparatus in which a portion is provided via a liquid pipeline and a second throttle portion is formed immediately before the nozzle portion.

Moreover, this invention provides the 1st throttling part, such as a venturi tube and an orifice, in a part of a liquid flow path, and is provided in the continuation part, the enlarged part extended gradually in the downstream, and the said 1st throttling part. A gas inlet is formed in an enlarged portion slightly downstream, and a mixing portion for mixing the liquid in the flow path and the gas introduced from the gas inlet is provided downstream of the enlarged portion, and a liquid conduit with a branch point downstream of the mixing portion is provided. A gas-liquid dissolution mixing apparatus in which a nozzle portion is provided on the downstream side of the branch point and a second throttle portion is formed immediately before the branch point, respectively.

The gas-liquid dissolving mixing apparatus of the present invention flows gas into the flow path from the negative pressure portion of the gas inlet, dissolves and mixes the gas into the liquid in the mixing portion having increased static pressure, and at the same time, the mixed bubbles are uneven in the fluid conduit. Even in the distribution state, the bubbles and liquid are mixed again in the second throttle to equalize the distribution of bubbles in the liquid, and the liquid is sprayed with a uniform ratio of bubbles from each nozzle hole in the nozzle section. In addition, when the liquid mixed with the bubbles can be injected from the nozzle port, the mixed bubbles are sheared and subdivided, and the dissolved gas is also precipitated to form minute bubbles. Similarly, by providing the second mixing portion in front of the branching point of the liquid flow path, bubbles are uniformly dispersed in the branched liquid so that the fluid is separated so that the liquid mixed with the gas uniformly is ejected from the nozzle portion.

Moreover, in this invention, a part of a fluid flow path is throttled by a venturi tube, an orifice, etc., and the expansion part which enlarged the pipe gradually on the downstream side of this throttle part is provided, and gas is inflowed in the slightly downstream side of the said throttle part. A gas inlet for forming the gas inlet is formed, and a pressure mixing flow path is formed on the downstream side of the enlarged portion, and the fluid is flowed from the top to the bottom, and a nozzle port is installed at the outlet or downstream of the pressure mixing flow path. One gas-liquid mixing device. In addition, an intermediate throttle having a larger cross-sectional area is provided in the middle of the pressure mixing flow passage as compared with the nozzle port described above, and pressure measuring means for measuring the pressure of at least the outlet side flow path of the intermediate throttling portion in the pressure mixing flow passage is provided. will be.

The gas-liquid dissolving mixing apparatus of the present invention introduces gas into the liquid flow from the gas inlet slightly downstream of the throttle, and pressurizes and dissolves the gas introduced into the liquid while mixing the gas and the liquid in the enlarged portion where the flow is slow. In addition, gas flows through the upper portion of the flow path of the pressurized mixing flow path, and liquid flows through the lower portion of the flow path, so that the contact area of the gas liquid becomes large. Moreover, by providing a nozzle in the outlet or downstream of the pressurized mixing flow path which flows down from the top, the positive pressure inside this pressurized mixture flow path can be raised, and reaction and melt | dissolution efficiency can be improved. In addition, since the outlet is lower than the inlet, the gas-liquid mixture is stagnant in the pressurized mixing flow passage described above, and the liquid having a higher density is easier to escape than gas. Therefore, even if the gas is stagnated more than the liquid and the ratio of the gas of the gas-liquid mixture flowing into the pressurized mixing flow path is low, the proportion of the gas in the pressurized mixing flow path is high.

The present invention also provides a gas-liquid dissolving mixer for mixing a liquid and a gas, in which the gas-liquid dissolving mixer continuously extends from the condensing portion such as a venturi tube or an orifice provided in the liquid flow path, and gradually expands the conduit. An enlarged portion, which is provided downstream of the enlarged portion, mixes the liquid in the flow path and the gas introduced from the gas inlet, and is provided at the outlet side of the mixed portion, and has several micrometers to several hundred micrometers in the liquid in which suspended particles exist. It is a gas-liquid dissolution mixing device provided with a nozzle hole for ejecting bubbles of the size of.

In the apparatus of the present invention, the gas mixed in the liquid in the negative pressure portion near the throttling portion is mixed and dissolved in the mixing portion under pressure, the liquid and gas are injected from the nozzle portion, the gas is sheared and broken down, and the dissolved gas Precipitates to form bubbles of a wide size ranging from several micrometers to several hundred micrometers in the liquid. As a result, relatively large bubbles are captured and floated by the floating particles in the liquid, and the floated particles and the relatively large bubbles in the bubbles are released from the particles away from the particles, but the relatively small bubbles do not fall from the particles. To keep the floating particles in the floating position.

In addition, the present invention is provided with a throttle part such as a venturi tube or an orifice provided in the flow path, and a gas inlet part which is provided downstream of the throttle part continuously and has the same cross-sectional area with respect to the flow path direction of the liquid. A gas inlet through which gas is introduced from the outside, and an enlarged part that gradually expands the flow path on the downstream side of the gas inlet part, and mixes the liquid in the flow path and the gas introduced from the gas inlet downstream of the enlarged part. It is a gas-liquid dissolution mixing apparatus provided with a part and provided with a nozzle on the outlet side of this mixing part.

The gas-liquid dissolution mixing apparatus of the present invention flows gas into a liquid flow from a negative pressure portion slightly downstream of a throttle portion such as a neck portion of a venturi tube, and pressurizes and dissolves the gas introduced into the liquid portion into a liquid in which the static pressure increases. After that, the above-mentioned gas-liquid mixture flow is accelerated by the nozzle at the outlet to lower the static pressure again, and the gas dissolved in the liquid is precipitated as fine bubbles. In particular, the gas inlet is formed in the gas inlet portion having a constant cross-sectional area with respect to the flow path direction, so that the gas is drawn into the liquid stably and efficiently.

According to the present invention, a part of the flow path is throttled by a throttling part such as a venturi tube or an orifice provided in the flow path, and the flow path is gradually expanded on the downstream side of the throttle part, and gas is introduced in a slightly downstream shaft of the throttle part. A gas-liquid mixture flow is formed, and the pressure in the upstream flow path of the nozzle is increased by a nozzle provided downstream of the flow path, gas is dissolved in the liquid in the flow path, and the gas-liquid mixture flow in which the gas is dissolved is It depressurizes by passing and discharges the gas-liquid mixture containing these microbubbles into the liquid in the liquid receiving member, precipitates the pressurized gas in the form of microbubbles, and simultaneously flows the gas which was not dissolved in the nozzle. Sheared into fine bubbles by the disturbance of the liquid, and by raising the fine bubbles in the liquid containing member, the liquid water A method for manufacturing a fine foam to form a fine foam layer on the liquid surface in the upper member.

EMBODIMENT OF THE INVENTION Hereinafter, the Example of the gas-liquid mixing method and the gas-liquid mixing apparatus of this invention are demonstrated with reference to drawings.

[First Embodiment]

1 and 2 show a first embodiment of the present invention. As shown in FIG. 1, a venturi tube having a neck portion 12, which is a throttle, is provided in a mixer 10 for mixing gas into a liquid. 14 is formed. In the enlarged portion 16 on the downstream side of the venturi tube 14, a gas inlet 18 is formed slightly downstream of the neck portion 12 to mix gas into the flow path.

On the downstream side of the enlarged portion 16, a mixing portion 20 for mixing the gas introduced from the gas inlet 18 and the liquid in the flow path is formed. The mixing part 20 can set the outer diameter arbitrarily according to the degree of pressurization, and is formed in the shape extended from the largest diameter of the expansion part 16 here. The nozzle part 24 in which the some nozzle port 22 was formed is attached to the front-end | tip of this mixing part 20. As shown in FIG.

The operation of the gas-liquid dissolution mixing apparatus of this embodiment will be described.

First, the liquid flowing into the inlet portion 26 of the mixer 10 is accelerated in the neck portion 12 of the venturi tube 14 so that the static pressure decreases once, and the flow velocity drops through the enlarged portion 16. Again, the static pressure increases. At this time, the gas inlet 18 is slightly downstream from the neck 12, and since the positive pressure of this portion becomes relatively negative, gas flows into the flow path. Since the gas inlet 18 is not arranged at the neck 12, the neck 12 is the lowest static pressure, but the gas inlet 18 is installed at the neck 12 so that the gas inlet 18 is actually gas. This is because the suction is not good, and gas is easily introduced to the part where the flow path begins to expand.

The gas flowing from the gas inlet 18 becomes a bubble and flows to the mixing part 20 together with the liquid in a flow path, and since the positive pressure of the mixing part 20 is higher than the neck part 12, it is a liquid. Dissolve into the stomach. Then, the liquid is injected with the bubbles through the nozzle port 22 from the mixing section 20. Since the liquid accelerates again when passing through the nozzle port 22, the static pressure is lowered, and the gas dissolved in the liquid precipitates as fine bubbles. In addition, bubbles which are not dissolved are also subdivided by flow disturbances or the like when they are accelerated by the nozzle port 22, and are bubbled together with a small diameter to be injected together with the liquid.

The relationship of the sum of the area of the expansion part 16 and the nozzle port 22 in the connection part of the gas inlet 18 of the gas-liquid mixing apparatus of this embodiment should satisfy | fill the following formula.

P _A P _G ------ (1)

P _G is the pressure of the gas flowing from the gas inlet 18, P _A is an enlarged portion at the connection portion of the gas inlet 18 given by the following equation according to the hydrodynamic continuous equation and Bernoulli's theorem ( 16 is the static pressure.

P _A = (1-S ² _B / S ² _A ) P ₁ + (δP + P _Bb ) S ² _B / S ² _A ------ (2)

Here, S _A is the cross-sectional area of the enlarged portion 16 at the connection portion of the gas inlet 18, S _B is the total sum of the cross-sectional areas of the nozzle port 22, and P ₁ is the connection portion of the gas inlet 18. Is the total pressure of the enlarged portion 16, δP is the pressure loss from the enlarged portion 16 to the nozzle port 22 at the connection portion of the gas inlet 18, P _B is the static pressure at the outlet of the nozzle port 22 to be.

Therefore, by setting the sizes of the enlarged portion 16 and the nozzle port 22 at the connection portion of the gas inlet 15 so as to satisfy the above expressions (1) and (2), the gas can be efficiently in the liquid. Optimum conditions for mixing and dissolving can be obtained. In addition, the mixing section 20 is preferable as long as it can obtain the connection time of the gas liquid until the gas is dissolved and saturated in the liquid under pressure, and the contact time of the gas is related to the volume of the mixing section. The longer one dissolves until the saturation point. In addition, when it is not necessary to melt | dissolve to saturated state, this mixing part 20 can also be shortened.

The gas-dissolved water production apparatus using the gas-liquid dissolution mixing apparatus of this embodiment will be described with reference to FIG.

In the gas-dissolved water producing apparatus of this embodiment, a water tank 30 and a pump 32 for feeding liquid are connected by a conduit 34, and the output side of the pump 32 is a mixer 10 via a conduit 36. Is attached. The mixer 10 is attached with the nozzle part 24 open to the bottom side of the water tank 38 for storing the liquid in which gas was dissolved. The gas tank 44 is connected to the gas inlet 18 of the mixer 10 via the conduit 40 and the flow regulating valve 42. In addition, a pipe line 48 connected to the water tank 30 through a relief valve 46 is connected to the pipe line 36.

This gas-dissolved water production apparatus pumps the liquid in the water tank 30 to the mixer 10 by means of a pump 32, and as described above, the gas pressurized from the gas tank 44 in the mixer 10 , Mixed with the liquid in the mixer 10, the gas is dissolved in the liquid in a large amount, and is sprayed together with the bubbles from the nozzle 22.

Here, the relief valve 42 is for maintaining the pressure of the liquid to be conveyed constant, and the flow rate adjusting valve 42 is for adjusting the gas flow rate so that fine bubbles are efficiently formed in the liquid. Experimentally, a large amount of fine bubbles could be efficiently obtained in the liquid when the gas flow rate was 10 to 30% of the liquid flow rate. Bubbles injected from the mixer 10 are dispersed in the liquid in the water tank 38 by the jet flow, and are suspended in the liquid for a long time because they are fine bubbles. In the gas-dissolved water production apparatus, in order to always disperse bubbles in the liquid, the pipes 34 and 36 may be connected to a form in which the water tank 30 and the water tank 38 are shared.

Table 1 shows the experimental results of dissolving ozone in water using the gas-liquid dissolving mixing apparatus of this example. Here, the ozone generation amount is 10,000ppm, the stainless pipe of length 0,7m is used for the mixing part 20 of the mixer 10. As shown in FIG.

In Table 1, the start-up time is the time required to start continuously producing ozone water at a predetermined concentration after the start of the apparatus, and when the conventional bubble tank is used, it takes about 30 minutes. Compared with the case where the above is required, the gas-liquid dissolving mixing apparatus of this embodiment can produce gas-dissolved water efficiently in a very short time.

Second Embodiment

Next, a second embodiment of the present invention will be described with reference to FIG. Here, the same reference numerals are used for the same members as those in the first embodiment, and description thereof is omitted. In the mixer 50 of this embodiment, the main body portion 52 on which the venturi tube 14 is formed, and the nozzle portion 54 on which the nozzle port is formed are separated, and the conduit 56 connecting them is a mixing portion.

The pipeline 56 may be a steel pipe or a flexible pipeline, and since the flow becomes turbulent, gas and liquid are more efficiently mixed, so that the pipeline 56 is spirally formed or the Reynolds number of the pipeline 56 is turbulent. You may set on conditions more than the value which becomes.

According to the gas-liquid dissolution mixing apparatus of this embodiment, the position of the nozzle portion 54 can be set freely, and only the nozzle portion 54 can be moved freely, thus increasing the degree of freedom.

Third Embodiment

Next, a third embodiment of the present invention will be described with reference to FIG. Here, the same reference numerals are used for the same members as the above-described embodiment, and description thereof will be omitted.

The mixer 60 of this embodiment forms the enlarged part 62 which continued from the neck part 12 of the venturi tube 14 which is an axial part in the shape which overlapped concentric cylinders step by step. In this way, manufacture of the mixer 60 becomes easy.

Fourth Embodiment

Next, a fourth embodiment of the present invention will be described with reference to FIG.

Here, the same reference numerals are used for the same members as in the above-described embodiment, and the description thereof is omitted. The gas-liquid dissolution mixing apparatus of this embodiment is for dissolving gas only, and no mixing and dispersing of bubbles is required. In the mixer 60, the main body 64 provided with the venturi tube forming the throttling portion and the nozzle portion 66 in which the nozzle port is formed are separated, and these are connected by a pipe 68 serving as the mixing portion.

The pipe line 68 may be a steel pipe or a flexible pipe line, and since gas and liquid are mixed more efficiently on the surface where the flow becomes turbulent, the pipe line 68 may be set in a spiral shape or the Reynolds of the pipe line 68 may be used. You may set conditions more than the value which turns into a turbulence. In addition, a tube may be connected to the tip of the nozzle portion 66 to reduce the liquid ejected from the nozzle portion 66.

According to the gas-liquid dissolution mixing apparatus of this embodiment, the position of the nozzle portion 66 can be set freely, and only the nozzle portion 66 can be moved freely, thus increasing the degree of freedom, so that the gaseous solution can be produced in large quantities easily. have.

[Example 5]

Next, a fifth embodiment of the present invention will be described with reference to Figs.

As shown in FIG. 6, the mixer 112 which mixes gas in a liquid is connected to the pipeline 110 which is a liquid flow path which supplies a liquid, and the pipeline 113 is also connected downstream of the mixer 112, The nozzle part 115 is provided in the front-end | tip of the 113 via the redistribution apparatus 114. As shown in FIG. The nozzle part 115 is provided in the side wall part of the water tank 116, and the water tank 116 and 118 are accommodated in the some nozzle hole 117. As shown in FIG. The pipes 110 and 113 may be fixed pipes such as steel pipes or pipes made of flexible tubes, or may be combined.

In the mixer 112, as shown in FIG. 7, the venturi tube 121 in which the neck part 120 which is the throttle part which thinned the middle of the liquid flow path is provided in the center part is formed. The gas inlet 123 for mixing gas in the flow path is formed in the enlarged part 122 of the downstream of this venturi tube 121 on the slightly downstream side of the neck part 120. As shown in FIG. A downstream side of the enlarged portion 122 is provided with a mixing portion 124 for mixing the gas introduced from the gas inlet 123 and the liquid in the flow path. The mixing part 124 can be set arbitrarily according to the degree of pressurization, and the base end part of the conduit 113 extended from the maximum diameter of the expansion part 122 becomes the mixing part 124 here.

In addition, as shown in FIG. 8, the venturi tube 131 is also formed in the redistribution unit 114 provided through the conduit 113 on the downstream side of the mixer 112, and the neck portion, which is an throttle tapering the middle of the liquid flow path. 130 is provided in the center of the venturi tube 131. The nozzle part 115 is connected to the downstream of the venturi tube 131, and the nozzle hole 117 is formed in this end part via the duct 132 of the internal space in this nozzle part 115. As shown in FIG. Here, the distance from the nozzle hole 117 to the neck portion 130 is preferably about 2 times or more and less than 10 times the diameter of the duct 132. The reason for this is that if the distance from the neck 130 to the nozzle hole 117 is too close, remixing of the gas and the liquid is not sufficiently performed, and if too far, the bubble distribution state in the recombined liquid becomes uneven again. In addition, the cross-sectional area of the neck portion 130 of the redistribution apparatus 114 was experimentally able to obtain a good gas-liquid dispersion mixed liquid at about 1.5 times the total cross-sectional area of the nozzle hole 117.

The operation of the gas-liquid dissolution mixing apparatus of this embodiment will be described next.

First, the liquid introduced into the mixer 112 is accelerated in the neck portion 120 of the venturi tube 121, and the static pressure is lowered once, and the static pressure is increased again while the flow velocity is slowed through the enlarged portion 122. . At this time, the gas inlet 123 is slightly downstream of the neck portion 120, and since the positive pressure of this portion is relatively negative, the gas flows into the flow path.

The gas introduced from the gas inlet 123 becomes a fine bubble and flows to the mixing unit 124 together with the liquid in the flow path. In addition, since the positive gas of the mixing part 124 is higher than the neck portion 120, the gas made of bubbles is dissolved into the liquid. Bubbles and liquid mixed in the mixing unit 124 flows through the conduit 113 to the redistribution device. At this time, the bubble in the liquid slowly rises upward while passing through the conduit 113, so that many bubbles are collected upwards of the conduit. Then, the liquid and bubbles that reach the redistribution device 114 at the tip of the conduit 113 are accelerated again by the neck 130 and mixed again in the duct 132 so that the bubbles are uniformly distributed in the liquid. In the above state, the jetting streams in which the bubbles are uniformly mixed are injected from the plurality of nozzle holes 117, respectively. When the bubble passes through the nozzle hole 117, the liquid is accelerated again, so the static pressure is lowered, and the gas dissolved in the liquid is precipitated as a fine bubble. In addition, bubbles which have not been dissolved are also subdivided by turbulence in the flow or the like when they flow in the nozzle hole 117, and are bubbled together with a liquid with small diameter bubbles.

According to the gas-liquid dissolving mixing apparatus of this embodiment, even if the gas-liquid mixture flows through the conduit 113, even if a deviation occurs in the distribution of bubbles mixed in the liquid by the mixer 112, the redistribution apparatus 114 makes use of the nozzle hole. Since the bubbles are uniformly dispersed and mixed in the liquid before being ejected from the 117, the jet streams in which the bubbles are dispersed are ejected from the nozzle holes 117 of the plurality of nozzle holes 117 in the same manner.

In particular, in the gas-liquid dissolving mixing apparatus of this embodiment, since the mixer 112 and the nozzle unit 115 are separated, and a pipe for supplying gas is connected to the mixer 112, a flexible material is used for the pipe 113. Thus, the nozzle unit 115 can be installed to be movable in the liquid 118 without fixing the nozzle unit 115 to the water tank 116. Thereby, it is also possible to easily inject the gas-liquid mixed stream from the nozzle hole 117 while moving the nozzle part 115 in the liquid 118, and since the gas supply line is not present in the nozzle part 115, Sex is also good.

Sixth Embodiment

Next, a sixth embodiment of the present invention will be described with reference to FIG.

Here, the same reference numerals are used for the same members as those of the fifth embodiment, and description thereof is omitted. In the gas-liquid dissolution mixing apparatus of this embodiment, the branch point 133 is formed at the tip of the pipe line 113. A redistribution device 114 is provided immediately before the branch point 133, and two pipelines 134 and 135 are connected downstream of the branch point 133. A nozzle portion 115 having a plurality of nozzle holes 117 is provided at a distal end of the pipeline 134 through a redistribution device 114, and a nozzle portion 136 having one nozzle hole formed at the distal end of the pipeline 135. ) Is installed. Since the distribution of gas-liquid may not be different in the nozzle 136 with one nozzle hole, it is not necessary to provide the redistribution device 114. Each nozzle part 115,116 may be attached to the water tank 116, and may be connected to the flexible conduits 113,134,135, and may be provided so that the inside of the water tank 116 may be moved.

[Example 7]

Next, a seventh embodiment of the present invention will be described with reference to FIG.

Here, the same reference numerals are used for the same members as those in the fifth embodiment, and description thereof is omitted. In the gas-liquid dissolution mixing apparatus of this embodiment, a branch point 133 is formed at the tip end of the conduit 113, and a branch point 143 is also provided at the tip end of the branched conduit 141. The redistribution device 114 is provided immediately before the branch points 133 and 143, respectively. Two pipelines 144 and 145 are also connected to the downstream side of the branch point 143.

[Example 8]

Next, an eighth embodiment of the present invention will be described with reference to FIG.

The gas-liquid dissolving mixing apparatus of this embodiment is provided with a mixer 204 to which a liquid inflow conduit 202 for supplying liquid is connected, and the mixer 204 is attached to the inlet portion 211 of the gas-liquid dissolving mixer 212. It is. The mixer 204 is formed with a venturi tube having a narrowly throttled neck portion 206 formed at the center thereof, and an enlarged portion 210 downstream of the neck portion 206 slightly downstream of the neck portion 206. A gas inlet 208 is formed for mixing gas into the conduit.

The gas-liquid pressure mixer 212 is assembled into a box shape, and a pressure mixing flow passage 213 is formed in which the horizontal portion 213a and the vertical portion 213b are alternately installed step by step. An exhaust port 214 is formed at an upper portion of the pressurized mixing flow path 213, an intermediate throttle portion 216 is attached to an intermediate portion of the flow path, and a nozzle hole 220 is provided at the outlet portion 218. The nozzle port 220 is connected to the outflow pipe path 222. Immediately before the outlet portion 218, a branch flow passage 224 branching upward is formed, and an excess gas discharge port 226 for discharging excess gas is provided in the upper portion of the branch flow passage 224.

The valve 230 is attached to the front end of the exhaust port 214 attached to the upper portion of the gas-liquid pressure mixer 212 via the conduit 228. The exhaust port 214 and the valve 230 prevent the gas which is pressurized when the inflow of the gas-liquid mixture flow is expanded and flows out into the inlet duct 202, the gas inlet 208, the outlet duct 222, or the like. For this purpose, the valve 230 is opened to stop the inflow of gas-liquid mixture flow, and is used to discharge gas to the outside through the exhaust port 214. In addition, this exhaust port 214 may be omitted suitably when it is unnecessary.

The total cross-sectional area of the intermediate throttle part 216 provided in the middle of the flow path in the gas-liquid pressure mixer 212 is larger than the total cross-sectional area of the nozzle port 220 provided in the outlet part 218 of this gas-liquid pressure mixer 212. And by providing the intermediate throttle part 216, the pressure of the flow path after the intermediate throttle part 216 becomes lower than the flow path before the intermediate throttle part 216. FIG. As a result, by measuring the pressurized state of the flow path before the intermediate throttle 216 and the flow path after the intermediate throttle 216, an emergency such as abnormally rising the pressure in the pressure mixing flow path 213 can be detected. The rupture and the like of the gas-liquid pressure mixer 212 can be prevented in advance. Here, in general, it can be seen that the pressure of the flow path after the intermediate throttle 216 is abnormal by the proximity of the pressure of the flow path before the intermediate throttle 216.

Here, since the pressure in the flow path before the intermediate throttle 216 can be known by the pressure of the gas-liquid mixed flow to be injected, the pressure after the intermediate throttle 216 is measured by the pressure sensor 250, so that this gas-liquid pressure mixer An abnormality of 212 may be detected. In addition, this intermediate throttle part 216 can be omitted suitably when it is unnecessary.

The branch flow passage 224 protruding upwards immediately before the nozzle port 220 of the gas-liquid pressure mixer 212 branches at the branch point 232 of the end portion of the pressurized mixing flow passage 213, and the branch flow passage 224 and the surplus It is connected to the flow control valve 236 in the conduit 234 via the gas outlet 226. Since the gas flowing inside the pressurized mixing flow passage 213 has a low density, the gas flowing through the pressure mixing flow passage 213 flows into the branch flow passage 224 protruding upward when it comes to the branch point 232 and flows through the conduit 234 to the flow rate control valve 236. Then, by appropriately adjusting the flow rate adjusting valve 236, the remaining gas can be exhausted and the pressurized value can be adjusted at the same time. If the branch flow path 224 is also unnecessary, it can be omitted as appropriate. In addition, when it is not necessary to adjust the pressure in the pressurized mixing flow path 213, the flow regulating valve 236 may be a fixed bridge.

Next, the operation of the gas-liquid dissolution mixing apparatus of this embodiment will be described below.

First, the liquid flowing from the inlet pipe 202 to the mixer 204 at a predetermined pressure is accelerated at the neck portion 206 of the venturi pipe, and once the static pressure is lowered, the flow velocity is increased via the enlarged portion 210. Slowly, the static pressure rises again. At this time, the gas inlet 208 is slightly downstream of the neck portion 206, and since the positive pressure of this portion becomes relatively negative, gas is introduced into the flow path.

The gas-liquid mixture flow in which the gas is mixed in the mixer 204 flows separately from the gas flow 240 and the liquid flow 242 inside the gas-liquid pressure mixer 212. At this time, the gas and liquid are brought into a high contact state in contact with each other in a large area under a strong pressure, thereby promoting gas-liquid reaction and dissolution of the gas into the liquid. Thereafter, the gas-liquid mixture flows out from the outlet pipe passage 222 through the nozzle port 220. At this time, since the outflow conduit 822 is provided at a position lower than the inflow conduit 202, the gas-liquid mixture flow is stagnant inside the pressurized mixing flow passage 213. In addition, since the liquid is likely to flow out and the gas is hard to flow out, the gas is further delayed. For this reason, even if the ratio of the gas of the gas-liquid mixture flowing into the gas-liquid pressure mixer 212 is low, the ratio of the gas is high inside the gas-liquid pressure mixer 212.

Also in the gas-liquid dissolution mixing apparatus of this embodiment, the relationship between the total cross sectional area of each of the enlarged portion 210 and the nozzle port 220 at the connection portion of the gas inlet 208 may satisfy the following equation.

PA PG… … … … (One)

PA = (1-Sb / Sa ) Pl + (σP + Pb) Sb / Sa … … … (2)

PG is the pressure of the gas flowing from the gas inlet (8),

PA is the static pressure of the enlarged portion 210 at the connection portion of the gas inlet 208 given from Bernoulli's theorem of hydrodynamics and a continuous equation,

Sa is the cross-sectional area of the enlarged portion 210 at the connection portion of the gas inlet 208,

Sb is the total cross-sectional area of the nozzle port 220,

P1 denotes the total pressure of the enlarged portion 210 at the connection portion of the gas inlet 208,

sigma P is the pressure loss from the enlarged portion 210 to the nozzle 220 at the connection portion of the gas inlet 208,

Pb is the static pressure of the nozzle port 220.

As a result of the ozone drainage test using this device, the ozone consumption of injection ozone was 99.4% and very high ozone utilization efficiency was obtained. In addition, since the gas-liquid pressure mixer 212 of this embodiment forms the pressurized mixing flow path 213 in a box shape, gas-liquids are efficiently mixed with a simple structure, and the apparatus can also be made small.

[Example 9]

Next, a ninth embodiment of the present invention will be described.

As shown in FIG. 12, the mixer 204 of this embodiment is connected to the gas-liquid pressurizing mixer 212 via the conduit 244. As shown in FIG. Moreover, the nozzle port 220 can also be provided in the front-end | tip part or the middle of the outflow pipe path 222. In addition, the pressurized mixing flow path 213 of the gas-liquid pressure mixer 212 may be formed by bending a pipe such as a pipe, and may be such that the gas-liquid mixed flow flows through a flow path of a gradient which repeats the completion.

[Example 10]

Next, a tenth embodiment of the present invention will be described with reference to FIGS. 13 to 16. FIG.

In the gas-liquid dissolving mixer 310 which mixes gas, such as air, in liquid, such as water, the venturi tube 314 provided with the neck part 312 which forms an throttle part in the center part is formed.

In the enlarged portion 316 on the downstream side of the venturi tube 314, a gas inlet 318 is formed on the slightly downstream side of the neck portion 312 to mix air supplied from the outside into the flow path. The front end of the conduit 320 is connected to 318. On the downstream side of the enlarged portion 316, a pipe section 322, which is a mixing section for mixing the gas introduced from the gas inlet 318 and the liquid in the flow passage in a relatively pressurized state, and conveys the mixed gas and liquid, is connected. have. The pipe 322 may be a steel pipe or a flexible pipe, and its outer diameter can be arbitrarily set in consideration of the pressure difference between the neck portions 312, and is formed in a shape extending from the maximum diameter of the enlarged portion 316. It is. The nozzle part 326 in which the some nozzle port 324 was formed is provided in the front-end | tip of this pipeline 322. As shown in FIG.

As shown in FIG. 16, the gas-liquid mixing apparatus of this embodiment is a case where the gas-liquid mixing mixer 310 is installed on the vessel 330, floated on a lake, and used as a floating particle floating separator. By sucking the water 336 of the lake through the suction pipe 334 is fed to the gas-liquid mixer 310. Moreover, the nozzle part 326 provided in the front-end | tip of the pipe line 322 is settled in the lower layer part in the water in which the floating particle is distributed. The portion to be submerged in water may be not the nozzle portion 326 but a gas-liquid discharge portion extending from the nozzle portion 326 by using a steel pipe or a flexible pipe.

The operation of the floating particle floating separator using the gas-liquid mixing apparatus of this embodiment will be described next.

First, in order to form the gas-liquid mixture, the liquid introduced into the gas-liquid dissolving mixer 310 by the pump 332 through the suction pipe passage 334 is formed in the neck portion of the venturi tube 314. Accelerated at 312, the static pressure is once lowered, the flow velocity is slowed down via the enlarged portion 316, and the static pressure is increased again. At this time, the gas inlet 318 is slightly downstream of the neck portion 312, and since the positive pressure of this portion is relatively negative, gas is introduced into the flow path.

The gas introduced from the gas inlet 318 becomes a bubble and flows into the conduit 322 together with the liquid in the flow path, and since the positive pressure of the conduit 322 is higher than that of the neck 312, the liquid made of the gas becomes liquid. Dissolve in the stomach. Then, the liquid is injected together with the bubbles from the conduit 322 via the nozzle port 324. Since the liquid is accelerated again when passing through the nozzle port 324, the static pressure is lowered, and the gas dissolved in the liquid becomes a bubble having a small diameter of several micrometers to several hundred micrometers and is injected together with the liquid. Accordingly, the bubbles injected from the gas-liquid dissolving mixer 10 are dispersed in the water 336 of the lake as fine bubbles having a wide diameter of several micrometers to several hundred micrometers.

Bubbles released into the water 336 of the lake adhere to the floating particles 338, as shown in FIG. The bubbles adhering to the floating particles 338 are large and small respective sizes, and as shown in the figure, various bubbles from the relatively large bubbles 340 to the small bubbles 342 adhere to the floating particles 338. The floating particles 338 attached to the bubbles 340 and 342 quickly rise by the buoyancy force of the large bubbles 340 and rise near the surface of the water. As shown in FIG. 15, when the large bubble 340 reaches the water surface 344, the large bubble 340 is separated from the floating particles 338 and disappears into the atmosphere. However, since small bubbles 342 continue to adhere to the floating particles 338, they float for a long time directly under the water surface.

Experiment of floating the seaweed powder using the floating particle flotation separation device of this embodiment and observing it with a video microscope showed that the seaweed powder was stretched by a large bubble to quickly sleep. As a result, it was observed that the large bubbles fell and the blue seaweed powder particles were located directly below the water surface by the small bubbles adhering to the lower portion of the blue seaweed powder particles.

According to the floating particle flotation separation apparatus of this embodiment, since a wide range of bubbles can be generated in the water from a minute bubble to a relatively large bubble using the gas-liquid mixer 310, floating particles can be efficiently floated. In addition, since the floating particles can be reliably supported directly under the water surface, the floating particles can be efficiently removed.

[Example 11]

Next, an eleventh embodiment of the present invention will be described with reference to FIG.

Here, the same reference numerals are used for the same members as the above-described embodiment, and the description thereof is omitted.

In the floating particle flotation separation apparatus of this embodiment, the gas-liquid mixer 310 is installed on the land 346, and the nozzle portion 326 is positioned in the water through the pipeline 322. In addition, the nozzle unit 326 may be provided on the land or the water surface, and the pipe line may be connected to the front end thereof, and a discharge part for injecting the gas-liquid mixture liquid may be provided at the front end of the pipe line to be positioned in the water. It may be formed by any one of the tubes.

[Twelfth Example]

Next, a twelfth embodiment of the present invention will be described with reference to FIG. 18 and FIG.

Here, the same reference numerals are used for the same members as those of the tenth embodiment, and description thereof is omitted.

Floating particle floating separator of this embodiment, the mixing unit for mixing the liquid inlet 352, the pump 332, the neck 312, the enlarged portion 316 and the gas liquid in the body 350 that is submerged in water ( 354 is formed, and the nozzle hole 324 is formed in the front-end | tip of the mixing part 353. In addition, in the expanded portion 316, a gas inlet 318 is formed in which the gas suction pipe 356 is connected to an end portion, as in the above-described embodiment.

According to the floating particle floating separator of this embodiment, the whole apparatus can be formed compact. In addition, the gas suction pipe can be omitted by embedding the air cylinder in the main body 350. In addition, the floating particle flotation separation apparatus of this embodiment exits in the direction opposite to the injection direction due to the reaction caused by the injection of the gas-liquid mixture, so that the liquid can be sucked efficiently. Also, by attaching a rudder, it is possible to freely navigate in the water.

[Thirteenth Embodiment]

20 and 21 show a thirteenth embodiment of the present invention, and as shown in FIG. 20, the gas-liquid dissolving mixing apparatus of this embodiment includes a mixer 420 for mixing gas into a liquid. The tip of the liquid conduit not shown in the drawing is attached to the inlet 423 of the mixer 420. In the mixer 420, as shown in FIG. 20, the venturi tube-shaped flow path 424 provided with the neck part 422 which is an throttle part is formed in the center part. On the downstream side of the venturi tube-shaped flow path 424, a cylindrical gas inlet 427 having a larger inner diameter than the neck portion 422 is formed, and on the downstream side of the gas inlet 427 in a smooth tapered shape. The expanded enlarged portion 426 is formed. The gas inlet 427 is provided with a gas inlet 428 for mixing gas into the flow path 424. The gas inlet 428 is connected to the tip of the gas inlet pipe, which is not shown in the figure for guiding the predetermined gas. At this time, since the flow of the fluid ejected from the neck portion 422 expands in a trumpet shape after passing through the neck portion 422, the length of the gas inlet 427 is limited. That is, it can be said that the length from the neck 422 to the flow at a predetermined angle until the flow hits the wall of the gas inlet 427 is the maximum. Experimentally, as shown in FIG. 21, the relationship between the step (a) of the neck portion 422 and the gas inlet portion 427 and the flow (b) of the parallel portion is expressed by the following equation.

b9.5a

If it satisfies, it is determined that the gas is sucked in a stable state. A downstream side of the enlarged portion 426 is provided with a mixing portion 430 for mixing the gas introduced from the gas inlet 428 and the liquid in the flow path. The mixing part 430 can arbitrarily set the outer diameter according to the degree of pressurization, and is formed in the cylindrical shape of the inside diameter slightly wider than the maximum diameter of the expansion part 426 here. A nozzle 434 having a plurality of nozzle holes 432 is attached to the tip of the mixing unit 430. And the nozzle 434 is connected to the bottom part, such as a water tank in which the predetermined | prescribed liquid was accommodated, and the nozzle hole 432 is opened in the liquid.

Next, the operation of the gas-liquid dissolution mixing apparatus of this embodiment will be described below.

First, the liquid flowing into the inlet 423 of the mixer 420 is accelerated at the neck 422 of the venturi tube, and once the static pressure is lowered, passes through the gas inlet 427 and the enlarged portion 426 As the flow rate slows down, the static pressure rises again. At this time, the gas inlet 428 provided in the gas inlet 427 is directly downstream of the neck 422, and this part becomes a relatively negative pressure. Therefore, gas is introduced into the flow path from the gas inlet 428.

The gas introduced from the gas inlet 428 becomes a bubble and flows into the mixing section 430 together with the liquid in the flow path, and since the positive pressure of the mixing section 430 is higher than the neck portion 422, the gas is in the liquid. Dissolves. Then, the liquid is injected together with the bubbles from the mixing section 430 via the nozzle port 432. When gas-liquid mixture flows through the nozzle port 432, it accelerates again, and the static pressure becomes low, and the gas dissolved in the liquid precipitates as a fine bubble. In addition, the bubbles which have not been dissolved are also sprayed together with the liquid as small bubbles subdivided by the turbulent flow of the flow when accelerated by the nozzle port 432.

The relationship between the gas inlet part 427 of the mixer 420 of this embodiment and the total area of the nozzle port 432 of the nozzle 434 may satisfy the following formulas (1) and (2).

PP -------- (1)

P is the pressure of the gas flowing from the gas inlet 428,

P is the static pressure at the gas inlet 427 given by the following equation by the hydromechanical continuous equation and Bernoulli's theorem and the continuous equation.

PA = (1-S / S ) P + (δP + P) S / S ------(2)

S is the cross-sectional area of the gas inlet 427,

S is the sum of the total cross-sectional area of the nozzle port 432,

P is the sum of the entire gas inlet 427,

δP is the pressure loss from the gas inlet 427 to the nozzle port 432,

P is the static pressure at the outlet of the nozzle port 432.

Therefore, by setting the inner diameters of the gas inlet 427 and the nozzle port 432 to satisfy the above formulas (1) and (2), an optimum condition for efficiently mixing and dissolving the gas in the liquid can be obtained. It can be. The mixing section 430 is more preferable as long as it can obtain the contact time of the gas liquid until the gas is dissolved and saturated in the liquid under pressure, and the contact time of the gas liquid is related to the volume of the mixing section. The longer the part is, the longer the gas dissolves to the saturation point.

According to the gas-liquid dissolution mixing apparatus of this embodiment, the mixing flow rate of the mixing section 430 was 160 liters / minute. there was. Therefore, it became clear that the treatment flow rate increased dramatically compared with the conventional case.

[Example 14]

Next, a fourteenth embodiment of the present invention will be described with reference to FIG.

Here, the same members as those in the above embodiment use the same reference numerals, and the description thereof will be omitted. The gas-liquid dissolution mixing apparatus of this embodiment is the mixing portion of the thirteenth embodiment described above, and as shown in FIG. 22, a gas-liquid mixing tank 440 is provided which forms a flow path 438 in which liquid flows from top to bottom. It is. Therefore, the mixer 420 is attached to the inlet part of the flow path 438, and the nozzle 444 is provided through the outlet pipe line 443 of the flow path 438.

The gas-liquid mixing tank 440 of this embodiment is provided with a flow path 438 in which liquid flows from the top to the bottom step by step while repeating the completion of the gas-liquid mixture, so that the gas-liquid mixture flows through the flow path 438. In this case, a gas flows on the upper portion and a liquid flows on the lower portion, whereby a flow having a large contact area of the gas liquid can be obtained. Then, the nozzle 444 is provided at the tip of the conduit 443 of the outlet portion of the flow path 438 which flows down from the top step by step while repeating the completion, thereby increasing the static pressure inside the flow path 438 and reacting the gas-liquid reaction. It is to increase the dissolution efficiency. In addition, since the position of the outlet pipe path 443 at the outlet is lower than that of the inlet pipe inlet of the gas-liquid mixture, the gas-liquid mixture is stagnant in the flow path 438. In addition, in the flow path 438, Since the liquid having a higher density is easier to flow out than the gas, the gas is stagnated more in the flow passage 438 than in the liquid, and at the inflow stage, even if the ratio of the gas is relatively low, the ratio of the gas in the flow passage 438 is low. This becomes high. Therefore, gas dissolution may be efficiently performed in the gas-liquid mixing tank 440.

[Example 15]

Next, a fifteenth embodiment of the present invention will be described with reference to FIGS. 23, 24 and 25. FIG.

Here, the same reference numerals are used for the same members as those of the thirteenth embodiment, and the description thereof is omitted. In this embodiment, in order to obtain only finer bubbles, bubbles which are not dissolved in the mixing section are not sheared at the nozzle port 432 of the nozzle 434 but upwardly from the branch point 445 immediately preceding the nozzle 434. It discharges to the outside as a surplus gas from the branch path 446 provided toward the outside. Thereby, since only the bubble which precipitated can be discharge | released in a liquid, only the liquid which has a finer bubble can be manufactured.

In addition, an intermediate tank 450 is provided between the pipes 447 and 448 through which the gas-liquid mixture flows from the mixer. The pipes 447 and 448 also serve as mixing portions, and may be steel pipes or flexible pipes, and the gas and liquid are more efficiently mixed when the flow becomes turbulent, so that the pipes are set in a spiral shape or The Reynolds number may be set to a condition that is higher than the value that becomes turbulent.

As another example of the mixer, the enlarged portion 456 of the mixer 460 is formed stepwise. As a result, the processing of the gas inlet 427 and the enlarged portion 456 becomes extremely easy, resulting in more efficient production. The number of stages of the enlarged portion 456 can be set arbitrarily, and at least one stage may be formed at least up to the mixing portion 430. The stepped portions of the enlarged portion 456 and the gas inflow portion 427 which are enlarged in stages may be formed on the inclined surface at a predetermined angle.

The gas-liquid dissolving mixing apparatus of the present invention can form fine bubbles continuously and efficiently with a simple apparatus, and thus it is possible to obtain a high pressure and a high suction state of the gas drawn into the liquid. The processing capacity can also be several times higher than that of the conventional one. Moreover, also in manufacture of an apparatus, it is a structure with which processing of a mixer is easy.

[Example 16]

Next, a sixteenth embodiment of the present invention will be described with reference to FIGS. 26, 27, and 28. FIG. The present invention relates to an embodiment of a gas-liquid pressurization device capable of separating excess gas, and includes a flow path 512 stepwise flowing from the top to the bottom of the inlet 510 through which the gas-liquid mixture flow fed by a pump or the like is introduced. It is. The gas separation flow passage 516 protruding upward from the end portion of the flow passage 512 flowing down from the top in this step is formed at the branch point 514. A flow passage 518 through which the gas-liquid mixture flows is connected to the outlet 511 of the downstream flow passage 512 of the branch point 514, and the throttle nozzle 20 is connected to the proximal end of the flow passage 518. ) Is installed.

In addition, behind the outlet 526 of the gas separation passage 516, the throttle part 528 and the solenoid valve 530 are connected, and capacitive proximity sensors 522 and 524 are disposed on the side of the gas separation passage 516. have. When a harmful gas is used in the gas discharge line 531 in which the solenoid valve 530 is installed, a gas treatment apparatus, for example, an ozone treatment apparatus or the like, which is not shown in the drawing is connected to process the discharged gas.

In the operation of the gas-liquid pressure mixing apparatus of this embodiment, first, when the gas-liquid mixture flow 515 pressurized to a predetermined pressure from the inlet 510 into the flow path 512, the gas flow 532 inside the flow path 512. ) And liquids 534. And the inside of the flow path 512 is pressurized by the throttling nozzle 520 of the base end part of the flow path 518 connected to the outlet 511 of the flow path 512. At this time, the relationship between the pressurization and the throttle nozzle 520 is given by the following equation in the theorem of the case when the size of the inside of the flow path 512 is sufficiently large.

P = ρu /2

P: pressure in the flow path 512

ρ: density of the liquid

u: flow velocity in the throttle nozzle 20

In addition, the flow branched from the branch point 514 flows liquid and gas into the gas separation flow path 516, the liquid having a high specific gravity stays below, and the gas flows upward of the gas separation flow path 516. In the gas separation passage 516, the inner diameters of the throttle nozzle 520 and the throttle portion 528 are adjusted such that the liquid level is approximately located between the sensors 522 and 524. When the liquid level rises to the position of the sensor 524 against the fluctuation of the liquid level, as shown in FIG. 27, the sensors 522 and 524 are also turned on, and the solenoid valve 530 is shut off. As a result, the discharge of the gas is stopped, the gas is filled above the gas separation passage 516, and the liquid level is lowered. When the liquid level is lowered below the sensor 522, the sensors 522 and 524 are both turned OFF to open the solenoid valve 530, and the liquid level starts to rise in the gas separation passage 516 again. In this way, excess gas is discharged to the outside from the gas separation passage 516, and only the liquid in which the gas is dissolved flows into the flow passage 518.

In the excess gas separation type gas-liquid pressure reactor of this embodiment, a large contact area can be obtained between the pressurized gas and the liquid, so that gas reaction or gas dissolution to the liquid can be performed very well. . In addition, since the outlet 511 is provided at a position lower than the inlet 510 in the passage 512, the liquids 34 in the gas-liquid mixture flow more easily downward, and the gas flow 32 is a passage. Since the state becomes stagnant in the upper portion of 512, even if the proportion of gas in the gas-liquid mixture flowing into the excess gas separation type gas-liquid pressure reactor is small, the proportion of gas in the apparatus becomes large. As a result, even a small amount of gas can efficiently perform gas-liquid reaction or gas dissolution to the liquid. The excess gas is separated from the gas separation passage 516 as it is under pressure, and the liquid in which gas is dissolved is pumped into the flow path 518 under pressure.

According to the excess gas separation type gas-liquid pressure reactor of this embodiment, the sprinkling and feeding of the liquid generated by the gas-liquid reaction can be performed without a pump for the spraying and feeding.

In this case, the excess gas separation type gas-liquid pressure reactor of this embodiment can be injected into the flow path 512 separately from gas and liquid. In this case, at least gas is pressurized to a predetermined pressure and injected. In addition, the attachment position of the throttle nozzle 520 can be provided immediately after the excess gas separation type gas-liquid pressurization apparatus, and can also be provided downstream of the outflow 511. In addition, the throttle nozzle 520 may be provided with one hole as shown in FIG. 26, may be provided with a plurality of holes, and a pressure regulating valve or the like may be provided instead of the throttle nozzle 520 to provide pressure. It can also be variable. In addition, the setting of this flow path 512 does not necessarily need to make the formation surface of the flow path 512 horizontal and vertical, and may make it incline. It is also possible to bend the pipe. In addition, as long as the condition that the outlet 511 is lower than the inlet 510 is satisfied, the intermediate part of the flow path 512 may be raised. In addition, the throttling nozzle 520 can be substituted for the throttling of the sprinkling portion such as the sprinkler. In addition, in FIG. 26, you may arrange | position the throttle part 528 and the solenoid valve 530 in the gas discharge line 531. FIG. Instead of the throttle 528, a pressure regulating valve or the like may be used.

28, the gas-liquid mixer shown in the thirteenth embodiment may be attached to the inlet 510 for use. As shown in FIG. 28, this gas-liquid mixer 542 is provided with the venturi tube-shaped flow path 545 in which the neck part 546 which is an throttling part is provided in the center part in the mixer 542. As shown in FIG. On the downstream side of the venturi tube-shaped flow path 545, a cylindrical gas inflow portion 547 having an inner diameter slightly larger than that of the neck portion 546 is formed, and a tapered shape is smoothly downstream of the gas inflow portion 547. An enlarged portion 548 is enlarged to be formed. The gas inlet 547 is provided with a gas inlet 550 for mixing gas into the passage 545. The gas inlet 550 is connected to a tip of a gas inlet pipe not shown in the drawing to guide a predetermined gas. As a result, since the gas-liquid dissolution reaction can be obtained more efficiently, a large amount of gaseous solution can be produced.

The sensor of this embodiment may detect only the upper limit of the liquid level, shut off the solenoid valve in accordance with the upper limit detection of the liquid level, and open the solenoid valve after a predetermined time has elapsed, or the lower limit of the liquid level. By detecting only the bay, the solenoid valve may be opened in accordance with the detection of the lower limit of the liquid level, and then the solenoid valve may be shut off at a predetermined time week. The solenoid valve may be a combination of the throttle portion and the solenoid valve provided on the tip side of the gas separation flow path.

[Example 17]

Next, a seventeenth embodiment of the present invention will be described with reference to FIGS. 29 to 34. FIG. This example shows an example of an apparatus for producing microcellular granules using the gas-liquid dissolving mixing apparatus of the present invention. As shown in FIG. 29, the apparatus for producing microcellular granules of this example includes a mixer for mixing gas into a liquid ( 610, and the tip of the liquid conduit 611 is attached to the inlet 613 of the mixer 610. In the mixer 610, as shown in FIG. 30, the venturi tube-shaped flow path 614 in which the neck part 612 which is a throttle part is provided in the center part is formed. An enlarged portion 616 is formed on the downstream side of the venturi tube-shaped flow path 614, and a gas flow in a cylindrical shape is slightly larger than the neck portion 612 between the neck portion 612 and the enlarged portion 616. A portion 617 is formed, and a gas inlet 618 is formed in the gas inlet 617 to mix gas into the flow path 614. The gas inlet 618 is connected to a tip end portion of the gas inlet pipe 619 for guiding a predetermined gas.

On the downstream side of the enlarged portion 616, a mixing portion 620 for mixing the gas introduced from the gas inlet 618 and the liquid in the flow path is provided. The mixing part 620 can set the outer diameter arbitrarily according to the degree of pressurization, and is formed in the cylindrical shape of the inner diameter slightly wider than the maximum diameter of the expansion part 616 here. The nozzle part 624 in which the some nozzle port 622 was formed in the front-end | tip of this mixing part 620 is provided. And the nozzle part 624 is connected to the bottom of the water tank 628 which is the liquid accommodation member in which the predetermined | prescribed liquid 626 was accommodated, and the nozzle hole 622 is open in the liquid 626.

Next, the action of the microcellular powder production method and microcellular powder production apparatus of this embodiment will be described below.

First, the liquid flowing from the liquid conduit 611 into the inlet 613 of the mixer 610 is accelerated at the neck 612 of the flow path 614, so that the static pressure is lowered once as in the above-described embodiment, and the enlarged part Via 616, the flow velocity is slowed down and static pressure rises again.

At this time, gas is absorbed from the gas inlet 618 to the gas inlet 617 of the flow path 614.

The gas inlet portion 617 in which the gas inlet 618 is formed is downstream from the neck portion 612 and slightly larger in diameter than the neck portion 612. Therefore, since it is lower than the mixing part 620 and becomes negative pressure, gas flows into the flow path 614. The opening of the gas inlet 618 at the neck portion 612 at which the static pressure becomes the lowest is the portion where the neck portion 612 is the lowest in the static pressure, but the gas inlet 668 is held at the neck portion 612. This is because when the gas is opened, the inflow of gas is not good, and the side of the portion where the flow path begins to expand slightly tends to flow.

The gas introduced from the gas inlet 618 flows into the mixing unit 620 together with the liquid in the flow path 614, and the bubbled gas has a positive pressure of the mixing unit 620 than the neck 612. Because it is high, it dissolves in liquid. Then, the liquid in which gas is dissolved together with the bubbles is injected into the liquid 626 of the water tank 628 from the mixing unit 620 via the nozzle port 622. When this gas-liquid mixture flows through the nozzle port 622, since the liquid is accelerated again, the static pressure is lowered, and the gas dissolved in the liquid is precipitated into fine bubbles. In addition, bubbles which are not dissolved also become fine bubbles while being subdivided by turbulent flow or the like when they are accelerated by the nozzle port 422, and are injected together with the liquid. In the liquid 626 in the water tank 628, these fine bubbles rise by the buoyancy of the liquid 626 toward the water surface 630 to form a layer of fine foam 632 on the water surface 630. .

The mixing portion 620 is more preferable as long as it can obtain the contact time of the gas liquid until the gas is dissolved and saturated in the liquid under pressure, and the contact time of the gas liquid is related to the volume of the mixing portion, and therefore the length of the mixing portion. The longer the gas is dissolved to the saturation point. In addition, when foaming a liquid containing a surfactant, such as milk, the microcellular powder production apparatus can be used, and as a result of the foaming experiment with the microcellular powder production apparatus using milk, the surface of milk A layer of fine foams of several cm was formed. Moreover, when a to-be-foamed liquid is a property which is difficult to hold | maintain foam, you may add a suitable surfactant to a to-be-foamed liquid. For example, when a small amount of a detergent commercially available as a surfactant was added to the water and tested, a fine foam layer larger than about 2 cm was formed on the surface of the water. Moreover, when the kind of detergent is changed, the layer of fine foam of several tens of cm or more may be formed, What is necessary is just to select the kind of surfactant according to a use.

According to the microcellular powder production method and apparatus of this embodiment, the microcellular powder by any gas can be continuously and efficiently formed, and the maintenance of the mixer 610 is also easy. In particular, in the mixer 610 of this embodiment, since the gas inflow portion 617 is formed parallel to the cylindrical flow, the inflow of the gas is stably performed, and the gas can be dissolved and mixed more efficiently.

In the mixer of this embodiment, like the mixer 640 shown in the first embodiment and FIG. 31, the gas inlet 627 may be used at a portion upstream of the enlarged portion 616. .

In addition, as in the mixer 650 shown in FIG. 32, bubbles which have not been dissolved in the mixing unit 620 in order to obtain finer foam are not sheared by the nozzle port 622 of the nozzle 624, and surplus gas is used. As an alternative, the gas may be discharged from the excess gas discharge port 652 which is a branch flow path provided in front of the nozzle 624. The excess gas discharge port 652 is formed in the upper part of the mixing part 620 because the gas is located in the upper part in the mixing part 620. Therefore, only finer foam can be produced. In addition, as in the mixer 660 shown in FIG. 33, a plurality of nozzles 624 are provided in one mixer 610 via a conduit 62, and the plurality of nozzles 624 are connected to the water tank 628. It may be opened from the lower side. The conduit 662 also serves as a gas-liquid mixing section, and may be a steel pipe or a flexible conduit, or the gas and liquid are more efficiently mixed with the flow turbulent, so that the conduit 62 is spiraled or The Reynolds number may be set to a condition that is higher than the value that becomes turbulent.

In addition, as shown in the sixteenth embodiment and FIG. 34, the gas-liquid mixing tank 670 in which the flow path 672 flows from top to bottom may be provided. As a result, an inflow pipe 676 at the inlet of the flow path 672 is formed with a flow path (not shown in the drawing) and a gas inlet connected immediately after the throttle portion of the flow path, and an outlet pipe path at the outlet of the flow path 672 ( A nozzle not shown in the figure is provided at the tip of 674.

In the gas-liquid mixing tank 670 of this embodiment, there is a flow path 672 in which the liquid is directed from top to bottom while repeating the completion of the gas-liquid mixing tank 670. A gas flows in the upper part of the flow path 672, and a liquid flows in the lower part of the flow path 672, so that a wide contact area of the gas liquid can be obtained. Then, a nozzle as a throttling portion is provided in the outflow conduit 674 of the outlet of the flow passage 672 flowing down from the top step by step while repeating the completion, thereby increasing the static pressure inside the flow passage and increasing the reaction and dissolution efficiency of the gas liquid. will be. In addition, since the position of the outlet pipe path 674 at the outlet is lower than the inlet of the inlet pipe 676 of the gas-liquid mixture flow, the gas-liquid mixture flow is stagnant in the flow path 672. Since the liquid having a higher density is more easily discharged than the gas, the gas is more stagnated in the flow path 672 than the liquid. Therefore, at the stage of the inlet pipe 676, even in a case where the proportion of gas is relatively low, the flow path 672 is less. The ratio of gas becomes high.

In addition to the case where it is used as it is, the microcellular malt prepared by the microcellular malformation apparatus of this embodiment may be dried, frozen or sintered to be solidified, and may be used by solidifying with a coagulant.

In addition, the gas-liquid dissolution mixing apparatus of the present invention can be used not only for bubble generation but also as an apparatus for dissolving gas into a liquid. The throttle portion may be formed by a venturi tube, or may be rapidly throttled into an orifice shape, and the shape is not limited. Moreover, the shape of a nozzle part and the number of nozzle openings can also be set suitably according to predetermined conditions.

The gas-liquid dissolving mixing method and gas-liquid mixing apparatus of the present invention can be used as an apparatus for producing ozone water or dissolving gas such as ozone in wastewater to treat wastewater, or a device for mass dispersing bubbles in liquid. Compared with the conventional gas-liquid dissolution mixing device, the gas can be dissolved in the liquid very efficiently or bubbles can be formed in the liquid. In addition, it can be used as a device for dispersing fine bubbles in water to float floating particles in water, for example, to remove ink particles, pigment particles in paint, or ink in the process of manufacturing recycled paper. Available. Moreover, you may mix chemical | medicinal agents, such as a flocculant, surfactant for neutralization, and a neutralizer, with a bubble in a liquid. These drugs may be sucked together with the gas into the liquid using a gas supply line. Moreover, in order to inject a chemical | medical agent, you may provide multiple gas inlet, chemical | medical agent inlet, etc.

The gas-liquid dissolution mixing device of the present invention is a simple device, and can efficiently form fine bubbles in a stable state continuously, so that the maximum processing flow rate can also be several times higher than that of the conventional one. Moreover, also in manufacture of an apparatus, it is a structure which is easy to process a mixer.

Claims (31)

A part of the liquid flow path is throttled, the pipe is gradually enlarged on the downstream side of the throttle, a gas is introduced in a slightly downstream side of the throttle, and the gas and the liquid are mixed on the downstream side of the enlarged portion. And a gas-liquid mixture mixing method, wherein the gas-liquid mixed stream is ejected from the nozzle unit provided at the outlet. By throttling a part of the flow path, the flow path is gradually expanded on the downstream side of the throttle part, and gas is introduced from the slightly downstream side of the throttle part to form a gas-liquid mixture flow, and the nozzle is provided downstream of the flow path. The pressure in the flow path upstream of the nozzle is increased, the gas is dissolved in the liquid in the flow path, and the gas-liquid mixture in which the gas is dissolved is passed through the nozzle to depressurize, and the gas-liquid mixture containing the fine bubbles is formed. The foam is released into the liquid in the liquid accommodating member, so that the pressurized dissolved gas is precipitated in the form of fine bubbles, and the fine bubbles are raised in the liquid of the liquid accommodating member, thereby raising the fine foam on the upper surface of the liquid in the liquid accommodating member. Gas-liquid dissolution mixing method, characterized in that to form a layer. The throttle part 12 provided in the liquid flow path, the enlarged part 16 connected to this throttle part 12, and the cross section expanded gradually, and the enlarged part 16 slightly downstream of the said throttle part 12. A mixing section 20 installed downstream of the gas inlet 18 and the enlarged section 16 to mix the gas in the flow path and the gas introduced from the gas inlet 18, and the outlet of the mixing section 20. A gas-liquid dissolution mixing device comprising a nozzle portion 24 provided. A gas inlet portion 427 and a gas inlet portion 427 which are connected to the throttle portion 422 provided in the flow path, and which are continuous with the throttle portion 422 and whose inner diameter is slightly larger than that of the throttle portion 422 and have a constant cross-sectional area. And an enlarged portion 426 extending in the flow path toward the downstream side and a gas inlet 428 provided in the gas inlet portion 427 and downstream of the enlarged portion 426. Gas-dissolving mixing, comprising a mixing unit 430 for mixing the liquid in the inside and the gas introduced from the gas inlet 428 and a nozzle unit 434 provided at the outlet side of the mixing unit 430. Device. The gas-liquid dissolution mixing apparatus according to claim 3, wherein a plurality of nozzle holes are formed in the nozzle unit. 4. The gas-liquid dissolving and mixing device according to claim 3, wherein the nozzle unit injects bubbles of several micrometers to several micrometers in the liquid in which the floating particles are present. The gas-liquid dissolution mixing apparatus according to claim 3, wherein the throttling portion and the nozzle portion are connected in a conduit serving as a mixing portion. And a liquid supply part 30 for delivering a liquid dissolving gas at a predetermined pressure. The mixer 10 which mixes the liquid pressurized from this liquid supply part 30, and predetermined | prescribed gas is provided, In this mixer 10, the throttle part 12 provided in the liquid flow path, and this throttle part 12 An enlarged portion 16 which is continuously extended from the gas inlet 18 and the above-described axial portion 12, which is provided slightly downstream of the pipe line, and is provided downstream of the enlarged portion 16, The mixer 10 which mixes the gas which flowed in from the said gas inlet 81, and the nozzle part 24 provided in the outlet of this mixing part 20 are installed in the said mixer 10, and said mixer The gas supply part 44 is connected to the gas inlet 18 of 10, and the nozzle part 24 of the said mixer 10 is connected, and the liquid which gas melt | dissolved in the said mixing part 20 flows in into. Gas-liquid dissolution mixing device, characterized in that the liquid receiving portion 38 is provided. 9. The mixer (10) according to claim 8, wherein the mixer (10) is composed of a main body portion (52) provided with a throttle portion (12) and the nozzle portion (54). A gas-dissolving mixing device, characterized in that the main body portion (52) and the nozzle portion (54) are connected in a conduit (56) serving as a mixing portion (20). A first throttle part 120 having a small cross-sectional area of the flow path is provided in a part of the gas flow path. An enlarged portion 122 which is continuous from the first throttle portion 120 and gradually expands in the downstream side is formed, and a gas inlet (3) is provided in the enlarged portion 122 slightly downstream of the first throttle portion 120. 123 is provided, and a mixing section 124 is provided downstream of the expansion section 122 for mixing the liquid in the flow path and the gas introduced from the gas inlet 123, and the downstream side of the mixing section 124. Connecting the liquid conduit 113 to the liquid conduit 113, providing a nozzle section 115 having a plurality of nozzle holes 117 at the distal end of the liquid conduit 113, and the cross-sectional area of the flow path immediately before the nozzle section 115. A gas-liquid dissolution mixing device, characterized in that the second throttle portion 130 is made smaller. 11. The nozzle unit (15) according to claim 10, wherein a plurality of nozzle holes (117) are formed in the nozzle unit (15), and the nozzle unit (115) is formed by a flexible conduit (134) formed of a liquid conduit provided at the tip end. Gas-liquid dissolution mixing device. A first throttle part 120 having a small cross-sectional area of the flow path is provided in a part of the gas flow path, and an enlarged part 122 which is continuously extended from the throttle part 120 and gradually enlarged to the downstream side is formed. A gas inlet 123 is provided in the enlarged portion 122 slightly downstream of the shaft portion 120 to mix the gas introduced from the gas inlet 123 and the liquid in the flow path downstream of the enlarged portion 122. The part 124 is provided, the liquid conduit 134 which has the branch point 133 is connected downstream of this mixing part 124, and the nozzle part 115 is provided in the downstream side of this branch point 133, respectively. And a second throttle portion (130) having a small cross-sectional area of the flow path immediately before the branch point (133). The nozzle part 115 is formed with a plurality of nozzle holes 117, characterized in that the nozzle part 115 is formed by a flexible conduit 134, the liquid conduit provided in the tip portion. Gas-liquid dissolution mixing device. The throttle part 206 which throttled a part of the fluid flow path, and the enlarged part 210 which enlarged the pipeline gradually in the downstream of this throttle part 206 are provided, and is slightly downstream of the throttle part 206 mentioned above. A gas inlet 226 is formed to introduce gas, and a pressurized mixing flow path 213 is formed on the downstream side of the enlarged part 210 to repeat the salary, and fluid flows from the top to the bottom. A gas-liquid dissolving mixing apparatus, characterized in that the nozzle port 220 is provided at the outlet or downstream of the pressure mixing flow passage (213). The intermediate bridge in the pressure mixing flow path 213 according to claim 14, wherein an intermediate throttling portion 216 having a larger cross-sectional area is provided in the middle of the pressure mixing flow path 213 as compared with the nozzle hole 220. A gas-liquid dissolution mixing device, characterized in that a pressure measuring device (250) is provided for measuring the pressure of at least an outlet side of the shaft portion (216). The gas-liquid dissolution mixing apparatus according to claim 3, wherein the enlarged portion is formed in a tapered shape in which the flow path is smooth. 4. The gas-liquid dissolving and mixing apparatus according to claim 3, wherein said enlarged portion has a passage formed stepwise, and its inner diameter is largely formed toward the downstream side. A flow path 512, which is pressurized in a flow path formed by repeated grades, or in which a high-speed gas-liquid mixture flows, is provided, protrudes above the flow path 512, and branches off from the gas flow path to separate surplus gas. Forming a gas separation flow path 516, and equipped with sensors 522 and 524 for detecting a liquid level in the gas separation flow path 516 at a predetermined position of the gas separation flow path 516, and the gas separation flow path 516 described above. The solenoid valve 530 is provided on the front end side of the throttling unit 528 and the sensor 522.524, and the throttling nozzle 520 is provided downstream of the gas passage at the branch point. Extra gas separation type gas-liquid dissolving mixing apparatus. 20. The gas-liquid dissolution mixing device according to claim 18, wherein the sensors (522, 524) detect at least one of at least an upper limit or a lower limit of the liquid level in the gas separation passage (516). The gas-liquid dissolution mixing apparatus according to claim 4, wherein a plurality of nozzle holes are formed in the nozzle unit. The gas-liquid dissolution mixing apparatus according to claim 4, wherein the throttling portion and the nozzle portion are connected in a conduit serving as a mixing portion. The gas-liquid dissolution mixing device according to claim 4, wherein the enlarged portion is formed in a tapered shape in which the flow path is smooth. The gas-liquid dissolving and mixing apparatus according to claim 8, wherein the enlarged portion is formed in a tapered shape with a smooth flow path. The gas-liquid dissolution mixing device according to claim 10, wherein the enlarged portion is formed in a tapered shape in which the flow path is smooth. The gas-liquid dissolution mixing device according to claim 12, wherein the enlarged portion is formed in a tapered shape in which the flow path is smooth. The gas-liquid dissolution mixing apparatus according to claim 14, wherein the enlarged portion is formed in a tapered shape in which the flow path is smooth. 5. The gas-liquid dissolving and mixing apparatus according to claim 4, wherein said enlarged portion has a passage formed stepwise, and its inner diameter is formed large toward the downstream side. 9. The gas-liquid dissolving and mixing apparatus according to claim 8, wherein the enlarged portion has a passage formed stepwise, and its inner diameter is formed large toward the downstream side. The gas-liquid dissolution mixing apparatus according to claim 10, wherein the enlarged portion has a passage formed in steps, and its inner diameter is largely formed toward the downstream side. 13. The gas-liquid dissolving and mixing apparatus according to claim 12, wherein said enlarged portion has a passage formed stepwise, and its inner diameter is formed large toward the downstream side. 15. The gas-liquid dissolving and mixing apparatus according to claim 14, wherein said enlarged portion has a passage formed stepwise, and its inner diameter is formed large toward the downstream side.